purification katalco mar 07

Purification catalysts and absorbents

Katalco

JM_960_869 bPurification Broch 27/4/06 11:42 am Page 2

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operate under any Patent.


Contents

Page

Introduction 2

Case studies 3

KATALCOJM PERFORMANCE adds value to your plant 5

Advantages of choosing Johnson Matthey purification catalysts and absorbents 6

Additional capability with KATALCOJM PERFORMANCE 9

Catalyst selector 12

Catalyst characteristics 13


2

Feedstock purification is a key unit operation in any

synthesis gas plant which employs steam reforming

technology. Its importance is often overlooked, however, and

the consequences of not installing the correct catalysts and

absorbents, or of not monitoring performance appropriately,

can have dramatic and costly consequences for downstream

catalysts. The key catalysts in synthesis gas plants that may

be poisoned by trace components in the feed gas are

pre-reforming, steam reforming, low temperature shift and

methanol synthesis.

The most common catalyst poisons experienced are

sulphur compounds present as hydrogen sulphide, COS,

mercaptans, organic sulphides and disulphides, and

thiophenes. Occasionally halogen compounds are present,

usually as hydrogen chloride, but sometimes as organic

chlorides. Some plants also experience feedstocks with

more unusual poisons such as mercury, arsenic and other

metallic species.

Very severe poisoning will lead to significant costs. For

example, with severe sulphur poisoning incidents the

affected steam reforming catalyst may need to be replaced.

In addition to downtime, possibly measured in weeks, the

catalyst cost must be added. The financial cost of such

incidents varies depending on the size and type of the plant,

however, for large scale plants (e.g. 100 MMSCFD hydrogen;

2,000 mtpd ammonia; 2,500 mtpd methanol) each day of

lost production costs in the order of US$ 350,000 and

typical catalyst replacement cost is in the order of

US$ 750,000. In comparison, the catalyst and absorbent

cost in a typical purification system for plants of a similar

scale is around US$ 240,000. Thus, the provision and

timely replacement of these materials is a comparatively

small investment compared to the potential costs of

poisoning the downstream catalysts.

IntroductionIn plants with a pre-reformer, sulphur removal is critical to

successful operation of the catalyst. A serious sulphur

incident usually means immediate catalyst replacement is

required. In addition to downtime, the replacement catalyst

cost will be significant, approaching that for a steam reformer

charge depending on the pre-reformer bed volume.

Both sulphur and chlorides severely affect both low

temperature shift (LTS) and methanol synthesis catalysts.

These copper-based catalysts scavenge both sulphur and

chlorides very effectively and are poisoned as a result. For a

2,000 mtpd ammonia plant, the cost in terms of lost LTS

life can be of the order of US$ 500,000 per year plus the

incremental production loss as water gas shift efficiency

decreases. The effect on methanol synthesis catalysts have

similar financial consequences.

In comparison, the total cost of the catalysts and absorbents

in the purification system is significantly less than the cost of

the problems that can occur if the purification catalysts are

not well maintained.


3

Case study – PURASPECJM™ ultrapurificationimproves reformer catalyst life

A Western European HyCO plant has operated for a

number of years with a two year turn-around cycle.

Historically at each turn-around, the operator replaced the

steam reforming catalyst in order to have confidence that

the plant would operate reliably and efficiently enough in

the next two year cycle. The steam reformer feedstock is a

methane rich natural gas and the steam reforming

conditions are relatively severe since this is a HyCO plant.

PURASPECJM 2084 was installed in the purification section

to reduce the level of trace sulphur slipping to the steam

reformer. Over the two year cycle following the installation

of the PURASPECJM 2084, the operator observed a much

slower rate of activity decline in the steam reforming

catalyst. The plant operating conditions for this cycle were

the same as for previous cycles, and it was concluded that

the improved performance was a result of the use of the

ultra-purification absorbent. The operator therefore had the

confidence that the installed steam reformer catalyst would

last for a second two year operating cycle.

The benefit to the operator was the saving in terms of steam

reformer catalyst purchase and replacement costs and an

improved efficiency of operation during the initial two year

operating cycle. This saved the plant US$ 400,000 in

catalyst replacement costs.

Case study – Correct sampling for poisonseliminates plant operating problems

Sampling and testing for sulphur is not a simple task and

there are many issues that have to be addressed. One plant

suffered severe hot banding leading to regular steam outs

and a loss of tube life. Sampling of the feedstock at the exit

of the desulphurization system detected no sulphur and this

was therefore ruled out as the cause of the problem. A

lengthy investigation was conducted to identify the root

cause of the problem but no other potential causes of the

hot banding were found.

The desulphurization system was then re-investigated.

The first issue highlighted was that the sample lines were

relatively long and the metal utilized for the sample lines

would absorb sulphur. The sample lines were therefore

redesigned, reducing the length significantly and using a

metallurgy that would not absorb sulphur. The sample

bombs were also replaced with a superior metallurgy.

Subsequent analysis of the feed gas established that

significant levels of sulphur were passing through the

desulphurization system to the steam reformer.

The installed catalysts and absorbents were then replaced

with KATALCOJM products and the steam reformer was

steamed a final time to remove the sulphur from the

catalyst. As a result of this the tube appearance has now

improved and the tube wall temperatures have returned to

the normal value.


4

Case study – KATALCOJM PERFORMANCEverifies plant modifications to deliverperformance

Through KATALCOJM PERFORMANCE Johnson Matthey

Catalysts delivers a range of services that ensures improved

performance of your plant. An example of how this has

benefited one of our customers is outlined below.

As part of a project to eliminate an operational problem, the

plant were proposing to change the outlet temperature from

the feed pre-heat coil upstream of the hydrodesulphurization

bed. The plant operator was concerned that such a change

could lead to operating problems within the coil and

potentially lead to hydrocarbon cracking.

Johnson Matthey was requested to review the proposed

modification in order to determine if there would be any

problems. Our process engineers used Aspen Technology’s

FIHR simulation package to model the performance of the

existing coil. The initial FIHR model used rationalised plant

data in order to calibrate the model and ensure that it was

accurate. The FIHR model was then used to predict the

performance of the coil with the modifications included. The

predicted internal metal skin temperatures were used in

Johnson Matthey’s in-house programs to determine if

hydrocarbon cracking would occur.

This showed that performance of the coil would be acceptable

and that hydrocarbon cracking would not be an issue.

The plant has now been modified and, after a significant

period of operation, has not seen any pressure drop increase

over the hydrodesulphurization bed, confirming that the

model prediction of no carbon formation was correct.

Case study – TRACERCO ZnO scanreduces turnaround costs

A Western European ammonia producer intended to

replace its zinc oxide bed during a planned shut down as it

had been installed for some time. The operator however

had no idea how much of the absorbent had been used.

Prior to the shut down, a TRACERCO MAXIMIZER™ scan was

performed on the zinc oxide vessel. The scan determined

that the boundary between reacted and unreacted zinc

oxide appeared to be approximately 40% down the bed,

indicating that at least 50% of the bed was unreacted ZnO.

Following the scan the vessel was discharged with samples

of the absorbent taken at intervals down the bed depth. The

samples were analysed in the bed and confirmed that from

50% onwards, the bed was unreacted ZnO. The operator

only changed out 50% of the absorbent, which saved them

US$ 190,000 in turn-around costs.

Sulphur absorbent profile results of scanning

zinc oxide vessel


5

Impact of Ultrapurification Reformer Activity

and the poisoning problem cannot be resolved, and plant

rate has to be reduced, there will be a loss of production,

which has been proven to cost the plant operator

US$ 6.3 million per year.

By installing ultra-purification upstream of a pre-reformer,

the pre-reformer life can be extended greatly and this can

be worth US$ 250,000 in reduced pre-reformer catalyst

replacement costs.

Chlorides are very difficult to remove from a steam reformer

during a steam out and in many cases the primary reformer

catalyst will have to be changed out. The total cost for a two

week shut-down to replace the catalyst is estimated to be

US$ 2.6 million per week, including shut-down, catalyst and

lost production costs.

KATALCOJM PERFORMANCE adds value to your plantOne plant suffered from a poorly operating purification

system that slipped sulphur to the primary reformer. In

order to continue operating the plant shut down regularly

to steam the primary reformer and remove the sulphur.

Replacing the purification system with KATALCOJM

purification products eradicated the problem saving the

plant operator an estimated US$ 2,100,000 each year.

PURASPECJM ultra-purification absorbent was installed

on a plant and resulted in doubled the life of the steam

reforming catalyst. This saved the customer over

US$ 400,000 in replacement catalyst costs.

Following a TRACERCO MAXIMIZER scan of a zinc oxide

vessel, the plant operators determined that it was only

necessary to change 50% of the bed. This gave a saving of

US$ 190,000 in replacement zinc oxide costs.

A number of plants have removed their hydrodesulphurization

catalysts for a variety of reasons. Of these, one plant found

that the steam reformer catalyst soon became poisoned

and the plant was forced to conduct regular steam outs

whilst they investigated the root cause of the problem. By

the time it was found that the feed to the plant contained

significant levels of organic sulphur, the plant had conducted

three steam outs costing US$ 450,000 in lost production.

During the same period, the reformer tubes were run at

higher than normal temperatures and this reduced the

tube life which increased the tube replacement costs by

US$ 300,000.

The additional sulphur absorption capacity of KATALCOJM 32-5

over competitive materials allows for increased run lengths

and therefore a reduction in absorbent costs. This is worth

US$ 50,000 per charge of zinc oxide plus the cost of

having to conduct the absorbent change out.

The cost of poisoning a steam reforming catalyst charge is

significantly greater than the cost to install, monitor and

operate a good purification system. Operating a plant with a

poisoned steam reforming catalyst leads to hot bands which

in turn increase the tube wall temperature. This increased

temperature reduces the life of the steam reformer tubes,

increasing the tube replacement costs by US$ 250,000. In

such circumstances, if regular steam outs are not conducted


6

• Reliable operation

Dependable delivery of purified feed gas into the

downstream process, even during upset conditions,

ensures that the downstream catalysts are able to deliver

high conversion and maintain long operating lives.

• Stable pressure drop

High strength of catalysts ensures that even if pressure

drop starts to build up due to deposition of foulants on

top of the bed, catalysts are strong enough to withstand

the hydraulic forces applied.

Organic sulphur removal - HDS

Effective breakdown of organic sulphur compounds in the

feedstock is essential so that the H2S produced can be

removed downstream. In addition, the catalyst must break

down any organo-chlorine compounds and hydrogenate

olefins to a level acceptable for the steam reformer.

The KATALCOJM HDS catalysts are available in both cobalt

molybdenum (CoMo), KATALCOJM 41-6T, and nickel

molybdenum (NiMo), KATALCOJM 61-1T, formulations to suit

the combination of reactions for particular plant situations.

KATALCOJM 41-6T and KATALCOJM 61-1T are manufactured

with an optimized loading of active components to give high

volumetric activity and ensure high selectivity for

hydrogenation. The high activity allows the catalyst to cope

with increased feed rates, upsets and impurities which would

otherwise lead to slippage of un-reacted organic sulphur

compounds. The products also remove trace levels of

arsenic compounds and, in the case of certain heavy

naphtha feeds, traces of most metallic species.

The trilobe shape offers a lower pressure drop than standard

extrudates. In addition, the strength and attrition resistance

are improved to minimize breakage during loading and

operation, so that a low pressure drop can be maintained

throughout the catalyst life.

The purification section in a syngas plant is usually designed

in two to four stages depending on the plant design

requirements. In the hydrodesulphurization (HDS) stage, the

organic sulphur compounds are catalytically converted to

liberate sulphur as hydrogen sulphide with analogous

reaction of any organo-chlorine compounds. The HDS

catalyst also acts as a trapping agent for many of the less

usual poisons if these are present. Where necessary, an

absorbent is next installed to remove hydrogen chloride by

chemical reaction. The third stage is removal of hydrogen

sulphide using absorbents based on zinc oxide, which reacts

to form zinc sulphide. In certain plants, a fourth ultra-

purification stage is used to reduce the sulphur content of

the feed to extremely low levels.

Operational benefits

All Johnson Matthey purification catalysts offer a number of

operational benefits:

• Flexible operating conditions

KATALCOJM and PURASPECJM catalysts and absorbents

can be operated over a wide range of temperatures,

pressures and feedstocks. For example, HDS catalysts and

zinc oxide absorbents have operated continuously in

systems designed to run at temperatures as low as 250°C

(482°F) and pressure as high as 50 bar (725 psi). Our

purification catalysts are proven to be effective on a wide

range of feedstocks, from light natural gases, through

LPG’s, light naphthas to heavy naphthas containing 20%

aromatics.

• Long lives

High activity and excellent absorption capacity mean that,

with appropriate product selection, the purification

catalysts lives will be maximized while extending the life of

the downstream catalysts.

Advantages of choosing Johnson Matthey purification

catalysts and absorbents


7

Desulphurization – zinc oxide

The performance of zinc oxide based H2S removal

absorbents is strongly influenced by the formulation of the

product. Usage of a very high purity zinc oxide (say 99+ wt%)

of the highest possible density would place the most

theoretical sulphur capacity in a reactor but would not

provide the best performance in practice. This is due to the

very low porosity and huge mass transfer zone of such a

product, resulting in premature breakthrough of sulphur to

downstream catalyst. Products must be formulated with the

highest possible porosity to facilitate the reaction between

the H2S and zinc oxide to maximize the rate and extent of

sulphur absorption. In turn, this leads to a tight mass

transfer zone and maximizes sulphur absorption capacity

and therefore the absorbent life for a given installed volume.

KATALCOJM 32-series absorbents combine specific zinc

oxide phases with a binder using granulation technology to

produce spheres with the required combination of

properties to provide excellent sulphur absorption capacity

in the differing designs for zinc oxide beds.

KATALCOJM 32-4 is a higher porosity material which has a

particularly sharp sulphur profile. This ensures that

conversion of the zinc oxide in the bed, and therefore

sulphur pick up, is maximized before sulphur breakthrough

occurs. KATALCOJM 32-4 is the product of choice for plants

which are designed with a single sulphur removal bed.

KATALCOJM 32-5 is a higher density material and provides

maximum saturation pick-up. This makes it ideal material for

two bed series lead/lag system designs. The lag bed provides

protection of the downstream process while the sulphur

level exiting the lead bed is allowed to increase before

replacement of the spent bed is required. This allows the

higher saturation capacity of the KATALCOJM 32-5 to be

fully utilized.

Chloride removal

Where chloride species are present in hydrocarbon feeds,

the level is usually low. After these species are converted to

hydrogen chloride over the HDS catalyst, they are present as

hydrogen chloride and must be removed upstream of the zinc

oxide absorbent. Zinc oxide reacts with chlorides to form zinc

chloride and this adversely affects the porosity of the zinc oxide

bed. This in turn impairs its sulphur absorption capacity and

reduces the absorbent life. In addition, at normal operating

temperatures, zinc chloride may migrate causing potential

poisoning, corrosion and metallurgy issues downstream.

The low chloride level means that the volume of absorbent

required is usually small as long as it has a good chloride

capacity. Consequently, it is usually included in the same

reactor(s) as the zinc oxide as a thin top layer. The low contact

time necessitates a fast efficient reaction between the HCl and

its absorbent to effectively remove chloride to extremely low

levels needed for protection of downstream catalysts.

KATALCOJM 59-3 is formulated to provide fast reaction times

and to have a high capacity for chloride removal. It contains

a highly reactive alkali phase, sodium aluminate, dispersed

on an alumina substrate. The gas phase reaction between

HCl and sodium aluminate locks up the chloride as sodium

chloride. Where higher chloride levels are encountered, the

high reactivity of KATALCOJM 59-3 allows spikes of HCl to be

removed effectively without compromising plant operation.


8

PURASPECJM for unusual purificationrequirements

In addition to our standard products, Johnson Matthey

Catalysts offer a number of PURASPECJM catalysts and

absorbents for difficult or unusual purification duties.

Arsenic as arsine or organo-arsine can be found

occasionally in natural gas and LPG cuts. Although the HDS

catalyst will remove these, the arsenic compounds act as a

poison. An alternative approach is to treat the hydrocarbon

upstream using a dedicated arsenic guard bed. For gas

phase, we recommend PURASPECJM 1152 whereas, for

liquid phase LPG, it is PURASPECJM 5152.

Mercury and organo-mercury compounds are being

reported more frequently in various hydrocarbon sources in

part due to improved analytical methods and in part due to

increased processing of mercury containing sources.

Mercury has been found in the ammonia synthesis section

of certain plants implying that it passes through the entire

flowsheet. Thus, if mercury is identified in the feed,

upstream treatment should be considered. For gas phase,

we recommend PURASPECJM 1156 whereas, for liquid phase

naphtha, it is PURASPECJM 6156. These products are able to

remove mercury to below ppb levels.

For various reasons, in certain flowsheets it is necessary to

run the purification section cooler than usual. In these cases,

special HDS catalyst and zinc oxide absorbents are preferred

which are optimized for the lower temperature. Where the

HDS reactor must operate at an inlet temperature below

300°C (572°F), KATALCOJM 61-2T is the preferred product.

This has a higher active metal level to initiate the reaction at a.cooler temperature. For H2S removal below 250°C (482°F),

PURASPECJM 2020 is preferred to KATALCOJM 32-series.

Ultra-purification

Ultra-purification or sulphur polishing absorbents are

appropriate in some specific plant circumstances where the

downstream catalysts are more susceptible to poisoning

even by low sulphur levels. Analysis indicates that the total

sulphur level exiting the zinc oxide absorbent is typically a

few tens of ppb comprising of H2S, COS and traces of

organo-sulphur species. The precise levels and mix vary as a

function of the feedstock composition, operating conditions

and effectiveness of the purification products installed. This

low level of sulphur may still have a negative impact, for

example, if the plant has a pre-reformer or a highly stressed

top fired reformer since these are both particularly sensitive

to sulphur poisoning. Thus, to maximize the life of these

absorbents, Johnson Matthey Catalysts recommends the use

of an ultra-purification catalyst, PURASPECJM 2084, as a

final stage in the purification system. This reacts with and

removes most of the trace sulphur compounds typically to

levels below 10 ppbv.


9

Since both of these methods have drawbacks, Johnson

Matthey recommends supplementing sample analysis with the

TRACERCO MAXIMIZER zinc oxide bed scanning technique.

This is a proven, highly effective method for determining zinc

oxide usage and prediction of remnant bed life. It uses an

external scanning device and so there is no need for a plant

shut down. Results are available almost instantly.

This measurement uses a radioactive neutron source and a

neutron detector to measure neutron back-scattering and to

detect density differentials in the material inside the vessel.

As zinc sulphide is more dense than zinc oxide, there is

greater neutron absorption through zinc sulphide than zinc

oxide. This difference is measured and therefore accurately

determines the position of the interface.

This service is available through the Johnson Matthey

TRACERCO business.

Monitoring consumption of ZnO

Proper monitoring to ensure optimum utilization of a zinc

oxide charge is a challenging task. One method of

calculating zinc oxide usage is to measure inlet and exit

sulphur levels together with gas flow rate to calculate the

amount of sulphur removed. This value can be compared to

the expected sulphur capacity of the bed to estimate the

proportion of the zinc oxide consumed and also to predict

the remaining life for the bed. In plants with frequent on line

low level sulphur analysis combined with flow monitoring,

this calculation may be reasonably accurate. Many plants,

however, rely on analysis of gas samples taken from the

process at intervals, sometimes with several days between

samples. This procedure reduces the calculation accuracy

and increases the risk of sulphur breakthrough.

Sampling of inlet gas sulphur content at intervals may not

identify variation and spikes in the sulphur content of the feed.

For example, natural gas may become sour as the wells

approach exhaustion. Alternatively, natural gas may be taken

from a number of fields with variation in sulphur content and

mixed in varying proportions. In such cases, samples analysed

at intervals are unlikely to detect variation accurately. Thus, the

calculation of the inlet sulphur will be inaccurate.

Sampling of exit gas sulphur content is essential to

determine that the downstream catalysts are protected. If

sampling at intervals, however, it is possible that the critical

point when breakthrough occurs may be missed. Also, exit

gas sampling provides no direct information on the extent to

which the zinc oxide bed has been consumed or of impending

sulphur breakthrough. Only a small proportion of plants

have gas sample points down the bed and even then the

gas sample may not be representative if the sample point is

damaged or blocked.

Additional capability with KATALCOJM PERFORMANCE


10

Sulphur sampling system design

Sulphur sampling and testing is a highly complex area.

Johnson Matthey Catalysts has a detailed knowledge of the

process and mechanical design of the sampling system and

also an extensive understanding of the analysis

methodologies. Using this, Johnson Matthey Catalysts can

review sampling and testing systems to identify improvement

opportunities. This will ensure that any sulphur that does slip

from the desulphurization will be detected before the impact

on the downstream equipment and catalysts is significant.

Catalyst probe

The TRACERCO catalyst probe allows insertion of a sample

of catalyst into a process stream. By selecting an

appropriate absorbent/catalyst it is possible to check for the

presence of poisons within a stream and thereby determine

the root cause of downstream problems. Intermittent ‘slugs’

of poisons can be identified using the sample probe

whereas such random levels of poisons will be almost

impossible to identify with spot sampling of the process

stream, but yet can cause severe plant problems.

Trouble-shooting – sulphur analysis

It is often helpful to determine the type of poisons present

in a feedstock to assist in designing the optimum purification

system. Johnson Matthey Catalysts can offer users of its

products a detailed sulphur analysis services through our

state of the art equipment for the characterisation of

sulphur compounds. The equipment utilizes a

chromatograph with a chemiluminescence detector that

allows for measurement and speciation of sulphur

containing compounds at levels of between 10 and 20 ppbv.

In comparison, the sulphur slip from zinc oxide is typically

50 ppbv and from ultra-purification is 10 ppbv.


11

This figure illustrates typical locations for installation of the

catalyst probe. A probe installed upstream of the purification

system will pick up and allow identification of the poisons in

the feed gas. A probe installed downstream of the purification

system will allow pick up and identification of any poisons

that have slipped through the purification system.

Carbon prediction in feed pre-heat coil

One problem that some operators have faced in the past has

been a gradual build up in the pressure drop across the

hydrodesulphurization bed which is greater than expected.

On inspection of the inlet distributor and catalyst bed,

significant amounts of carbon has been found to be have

been deposited. The root cause of this is that although the

bulk gas temperature leaving the feed pre-heat coils is not

high enough to cause hydrocarbon cracking, the internal

metal skin temperature of the coil can be much hotter than

this. In some cases, this temperature is sufficiently high that

hydrocarbons, particularly longer chained species, will crack

and the carbon is deposited on the catalyst bed.

Johnson Matthey Catalysts can provide detailed modelling of

the feed pre-heat coil to determine whether this will be an

issue or not. Using the HYSYS flowsheet package available

from our partner, Aspen Technology, a model can be

constructed that defines the heat and mass balances

around the pre-heat coil. From this heat and mass balance,

a more detailed model of the coil itself is produced using

Aspen Technology’s FIHR program. This allows for

determination of the internal skin temperature of the coil.

Using Johnson Matthey’s in-house carbon cracking models,

it is possible to determine the cracking temperature of the

feed and therefore whether there is a potential problem in

the feed pre-heat coil.

Such modelling is useful in troubleshooting pressure drop

problems over a hydrodesulphurization vessel and also in

determining whether changes in operating conditions will

change the temperature regime such that hydrocarbon

cracking will be an issue.


12

KATALCOJM and PURASPECJM purification catalysts are

suitable for the full range of feeds to synthesis gas plants,

whether an off gas, a natural gas, LPG or naphtha. Typical

recommendations for our standard purification products are

given below, however, Johnson Matthey Catalysts will provide

specific recommendations to suit particular plant conditions

depending on the feedstock composition, poisons present

and vessel configuration.

Johnson Matthey Catalysts are experts in difficult and

unusual purification requirements and for these applications

offer the PURASPECJM product range for a wide range of

trace impurity removal. These include HDS catalyst and ZnO

absorbents for low temperature applications, as well as

products to remove the less usual poisons such as mercury

and arsenic compounds.

Catalyst selectorPre-sulphided HDS catalysts may be recommended in the

following circumstances:

Pre-sulphiding can be achieved in situ by injection of a

sulphiding agent with hydrogen at defined conditions.

Alternatively, Johnson Matthey Catalysts can deliver the

catalyst in the pre-sulphided form.

PURASPECJM products may be recommended for removal of

the less usual poisons. The most frequently offered products

are summarised.

Feedstock impurity/ KATALCOJM product

operating situation recommendation

organic sulphur 41-6T

olefins saturation 61-1T

high COx content 61-1T

halide removal 59-3

low sulphur content (single bed) 32-4

moderate sulphur content (single bed) 32-5 & 32-4

high sulphur content (lead lag beds) 32-5

downstream pre-reformer PURASPECJM 2084

long reformer catalyst cycle times PURASPECJM 2084

Operating situation PURASPECJM product

recommendation

mercury PURASPECJM 1156/

PURASPECJM 6156

arsenic PURASPECJM 1152/

PURASPECJM 5152

low temperature HDS KATALCOJM 61-2T

low temperature ZnO PURASPECJM 2020

very high sulphur feeds fully active immediately

high olefin feeds fully active immediately

high carbon oxide feeds avoid methanation

very low sulphur feeds avoid possible over reduction

very high hydrogen feeds avoid possible over reduction


13

Catalyst characteristics

Physical properties (typical)

Composition

KATALCOJM 41-6T cobalt oxide/molybdenum oxide/alumina

KATALCOJM 61-1T nickel oxide/molybdenum oxide/alumina

KATALCOJM 59-3 sodium aluminate/alumina

KATALCOJM 32-4 zinc oxide

KATALCOJM 32-5 zinc oxide

PURASPECJM 2084 copper/zinc oxide/alumina

Catalyst KATALCOJM 41-6T KATALCOJM 61-1T KATALCOJM 59-3 KATALCOJM 32-4 KATALCOJM 32-5 PURASPECJM 2084

Form trilobe extrusions trilobe extrusions spherical granules spherical granules spherical granules spherical granules

Diameter 2.5 2.5 2.0-4.75 2.8-4.75 2.8-4.75 2.5-4.75

(mm)

Typical loaded density

(kg/m3) 590 560 860 1140 1350 870

(lb/ft3) 37 35 54 71 84 54

KATALCOJM 61-1T

KATALCOJM 59-3

KATALCOJM 41-6T

KATALCOJM 32-4

KATALCOJM 32-5

PURASPEC 2084


PO Box 1

Belasis Avenue

Billingham

Cleveland

TS23 1LB

UK

Tel +44 (0)1642 553601

Fax +44 (0)1642 522542

Oakbrook Terrace

Two Transam Plaza Drive

Chicago

Illinois 60181

USA

Tel +1 630 268 6300

Fax +1 630 268 9797

For further information on Johnson Matthey Catalysts, contact your local sales office or visit our website at www.jmcatalysts.com

KATALCO, PURASPEC, STREAMLINE and TRACERCO are trademarks of the Johnson Matthey group of companies.

www.jmcatalysts.com© 2005 Johnson Matthey Group

1061JM/0307/2/AMOG


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