EP0191083A1 - Fischer-tropsch catalysts - Google Patents
Fischer-tropsch catalystsInfo
- Publication number
- EP0191083A1 EP0191083A1 EP85904269A EP85904269A EP0191083A1 EP 0191083 A1 EP0191083 A1 EP 0191083A1 EP 85904269 A EP85904269 A EP 85904269A EP 85904269 A EP85904269 A EP 85904269A EP 0191083 A1 EP0191083 A1 EP 0191083A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- carbon
- vii
- catalyst according
- surface area
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
- C07C1/0425—Catalysts; their physical properties
- C07C1/043—Catalysts; their physical properties characterised by the composition
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- C07C2527/06—Halogens; Compounds thereof
- C07C2527/08—Halides
- C07C2527/10—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- C07C2527/06—Halogens; Compounds thereof
- C07C2527/128—Compounds comprising a halogen and an iron group metal or a platinum group metal
Definitions
- the present invention relates to catalysts suitable for use in the Fischer-Tropsch process, and to a Fischer-Tropsch process carried out using the catalysts.
- a supported Fischer-Tropsch catalyst containing a catalyst metal is characterised in that the catalyst contains a, minor amount of an element of Groups VI and VII of the Periodic Table.
- the element is preferably in the form of an anion.
- the element or anion must be one which is adequately stable to hydrogenation under the conditions used.
- the anion is preferably an anion of the element itself, not linked: to other elements.
- Preferred anione are the halides eg chloride.
- Table introduced is preferably such that the conversion of CO by the catalyst is not less than 20%, preferably not less than 40% of the conversion (under the same conditions) obtained with a catalyst prepared in the same way but without the presence of the Group VI or
- the catalyst of the present invention preferably has an activity such that at a temperature of 300°C, an H 2 :CO ratio of 2:1, a pressure of 0.7 MPa absolute, and a GHSV of 500 h -1 the CO conversion is at least 50%, preferably at least 70%.
- the quantity of the element may for example be in the range
- the Fischer-Tropsch catalytic metals are active in the metallic form.
- the element of Group VI-VII must therefore be introduced without affecting the ability to reduce the metallic catalyst, and must not be removed by the procedures used to prepare and activate the catalyst.
- the metal halide can be reduced some or all of the halide will be removed as the hydrogen halide. Where the halide cannot be reduced or when the halide is retained by the reduced catalyst an active catalyst will not be obtained.
- Fischer-Tropsch catalysts from ferric chloride or cobaltous chloride the resulting products had such low activities (due to Insufficient active metal and/or excessive Group VII element) that they were not useful Fischer-Tropsch catalysts.
- the introduction of the Group VI or VII element is therefore preferably a separate operation from the deposition of the catalytic metal.
- the element of Group VI or VII may conveniently be introduced by using a non-metallic compound, either an inorganic compound for example an ammonium compound e.g. ammonium chloride, or an organic compound e.g. a chlorohydrocarbon which decomposes to give chlorine under the conditions under which it is introduced or under the reaction conditions.
- a non-metallic compound either an inorganic compound for example an ammonium compound e.g. ammonium chloride, or an organic compound e.g. a chlorohydrocarbon which decomposes to give chlorine under the conditions under which it is introduced or under the reaction conditions.
- Fischer-Tropsch catalysts and methods of making them are well-known.
- Examples of catalytic metals which may be used are Co, Fe and Ni but Ru may also be used.
- the quantity of catalytic metal (e.g. iron or cobalt) deposited on the catalyst may be in the range 5 to 100% wt based on weight of support.
- the catalyst may be prepared by impregnation with an aqueous solution of a salt of the catalytic metal. Examples of suitable salts are nitrates.
- Fischer-Tropsch catalysts e.g. inorganic metal oxides e.g. alumina, silica, thoria, zirconia, and molecular sieves.
- the present invention Is particularly useful when applied to catalysts according to our copending patent application bib (Case 5869) comprising cobalt or iron on a support characterised in that the support is a carbon having a BET surface area of at least 100 m 2 /g, a ratio of BET to basal plane surface area not greater than 4:1, and a ratio of basal plane surface area to edge surface area of at least 10:1.
- Carbons may be characterised by their BET, basal plane, and edge surface areas.
- the BET surface area is the surface area determined by nitrogen adsorption using the method of Brunauer
- the basal plane surface area is the surface area determined from the heat of adsorption on the carbon of n-dotriacontane from n-heptane by the method described in Proc.Roy.Soc. A314 pages 473-498, with particular reference to page 489.
- the edge surface area is the surface area determined from the heat of adsorption on the carbon of n-butanol from n-heptane as disclosed in the Proc.Roy.Soc. article mentioned above with particular reference to page 495.
- the carbon supports are known, for example from GB 1 565 074.
- the catalysts of the present Invention behave in a completely different manner from the catalysts of GB 1 565 074.
- the catalysts of GB 1 565 074 have their activity increased by the presence of alkali metals, and the presence of chloride ion is stated to be undesirable.
- the preferred carbons for use in the present invention have a BET surface area of at least 200 m 2 /g,most preferable at least 300m 2 /g.
- the BET surface area is preferably not greater than 1000 m 2 /g, more preferably not greater than 750 m 2 /g.
- the ratio of BET to basal plane surface area is preferably not greater than 2.5:1. It is particularly preferred to use carbons with ratios of BET to basal plane surface area of not greater than 1.5:1.
- carbons with ratios of basal plane surface area to edge surface area of at least 100:1. It is not believed that there is an upper limit on the ratio, although in practice it will not usually exceed 200:1.
- the preferred carbon support may be prepared by heat treating a carbon-containing starting material.
- the starting material may be an oleophilic graphite e.g. prepared as disclosed in GB 1 168 785 or may be a carbon black.
- oleophilic graphites contain carbon in the form of very fine particles in flake form and are therefore not very suitable materials for use as catalyst supports. We prefer to avoid their use. Similar considerations apply to carbon blacks which also have a very fine particle size.
- the preferred materials are activated carbons derived from vegetable materials e.g. coconut charcoal, or from peat or coal or from carbonizable polymers.
- the materials subjected to the heat treatment preferably have particle sizes not less than these indicated above as being preferred for the carbon support.
- the preferred starting materials have the followingcharacteristics: BET surface area of at least 100, more preferably at least 500 m 2 /g.
- the preferred heat treatment procedure for preparing carbon supports having the defined characteristics comprise successively (1) heating the carbon in an inert atmosphere at a temperature of from 900°C to 3300°C, (2) oxidizing the carbon at a temperature between 300°C and 1200°C, (3) heating in an Inert atmosphere at a temperature of between 900°C and 3000°C.
- the oxidation step is preferably carried out at temperatures between 300° and 600oC when oxygen (eg as air) is used as the oxidising agent.
- the duration of the heating in inert gas is not critical.
- the time needed to heat the carbon to the required maximum temperature is sufficient to produce the required changes in the carbon.
- the oxidation step must clearly not be carried out under conditions such that the carbon combusts completely. It is preferably carried out using a gaseous oxidizing agent fed at a controlled rate to avoid over oxidation. Examples of gaseous oxidising agents are steam, carbon dioxide, and gases containing molecular oxygen eg air.
- the oxidation is preferably carried out to give a carbon weight loss of at least 10% wt based on weight of carbon subjected to the oxidation step, more preferably at least 15% wt.
- the weight loss is preferably not greater than 40 % wt of the carbon subjected to the oxidation step, more preferably not greater than 25 % wt of the carbon.
- the rate of supply of oxidizing agent is preferably such that the desired weight loss takes place over at least 2 hours, more preferably at least 4 hours.
- an inert atmosphere may be supplied by nitrogen or an inert (Group 0) gas.
- the catalysts of the present invention may be used for the Fischer-Tropsch conversion of synthesis gas to hydrocarbons which are liquid at normal temperatures and pressures.
- the temperature may for example be in the range 150° to 300°C, preferably 200 to 250oC.
- the pressure may for example be in the range 1 to 50 bar.
- the molar ratio of hydrogen to carbon monoxide may for example be In the range 3:1 to 1:1, more preferably about 2:1.
- the gas hourly space velocity may be 100 to 10000, preferably 500 to 3000.
- the carbon used as support was prepared from a commercially available extrudate activated carbon sold by Degussa under the designation Katepon BKIV.
- the carbon was in the form of extrudates of 4mm diameter and had typical BET, basal plane, and edge surface areas of 939,182 and 32 m 2 /g respectively.
- the activated carbon was heat treated as follows. The carbon was heated from room temperature in a stream of helium to 1700°C over a period of about 1 hour. When the temperature reached 1700oC the carbon was allowed to cool in the stream of helium to 25°C. The carbon was then heated in air in a muffle furnace at approximately 520°C for a time known from experience to give a weight loss of 20 %wt. The carbon was then heated in helium to between 1800°C and 1850°C as In the helium heating step mentioned above. The carbon was allowed to cool to room temperature in a helium atmosphere.
- Typical values found for carbon treated in this manner were: BET surface area 710-749 m 2 /g Basal plane surface area 416-666 m 2 /g
- the support was ground and sieved to 16-30 mesh (0.5-1.0 mm) and washed by refluxing in (1) dilute (10% w/w) hydrochloric acid and (2) distilled water to remove sulphur and impurity transition metals before use.
- the carbon was then impregnated with an aqueous solution of cobalt nitrate (analytical reagent grade).
- the quantity of cobalt nitrate used was such that 10g of carbon support were treated with 2g of cobalt (giving a nominal metal loading of 16.7% w/w based on weight of catalyst).
- the quantity of water used was the minimum used necessary to ensure even wetting of the carbon support (a few drops of methanol may be added to assist in wetting of the support).
- the impregnation of the carbon was conducted in a rotary evaporator at 50-80°C under a vacuum of 200-800 m bar (20 kPa-80 kPa).
- the impregnated carbon was dried overnight in a vacuum oven at 120°C, 200-300 m bar (20 kPa-30 kPa).
- the catalyst was tested (using a 2.2ml sample) in a oncethrough microreactor equipped with an on-line gas chromatography apparatus to analyse for CO, CO 2 , and C 1 -C 10 organic products.
- the catalyst was reduced before use by treating for 2-8 hours with a stream of hydrogen (25-100 ml/min) at 400-450°C and 8 bar (0.8 MPa) gauge. Synthesis gas at a molar ratio of CO-H 2 of 2:1 was then admitted.
- the conditions used and the results obtained are given in Table 1. Definition of Terms used in the Results
- the CO conversion is defined as the percentage of the carbon monoxide fed to the reactor that was converted to analysed products. It may be represented as:
- the selectivity to organic products is defined as the percentage of the total carbon monoxide converted to C 1 -C 10 organic products rather than to CO 2 . It may be represented as:
- the alpha factor represents the relative quantities of the organic products and is defined by P. Biloen and W.M.H. Sachtler in
- the gas hourly space velocity is defined as the ml/hour of CO/H 2 feedstock (at NTP) per ml of catalyst.
- Example 1 The Example shows the effect of chlorine on the catalysts of the present invention.
- Test A After a sample of the catalyst used in Test A had been reduced with hydrogen it was impregnated with ammonium chloride so as to add 0.1% w/w chlorine. The catalyst was then tested as in Test A and the results given in Table 1. A reduction In activity (from 99% to 67% at about 270°C) was accompanied by an increase in the selectivity towards organic products (from 65% to 75% at about 270°C). Test B A further batch of catalyst was prepared and tested as in Test A. The results are given in Table 2.
- Example 2 Example 2
- Test B was repeated except that chlorine was introduced on to the catalyst by treatment with chloroethane.
- a quantity of chloroethane calculated to introduce 0.3% w/w of catalyst of chlorine was passed in a stream of hydrogen (1% v/v in hydrogen) over another sample of the catalyst prepared for in Test B.
- a gas flow of 3 ml/min (total flow) was used at 225°C and atmospheric pressure. For the purposes of calculating the amount to be used it was assumed that all chlorine fed was retained by the catalyst. The results are given In Table 2. Comparative Test C
- Example 6 was repeated except that 0.05% w/w of chlorine was introduced by re-impregnation of a sample of the reduced catalyst with ammonium chloride. The results are shown in Table 3. Test D
- Test D The catalyst used in Test D was retained in the test reactor and the pressure was then reduced to atmospheric pressure and 1% v/v chloroethane in hydrogen was then passed over the catalyst (as described in Example 2) until a theoretical chlorine loading of 0.05% w/w had been achieved. The activity and selectivity of the resulting catalyst was then measured as previously. The cycle of pressure reduction and chloroethane treatment was subsequently repeated to give cumulative chlorine loadings of 0.15, 0.25 and 0.50% w/w. The effect of increase in chlorine content is clearly indicated in Table 4.
- a carbon support was prepared using a method similar to that described in Test A.
- the starting material however was a commercially available activated carbon sold by Degussa as BK 16.
- the heat-treated carbon used as support had the following surface area values:-
- the particle size was 16-30 BSS (0.5-1mm).
- a carbon-supported catalyst containing 16.7% w/w of iron as graphitised carbon was prepared from ferric chloride using the technique described in Test A. The results are shown in the Table 5 and show very low catalyst activity. Comparative Test F
Abstract
Catalyseurs Fischer-Tropsch supporté, contenant une faible quantité d'un élément des groupes VI et/ou VII de la table périodique. Cette composition permet de réduire le CO2.Supported Fischer-Tropsch catalysts, containing a small amount of an element from groups VI and / or VII of the periodic table. This composition makes it possible to reduce the CO2.
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB8421828 | 1984-08-29 | ||
GB848421828A GB8421828D0 (en) | 1984-08-29 | 1984-08-29 | Fischer-tropsch catalysts |
Publications (1)
Publication Number | Publication Date |
---|---|
EP0191083A1 true EP0191083A1 (en) | 1986-08-20 |
Family
ID=10565984
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP85904269A Pending EP0191083A1 (en) | 1984-08-29 | 1985-08-29 | Fischer-tropsch catalysts |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0191083A1 (en) |
AU (1) | AU4770885A (en) |
GB (1) | GB8421828D0 (en) |
WO (1) | WO1986001500A1 (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
MY171507A (en) * | 2013-07-24 | 2019-10-16 | Shell Int Research | Process for preparing a chlorine comprising catalyst, the prepared catalyst, and its use |
US20160160128A1 (en) * | 2013-07-24 | 2016-06-09 | Shell Oil Company | Method for starting up a fischer tropsch process |
AU2014295288B2 (en) * | 2013-07-24 | 2016-10-27 | Shell Internationale Research Maatschappij B.V. | Process for preparing a chlorine comprising catalyst, the prepared catalyst, and its use |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB621902A (en) * | 1946-08-23 | 1949-04-22 | Standard Oil Dev Co | Improved process for the catalytic synthesis of hydrocarbons |
US4054644A (en) * | 1972-03-16 | 1977-10-18 | Exxon Research & Engineering Co. | Water gas shift process |
GB1565074A (en) * | 1976-11-03 | 1980-04-16 | British Petroleum Co | Process for the production of ammonia |
US4478954A (en) * | 1983-05-23 | 1984-10-23 | Standard Oil Company (Indiana) | Synthesis gas reaction |
-
1984
- 1984-08-29 GB GB848421828A patent/GB8421828D0/en active Pending
-
1985
- 1985-08-29 EP EP85904269A patent/EP0191083A1/en active Pending
- 1985-08-29 AU AU47708/85A patent/AU4770885A/en not_active Abandoned
- 1985-08-29 WO PCT/GB1985/000386 patent/WO1986001500A1/en not_active Application Discontinuation
Non-Patent Citations (1)
Title |
---|
See references of WO8601500A1 * |
Also Published As
Publication number | Publication date |
---|---|
AU4770885A (en) | 1986-03-24 |
GB8421828D0 (en) | 1984-10-03 |
WO1986001500A1 (en) | 1986-03-13 |
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Legal Events
Date | Code | Title | Description |
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PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
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17P | Request for examination filed |
Effective date: 19860425 |
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AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): BE DE FR GB IT NL |
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17Q | First examination report despatched |
Effective date: 19870630 |
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STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
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RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: PARTINGTON, STEPHEN, ROY Inventor name: SPIERS, RANALD, GORDON, LYON Inventor name: FOSTER, ALAN, IVOR Inventor name: JOYNER, RICHARD, WILLIAM |