rekind a.1 reva

TECH. RESEARCH & DEVELOPMENT DEPARTMENT

PROYEK STUDI KELAYAKAN DAN PERENCANAAN ROADMAP DAN STRATEGI PENELITIAN DAN PENGEMBANGAN BIOETANOL BERBAHAN BAKU LIGNOSELULOSA

Kajian Paten dan Lisensi

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RANCANGAN KONSEPTUAL PROSES DAN PABRIK BIOETANOLKAJIAN PATEN DAN LISENSI TEKNOLOGI

APPROVAL BOX

AIssued for Comment

C.B. Rasrendra/Stephanie

Sutoko

M.T.A. Penia Kresnowati

Ronny Purwadi

REVSTATUS

REVISI

Prepared By Checked By Approved By Reviewed By Approved By

Peneliti PenelitiPeneliti Utama

TRD Engineer

Sr. Mgr. TRD

APPROVAL KONSULTAN APPROVAL REKIND

REVISION RECORD

Rev Status Revisi Tanggal Terbit Deskripsi

A Issue for Review 13 Agustus 2012 Initial Release

DISTRIBUTION LIST

1. Yayasan LAPI-ITB

CONTROLLED COPY, DO NOT DUPLICATE For Internal Use Only




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RIWAYAT PERUBAHAN DOKUMEN

Rev Tanggal Deskripsi Perubahan





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DAFTAR ISI

EXECUTIVE SUMMARY........................................................................................61. PENDAHULUAN............................................................................................7

1.1.Latar Belakang......................................................................................7

1.2.Tujuan...................................................................................................7

1.3.Ruang Lingkup......................................................................................8

2. STUDI PUSTAKA...........................................................................................92.1.Biomass Lignosellulosa.........................................................................9

2.1.1. Selulosa..........................................................................................92.1.2. Hemiselulosa................................................................................102.1.3. Lignin............................................................................................112.1.4. Jenis dan Tipikal Komposisi Biomassa Lignoselulosa....................122.2.Proses Produksi Bioetanol Lignoselulosa.............................................13

2.3.Perbandingan Proses Produksi Bioetanol Lignoselulosa dengan Bioetanol Generasi Pertama......................................................................15

2.4.Produksi Bioetanol Lignoselulosa........................................................16

2.4.1. Perlakuan Awal (Pretreatment).....................................................162.4.2. Sakarifikasi...................................................................................212.4.3. Hidrolisis Asam.............................................................................212.4.4. Hidrolisis Enzimatik.......................................................................222.4.5. Perbandingan Hidrolisis Asam dan Enzimatik...............................222.5.Fermentasi..........................................................................................23

2.5.1. Mikroorganisme untuk Fermentasi Biomassa Lignoselulosa Menjadi Etanol 232.5.2. Teknologi Fermentasi...................................................................262.6.Pemisahan dan Pemurnian..................................................................29

2.7.Pemanfaatan Produk Samping............................................................29

3. METODOLOGI............................................................................................304. HASIL DAN PEMBAHASAN..........................................................................30

4.1.Teknologi Proses Produksi Bioetanol Lignoselulosa dan Status Pengembangannya...................................................................................30

4.1.1. Status Pengembangan dan Komersialisasi...................................304.1.2. Bahan Baku dan Perlakuan Awal..................................................324.1.3. Metoda Sakarifikasi: Hidrolisis asam encer...................................324.1.4. Hidrolisis Enzimatik.......................................................................334.1.5. Fermentasi....................................................................................334.1.6. Proses Integrasi............................................................................34





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4.2.Perbandingan Teknologi Produksi Bioetanol Lignoselulosa.................34

5. KESIMPULAN DAN SARAN..........................................................................415.1.KESIMPULAN........................................................................................41

5.2.SARAN.................................................................................................41

6. DAFTAR PUSTAKA......................................................................................427. LAMPIRAN..................................................................................................43LAMPIRAN – 1...................................................................................................44

ABENGOA..................................................................................................44

AE BIOFUELS (AEMETIS)............................................................................50

AMERICAN PROCESS.................................................................................51

ARKENOL – BLUE FIRE ETHANOL...............................................................55

BBI BIO VENTURES LLC.............................................................................60

BIOGASOL.................................................................................................61

BLUE SUGARS (d.h KL ENERGY)................................................................66

BORREGAARD...........................................................................................69

CHEMTEX – PROESA - MGM.......................................................................73

DEDINI.......................................................................................................75

DuPONT Danisco Cellulosic Ethanol (DDCE)..............................................77

FUTUROL PROCETHOL...............................................................................80

GREEN FIELD ETHANOL.............................................................................83

INBICON....................................................................................................86

IOGEN........................................................................................................90

LIGNOL......................................................................................................96

MASCOMA (SunOpta)................................................................................99

METSA BOARD (d.h. M-REAL-HALEIM AG)................................................100

PACIFIC ETHANOL....................................................................................102

POET-DSM...............................................................................................105

QTEROS...................................................................................................112

SEKAB.....................................................................................................114

SUD CHEMIE (SUN LIQUIDS)....................................................................117

VERENIUM...............................................................................................120

WEYLAND AS...........................................................................................122

ZEACHEM................................................................................................123





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LAMPIRAN – 2.................................................................................................126INDONESIA..............................................................................................126

CHINA......................................................................................................127

JEPANG....................................................................................................129

THAILAND................................................................................................130

MALAYSIA................................................................................................131

VIETNAM..................................................................................................132

1. PENDAHULUAN

1.1. Latar Belakang

Bioetanol lignoselulosa, sering disebut sebagai bioetanol generasi kedua, diidentifikasi sebagai

salah satu bahan bakar nabati yang atraktif dari sumber terbarukan. Hal ini didukung oleh

keberadaan biomassa lignoselulosa yang melimpah dan tidak berkompetisi dengan bahan

pangan. Pengembangan teknologi dan proses untuk komersialisasi bioetanol lignoselulosa

menjadi perhatian kalangan ilmuwan, praktisi, dan pelaku industri bioetanol pada dasawarsa ini.

Meskipun bioetanol generasi pertama yang berbahan baku tetes tebu (molase) dan pati telah

berhasil diproduksi pada skala komersial dari pada dekade 1970, hingga saat ini (2012) skala

komersial bioetanol lignoselulosa belum tersedia. Namun demikian, pengembangan proses

produksi bioetanol lignoselulosa pada skala pilot dan demonstrasi telah tersedia. Beberapa

pengembang teknologi telah mencanangkan dan berproses untuk membuat produksi bioetanol

lignoselulosa skala komersial pertama di dunia pada periode 2013.

Selaras dengan upaya untuk mengoversi bahan baku lignoselulosa lokal Indonesia menjadi

bioetanol dengan teknologi milik sendiri, paparan pada laporan ini menyampaikan tahapan proses

produksi bioetanol lignoselulsa, pilihan-pilihan teknologi yang tersedia termasuk perbandingan

keunggulan dan kekurangannya, dan ulasan status dan teknologi proses bioetanol lignoselulosa

yang telah dan akan dikembangkan untuk mencapai skala produksi komersial.

1.2. Tujuan

Laporan ini bertujuan untuk menyajikan perkembangan terkini (state of the art) teknologi bioetanol

lignoselulosa secara terperinci. Hasil dari kajian ini akan digunakan sebagai basis pemilihan





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teknologi dan penyusunan ugeran-ugeran untuk studi rancangan konseptual dan perancangan

pabrik bioetanol lignoselulosa.

1.3. Ruang Lingkup

Ruang lingkup laporan ini adalah:

1. Laporan kajian pustaka mengenai state of the art dan kajian komprehensif paten-paten

teknologi produksi bioetanol berbasis lignoselulosa yang berpotensi untuk diterapkan

dalam proyek pengembangan bioetanol perusahaan.

2. Telaah/review mengenai hasil kajian teknologi bioetanol lignoselulosa, mencakup

kekurangan dan kelebihan dari masing-masing teknologi tersebut.

3. Identifikasi lisensi teknologi-teknologi produksi bioetanol dan menyusun daftar lisensor

dari teknologi tersebut, termasuk perkembangan penerapan teknologi tersebut di industri

bioetanol.

4. Analisis kelemahan dan kekuatan lisensor teknologi yang ada dan analisis peluang

perbaikannya.





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2. STUDI PUSTAKA

2.1. Biomass Lignosellulosa

Biomassa lignoselulosa pada dasarnya terdiri atas tiga biopolimer utama, yaitu selulosa

(biopolimer rantai lurus dengan monomer glukosa), hemiselulosa (biopolimer gula yang tersusun

dengan dominasi monomer pentosa), dan lignin (biopolimer kompleks dengan senyawa fenol

sebagai monomernya). Ilustrasi biomassa lignoselulosa dan struktur biopolimer-biopolimernya

disajikan pada Gambar A.1.1.

Gambar A.1.1 Komponen biomassa lignoselulosa

2.1.1.Selulosa

Selulosa merupakan biopolimer gula (polisakarida) yang keberadaanya paling melimpah di bumi.

Selulosa tersusun atas rantai linear monomer glukosa yang saling terikat oleh ikatan (1-4)

glikosida. Struktur polimer rantai lurus glukosa ini sering disebut juga dengan istilah glukan.

Adanya interaksi antara atom oksigen dan gugus hidoksi (OH) melalui ikatan hidrogen membuat

struktur selulosa mempunyai kekuatan tarik (tensile strength) yang tinggi dan membentuk struktur





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serat-serat mikro. Hal ini pulalah yang mengakibatkan selulosa mempunyai struktur kristalinitas

yang kuat.

Gambar A.1.2. Struktur selulosa (a) monomer dan struktur ikatan (1-4) glikosidik antar monomer dalam selulosa, (b) ikatan hidrogen pada selulosa

Apabila digunakan sebagai bahan baku bioetanol melalui jalur fermentasi, glukosa dari selulosa

merupakan komponen utama yang dikonversi menjadi etanol. Dibandingkan dengan biopolimer

pati yang menjadi bahan baku bioetanol generasi pertama, proses memperoleh unit monomer

glukosa dari selulosa lebih susah. Hal ini menjadi salah satu pembatas (barrier) komersialiasi

bioetanol lignoselulosa. Perbandingan antara selulosa dan pati disajikan pada Tabel A.1.1

Tabel A.1.1 Perbandingan selulosa dan pati

Selulosa Patistrukur terusun atas -glukosa yang

terhubung dengan ikatan (1-4) glikosidik

terusun atas -glukosa yang terhubung dengan ikatan (1-4)

glikosidikRantai linear linear: amilosa

bercabang: amilopektinKristalinitas tinggi rendah

Berubah menjadi amorf di air perlu T:300 °C, 250 bar cukup pada T > 60 °CKetercernaan (digestibility) Tidak Ya


(a) (b)




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2.1.2.Hemiselulosa

Hemiselulosa merupakan biopolimer gula komplek yang khas terdapat dalam biomassa

lignoselulosa. Hemiselulosa tersusun atas beragam monomer gula yang saling terikat dan tidak

memiliki pola (Gambar A.1.3). Komposisi dan struktur hemiselulosa ini sangat beragam tergantung

pada jenis biomassa dan lingkungannya. Komposisi hemiselulosa umumnya didominasi oleh gula

berkarbon lima (pentosa) seperti xilosa dan arabinosa. Meskipun demikian, gula berkarbon enam

(heksosa) seperti glukosa, manosa, dan galaktosa juga terdapat dalam biopolimer ini.

Hemiselulosa kaya akan xilosa, seperti tongkol jagung atau tandan kosong sawit sering disebut

sebagai xilan.

Dibandingkan dengan selulosa, hemiselulosa lebih mudah dihidrolisis untuk mendapatkan

monomer-monomer gula penyusunnya. Monomer-monomer gula penyusun hemiselulosa

merupakan bahan yang dapat dikonversi menjadi bioetanol. Mempertimbangkan kemampuan

metabolisme mikroba yang digunakan dalam proses fermentasi bioteanol, sumber gula heksosa

dapat difermentasi bersama glukosa yang dihasilkan dari selulosa, sedangkan gula pentosa perlu

difermentasi menjadi bioetanol secara terpisah.

Gambar A.1.3 Struktur hemiselulosa





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2.1.3.Lignin

Lignin merupakan biopolimer komplek dan khas yang terdapat dalam biomassa lignoselulosa.

Strukutur lignin tersusun atas jaringan aromatik (fenol) yang terikat secara silang (cross-linked)

dan tidak berpola (Gambar A.1.4). Lignin beperan sebagai pengikat selulosa dan hemiselusosa

dan penyokong (support) yang memberikan kekuatan struktur pada biomassa.

Di dalam produksi bioetanol, keberadaan lignin ini merupakan salah satu pembatas yang perlu

dibongkar agar gula-gula yang terdapat pada selulosa dan hemiselulosa dapat diakses dan

dihidrolisis. Lignin merupakan produk samping atau limbah dalam produksi bioetanol. Kisaran

komposis lignin sekitar 30% pada biomassa lignoselulosa memotivasi pemanfaatan produk

samping ini untuk meningkatkan keekonomian bioetanol selulosa.

Gambar A.1.4 Struktur lignin





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2.1.4.Jenis dan Tipikal Komposisi Biomassa Lignoselulosa

Jenis biomassa lignoselulosa dapat dikategorikan menjadi 4 jenis yaitu, (1) residu kayu,

limbah/sisa dari industri kayu, termasuk industri kertas (2) residu pertanian, seperti tandan kosong

sawit, jerami, tongkol jagung, bagas, kulit batang sagu, dan sekam padi, (3) tanaman energi

(energy crops) seperti rumput gajah, miscanthus, dan (4) limbah padat (selulosa)

perumahanUntuk residu kayu atau sisa kayu industri, para pengembang teknologi konversi

lignoselulosa sering menggunakan istilah yang biasa digunakan dalam perkayuan, yaitu hardwood

dan softwood.

Tabel A.1.2 menyajikan komposisi biopolimer beragam biomassa lignoselulosa. Komposisi tipikal

biopolimer secara berturut-turut untuk selulosa, hemiselulosa dan lignin adalah 38-50%, 23-32%,

dan 15-25%, variasi bergantung pada jenis biomassa lignoselulosa, usia dan tahap pertumbuhan,

dan kondisi lainya (Kumar, dkk., 2009).

Tabel A.1.2 Tipikal komposisi biomassa lignoselulosa* (Kumar, dkk., 2009)

Biomassa Lignoselulosa selulosa (%) hemiselullosa (%) lignin (%)batang kayu keras (hardwood) 40-55 24-40 18-25batang kayu ringan (softwood) 45-50 25-35 25-35kulit biji (nut sheels) 25-30 25-30 30-40tongkol jagung 45 35 15rerumputan (grasses) 25-40 35-50 10-30wheat straw 30 50 15dedaunan 15-20 80-85 0limbah pabrik pulp 60-70 10-20 5-10switch grass 45 31.4 12tandang kosong sawit (Zainudin, 2012)

42.85-51.28 24.01-28.51 11.70-15.17

jerami padi (Sarkar, 2012) 32-47 19-27 5-24bagas pabrik (Sarkar, 2012) 65 (total karbohidrat) 18.4

*perhitungan komposisi yang disajikan menggunakan basis kering

Indonesia memilki sumber biomassa lignoselulosa yang beragam dan aktratif sebagai bahan baku

bioetanol generasi kedua, seperti residu pertanian: tandan kosong kelapa sawit, jerami dan sekam

padi, dan kulit batang sagu. Ketersediaan dan potensi biomassa lignoselulosa tersebut akan diulas

secara mendalam dan detail pada Sub-Paket B.1. dan A.3., tentang evaluasi ketersediaan tandan

kosong sawit sebagai bahan baku bioetanol generasi kedua dan 3 (tiga) bahan baku lignoselulosa

lokal alternatif.





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2.2. Proses Produksi Bioetanol Lignoselulosa

Bioetanol lignoselulosa pada umumnya dapat diperoleh melalui empat jalur proses yang dapat

dikelompokkan menjadi dua kelompok proses konversi, yaitu proses konversi secara biologis

(biochemical conversion) dan proses konversi termal (thermochemical conversion). Skema A.1.1

memberikan ilustrasi diagram proses dari jalur-jalur proses produksi bioetanoll lignoselulosa.

Skema A.1.1 Skema jalur-jalur proses konversi produksi bioetanol lignoselulosa

Inti dari proses produksi bioetanol secara biologis adalah proses fermentasi gula yang terkandung

dalam biomassa lignoselulosa menjadi etanol. Ada dua cara memperoleh gula yang dapat

difermentasi dari biomassa lignoselulosa, yaitu melalui hidrolisis enzimatik (jalur proses 1) dan

hidrolisis asam (jalur proses 2). Berbeda dengan proses konversi secara biologis, proses konversi

termal melibatkan reformasi biopolimer di dalam biomassa lignoselulosa menjadi gas sintesa

(syngas) melalui proses gasifikasi (T>600 °C). Selanjutnya, syngas yang terbentuk dikonversi

menjadi etanol melalui jalur fermentasi (Jalur proses 3) atau sintesa katalitik (Jalur proses 4).

Tabel A.1.3 menyajikan jalur proses konversi bioetanol lignoselulosa dan pengembang teknologi

prosesnya. Selain keempat jalur utama konversi bioetanol terdapat beberapa pengembang

teknologi yang menggunakan jalur gabungan (konversi termal dan fermentasi) untuk mengonversi

gula menjadi etanol. Tabulasi pengembang teknologi tersebut mengindikasikan bahwa jalur





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produksi bioetanol melalui jalur fermentasi gula merupakan jalur produksi yang lebih popular dan

lebih banyak dikembangkan daripada jalur poses konversi termal. Selaras dengan ruang lingkup

dan fokus pekerjaan ini, kajian paten dan proses teknologi bioetanol lignoselulosa difokuskan pada

teknologi bioetanol melalui jalur fermentasi gula (biochemical conversion). Selanjutnya, istilah

teknologi bioetanol lignoselulosa yang dimaksd pada bagian laporan ini adalah teknologi bioetanol

menggunakan jalur konversi secara biologis.

Tabel A.1.3 Tabel jalur proses konversi bioetanol lignoselulosa dan pengembang teknologinya.

No Jalur Proses Pengembang Teknologi

1 Jalur 1: Hidrolisis enzimatik-fermentasi

gula

POET-DSM, IOGEN, Inbicon Biomass Refinery,

Mossi & Ghisolfi - Chemtex Italia, Dupont

Danisco Cellulosic Ethanol LLC, Lignol, KL

Energy, AE Biofuels, Logos Technologies, Inc.

Abengoa Bioenergy

2 Jalur 2: Hidrolisis Asam-fermentasi gula Bluefire ethanol, SEKAB, Archer Daniels

Midland, Weyland AS

3 Jalur 3: Gasifikasi-fermentasi Coskata, INEOS New Planet Bioenergy LLC

4 Jalur 4: Gasifikasi-sintesa katalitik Enerkem, Range Fuels (d.h. Kergy)

5 Jalur Proses Gabungan/Alternatif

a) Fermentasi alternatif (jalur

asetat)

Zeachem

b) Fermentasi langsung biopolimer

gula menjadi etanol

Mascoma, Qteros (d.h. Sun Ethanol), American

Process, Inc., Pacific Ethanol

2.3. Perbandingan Proses Produksi Bioetanol Lignoselulosa dengan

Bioetanol Generasi Pertama

Produksi bioetanol pada dasarnya terdiri atas tiga (3) tahap utama, yaitu perolehan gula yang

dapat difermentasi (fermentable sugar), fermentasi, dan pemisahan dan pemurnian produk.

Skema A.1.2 menampilkan overview proses produksi bioetanol dari beragam sumber bahan baku,





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meliputi bioetanol generasi pertama (tetes gula/molase dan pati singkong) dan biomassa

lignoselulosa. Tahap sebelum fermentasi, untuk memperoleh gula yang dapat difermentasi,

merupakan pembeda utama tahapan proses produksi bioetanol dari gula sederhana (tetes

gula/molase), pati, dan bahan lignoselulosa.Tetes tebu (molase) dapat langsung difermentasi

menjadi etanol, sedangkan pati singkong perlu melalui tahapan likuifaksi dan sakarifikasi untuk

memperoleh gula yang dapat difermentasi. Sementara itu, biomassa lignoselulosa membutuhkan

tahapan perlakuan awal dan tahapan hidrolisis untuk menghasilkan gula yang dapat difermentasi.

Selain glukosa, biomassa lignoselulosa juga menghasilkan gula pentosa yang juga dapat

dikonversi menjadi bioetanol.

Skema A.1.2 Perbandingan tahap produksi bioetanol lignoselulosa (generasi kedua) dengan bioetanol generasi pertama

Proses fermentasi dan pemurnian etanol dari dari ketiga jenis bahan baku tersebut relatif

sama, kecuali untuk tahap tambahan fermentasi pentosa. Para pengembang teknologi bioetanol

lignoselulosa menggunakan proses fermentasi dan pemurnian etanol yang sama dengan proses

bioetanol generasi pertama yang telah mencapai tahap komersial.

2.4. Produksi Bioetanol Lignoselulosa

Produksi bioetanol lignoselulosa melalui jalur fermentasi terdiri atas 5 tahap, yaitu (1) tahap

perlakuan awal (pretreatment), (2) tahap hidrolisis, (3) tahap fermentasi, (4) pemisahan dan





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pemurnian, dan (5) pemanfaatan produk samping. Sub-bab berikut mengulas secara

komprehensif tiap tahap produksi bioetanol beserta status perkembangannya.

2.4.1.Perlakuan Awal (Pretreatment)

Proses perlakukan awal bertujuan untuk memecah lignin dan merusak struktur kristalin dari

selulosa seperti yang diilustrasikan pada Gambar A.1.5 sehingga struktur biomassa menjadi lebih

mudah diakses oleh media penghidrolisis (Mosier, dkk., 2005). Perlakuan awal dilaksanakan

sebagai proses pendahuluan bagi konversi bahan baku berlignoselulosa dengan

mempertimbangkan kompleksitas dari struktur lignoselulosa yang telah dijelaskan pada subbab

2.1.

Gambar A.1.5 Skema tujuan perlakukan awal biomassa lignoselulosa (diambil dari (Mosier, dkk., 2005))

Proses perlakuan awal yang efektif diharapkan dapat memenuhi beberapa target seperti

berikut (Yang dan Wyman, 2008):

kebutuhan bahan kimia dapat diminimalisasi,

menghindari proses reduksi ukuran partikel karena proses membutuhkan biaya dan energi

yang besar,

perolehan gula tereduksi dari hemiselulosa (mendekati 100%) dan selulose (lebih besar

dari 90%) yang tinggi,

konsentrasi gula pada proses pretreatment dan fermentasi lebih besar dari 10% agar

efisiensi proses downstream dapat terjaga,





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reaktor pretreament harus ekonomis (minimalisasi volume dan penggunaan material yang

sesuai),

tidak menghasilkan residu yang mengganggu kontuinitas proses pretreatment maupun

proses selanjutnya,

lignin dan konstituen lainnya dapat diambil kembali sebagai produk samping serta

bertujuan untuk tidak mengganggu proses downstream, dan

kebutuhan panas dan energi rendah serta dapat diintegrasikan secara termal dalam

proses.

Dengan demikian, pemilihan teknologi perlakuan awal harus dilakukan dengan seksama dengan

mempertimbangkan konsentrasi padatan dan pola pelepasan gula sehingga sesuai dengan

keseluruhan proses, bahan baku yang digunakan, media penghidrolisis, organisme yang

digunakan, serta kondisi optimum tercapai. Pilihan-pilihan teknologi serta perbandingannya

ditunjukkan pada Tabel A.1.4.





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Tabel A.1.4. Perbandingan perlakuan awal (Kumar dan Murthy, 2011; Limayem dan Ricke, 2012; Mosier, dkk., 2005; Sun dan Cheng, 2002; Taherzadeh dan Karimi, 2007; Taherzadeh dan Karimi, 2007; Yang dan Wyman, 2008)

Perlakuan Awal Karakteristik Kunci Efek Tipikal Bahan Baku Tipikal Kondisi Operasi Ref

Fisik/Physical pretreatment (penggilingan, iradiasi, dan lain-lain)

- Membutuhkan energi yang tinggi- Tidak dapat menghilangkan lignin- Tidak disarankan untuk aplikasi pada

industri- Tidak membutuhkan bahan kimia

1+, 2# (Taherzadeh dan Karimi, 2008)

Hidrolisis Asam encer(HCl/H2SO4, 0.5-5%)

- Teknik sederhana dan praktis.- Tidak butuh energi termal tinggi- Efektif untuk menghidrolisis hemiselulosa

pada kondisi moderate- Menghasilkan inhibitor bersifat toksik- Membutuhkan tahap recovery dan

netralisasi/detoksifikasi

1+, 3+, 5+ Serpihan kayu, straw Konsentrasi : 0.05-5%T : 160-220oCt : 1-60 menitP : tekanan uap jenuh

(Limayem dan Ricke, 2012; Mosier, dkk., 2005)

Perlakuan Air panas (Hot water- Hydrothermal Treatment)

- Sebagian besar hemiselulosa dapat dilarutkan

- Tidak menghasilkan bahan kimia ataupun inhibitor toksik

- Diapplikasikan pada beban padatan rata-rata

- Tidak cocok untuk softwood

1+, 3+, 5# Fiber jagung, straw pH : 4-7 T : 160-230oCt : 12-60 menitP : hingga 5 Mpa

(Limayen, 2012)(Mosier, 2005) (Hendrik, 2009)Kumar, 2011)

Hidrolisis Alkalin (Lime) - Perolehan gula pentosa dan heksosa total yang tinggi

- Efektif untuk hardwood dan residu pertanian

- Temperatur dan tekanan operasi tinggi- Masalah pada skala komersial

1+, 3#, 4+, 5+

Softwood dengan kandungan lignin < 26% dan jerami dengan kandungan lignin 10-18%

Konsentrasi : 0.5-3%T : > 100oCt : beberapa menit – jamP : tekanan uap jenuh

(Limayen, 2012)(Mosier, 2005)(Kumar, 2009)(Kumar, 2011)

Ammonia Fiber Expansion - Efektif untuk residu pertanian (bonggol 1+,2+,3#,4+, Bahan baku tidak Konsentrasi : 1-2 kg (Limayen, 2012)





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(AFEX) jagung) tanpa pembentukan produk akhir yang bersifat toksik

- Tidak cocok untuk bahan baku berlignin tinggi

- Ammonia recovery- Tidak menghasilkan air limbah

5+ berlignin tinggi ammonia cair/kg biomassa keringT : 90oCt : 30 menit

Ammonia Recycle Percolation (ARP)

- Redistribusi lignin tinggi (85%)- Daur ulang amoniak- Mendekati perolehan teoritik

1+, 2+, 3#, 4+, 5+

Limbah pertanian, moderate utk hardwood, softwood tidak sesuai

Konsentrasi : 10-15% w/wT : 150-170oCt : 14 menit

Ledakan Kukus Katalitik (steam explosion with catalyst)

- Efektif untuk residu pertanian dan hardwood, namun tidak terlalu efekti untuk softwood

- Penghilangan fraksi hemiselulosa tinggi- Tidak terlalu efektif untuk softwood

3+, 5+ Hardwood dan residu pertanian

T : 160-290oCT : beberapa detik - menitP : 0.69-4.83 Mpa

Pelarutan Lignin dengan senyawa Organik (Organosolv)

- Perolehan tinggi dicapai dengan kombinasi asam

- Efektif untuk softwood dan hardwood- Konsentrasi gula dari hemiselulosa

rendah- Membentuk inhibitor toksik- Kebutuhan daur ulang pelarut organik- Modal kapital investasi tinggi

3+, 4+ Serpihan kayu Konsentrasi : 35-70% alkoholpH : 2.0-3.8T : 180-195oCt : 30-90 menit

Sulfite pretreatment top overcome recalcitrance (SPORL)

- Efektif untuk bahan baku berlignin tinggi, hardwood, dan softwood

- Efisiensi energi tertinggi- Pembentukan inhibitor minimal- Kompatibiltas bahan baku tinggi- Kombinasi SPORL dan steam explosion

1+, 2+, 3#, 4+, 5+

Serpihan kayu, kayu bahan baku kertas





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dengan kehadiran enzim sangat efektif untuk softwood

- Biaya efektif

Penghilangan Lignin dengan Ozone

- Penghilangan lignin efektif- Kompatibiltas bahan baku luas- Tidak menghasilkan inhibitor- Mahal

4+ Jerami, bagas, sekam, hardwood

Oksidasi basah alkalin - Kombinasi oksigen, air, temperatur tinggi, dan alkali mengurangi inhibitor toksik

- Delignifikasi dan pelarutan bahan baku yang tinggi

- Hidrolisis oligomer rendah

1+, 5+

Bioconversi lignin dengan fungal - Ramah lingkungan- Penggunaan energi dan bahan kimia yang

rendah- Biokonversi lambat

2+, 3+, 5+ Waste material

Keterangan notasi kolom Efek: Angka: (1) meningkatkan luas permukaan akses, (2) dekristalinasi selulosa, (3) menghilangkan hemiselulosa, (4) menghilangkan lignin, (5) merubah/merusak struktur lignin. Notasi setelah angka: positif(+): efek signifikan, tanda binang(#) efek tidak signifikan]





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2.4.2.Sakarifikasi

Sakarifikasi adalah proses hidrolisis untuk memecah polisakarida menjadi monomer-monomer

gula terlarut. Sakarifikasi biomassa lignoselulosa ditujukan untuk memecah biopolimer gula

menjadi monomer gula yang dapat difermentasi dengan bantuan katalis melalui proses hidrolisis

(Tahap ini sering juga disebut sebagai tahap hidrolisis). Ada dua metoda yang digunakan untuk

menghidrolisis biomassa lignoselulolsa, yaitu hidrolisis asam dan enzimatik.

2.4.3.Hidrolisis Asam

Hidrolisis asam menggunakan bantuan asam (biasanya HCl atau H2SO4) sebagai katalis. Ion

hidronium (H3O+) berperan memutus ikatan glikosidik yang menghubungkan monomer-monomer

gula. Berdasarkan konsentrasi asam, proses hidrolisis asam dibagi menjadi hidrolisis asam encer

(dilute acid) dan hidrolisis asam pekat (concentrated acid).

Hidrolisis asam encer biasanya diselenggarakan pada rentang konsentrasi asam 2-5 wt% pada

temperatur di atas 120 °C. Hemiselulosa dapat dihidrolisis dengan metoda ini pada temperatur

moderat (T: 120-150 °C), tetapi dibutuhkan kondisi yang ekstrim untuk menghidrolisis selulosa

(T>190 °C). Pada proses hidrolisis ini, reaksi dilakukan pada kondisi temperatur dan tekanan yang

tinggi dan karena perolehan glukosa yang rendah dari selulosa pada proses hidrolisis ini, maka

perolehan etanol pun rendah.

Hidrolisis asam pekat biasanya diselenggarakan pada konsentrasi asam 10-30 wt%, rentang

temperatur operasi di bawah 50 °C, dan tekanan atmosfir. Proses ini membutuhkan waktu tinggal

yang lebih lama dan menghasilkan perolehan etanol yang lebih tinggi dibandingkan dengan

hidrolisis asam terlarut.

Meskipun hidrolisis asam memiliki kehandalan dalam hal menghidrolisis biopolimer selulosa dan

hemiselulosa secara serempak, namun metoda ini memiliki kekurangan yaitu terjadinya reaksi

lanjutan (konsekutif) dari gula yang terbentuk. Glukosa yang terbentuk akan membentuk

hidroksimetilfurfural (HMF) dan xilosa dapat terkonversi menjadi furfural. Selain menurunkan

perolehan gula yang terbentuk, komponen HMF dan furfural merupakan inhibitor mikroorganisme

pada proses fermentasi. Strategi umum yang biasa dilakukan untuk hidrolisis biomassa ini adalah

(1) menyelenggarakan hidrolisis pada kondisi yang tepat dan menghentikan reaksi saat gula

terproduksi pada level optimum dan (2) melakukan detoksifikasi hidrolisat sebelum diumpankan

untuk menghilangkan zat racun bagi microorganism. Detoksifikasi biasanya dilakukan dengan

menambahkan basa seperti Ca(OH)2 atau amoniak (Taherzadeh dan Karimi, 2007).





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2.4.4.Hidrolisis Enzimatik

Hidrolisis biopolimer secara enzimatik menggunakan enzim yang diproduksi oleh sejumlah

mikroorganisme yang dapat memecah komponen lignoselulosa menjadi gula. Proses ini biasanya

diselenggarakan pada temperatur rendah tetapi membutuhkan waktu reaksi yang lebih lama.

Sesuai dengan sifat enzim yang bekerja spesifik, hidrolisis selulosa dan hemiselulosa memerlukan

jenis enzim yang berbeda, yaitu enzim selulase dan enzim hemiselulase.

Hidrolisis Selulosa (Selulase)

Proses hidrolisis selulosa secara enzimatik melibatkan peran selulase. Tahapan kinerja selulase

melalui tahap-tahap berikut: adsorpsi selulase pada permukaan selulosa, biodegradasi selulosa

menjadi gula tereduksi, dan desorpsi selulase. Selulase terdiri dari 3 kelas utama enzim yaitu

endo-glukanase, ekso-glukanase, dan β-glukosidase. Ketiga kelas enzim tersebut memiliki

karakteristik kinerja enzim yang berbeda; endo-glukanase menyerang serat selulosa yang memiliki

kristalitas rendah serta menghasilkan rantai bebas, ekso-glukanase mendegradasi rantai gula

dengan menyingkirkan unit selobiosa pada rantai bebas, dan β-glukosidase memotong selobiosa

menjadi glukosa. Selulase dapat dihasilkan oleh mikroorganisme di antaranya Trichoderma spp.,

dan Aspergillus niger (Taherzadeh dan Karimi, 2007).

Hidrolisis Hemiselulosa (Hemiselulase)

Hemiselulase berperan pada proses hidrolisis hemiselulosa. Sama halnya dengan selulase,

hemiselulase juga terdiri dari beberapa kelas enzim seperti endo-1,4-β-D-xylanase, ekso-1,4-β-D-

xylanase, endo-1,4-β-D-mannanase, β-manosidase, asetil xylan esterase, α-glukuronidase, α-L-

arabinofuranosidase, dan α-galaktosidase. Perbedaan karakteristik dari beberapa kelas enzim

tersebut dapat dilihat pada pola penyerangan, daerah yang diserang, hasil konversi, dan lain-lain.

Beberapa spesies bakteri dari kelas Clostridium, Cellumonas, Thermomonospora, Bacillus,

Bacteriodes, Ruminococcus, Erwinia, Acetovibrio, Microbispora, dan Streptomyces serta fungi dari

kelas Trichoderma, Penicillium, Fusarium, Phanerochaete, Humicola, dan Schizophillum dapat

memproduksi hemiselulase (Taherzadeh dan Karimi, 2007).





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2.4.5.Perbandingan Hidrolisis Asam dan Enzimatik

Tabel A.1.5 menyajikan perbandingan antara hidrolisis asam dan enzimatik. Karena hidrolisis

enzimatik menghasilkan perolehan gula yang lebih tinggi dari lignoselulosa, teknologi enzimatik

lebih banyak dipilih untuk produksi bioetanol lignoselulosa. Namun demikian, harga enzim selulase

yang tinggi menjadi salah satu pembatas komersialisasi bioetanol lignoselulosa.

Tabel A.1.5 Perbandingan Hidrolisis Asam dan Enzimatik

No Variabel Hidrolisis

Asam Encer Asam Pekat Enzimatik

1 Kondisi hidrolisis ringan (mild) Tidak Tidak YaTemperatur rendah (T < 50 °C)

Tidak ( > 130 °C) Ya Ya

Tekanan atmosferik Tidak (>10 bar) Ya Ya2 Perolehan gula tinggi Tidak Ya Ya3 Terjadi inhibisi produk selama hidrolisis Tidak Tidak Ya4 Terbentuk produk inhibitor fermentasi Ya Tidak Tidak5 Biaya katalis murah Ya Ya Tidak6 Waktu reaksi singkat Ya (Menit) Ya

(1-6 jam)Tidak (xx jam)

7 Rekoveri katalis Tidak Ya Tidak

2.5. Fermentasi

2.5.1.Mikroorganisme untuk Fermentasi Biomassa Lignoselulosa Menjadi Etanol

Sesuai dengan komposisi gula yang dapat difermentasi, produksi bioetanol lignoselulosa dapat

dihasilkan dari fermentasi heksosa dan fermentasi pentosa. Mikroorganisme yang digunakan

untuk fermentasi heksosa pada bioetanol lignoselulosa ini sama dengan mikroorganisme yang

digunakan pada fermentasi heksosa pada proses produksi bioetanol generasi pertama.

Sementara itu, umumnya fermentasi pentosa menjadi etanol harus diselenggarakan terpisah

dengan mikroorganisme lain. Error: Reference source not found menampilkan mikroorganisme

untuk fermentasi biomass lignoselulosa menjadi bioetanol, meliputi karakteristik beserta

keunggulan dan kerugiannya.





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Tabel A.1.6 Mikroorganisme untuk Fermentasi Biomassa Lignoselulosa Menjadi Etanol

Spesies Karakteristik Keunggulan Kerugian RefsSaccharomyces cerevisiae Ragi fakultatif anaerobik - Secara alami fermentasi etanol terjadi

- Perolehan alkohol tinggi (90%)- Toleransi etanol (10% v/v) dan inhibitor

tinggi- Cocok untuk modifikasi genetik

- Tidak dapat memfermentasi xylosa dan arabinosa

- Tidak tahan terhadap temperatur tinggi

Candida shehatae Ragi mikro-aerofilik - Fermentasi xilosa - Toleransi etanol rendah- Perolehan etanol rendah- Membutuhkan kondisi mikro-aerofilik- Tidak melakukan fermentasi xylosa

pada pH rendahZymomonasmobilis Bakteri Gram negatif

ethanologenic- Perolehan etanol tinggi (perolehan teoritik

97%)- Toleransi etanol tinggi (14% v/v)- Produktivitas etanol tinggi- Cocok untuk modifikasi genetik- Tidak membutuhkan tambahan oksigen

- Tidak dapat melakukan fermentasi xylosa

- Toleransi terhadap inhibitor rendah- Rentang pH netral

Pichia stiplis Ragi fakultatif anaerobik - Memberikan performansi terbaik pada fermentasi xilosa

- Perolehan etanol 82%- Dapat memfermentasi sebagian besar gula

tereduksi dari selulosa- Rekomendasi selulase pada proses SSF

- Tidak tahan etanol pada konsentrasi > 40g/l

- Tidak melakukan fermentasi pada pH rendah

- Sensitif terhadap inhibitor kimiawi- Membutuhkan kondisi mikro-aerofilik- Reasimilasi etanol yang terbentuk

Pachysolen tannophilus Fungi aerobik - Fermentasi xilosa - Perolehan etanol rendah- Membutuhkan kondisi mikro-aerofilik- Tidak melakukan fermentasi xilosa





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Spesies Karakteristik Keunggulan Kerugian Refspada pH rendah

Esherichia coli Bakteri Gram negatif mesofilik

- Mampu fermentasi gula pentosa dan heksosa

- Cocok untuk modifikasi genetik

- Represi katabolime mengganggu co-fermentasi

- Toleransi etanol terbatas- Rentang pH dan temperatur

pertumbuhan yang sempit- Produksi asam organik- Stabilitas genetik belum terbukti- Toleransi rendah terhadap etanol dan

inhibitorKluveromycesmarxianus Ragi termofilik - Dapat tumbuh pada temperatur > 52oC

- Cocok untuk proses SSF/CBP- Mengurangi biaya pendinginan- Mengurangi kontaminasi- Fermentasi rentang fula tereduksi yang

lebar- Cocok untuk modifikasi genetik

- Gula berlebih mempengaruhi perolehan etanol

- Toleransi etanol rendah- Fermentasi xylosa rendah- Pembentukan xylitol

Thermophilicbacteria:Thermoanaerobacterium

saccharolyticumThermoanaerobacter ethanolicusClostridium thermocellum

Bakteri anaerobik ekstrim - Tahan pada temperatur tinggi ekstrim 70oC- Cocok untuk proses SSCF/ CBP- Fermentasi variasi gula- Menunjukkan aktivitas selulolitik- Cocok untuk modifikasi genetik

- Toleransi etanol rendah





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2.5.2.Teknologi Fermentasi

Untuk memperoleh hasil yang optimal fermentasi dapat diselenggarakan pada beberapa

konfigurasi hidrolisis dan fermentasi yang sesuai. Berikut diulas strategi-strategi hidrolisis dan

fermentasi bioetanol lignoselulosa. Strategi-strategi tersebut dilakukan dengan

mempertimbangkan keuntungan dan kerugian tersebut dengan aspek efisiensi sumber daya

(enzim, mikroorganisme, utilitas) dan efektivitas proses (konsentrasi gula, konsentrasi etanol,

keberlangsungan proses downstream) sehingga proses fermentasi ini menjadi optimal. Umumnya

strategi-strategi berikut diaplikasikan pada hidrolisis enzimatik.

Separate Enzymatic Hydrolysis and Fermentation (SHF)

Proses SHF meliputi proses hidrolisis menjadi glukosa dan fermentasi etanol secara berurutan

dalam unit yang terpisah. Ilustrasi konfigurasi ini ditampilkan pada Gambar A.1.6. Proses

fermentasi pentosa dan heksosa dilakukan secara terpisah dalam unit bioreaktor yang berbeda.

Gambar A.1.6 Skema hidrolisis enzimatik dan fermentasi SHF





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Simultaneous Saccharification and Fermentation (SSF)

Proses hidrolisis enzimatik dan proses fermentasi dalam 1 unit diterapkan dalam konfigurasi SSF

ini. Glukosa yang dihasilkan melalui hidrolisis enzimatik langsung dikonsumsi oleh mikroorganisme

dalam proses fermentasi dalam unit bioreaktor yang sama. Teknologi fermentasi ini diilustrasikan

pada Gambar A.1.6. Fermentasi pentosa dilakukan dalam bioreaktor yang terpisah dengan

fermentasi heksosa karena hidrolisat yang kaya akan pentosa telah dipisahkan terlebih dahulu

selama proses perlakuan awal.

Gambar A.1.7 Skema hidrolisis SSF

Simultaneous Saccharifiaction and Cofermentation (SSCF)

Konfigurasi SSCF melibatkan proses sakarifikasi dan proses ko-fermentasi secara simultan dalam

1 unit biorekaktor. Istilah ko-fermentasi memiliki pengertian fermentasi baik pentosa dan heksosa

menjadi etanol oleh 1 mikroorganisme. Dengan demikian, hanya dibutuhkan 1 tahap untuk





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memproses hidrolisat dan fraksi padat dari lignoselulosa yang telah diberi perlakuan awal. Proses

diagram teknologi SSCF ditampilkan pada Gambar A.1.8.

Gambar A.1.8 Strategi Hidrolisis dan Fermentasi SSCF

Consolidated Bioprocessing (CBP)

Untuk menghilangkan unit operasi produksi enzim secara terpisah, teknologi CBP dikembangkan

dan memberikan kontribusi terhadap produksi enzim serta etanol dalam 1 bioreaktor dari populasi

mikroorganisme tunggal. Aplikasi teknologi CBP membutuhkan pengembangan strain

mikroorganisme lebih lanjut untuk menghasilkan strain yang dapat menghasilkan baik etanol dan

selulase yang efektif. Diagram alir proses teknologi CBP diilustrasikan padaGambar A.1.9.





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Gambar A.1.9 Strategi Hidrolisis dan Fermentasi CBP

Tabel A.1.7 Perbandingan Keuntungan dan Keterbatasan Strategi Hidrolisis dan Fermentasi (Sarkar, dkk., 2012; Taherzadeh dan Karimi, 2007)

Strategi Fermentasi dan Hidrolisis Fitur dan keuntungan KeterbatasanSeparate Enzymatic Hydrolysis and Fermentation (SHF)

- Setiap tahap dapat diproses pada kondisi operasi optimum

- Meminimasi interaksi antara tahap

- Inhibisi produk akhir meminimasi perolehan etanol

- Resiko kontaminasi karena durasi proses yang lama

Simultaneous Saccharification and Fermentation (SSF)

- Biaya rendah- Perolehan etanol lebih tinggi

karena penghilangan inhibisi- Mengurangi jumlah reaktor

yang diperlukan

- Perbedaan kondisi optimum enzim untuk hidrolisis dan fermentasiKebutuhan enzim besar

Simultaneous Saccharifiaction and Cofermentation (SSCF)

- Penggunaan 1 bioreaktor- Perolehan etanol tinggi (91,9-

92,8% terhadap perolehan teoritik)

Consolidated Bioprocessing (CBP)

- Tidak ada biaya operasi dan modal investasi untuk pembelian serta produksi enzim

- Konversi substrat tinggi

- Membutuhkan mikrooganisme rekayasa yang termofilik, tidak menghasilkan asam organik, dan tahan pada konsentrasi etanol tinggi





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2.6. Pemisahan dan Pemurnian

Bioetanol yang diperoleh dari proses fermentasi membutuhkan proses pemisahan dan pemurnian.

Pada umumnya, proses hilir (downstream) ini didominasi oleh proses distilasi yang dilakukan

secara terfraksionasi. Prinsip dasar dari proses distilasi ini adalah perbedaan titik didih komponen

air dan etanol. Konsentrasi etanol yang diperoleh setelah proses distilasi adalah sekitar 95%.

Untuk mencapai konsentrasi etanol yang lebih tinggi lagi (mendekati 100%), dibutuhkan distilasi

azeotrop karena batasan sifat azeotropis dari campuran etanol dan air dengan konsentrasi etanol

98%. Aplikasi pada industri menitikberatkan pada kontinuitas proses distilasi.[ref]

2.7. Pemanfaatan Produk Samping

Komponen lignin yang terdapat dalam biomassa lignoselulosa biasanya menjadi produk samping

utama dalam proses produksi bioetanol. Pada umumnya, lignin digunakan sebagai bahan bakar

boiler. Beberapa pengembang teknologi mengupayakan pemanfaatan lignin menjadi bahan kimia

yang lebih bermanfaat untuk meningkatkan keekonomian (misalnya sumber fenol digunakan

sebagai bahan baku adesif kayu). Beberapa pengembang mengonversi lignin menjadi sumber

energi lain dengan mengubah menjadi sumber metana (biogas) atau hidrogen (gasifikas).





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3. METODOLOGI

Kajian pustaka diawali dengan ulasan ringkas tentang biomassa lignoselulosa dan komponen-

komponen utamanya. Kajian produksi bioetanol lignoselulosa meliputi deskripsi struktur-struktur

serta fungsi-fungsi yang diperlukan disajikan secara komprehensif. Kajian pustaka tersebut

dikumpulkan dari beragam pustaka ilmiah terkini. Sementara itu perkembangan teknologi produksi

bioetanol lignoselulosa dikumpulkan dari pustaka ilmiah, laporan-laporan berbagai gugus kerja di

dunia untuk pengembang bioetanol lignoselulosa, berita-berita komersial, dan penelusuran

informasi dari website dan presentasi dari pihak pengembang teknologi, serta paten-paten yang

didaftarkan atau dimiliki pengembang teknologi bioetanol.

Telaah perkembangan teknologi bioetanol diulas secara komprehensif meliputi pilihan bahan

baku, teknologi perlakuan awal, strategi fermentasi termasuk fitur-fitur unit/khas yang dimiliki dari

pengembang teknologi.

4. HASIL DAN PEMBAHASAN

4.1. Teknologi Proses Produksi Bioetanol Lignoselulosa dan Status

Pengembangannya

Tabel A.1.10 menyajikan rekapitulasi pengembang teknologi bioetanol lignoselulosa beserta

dengan teknologi yang digunakan dan status pengembangannya. Detail uraian meliputi deskripsi

singkat, diagram blok proses, dan paten-paten para pengembangang teknologi bioetanol

lignoselulosa disajikan pada Lampiran 1. Perkembangan teknologi dan bioetanol lignoselulosa

selanjutnya diuraikan berdasarkan arah perkembangan dan karakter-karakter kunci untuk

mengidentifikasi status perkembangan teknologi dan arah pengembangannya.

4.1.1.Status Pengembangan dan Komersialisasi

Pengembangan teknologi dan komersialisasi bioetanol lignoselulosa berkembang pesat pada era

tahun 2005 setelah beragam program insentif dari berbagai negara untuk memproduksi bahan

bakar dari sumber terbarukan, terlebih dari bahan baku non-pangan. Keberadaan selulosa

sebagai biopolimer yang paling melimpah menjadi target yang atraktif untuk dikonversi menjadi

bioetanol. Beberapa pengembang teknologi mencanangkan proses pengembangan, dari skala

pilot, demonstrasi, dan mayoritas merencanakan untuk komersialisasi bioetanol lignoselulosa

pada tahun 2012-2013 (Tabel A.1.8). Meskipun hingga saat ini belum ada pabrik bioetanol





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lignoselulosa skala komersial, beberapa pengembang yang masih aktif dan sesuai target untuk

membangun skala komersial bioetanol selulosa adalah: ABENGOA, POET-DSM , ZEACHEM,

CHEMTEX M&G (Thane, 2012). Namun demikian, meskipun telah mencapai skala demonstrasi

untuk memproduksi bioetanol dari switch grass, Royal Shell Dutch (mitra kerja IOGEN)

memutuskan kerjasama dan pendanan untuk IOGEN ENERGY pada bulan Juni 2012 ini. Hal ini

mengakibatkan IOGEN mengatur ulang strategi komersialisasi bioetanol selulosa dengan fokus

integrasi bioetanol selulosa dengan pengolahan gula (sugar cane) di Brazil dan bisnis teknologi

enzim mereka.

Tabel A.1.8 Tahap Pengembangan Bioetanol Lignoselulosa (hingga tahap demonstrasi dan rencana komersialisasi)

Pengembang Skala Pilot Skala Demonstrasi Skala KomersialABENGOA Nebraka, AS

Operasi: 2008Etanol: 75 kL/tahun

Salamanca, SpanyolOperasi: 2009Etanol:5000 kL/tahun

Hugoton, USRencana 2012-2013Etanol:95 000 kL/tahun l

IOGEN Ottawa, KanadaOperasi 1984Produk gulaKayu: 1 ton/hari

Ottawa, KanadaOperasi 2004Etanol:2000 kL/tahun l (1600 ton/tahun jerami)

Ottawa, KanadaDirencanakan 2012Etanol:90 000 kL/tahun(750 ton/hari jerami)Status: batal

BIOGASOL Ballerup, DenmarkOperasi: 2011

Bornholm, DenmarkSedang dibangun, operasi 2016Etanol 5200 kL/tahun

INBICON (DONG ENERGI)

Fredericia, DenmarkOperasi: 2003Jerami 0,1 ton/tahun

Kalundborg, DenmarkOperasi: 2010Etanol: 5700 kL/hariJerami 100 ton/hari

POET-DSM South Dakota, SOperasi: 2008Etanol: 75 kL/tahun

Emmetsburg, Iowa, ASRencana: 2013Etanol:95 000 kL/tahun

CHEMTEX (PROESATM) Tortona, Piedmont, ItaliaOperasi: 2009Jerami: 50 ton/tahun

Crescention, ItaliaRencana: 2012Etanol:

DuPont Danisco Vonore, Tennessee, ASOperasi: 2011Etanol: 1000 kL/tahun

NevadaRencana: 2012Etanol: 105 000 kL/tahun

SEKAB (Swedia) Örnsköldsvik, SwediaOperasi: 2004Etanol: 0,3 kL/tahun

Örnsköldsvik, SwediaOperasi: 2011Etanol: 6000 kL/tahunOperasi dihentikan (biaya operasi)

Örnsköldsvik, SwediaOperasi: 2012Etanol: 15000 kL/hari (tunda)

ZeaChem Boardman, Oregon, ASOperasi: 2008Etanol: 1000 kL/tahun

Boardman, Oregon, ASOperasi: 2012Etanol: 95 000 kL/tahun





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Gambar A.1.10 Garis waktu pengembangan dan komersialisasi bioetanol lignoselulosa

Sebagian besar para pengembangan teknologi melanjutkan rute pengembangan bioetanol

berbasis fermentasi generasi pertama. Oleh karena itu, pada masa transisi dan pengembangan

tersebut, fokus para pengembang diarahkan pada (1) perlakuan awal, (2) metoda hidrolisis dan

pengembangan enzim, (3) fermentasi pentosa, (4) proses integrasi, dan (5) reduksi harga produksi

(Gambar A.1.10).

4.1.2.Bahan Baku dan Perlakuan Awal

Jenis perlakuan awal yang ditujukan untuk meningkatkan aksebilitas terhadap biopolimer gula

(selulosa dan hemiselulosa) bergantung pada karakteristik bahan baku yang digunakan para

pengembang. Pada umumnya untuk bahan baku residu pertanian dan jerami, para pengembang

teknologi menggunakan metode perlakuan awal steam explositon (ABENGOA ), modified steam

explosition (IOGEN), hydrothermal pretratment (INBICON). Sementara itu, untuk limbah kayu,

para pengembang menggunakan hidrolisis asam encer (SEKAB) dan hidrolisis asam pekat

(ARKINOV, BORREGAARD).





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4.1.3.Metoda Sakarifikasi: Hidrolisis asam encer

Strategi hidrolisis biopolimer selulosa dan hemiselulosa untuk menghasilkan gula yang dapat

fermentasi dapat ditempuh dengan cara hidrolisis asam atau hidrolisis encer. Hidrolisis asam

encer biasanya digabungkan perlakuan awal untuk mengoptimalkan perolehan gula pentosa dari

hemiselulosa dan gula heksosa dari selulose. Strategi ini dikenal sebagai hidrolisis asam encer

dua tahap. Hidrolisis pertama diselenggarakan pada temperatur moderat (150 °C, 15 menit) denga

katalias asam sulfat (1-3 %wt) untuk menghidrolisis hemiselulosa menjadi gula dapat fermentasi.

Hidrolisat kaya gula pentosan ini dinetralkan lalu diumpankan ke fermentasi heksosa untuk

mengubah gula pentose menjadi Etanol. Sementara itu, sisa padatan dihidrolisis pada

temperature lebih tinggi (200 °C, 2-3 menit) untuk menghasilkan gula heksosa dari selulosa.

Selanjutnya, hidrolisat kaya heksosa difermentasi menjadi bioetanol. SEKAB menggunakan teknik

ini untuk memperoleh gula yang dapat difermentasi dari residu kayu. Proses ini mempunyai

keunggulan tidak melibatkan enzim yang menjadi salah satu kendala (harga tinggi) pada proses

hidrolisis enzimatik, meskipun proses ini menghasilkan produk samping yang dapat menjadi

inhibitor proses fermentasi.

4.1.4.Hidrolisis Enzimatik

Seiring dengan perkembangan teknologi enzim, mayoritas pengembangan menggunakan metoda

enzimatik untuk memperoleh gula dapat difermentasi dari selulosa dan hemiselulosa. Untuk

menekan biaya proses, para pengembang teknologi bioetanol lignoselulosa menambah unit

produksi enzim dalam prosesnya (IOGEN, POET-DSM, DUPONT). Sementara itu, beberapa pihak

mengandalkan enzim yang diproduksi oleh pihak produsen enzim. Untuk keperluan pembangunan

skala demonstrasi dan komersial, para pengembang ini bekerjasama dan mengandalkan fasilitas

produksi produsen enzim. Chemtex dengan proses PROESA menggunakan enzim yang produksi

oleh Novozyme. Kolaborasi dan kontrak penyediaan enzim menjadi titik kunci jaminan

ketersediaan enzim, termasuk pabrik penyedia enzim yang dekat dengan pabrik bioetanol

lignoselulosa.

4.1.5.Fermentasi

Pilihan teknologi fermentasi sangat bergantung pada jenis bahan baku dan konsentrasi gula yang

dapat fermentasi terbentuk. Umumnya para pengembang teknologi menggunakan proses

hidrolisis dan fermentasi terpisah (SHF) atau hidrolisis dan fermentasi serempak (SSF). Dua





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proses ini akan melibatkan dua mikroorganisme yang berbeda untuk memfermentasi gula heksosa

dan gula pentosa.

Strategi pengembangan diambil Sud Chemie dengan proses Sun LiquidsTM nya menggunakan

teknik fermentasi gula heksosa dan pentosa secara serempak (SSCF). Kemampuan

pengembangan mikroorganisme yang dapat mengonversi serentak gula heksosa dan pentose

menjadi salah satu kunci proses sun liquids. Sementara itu, pengembang Mascoma menggunakan

teknologi konversi biopolimer secara serempak menjadi etanol. Teknologi ini dikenal sebagai

Consolidate Bioprocessing (CBP). Pada proses ini, penggunaan enzim sakarolitik (enzim untuk

mengonversi) dan mikroorganisme untuk memfermentasi tidak diperlukan.

Gambar A.1.11 Pilihan teknologi fermentasi

4.1.6.Proses Integrasi

Untuk meningkatkan keekonomian bioetanal selulosa, strategi proses integrasi menjadi salah satu

titik penting untuk diperhatikan. Proses terintegrasi dengan industri yang sudah ada diambil oleh

para pengembang untuk mengembangkan bioetanol lignoselulosa. POET-DSM mengintegrasikan

proses dan pabrik skala komersial mereka dengan fasilitas pabrik bioetanol generasi pertama dari





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pati jagung (corn starch ethanol). Dedini mengintegrasikan rencana pembangunan pabrik

bioetanol generasi pertama mereka dengan pabrik bioetanol generasi pertama dari tebu. Bagas

yang merupakan limbah dari pabrik bioetanol generasi pertama menjadi bahan baku proses

mereka. American Process Inc menggunakan strategi serupa dengan memanfaatkan bagas dari

pabrik gula/bioetanol gula.

4.2. Perbandingan Teknologi Produksi Bioetanol Lignoselulosa

Tabel A.1.9 menyajikan perbandingan pengembang utama bioetanol lignoselulosa yang telah

mencapai tahap demonstrasi. Keunggulan dan karakteristik kunci terletak dari teknologi yang

dipilih pada perlakuan awal, hidrolisis, dan fermentasi. Sementara itu, keterbatasan pengembang

adalah fleksibilitas penggunana bahan baku, terutama untuk mengolah bahan baku berkategori

kayu (hardwood maupun softwood). Proses dengan jalur teknologi asam, baik asam encer mapun

pekat, telah teruji untuk memproduksi bioetanol dari bahan baku berbasis kayu (SEKAB,

BORREGAARD).

Tabel A.1.9 Perbandingan Teknologi Utama Bioetanal Lignoselulosa

Proses/Lisensor Nama Dagang Proses

Karakteristik Kunci dan Keunggulan

Keterbatasan

CHEMTEX PROESATM Perlakukan awal tidak membutuhkan katalis atau bahan kimiaFermentasi gula pentose dan heksosa terpisah

Enzim bergantung pada penyediaan novozym

BIOGASOL CarbofracTM

PentofracTMBelum teruji untuk proses hardwoodEnzim bergantung pada penyediaan novozym

ABENGOA Perlaukan awal tidak membutuhkan katalis atau bahan kimia

Belum teruji untuk proses hardwoodEnzim bergantung pada penyediaan novozym

IOGEN Unit produksi enzim terpadu Belum teruji untuk proses hardwood

INBICON Perlaukan awal tidak membutuhkan katalis atau bahan kimia

Belum teruji untuk proses hardwood

ZEACHEM Fermentasi melalui jalur acetic acid (carbon efisiensi tinggi)

Intensifikasi energi tinggi (gasifikas dan esterifikasi)

AMERICAN PROCESS INC

GreenPowerTM Fraksionasi hemiselulosa dan selulosa, tanpa menggunakan bahan kimia


POET-DSM Enzim DSM dapat dioperasikan pada temperatur relatif tinggiUnit produksi enzim terpadu


SUD CHEMIE Sun LiquidsTM Perlakuan awal tidak membutuhkan zat kimia,






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fermentasi gula heksosa dan pentose serempak

SEKAB Tidak membutuhkan enzimMembutuhkan proses netralisasi

Proses sedikit korosifMenghasilkan limbah yang bersifat korosif





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Tabel A.1.10 Pengembang Teknologi Bioetanol dan Teknologi yang Digunakan

No Lisensor/Pengembang

Teknologi

Bahan baku Kapasitas produksi

Teknologi

Perlakuan awal Fermentasi Permisahan

1 Abengoa (EU/Spanyol, AS)

Corn stover, wheat straw, dan switchgrass

16 Mgal/tahun dan 75 MW

Renewable Power

Biomass Handling, acid impregnation,

steam explosion, neutralization

Sakarifikasi, yeast propagation dan

fermentasi

Distiasli (ethanol recovery dan stillage

processing)

2 American Energy Enterprise (AS)

Plant biomass dan wood waste

30-38 ML/tahun (perkembangan

300-380 ML/tahun)

- - AEE Distilasi (beban kerja 24-50 Mgal/tahun)

3 Bluefire Ethanol (AS)

Cellulosic waste diverted dari landfill

15 ML/tahun (Lancester) dan

72 ML/tahun (Fulton)

Hidrolisis asam Fermentasi ragi konvensional

-

4 ICM (AS) Sorgum, switchgrass, dan bonggol jagung

10 ML/tahun (demosntrasi) dan

190 ML/tahun (komersial)

Biochemical pretreatment

Fermentasi C5/C6 (Suplai Novozymes)

-

5 Mascoma (AS) Bervariasi termasuk hardwood

0,8-1,9 ML/tahun untuk komersial 151 ML/tahun

(Kinross, Michigan)

- - -

6 POET-DSM (Project Liberty)

(US)

Corn cobs dan stover 25Mgal/tahun - - -

7 Raven Biofuels, Wood waste 79,5 ML/tahun Hidrolisis asam Fermentasi C6 Distilasi





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Teknologi


Teknologi


Pure Energy, Eco-Energy dan Price

Biostock

(asam sulfat lemah) 2 tahap

8 Verenium dan British Petroleum

(AS/UK)

- 5,5 ML/tahun (BB 2tpd) dan 136

ML/tahun (Highlands

Florida)

Hidrolisis asam lemah

Fermentas hemiselulosa dan sakarifikasi serta

fermentasi

Distilasi

9 Iogen, Otawa (Kanada)

Agricultural residu (BB wheat 40 tpd)

2,5 ML/tahun (BB 30 tpd) dan 70

ML/tahun (Prince Albert, Sask)

[340 L etanol/ton BB]

Modified steam explosion

Sakarifikasi /hidrolisis enzimatik(selulase) dan

Fermentasi C5/C6

Distilasi

10 Lignol (Kanada) Switchgrass, corn stover, dan wheat straw

0,1 ML/tahun (BB 1 tpd)

Solvent based pretreatment

Sakarifikasi dan fermentasi

Distilasi

11 Dedini, Sao Paulo (Brasil)

Residu tebu 1,81 ML/tahun Diluted acid hydrolysis dan lignin solvent

Sakarifikasi (Novozymes) dan fermentasi

Distilasi

12 SEKAB, Ornskoldsvik dan Etek Etanolteknik AB (EU/Swedia)

Pine wood chips, bagas, wheat, corn stover, recycled waste, dan

energy grasses

0,14 ML/tahun, 6 ML/tahun

(demonstrasi), dan 120 ML/tahun

(komersial)

Acid and steam pretreatment (200oC) dan

hidrolisis enzimatik

Fermentasi C5 dan C6 (Taurus Energy, Modified strain yeast); SSF atau

SHF

Distilasi

13 INBICON Biomass Refinery

(Kalundborg) (EU/Denmark)

Wheat straw, corn cobs dan stover

20 Mgal/tahun (BB 460000 tpy)

Hydrothermal pretreatment

Hidrolisis enzimatik (supplier Danisco

Genencor & Novozymes) dan fermentasi

-

14 BioGasol (EU/Denmark)

Agricultural residu 5 ML/tahun wet explosion (Kombinasi steam

Hidrolisis enzimatik dan fermentasi glukosa

Distilasi





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Teknologi


Teknologi


explosion dan wet oxidation)

(yeast). Fermentasi xylosa (immobilized

reaktor)15 HCL Technologies,

IsraelWoody biomass - Hidrolisis

hydrocloric acid (recycle full HCl in

gas form)

Fermentasi -

16 TMO Renewables Cassava stalk 70-80gal/ ton BB - Fermentasi termofilik baketri

-

17 BioEthanol Japan (Celunol Proess

from SunOpta Inc.)

Wodd construction waste 1,4 ML/tahun (berkembang

menjadi 4ML/tahun)

- Fermentasi C5 & C6 (modified E. coli)

Distilasi

18 Marubeni,saraburi, Thailand

Bagas tebu 3 ML/tahun Hidrolisis asam lemah

Fermentas hemiselulosa dan sakarifikasi serta

fermentasi

Distilasi

19 China Resources Alcohol corporation

(CRAC)

Bonggol jagung 6 ML/tahun dan 1250 ML/tahun

(komersial)

Steam explosion (SunOpta Inc.)

- -

20 Mission New Energy

Agricultural waste 10000 gal/tahun Chemical pretreatment,

Hydrolisis dan fermentasi -

21 Ethtec, Australia Wood residu dan bagas (BB 2tpd)

- Feedstock impregnation dan

hidrolisis asam

Fermentasi simultan C5 & C6

Induksi pemisahan fasa dengan

potasium karbonat22 Pure Power,

SingapuraWood crop salix, a

variety of willow (BB 250 tpd)

- Milling dan pretreatment

ethanol

Hidrolisis enzimatik (selulase) dan fermentasi

Distilasi

23 Chempolis Agricultural residu - FormicodeliTM

(pelarutan dengan Hidrolisis enzimatik dan

fermentasiDistilasi diintegrasi

dengan formicopureTM





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Teknologi


Teknologi


biosolvent) fraksionasi

(byproduct asetat dan furfural)

24 Sud-Chemie AG (EU/Jerman Barat)

Cereal straw 2000 metric ton/tahun

Mechanical dan thermal

pretreatment

Hidrolisis enzimatik dan fermentasi C5 & C6

(modified yeast)

Reactification tower

25 Statoil dan Innovation Norway

(EU/Nowergia)

- 200000 L/tahun Hidrolisis asam (Weyland Process)

- -

26 Dupont Danisco Cellulosic Ethanol

(AS)

- 27,5ML/tahun Biological Pretreatment

Hidrolisis enzimatik dan fermentasi C5 &C6

-

28 Qteros (Amerika Serikat)

- - - Consolidated Bioprocessing (Clostridium

phytofermentans)

Distilasi

29 IMECAL (AteneaProject)

Citric waste - Biological Pretreatment

(Fungi)

SSF (Enzyme;ovozymes, Fermentis, Yeast)

Distilasi dan dehidrasi

30 IMECAL (PERSEO Project)

Organic matter MWS (BB 500 tpd)

16000L/day Thermochemical treatment

SSF (Enzyme;ovozymes, Fermentis, Yeast)

Distilasi dan dehidrasi

31 Zeachem (Amerika Serikat)

Hardwood, softwood, switch grass, corn stover

- Chemical fractionation

Fermentasi (asam asetat), ester production

(etil asetat)

Hydrogenasi (etanol)

32 Mossi & Ghisolfi Group (M&G) Italia

(Chemtex)

Non-foodchain crops, agricultural waste

13Mgal/tahun PROESA TM

33 Biogasol dan Danish Energy

Aganecy

BB 27000 ton/tahun 7 ML/tahun Biogasol proses





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Teknologi


Teknologi


34 Biogasol dan Pacific Ethanol Inc.

Straw. Hybrid poplar, dan cornstover (BB 5,8

ton/hari)

10 ML/tahun Biogasol Proses

35 GreenField Ethanol corn cobs, corn residue, wood pulp

- - Hydrolysis and fermentation continuously

Membran

36 American Process (AVAPTM process)

wood - Fractionation (Digester)

Hidrolisis asam hemiselulosa, hidrolisis enzimatik selulosa, dan

fermentasi

-





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5. KESIMPULAN DAN SARAN

5.1. KESIMPULAN

1. Teknologi konversi produksi bioetanol lignoselulosa telah mencapai tahap matang (matur).

Para pengembang teknologi telah mencapai pengembangan produksi skala pilot dan

demonstrasi, dan tengah berproses untuk membangun skala komersial pertama bioetanol

lignoselulosa pada tahun 2012-2013.

2. Pengembangan bioetanol lignoseluosa jalur biokonversi umumnya berbasis proses

fermentasi heksosa dan pemurnian etanol seperti pada proses komersial yang telah

dioperasikan secara komersial. fokus para pengembang diarahkan pada (1) perlakuan

awal, (2) pengembangan enzim, (3) fermentasi pentose, (4) proses integrasi, dan (5)

reduksi harga produksi.

3. Karakteristik bahan bakau menentukkan piliah perlakuan awal yang tepat. Perlakuan awal

yang optimal (hemat biaya dan energi) dan menghasilkan gula seoptimum merupakan

salah satu kunci komersialisasi bioetanol selulosa.

4. Hidrolisis polisakarida menjadi gula yang dapat difermentasi secara efisien menjadi

tantangan pengembangan metoda hidrolisis asam dan enzimatik.

5. Teknik fermentasi harus disesuaikan dengan karakteristik mikroorganisme dan tipe bahan

baku (konsentrasi gula yang dihasilkan)

6. Pemanfaatan produk samping perlu dilakukan secara cermat. Di samping untuk

mengurangi limbah, langkah ini dapat meningkatkan perolehan gula.

7. Teknologi pengembangan yang hampir mendekati skala komersial dan diuji pada skala

pilot dan demonstrasi adalah IOGEN, Chemtex (PROESATM), SEKAB, Sud-Chemie (Sun

liquids TM) dan

5.2. SARAN

1. Karakteristik bahan baku menentukan pilihan teknologi proses perlakuan awal dan

sakarifikasi untuk produksi bioetanol lignoselulosa. Oleh karena itu, karakterisasi bahan

baku dan pengujian perlakuan awal harus dilakukan secara memadai untuk menentukan

pilihan teknologi biomassa.





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2. Proses integrasi dalam pengembangan bioetanol lingnoselulosa dengan industri yang

sudah ada penting untuk menunutun dan meningkatkan potensi ekonomi bioetanol

lignoselulosa. Sebagai contoh, instalasi pemroses bagas menjadi bioetanol di industri gula

atau instalasi pemroses tandan kosong sawit di pabrik pengolahan kelapa sawit. Konsep

ini merupakan proses pemanfaatan optimum seluruh komponen bahan baku menjadi

beragam produk yang berguna, dan dikenal sebagai biorefineri.

6. DAFTAR PUSTAKA

Kumar, D., Murthy, G.S., Impact of pretreatmnt and downstream processing technologies on economics and energy in cellulosic ethanol production, Biotechnology for Biofuels, 4 (2011) 1-19.

Kumar, S., Singh, S.P., Mishra, I.M., Adhikari, D.K., Recent advances in production of bioethanol from lignocellulosic biomass, Chemical Engineering and Technology, 32 (2009) 517-526.

Limayem, A., Ricke, S.C., Lignocellulosic biomass for bioethanol production: Current perspectives, potential issues and future prospects, Progress in Energy and Combustion Science, 38 (2012) 449-467.

Mosier, N., Wyman, C., Dale, B., Elander, R., Lee, Y.Y., Holtzapple, M., Ladisch, M., Features of promising technologies for pretreatment of lignocellulosic biomass, Bioresource Technology, 96 (2005) 673-686.

Sarkar, N., Ghosh, S.K., Bannerjee, S., Aikat, K., Bioethanol production from agricultural wastes: An overview, Renewable Energy, 37 (2012) 19-27.

Sun, Y., Cheng, J., Hydrolysis of lignocellulosic materials for ethanol production: A review, Bioresource Technology, 83 (2002) 1-11.

Taherzadeh, M.J., Karimi, K., Acid-based hydrolysis processes for ethanol from lignocellulosic materials: A review, BioResources, 2 (2007) 472-499.

Taherzadeh, M.J., Karimi, K., Enzyme-based hydrolysis processes for ethanol from lignocellulosic materials: A review, BioResources, 2 (2007) 707-738.

Taherzadeh, M.J., Karimi, K., Pretreatment of lignocellulosic wastes to improve ethanol and biogas production: A review, International Journal of Molecular Sciences, 9 (2008) 1621-1651.

Thane, P., Cellulosic ethanol becoming reality, in: Biofuels International, 2012, pp. 36-40.

Yang, B., Wyman, C.E., Pretreatment: The key to unlocking low-cost cellulosic ethanol, Biofuels, Bioproducts and Biorefining, 2 (2008) 26-40.





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7. LAMPIRAN

LAMPIRAN – 1 Deskripsi Singkat Proses Teknologi Produksi Bioetanol Lignoselulosa dan

Status Pengembangannya (Jalur Biokonversi)

LAMPIRAN – 2 Daftar Pengembangan Bioetanol Lignoselulosa di Asia, khususnya Asia

Tenggara





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LAMPIRAN – 1

Deskripsi Singkat Proses, Diagram Blok Proses, Status dan Rencana

Pengembangan, dan Daftar Paten Pengembang Teknologi Produksi

Bioetanol Lignoselulosa (Jalur Biokonversi)

ABENGOA1. Deskripsi Singkat

Lisensor Abengoa Bioenergy New TecnologiesLokasi York, Nebraska, Amerika SerikatBahan Baku LignoselulosaInput 330 ton/tahun; 520.000 ton/tahunProduk EtanolTahap Pengembangan Pilot: 75 ton/tahun; 0,02 juta galon/tahun (2007)

Demo:Komersial: 56 juta galon/tahun; 210 ML/tahun

Status dan Rencana Pengembangan

Skala pilot beroperasi pada tahun 2007.

Deskripsi proses ringkas Fasilitas pilot yang sangat fleksibel dengan pengujian konfigurasi proses yang sangat bervariasi (steam explosion batch vs kontinu, fraksionasi biomassa yang berbeda tingkat dan teknik, fermentasi C5/C6 terpisah atau ko-fermentasi). Fasilitas komersial dicapai dengan pemanasan batch kontinu dan proses fermentasi

Website http://www.abengoabioenergy.com

Lisensor Abengoa Bioenergy , Biocarburantes Castilla y Leon, Ebro PulevaLokasi Babilafuente, Salamanca, SpanyolBahan Baku Lignoselulosa; steam explosion, gandung/jerami gandum, residu jagungInput 25.000 ton/tahunProduk EtanolTahap Pengembangan Pilot:

Demo: 4.000 ton/tahun; 1,32 juta galon/tahun (5000 kL)Komersial: -


Konstruksi skala demo selesai pada Desember 2008 dan mulai beroperasi sejak September 2009. Skala komersial direncakan untuk beberapa tahun ke depan.

Deskripsi proses ringkas Teknologi hidrolisis enzimatik. Etanol yang diproduksi didistilasi hingga konsentrasi 42%, dipekatkan, dan kemudian didehidrasi.


Lisensor Abengoa Bioenergy Biomass of Kansas, LLCLokasi Hugoton, Kansas, Amerika Serikat


http://www.abengoabioenergy.com/





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Bahan Baku LignoselulosaInput 1.000 ton/hariProduk Etanol, listrik ko-generasiTahap Pengembangan Pilot: -

Demo:-Komersial: 25 juta galon/tahun; 100 ML/tahun


Skala komersial mulai dibangun pada Juli 2011 dan direncanakan akan beroperasi pada Juni 2013.

Deskripsi proses ringkas Steam explosion digabungkan dengan fraksionasi biomassa, fermentasi C5/C6, distilasi untuk etanol recovery. Panas dan energi disediakan melalui gasifikasi biomassa.


2. Diagram Blok Proses

Gambar A.1.L1.1 Skema diagram blok bioetanol generasi kedua ABENGOA






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3. Status dan Rencana Pengembangan

Gambar A.1.L1.2 Rencana pengembangan dan implementasi bioetanol generasi kedua ABENGOA





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4. Daftar Paten Teknologi Bioetanol Lignoselulosa Milik ABENGOA

No Paten Tanggal Pendaftaran (Filling Date)

Judul Ringkasan

WO/2009/079183A1 2008-11-26 Improved quality and value of co-products of the ethanol production industry

A process for improving the nutritional quality of a feed co-product, resulting from the fermentation of a grain, sugar beets, or sugar cane to produce ethanol. The process comprises combining water, a source of nitrogen, a source of phosphorus, a feed co-product comprising a cellulose and/or a hemi-cellulose, and a microbe to form a fluid fermentation mixture suitable for submerged fermentation, wherein the feed co-product is derived from the fermentation of a grain, sugar beet, or sugar cane to produce ethanol and wherein the microbe is a microbe capable of breaking down the cellulose and/or the hemi-cellulose to one or more sugars and then utilizing the sugars to proliferate; fermenting the fluid fermentation mixture such that the microbe converts at least a portion of the cellulose and/or the hemi-cellulose into at least one sugar and uses the sugar to proliferate thereby increasing the concentration of microbes in the fermentation mixture.

US20110008489 2008-11-26

US20110262984 2010-08-24 Method for producing ethanol and co-products from cellulosic biomass

The present invention generally relates to processes for production of ethanol from cellulosic biomass. The present invention also relates to production of various co-products of preparation of ethanol from cellulosic biomass. The present invention further relates to improvements in one or more aspects of preparation of ethanol from cellulosic biomass including, for example, improved methods for cleaning biomass feedstocks, improved acid impregnation, and improved steam treatment, or “steam explosion.”

WO/2011/028554A1 2010-08-24

US20120045545 2010-11-04 High efficiency ethanol process and high protein feed co-product

A process is disclosed for producing a feed co-product by ethanol fermentation of plant matter comprising starch and another

WO/2011/056991A1 2010-11-04





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polysaccharide selected from the group consisting of hemicellulose and cellulose. The process comprises: (i) carrying out a primary fermentation process, distilling the primary fermentation mixture to form a primary feed co-product derived from the fermentation of the primary fermentation mixture and a primary distillate product comprising ethanol and (ii) carrying out a secondary fermentation process and distilling the secondary fermentation mixture to form the modified feed co-product and a secondary distillate product comprising ethanol.

US20120111321 2011-01-26 Method and apparatus for treating a cellulosic feedstock

Methods and apparatus for treating, pre-treating, preparing and conveying a cellulosic feedstock, such as for ethanol production, are disclosed. More specifically, the invention relates to methods and apparatus for treating a cellulosic feedstock by mixing and heating the cellulosic feedstock and/or by moistening and heating the cellulosic feedstock. The invention also relates to a holding tank, and a method of utilizing the holding tank whereby bridging may be reduced or eliminated and may result in a product stream from autohydrolysis or hydrolysis having an improved yield. The invention further relates to methods and apparatus for obtaining and conveying a cellulosic feedstock, which may be used for the subsequent production of a fermentable sugar stream from the cellulose and hemicellulose in the cellulosic feedstock wherein the fermentable sugar stream may be used for subsequent ethanol production. The invention also relates to a method and apparatus for withdrawing one or more feedstock stream from a holding tank.

US20110271875 2011-05-04 Process for recovery of values from a fermentation mass obtained in producing ethanol and products thereof

The present invention generally relates to processes for recovery of values from a fermentation mass obtained in producing ethanol. Further, the present invention relates to

WO/2011/140222A1 2011-05-04





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processes for the recovery of values from an inorganic- and lignin-containing mass.

US20120006320 2011-09-19 Method for producing ethanol and co-products from cellulosic biomass

The present invention generally relates to processes for production of ethanol from cellulosic biomass. The present invention also relates to production of various co-products of preparation of ethanol from cellulosic biomass. The present invention further relates to improvements in one or more aspects of preparation of ethanol from cellulosic biomass including, for example, improved methods for cleaning biomass feedstocks, improved acid impregnation, and improved steam treatment, or “steam explosion.”

WO/2012/103220A1 2012-01-25 Method and apparatus for treating a cellulosic feedstock

Methods and apparatus for treating, pre-treating, preparing and conveying a cellulosic feedstock, such as for ethanol production, are disclosed. More specifically, the invention relates to methods and apparatus for treating a cellulosic feedstock by mixing and heating the cellulosic feedstock and/or by moistening and heating the cellulosic feedstock. The invention also relates to a holding tank, and a method of utilizing the holding tank whereby bridging may be reduced or eliminated and may result in a product stream from autohydrolysis or hydrolysis having an improved yield. The invention further relates to methods and apparatus for obtaining and conveying a cellulosic feedstock, which may be used for the subsequent production of a fermentable sugar stream from the cellulose and hemicellulose in the cellulosic feedstock wherein the fermentable sugar stream may be used for subsequent ethanol production. The invention also relates to a method and apparatus for withdrawing one or more feedstock stream from a holding tank.





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AE BIOFUELS (AEMETIS)

1. Deskripsi Singkat

Lisensor AE BiofuelsLokasi Butte, Montana, Amerika SerikatBahan Baku Lignoselulosa; switchgrass, bibit rumput, jerami rumput, dan tangkai

jagungInput -Produk EtanolTahap Pengembangan Pilot: 500 ton/tahun; 0,16 juta galon/tahun (2008)

Demo:Komersial: 55 juta galon/tahun


Skala pilot beroperasi pada tahun 2008.

Deskripsi proses ringkas Hidrolisis pati selulosa pada temperatur ambien. Skala komersial menggunakan enzim ATSCH dan proses produksi enzim substrat padat. Proses ini menggunakan teknologi consolidated bioprocessing (CBP) untuk mengurangi tahap pemanasan dan pemakaian air.

Website http://www.aebiofuels.com


http://www.aebiofuels.com/




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AMERICAN PROCESS


Lisensor American Process IncLokasi Amerika SerikatBahan Baku Wood, Baggas tebuInput 52.000 ton/tahunProduk EtanolTahap Pengembangan Pilot:

Demo:Komersial: 13.000 ton/tahun; 4,5 juta galon/tahun


Plant ini dibangun pada akhir tahun 2008 dan dilanjutkan dengan coba start-up pada pertengahan tahun 2009. Plant selanjutnya dirancang untuk kapasitas 5-15 juta galon/tahun.

Deskripsi proses ringkas Tidak dilakukan fermentasi C5, menghindari produksi gipsum dan pembakaran lignin.

Website http://www.bbibioventures.com



http://www.bbibioventures.com/




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4. Daftar Paten Terkait Teknologi Bioetanol Lignoselulosa


Judul Abstrak

4318748 1980-04-09 Continuous process for saccharification of whole starchy materials

A continuous process is provided for effecting the acid hydrolysis of whole grains, e.g., corn, at high solids and in an economically desirable manner. The process produces glucose which is readily fermentable to produce ethanol.

4920055 1986-02-04 Conversion of alcohols to aldehydes and hydrogen peroxide by substrate and product tolerant methanol oxidases

Disclosed is a process for converting alcohols to aldehydes and hydrogen peroxide through the use of a methanol oxidase enzyme. The process involves introducing a lower alkyl or lower alkylene alcohol, such as methanol, ethanol, or allyl alcohol, as an aqueous solution into a reaction zone. Methanol oxidase enzyme that is stable in methanol concentrations of at least 0.5% and formaldehyde concentrations of at least 1.0% is also introduced into the reaction zone, which is maintained at an elevated pressure in contact with an oxygen-containing gas. The preferred methanol oxidase enzyme has the properties of the methanol oxidase enzyme produced by Hansenula polymorpha ATCC 34438. Both batchwise and continuous processes are disclosed. Also disclosed is a process in which a catalase is present in the reaction zone to decompose hydrogen peroxide as it is formed, so that the net reaction is the conversion of alcohol to aldehyde. In one aspect of that process, the aldehyde may be removed as a gas and subsequently condensed to an essentially pure liquid.

WO/ 1987-02-04 Conversion of alcohols A process for converting alcohols to aldehydes and





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1987/004725A1

to aldehydes and hydrogen peroxide by substrate and product tolerant methanol oxidases

hydrogen peroxide through the use of a methanol oxidase enzyme. The process involves introducing a lower alkyl or lower alkylene alcohol, such as methanol, ethanol, or allyl alcohol, as an aqueous solution into a reaction zone. Methanol oxidase enzyme that is stable in methanol concentrations of at least 0.5% and formaldehyde concentrations of at least 1.0% is also introduced into the reaction zone, which is maintained at an elevated pressure in contact with an oxygen-containing gas. The preferred methanol oxidase enzyme has the properties of the methanol oxidase enzyme produced by Hansenula polymorpha ATCC 34438. Both batchwise and continuous processes are disclosed. In one embodiment, a catalase is present in the reaction zone to decompose hydrogen peroxide as it is formed, so that the net reaction is the conversion of alcohol to aldehyde. In another aspect of the process, the aldehyde may be removed as a gas and subsequently condensed to an essentially pure liquid.

WO/1999/031315A1

1998-12-10 Separation and determination of cellulosic components from plant material

A method for separating cellulosic components from, and determining cellulosic component content of, plant material. Plant material and an electromagnetic active solvent, e.g. ethanol, are heated by means of electromagnetic radiation (e.g. microwave radiation), whilst the material and solvent are in contact each with the other and are located in a closed chamber. The temperature of the solvent and the vapour pressure in the chamber are increased thus to effect solution in the solvent of non-cellulosic components of the plant material. The cellulosic components of the plant material are isolated from the solvent and the solute therein. A gravimetric determination may then be made of the cellulosic component content of the plant material.

US20070141689

2005-03-18 Liquefaction process The present invention relates to method of liquefying starch-containing material, wherein the method comprises the steps of (a) treating the starch-containing material with a bacterial alpha-amylase at a temperature around 70-90° C. for 15-90 minutes, and (b) treating the material obtained in step (a) with an alpha-amylase at a temperature between 60-80° C. for 30-90 minutes. The invention also relates to a process of producing a fermentation product, preferably ethanol, comprising a liquefaction step carried out according to the liquefaction method of the invention.





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ARKENOL – BLUE FIRE ETHANOL


Lisensor ArkenolLokasi Orange, CA, Amerika SerikatBahan Baku Lignoselulosa; limbahInput 1 ton/hari; 190ton/hari (skala demo)Produk Etanol, ligninTahap Pengembangan Pilot :

Demo : 3,9 juta galon/tahunKomersial :


Skala pilot telah dibangun dan beroperasi sejak tahun 1994 hingga 2000. Uji skala pilot dilakukan oleh Arkenol kerja sama dengan JGS Jepang di Izumi, Jepang. Skala demo mulai dibangun pada tahun 2008 di Lancester, California.Proses ARKENOL dilanjutkan oleh BLUE FIRE Renewables. P

Deskripsi proses ringkas Hidrolisis asam pekat, ko-fermentasi C5 dan C6Website http://www.arkenol.com

http://bfreinc.com



http://www.arkenol.com/




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Gambar A.1.L1.3 Blok Proses Diagram Bioetanol Lignoselulosa Arkenol






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Pegembangan selanjutnya dilakukan oleh BlueFire Renewables

Gambar A.1.L1.4 Rencana pengembangan dan implementasi bioetanol generasi kedua ARKENOL

4. Daftar Paten Terkait Bioetanol Lignoselulosa Milik ARKENOL

No Paten Tanggal Pendaftaran

(Filling)

Judul Abstrak

US 5562777 1993-03-26 Method of producing sugars using strong acid hydrolysis of cellulosic and hemicellulosic materials

A economically viable method for producing sugars using concentrated acid hydrolysis of biomass containing cellulose and hemicellulose is disclosed. The cellulose and hemicellulose in the biomass is first decrystallized and then hydrolyzed to produce a hydrolysate containing both sugars and acid. Silica present in the biomass can then be removed for further processing. The remaining solids are then subjected to a second decrystallization and hydrolyzation to optimize the sugar yields. An improved method for separating the sugars from the acid in the hydrolysate is also disclosed. The resulting sugar stream can then be fermented, using an improved method which allows both hexose and pentose sugars to be fermented simultaneously.

US 5620877 1995-06-06 Method of fermenting sugars resulting from strong acid hydrolysis

An economically viable method of fermenting a mixture of sugars resulting from the acid hydrolysis of material containing cellulose and hemicellulose





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allows for the simultaneous fermentation of both pentose and hexose sugars. The sugar solution is mixed with a microbial organism known to produce a useful fermentation product, and the fermentation process is allowed to proceed for 3-5 days, during and after which the fermentation products are removed and purified.

US 5580389 1995-06-06 Method of separating acids and sugars resulting from strong acid hydrolysis


US 5782982 1995-06-07 Method of removing silica or silicates from solids resulting from the strong acid hydrolysis of cellulosic and hemicellulosic materials

A method of removing silica or silicates from solids results from the acid hydrolysis of materials containing cellulose and hemicellulose is disclosed. The method includes the steps of treating the solids with a metal hydroxide solution to produce an extract, reducing the pH of the extract to produce silicic acid, and removing the silicic acid from the extract.

US 5597714 1995-06-07 Strong acid hydrolysis of cellulosic and hemicellulosic materials

A economically viable method for producing sugars using concentrated acid hydrolysis of biomass containing cellulose and hemicellulose is disclosed. The cellulose and hemicellulose in the biomass is first decrystallized and then hydrolyzed to produce a hydrolysate containing both sugars and acid. Silica and silicates present in the biomass can then be removed for further processing. The remaining solids are then subjected to a second decrystallization if necessary and a second hydrolyzation to optimize the sugar yields.

US 5820687 1996-06-13 Method of separating acids and sugars using ion resin separation


US 5726046 1996-07-02 Method of producing sugars using strong acid hydrolysis

A economically viable method for producing sugars using concentrated acid hydrolysis of biomass containing cellulose and hemicellulose is disclosed. The cellulose and hemicellulose in the biomass is first decrystallized and then hydrolyzed to produce a





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hydrolysate containing both sugars and acid. Silica and silicates present in the biomass can then be removed for further processing. The remaining solids are then subjected to a second decrystallization if necessary and a second hydrolyzation to optimize the sugar yields.

US 5892107 1996-11-08 Method for the production of levulinic acid

A method of producing dehydration products from one or more 5-carbon or 6-carbon sugars includes reacting said one or more sugars at 40°-240 ° C. for 1 to 96 hours in the presence of 10-90% sulfuric acid, separating the reaction products, and recovering levulinic acid. The sugars can be generated from strong acid hydrolysis of biomass, such as rice straw, paper, cotton and other cellulosic materials.

US 6054611 1998-05-13 Method for the production of levulinic acid and its derivatives

A method of producing dehydration products from one more 5-carbon or 6-carbon sugars includes reacting said one or more sugars at 40-240° C. for 1 to 96 hours in the presence of 5-90% sulfuric acid, separating the reaction products, and recovering levulinic acid. The sugars are can be generated from strong acid hydrolysis of biomass, such as rice straw, paper, cotton and other cellulosic materials.

US 6743610 2001-03-30 Method to produce succinic acid from raw hydrolysates

A method for producing succinic acid from industrial-grade hydrolysates is provided, comprising supplying an organism that contains mutations for the genes ptsG, pflB, and ldhA, allowing said organism to accumulate biomass, and allowing said organism to metabolize the hydrolysate. Also provided is a bacteria mutant characterized in that it produces succinic acid from substrate contained in industrial-grade hydrolysate in a ratio of between 0.6:1 and 1.3:1 succinic acid to substrate.

US20030017559 2001-03-30 Method to produce succinic acid from raw hydrolysates

A method for producing succinic acid from industrial-grade hydrolysates is provided, comprising supplying an organism that contains mutations for the genes ptsG, pflB, and ldhA, allowing said organism to accumulate biomass, and allowing said organism to metabolize the hydrolysate. Also provided is a bacteria mutant characterized in that it produces succinic acid from substrate contained in industrial-grade hydrolysate in a ratio of between 0.6:1 and 1.3:1 succinic acid to substrate.

US20070148750 2005-02-08 Method for producing monosaccharides from biomass and monosaccharide production device

This monosaccharide production method is a method for producing monosaccharides from biomass having a first step 3 in which a raw material biomass is pretreated in 65 to 85 (w/w) % sulfuric acid at a temperature of 30 to 70° C., and a second step 4 in which the first step treatment product pretreated in the first step is subjected to saccharification treatment in 20 to 60 (w/w)% sulfuric acid at a temperature of 40 to 100° C.

US20080026101 2007-06-14 Food products Methods of producing a food product for mammals from the soluble by-product fraction of ethanol production are provided. One method comprises the step of incubating the treated soluble by-product fraction with an enzyme mixture capable of digesting complex polysaccharides to yield a food product having a fermentable sugar content of at least about 10% of the total carbohydrate content of the food product. Another method comprises the steps of





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incubating the unconcentrated soluble by-product fraction with an enzyme mixture capable of digesting complex carbohydrates followed by removal of at least a portion of the fatty acids from the digested material to render a food product having a fatty acid content of less than about 10% dry weight.

US20110065159 2010-06-24 BIOMASS HYDROLYSIS High-yielding method for chemical hydrolysis of lignocellulose into monosaccharides. The process of the invention can additionally be applied to cellulose, xylan and related biomass polysaccharides, such as galactan, mannan, or arabinan. The method is employed for hydrolysis of a biomass polysaccharide substrate. The process is carried out in an ionic liquid in which cellulose is soluble in the presence of catalytic acid at a temperature sufficiently high to initiate hydrolysis. Water is added to the reaction mixture after initiation of hydrolysis at a rate controlled to avoid precipitation yet avoid undesired sugar dehydration products such ad HMF. Hydrolysis product is useful as feedstock for fermentations including fermentation processes for ethanol, butanol and other fuels.

US20120167876 2011-12-29 ORGANO-CATALYTIC BIOMASS DECONSTRUCTION

The present invention provides processes for catalytic deconstruction of biomass using a solvent produced in a bioreforming reaction.

US20120167875 2011-12-29 SOLVOLYSIS OF BIOMASS USING SOLVENT FROM A BIOREFORMING PROCESS

The present invention provides processes for deconstructing biomass using a solvent produced in a bioreforming reaction.





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BBI BIO VENTURES LLC


Lisensor BBI BioVentures LLCLokasi Denver, Colorado, Amerika SerikatBahan Baku Lignoselulosa;pre-collected bahan baku yang tidak membutuhkan atau

sedikit perlakukan awalInput 52.000 ton/tahunProduk EtanolTahap Pengembangan Pilot:

Demo:Komersial: 13.000 ton/tahun; 4,5 juta galon/tahun


Plant ini dibangun pada akhir tahun 2008 dan dilanjutkan dengan coba start-up pada pertengahan tahun 2009. Plant selanjutnya dirancang untuk kapasitas 5-15 juta galon/tahun.

Deskripsi proses ringkas Tidak dilakukan fermentasi C5, menghindari produksi gipsum dan pembakaran lignin.

Website http://www.bbibioventures.com


http://www.bbibioventures.com/




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BIOGASOL


Lisensor BioGasol / AAU

Lokasi Ballerup, DenmarkBahan Baku Lignoselulosa; fleksibelInput 0,5 ton/tahunProduk Etanol, biogas, selulosa, hemiselulosa, ligninTahap Pengembangan Pilot: 10 ton/tahun, 40L/hari

Demo:Komersial:


Konsep teknologi diimplementasikan pada tahun 2006 di Denmark’s Technical Univeristy. Skala pilot beroperasi pada awal tahun 2011 dengan pembangunan selama 2 tahun (2008-2010).

Deskripsi proses ringkas Uji coba teknologi perlakuan awal dan fermentasi C5 pada skala pilot serta fleksibiltas bahan baku.

Website http://www.biogasol.com

Lisensor BioGasolLokasi Aakirkeby, Bornholm, DenmarkBahan Baku Lignoselulosa;macam-macam rumput, limbah kebun, jeramiInput 3,4 ton/tahunProduk Etanol, biogas, lignin, hidrogenTahap Pengembangan Pilot:

Demo: 4.000 ton/tahun; 5,2 ML/tahunKomersial:


Skala demo dalam perencanaan dan akan beroperasi pada tahun 2016. Uji skala pilot terletak pada Ballerup, Denmark.

Deskripsi proses ringkas Perlakuaan awal wet explosion (kombinasi steam explosion dan oksidasi basah), hidrolisis dan fermentasi C6 secara simultan, fermentasi C5 dalam immobilized reaktor. Daur ulang pemakaian air proses.

Website http://www.biogasol.com

Bisnis penjualan/lisensi proses teknologi bioetanol lignoselulosa (proprietary core technologies)

Perlakuan awal CarbofracTM

Fermentasi pentose PentcrobeTM Konsep proses (integrasi)


http://www.biogasol.com/

http://www.biogasol.com/




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Gambar A.1.L1.5 Skema digram blok bioetanol generasi kedua BIOGASOL





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Gambar A.1.L1.6 Rencana pengembangan dan implementasi bioetanol generasi kedua BIOGASOL

4. Daftar Paten


(Filling)

Judul Abstrak

US20100143988

2007-05-22 Thermoanaerobacter mathranii strain bg1

Strict anaerobic thermophilic bacterium belonging to the group of Thermoanaerobacter mathranii and mutants and derivatives thereof. The bacterium is particularly suitable for the production of fermentation products such as ethanol, lactic acid, acetic acid and hydrogen from lignocellulosic biomass.

WO/2007/134607A1

2007-05-22

US20090258 2007-06-28 Production of Production of fermentation products, such as





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(Filling)

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404 fermentation products in biofilm reactors using microorganisms immobilised on sterilised granular sludge

ethanol and lactic acid in biofilm reactors by microorganisms immobilised on sterilised granular sludge.

WO/2008/000809A1

2007-06-28

8236547 2009-07-22 Increased ethanol production in recombinant bacteria

The invention pertains to a recombinant bacterium with enhanced ethanol production characteristics when cultivated in a growth medium comprising glycerol. The recombinant bacterium comprises an inserted heterologous gene encoding glycerol dehydrogenase, and/or an up-regulated native gene encoding glycerol dehydrogenase. Particularly there is provided the recombinant bacterium BG1G1 of the Thermoanaerobacter mathranii species with an inserted heterologous gene encoding the E.C. 1.1.1.6 type, a NAD dependent glycerol dehydrogenase obtained from Thermotoga maritima.

US20110287501

2009-07-22

WO/2010/010116A1

2009-07-22

US20120100045

2010-01-12 Apparatus for rapid mixing of media and method

The present invention relates to an apparatus, which can be part of a pre-treatment system in a plant for the production of fuels, e. g. bio-ethanol, derived from plant biomass, e. g. first generation crops, such as grain, sugarcane and corn or second generation crops such as lignocellulosic biomass. The invention relates to an apparatus for processing, such as fluffing and mixing, at least two media, such as a solid, e. g. biomass, and a fluid, e. g. steam, so as to rendering the first medium susceptible to efficient receiving of energy and/or mass which is provided by localized release of the second medium. Although the description of the present invention focuses on biomass, it is envisaged that the invention is generally applicable to control the mixing of at least two media by crossing their stream of while dispersing at least one of them.

WO/2010/081477A1

2010-01-12

WO/2010/081476A1

2010-01-12 Method and apparatus for in-feeding of matter to a process reactor

The present invention relates to an apparatus, which can be part of a pretreatment (101) system in a plant for the production of fuels derived from plant biomass, e. g. first generation crops, such as grain, sugarcane and corn or second generation crops such as lignocellulosic biomass. The apparatus has the function of in-feeding and dewatering biomass so as to control water content in biomass before the dewatered biomass is introduced into a process reactor (215) in a plant for the production of, for example, bio-ethanol. The in-feeding and dewatering processes are carried out at a pressure higher than or equal to the





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(Filling)

Judul Abstrak

pressure inside the process reactor (215) providing the advantage of a fluid tight sealing of the process reactor and facilitating its continuous feeding.

WO/2011/076797A1

2010-12-21 Thermophilic thermoanaerobacter italicussubsp. marato having high alcohol productivity

Strict anaerobic thermophilic bacterium belonging to the group of Thermoanaerobacter italicus subsp. marato subsp. nov. and mutants and derivatives thereof. The bacterium is particularly suitable for the production of fermentation products such as ethanol, lactic acid, acetic acid and hydrogen from lignocellulosic biomass.





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BLUE SUGARS (d.h KL ENERGY)


Lisensor KL Energy Corporation / Blue SugarsLokasi Upton, Wyoming, Amerika SerikatBahan Baku Lignoselulosa; limbah kayu termasuk papan dan kertasInput 33.500 ton/tahunProduk EtanolTahap Pengembangan Pilot:

Demo: 4.500 ton/tahun; 1,5 juta galon/tahunKomersial: 10-15 kali lipat


Skala demo beroperasi pada tahun 2009

Deskripsi proses ringkas Teknologi perlakuan awal dengan enzim tanpa menggunakan asam.Website http://bluesugars.com http://www.klenergycorp.com


http://www.klenergycorp.com/

http://bluesugars.com/




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(a)

(b)

Gambar A.1.L1.7





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Judul Ringkasan

WO/2011/044292 2009-12-16 PROCESS FOR THERMAL-MECHANICAL PRETREATMENT OF BIOMAS

Disclosed is a process for the thermal-mechanical pretreatment of biomass. The process includes subjecting a biomass feedstock including fibers containing cellulose, hemicellulose and lignin, to thermal reaction under conditions exceeding atmospheric pressure, at a temperature exceeding ambient temperature, at a predetermined moisture content and for a predetermined amount of time. Subsequently, the pressure of said thermal reaction is reduced under conditions resulting in explosive decompression of said biomass. The decompressed biomass is then subjected to axial shear forces to mechanically reduce the size of the fibers of the biomass to obtain treated biomass. The resultant treated biomass has a high level of enzymatic digestability and a low concentration of degradation products.





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BORREGAARD


Lisensor Borregaard Industries LTDLokasi Sarpsborg, NorwegiaBahan Baku Lignoselulosa; sulfite spent liquor (SSL, 33% kadar kering) dari pulping

kayu cemaraInput 500.000 ton/tahunProduk EtanolTahap Pengembangan Pilot:

Demo:Komersial: 15.800 ton/tahun; 20 ML/tahun


Skala komersial beroperasi pada tahun 1930Proses integrasi dan pengembangan produk dari industry kayu

Deskripsi proses ringkas Pulp dari penggilingan kertas diproduksi dengan pemanasan potongan spruce dengan larutan panas asam kalsium bisulfit. Hemiselulosa dihidrolisis menjadi bermacam-macam gula selama proses pemanasan. Setelah SSL terkonsentratkan, gula diferentasi dan etanol didistilasi dalam beberapa tahap. Etanol 96% didehidrasi untuk mendapatkan etanol absolut

Website http://www.borregaard.com



http://www.borregaard.com/




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Gambar A.1.L1.8 Skema produksi terpadu bioetanol BORREGARD





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Gambar A.1.L1.9 Skema perlakuan awal BORREGARD

3.





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5.





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Judul Ringkasan

WO/2010/078930USP 20110250638

2009-12-16 LIGNOCELLULOSIC BIOMASS CONVERSION BY SULFITE PRETREATMENT

The present invention relates to a process for the production of second generation biofuels and/or sugar based chemicals - for example ethanol, butanol etc - and/or materials - for example plastics, single cell proteins etc. - together with sulfonated lignin from lignocellulosic biomass, in particular from lignocellulosic biomass comprising, among others, annual plants, agricultural waste, or wood. In particular, the present invention relates to a process for the production of sugar based chemicals, biofuels or materials together with sulfonated lignin from lignocellulosic biomass comprising the pretreatment of a lignocellulosic biomass in a sulfite cooking step.





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CHEMTEX – PROESA - MGM


Lisensor Mossi & Ghisolfi – Chemtex ItaliaLokasi Tortona, Piedmont, ItaliaBahan Baku Lignoselulosa; residu jagung, jerami, sekam, biomassa berkayuInput 200 ton/tahunProduk EtanolTahap Pengembangan Pilot: 50 ton/tahun (2009)

Demo:Komersial:


Skala pilot beroperasi pada tahun 2009

Deskripsi proses ringkas Konversi enzimatik untuk biomassa tertentu. Perlakuan awal, penanganan material yang telah diberi perlakukan awal dan hidrolisis dilakukan dalam peralatan yang didesain secara khusus

Website http://www.gruppomg.com




http://www.gruppomg.com/




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Paten berkait dengan detail PROESA belum ditemukan.





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DEDINI


Lisensor DEDINILokasi BrasilBahan Baku Bagas tebu dan JeramiInputProduk EtanolTahap Pengembangan Pilot: (2007)

Demo:Komersial:

Status dan Rencana PengembanganDeskripsi proses ringkas Proses terintegrasi dengan Bioetanol generasi pertama dari Sugar Cane,

Hidrolisis enzimatik, dari NovozymWebsite http://www.dedini.com.br/






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Judul Abstrak

WO/2010/085862A1

2009-01-30 Process of fermentation for production of bioethanol

'Process of fermentation for production of bioethanol', it refers to a process of alcoholic fermentation that uses strains of flocculant yeasts, in bioreactor of fixed tower kind, expanded bed or fluidized, with an unit of regeneration of biocatalytic coupled, using vegetable products that contain saccharose, glucose and fructose as raw material; the developed process is applied in the unit of fermentation of sugary materials containing saccharose, glucose and fructose, coming from vegetable sources of direct way or after hydrolysis, in the industries of production of alcoholic drunk, fuel alcohol, industrial alcohol and anhydrous alcohol; such process comprehends the following stages: 1) Preparation of the must, 2) Alimentation of the bioreactor, 3) Process of conversion, 4) Degassing of the fermented material, 5) Recovery of the biocatalytic, 6) Treatment of the biocatalytic, 7) Return of the biocatalytic to fermenter, and 8) Recovery of ethanol.

US20110232343

2009-06-24 Process for the recovery of water and energy from the processing of sugar cane in sugar and ethanol production mills

A process is proposed for recovery of water in the sugar cane processing in production mills of sugar and alcohol or only alcohol (ethanol). In the process, the thermal energy available in the exhausted steam from the electric energy generation turbines is transferred to the different mixed juice processing phases, with the reuse of the exhausted steam condensates in the boilers and of the other condensates, after using thermal energy, for imbibition, in the juice extraction phase, for cooling in the process, after passing through cooling towers, for other industrial uses and for possible treatment or use in the irrigation out of the productive system in the mill

WO/2009/155675A2

2009-06-24

WO/2009/155675A3

2009-06-24





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DuPONT Danisco Cellulosic Ethanol (DDCE)


Lisensor DDCE DuPont Danisco Cellulosic EthanolLokasi Vonore, Tennessee, Amerika SerikatBahan Baku Lignoselulosa; residu jagung; bonggol dan serat; switchgrassInput -Produk EtanolTahap Pengembangan Pilot: 750 ton/tahun; 0,25 juta galon/tahun

Demo:Komersial: 27,5 juta galon/tahun (2012)


Skala pilot dibangun pada tahun 2008 dan beroperasi pada tahun 2011. Lahan untuk plant skala komersial telah dibeli pada tahun 2012 di Nevada, Iowa

Deskripsi proses ringkas Hidrolisis enzimatikWebsite http://www.ddce.com



http://www.ddce.com/




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Gambar A.1.L1.10 Blok Diagram Proses Produksi Bioetanol DuPONT – Danisco (DDCE)






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FUTUROL PROCETHOL


Lisensor PROCETHOL 2GLokasi POMACLE, PerancisBahan Baku LignoselulosaInput -Produk EtanolTahap Pengembangan Pilot: 0,18 ML/tahun

Demo: 2.700 ton/tahun; 3,5 ML/tahunKomersial: 180 juta liter/tahun


Skala pilot dikonstruksi pada tahun 2008 dan beroperasi pada Oktober 2011. Skala demo dibangun di Tereos dan dikonstruksi sejak tahun 2011. Teknologi skala pilot yang telah matang diaplikasikan pada skala demo pada tahun 2015. Skala komersial diharapakan dapat diap pada tahun 2016.

Deskripsi proses ringkas Pengembangan enzim dan fermentasi bermacam-macam bahan baku secara efektif.

Website http://www.chemicals-technology.com/projects/futurol-project/






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GREEN FIELD ETHANOL






Judul Abstrak

7935514 2008-11-14

Genetically modified yeast strain

A polyploid transformed yeast cell comprising a deleted or disrupted GDH1 gene encoding an NADPH-dependent glutamate dehydrogenase. The polyploid yeast cell shows increased production of ethanol and reduced production of glycerol when compared with a control polyploid yeast cell.

US20090239276

2008-11-14

US20110229949

2011-03-23

US20100065128

2009-09-16

Cellulose pretreatment process

A process for the production of ethanol from biomass is disclosed. The process relates to the pretreatment of corncob biomass and includes the steps of exposing corncob to steam in a reaction vessel at an elevated temperature and reaction pressure for a preselected exposure time. Volatile compounds are continuously vented during pretreatment. The reaction pressure is released for explosive decomposition of the corncob biomass into fibrous solids and condensate. The exposure is preferably carried out at a temperature of 190-210° C. and a pressure of 190 psig to 275 psig and an exposure time of 3 to 10 minutes.

US20100159552

2009-12-22

Process for alcoholic fermentation of lignocellulosic biomass

A process for the production of ethanol wherein a hydrolyzed lignocellulosic biomass is fermented in the presence of a stillage residue. The fermentation of cellulosic hydrolysates is improved by adding prior to and/or during fermentation a stillage residue side stream from a corn starch-to-ethanol process as a nutrient source for the yeast organisms used in the





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fermentation. Stillage residues from the grain dry mill ethanol producing process, including the whole stillage, wet cake, thin stillage, and/or syrup are added to assist as a nitrogen and nutrient source for the fermentive processes. The stillage residue is produced by any grain-to-ethanol process.

WO/2010/071987A1

2009-12-22

Use of stillage residue as a nutrient source for fermentation of hydrolyzed lignocellulosic biomass to ethanol

A process for the production of ethanol wherein a hydrolyzed lignocellulosic biomass is fermented in the presence of a stillage residue. The fermentation of cellulosic hydrolysates is improved by adding prior to and/or during fermentation a stillage residue side stream from a corn starch-to-ethanol process as a nutrient source for the yeast organisms used in the fermentation. Stillage residues from the grain dry mill ethanol producing process, including the whole stillage, wet cake, thin stillage, and/or syrup are added to assist as a nitrogen and nutrient source for the fermentive processes. The stillage residue is produced by any grain-to- ethanol process.

US20100181034

2010-01-15

Removal of inhibitory compounds during pre-treatment of lignocellulosic biomass

A process for the pretreatment of lignocellulosic biomass, in particular during the production of ethanol from biomass. The process including a cooking step where the biomass is exposed to steam at elevated temperatures and pressures for a preselected period of time in a treatment vessel. During the process, volatile and liquid compounds are purged from the treatment vessel.

WO/2010/081227A1

2010-01-15

US20100263814

2010-04-07

Pretreatment of lignocellulosic biomass through removal of inhibitory compounds

A process for the pretreatment of lignocellulosic biomass is disclosed. The process is intended for use in connection with biomass to ethanol processes and is directed in particular to an economical removal of inhibitory compounds generated in biomass pretreatment, which are inhibitory to downstream hydrolysis and fermentation steps. The process includes the steps of heating the lignocellulosic biomass with steam to a preselected temperature, at a preselected pressure and for a preselected time to hydrolyze and solubilize hemicelluloses in the biomass; explosively decomposing the biomass into fibers; and extracting from the resulting reaction mixture a liquefied portion of the lignocellulosic biomass before or after explosive decomposition. The liquefied portion is extracted to remove compounds from the lignocellulosic biomass which are inhibitory to enzymatic cellulose hydrolysis and sugar fermentation to ethanol. For improved efficiency and economy, the inhibitory compounds are not completely removed. Furthermore, xylose has been found to be a good indicator compound for the general level of inhibitory compounds in the reaction mixture and the extraction step is therefore controlled on the basis of the xylose content in the reaction mixture. In particular, the extracting step is discontinued once a dry matter (dm) content of xylose, as monomer or oligomer, in the reaction mixture of 4% to 8% (w/w dm) is achieved. This most economically balances the practical need for inhibitory compound removal with the economical need to control and preferably minimize the costs of the overall ethanol production process.

WO/2010/121348A1

2010-04-07





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US20100313882

2010-04-23

Fractionation of biomass for cellulosic ethanol and chemical production

A process is defined for the continuous steam pretreatment and fractionation of corn cobs and low lignin lignocellulosic biomass to produce a concentrated cellulose solid stream that is sensitive to enzymatic hydrolysis. Valuable chemicals are recovered by fractionating the liquid and vapor stream composed of hydrolysis and degradation products of the hemicellulose. Cellulosic derived glucose is produced for fermentation to biofuels. A hemicellulose concentrate is recovered that can be converted to value added products including ethanol.

WO/2010/121367A1

2010-04-23

WO/2010/121367A8

2010-04-23

US20100269990

2010-04-23

Separation of reactive cellulose from lignocellulosic biomass with high lignin content

A process for separating the components of lignocellulosic biomass for the purpose of producing a pure reactive cellulose is disclosed. The process has two stages. In the first stage, the lignocellulosic biomass is pretreated with steam, with or without an acid catalyst, and then pressed, with or without the presence of an eluent, to remove hemicellulose and other impurities. In the second stage, the pretreated biomass is extracted with a solvent such as ethanol with or without acid catalysts in order to remove lignin and release a purified cellulose stream. The extracted cellulose is then rapidly decompressed to rupture the fibrous structure. The process provides a purified cellulose stream that is relatively easy to hydrolyze with enzymes and ferment to biofuels and other chemicals such as ethanol.

WO/2010/121366A1

2010-04-23

WO/2012/034230A1

2011-09-13

De icing formulation utilizing co-products from lignocellulose to bio fuel process

The use of a side stream and residue from the lignocellulose to ethanol process for use in preventing the formation of ice and in melting ice and snow on roadways. The future lignocellulose to ethanol industry will provide a significant proportion of these streams that provide an organic solution that when added to chloride salts of calcium, magnesium and sodium provides an improved environmentally friendly road deicing product with reduced corrosiveness and increased friction. A deicer composition of calcium chloride aqueous solution containing 25-38% by weight calcium chloride mixed up to 50% by volume of hemicellulose hydrolysis side stream can reduce the corrosivity of calcium chloride to 70% less that of a sodium chloride solution.

US20120111514

2011-11-04

Bagasse fractionation for cellulosic ethanol and chemical production

A process is defined for the continuous steam pretreatment and fractionation of bagasse to produce a concentrated cellulose solid stream that is sensitive to enzymatic hydrolysis. Valuable chemicals are recovered by fractionating the liquid and vapor stream composed of hydrolysis and degradation products of the hemicellulose. Cellulosic derived glucose is produced for fermentation to biofuels. A hemicellulose concentrate is recovered that can be converted to value added products including ethanol.

WO/2012/058776A1

2011-11-04

US20120115200

2011-11-08

Continuous process for the production of ethanol from lignocellulosic biomass

A continuous process for the recovery of ethanol from hemicellulose and cellulose from lignocellulosic biomass. Yield of fermentable sugars can be maximized by continuous operation of the pre-treatment system and careful selection of pretreatment conditions including the addition of only

WO/2012/061939A1

2011-11-08





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small amounts of dilute mineral acid and low pressure. With this approach, the xylose component that is mainly present in its unfermentable oligomeric form in known pre-hydrolysis Kraft processes can be recovered more efficiently and as a monomer that can be fermented by xylose fermenting yeasts and bacteria. Due to the use of only dilute acids, there is a very low loss of glucose and xylose hence very low production of toxic chemicals (e.g. HMF, furfural) in the pretreatment step. The resulting overall fermentation efficiency of both hexose and pentose sugars is 90% of the theoretical maximum.

WO/2012/061939A8

2011-11-08





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INBICON


Lisensor Inbicon (DONG Energy)

Lokasi Fredericia, DenmarkBahan Baku Lignoselulosa; jeramiInput 0,1 ton/tahunProduk Etanol, molase C5; biofuel padatTahap Pengembangan Pilot: -

Demo:Komersial:



Deskripsi proses ringkas Perlakuan awal hidrotermal, hidrolisis gravitasi tinggi, dan fermentasi ragiWebsite http://www.inbicon.com

Lisensor Inbicon (DONG Energy)Lokasi Fredericia, DenmarkBahan Baku LignoselulosaInput 1 ton/tahunProduk Etanol, molase C5; biofuel padatTahap Pengembangan Pilot: -

Demo:Komersial:



Deskripsi proses ringkas Perlakuan awal hidrotermal, hidrolisis gravitasi tinggi, dan fermentasi ragiWebsite http://www.inbicon.com

Lisensor Inbicon (DONG Energy)Lokasi Kalundborg, DenmarkBahan Baku Lignoselulosa; jerami gandumInput 30.000 ton/tahunProduk Etanol, molase C5; biofuel padatTahap Pengembangan Pilot: -

Demo: 4.300 ton/tahun; 1,5 juta galon/tahunKomersial: -


Skala demo dikonstruksi pada tahun 2007 dan beroperasi pada tahun 2009

Deskripsi proses ringkas Integrasi energi dengan stasiun dayaWebsite http://www.inbicon.com



http://www.inbicon.com/






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Gambar A.1.L1.11 Proses Produksi Bioetanol Lignoselulosa INBICON (1: Penyimpanan

biomassa, 2) Perlakuan Mekanik (grinding), 3) Perlakuan Awal Hydrothermal, 4) Hidrolisis

Enzimatik, 5) Fermentasi, 6) Penangkapan CO2, 7) Distilasi, 8) Pemisahan Padat/Cairan, 9)

Penyimpanan Tetes Gula (Molase), 10) Evaporasi, 11) Penyimpanan Etanol, 12) Pengeringan,

13)Kogenerasi






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4. Daftar Paten Terkait Teknologi Bioetanol Lignoselulosa INBICON





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(Filling)

Judul Abstrak

US7842490 2005-11-07 Enzymatic hydrolysis of biomasses having a high dry matter (DM) content

The present invention relates to a process for liquefaction and saccharification of polysaccharide containing biomasses, having a relatively high dry matter content. The present invention combines enzymatic hydrolysis with a type of mixing relying on the principle of gravity ensuring that the biomasses are subjected to mechanical forces, primarily shear and tear forces. Furthermore, the present invention relates to the further utilization of such processed biomasses, e.g. for subsequent fermentation into bio-ethanol, bio-gas, specialty carbohydrates for food and fees as well as carbon feedstock for processing into plastics and chemicals.

EP2154236A1 2005-11-07

EP2172568A1 2006-07-19 Method and apparatus for conversion of cellulosic material to ethanol

The present invention provides an apparatus and a method for conversion of cellulosic material, such as chopped straw and corn stover, and household waste, to ethanol and other products. The cellulosic material is subjected to continuous hydrothermal pre-treatment without addition of chemicals, and a liquid and a fibre fraction are produced. The fibre fraction is subjected to enzymatic liquefaction and saccharification. The method of the present invention comprises:- performing the hydrothermal pre-treatment by subjecting the cellulosic material to at least one soaking operation, and conveying the cellulosic material through at least one pressurised reactor, and subjecting the cellulosic material to at least one pressing operation, creating a fibre fraction and a liquid fraction;- selecting the temperature and residence time for the hydrothermal pretreatment, so that the fibrous structure of the feedstock is maintained and at least 80% of the lignin is maintained in the fibre fraction.

US8123864 2006-07-19

US20120138246

2012-01-31

8187849 2008-12-18 Non-sterile fermentation of bioethanol

A range of concentrations exists in which fermentation inhibitors derived from pretreatment of lignocellulosic feed stocks inhibit growth of lactic acid bacteria without affecting fermentive yeast. By optimizing levels of fermentation inhibitors to fall within this range, yeast fermentations of lignocellulosic biomass can be conducted under non-sterile conditions with ethanol yields comparable to those achieved under sterile conditions. Optimised inhibitor levels can be achieved by controlling the water/biomass ratio of a lignocellulosic biomass during and after pretreatment, for example by washing the fiber fraction of a previously pretreated lignocellulosic biomass with a pre-defined amount of fresh water or recycled process solutions. Crude extracts of liquid fraction or process solutions from pretreatment of lignocellulosic biomass can also provide an effective anti-bacterial treatment for first generation starch fermentations.

WO/2009/090480A2

2008-12-18

WO/2009/090480A3

2008-12-18

WO/2009/090480A4

2008-12-18

US20120122174

2012-01-24





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IOGEN


Lisensor Iogen Corporation

Lokasi Ottawa, Ontario, KanadaBahan Baku Lignoselulosa; jerami gandum, barley, dan oatInput 30 ton/hariProduk EtanolTahap Pengembangan Pilot:

Demo: 1.600 ton/tahun; 2 ML/tahun (2004)Komersial:



Deskripsi proses ringkas Perlakuan awal steam explosion, hidrolisis enzimatik yang terpisah dengan fermentasi menggunakan proses hidrolisis multitahap, ko-fermentasi, dan distilasi konvensional. Skala besar didesain dengan intrgrasi panas, daur ulang air, dan produksi produk samping.

Website http://www.iogen.com

Lisensor Iogen CorporationLokasi Birch Hills, Saskatchewan, KanadaBahan Baku Lignoselulosa; jerami gandum,dan lain-lainInput 750 ton/hariProduk Etanol 90.000 kL /tahunTahap Pengembangan Pilot:

Demo:Komersial: 70.000 ton/tahun; 90 ML/tahun


Perencanaan skala komersial dimulai sejak awal tahun 2008 dan beroperasi pada tahun 2011

Deskripsi proses ringkas Perlakuan awal steam explosion, hidrolisis enzimatik yang terpisah dengan fermentasi menggunakan proses hidrolisis multitahap, ko-fermentasi, dan distilasi konvensional. Skala besar didesain dengan intrgrasi panas, daur ulang air, dan produksi produk samping.

Website http://www.iogen.com



http://www.iogen.com/

http://www.iogen.com/




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Gambar A.1.L1.12 Diagram Alir Produksi Bioetanol Lignoselulosa IOGEN






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(Filling)

Judul Abstrak

5916780 1997-06-09 Pretreatment process for conversion of cellulose to fuel ethanol

An improved pretreatment of cellulosic feedstocks, to enable economical ethanol production by enzyme treatment. The improved pretreatment comprises choosing either a feedstock with a ratio of arabinoxylan to total nonstarch polysaccharides (AX/NSP) of greater than about 0.39, or a selectively bred feedstock on the basis of an increased ratio of AX/NSP over a starting feedstock material, and reacting at conditions that disrupt the fiber structure and hydrolyze a portion of the cellulose and hemicellulose. This pretreatment produces a superior substrate for enzymatic hydrolysis, by enabling the production of more glucose with less cellulase enzyme than any known procedures. This pretreatment is uniquely suited to ethanol





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(Filling)

Judul Abstrak

production. Preferred feedstocks with an AX/NSP level greater than about 0.39 include varieties of oat hulls and corn cobs.

6015703 1998-03-10 Genetic constructs and genetically modified microbes for enhanced production of beta-glucosidase

This invention relates to the genetic modification of a microbe to enhance its production of an enzyme, beta-glucosidase, that is important in the cellulose conversion process. The inventors have discovered genetic constructs that, when expressed in recombinant microbes, dramatically increase the amount of beta-glucosidase produced relative to untransformed microbes. The genetic constructs comprise a promoter, a xylanase secretion signal, and a mature beta-glucosidase coding region. The increased level of beta-glucosidase significantly increases the efficiency of hydrolysis of cellulose to glucose by cellulase enzymes, thereby enhancing the production of fuel ethanol from cellulose.

WO/1999/046362A1

1999-03-09

EP0884391A1

1998-06-04 Improved pretreatment process for conversion of cellulose to fuel ethanol

An improved pretreatment of cellulosic feedstocks, to enable economical ethanol production by enzyme treatment. The improved pretreatment comprises choosing either a feedstock with a ratio of arabinoxylan to total nonstarch polysaccharides (AX/NSP) of greater than about 0.39, or a selectively bred feedstock on the basis of an increased ratio of AX/NSP over a starting feedstock material, and reacting at conditions that disrupt the fiber structure and hydrolyze a portion of the cellulose and hemicellulose. This pretreatment produces a superior substrate for enzymatic hydrolysis, by enabling the production of more glucose with less cellulase enzyme than any known procedures. This pretreatment is uniquely suited to ethanol production. Preferred feedstocks with an AX/NSP level greater than about 0.39 include varieties of oat hulls and corn cobs.

EP0884391B1

US6090595

1998-06-04

1998-12-08

EP1320588A2

2001-09-25 Method for glucose production with a cellulase mixture comprising a modified cellulase

The present invention pertains to a method of converting cellulose to glucose by treating a pretreated lignocellulosic substrate with an enzyme mixture comprising cellulase enzyme and a modified CBHI, wherein the modified CBHI is present in the enzyme mixture at an amount relative to all CBHI-type enzymes from about 15% to about 100% (w/w), dpending upon the modified CBH1 used. The pretreated lignocellulosic substrate is selected from the group consisting of agricultural residues, residues after starch or sugar removal, dedicated ethanol crops, forestry products, and pulp and paper products, or combinations thereof.

EP1320588B1

2001-09-25

7419809 2001-09-25

WO/2002/024882A2

2001-09-25

7901511 2002-02-27 Method of processing lignocellulosic feedstock for enhanced xylose and ethanol production

The present invention provides a method of producing xylose from lignocellulosic feedstock. The method comprises disrupting lignocellulosic feedstock; leaching the lignocellulosic feedstock by contacting the feedstock with at least one aqueous solution for a period greater than about 2 minutes to produce a leached feedstock and a leachate; removing the leachate from the leached feedstock; acidifying the leached feedstock to a pH between

EP1364072A2

2002-02-27

EP1364072B1

2002-02-27

EP1767658A1

2002-02-27

EP2261381A 2002-02-27





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(Filling)

Judul Abstrak

2 about 0.5 and about 3 to produce an acidified feedstock, and; reacting the acidified feedstock under conditions which disrupt fiber structure and hydrolyze a portion of hemicellulose and cellulose of the acidified feedstock, to produce a composition comprising xylose and a pretreated feedstock. The xylose may be purified from the pretreated feedstock or it may be converted to ethanol with the pretreated feedstock.

EP2261381A3

2002-02-27

WO/2002/070753A2

2002-02-27

7993463 2007-01-31

US20070148751

2007-01-31

8012721 2003-03-05 Method for glucose production using endoglucanase core protein for improved recovery and reuse of enzyme

The present invention pertains to a method of converting cellulose to glucose by treating a pretreated lignocellulosic substrate with an enzyme mixture comprising cellulase enzyme and endoglucanase core proteins, wherein the endoglucanase core proteins are present in the enzyme mixture at an amount relative to all endoglucanases from about 35 wt. % to about 100 wt. % and wherein the endoglucanase cellulase enzymes are present in the enzyme mixture at an amount relative to the amount of CBH and EG enzymes from about 2 wt. % to about 50 wt. %. The pretreated lignocellulosic substrate is selected from the group consisting of agricultural residues, residues after starch or sugar removal, dedicated ethanol crops, forestry products, and pulp and paper products, or combinations thereof.

WO/2003/078644A2

2003-03-05

8057635 2007-06-28 Method and system for the large scale collection, preparation, handling and refining of ligno-cellulosic biomass

A system for collecting ligno-cellulosic biomass over a large area to enable the commercial refining of biomass from 2,500 to in excess of 50,000 tons of biomass per day to produce ethanol or other products. The biomass is collected at a series of collection points and then transported through a network of conduit “loops” interconnecting each of the collection points and the central refining plant. The water used to transport the biomass, as a slurry, is recovered and sequentially recycled in the same pipeline system to push the biomass slurry around the system in a “loop”.

WO/2009/015481A1

2008-07-31 Cellulase enzyme based method for the production of alcohol and glucose from pretreated lignocellulosic feedstock

A process for the production of glucose and ethanol from a pretreated lignocellulosicfeedstock is provided. The method comprises enzymatically hydrolyzing thepretreated lignocellulosic feedstock with cellulase enzymes to produce a hydrolyzateslurry comprising glucose and unhydrolyzed cellulose and fermenting the hydrolyzateslurry in a fermentation reaction to produce a fermentation broth comprisingalcohol. A process stream is obtained comprising unhydrolyzed cellulose, whichis then subjected to a denaturing step, preferably comprising exposing the unhydrolyzedcellulose to elevated temperatures, thereby producing a heat-treated streamcomprising the unhydrolyzed cellulose. The heat-treated stream comprisingunhydrolyzed cellulose is then further hydrolyzed





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(Filling)

Judul Abstrak

with cellulase enzymes tohydrolyze the cellulose to glucose.

US20100190226

2010-03-12 Process for producing a pretreated feestock

A process for producing ethanol from a pretreated feedstock is provided. The feedstock is selected from grasses, cereal straws, stover, and combinations thereof, and least about 80% of the feedstock has a particle length of between about 2 cm and about 40 cm. This process comprises wetting the feedstock in liquid, pressing the wet feedstock through one roll press or a series of roll presses to remove at least a portion of water and soluble substances from the wetted feedstock and to shear the feedstock to produce feedstock particles of a size suitable for pumping at a solids concentration of about 8% to about 20% when slurried. At least one roll press, or at least one roll press in the series of roll presses comprises rolls with circumferential v-shaped grooves. The pressed feedstock particles are slurried to produce a slurried feedstock having a consistency of between about 8% and about 20%, and the slurried feedstock pumped into a pretreatment reactor. Dilute acid pretreatment of the slurried feedstock is carried out at a temperature of 160° C. to 280° C.

US20110159560

2010-12-30 Modified yeast strains exhibiting enhanced fermentation of lignocellulosic hydrolysates

The present invention relates to novel xylose-fermenting yeast strains (for example, yeast of the genus Saccharomyces, e.g., S. cerevisiae) with an enhanced ability to ferment the xylose (and/or another pentose sugar) present in a lignocellulosic hydrolysate to a fermentation product(s) (for example, an alcohol (e.g., ethanol) or a sugar alcohol (e.g., xylitol)).

8157955 2011-02-04 Method and system for the large scale collection of ligno-cellulosic biomass

A system for collecting ligno-cellulosic biomass over a large area to enable the commercial refining of biomass from 2,500 to in excess of 50,000 tons of biomass per day to produce ethanol or other products. The biomass is collected at a series of collection points and then transported through a network of conduit “loops” interconnecting each of the collection points and the central refining plant. The water used to transport the biomass, as a slurry, is recovered and sequentially recycled in the same pipeline system to push the biomass slurry around the system in a “loop.” The outgoing and return legs of each loop optionally are located adjacent each other.

US20110188949

2011-02-04

US20120023814

2011-10-04 Method and system for the large scale collection, preparation, handling and refining of ligno-cellulosic biomass

A system for collecting ligno-cellulosic biomass over a large area to enable the commercial refining of biomass from 2,500 to in excess of 50,000 tons of biomass per day to produce ethanol or other products. The biomass is collected at a series of collection points and then transported through a network of conduit “loops” interconnecting each of the collection points and the central refining plant. The water used to transport the biomass, as a slurry, is recovered and sequentially recycled in the same pipeline system to push the biomass slurry around the system in a “loop”.





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LIGNOL


Lisensor Lignol Energy CorporationLokasi Burnaby, British Columbia, KanadaBahan Baku Lignoselulosa; residu hardwood dan softwoodInput 1 ton/hariProduk Etanol, ligninTahap Pengembangan Pilot: 80 ton/tahun; 0,1 ML/tahun

Demo:Komersial:


Skala pilot mulai dibangun pada tahun 2008 dan beroperasi pada tahun 2010

Deskripsi proses ringkas Proses delignifikasi untuk menghasilkan etnaol dan organosolv lignin untuk digunakan sebagai bahan bakar turbin gas.

Website http://www.lignol.ca


Gambar A.1.L1.13



http://www.lignol.ca/




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Judul Abstrak

US20080299628 2007-08-15 Continuous counter-current organosolv processing of lignocellulosic feedstocks

A modular process for organosolv fractionation of lignocellulosic feedstocks into component parts and further processing of said component parts into at least fuel-grade ethanol and four classes of lignin derivatives. The modular process comprises a first processing module configured for physico-chemically digesting lignocellulosic feedstocks with an organic solvent thereby producing a cellulosic solids fraction and a liquid fraction, a second processing module configured for producing at least a fuel-grade ethanol and a first class of novel lignin derivatives from the cellulosic solids fraction, a third processing module configured for separating a second class and a third class of lignin derivatives from the liquid fraction and further processing the liquid fraction to produce a distillate and a stillage, a fourth processing module configured for separating a fourth class of lignin derivatives from the stillage and further processing the stillage to produce a sugar syrup.

US20080295980 2008-01-18

7465791 2008-01-30

US20080299629 2008-01-30

WO/2008/144878A1

2008-04-25

8227004 2008-11-10

US20090117226 2008-11-10

US20090011484 2008-07-03 Concurrent saccharification and fermentation of fibrous biomass

A process for simultaneous saccharification and fermentation of a cellulosic solids fraction extracted from a lignocellulosic feedstock. The viscosity of the cellulosic solids fraction is reduced by intermixing with a liquid carbohydrate stream. A suitable liquid carbohydrate stream is a de-lignified liquids fraction that was previously separated from the solids fraction during processing of the lignocellulosic feedstock. Alternatively, the viscosity of the solids fraction may be reduced by commingling with a liquid carbohydrate stream comprising one or more monosaccharides. The reduced-viscosity cellulosic solids fraction is then commingled with a fermentative microbial inoculant and a cellulosic biomass-degrading enzyme composition. The commingled mixture is maintained in a pressurized reaction vessel under elevated temperatures to enable simultaneous enzymatic hydrolysis of the cellulosic solids to monosaccharides and fermentation of the monosaccharides to produce an ethanolic beer. The ethanolic beer is distillable for recovery of fuel-grade ethanol and a stillage that may be further processed.

WO/2009/003292A1

2008-07-04

WO/2010/081231A1

2010-01-15 Organosolv biorefining of whole sugar cane

An apparatus for processing sugar cane to concurrently produce sugar from cane juice, and ethanol and other co-products from bagasse. The apparatus comprises equipment for separating a cane juice stream and a fibrous bagasse from a sugar cane feedstock, equipment for refining the cane juice, equipment for processing the fibrous bagasse for recovery therefrom of a cellulosic pulp and a liquor stream, equipment for saccharifϊcation





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and fermentation of the cellulosic pulp to produce a fermentation beer therefrom, and equipment for recovery of an ethanol stream from the fermentation beer. Legacy sugar mills may be retrofitted with a bagasse biorefining apparatus to concurrently produce ethanol and co-products, with existing cane juice extraction and processing operations.





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MASCOMA (SunOpta)


Lisensor Mascoma CorporationLokasi Rome, New York, Amerika SerikatBahan Baku Lignoselulosa; potongan kayu; switchgrass, dan bahan baku lainnyaInput 5 ton/hariProduk Etanol, ligninTahap Pengembangan Pilot:

Demo: 500 ton/tahun; 0,125 juta galon/tahunKomersial:



Deskripsi proses ringkas Pengembangan ragi dan bakteri yang dimodifikasi sehinga menghasilka enzim dengan kuantitas yang besar. Consolidated Bioprocessing (CBP) mengkombinasikan 2 tahap yaitu sakarifikasi enzimatik dan fermentasi yang mengurangi jumlah enzim yang dibutuhkan

Website http://www.mascoma.com

Lisensor Frontier Renewable ResourcesDibeli oleh Mascoma

Lokasi Kincheloe, Michigan, Amerika SerikatBahan Baku Lignoselulosa; potongan kayuInput 700 ton/hariProduk Etanol, ligninTahap Pengembangan Pilot:

Demo:Komersial: 60.000 ton/tahunl 20 juta galon/tahun


Pembangunan skala pilot dimulai pada akhir tahun 2011 atau awal tahun 2012.

Deskripsi proses ringkas Consolidated Bioprocessing (CBP) mengkombinasikan 2 tahap yaitu sakarifikasi enzimatik dan fermentasi yang mengurangi jumlah enzim yang dibutuhkan

Website http://www.frontier-renewable.com/





http://www.mascoma.com/




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METSA BOARD (d.h. M-REAL-HALEIM AG)


Lisensor M-real Hallein AGLokasi Hallein, AustriaBahan Baku Lignoselulosa; sulfite spent liqour (SSL) dari pulping kayu cemaraInput 600.000 SSL (33% kadar kering) ton/tahunProduk EtanolTahap Pengembangan Pilot:

Demo: 12.000 ton/tahun; 15 ML/tahunKomersial:


Skala demo sedang direncanakan dan akan beroperasi pada tahun 2016

Deskripsi proses ringkas Pulp dari penggilingan kertas diproduksi dari pemanasan potongan cemara dengan larutan panas asam magnesium bisulfit. Setelah SSL terkonsentrasi dalam evaporator, SSL dibakar dalan boiler untuk menghasilkan steam dan listrik sedangkan magnesium oksida dan sulfur dioksida akan didaur ulang. Etanol hasil fermentasi didistilasi hingga konsentrasi 96% dan kemudian didehidrasi dengan molecular sieve untuk mendapatkan etanol absolut.

Website http://www.m-real.com



http://www.m-real.com/




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Gambar A.1.L1.14 Skema produksi bioetanol M-real Hallein AG







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PACIFIC ETHANOL


Lisensor Pacific EthanolLokasi Boardman, Oregon, Amerika SerikatBahan Baku Lignoselulosa; jerami gandum, residu jagung, residu poplarInput 5,8 ton/tahunProduk Etanol, biogas, ligninTahap Pengembangan Pilot:

Demo: 8.000 ton/tahun; 2,7 juta galon/tahun (2008)Komersial:


Skala demo dibanung sejak tahun 2008 dan beroperasi pada tahun 2010. Skala demo ini akan dikembangkan menjadi skala komersial pada tahun 2012.

Deskripsi proses ringkas Teknologi proses BioGasol dan teknologi enzim didiukung oleh Joint BioEnergy Institute.

Website http://www.pacificethanol.net


Gambar A.1.L1.15



http://www.pacificethanol.net/




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Judul Abstrak

7611716 2004-07-23

Method of processing seaweed

A method of processing seaweed, preferably a brown seaweed, comprises the following steps: (I) treating seaweed with an alcohol having one to six carbon atoms, preferably ethanol, to form an alcoholic fraction and an insoluble first seaweed residue; (II) separating the alcoholic fraction; (III) removing the alcohol from the alcoholic fraction to form a concentrate comprising biologically active low molecular weight compounds; (iv) extracting the first seaweed residue with an aqueous solution at a pH of less than 6 to form an aqueous first extract and an insoluble second seaweed residue; (v) optionally concentrating the first extract; and (vi) adjusting the pH of the resulting concentrated extract to a value in the range of 5 to 8 to obtain a first polysaccharide, fraction comprising a mixture of laminaran and fucoidan.

WO/2005/014657A1

2004-07-23

WO/2006/099593A2

2006-03-15

Carbon based electrocatalysts for fuel cells

Novel proton exchange membrane fuel cells and direct methanol fuel cells withnanostructured components are configured with higher precious metal utilizationrate at the electrodes, higher power density, and lower cost. To form a catalyst,platinum (735) or platinum-ruthenium nanoparticles are deposited onto carbon-basedmaterials, for example, single-walled, dual-walled, multi-walled and cup-stackedcarbon nanotubes (710). The deposition process includes an ethylene glycolreduction method (720). Aligned arrays of these carbon nanomaterials are preparedby filtering (740) the nanomaterials with ethanol. A membrane electrode assemblyis formed by sandwiching the catalyst between a proton exchange membrane (770)and a diffusion layer (796) that form a first electrode. The second electrodemay be formed using a conventional catalyst. The several layers of the MEA (790)are hot pressed (780) to form an integrated unit. Proton exchange membrane fuelcells and direct methanol fuel cells are developed by stacking the membrane electrodeassemblies in a conventional manner.

WO/2006/099593A3

2006-03-15

WO/2007/149643A1

2007-05-04

Formaldehyde free binder The present invention relates to a new formaldehyde- free binder composition, tothe related method of its use for making fibrous products (including glass fiberproducts and especially fiberglass insulation), and to the fiber products themselves.The present invention specifically relates to an





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aqueous binder compositioncontaining a mofified copolymer of maleic anhydride and a vinyl aromatic compoundsuch as styrene. The copolymer is modified by reaction with a primary alkanolamine(preferably mono ethanol amine (MEA) ). The modified copolymer is self-curingand cures as a consequence of cross-linking, esterification reactions betweenpendant carboxyls and hydroxyl groups on the solubilized (hydrolyzed) modifiedcopolymer chains. Additional polyol (s), including diethanolamine and/ortriethanolamine, can be added to the binder to increase either, or both the pHof the aqueous binder composition and the crosslink density of the cured binder.

7718832 2007-12-28

Combination catalytic process for producing ethanol from synthesis gas

A catalytic process selectively produces ethanol by contacting synthesis gas (syngas), composed primarily of hydrogen and carbon monoxide, with three catalysts within a reactor. The first catalyst is a hydrogenation promoter comprising Cu—Zn, Mo or Fe with an optional alkali metal additive and an optional support of aluminum oxide, silica, zeolite or clay. The second catalyst is a homologation promoter comprising one or more of the Group VIII metals in free or combined form with a co-catalyst metals consisting of Y or lanthanide or actinide series metals with optional additives and support. The third catalyst is a hydrogenation promoter. This series of catalysts improves the selectivity and yield for ethanol from syngas.





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POET-DSM


Lisensor POET - DSM

Lokasi Scotland, South Dakota, Amerika SerikatBahan Baku Lignoselulosa; serat jagung, bonggol dan tangkaiInput -Produk EtanolTahap Pengembangan Pilot: 60 ton/tahun; 0,02 juta galon/tahun

Demo:Komersial:



Deskripsi proses ringkas Hidrolisis enzimatikWebsite http://www.poet.com

Lisensor POETLokasi Emmetsburg, Iowa, Amerika SerikatBahan Baku Lignoselulosa; bonggol jagung, residu pertanianInput 280.000 ton kering/tahunProduk EtanolTahap Pengembangan Pilot:

Demo:Komersial: 75.000 ton/tahun; 25 juta galon/tahun


Perancangan skala komersial telah dilakukan sejak tahun 2006 dan akan beroperasi pada tahun 2013

Deskripsi proses ringkas Hidrolisis enzimatik. Didukung oleh DSM untuk teknologi konversi (ragi dan enzim) serta ko-fermentasi [gula C6 dan C5 (xylosa dan arabinosa)].

Website http://www.projectliberty.com



http://www.projectliberty.com/

http://www.poet.com/




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(a)

(b)

Gambar A.1.L1.16






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Judul Abstrak

EP2281898A1

2005-03-10 High protein distiller's dried grain and production thereof

The present invention relates to methods for producing high levels of alcohol during fermentation of plant material, and to the high alcohol beer produced. The method can include fractionating the plant material. The present invention also relates to methods for producing high protein distiller's dried grain from fermentation of plant material, and to the high protein distiller's dried grain produced. The method can include drying a co-product by ring drying, flash drying, or fluid bed drying. The present invention further relates to reduced stack emissions from drying distillation products from the production of ethanol.

7919291 2009-03-16 Method for producing ethanol using raw starch

The present invention relates to methods for producing high levels of alcohol during fermentation of plant material, and to the high alcohol beer produced. The present invention also relates to methods for producing high protein distiller's dried grain from fermentation of plant material, and to the high protein distiller's dried grain produced. The present invention further relates to reduced stack





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emissions from drying distillation products from the production of ethanol.

WO/2010/075541A2

2009-12-23 System for production of ethanol and co-products

A system for the production of ethanol and co-products is provided. The system facilitates an overall reduction in the use of energy, for example, by reducing the mass of wet solids supplied to a distillation system. The system also reduces the amount of energy used to dry the wet solids component of a fermentation product, for example, by increasing the ethanol concentration of the wet solids. The system also facilitates the recovery of co-products including bioproducts and other biochemicals extracted from components of the fermentation product. The solids component of the fermentation product may be dried and constituted into a meal that may be used for animal feed, among other uses.

WO/2010/075541A3

2009-12-23

US20100178675

2009-12-31 System for extracting protein from a fermentation product

A method of producing bioproducts from a feedstock in a system configured to produce ethanol and distillers grains from a fermentation product is disclosed. A system configured to process feedstock into a fermentation product and bioproducts including ethanol and meal is disclosed. A bioproduct produced from a fermentation product produced from a feedstock in a biorefining system is disclosed.

WO/2010/078528A1

2009-12-31 Zein composition A method of producing bioproducts from a feedstock in a system configured to produce ethanol and distillers grains from a fermentation product is disclosed. A system configured to process feedstock into a fermentation product and bioproducts including ethanol and meal is disclosed. A bioproduct produced from a fermentation product produced from a feedstock in a biorefining system is disclosed.

WO/2010/102060A3

2010-03-03 Pre-treatment of biomass for the production of ethanol

A system for the pre-treatment of biomass for use in a biorefinery to produce ethanol and other bioproducts is disclosed. The system comprises a method to pre-treat biomass to be used in a biorefinery to produce a fermentation product. The method comprises the steps of preparing the biomass into prepared biomass; and pre-treating the prepared biomass into pre-treated biomass by application of a dilute acid having a concentration of about 0.8 to 1.1 percent by weight at a temperature of about 130 to about 170 degrees Celsius for a period of time in a range of about 8 to 12 minutes.

WO/2010/102063A2

2010-03-03 System fro fermentation of biomass for the production of ethanol

A system for fermentation of biomass is disclosed. The system comprises a method for producing a fermentation product in a fermentation system from biomass that has been pre-treated and separated into a first component and a second component. The method comprises the steps of supplying the first component to the fermentation system; providing an ethanologen to the fermentation system; maintaining the first component and ethanologen in the fermentation system; and recovering the fermentation product from the fermentation system. A fermentation system configured to produce a fermentation product from biomass that has been pre-treated and separated





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into a first component and a second component is disclosed. The system comprises a first vessel configured to receive the first component and an ethanologen and a second vessel configured to propagate the ethanologen for supply to the first vessel. A biorefinery for producing a fermentation product from biomass is also disclosed. The biorefinery comprises a preparation system to prepare the biomass into prepared biomass; a pre-treatment system to pre-treat the prepared biomass with a dilute acid for separation into a first component from which pentose can accessed for fermentation and a second component from which hexose can be made available for fermentation; a first treatment system to treat the first component into a treated first component by removing removed components from the first component; a first fermentation system to produce a first fermentation product from the pentose; a distillation system to recover ethanol from the first fermentation product; and a treatment system to process removed components. The biomass comprises lignocellulosic material; the lignocellulosic material comprises at least one of corn cobs, corn plant husks, corn plant leaves and corn plant stalks. The first component comprises pentose; the pentose comprises xylose. The ethanologen is capable of fermenting xylose into ethanol.

WO/2010/102060A2

2010-03-03 System for pre-treatment of biomass for the production of ethanol

A system for the pre-treatment of biomass for use in a biorefinery to produce ethanol and other bioproducts is disclosed. The system comprises a method to pre-treat biomass to be used in a biorefinery to produce a fermentation product. The method comprises the steps of preparing the biomass into prepared biomass; and pre-treating the prepared biomass into pre-treated biomass by application of a dilute acid having a concentration of about 0.8 to 1.1 percent by weight at a temperature of about 130 to about 170 degrees Celsius for a period of time in a range of about 8 to 12 minutes. The system may also comprise a method to pre-treat biomass to be used in a biorefinery to produce a fermentation product. The method comprises the preparing the biomass into prepared biomass; and pre-treating the prepared biomass into pre-treated biomass by application of a dilute acid having a concentration of about 0.8 to 1.1 percent by weight at a temperature of about 130 to about 170 degrees Celsius for a period of time in a range of about 5 to 15 minutes. The fermentation product can be obtained by separating the pre-treated biomass into a liquid component comprising xylose and a solids component from which glucose can be made available and accessing xylose for fermentation into the fermentation product. A system for pre-treating biomass to be used in a biorefinery to produce a fermentation product may comprise an apparatus to preparing the biomass into prepared biomass; an apparatus for pre-treating the prepared biomass into pre-treated biomass by application of a dilute acid having a concentration of about 0.8 to 1.1 percent





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by weight at a temperature of about 130 to about 170 degrees Celsius for a period of time in a range of about 5 to 15 minutes; an apparatus for separating the pre-treated biomass into a liquid component comprising pentose available to be fermented and a solids component comprising cellulose from which hexose can be made available for fermentation and lignin; a fermentation system configured to produce the fermentation product; and a distillation system configured to recover ethanol from the fermentation product. The fermentation product comprises ethanol produced by fermentation of pentose and ethanol produced from the fermentation of hexose. The biomass comprises lignocellulosic material. The lignocellulosic material comprises corn cobs, corn plant husks, corn plant leaves and corn plant stalks.

US20100261243

2010-04-09 System for recycling water to facilitate the production of ethanol

A system for the production of ethanol is disclosed. The system comprises a system for recycling water in an ethanol production process. The system may comprise: a water supply that supplies water to the ethanol production process, a cooling tower system that supplies water to the ethanol production process, and a treatment system that supplies water to the ethanol production process. The treatment system may be a reverse osmosis system that supplies a retentate stream to the ethanol production process.

WO/2010/118369A1

2010-04-09

WO/2010/118369A4

2010-04-09

WO/2010/135366A1

2010-05-18 System for treatment of biomass to facilitate the production of ethanol

A method for treating fermented lignocellulosic biomass to be supplied to a distillation system for production of ethanol is provided. The method includes pre- treating lignocellulosic biomass into pre-treated biomass and separating the pre-treated biomass into a liquid component comprising sugars and a solids component comprising cellulose and lignin. The method also includes hydrolysing the solids component of the pre-treated biomass into a hydrolysed biomass comprising sugars and lignin and fermenting the hydrolysed solids component of the pre-treated biomass into a fermentation product comprising ethanol and lignin. The method also includes treating the fermentation product and distilling the treated fermentation product to recover the ethanol. The lignocellulosic biomass comprises cellulose, hemi-cellulose and lignin.

US20120129234

2011-11-18

US20110079219

2010-09-23 Biomass pretreatment A system for pre-treating biomass for the production of ethanol is provided. The system comprises a method for pre-treating biomass. The method comprises supplying biomass to a steaming bin, wherein the biomass is mixed with water, and inputting the steamed biomass to a first pretreatment reactor, wherein the steamed biomass comprises liquids and solids. The method also comprises removing a bulk of liquids from the solids and feeding the solids into a second pretreatment reactor. The method further comprises applying a pressure drop to the solids in the second pretreatment reactor, wherein the pressure drop opens up a structure of the solids, and sending the solids to a fermentation process for ethanol processing.

WO/2011/043935A1

2010-09-24





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US20110111085

2010-11-11 Methods and systems for producing ethanol using raw starch and fractionation

The present invention relates to methods for producing high levels of alcohol during fermentation of plant material, and to the high alcohol beer produced. The method can include fractionating the plant material. The present invention also relates to methods for producing high protein distiller's dried grain from fermentation of plant material, and to the high protein distiller's dried grain produced. The method can include drying a co-product by ring drying, flash drying, or fluid bed drying. The present invention further relates to reduced stack emissions from drying distillation products from the production of ethanol.

WO/2011/116317A1

2011-03-18 System for the treatment of biomass

A system for treating biomass for the production of ethanol is disclosed. A biorefinery for producing a fermentation product from biomass is disclosed. The biorefinery comprises a system for preparing the biomass into prepared biomass and a system for pre-treating the biomass into pre-treated biomass. The biorefinery comprises a separator, a first treatment system, a second treatment system, and a fermentation system. A method for producing a fermentation product from biomass is disclosed.

WO/2011/159915A1

2011-06-16 Fermentation of biomass A method for producing a fermentation product in a fermentation system from biomass that has been pre-treated and separated into a first component and a second component is provided. The method comprises preparing a slurry comprising: supplying the first component to the fermentation system; and providing an ethanologen to the fermentation system. The method also comprises adjusting the pH of the slurry to a range of about 4.5 to about 6.5, maintaining the first component and ethanologen in the fermentation system at a temperature of between about 25 and about 37 degrees Celsius, and recovering fermentation product from the fermentation system. The ethanologen is supplied to the fermentation system in a concentration of less than 2 grams of ethanologen on a dry basis per liter of slurry. The biomass comprises lignocellulosic material. The first component comprises pentose, which can comprise xylose. The ethanologen is capable of fermenting xylose into ethanol.

WO/2012/078882A1

2011-12-08 System and methods for collecting biomass

A system for collecting biomass for the production of ethanol is disclosed. Also disclosed is a method for collecting biomass. The method comprising: harvesting biomass with a combine, wherein a first portion of the biomass is substantially forced against the ground and a second portion of the biomass passes through the combine and forming bales comprising the second portion of the biomass. According to an aspect, the bales comprise a majority of the second portion of the biomass and a small part of the first portion of the biomass.

WO/2012/078885A2

2011-12-08 System and methods for feedstock quality assessment

Assessing quality of feedstock is provided and may be useful for determining quality of feed (such as corn kernels). The assessment determines endogenous enzyme activity within the feedstock, which correlates with total ethanol yields in raw starch hydrolysis (non-cooked) systems. In some embodiments, a sample containing flour (ground





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feedstock) is provided. In some cases, flour is diluted in water and buffered with a phosphate buffered solution. The buffered flour solution is contacted with a molecule, or fluorescent dye, such as fluorescein diacetate and/or difluorofluorescein that is altered by enzymatic (esterase) activity in a detectable fashion. Enzyme activity may be facilitated using an incubator. The detectible alteration may be measured using a fluorometer. In some embodiments, two incubations and fluorescence measurements can be performed. By subtracting the difference between the measured fluorescence, a fluorescence index may be found, which correlates with the endogenous enzyme activity in the feedstock sample.





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QTEROS






Judul Abstrak

7943363 2009-07-28 Methods and compositions for improving the production of products in microorganisms

Methods and compositions are provided for improving the production of products, such as fuel products like ethanol, in microorganisms. In particular, methods and compositions are described for improving ethanol production utilizing genes identified in Clostridium phytofermentans.

WO/2010/014632A2

2009-07-28

WO/2010/014632A3

2009-07-28

US20120196338

2011-04-14

WO/2010/104896A1

2010-03-09 Production of fermentive end products from clostridium sp.

In one aspect, methods to enhance the production of ethanol and other fermentive end products from a wide variety of feedstocks by Clostridium microorganisms, such as Clostridium phytofermentans are disclosed. A method of improving fermentation performance of Clostridium microorganisms, such as Clostridium phytofermentans through the use of a fed-batch strategy is described, as well as methods of producing fermentive end products, such as alcohols and/or chemicals by fermenting Clostridium microorganisms, such as Clostridium phytofermentans in the presence of fatty acid-containing compounds and/or at reduced pH.

WO/2010/104896A9

2010-03-09

US20100298611

2010-03-09

US20110230682

2010-03-22 Microorganisms with inactivated lactate dehydrogenase gene (LDH) for chemical production

This invention provides systems and methods for the increased production of ethanol and other chemical compounds by recombinant Clostridium species whereby the recombinant species are genetically-engineered to disrupt lactate dehydrogenase activity and to hydrolyze and ferment carbonaceous biomass and synthesize compounds of commercial value without production

WO/2011/116358A2

2011-03-18

WO/2011/116358A

2011-03-18





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3 of lactic acid.

WO/2011/088422A2

2011-01-14 Biofuel production using biofilm in fermentation

Compositions and methods for improving the efficiency of bio fuels and chemicals, e.g., ethanol, production is described. Increased yield was obtained by facilitating biofilm formation in a bioreactor coupled with a particular microbial species. Compositions and methods for increased processing of solid biomass in a bioreactor are also described.

WO/2011/088422A3

2011-01-14

WO/2012/083244A2

2011-12-16

WO/2011/133952A2

2011-04-22 New bacterium for production of chemicals and recombinants thereof

Provided is an isolated novel Gram-positive Clostridium bacterium, wherein the bacterium is an anaerobic, cellulolytic and xylanolytic mesophile that produces colonies that are beige pigmented, wherein the bacterium can use carbonaceous biomass as a carbon source and can ferment sugars into ethanol, biofuels, and other chemicals. Also provided are recombinant strains of several Clostridium species wherein sporulation is disrupted. Further provided are methods of using the bacterium and strains to degrade organic material and for use in industrial processes.

WO/2011/133952A3

2011-04-22

WO/2011/133984A2

2011-04-25

WO/2011/133984A3

2011-04-25

WO/2011/149956A2

2011-05-24 Methods for producing chemical products from fermentation byproducts

Disclosed herein are processes in which carbonaceous byproducts from corn-ethanol production or grain processing plants are utilized as feed streams to a novel consolidated bioprocessing (CBP) process. CBP processes described herein are additional processes to initial fermentation step of dry milling process. In CBP processes, microorganisms disclosed herein produce either sugars or ethanol or other chemicals directly from various feed streams that are fed into the CBP process. By employing CBP processes, thus, the total amount of product production is increased. In addition, CBP processes described herein have other benefits: decrease waste; lower production cost; and increase value of animal feeds or other valuable chemical products.

WO/2011/149956A3

2011-05-24





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SEKAB


Lisensor EtanolPiloten i Sveringe ABLokasi Örnsköldsvik, SwediaBahan Baku Lignoselulosa; umumnya potongan kayu dan bagas tebu, tetapi bahan

mentah lainnya akan diujikan seperti gandum, residu jagung, rumput-rumputan, limbah daur ulang, dan lainnya

Input -Produk EtanolTahap Pengembangan Pilot: 80 ton/tahun; 300 L/hari (2004)

Demo I: 4.500 ton/tahun; 6 ML/tahun (2011_Demo II : 50.000 ton/tahun; 60 ML/tahun (2011)Komersial: 120.000 ton/tahun; 150 ML/tahun (rencana 2012)


Skala pilot beroperasi pada tahun 2004. Skala demo I telah beroperasi sejak 2011. Skala demo II sedang direncanakan dan akan beroperasi pada tahun 2014. Skala komersial sedang direncanakan dan akan beroperasi pada tahun 2016.

Deskripsi proses ringkas Perlakuan awal dengan steam dan asam. Dua tahap hidrolisis asam encer dan enzimatik. Fermentasi dilakukan melalui SSF atau SHF tergantung dengan bahan baku dan produk samping yang akan digunakan

Website http://www.sekab.com



http://www.sekab.com/




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Gambar A.1.L1.17 Proses Produksi Bioetanol Lignoselulosa SEKAB (1:perlakuan awal, 2:

transportasi, 3:steaming, 4:prehidrolisis, 5: hidrolisis ensimatik, 6: fermentasi, 7: netralisasi,

8:detoksifikasi, 9: distilasi, 10:bioraktor )






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Judul Abstrak

EP2204433A1 2008-12-30 Ethanol-based fuel for compression engines

The present invention provides a fuel for a compression engine comprising a major amount of an ethanol liquid and minor amounts of an ignition improver and a viscosity increasing agent, wherein the viscosity of the fuel is 1.6 - 4.5 cSt at 40 °C and the ignition improver and the viscosity increasing agent are the same or different. Further, there is provided a use of the fuel, a use of a chemical compound as a viscosity increasing agent and a method a producing an ethanol-based fuel.

WO/2009/102256A2

2009-02-10 Method of production of ethanol from two different starting materials

The present invention provides a method of improving the ethanol yield in production of an ethanol-containing product from a lignocellulosic biomass and a sugar product containing fermentable sugars derived from a sugar-rich material. The method comprises treatment, involving hydrolysis, of said lignocellulosic biomass in one or more steps to obtain lignocellulose-derived treatment products including fermentable sugars; and fermentation, using a fermenting agent, of a mixture comprising at least part of said lignocellulose-derived treatment products and said fermentable sugars derived from said sugar-rich material to obtain the ethanol-containing product, wherein an amount of said sugar product is mixed with an amount of at least one of the following: (i) lignocellulose-derived material in the treatment; (ii) lignocellulose-derived treatment products from the treatment; and (iii) lignocellulose-derived treatment products in the fermentation, such that said fermentable sugars derived from said sugar-rich material and said at least part of said lignocellulose-derived treatment products are

WO/2009/102256A3

2009-02-10

WO/2009/102256A9

2009-02-10





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present in the mixture, and said amounts are controlled such that the fermenting agent is subjected to stress by lignocellulose-derived treatment products to the extent that the ethanol yield is improved. Further, a corresponding method using a starch-rich starting material is provided as well as a corresponding use, composition and system.

EP2270190A1 2009-07-03 Pretreatment of non-wood lignocellulosic material

The present disclosure provides a method for pre-treating non-wood lignocellulosic material containing less than 5 % (w/w) starch or sugar in a process for production of ethanol from lignocellulose, comprising the steps of: adding organic acid or organic acid-producing bacteria to the lignocellulosic material; storing the lignocellulosic material in the presence of the organic acid for a period of at least two weeks in an atmosphere of less than 5 % oxygen to obtain organic acid-impregnated material; and heating the organic acid-impregnated material at a temperature of at least 190 °C for a period of at least 5 minutes to obtain pre-treated lignocellulosic material, wherein no, or substantially no, inorganic acid or base, including SO2, is added in the method

WO/2010/071595A1

2009-12-21 Denaturant-containing, ethanol-based liquid

The present invention relates to a method for explicit denaturation of, and/or addition of denaturing capacity to other denaturants in, ethanol-based liquids, i.e. liquids that consist predominantly of ethanol, by addition of an organic chemical, characterized in that the added chemical has the formula (I) Wherein α is a single or double bond, β is a single or double bond, y is a single or double bond if both α and β are single bonds, v is a single bond if α or β is a double bond, and R1 and R2 are independently selected from the group consisting of hydrogen, methyl, ethyl, methoxy and ethoxy.

WO/2011/000712A1

2010-06-17 Pretreatment of non-wood lignocellulosic material

The present disclosure provides a method for pre-treating non-wood lignocellulosic material containing less than 5 % (w/w) starch or sugar in a process for production of ethanol from lignocellulose, comprising the steps of: adding organic acid or organic acid-producing bacteria to the lignocellulosic material; storing the lignocellulosic material in the presence of the organic acid for a period of at least two weeks in an atmosphere of less than 5 % oxygen to obtain organic acid-impregnated material; and heating the organic acid-impregnated material at a temperature of at least 160 °C to obtain pre-treated lignocellulosic material, wherein no, or substantially no, inorganic acid or base, including SO2, is added in the method.





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SUD CHEMIE (SUN LIQUIDS)


Lisensor Sud Chemie (Sun Liquids Process)Lokasi MunichBahan Baku Lignoselulosa; residu jagung, jeramiInputProduk EtanolTahap Pengembangan Pilot: 2009

Demo: 2012Komersial:


Skala pilot beroperasi pada tahun 2009 di Munich, Skala Demo dibangun di Straubing, diharapkan beroperasi pada tahun 2012

Deskripsi proses ringkas Inovasi: Produksi enzim terintegrasi; Co-fermentasi heksosa dan pentosaWebsite http://www.sud-chemie.com/scmcms/web/content.jsp?

nodeId=7760&lang=en

2.





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VERENIUM


Lisensor VereniumLokasi Jennings, Los Angeles, Amerika SerikatBahan Baku Lignoselulosa; bagas tebu, energy cane, produk kayu, dan switchgrassInput -Produk Etanol selulosaTahap Pengembangan Pilot: 150 ton/tahun; 0,05 juta galon/tahun

Demo: 4.200 ton/tahun; 1,4 juta galon/tahunKomersial: 30-60 juta galon/tahun


Skala pilot dioperasikan pada tahun 2007. Skala demo dioperasikan pada tahun 2008. Skala komersial dapat diabngun pada lokasi yang sama ataupun di Texas, Lousiana dan Florida.

Deskripsi proses ringkas Hidrolisis menggunakan steam dalam kondisi asam lemah, sakarifikasi enzimatik, fermentasi C5 dan C6 secara terpisah, dan distilasi. Residu distilasi dikumpulkan, didehidrasi, dan dibakar dalam boiler untuk integrasi energi dan steam.

Website http://www.verenium.com



http://www.verenium.com/




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Gambar A.1.L1.18 Proses Produksi Bioetanol Lignoselulosa Verenium







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WEYLAND AS


Lisensor Weyland ASLokasi Blomsterdalen, NorwegiaBahan Baku Lignoselulosa; asam pekat; coniferous wood sawdustInput 75 kg/jamProduk EtanolTahap Pengembangan Pilot: 158 ton/tahun; 53.000 galon/tahun (2009)

Demo: -Komersial: 6-8 juta galon/tahun


Skala pilot dibangun pada tahun 2008 dan dioperasikan sejak tahun 2010.

Deskripsi proses ringkas Proses asam pekat dan recovery asam pekatWebsite http://www.weyland.no





http://www.weyland.no/




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ZEACHEM


Lisensor ZeaChemLokasi Boardman, Oregon, Amerika SerikatBahan Baku Lignoselulosa; pohon poplar, gula, potongan kayuInput -Produk Etanol, campuran alkohol, bermacam-macam bahan kimiaTahap Pengembangan Pilot: 250.000 galon/tahun (2008)

Demo: -Komersial: 25-50 juta galon/tahun (Direncanakan 2012)


Skala pilot mulai direncanakan pada thaun 2008 serta dikonstruksikan pada tahun 2010. Skala pilot telah selesai dibangun pada awal tahun 2012. Skala komersial direncanakan akan dikonstruksi pada tahun 2012.

Deskripsi proses ringkas Proses hybrid. Fraksionasi biomassa, fermentasi asetogenik, asam asetat dikonversi menjadi ester dan dikonversi menjadi etanol dengan direaksikan dengan hidrogen. Residu lignin didapatkan dari fraksionasi dan digasifikasi.

Website http://www.zeachem.com

2.


http://www.zeachem.com/




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Gambar A.1.L1.19. Proses Produksi Bioetanol Lignoselulosa ZEACHEM




Judul Abstrak

EP1165820A4

2000-03-10 Process for producing ethanol

A process for producing ethanol including a combination of biochemical and synthetic





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conversions results in high yield ethanol production with concurrent production of high value coproducts. An acetic acid intermediate is produced from carbohydrates, such as corn, using enzymatic milling and fermentation steps, followed by conversion of the acetic acid into ethanol using esterification and hydrogenation reactions. Coproducts can include corn oil, and high protein animal feed containing the biomass produced in the fermentation.

EP2011879A2

2000-03-10

EP2011879A3

2000-03-10

6509180 2000-12-29US20030077771

2002-12-04

7351559 2005-06-297682812 2008-03-19US20090023192

2008-03-19

7964379 2010-01-26US20100273229

2010-01-26

US8236534 2011-05-05US20110275127

2011-05-05

EP1813590A1

2000-03-10 Process for recovering an ester

A process for producing ethanol including a combination of biochemical and synthetic conversions results in high yield ethanol production with concurrent production of high value coproducts. An acetic acid intermediate is produced from carbohydrates, such as com, using enzymatic milling and fermentation steps, followed by conversion of the acetic acid into ethanol using esterification and hydrogenation reactions. Coproducts can include corn oil, and high protein animal feed containing the biomass produced in the fermentation.

7074603 2002-10-09 Process for producing ethanol from corn dry milling

A process for producing ethanol by the conversion of carbohydrates from a corn dry milling process in which the bottoms fraction from distillation of ethanol in a conventional yeast fermentation is used in a process including a combination of biochemical and synthetic conversions. The process results in high yield ethanol production with concurrent production of high value coproducts. An acetic acid intermediate is produced from bottoms fraction, followed by conversion of the acetic acid into ethanol using esterification and hydrogenation reactions. Coproducts of the process include a high protein content solids fraction produced in the fermentation.

7507562 2006-01-24US20060127999

2006-01-24

US7888082 2008-11-26





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LAMPIRAN – 2

Daftar Pengembangan Bioetanol Lignoselulosa di Asia, khususnya Asia

Tenggara

INDONESIALisensor LIPI Puspitek Serpong Bekerjasama dengan KOICA Korea SelatanLokasi Puspitek SerpongBahan Baku Tandan Kosong SawitInputProduk EtanolTahap Pengembangan Pilot:

Demo:Komersial:


Skala pilot sedang dibangung di puspitek serpon, ker

Deskripsi proses ringkasWebsite





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CHINALisensor China Resources Alcohol Corporation (CRAC)Lokasi Zhaodong City, Heilongjiang, CinaBahan Baku Lignoselulosa; tangkai dan daun jagungInput -Produk EtanolTahap Pengembangan Pilot: 5.000 ton/tahun; 1,7 juta galon/tahun

Demo:Komersial: 1 juta ton/tahun; 330 juta galon/tahun


CRAC dibantu oleh SunOpta sejak September 2006 dan mulai beroperasi sejak akhir Oktober 2006. Skala komersial akan dilakukan pada tahun 2012 ini.

Deskripsi proses ringkas Perlakuan awal steam explosion didukung oleh paten SunOpta. Enzim yang digunakan dipasok oleh Novozymes.

Website -

Lisensor Shengquan GroupLokasi Jinan City, Shandong, CinaBahan Baku Lignoselulosa; bonggol jagung, selulosa produk samping proses produksi

furfuralInput -Produk EtanolTahap Pengembangan Pilot: 20.000 ton/tahun

Demo:Komersial: 20 juta galon/tahun


Fasilitas skala pilot sedang dalam proses konstruksi dan diharapkan telah siap pada Juli 2012. Skala komersial dalam tahap perencanaan dan pengembangan.

Deskripsi proses ringkas Pasokan enzim diperoleh dari Novozymes. Shengquan Group menanamkan modal untuk pembuatan enzim ‘khusus’ ini.

Website -

Lisensor Shandong Longlive Biotechnology CompanyLokasi Yucheng, Shandong, CinaBahan Baku Lignoselulosa; bonggol jagungInput -Produk Etanol; CO2 cairTahap Pengembangan Pilot: 10.000 ton/tahun

Demo:Komersial:


Skala pilot sedang dalam pembangunan.

Deskripsi proses ringkas Produksi cellulase on-site, proses sakarifikasi dan fermentasi secara simultan. Pengembangan teknologi bekerja sama dengan Shandong University.

Website -

Lisensor Henan Tianguan Fuel Ethanol Co., Ltd.Lokasi Nanyang City, Henan, CinaBahan Baku Lignoselulosa; jerami





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Input 1juta ton/tahunProduk EtanolTahap Pengembangan Pilot: 120.000 ton/tahun (12 plant @ 10.000 ton/tahun)

Demo:Komersial:


Konstruksi skala pilot dimulai sejaka akhir tahun 2011 dan direncanakan akan siap pada tahun 2014.

Deskripsi proses ringkas Produksi cellulase, direncanakan untuk menggunakan lignin produk samping dari produksi etanol selulosa

Website -





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JEPANGLisensor JGC CorporationLokasi Izumi, Kagoshima, JepangBahan Baku Lignoselulosa; limbah kayu dan pertanianInput -Produk EtanolTahap Pengembangan Pilot:

Demo: -Komersial: 8 juta galon/tahun; 3 ML/tahun


Skala pilot telah diujikan oleh Arkenol dan bertempat di Orange, CA, Amerika Serikat. Skala komersial mulai direncanakan dan dikonstruksi pada awal tahun 2007. Start-up komersial dioperasikan pada awal tahun 2009.

Deskripsi proses ringkas Teknologi hidrolisis asam pekat yang diadaptasi dari Arkenol.Website -

Lisensor Marubeni and Tsukishima Kikai Co., Ltd.Lokasi Osaka, JepangBahan Baku LignoselulosaInput -Produk EtanolTahap Pengembangan Pilot: 1,3 juta galon/tahun

Demo: 4 ML/tahunKomersial:


Skala pilot mulai beroperasi sejak Agustus 2007. Skala demo dioperasikan sejak tahun 2008.

Deskripsi proses ringkas Teknologi produksi diadaptasi dari teknologi Verenium.Website -





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THAILAND

Lisensor Marubeni and Tsukishima Kikai Co., Ltd.Lokasi Saraburi, ThailandBahan Baku Lignoselulosa; bagas tebu, sekam padiInput -Produk EtanolTahap Pengembangan Pilot:

Demo: 3 ML/tahunKomersial:


Skala pilot telah diujikan melalui plant di Osaka. Pembangunan skala demo di Thailand dimulai pada tahun 2008.

Deskripsi proses ringkas Teknologi produksi diadaptasi dari teknologi Verenium.Website -





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MALAYSIA

Lisensor Sime DarbyLokasi Selangor, MalaysiaBahan Baku Lignoselulosa; empty fruit bunches (EFB) kelapa sawit.Input 1,25 metrik ton EFB/hariProduk EtanolTahap Pengembangan Pilot: 35.000-50.000 galon/tahun

Demo:Komersial:


Skala pilot mulai direncanakan sejak akhir 2009 dan beroperasi sejak tahun 2011.

Deskripsi proses ringkas Teknologi produksi diadaptasi dari teknologi Inbicon (perlakuan awal hidrotermal dan hidrolisis enzimatik). Enzim yang digunakan dipasok oleh Novozymes.

Website -





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VIETNAM

Lisensor Phuc Yen CompanyLokasi Ho Chi Minh, City, VietnamBahan Baku Lignoselulosa; limbah padat kotaInput -Produk EtanolTahap Pengembangan Pilot:

Demo: 1 juta galon/tahunKomersial:


Skala demo mulai direncanakan sejak akhir tahun 2008.

Deskripsi proses ringkas Perlakuan awal kombinasi asam dan basa lemah. Teknologi diadaptasi oleh Agresti Biofuels.

Website -

Lisensor PetroVietnam Central BiofuelsLokasi Dung Quat, VietnamBahan Baku Lignoselulosa; bagas tebuInput -Produk EtanolTahap Pengembangan Pilot: 50.000 ton/tahun

Demo:Komersial:


Skala pilot direncanakan sejak tahun 2011.

Deskripsi proses ringkas Teknologi diadaptasi dari teknologi ChempolisWebsite -





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rekind a.1 reva

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