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Catalystsfor Purification

of Steamcracker Cuts

SUD-CHEMIECreating Performance Technology

Catalysts for Purificationof Steamcracker Cuts

Olefins are the raw materials for Polyethyleneand Polypropylene, which are important in ourdaily life, such as plastics, packing or piping.

Contents

CD I0-9xo

Ja

General IntroductionThe SUD-CHEMIE GroupOur Primary Goal - Satisfied CustomersCatalysts of the SUD-CHEMIE GroupSelective HydrogenationCatalysts for the Purification of Steamcracker Cuts

Selective Hydrogenation of Acetylenes & DienesFrontend HydrogenationTail End\HydrogenationC3 - Cut Tail End Hydrogenation "Gas Phase"C3 - Cut Tail End Hydrogenation "Liquid Phase"C4 - Cut Hydrogenation

Total Saturation of C4-/C5-CC4-/C5-Cut Hydrogenation

Hydrogenation of Pyroiysis GeFirst Stage Dienes HydrogenationSecond Stage Olefins Saturation & Sulphur Conversion

Purification of Hydrocarbon StreamsMercury RemovalCOS-HydrolysisH2S RemovalCOS & AsH3 RemovalAcetylene Trace RemovalCO RemovalOxygen Removal

Inert MaterisInert Material

Catalysts for Purification of Steamcracker CutsCatalyst Index

Your Partners for Selective Hydrogenation CatalystsQuality and Enironmental ManagementSales and Technical ServiceContacts

45567

89101112

13

1415

17171718192022

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262627

General Introduction

The Sud-Chemie Group The history of Sud-Chemie began in 1857 with the foundation of the"Bayrische Aktien-Gesellschaft fur chemische und landwirtschaftlichchemische Fabrikate Heufeld", the legal predecessor of the companytoday. At the turn of the century, bleaching earth extended the productrange and clay chemicals assumed greater role in the operations of thecompany. The product range of Sud-Chemie was further enhanced by theinternational catalysts group.

Sud-Chemie is involved in a diverse range of markets and with a widearray of customers. Our products are used extensively in the processes forthe manufacture of chemicals, petrochemicals, fertilizers and paper pro-ducts. One more key area is the oil refining and lube oil industry. Otherareas of applications include foundries, paint and surface coatings, buil-ding construction, detergents, agriculture and waste water treatment.

Sud-Chemie today is a cooperation of international standing with its head-quarters in Munich, Germany. The leading position we hold in marketsaround the world has been achieved by a combination of outstandingproducts and associated services. Where advantageous, our position hasbeen further strengthened by strategic acquisitions and mergers that havebeen taken place over the last three decades. Nearly fifty manufacturingand marketing companies - in almost every region of the globe make upSud-Chemie. The core activities of Sud-Chemie have been integrated intotwo corporate divisions:

> Catalysts> Adsorbents & Additives

Sud-Chemie - 140 yearsknow-how and experience

The annual turnover of SUD-CHEMIE is approximately 800 million.World-wide the companies belonging to Sud-Chemie employ more than5.000 people. Catalysts is a value creating innovative core.

The Factory at Heufeld in 1857 HEUFE ()

Our primary goal -satisfied customers

The companies belonging to Sud-Chemie offer innovative products andhigh tech quality engineering services as a leading supplier in the marketsaround the world.

Today and tomorrow, all Sud-Chemie companies are committed to qualityand responsible care. The ISO 9001 quality management system and theISO 14001 environmental management system have been introduced toall companies of Sud-Chemie. In addition, German production sites havereceived the validation according to "Environmental Management andAuditing Scheme (EMAS)".

Catalysts of theSud-Chemie Group

As one of the leading international catalyst suppliers, Sud-Chemie offersa wide range of catalysts for the chemical, petrochemical and fertilizerindustries, refineries, the food industry and for environmental technology.With the production sites in Europe, North America, Africa and Asia, weare in direct contact with our markets and provide our customers withefficient on-the-spot support.

Some of the areas the Sud-Chemie catalyst group is involved in includethe following:

Catalysts for... Products + Processes

SelectiveHydrogenation

Synthesis Gases

Refining & Lube OilIndustries

PetrochemicalIndustries

Houdry Process

Dehydrogenation

GeneralHydrogenation

EnvironmentalTechnology

Custom Catalysts

Ethylene & Propylene for the production of plastics(, )

Hydrogen, ammonia, methanol, reducing gases forsteel production, carbon monoxide

Production of high quality transportation fuels(gasoline, jet fuel, diesel) & lubes; Production ofprecursors for the chemical & petrochemicalindustries

Intermediate products for fibres, solvents and otherhydrocarbon-based synthetic materials

Manufacture of propylene and butylene

Styrene as an intermediate to production ofpolystyrene

Fatty alcohols for detergents and industrial cleaningmaterials, resins for adhesives and industrial paints

Waste gas purification through oxidation of volatileorganic components (VOC)

Catalysts production according to the recipe ofcustomers

Purification of steamcracker cuts

Frontend Sel.Hydrogenation

NiSPoison Guai

TRAP'IT

Cracked GasDryer

-I H^rontend Sel.

HydrogenationPd

Light Ends

C3+ orC4 +

C5+

Poison Guards / TRAP'IT*

Other Processing

Monomer Purification

Selective Hydrogenation

Selective HydrogenationGas Phase Operation Standard procedure for purifying olefin streams in a steam cracker plant

is the catalytic selective hydrogenation of acetylenes and dienes in thepresence of olefins. High selectivity is required to gain olefins from thehydrogenated acetylenes and dienes, while achieving high purity products.

Liquid Phase Operation C4- / C5-cuts may also be selectively hydrogenated or completelysaturated as well as hydroprocessing of aromatic concentrates such aspyrolysis gasoline or dripolene.

Trace Removal The high purities required in certain conversion processes to polymers orother chemical products are obtained in further separation and purificationsteps.

Catalyst Shapes used inSelective Hydrogenation Applications

Selective Hydrogenationof Acetylenes and Dienes

Selective Hydrogenation ofAcetylenes and Dienes

Olefin streams to be catalytically purified may be classified in:

> Front End Streamswith C2-minus gas up to raw gas containing also hydrogen,methane, CO and sometimes sulphur.

*> Tail End Streamswith concentrated ethylene / ethane mixtures and propylene / propanemixtures respectively.

Front End Hydrogenation Sulphur-free GasesThe G-83 family of front end hydrogenation catalysts is characterized byhigh selectivity in the hydrogenation of acetylenes and dienes in raw olefin,-minus and C2-minus streams. They are suitable for isothermal tubularreactors as well as for adiabatic beds and regenerated by either stream /air treatment in situ or with air ex situ. The average side crush strength is180 N and almost no attrition occurs during loading.

G-83C is the preferred choice for streams with low and / or fluctuating COlevels.

Nominal Content [%wt]PdAgAI203

ShapeSize [mm]Bulk Density [kg/I]

G-83

0.018

balance

Tablets4 x 4

1.2

G-83C

0.0180.03

balance

Tablets4 x 4

1.2

Sulphur-bearing GasesC36 catalysts selectively hydrogenate acetylenes and dienes in sulphurbearing cracked gas streams. Selection from among the following typesdepends on the expected sulphur content of the gas stream. C36 typesare resistant to deactivation by traces of heavy metals often found inthese streams.

C36-1 C36-2 C36-3 C36-4

NiSCoCrSiO2-AI2O3


2.01.0

0.200.10

balance

Spheres8

1.1

1.01.00.1

0.05balance

Spheres8

1,1

0.50.5

0.150.05

balance

Spheres8

1,1

3.00.7

0.200.10

balance

Spheres8

1.1

Tail End Hydrogenation C2 Tail-End HydrogenationAcetylene hydrogenation in an ethylene / ethane stream is performed withalmost stoichiometric addition of hydrogen. The Ag-promoted G-58catalysts ensure outstanding performance with high ethylene gain com-bined with long cycles, even in plants with high severity cracking. Theproduct purity achieved is typically below 0.3 ppm acetylene. In situsteam/air treatment is the preferred way to regenerate the catalysts.

Nominal Content \/PdAgAI203

ShapeSize [mm]Bulk Density [kg/I]Surface Area [m2/g]

G-58C

0.030.18

balance

Spheres2 -40.7

Medium

G-58D

0.0180.12

balance

Tablets4 x 41.2Low

G-58E

0.030.18

balance

Spheres3 - 50.7High

G-58H

0.030.18

balance

Extrusions3

0.85Medium

G-581

0.0270.20

balance

Extrusions3

0.8Low

Siid-Chemie - Expertise in Catalysts

Tail End Hydrogenation Gas PhaseThe conventional method for the removal of methylacetylene and pro-padiene from propylene / propane streams is selective hydrogenationover a Pd based catalyst. The aim is to increase the propylene con-centration and to decrease MAPD to below 10 ppm. Typically, thepurification is performed with a molar ratio of hydrogen to MAPD of 1 :to maximum 1.5: 1.

G-55A G-55B C31-1

Nominal Content [%wt.PdCrAI203

ShapeSize [mm]Bulk Density [kg / i]

0.030.03

balance

Tablets4.5x4.5

0.8

0.030.03

balance

Spheres3 - 60.7

0.03

balance

Spheres3 - 60.7

The Pd catalyst G-55A applied for C3 tail end hydrogenation has alsobeen successfully installed in several gas phase hydrogenations of1,3-butadiene in butene streams.

The Pd-catalysts are regenerable with steam / air in situ.

Ethylene Plant (by courtesy of LINDE AG)

10

Tail End Hydrogenation Liquid PhaseIt is common practice in steam cracker plants to selectively hydrogenatethe higher olefin streams in liquid phase by means of Pd catalysts with aPd content of 0.1 - 1.0 %wt., where gas phase hydrogenation catalyststypically consist of Pd on alumina in a concentration of only 0.01 - 0.1%wt. palladium. For the C3-cut hydrogenation the aim is to selectivelyhydrogenate up to 7% methylacetylene and propadiene in a propylenestream with an increase in propylene and suppression of byproduct forma-tion. The applied temperature range varies from 10 - 200 C dependingon the carbon number and the pressure of the olefin stream.

G-68HX G-681 G-68F

PdAgAI203

ShapeSize [mm]Bulk DensitySurface Area [m2/g]

0.3

balance

CDS-Extr.1.60.4

High

0.20.1

balance

Extrusions2.51.0

Low

0.3

balance

Spheres3 - 70.7

Medium

G-68 HXin CDS-extrusions is the ideal highselective catalyst for adiabaticreactor systems. "CDS" stands forComputer Designed Shape with ahigh geometric surface area.A specialized Pd impregnationtechnique provides together withthe high activity a superior selec-tivity.

G-681is the preferred catalyst for isother-mal reactors due to its exceptionalhigh mechanical strength of 140 N.The Ag promoter helps to com-pletely suppress the greenoil for-mation.

G-68Fis the most active of this family ofcatalysts and mainly applied toremove minor traces of MAPD andO2 from polymer grade liquid pro-pylene streams.

11

C4-Cut Hydrogenation The steam cracker C4-cut consists of approximately. 50 %wt.1,3-butadiene and 1 %wt. acetylenes in a mixture of butenes andbutanes. Purification of this stream require several hydrogenation stepsdepending upon the further use of the stream. Acetylenes hydrogenationis in most cases the first steps of a treatment if the total feed is sent to abutadiene extraction unit. After butadiene extraction the remaining0.3 - 2 %wt. butadiene can be selectively hydrogenated, if the desiredproduct is iso-butylene or butene-1. In some applications a well-definedmixture of butene-1 and butene-2 is the desired product after iso-butyleneseparation. In this case a catalyst is required for selective trace removal ofbutadiene in conjunction with isomerization of butene-1 to butene-2.Economic considerations lead in some plants to recycle of treated C4streams to the cracking furnaces. For this duty only butadiene saturation isrequired. Complete saturation of the C4-cut is necessary if the C4-cut issold as household gas.Pd catalysts are typically used in this application. Conditions are adjustedto optimize the yield of the desired product from the crude C4-cut.

Vinylacetylene Hydrogenation The crude C4 stream typically contains 0.5 - 2 %wt. vinylacetylene andethylacetylene. These components can drastically impact the efficiency ofthe butadiene extraction solvent system.

Nominal Content [%wt.]PdAI203


G-68G

0.2balance

Spheres2 -40.65

Medium

G-68HX

0.3balance

CDS-Extrusions1.60.4

High

G-68G and newly developed G-68HX are in successful operation forselective hydrogenation of acetylenes to butadiene with an almostnegligible butadiene loss.

Selective ButadieneHydrogenation

T-2464 is used for butadiene hydrogenation in combination with ahigh isomerization activity.G-68E is used when low isomerization is required. G-58A hydrogenates1,3-butadiene with no butene-1 isomerization and no butene-1 lossi.

Nominal Content [%wt.]Pd!20


T-2464

0.3 - 0.7balance

G-68E

0.2balance

G-58A

0.05balance

CDS-Extr.1,30.5

High

Tablets4 x 4

1.2Low

Tablets4.5x4.5

0.8High

12

Total Saturation of C4-/C5-CutsC4-/C5-CutHydrogenation

Total saturation of C4- and/or C5-streams is carried out over either Pd-or Pt-based catalysts.

Long term experience is available on our platinum catalyst G-97 as wellas on the palladium catalyst T-2464. The sulphur tolerance of T-2464 ishigher and therefore widely used if the feed contain trace amounts ofsulphur in form of COS. Typically, a hydrogen to unsaturates molar ratioabove 2 is recommended at a temperature above 50 C.

Nominal ContentPdPtAI203


T-2464

0.3 - 0.7

balance

CDS-Extrusions1.60.5

G-97

0.3 - 0.5balance

Tablets4.5x4.5

0.7

Advanced technology allows precise control ofPd/Pt placement, e.g. eggshell" deposition.

T-2464, G-97 Hydrogenation Catalysts

t*-A

13

Hydrogenation of Pyrolysis Gasoline

Palladium on alumina catalysts designed for the selective hydrogenation ofdienes in aromatic concentrates such as pyrolysis gasoline or dripolenehave been applied commercially for more than 40 years. Most of thesecatalysts are tailormade to selectively hydrogenate only the dienes inpresence of sulphur while not attacking aromatic compounds. 10 % olefinsaturation can in most cases be tolerated or is even desired. Completediene saturation is required to prevent polymerization of the feed in thestorage tanks.

First Stage DienesHydrogenation

G-68C and G-68C-1 are applied in the so-called first-stage hydrogenationof a pyrolysis gasoline treatment unit to selectively hydrogenate the dienes.Both catalysts are widely used in various feedstocks and process con-ditions, which are typically 50-180 C, 20 - 70 bar and a LHSV of up to30 h-1. For high severity cases G-68C-1 catalyst is the preferred type.

These Pd catalysts can be regenerated by in situ steam/air treatment orhot hydrogen stripping.

;

G-68C G-68C-1

Nominal Content [%PdAI203


0.3balance

Spheres2 -40.7

0.4balance

Spheres1.2-2.8

0.7

G-68C Hydrogenation Catalyst

14

Second StageOlefin Hydrogenation& Sulphur Conversion

The so-called second stage hydrogenation in commercial pyrolysisgasoline units often utilizes a mixed catalyst loading. Typically, the reactorloading comprises of:

> 30 % NiMo-catalyst C20-7 as a top layer on> 70 % CoMo-catalyst C20-6.

C20-7 is the active for olefin saturation and conversion of organic nitrogencompounds whereas C20-6 converts the organic sulphur compoundssuch as thiophenes, disulphides and mercaptanes to below 1 ppm.

Nominal Content [%wt.|NiOCoOMo03AI203


C20-7

3.5

C20-6

18balance

CDS-Extrusions1.5 ; 3.0

0.7

3.518

balance

CDS-Extrusions1.5 ;3.0

0.7

C20-6-Series Hydrogenation Catalyst

C20-7 Series Hydrogenation Catalyst

15

Purification of Hydrocarbon Streams

With the development of new generations of polymerization catalysts forthe production of various grades of polyethylene and polypropylene andthe increase in crude feedstocks applied in refineries and steamcrackersthe demand for poison removal catalysts has drastically increased overthe last ten years.

Complete removal of mercury and arsenic traces from the crude feed-stocks is required prior to steamcracking to prevent distribution of the poi-sons to all feedstreams. In case of insufficient crude feed purification pro-tection of the selective hydrogenation catalysts is an absolute necessity.

A final clean-up step prior to polymerization is also recommended for opti-mal operation and for maintaining the requested product specification.

Feeds requiring purification can be classified as

- Gaseous and liquid feeds prior to steam cracking

- Cracked gases or liquids prior to selective hydrogenation

- Refinery gases and liquids prior to polymerization

> Steamcracker products with polymer grade quality prior topolymerization with metallocene orother highly sensitive polymerizationcatalysts

The purification catalysts are tailormade forthe different nature of the various poisons.

16

Mercury Removal

COS-Hydrolysis

Mercury traces in cracked gases are a severe poison for the selective Pdhydrogenation catalysts, because the mercury is layed down on the Pdsurface blocking active sites for the hydrogenation reaction.The catalysts T-2552 and T-2662 absorb traces of mercury from all typesof feed to non-detectable levels.

T-2552

Nominal Content [%wt.]AgFeMnAI203


T-2662

Proprietary

balance

Spheres2-40.8

Extrusions3

0.8

COS hydrolysis in gaseous propylene to below 30 ppb is obtained withour PtS-Catalysts C53-2. C53-2 has a dual function i.e. COS removal andO2 conversion with H2 to H20. Therefore, a speciality application Is thepurification of gases from partial oxidation prior to their use in oxo-alcoholplants.G-41P is tailormade selectively hydrolyze COS in the presence of largeamounts of CO and H2 - see also synthesis gas catalysts listing.

Nominal Content [/Cr203K2OPtAI203


G-41P

116

balance

Tablets4.5x4.5

0.8

C53-2

0.08Balance

Extrusions3.00.5

H2S Removal G-72 D is manufactured from high activity zinc oxide and has a high sur-face area in excess of 50 m2/g. It is used for the removal of H2S, CH3SH,carbonyl sulphides form a variety of feedstreams. Recommended opera-ting temperature for olefin streams is typically ambient in these applica-tions. G-72 D normally absorbs up to 1 5 %wt. sulphur at low temperatu-res, before sulphur leakage exceeds 1 0 ppb. The capacity increases withraising temperature.

Nominal Content [%wt/ZnOBinder


G-72D

90balance

Extrusions4.51.1

17

COS & Arsine Removal Refinery feeds and C3 stream from the steamcrackers often contain bothCOS and AsH3 and sometimes PH3 traces. CuO-catalysts such as G-132and T-2550 are in successful operation to purify mainly propylene. Theabsorption of the poisons can be accomplished in either gas or liquidphase. The achieved product purity normally is below the detectable limit.As a consequence the selective hydrogenation catalyst installed down-stream is perfectly protected and can operate at its basic activity andselectivity. The consumption of polymerization catalysts is drasticallyreduced with a poison guard. Therefore, feed polishing prior to polymeriza-tion is very valuable for the downstream operations.

Nominal Content [%wt.]CuOZnOMn02AI203


G-132A

4141

balance

Tablets6 x 3 , 4.5x2.4

1.3

T-2550

16

25balance

CDS-Extrusions1.5/2.5

0.7

G-132, T-2550 - The solutions to COS &Arsine Removal

18

Acetylene Trace Removal fromMonomer Streams

For many polymerisation processes it is essential to have in the ethyleneand propylene streams an acetylene and dienes content of below 0.3 ppm.In the steamcracker cuts the bulk hydrogenation of acetylenes and dienesresults in a typical purity level of 1 to 10 ppm. For the trace removal ofacetylenes and dienes basically the same catalysts and conditions areapplied as for bulk hydrogenation.

Acetylene Trace Removal fromEthylene

For trace acetylene hydrogenation in a pure ethylene stream the G-58 catalyst ensures high activity and optimum selectivity. Hydrogen is added5 to 10 molar referred to incoming acetylene traces. Usually no regenera-tion is required as the typical cycle is more than 10 years. For subsequentconsumption of excess hydrogen the G-133 A catalyst may be installed inthe bottom part of the G-58 reactor.

G-58 G-133 A

Nominal Content [%PdAI203


0.05balance

Spheres3-50.7

0.15balance

Spheres3-50.7

Acetylene Trace Removalfrom Propylene

Basically two methods for the trace removal are commonly applied:>- Selective hydrogenation in gaseous propylene streams;5* Selective hydrogenation in liquid propylene streams.

In the gaseous treatment Pd catalysts C31-3 or G-133 A are recommen-ded. Normal operating temperatures are in the range of 70-120 C.Oxygen traces are removed simultaneously with the MAPD and butadienetraces. The hydrogen addition is 2 to 3 molar.

The liqiud propylene streams are treated at around 40 - 50 C and bymeans of a catalyst with higher palladium content: G-68 F. This catalyst isactive at these conditions and removes the MAPD plus butadiene plusoxygen traces to below 0.1 ppm with a hydrogen surplus of 3 to 5 molar.

Nominal Content [%wt.]Pd!20


C31-3

0.14balance

Spheres3-70.7

G-133 A

0.15balance

Spheres3-50.7

G-68F

0.3balance

Spheres4-60.7

19

CO Removal Various feed streams do contain CO in concentrations of several ppmup to one percent which has to be removed to levels below 10 ppb.The type of catalyst is chosen according to the feed, e.g. Ni-catalysts tomethanate CO in hydrogen streams and CuO-catalysts to remove COfrom ethylene and nitrogen by adsorption or by catalytic reaction withair/oxygen addition.

CO Removal from Ethylene Complete CO removal from polymer grade ethylene is successfully per-formed with either G-66B or T-4427B. The tolerable remaining CO level inthe ethylene is determined by the polymerization catalyst applied in thevarious processes. G-66B exhibits excellent mechanical strength andrequires slightly higher operation temperatures compared to T-4427B andour latest development T-4492. Complete CO removal is achieved atambient temperatures with T-4492. The purification is cyclic and re-oxidation of the catalyst is necessary.

NomiriiCuOMn02ZnO


G-66B

32

66

Tablets6 x 31.3

T-4427B

30

63

Extrusions3

0.95

T-4492

424-5

47

Extrusions3

0.9

Copper Catalysts

20

CO Removal from Nitrogen CO removal from nitrogen can be performed by means of CuO-catalystssuch as G-66B or T-4427B. Absorptive removal requires periodic re-oxidation of the catalyst, so a cyclic operation with two catalyst beds istypical. Catalytic operation requires a well controlled addition of air for thereaction across the reduced catalyst.

CO Removal from Hydrogen In steam cracker plants the hydrogen contains typically 0,2 - 1 %vol. CO,but without CO2. The CO-methanation is preferably carried out at thelowest possible temperature. We offer for this duty a Ru-catalyst foroperating temperatures of around 170 C and two Ni-catalysts withdifferent Ni-levels, which need to be operated above 200 C to avoidNi-carbonyl formation. We offer the Ni-catalysts prereduced and stabilizedgiving the tremendous advantage of a quick start-up with a activationtemperature of no more than 270 C.

Nominal Content [%wt.]NiRuCaOAI203Si02

Shape

Size [mm]Bulk Density [kg/I]

C13-3RS

34

6balance

Spheres

3-61.0

G-33RS

34

balance

Tablets

6 x 61.0

G-65RSC13-4RS

20

5balance

Extrusions,Spheres3; 4.50.9

C13LT

0,3

balance

Tablets

4,5 x 4.50.8

Nickel Catalysts

21

Oxygen Removal In hydrogen, nitrogen, ethylene and propylene streams it is not onlyrequired to remove traces of sulphur, acetylenes and CO but also oxygen.The catalytic active metal is chosen upon the teed stream to be purified.

Oxygen Removal from Ethylene For oxygen trace removal from ethylene reduced copper catalysts aresuccessfully applied. Depending on the required purity and temperaturethe most suitable catalyst may be chosen from one of the coppercatalysts listed below.

G-66B T-4427B T-4492

.Nominal Content [%wt.CuOMnO2A1203

ShapeSize [mm]:Bulk Density [kg/I]:

32

66

Tablets6 x 31.3

30

63

Extrusions3

0.95

424-5

47

Extrusions3

0.9

Oxygen Removal fromPropylene

For oxygen trace removal in propylene streams in the presence ofhydrogen for gasphase operation G-133 and for liquid phase G-68F arerecommended.

Nominal Content [%wt]PdAI203


G-133 Series

0.15balance

0.30balance

Spheres Spheres3-5 3-50.7 0.7

0.50balance

G-68F

0.30balance

Spheres Spheres3-5 4-60.7 0.7

1 Oxygen Removal Catalysts: G-68 F; G-43; G-133

22

Oxygen Removal fromHydrogen

Oxygen removal from hydrogen is carried out by the catalytic reaction ofO2 and H2 over Pd catalysts. G-133 catalyst with Pd concentrations from0.15 to 0.5 %wt. is recommended. A maximum of 2 - 3 %vol. oxygen canbe removed per pass with G-133. It also effectively removes only oxygentraces from hydrogen.

G-133 SeriesA G O

Nominal Content [%wt]Pd 0.15 0.30 0.5PtNi!2 balance balance balance

Shape Spheres Spheres SpheresSize [mm] 3-5 3-5 3-5Bulk Density [kg/I] 0.7 0.7 0.7

G-43

0.13

balance

Tablets4.5x4.5

0.8

Oxygen Removal from Nitrogen Oxygen removal from nitrogen can be performed in the same way i.e. thecatalytic reaction of O2 and H2 over Pd catalysts.

In some rare cases higher O2 levels and the resulting high temperatureshave to be handled. Then a combination of G-133 Pd catalyst on top ofG-43 Pt-catalyst is recommended. G-43 tolerates temperatures up to1350C.

In case nitrogen contains only traces of oxygen, the easiest way ofremoval is the adsorption on a reduced Cu-catalyst like T-4427B incyclic mode.

An unusual application of use of polymers isthe Olympic Stadion in Munich (Germany)

from 1972

23

Inert MaterialInert Material Inert balls are used both on support screens and to hold down the

catalyst top layer. The size of the inert material closest to the catalystmust be no more than twice the minimum dimension of the catalyst.

Sud-Chemie's inert material is rugged, chemically inert and temperaturestable. Its high crush strength and low attrition loss provide long andtrouble free operation. Various sizes required for the different screen andcatalyst sizes are available.

Nominal Content [%wt.]AI2O3 + TiO2SiO2Fe2O3


CS346

>99

Catalyst Index

Catalyst Index

CATALYST

C13-3

C13-4

C13LT

C31-1/C31-3

C36 series

C20-6

C20-7

C53-2

G-33 RS

G-41 P

G-43

G-55 A/B

G-58 series

G-65 RS

G-66B

G-68 series

G-72 D

G-83 series

G-97 series

G-132 series

G- 133 series

T-2464 series

T-2550

T-2552

T-2662

T-4427

T-4492

CS346

COMPOSITION

Ni/AI2O3

Ni/AI2O3

Ru/AI2O3

Pd/AI2O3

NiCoCr/AI2O3

CoMo/AI2O3

NiMo/AI2O3

PtS/AI2O3

Ni/Si02

Cr/AI2O3

PtNi/Ai2O3

Pd/AI203

PdAg/AI2O3

Ni/AI203

CuOZnO

Pd/AI2O3

ZnO

Pd/AI203

Pt/AI2O3

CuOZnO/AI203

Pd/AI203

Pd/AI2O3

CuOMnO2/AI203

Ag/AI203

Fe2O3MnO2/Ai2O3

CuOZnO

CuOMnO2/AI203

AI203

APPLICATION

Methanation

Methanation

Methanation

MAPD Hydrogenation

Acetylene Hydrogenation

Hydrodesulphurization

Olefins Saturation

COS Hydrolysis

Methanation

COS Hydrolysis

Gas Purification

MAPD Hydrogenation


Methanation

CO/O2-Removal

Selective Hydrogenation

H2S-Removal


Aromatics/Olefins Saturation

Gas Purification

Gas Purification

Hydrogenation

Gas Purification

Gas Purification

Gas Purification

CO/O2-Removal

CO-Removal

Inert Balls

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20, 21 , 22, 23

20,21,22,23

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Your Partners

Sales & Technical Service Sud-Chemie firmly believes that even an outstanding catalyst may not pro-vide the best performance without the appropriate level of assistanceduring the phases of selection, installation, start-up and operation. OurTechnical Services Group has specific expertise in the areas of catalystcharacterization/ research, catalyst installation/start-up, plant operation,and performance evaluations. This depth of knowledge allows us to provi-de the following services:

> Review of reactor system design

* Selection of proper catalyst> Technical reviews of start- up/shutdown procedures

> Technical assistance for loading, catalyst start-up and shut-down

> Routine performance evaluations> Troubleshooting

> Catalyst life projections> On-site training seminars for engineering & operations personnel

Chemical and physical analyses of spent catalyst

> Extensive range of state-of-the-art analytical equipment

> Process simulation via computer systems for design and evaluationpurposes

Quality and EnvironmentalManagement

The Sud-Chemie is committed to quality and responsible care.The ISO 9001 quality management system and the ISO 14001environmental management system have been introduced to allcompanies of Sud-Chemie.

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Contacts

USASUD-CHEMIE INC.P.O. Box 32370Louisville, Ky. 40232Phone: +1-502-6347200Fax: +1-502-6378765

GermanySUD-CHEMIE AGLenbachplatz 680333 MunchenPhone: +49-89-5110-322Fax: +49-89-5110-444

JapanSUD-CHEMIE NISSAN CATALYSTS INC.Kundanminami C&M; Bldg 9-14Kundanminami 3-Chome; Chiyoda-Ku; Tokyo 102Phone: +81-3-3265-7331Fax: +81-3-3265-7717

Active World-wide -SUD-CHEMIE Offices in:

1 Bahrain 6 Republic of South Africa2 Brazil 7 Russia3 India 8 Singapore4 Indonesia 9 Spain5 Japan 10 United Kingdom

A/though these instructions have been pre-pared by experienced technicians and havebeen based on the best available informati-on derived from laboratory, pilot plant andcommercial experience with our catalysts,these technicians do not have intimateknowledge of the customer's plant andoperation.

Therefore, Sud-Chemie, in issuing theseinstructions, cannot assume liability forupsets and damage to either the customer'splant or personnel. The customer is urgedto review these instructions carefully and tosatisfy himself that their application will notbe hazardous to his specific operation.

Further, Sud-Chemie's Technical Servicerepresentatives are present at plant start-ups in an advisory capacity only and cannotbe charged with knowledge and responsibi-lity for hazardous conditions that mightresult from the application of the instruc-tions

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Sud-Chemie AGLenbachplatz 680333 MunichGermanyPhone: +49-89-51 10-322Fax: +49-89-51 [email protected]

06 £ . - Фонд промышленных...

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