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Example Problem

Calculate the length of time between regeneration of catalyst

in a reformer operating

at the following conditions:

Liquid hourly space velocity (LHSV) 3.0 v/hr/v

Feed rate 5000 BPSD

Feed gravity 55.0API

Catalyst bulk density 50 lb/ft3

Hydrogen-to-feed ratio 8000 scf/bbl

Number of reactors 3

Catalyst deactivates after processing 90 barrels

of feed per pound of catalyst.

If the catalyst bed is 6 ft deep in each reactor,

what are the reactor insidediameters? Assume an equal volume of catalyst in each reactor.

Solution:

Time between regenerations:

5000 BPD = 1170 ft3/hr

Total catalyst = 1170/3 = 390 ft3

(390 ft3) (50 lb/ft3) = 19,500 lb

(19,500 lb) (90 bbl/lb)/5,000 bbl/day = 351 daysInside diameter:

Volume of catalyst per reactor = 390/3 = 130 ft3

Inside area = (130 ft3)/(6 ft) = 21.67 ft2

Inside diameter = 5.25 ft


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Catalytic reforming yield correlations


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Catalytic reforming yield correlations


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Catalytic reforming yield correlations.


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Catalytic reforming yield correlations.


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Catalytic reforming unit investment cost: 1999 U.S. Gulf Coast


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Catalytic Reforming Unit Cost DataCosts inc luded

1. All battery limit facilities required for producing 102 RON unleaded reformate

from a HSR naphtha sulfur-free feed2. Product stabilizer

3. All necessary control and instrumentation

4. Preheat and product cooling facilities to accept feed and release products at

ambient temperatures

Costs not inc luded

1. Cooling water, steam, and power supply

2. Initial catalyst charge3. Royalty

4. Feed fractionation or desulfurization

Catalyst charge

Initial catalyst charge cost is approximately $200/BPD of feed.

Royalt ies

Running royalty is about $0.05 to $0.10/bbl.

Paid-up royalty is about $50 to $100/BPD.Util i ty data (per bbl feed)

Steam,a lb 30

Power, kWh 3

Cooling water, gal 400

Fuel gas (LHV), MMBtu 0.3

Catalyst replacement, $ 0.10


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Following is a simplified conversion summary for a typical LSR cut. The

values are on a relative weight basis and do not account for the weight loss

resulting from hydrocracking to molecules lighter than pentane.


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Paraffin isomerization units (platinum catalyst type) investment cost:

1999 U.S. Gulf Coast.


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Table 10.3 Paraffin Isomerization with Platinum Catalysts Cost Data

Costs included

1. Feed drying

2. Drying of hydrogen makeup

3. Complete preheat, reaction, and hydrogen circulation facilities

4. Product stabilization

5. Sufficient heat exchange to cool products to ambient temperatures

6. Central controls

7. Paid-up royalty

Costs not included

1. Hydrogen source

2. Cooling water, steam, and power supply

3. Feed desulfurization

4. Initial catalyst charge, about $100/BPD of reactor feed

Royalt iesPaid-up royalty is about $90 to $160/BPD.

Utility data (per bbl fresh feed)

Power, kWh 1.0

Cooling water, gal (30F) 6001000

Fuel (LHV), MMBtu 0.20

Catalyst replacement, $ 0.05

Hydrogen makeup, scf 40

Table 10.4 Isomerization Yields

Component vol% on feed

C3 0.5

iC4 1.5

nC4 1.0

C5

C7 102.0

Costs not included


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1. Calculate the characterization factor (KW) of the feed.

2. Determine C5 gasoline volume yield from Figure 10.3.

3. Determine weight or volume yields of H2, C1 C2, C3, iC4, and nC4

from Figures 10.4, 10.5, and 10.6.

4. Calculate weight yield of all product streams except C5 gasoline.

5. Determine weight yield of C5 gasoline by difference.

6. Calculate API gravity of C5 gasoline.

7. Make sulfur and/or nitrogen balance if needed to determine H2S and

NH3 made and net hydrogen produced.

8. Estimate utility requirements from Table 10.2.


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