Catadiene Class c

7/22/2019 Catadiene Class c

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LUMMUS CATADIENE

n-ButaneDehydrogenation Unitfor Butadiene Production

Technical Information


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Table of Contents

CATADIENE Butane Dehydrogenation for Butadiene (8/11)

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.............................................11Plant Operation ....................................................................13

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

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

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

Experience .......................................................................................17


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Introduction

CATADIENE Butane Dehydrogenation for Butadiene 1

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 convertnormal 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 mostwidely used process backed by Lummus commitment to technicalexcellence.

Nineteen CATADIENE plants have been constructed worldwide with

a combined capacity in excess of 1,200,000 MTA of butadiene. Themost 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 worldspropane/isobutane dehydrogenation capacity. Commercial operatingexperience demonstrates the capability to exceed design capacity,yield, and catalyst life. The CATOFIN process is used for the worldslargest 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 C 3CATOFIN Unit for Tianjin Bohua Petrochemical Co., China. Inaddition, the basic design for a 650 KMTA C3CATOFIN Unit for Ibn

CATADIENE is theonly one-step routefrom n-butane to

butadiene

Unmatched

CommercialExperience


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Introduction


Rushd, a SABIC Affiliate in Saudi Arabia has been completed. Thesetwo designs represent the largest single train propane

dehydrogenation facilities in the world.

Lummus completed the basic design of a 500 KMTA C3CATOFINUnit for Kazakhstan Petrochemical Industries Inc. (KPI) inKazakhstan.

Lummus completed the design for a 545 KMTA C3CATOFIN Unitfor PL Propylene in Houston, USA. The Plant started up in 2010 andmet or exceeded all performance guarantees. This unit represents theworlds largest propane dehydrogenation unit in operation.

Lummus has two operating units at 455,000 MTA propylene designcapacity. The Saudi Polyolefins (SPC) plant for production of455,000 MTA of propylene came on stream in the first quarter of2004. The Advanced Polypropylene Co. (APPC) plant came onstream in February 2008. The plants continue to run above 100%capacity.

The CATOFIN/CATADIENE dehydrogenation technology hasseveral hundreds of years of operating experience throughout theworld. These plant operations support the capability to exceedcapacity, overall yield, and catalyst life.

On-stream factors exceeding 97% are routinely achieved incommercial operations. This is reflected in reduced plant size andmaintenance costs compared to competing technologies. TheCATADIENE process has no significant fouling problems and designthroughput is quickly achieved after a startup. The process uses fixedbed reactors containing a robust Sd-Chemie catalyst that is resistantto 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 alarge 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, Lummusoffers advanced process control, computer simulators, operatingtraining, detailed engineering, and start-up services.

High Reliability

CATOFIN has

worlds largest unitin operation

Support andCommitment to

TechnicalAdvancement


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Introduction


Sud-Chemie, the exclusive supplier of the proprietary CATOFIN andCATADIENE 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 fromits high yields, on-stream availability, and lower investment cost, theLummus dehydrogenation processes are the technology of choice intodays market for the dehydrogenation of propane or butanes. Theselection of the CATADIENE technology will be instrumental inattaining the financial and project goals targeted by your company.

Lummustechnologies,experience, andcapabilities ensurea successful

project


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Technology Overview


Using the CATADIENE process, butadiene can be produced from

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

The processing scheme for the CATADIENE butadiene process isshown 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 continuousproduction and has demonstrated safe and reliable operation withhundreds of years of operating experience. Features of the technologyinclude:

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 feed back from actualplant operations, which results in improved reliability, operation andefficiency.

CATADIENETechnology

Overview


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Technology Overview


Process Flow

Schematic

GasTurbine

Air

Fuel

Reactor onReheat

Reactors onStream

Reactor onPurge

Charge

Heater

Steam

To Stack

Waste Heat Boiler

Quench Section

SteamCooler

HeatRecovery

HeatRecovery

Fresh Butane

RecycleButane/Butenes

Cooler

Flash Drum

DeC3

FuelGas

Product

CompressorProduct toPrefractionatorand BDE Unit

Cooler

Air Heater

Low TempSection


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The CATADIENE unit can be designed to process a wide variety offeedstocks. A typical feedstock has the following characteristics:

Butane Feed

Component Wt%

Isobutane 2.0

N-Butane 97.8

C5+ 0.2

Lower purity butane streams can be handled in the CATADIENEunit. However, any increase in the level of C3 and C5 impuritieswould increase the amount of offgas since these impurities are

cracked to lighter hydrocarbons.

The CATADIENE unit is designed to produce a C4stream containing27 wt. % butadiene as feed to a downstream butadiene extraction unit.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 isnormally burned as fuel. A significant portion of the hydrogen in theoffgas can be recovered at high purity in a pressure swing adsorption(PSA) unit.

Feedstock andProduct

Specifications


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The process description provided in this section can be followed moreclearly 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 and n-butenes are recycled to the reactor section so thatbutadiene is the only net product. Operating conditions for theprocess are selected to optimize the relationship among selectivity,conversion, and energy consumption in the temperature and pressure

range of 575-625o

C and 0.14-0.24 bar absolute. Side reactionsproduce light hydrocarbon gases in small quantities, along withhydrocarbons heavier than the feed (polymer). The heaviest of thesehydrocarbons are deposited as coke on the catalyst.

A key feature of the process is that the heat is absorbed from thecatalyst bed by the reaction as dehydrogenation proceeds, graduallyreducing the temperature of the catalyst bed. This temperaturereduction, coupled with coke deposited on the catalyst decreases itsability to produce the desired products. To remove coke and torestore 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 thenpurged 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.

ProcessDescription and

Process FlowDiagram


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Process Description

Reaction Section

In the reaction section, butane is converted to butadiene while passingthrough a catalyst bed.

Fresh butane feed is combined with recycle butane and butenes fromthe downstream butadiene extraction unit. The total feed is thenvaporized by heat exchange with a circulating quench oil stream.Upstream of this exchanger, a small quantity of a sulfiding agent isadded to the feed to passivate metals in the alternating oxidating andreducing atmosphere of the reactors. The total feed is then brought to

reaction temperature in the gas fired charge heater and sent to thereactors.

Non-selective cracking of hydrocarbons is minimized by injectingfuel gas during the reheat portion of the cycle to keep the heater outlettemperature as low as possible. Hot effluent from the reactors flowsto a pre-quench tower and the main quench tower where the vapor iscooled by direct contact with a circulating quench oil stream.Polymeric compounds in the reactor effluent are absorbed by thequench oil. In order to maintain the properties of the quench oil, aslipstream is withdrawn and charged to a quench oil vaporizer. Steamis injected and the stream is partially vaporized. The vapor portion isreturned to the system and the heavy liquid is rejected. Make-upquench oil may be added intermittently to maintain 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 residualhydrocarbons from the catalyst and reactor into the recovery system.

Reheat of the catalyst takes place at slightly above atmosphericpressure. Reheat air is supplied typically by a gas turbine or aircompressor and heated to the required temperature in a direct-fired

duct burner before passing through the reactors. The reheat air servesto 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 generatesteam in a waste heat boiler.

When the reheat of a reactor is complete, the reactor is re-evacuatedbefore the next on-stream period. Prior to introducing butane feed,hydrogen rich offgas is introduced to the reactor for a short time to


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remove absorbed oxygen from the catalyst bed. This reduction stepdecreases 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 heatboiler 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 valvebonnet when the main valve is in the closed position. The seal gasprevents mixing of process streams if there should be any leakagebetween the wedge and the seat. Inert gas such as N2or steam is usedfor 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 therecovery section. For each stage, a compression ratio is selected tooptimize compressor performance and keep gas temperature low tominimize polymer formation.

Any water that condenses after each stage of compression is separatedin the interstage knock-out drums. Additionally, a sodium nitritesolution is circulated in the final stage suction drum as an oxygen


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scavenger to aid in the prevention of polymer in the downstream gasplant section.

The compressor discharge vapor is cooled and the resulting vapor-liquid is separated in a flash drum. The reactor effluent condensateand the uncondensed reactor effluent vapor streams both flow to therecovery section.

Recovery Section

The recovery section removes inert gases and light hydrocarbons fromthe compressed reactor effluent. The vapor from the flash drum isdried and sent to the low temperature recovery system where butanes

are recovered by chilling and condensation. These butanes arecombined with liquid from the flash drum and sent to thedepropanizer. The depropanizer removes C3 and lighterhydrocarbons from the butanes and heavier material. The C4s andheavier components are sent to downstream facilities where 1,3-butadiene is recovered (typically by solvent extraction) and normalbutane and n-butenes are recycled to the CATADIENE reactors.

The following material balance is typical of the average performanceof 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 68,750 MTA

C5+and coke 19,750 MTA

The light ends produced by the CATADIENE process are typicallyused within the unit as fuel. However, they contain significantamounts of hydrogen, as well as C2and C3components which couldbe recovered for higher value uses.

Overall MaterialBalance


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The estimated overall normal utility requirements only for theCATADIENE 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 kWh

Boiler Feed water (BFW) 1.3 metric ton

Cooling Water(1) 525 m3

Fuel(2) Net Gas Consumption 4.7 MWh

Notes:

1. Based on 10 oC temperature rise.2. Offgas and C5+ streams from the CATADIENE unit are consumedas fuel within the CATADIENE unit.

Catalyst Requirements

The dehydrogenation reactors contain a mixture of chromia-aluminacatalyst and inert grain. The expected catalyst life is 2.5 years. Theinert 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 ofbutadiene is approximately $US 19 per metric ton of butadieneproduct.

Chemical Requirements

A sulfiding agent is added to the total reactor feed to passivate themetals in the alternating oxidizing and reducing atmosphere in thereactors. If the fresh and recycle feeds contain no sulfur, themaximum addition rate is about 15 ppm.

Atmospheric 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 catalyticreduction can also be applied for NOx reduction. The flue gas is

UtilityConsumption

Catalyst andChemical

Consumption

EnvironmentalConsiderations


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discharged to the atmosphere after being cooled in waste heatrecovery. 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 emissionsfrom the CATADIENE unit. Fugitive emissions from equipment areminimized by the application of the following engineering practices:

All pumps in light liquid service are equipped with dualmechanical 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. Provisions are made to depressure all equipment to the flare

system prior to opening for maintenance.

Spent Catalyst Disposal

The CATADIENE catalyst operates in fixed-bed reactors so no lossesfrom attrition or breakage occur. The catalyst is not dangerous andonly normal precautions are necessary when unloading to preventlosses and inhalation of dust. Tests on commercial CATADIENEplants have shown that no catalyst dust is detectable in the emissionsfrom the plant.

The primary ingredients of CATADIENE dehydrogenation catalystare alumina and chromium oxide. Once the catalyst becomes spent,its ingredients can be utilized as raw material for metal industry andrefractory 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 theproduction 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.


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Turndown

The CATADIENE unit can be operated economically at 60% of thedesign capacity. At this point, the limiting factor is usually turndowncapacity of the product compressor. Operating below 60% ofcapacity is possible by use of recycle in the compression section, butthis 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 widelyacknowledged by current licensees. The operating plants haveexperienced in excess of 40 million reactor cycles without seriousmishap. This safety record is based on the very careful design of thesystem.

The reactor system as well as the operation of all other items of majorequipment within a CATADIENE unit have been subjected to criticalreviews by technical experts within Lummus, using state-of-the-artanalysis techniques and methodology for process hazards analysis.This type of analysis is directed at identification and prevention ofundesired events and results in calculation of an average hazard ratefor the plant. The rate calculated for the CATDIENE process wasfound to be well within the corporate goals established by majorchemical companies.

On-Stream Factor

Achieving a high on-stream factor is critical to the projectseconomics. 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 CATADIENEplant have withstood the test of time, having maintained theiroperating integrity.

The CATADIENE technology has repeatedly demonstrated on-streamefficiencies well in excess of 97%. This proven record, as well as therobust reactor design which withstands transient conditions and quick

Plant Operation


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restarts, is a significant advantage over competitive PDH processeswhich use fragile reactor internals.

Maintenance

Total maintenance costs for the CATADIENE unit, includingturnaround costs, but excluding the catalyst, are normally about 2% ofreplacement capital cost. This compares favorably with themaintenance 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.

Plot

Requirements


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Manpower Requirements


Staffing

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


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Licensor Capabilities Sole Source Responsibility


As licensor of the CATADIENE technology, Lummus can provide:

Feasibility studies Basic design engineering Interface with the detailed engineering contractor Supply of catalyst Training 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 withunequaled quality and satisfaction:

Preliminary estimates & scheduling Project financing Site surveys Permitting Environmental Services Detailed design Estimating and scheduling

Worldwide procurement Construction Project management

This sole source responsibility greatly simplifies the coordination ofthe project work, thus enabling a faster schedule to be achieved, fewerconstruction problems to arise, and simplifying the task of the client'steam of resident engineers. Ultimately, these advantages result in alower cost facility.


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

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 theworlds largest propane dehydrogenation unit in operation.

Lummus now has two operating units at 455,000 MTA propylenedesign capacity. The Saudi Polyolefins (SPC) plant for production of455,000 MTA of propylene came on stream in the first quarter of2004. The capacity was achieved in a single reaction train. Recently,the plant has run above 515,000 MTA propylene production. TheAdvanced Polypropylene Co. (APPC) plant came on stream inFebruary 2008. The plants continue to run above 100% capacity.

CATOFIN/CATADIENE Process

Licensed Units

Client/Location

Onstream

Date

Capacity

MTA*

Products

Primary

Status Alternat

Product

Ningbo Haiyue NewMaterial Co., China

2015 600,000 Propylene Engineering

Liaoning TongyiPetrochemical Co.,

(Chengheng), China

2013 684,000 Isobutylene Engineering

Tianjin BohuaPetrochemical Co., China

2013 600,000 Propylene Engineering

Shandong YuhuangChemical Co., China

2013 300,000 Isobutylene Engineering

KPI, Kazakhstan 2015 500,000 Propylene Engineering

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


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Experience



Licensed Units

Client/Location

Onstream

Date

Capacity

MTA*

Products

Primary

Status Alternat

Product

Confidential, Africa On hold 250,000 Propylene On hold

PL Propylene(Petrologistics), USA

2010 545,000 Propylene Operating

Advanced PolypropyleneCo, Al-Jubail, Saudi Arabia


Saudi Polyolefins Co,Al-Jubail, Saudi Arabia


Confidential On hold 315,000 Isobutylenefor MTBE

On hold

Confidential Cancelled 315,000 Isobutylenefor MTBE

Cancelled

Dubai Natural Gas, UAE 1995 315,000 Isobutylenefor MTBE

Operating

Mobil/Chemvest Cancelled 513,000 Isobutylenefor MTBE

Cancelled after BE

Pemex, Morelos, Mexico 1995 350,000 Propylene Shut down

SABIC/IBN SINA AlJubail, Saudi Arabia

1994 452,000 Isobutylenefor MTBE

Operating

SABIC/IBN ZAHR 2 AlJubail, Saudi Arabia


Operating

Global Octanes, USA 1992 315,000 Isobutylenefor MTBE

Shut down in 2004

Borealis, Kallo, Belgium 1992 250,000 Propylene Operating

Super-Octanos, Jose,Venezuela


Operating

Texas Petrochemicals,

Houston, TX, USA

1990 235,000 Isobutylene

for MTBE

Operating

SABIC/IBN ZAHR 1, AlJubail, Saudi Arabia


Operating

TMI, Tobolsk, USSR 1988 180,000 Butadiene Operating 2 trains

Texas Petrochemicals,Houston, TX, USA


Operating Butadien

PEMEX Madero, Mexico 1974 60,000 Butadiene Shut down

TMI, Nizhnekamsk, USSR 1974 90,000 Butadiene Operating


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Experience


Licensed Units

Client/Location

Onstream

Date

Capacity

MTA*

Products

Primary

Status Alternat

Product

Petro-Tex, No. 3, Houston,TX USA

1972 100,000 Butylenes Shut down Butadien

Polimex, Plock, Poland 1970 60,000 Butadiene Shut down

Petrobras, Rio de Janeiro,Brazil

1968 50,000 Butadiene Shut down

Pasa, Rosario, Argentina 1966 50,000 Butadiene Shut down

Japan Synthetic Rubber,Yokkaichi, Japan


ANIC, Ravenna, Italy 1960 50,000 Butadiene Shut down

Chemische Werke Huels,Marl, Germany


El Paso Products Co.,Odessa, TX USA

1957 100,000 Butadiene Shut down Butylene

Arco Chemical, No., 2,Channelview, TX, USA


Petro-Tex, No.2, Houston,TX, USA


Petro-Tex, No. 1, Houston,TX, USA


Firestone, Orange TX, USA 1957 70,000 Butadiene Shut down ButyleneIsoprene

Arco Chemical, No. 1,Channelview, TX, USA


Standard Oil Co. ofCalifornia, El Segundo,CA, USA


Magnolia Petroleum,Beaumont, TX, USA

1944 Butadiene Shut down

* Based on primary product

Catadiene Class c

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