Download pdf - Butadien Production Scribd File.pdf

7/22/2019 Butadien Production Scribd File.pdf

1/22

LUMMUS CATADIENE

n-

Butane Dehydrogenation

Unit for Butadiene

Production

Technical Information


2/22

Table of Contents

Introduction ............................................................................................................................. 1

Technology Overview .............................................................................................................. 4


Feedstock and Product Specifications ...................................................................................... 6

Process Description and Process Flow Diagram ....................................................................... 7

Overall Material Balance ....................................................................................................... 10

Utility Consumption .............................................................................................................. 11

Catalyst and Chemical Consumption...................................................................................... 11

Environmental Considerations ............................................................................................... 11

Plant Operation ...................................................................................................................... 13

Plot Requirements.................................................................................................................. 14

Manpower Requirements ....................................................................................................... 15

Licensor Capabilities - Sole Source Responsibility ................................................................ 16

Experience ............................................................................................................................. 17Reference .............................................................................................................................. 20

CATADIENE Butane Dehydrogenation for Butadiene (8/11)


3/22

Introduction

CATADIENE is the

on ly one-step route

from n -butane to

butadiene

Lummus Technology, a CB&I Company (Lummus) is pleased topresent this technical information document to support your efforts tobuild a CATADIENE plant to produce butenes or/and butadiene. TheCATADIENE process is the only available technology to convert

normal butane to n-butenes and n-butenes to butadiene in a singlereaction step. By selecting our CATADIENE technology for a 1,3-

butadiene project, the producer is provided with the worlds most

widely used process backed by Lummus commitment to technical

excellence.

Unmatched Nineteen CATADIENE plants have been constructed worldwide with

Commercial a combined capacity in excess of 1,200,000 MTA of butadiene. TheExper ience most recent CATADIENE plant to start up is located in Tobolsk,

Russia. This plant, at a capacity of 180,000 MTA, continues tooperate reliably today. Most of the earlier CATADIENE plants wereshut down in the 1970s and 1980s when cheap byproduct butadienefrom steam cracking of liquid feeds made butane dehydrogenationuneconomical. A recent trend to lighter feedstocks has reduced theamount of byproduct butadiene and the butane dehydrogenation routeto butadiene is once again attractive in many locations.

The CATADIENE process was the forerunner to the widely accepted

CATOFIN technology and uses the same basic reaction system.Building on the well-proven CATADIENE system, CATOFIN wasdeveloped to meet the rapidly growing demand for propylene andisobutylene.

CATOFIN is currently used for about 65% of the w orlds

propane/isobutane dehydrogenation capacity. Commercial operatingexperience demonstrates the capability to exceed design capacity,yield, and catalyst life. The CATOFIN process is used for the worlds

largest dehydrogenation units in operation.

Two new i-C4CATOFIN projects have been awarded to Lummus in

2010 to produce isobutylene from isobutane.

A total of ten C3CATOFIN units have been licensed for production

of propylene. Licensed capacities range from 250 KMTA to 650KMTA.

Lummus is currently carrying out the basic design of a 600 KMTA C3

CATOFIN Unit for Tianjin Bohua Petrochemical Co., China. Inaddition, the basic design for a 650 KMTA C3CATOFIN Unit for Ibn

CATADIENE Butane Dehydrogenation for Butadiene 1


4/22

Introduction

CATOFIN has

worlds largestuni t in op erat ion

High Reliabi l i ty

Suppor t and

Commitment to

Technical

Advancement

Rushd, a SABIC Affiliate in Saudi Arabia has been completed. These

two designs represent the largest single train propane

dehydrogenation facilities in the world.

Lummus completed the basic design of a 500 KMTA C3CATOFIN

Unit for Kazakhstan Petrochemical Industries Inc. (KPI) in

Kazakhstan.

Lummus completed the design for a 545 KMTA C3CATOFIN Unit

for PL Propylene in Houston, USA. The Plant started up in 2010 andmet or exceeded all performance guarantees. This unit represents the

worlds largest propane dehydrogenation unit in operation.

Lummus has two operating units at 455,000 MTA propylene designcapacity. The Saudi Polyolefins (SPC) plant for production of

455,000 MTA of propylene came on stream in the first quarter of

2004. The Advanced Polypropylene Co. (APPC) plant came on

stream in February 2008. The plants continue to run above 100%

capacity.

The CATOFIN/CATADIENE dehydrogenation technology has

several hundreds of years of operating experience throughout the

world. These plant operations support the capability to exceed

capacity, overall yield, and catalyst life.

On-stream factors exceeding 97% are routinely achieved in

commercial operations. This is reflected in reduced plant size andmaintenance costs compared to competing technologies. TheCATADIENE process has no significant fouling problems and design

throughput is quickly achieved after a startup. The process uses fixedbed reactors containing a robust Sd-Chemie catalyst that is resistant

to the typical feed contaminants. Therefore, no feed treatmentfacilities are required for the CATADIENE process.

Effective technology transfer is a critical factor in the success of a

large project. Lummus is committed to supporting its licensees

through the entire life cycle of a project to ensure that the technologytransfer is successful. In addition to our process technology, Lummus

offers advanced process control, computer simulators, operating

training, detailed engineering, and start-up services.



5/22

Introduction

Lummus

technologies,

experience, and

capabil i t ies

ensure a

suc cessful project

Sud-Chemie, the exclusive supplier of the proprietary CATOFIN and

CATADIENE catalysts, and Lummus in its role as licensor, are firmly

committed to the continued development of the dehydrogenationtechnologies.

Because of its commercial success and the cost savings resulting from

its high yields, on-stream availability, and lower investment cost, theLummus dehydrogenation processes are the technology of choice in

todays market for the dehydrogenation of propane or butanes. The

selection of the CATADIENE technology will be instrumental in

attaining the financial and project goals targeted by your company.



6/22

Technology Overview

CATADIENE Using the CATADIENE process, butadiene can be produced from

Technology either a butane rich or a mixed butane/butylene stream.

OverviewThe processing scheme for the CATADIENE butadiene process is

shown in the overall process flow schematic and consists of thefollowing steps:

1. Dehydrogenation of the butane to make butadiene

2. Compression of reactor effluent

3. Recovery and purification of the product

The technology utilizes cyclic fixed-bed reactors with continuous

production and has demonstrated safe and reliable operation with

hundreds of years of operating experience. Features of the technology

include:

High tolerance to C4feed impurities

No halide (chlorine) facilities needed for reheat Inexpensive and robust catalyst No catalyst losses

Demonstrated catalyst life No hydrogen recirculation No steam dilution Technically sound and commercially proven process

equipment No significant fouling problems Minimum time required to achieve design throughput after a

shut-down Robust reactor design and internals Low sulfur injection (15 wppm on reactor feed)

The current CATADIENE design includes feedback from actual plantoperations, which results in improved reliability, operation and

efficiency.



7/22

Technology Overview

Process Flow

Schematic



8/22


Feedstock and

ProductSpecifications

The CATADIENE unit can be designed to process a wide variety of

feedstocks. A typical feedstock has the following characteristics:

Butane Feed

Component Wt%

N-Propane 3.0

N-Butane 94.5

C5+ 2.5

Lower purity butane streams can be handled in the CATADIENE

unit. However, any increase in the level of C3 and C5 impurities

would increase the amount of offgas since these impurities are

cracked to lighter hydrocarbons.

Butadiene extraction unit can be designed to produce the followinghigh purity product. The raffinate from the extraction unit, consistingof unconverted butane and butylenes is recycled to the CATADIENEunit for ultimate conversion to butadiene.

1,3-Butadiene Product

1,3 Butadiene 99.7 wt%

Propadiene < 5 ppm by wt

1,2 Butadiene < 20 ppm by wt

Acetylenes < 20 ppm by wt

NMP (BASF solvent) < 5 ppm by wt

By-Products

Offgas from the recovery section is produced as a by-product and is

normally burned as fuel. A significant portion of the hydrogen in the

offgas can be recovered at high purity in a pressure swing adsorption

(PSA) unit.



9/22


Process

Description and

Process FlowDiagram

The process description provided in this section can be followed more

clearly by referring to the Process Flow Schematic in the Technology

Overview section.

Process Overview

The CATADIENE process converts normal butane and n-butenes tobutadiene by successive dehydrogenation in a single step operationemploying a chromia-alumina catalyst. The unconverted normalbutane is recycled to the reactor section so that butadiene is the onlynet product. Operating conditions for the process are selected tooptimize the relationship among selectivity, conversion, and energy

consumption in the temperature and pressure range of 575-625oC and

0.14-0.24 bar absolute. Side reactions produce light hydrocarbongases in small quantities, along with hydrocarbons heavier than thefeed (polymer). The heaviest of these hydrocarbons are deposited ascoke on the catalyst.

A key feature of the process is that the heat is absorbed from the

catalyst bed by the reaction as dehydrogenation proceeds, gradually

reducing the temperature of the catalyst bed. This temperaturereduction, coupled with coke deposited on the catalyst decreases its

ability to produce the desired products. To remove coke and to restore

the necessary heat to the catalyst bed, periodic reheat of the catalyst

with hot air is required.

The process is carried out in a train of fixed-bed reactors that operateon a cyclic basis and in a defined sequence to permit continuousuninterrupted flow of the major process streams. In one completecycle, hydrocarbon vapors are dehydrogenated and the reactor is then

purged with steam and blown with air to reheat the catalyst and burnoff the small amount of coke that is deposited during the reactioncycle. These steps are followed by an evacuation and reduction andthen another cycle is begun. Cycle timing instrumentation sequencesthe actuation of hydraulically operated valves to control the operation.

The system is suitably interlocked to ensure safe operation of thevalves in sequence and prevent mixing of air and hydrocarbon gas.



10/22


Process Descri ption

Reaction Section

In the reaction section, butane is converted to butadiene while passing

through a catalyst bed.

Fresh butane feed is combined with recycle butane from the mixersettler unit. The total feed is then brought to reaction temperature inthe gas fired charge heater and sent to the reactors.

Non-selective cracking of hydrocarbons is minimized by injectingfuel gas during the reheat portion of the cycle to keep the heater outlet

temperature as low as possible. Hot effluent from the reactors flows toa pre-quench tower and the main quench tower where the vapor iscooled by in-direct contact with a circulating quench water stream.Make-up quench water stream may be added intermittently tomaintain system inventory.

In the reactors, the hydrocarbon on-stream period takes place at 0.14-

0.24 bar absolute pressure. While the system is still under vacuum,

the reactor is thoroughly purged with steam, thereby stripping residual

hydrocarbons from the catalyst and reactor into the recovery system.

Reheat of the catalyst takes place at slightly above atmospheric

pressure. Reheat air is supplied typically by a gas turbine or aircompressor and heated to the required temperature in a direct-firedduct burner before passing through the reactors. The reheat air serves

to restore both the temperature profile of the bed to its initial on-stream condition and catalyst activity, in addition to burning the cokeoff the catalyst. The reheat air leaving the reactors is used to generate

steam in a waste heat boiler.

When the reheat of a reactor is complete, the reactor is re-evacuated

before the next on-stream period. Prior to introducing butane feed,

hydrogen rich offgas is introduced to the reactor for a short time to



11/22


remove absorbed oxygen from the catalyst bed. This reduction step

decreases the loss of feed by combustion and restores the chrome on

the catalyst to its active state.

The reheat air stream leaving the reactors flows to the waste heat

boiler which generates and superheats high pressure steam.

Automatic Process Control

The reactor system consists of a train of reactors operating in a cyclicfashion. The cycle results in continuous uninterrupted flow ofhydrocarbon and air through the reactor system. The process streamsto the individual reactors are controlled by hydraulically-operated

valves. A central cycle timing device controls the operation of thesevalves. The cycle timer sends electrical control impulses in aprogrammed sequence and at precisely space intervals. Some of theimpulses actuate relays that control the motion of the valves, whileothers are used for testing reactor conditions and valve positions.Mixing of air and hydrocarbon streams is prevented by electricallyinterlocking both the valve operators and valve operations with keyreactor conditions.

The hydraulically-operated valves are of a special design, permittingfrequent operation with little maintenance. A seal valve furnishedwith the main valve actuator admits an inert gas seal to the valve

bonnet when the main valve is in the closed position. The seal gasprevents mixing of process streams if there should be any leakage

between the wedge and the seat. Inert gas such as N2or steam is used

for valve sealing. The main reactor valves are also equipped withlimit switches which, through relays, provide the necessary contactsfor valve actuation, position testing, valve interlocking and valveposition indication in the control room.

Compression Section

In this section, the cooled effluent gas from the quench tower flows to

the product compressor train where it is compressed in severalsuccessive stages to a suitable pressure for the operation of the

recovery section. For each stage, a compression ratio is selected to

optimize compressor performance and keep gas temperature low to

minimize polymer formation.

Any water that condenses after each stage of compression is separated

in the interstage knock-out drums. Additionally, a sodium nitrite

solution is circulated in the final stage suction drum as oxygenCATADIENE Butane Dehydrogenation for Butadiene 9


12/22


Overall Material

Balance

scavenger to aid in the prevention of polymer in the downstream gas

plant section.

The compressor discharge vapor is cooled and the resulting vapor-

liquid is separated in a flash drum. The reactor effluent condensate

and the uncondensed reactor effluent vapor streams both flow to the

recovery section.

Recovery Section

The recovery section removes inert gases and light hydrocarbonsfrom the compressed reactor effluent in absorber operating at 1 atmpressure and feed temperature. The absorber removes C3 and lighterhydrocarbons from the butanes and heavier material. Naphtha is usedas a solvent in the absorber which absorbed the other hydrocarbonsexcept H2 and C3. On the other hand, microscopic fraction of C3 is

also absorbed in Naphtha. This fraction can be neglected. C4s and

heavier components are sent to stripper. Naphtha recovery in thestripper is 99.99%. Make-up stream may be used to make the process

steady. C4s and heavier components are sent to the distillation

column where crude butadiene is recovered using butadiene tower(99.95% wt crude butadiene) and normal butane is further recycled tothe CATADIENE reactors. In purifier and ammonia still, NH3 andwater incoming flow rate is 0.2 times of the total entering mixture. At

the end of process- 1, 3 Butadiene is 98-99% is recovered inbutadiene purifier.

The following material balance is typical of the average performance

of the unit and is based on producing 125,000 MTA of 1,3-butadiene.

Butane Feed (97.8 wt%) 213,500 MTA

1,3-Butadiene Product 125,000 MTA

Light ends 68,75 MTA

C5+and coke 19,7 MTA

The light ends produced by the CATADIENE process can be usedwithin the unit as fuel. However, they contain significant amounts

of hydrogen, as well as C2and C3components which could berecovered for higher value uses.



13/22


UtilityConsumption

Catalyst and

ChemicalConsumption

Environmental

Considerations

The estimated overall normal utility requirements only for the

CATADIENE unit for processing a 97.8 wt.% butane fresh feed to

produce 125,000 MTA of 1,3-butadiene are summarized in thefollowing table.

Total Per Ton of Product

Power 140 kWhBoiler Feed water (BFW) 1.3 metric ton

Cooling Water 525 m

Fuel(2)

Net Gas Consumption 4.7 MWh

Notes:

1. Based on 10oC temperature rise.

2.Offgas and C 5+ streams from the CATADIENE unit areconsumed as fuel within the CATADIENE unit.

Catalyst Requi rements

The dehydrogenation reactors contain a mixture of chromia-alumina

catalyst and inert grain. The expected catalyst life is 1 - 2.5 years. The

inert material is recovered and reused when the catalyst is changed.

Annual Cost

The annual cost of catalyst and inert materials loaded into the reactors

(inert grain and alumina balls) based on producing 125,000 MTA of

butadiene is approximately $US 19 per metric ton of butadiene

product.

Chemical Requi rements

A sulfiding agent is added to the total reactor feed to passivate the

metals in the alternating oxidizing and reducing atmosphere in the

reactors. If the fresh and recycle feeds contain no sulfur, the

maximum addition rate is about 15 ppm.

Atmospheri c Emissions

There are two sources of process waste gas from the CATADIENEunit: the reheat effluent and the evacuation ejector effluent. Ifrequired, the reheat effluent can be sent to a thermal or catalyticincinerator to convert the trace amounts of hydrocarbon and carbonmonoxide present into carbon dioxide and water. Selective catalytic

reduction can also be applied for NOxreduction. The flue gas is



14/22


discharged to the atmosphere after being cooled in waste heat

recovery. The ejector effluent stream is discharged to atmosphere via

the waste heat recovery stack.

Flue gas from the charge heater is the only other continuous emissions

from the CATADIENE unit. Fugitive emissions from equipment are

minimized by the application of the following engineering practices:

All pumps in light liquid service are equipped with

dual mechanical seals.

All sampling connections are equipped with a closed purgesystem or closed vent system.All open-end valves or lines are equipped with a cap or plug.

Each vapor relief valve is tied into a flare system. Provisionsare made to depressure all equipment to the flare systemprior to opening for maintenance.

Spent Catalyst Di sposal

The CATADIENE catalyst operates in fixed-bed reactors so no losses

from attrition or breakage occur. The catalyst is not dangerous and

only normal precautions are necessary when unloading to prevent

losses and inhalation of dust. Tests on commercial CATADIENE

plants have shown that no catalyst dust is detectable in the emissions

from the plant.

The primary ingredients of CATADIENE dehydrogenation catalyst

are alumina and chromium oxide. Once the catalyst becomes spent, itsingredients can be utilized as raw material for metal industry and

refractory applications. Uses include the production of ferrochromium and other alloys for the specialty steel industry, as anadditive or conditioner for slags, and as an ingredient in the

production of refractory. Similar catalysts have been used in thealumina smelting industry to make certain chromium alumina alloys.

Lummus and Sud-Chemie can offer assistance for catalyst disposal.



15/22


Turndown

Plant Operation The CATADIENE unit can be operated economically at 60% of thedesign capacity. At this point, the limiting factor is usually turndown

capacity of the product compressor. Operating below 60% of capacity

is possible by use of recycle in the compression section, but this

requires increased energy costs for compression of the recycle.

Safety

The CATADIENE reactors operate on a cyclic basis. By use ofmultiple reactors, continuous flow of the major process streams isachieved. This type of system has been in continuous commercial

operation since 1944 when the first Houdry CATADIENE

unit wasplaced on stream for production of butadiene from butane.

The CATOFIN/CATADIENE unit operating dependability is widely

acknowledged by current licensees. The operating plants have

experienced in excess of 40 million reactor cycles without serious

mishap. This safety record is based on the very careful design of the

system.

The reactor system as well as the operation of all other items of majorequipment within a CATADIENE unit have been subjected to critical

reviews by technical experts within Lummus, using state-of-the-art

analysis techniques and methodology for process hazards analysis.This type of analysis is directed at identification and prevention of

undesired events and results in calculation of an average hazard ratefor the plant. The rate calculated for the CATDIENE process was

found to be well within the corporate goals established by majorchemical companies.

On-Stream Factor

Achieving a high on-stream factor is critical to the projects

economics. As mentioned above, the CATADIENE unit operating

dependability is widely acknowledged. All processing plants are onlyas reliable as their individual parts and all parts of a CATADIENE

plant have withstood the test of time, having maintained their

operating integrity.

The CATADIENE technology has repeatedly demonstrated on-stream

efficiencies well in excess of 97%. This proven record, as well as the

robust reactor design which withstands transient conditions and quick



16/22


Plot

Requirements

restarts, is a significant advantage over competitive PDH processes

which use fragile reactor internals.

Maintenance

Total maintenance costs for the CATADIENE unit, including

turnaround costs, but excluding the catalyst, are normally about 2% of

replacement capital cost. This compares favorably with the

maintenance costs in the refining industry.

An area of about 30,000 m2 will be sufficient for the ISBL

CATADIENE unit to produce 125,000 MTA of butadiene. The plotplan can be optimized based on site-specific limitations.



17/22

Manpower Requirements

Staffing

Staffing requirements for the CATADIENE units have beenestablished through Lummus experience. The following table

summarizes the personnel required to operate the complex.

Shift Day

Operations Foreman 1

Board Operator 2

Outside - Operator 1

Laboratory Supervisor 1

Laboratory Technician 1

Maintanance Technician 1



18/22

Licensor Capabilities Sole Source Responsibility

As licensor of the CATADIENE technology, Lummus can provide:

Feasibility studiesBasic design engineeringInterface with the detailed engineering contractorSupply of catalystTraining of client's personnel

Plant start-up services

Follow-up technical services after start-up

In addition, Lummus can provide the detailed engineering,

procurement and construction management. With engineering andproject execution centers strategically located around the world, our

team of experienced professionals stands ready to provide the latestprocess technologies and the following project-related services with

unequaled quality and satisfaction:

Preliminary estimates & scheduling

Project financing

Site surveys

Permitting

Environmental ServicesDetailed designEstimating and

scheduling Worldwideprocurement ConstructionProject management

This sole source responsibility greatly simplifies the coordination of

the project work, thus enabling a faster schedule to be achieved, fewer

construction problems to arise, and simplifying the task of the client's

team of resident engineers. Ultimately, these advantages result in a

lower cost facility.



19/22

Experience

Currently two CATADIENE units are in operation producing over250,000 MTA of butadiene. Fifteen CATOFIN dehydrogenation

plants have been commissioned for the production of isobutylene andpropylene, in addition to many other units for the production ofbutadiene. Eleven CATOFIN plants are currently on stream

producing over 2,300,000 MTA of isobutylene for the production of101,000 BPSD of MTBE, and 1,700,000 MTA of propylene. Theseplants have established CATOFIN's track record, and providevaluable data on commercial performance and yield. A summary of

these and other CATOFIN/CATADIENE projects are shown on thefollowing table.

Lummus completed the design for a 545 KMTA C3 CATOFIN Unit

for PL Propylene in Houston, USA. The Plant started up in 2010 andmet or exceeded all performance guarantees. This unit represents the

worlds largest propane dehydrogenation unit in operation.

Lummus now has two operating units at 455,000 MTA propylene

design capacity. The Saudi Polyolefins (SPC) plant for production of455,000 MTA of propylene came on stream in the first quarter of

2004. The capacity was achieved in a single reaction train. Recently,

the plant has run above 515,000 MTA propylene production. The

Advanced Polypropylene Co. (APPC) plant came on stream inFebruary 2008. The plants continue to run above 100% capacity.

CATOFIN/CATADIENE Process

Licensed Units

Onstream Capacity Products Status Alternat

Client/Location Date MTA* Primary Product

Ningbo Haiyue New 2015 600,000 Propylene Engineering

Material Co., ChinaLiaoning Tongyi 2013 684,000 Isobutylene Engineering

Petrochemical Co.,

(Chengheng), ChinaTianjin Bohua 2013 600,000 Propylene Engineering

Petrochemical Co., ChinaShandong Yuhuang 2013 300,000 Isobutylene Engineering

Chemical Co., China

KPI, Kazakhstan 2015 500,000 Propylene Engineering

Ibn Rushd, Saudi Arabia On hold 650,000 Propylene BE completed



20/22

Experience


Licensed Units

Onstream Capacity

Client/Location Date MTA*

Confidential, Africa On hold 250,000

PL Propylene 2010 545,000

(Petrologistics), USAAdvanced Polypropylene 2008 455,000

Co, Al-Jubail, Saudi Arabia

Saudi Polyolefins Co, 2004 455,000Al-Jubail, Saudi Arabia

Confidential On hold 315,000

Confidential Cancelled 315,000

Dubai Natural Gas, UAE 1995 315,000

Mobil/Chemvest Cancelled 513,000

Pemex, Morelos, Mexico 1995 350,000SABIC/IBN SINA Al 1994 452,000

Jubail, Saudi ArabiaSABIC/IBN ZAHR 2 Al 1993 452,000

Jubail, Saudi Arabia

Global Octanes, USA 1992 315,000

Borealis, Kallo, Belgium 1992 250,000Super-Octanos, Jose, 1991 315,000

VenezuelaTexas Petrochemicals, 1990 235,000

Houston, TX, USASABIC/IBN ZAHR 1, Al 1988 310,000

Jubail, Saudi Arabia

TMI, Tobolsk, USSR 1988 180,000Texas Petrochemicals, 1974 235,000

Houston, TX, USA

PEMEX Madero, Mexico 1974 60,000

TMI, Nizhnekamsk, USSR 1974 90,000

Products Status Alternate

Primary Product

Propylene On hold

Propylene Operating

Propylene Operating

Propylene Operating

Isobutylene On hold

for MTBEIsobutylene Cancelled

for MTBEIsobutylene Operating

for MTBEIsobutylene Cancelled after BE

for MTBE

Propylene Shut downIsobutylene Operating


for MTBEIsobutylene Shut down in 2004

for MTBE

Propylene OperatingIsobutylene Operating



for MTBE

Butadiene Operating2 trainsIsobutylene Operating Butadiene

for MTBE

Butadiene Shut down

Butadiene Operating



21/22

Experience


Licensed Units

Onstream Capacity

Client/Location Date MTA*

Petro-Tex, No. 3, Houston, 1972 100,000

TX USA

Polimex, Plock, Poland 1970 60,000Petrobras, Rio de Janeiro, 1968 50,000

Brazil

Pasa, Rosario, Argentina 1966 50,000

Japan Synthetic Rubber, 1960 50,000Yokkaichi, Japan

ANIC, Ravenna, Italy 1960 50,000Chemische Werke Huels, 1958 70,000

Marl, GermanyEl Paso Products Co., 1957 100,000

Odessa, TX USAArco Chemical, No., 2, 1957 70,000

Channelview, TX, USAPetro-Tex, No.2, Houston, 1957 100,000

TX, USAPetro-Tex, No. 1, Houston, 1957 100,000

TX, USA

Firestone, Orange TX, USA 1957 70,000

Arco Chemical, No. 1, 1957 70,000

Channelview, TX, USAStandard Oil Co. of 1944 20,000California, El Segundo,CA, USAMagnolia Petroleum, 1944

Beaumont, TX, USA* Based on primary product

Products Status Alternate

Primary Products

Butylenes Shut down Butadiene

Butadiene Shut down

Butadiene Shut down

Butadiene Shut down

Butadiene Shut down

Butadiene Shut down

Butadiene Shut down

Butadiene Shut down Butylenes





Isoprene



Butadiene Shut down



22/22

References1. Austin.G.T., (1984) Shreves Chemical Process Industries, Fifth

edition,Mcgraw-Hill International Book Co., Singapore2. Bhatt.B.L., Vora.S.M., (1976) Stoichiometry, Tata Mcgraw-Hill3. Coughnowr and Koppel, (1986) Process Systems Analysis and

Control,Mcgraw-Hill, New York4. Coulson.J.M., Richardson.J.F., (1977) Chemical Engineering,Vol. 6, PergamonPress5. Dryden.C.E., (1993) Outlines of Chemical Technology, Secondedition,Affiliated East-West Press6. Eckman.D.P., (1978) Industrial Instrumentation, Wiley7. Hougen.O.A., Watson.K.M. and Ragatz.R.A., (1970) Chemical

Process

Principles Part-1, John Wiley and Asia Publishing,.8.Http://digitallibrary.srmuniv.ac.in/dspace/bitstream/123456789/233/1/2793.pdf9. Kirk and Othmer, Encyclopedia of Chemical Engineering

10. Levenspiel.O., (1972) Chemical Reaction Engineering, JohnWiley, Secondedition11. Mccabe.W.L., Smith.J.C. and Harriot.P., (1993) Unit Operationsin ChemicalEngineering, Mcgraw-Hill edition12. Mcketta, Encyclopedia of Chemical Engineering

13. Perry.R.H., Green.D.W., (1997) Perrys Chemical EngineersHandbook,Mcgraw-Hill edition14. Peter and Timmerhaus, Plant design and Economicsfor ChemicalEngineers

15. Treybal.R.E., (1980)Mass Transfer Operations, Mcgraw-HillKogukosha16. Ullman, Industrial Chemistry Handbook