CA1333006C - Shut-down process for a fischer-tropsch reactor, and said reactor - Google Patents
Shut-down process for a fischer-tropsch reactor, and said reactorInfo
- Publication number
- CA1333006C CA1333006C CA000605253A CA605253A CA1333006C CA 1333006 C CA1333006 C CA 1333006C CA 000605253 A CA000605253 A CA 000605253A CA 605253 A CA605253 A CA 605253A CA 1333006 C CA1333006 C CA 1333006C
- Authority
- CA
- Canada
- Prior art keywords
- reactor
- catalyst
- inert
- hydrogen
- bodies
- 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.)
- Expired - Fee Related
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- 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
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/04—Feed or outlet devices; Feed or outlet control devices using osmotic pressure using membranes, porous plates
-
- 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
- C07C1/0405—Apparatus
-
- 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
- C07C1/0455—Reaction conditions
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The invention relates to a process for the shut-down of a reactor which is used for the preparation of an at least partly liquid hydrocarbonaceous product by reaction of carbon monoxide with hydrogen at elevated temperature and pressure and using a catalyst, which reactor is provided with cooling means and with means to recycle gas through the catalyst for temperature equalizing of the catalyst, comprising the steps of:
(i) interrupting the feed of synthesis gas;
(ii) depressurizing the reactor downstream of the catalyst, and providing the reactor upstream of the catalyst with inert gas; and (iii) cooling the catalyst to ambient conditions.
The invention relates further to a reactor suitable for carrying out the shut-down process.
(i) interrupting the feed of synthesis gas;
(ii) depressurizing the reactor downstream of the catalyst, and providing the reactor upstream of the catalyst with inert gas; and (iii) cooling the catalyst to ambient conditions.
The invention relates further to a reactor suitable for carrying out the shut-down process.
Description
13330~
SHUT-DOWN PROCESS FOR A FISCHER-TROPSCH
REACTOR, AND SAID REACTOR
The invention relates to a shut-down process for a reactor which is used for the preparation of an at least partly liquid hydrocarbonaceous product by reaction of carbon monoxide and hydrogen at elevated temperature and pressure using a Fischer-Tropsch catalyst, and to a reactor specifically designed for carrying out this shut-down process.
Processes for the preparation of an at least partly liquid hydrocarbonaceous product by catalytic 1~ reaction of carbon monoxide with hydrogen (synthesis gas) are well known. This reaction is highly exothermic and cooling means are used in the reactor for the removal of heat from the reaction zone. Additionally such a reactor is usually provided with means to recycle gas through the catalyst for equalizing the temperature in the catalyst bed. Preferably such a reactor is also provided with means to recycle liquid hydrocarbonaceous product through the catalyst for equalizing the temperature of the catalyst bed, and further to avoid the formation of hydrocarbonaceous deposits on the catalyst.
When such a reactor is to be shut-down the supply of carbon monoxide and hydrogen is interrupted. In the dome-like reactor space above the catalyst bed a large amount of reactant gas mixture is present, which will pass through the catalyst bed at a relatively low velocity. The reaction heat is insufficiently removed and hot spots are formed in the catalyst bed. These hot spots result in a deterioration of the performance of the catalyst.
13~300~
The invention has for its object to provide a shut-down process which does not result in a deterioration of the performance of the catalyst and includes a passivation thereof.
The invention relates to a process for the shut-down of a reactor which is used for the preparation of an at least partly liquid hydrocarbonaceous product by reaction of carbon monoxide and hydrogen at elevated temperature and pressure and using a catalyst, which reactor is provided with cooling means and with means to recycle gas through the catalyst for temperature equalizing of the catalyst, comprising the steps of:
(i) interrupting the feed of synthesis gas;
15 (ii) depressurizing the reactor downstream of the catalyst, and providing the reactor upstream of the catalyst with inert gas; and (iii) cooling the catalyst to ambient conditions.
Accordingly after the interruption of the supply of carbon monoxide and hydrogen (primary synthesis gas as well as recycled synthesis gas), a gas stream through the catalyst bed is maintained at a sufficient velocity to prevent the formation of hot spots, which gas stream becomes more and more inert by the increasing proportion of inert gas. The supply of inert gas is maintained until the catalyst is cooled down to ambient conditions. Then the catalyst can be unloaded.
When the reactor is provided with means to recycle liquid product through the catalyst, the process comprises further between step (ii) and step (iii) the step (iia) of cooling the catalyst to a temperature slightly above the solidification temperature of the liquid product; and (iib) of interrupting the recycling of the liquid product, so that initially the liquid product recycling is used for the cooling and temperature levelling and deposits of solidified hydrocarbons are avoided.
Since hydrogen is available in large amounts in the plant in which the reactor is used, hydrogen is preferably used as inert gas.
In order to reduce the amount of the reactant gas mixture in the dome-like space above the catalyst bed, it is advantageous to arrange inert packing bodies, for example spherical bodies, in the reactor space above the catalyst.
When the inert bodies contain hydrogen releasable therefrom when the pressure in the reactor falls below the working pressure, hydrogen is automatically released in the reactor space above the catalyst when during the shut-down operation the supply of carbon monoxide and hydrogen is interrupted.
Hydrogen for use during the shut-down process is accumulated in or on the inert bodies during the normal operation of the reactor, when according to a first embodiment the inert bodies comprise an interfacial membrane permeable to hydrogen and impermeable to carbon monoxide, or according to a second embodiment the inert bodies comprise material which absorbs hydrogen under reaction conditions and desorbs hydrogen under shut-down conditions.
The invention relates further to a reactor suitable for carrying out the shut-down process, comprising a reactor housing provided with at least one catalyst section containing catalyst, which section is in communication with inlet means for synthesis gas, with product outlet means, with means for recycling gas, with means for depressurizing the catalyst section, arranged downstream of the catalyst section and with means for supplying inert gas to the catalyst section, arranged upstream from the catalyst section.
13~3~ ~3 Finally the invention relates to a reactor for the preparation of at least partly liquid hydrocarbonaceous product in a conversion reactor, by catalytic reaction of carbon monoxide with hydrogen at elevated temperature and pressure, which reactor is provided with inlet means for synthesis gas, and product outlet means, wherein inert bodies are arranged in the reactor space above the catalyst.
The shut-down process according to the invention is particularly suitable for a reactor in which synthesis gas is converted into hydrocarbons, preferably having at least 10 carbon atoms per molecule; more preferably paraffinic hydrocarbons having at least 20 carbon atoms per molecule.
Normally synthesis gas is used as the gas feed for the reactor. Synthesis gas contains as major compounds hydrogen and carbon monoxide; in addition it may contain small amounts of carbon dioxide, water, nitrogen, argon and minor amounts of compounds having 1-4 carbon atoms per molecule, such as methane, methanol and ethene.
The synthesis gas is prepared in any manner known in the art, for instance by means of steam/oxygen gasification of hydrocarbonaceous material such as brown coal, anthracite, coke, crude mineral oil and fractions thereof, and oil recovered from tar sand and bituminous shale. Alternatively, steam methane reforming and/or catalytic partial oxidation of a hydrocarbonaceous material with an oxygen-containing gas may be used to produce synthesis gas.
The process conditions in the reactor for the preparation of the at least partly liquid hydrocarbonaceous product are: a temperature from 100-500 C, a total pressure from 1-200 bar abs. and a space velocity from 200-20,000 m3 (S.T.P.) gaseous 133~
feed/m3 reaction zone/hour. Preferred process conditions include a temperature from 150-300 C, a pressure from 5-100 bar abs. and a space velocity from 500-5000 m3 (S.T.P.) gaseous feed/m3 reaction zone~hour. The expression "S.T.P." as referred to hereinbefore means Standard Temperature (0 C) and Pressure (1 bar abs.). The molar ratio of hydrogen to carbon monoxide is normally 0.4-4 and preferably from 1.8-2.5.
Suitable catalysts for the preparation of (paraffinic) hydrocarbons from the synthesis gas contain at least a metal (compound) from Group VIII of the Periodic Table of Elements, preferably a non-noble metal, in particular cobalt, optionally in combination with a noble metal for instance ruthenium, on a refractory oxide carrier such a silica, alumina or silica-alumina, preferably silica. Furthermore these catalysts preferably contain at least one other metal (compound) from Group IVb and/or VIb of the Periodic Table of Elements. This metal or compound is preferably chosen from the group consisting of zirconium, titanium and chromium. The catalysts contain preferably from 3-60 parts by weight cobalt, optionally 0.05-0.5 parts by weight of ruthenium, and from 0.1-100 parts by weight of other metal(s), especially zirconium, per 100 parts by weight of carrier.
The inert bodies present in the dome-like reactor space above the catalyst bed may consist of a spherical ceramic scale filled with pressurized gas, which scale collapses when the pressure in the reactor drops below the operation pressure.
If hydrogen is used as inert gas, a supply of hydrogen may be automatically formed during the normal operation of the reactor. According to a first embodiment a supply of hydrogen is formed by diffusion 13330~
of hydrogen into an inert body through a semi-permeable membrane which is permeable to hydrogen and impermeable to other components of the synthesis gas. According to another embodiment of such a supply for hydrogen the inert bodies consist at least partly of a material on which hydrogen is absorbed with preference over other components of the synthesis gas mixture. A nickel-samarium alloy may be used as an absorbent metal material.
If the reactor is provided with a liquid product recycling circuit, it is preferred that the inert bodies are supported on a netting separating the dome-like reactor space from the catalyst bed.
SHUT-DOWN PROCESS FOR A FISCHER-TROPSCH
REACTOR, AND SAID REACTOR
The invention relates to a shut-down process for a reactor which is used for the preparation of an at least partly liquid hydrocarbonaceous product by reaction of carbon monoxide and hydrogen at elevated temperature and pressure using a Fischer-Tropsch catalyst, and to a reactor specifically designed for carrying out this shut-down process.
Processes for the preparation of an at least partly liquid hydrocarbonaceous product by catalytic 1~ reaction of carbon monoxide with hydrogen (synthesis gas) are well known. This reaction is highly exothermic and cooling means are used in the reactor for the removal of heat from the reaction zone. Additionally such a reactor is usually provided with means to recycle gas through the catalyst for equalizing the temperature in the catalyst bed. Preferably such a reactor is also provided with means to recycle liquid hydrocarbonaceous product through the catalyst for equalizing the temperature of the catalyst bed, and further to avoid the formation of hydrocarbonaceous deposits on the catalyst.
When such a reactor is to be shut-down the supply of carbon monoxide and hydrogen is interrupted. In the dome-like reactor space above the catalyst bed a large amount of reactant gas mixture is present, which will pass through the catalyst bed at a relatively low velocity. The reaction heat is insufficiently removed and hot spots are formed in the catalyst bed. These hot spots result in a deterioration of the performance of the catalyst.
13~300~
The invention has for its object to provide a shut-down process which does not result in a deterioration of the performance of the catalyst and includes a passivation thereof.
The invention relates to a process for the shut-down of a reactor which is used for the preparation of an at least partly liquid hydrocarbonaceous product by reaction of carbon monoxide and hydrogen at elevated temperature and pressure and using a catalyst, which reactor is provided with cooling means and with means to recycle gas through the catalyst for temperature equalizing of the catalyst, comprising the steps of:
(i) interrupting the feed of synthesis gas;
15 (ii) depressurizing the reactor downstream of the catalyst, and providing the reactor upstream of the catalyst with inert gas; and (iii) cooling the catalyst to ambient conditions.
Accordingly after the interruption of the supply of carbon monoxide and hydrogen (primary synthesis gas as well as recycled synthesis gas), a gas stream through the catalyst bed is maintained at a sufficient velocity to prevent the formation of hot spots, which gas stream becomes more and more inert by the increasing proportion of inert gas. The supply of inert gas is maintained until the catalyst is cooled down to ambient conditions. Then the catalyst can be unloaded.
When the reactor is provided with means to recycle liquid product through the catalyst, the process comprises further between step (ii) and step (iii) the step (iia) of cooling the catalyst to a temperature slightly above the solidification temperature of the liquid product; and (iib) of interrupting the recycling of the liquid product, so that initially the liquid product recycling is used for the cooling and temperature levelling and deposits of solidified hydrocarbons are avoided.
Since hydrogen is available in large amounts in the plant in which the reactor is used, hydrogen is preferably used as inert gas.
In order to reduce the amount of the reactant gas mixture in the dome-like space above the catalyst bed, it is advantageous to arrange inert packing bodies, for example spherical bodies, in the reactor space above the catalyst.
When the inert bodies contain hydrogen releasable therefrom when the pressure in the reactor falls below the working pressure, hydrogen is automatically released in the reactor space above the catalyst when during the shut-down operation the supply of carbon monoxide and hydrogen is interrupted.
Hydrogen for use during the shut-down process is accumulated in or on the inert bodies during the normal operation of the reactor, when according to a first embodiment the inert bodies comprise an interfacial membrane permeable to hydrogen and impermeable to carbon monoxide, or according to a second embodiment the inert bodies comprise material which absorbs hydrogen under reaction conditions and desorbs hydrogen under shut-down conditions.
The invention relates further to a reactor suitable for carrying out the shut-down process, comprising a reactor housing provided with at least one catalyst section containing catalyst, which section is in communication with inlet means for synthesis gas, with product outlet means, with means for recycling gas, with means for depressurizing the catalyst section, arranged downstream of the catalyst section and with means for supplying inert gas to the catalyst section, arranged upstream from the catalyst section.
13~3~ ~3 Finally the invention relates to a reactor for the preparation of at least partly liquid hydrocarbonaceous product in a conversion reactor, by catalytic reaction of carbon monoxide with hydrogen at elevated temperature and pressure, which reactor is provided with inlet means for synthesis gas, and product outlet means, wherein inert bodies are arranged in the reactor space above the catalyst.
The shut-down process according to the invention is particularly suitable for a reactor in which synthesis gas is converted into hydrocarbons, preferably having at least 10 carbon atoms per molecule; more preferably paraffinic hydrocarbons having at least 20 carbon atoms per molecule.
Normally synthesis gas is used as the gas feed for the reactor. Synthesis gas contains as major compounds hydrogen and carbon monoxide; in addition it may contain small amounts of carbon dioxide, water, nitrogen, argon and minor amounts of compounds having 1-4 carbon atoms per molecule, such as methane, methanol and ethene.
The synthesis gas is prepared in any manner known in the art, for instance by means of steam/oxygen gasification of hydrocarbonaceous material such as brown coal, anthracite, coke, crude mineral oil and fractions thereof, and oil recovered from tar sand and bituminous shale. Alternatively, steam methane reforming and/or catalytic partial oxidation of a hydrocarbonaceous material with an oxygen-containing gas may be used to produce synthesis gas.
The process conditions in the reactor for the preparation of the at least partly liquid hydrocarbonaceous product are: a temperature from 100-500 C, a total pressure from 1-200 bar abs. and a space velocity from 200-20,000 m3 (S.T.P.) gaseous 133~
feed/m3 reaction zone/hour. Preferred process conditions include a temperature from 150-300 C, a pressure from 5-100 bar abs. and a space velocity from 500-5000 m3 (S.T.P.) gaseous feed/m3 reaction zone~hour. The expression "S.T.P." as referred to hereinbefore means Standard Temperature (0 C) and Pressure (1 bar abs.). The molar ratio of hydrogen to carbon monoxide is normally 0.4-4 and preferably from 1.8-2.5.
Suitable catalysts for the preparation of (paraffinic) hydrocarbons from the synthesis gas contain at least a metal (compound) from Group VIII of the Periodic Table of Elements, preferably a non-noble metal, in particular cobalt, optionally in combination with a noble metal for instance ruthenium, on a refractory oxide carrier such a silica, alumina or silica-alumina, preferably silica. Furthermore these catalysts preferably contain at least one other metal (compound) from Group IVb and/or VIb of the Periodic Table of Elements. This metal or compound is preferably chosen from the group consisting of zirconium, titanium and chromium. The catalysts contain preferably from 3-60 parts by weight cobalt, optionally 0.05-0.5 parts by weight of ruthenium, and from 0.1-100 parts by weight of other metal(s), especially zirconium, per 100 parts by weight of carrier.
The inert bodies present in the dome-like reactor space above the catalyst bed may consist of a spherical ceramic scale filled with pressurized gas, which scale collapses when the pressure in the reactor drops below the operation pressure.
If hydrogen is used as inert gas, a supply of hydrogen may be automatically formed during the normal operation of the reactor. According to a first embodiment a supply of hydrogen is formed by diffusion 13330~
of hydrogen into an inert body through a semi-permeable membrane which is permeable to hydrogen and impermeable to other components of the synthesis gas. According to another embodiment of such a supply for hydrogen the inert bodies consist at least partly of a material on which hydrogen is absorbed with preference over other components of the synthesis gas mixture. A nickel-samarium alloy may be used as an absorbent metal material.
If the reactor is provided with a liquid product recycling circuit, it is preferred that the inert bodies are supported on a netting separating the dome-like reactor space from the catalyst bed.
Claims (23)
1. Process for the shut-down of a reactor which is used for the preparation of an at least partly liquid hydrocarbonaceous product by reaction of carbon monoxide and hydrogen at elevated temperature and pressure and using a catalyst, which reactor is provided with cooling means and with means to recycle gas through the catalyst for equalizing the temperature of the catalyst, comprising the steps of:
(i) interrupting the feed of synthesis gas;
(ii) depressurizing the reactor downstream of the catalyst, and providing the reactor upstream of the catalyst with inert gas; and (iii) cooling the catalyst to ambient conditions.
(i) interrupting the feed of synthesis gas;
(ii) depressurizing the reactor downstream of the catalyst, and providing the reactor upstream of the catalyst with inert gas; and (iii) cooling the catalyst to ambient conditions.
2. Process as claimed in claim 1, wherein the reactor is provided with means to recycle liquid product through the catalyst, comprising between step (ii) and step (iii):
(iia) cooling the catalyst to a temperature slightly above the solidification temperature of the liquid product; and (iib) interrupting the recycling of the liquid product.
(iia) cooling the catalyst to a temperature slightly above the solidification temperature of the liquid product; and (iib) interrupting the recycling of the liquid product.
3. Process as claimed in claim 2, wherein in step (iia) the catalyst is cooled to about 160-200°C.
4. Process as claimed in claim 1, 2 or 3, wherein in step (ii) nitrogen gas is used as inert gas.
5. Process as claimed in claim 1, 2 or 3, wherein in step (ii) hydrogen is used as inert gas.
6. Process as claimed in claim 1, 2 or 3, wherein inert bodies are arranged in the reactor space above the catalyst.
7. Process as claimed in claim 6, wherein the inert bodies contain hydrogen releasable therefrom when the pressure in the reactor falls below the working pressure.
8. Process as claimed in claim 7, wherein the inert bodies comprise an interfacial membrane permeable to hydrogen and impermeable to carbon monoxide.
9. Process as claimed in claim 7, wherein the inert bodies comprise material which absorbs hydrogen under reaction conditions and desorbs it under shut-down conditions.
10. Process as claimed in claim 1, 2, 3, 7, 8 or 9, wherein inert bodies are arranged in the reactor space under the catalyst.
11. Reactor suitable for carrying out the shut-down process according to claim 1, 2, 3, 7, 8 or 9, comprising a reactor housing provided with at least one catalyst section containing catalyst, which section is in communication with inlet means for synthesis gas, with product outlet means, with means for recycling gas, with means for depressurizing the catalyst section, arranged downstream of the catalyst section and with means for supplying inert gas to the catalyst section, arranged upstream from the catalyst section.
12. Reactor as claimed in claim 11, wherein inert bodies are arranged in the reactor space above the catalyst.
13. Reactor as claimed in claim 12, wherein the inert bodies contain hydrogen releasable therefrom when the pressure in the reactor falls below the working pressure.
14. Reactor as claimed in claim 13, wherein the inert bodies comprise an interfacial membrane permeable to hydrogen and impermeable to carbon monoxide.
15. Reactor as claimed in claim 11, wherein the inert bodies comprise material which absorbs hydrogen under reaction conditions and desorbs it under shut-down conditions.
16. Reactor as claimed in claim 11, wherein inert bodies are arranged in the reactor space under the catalyst.
17. Reactor for the preparation of at least partly liquid hydrocarbonaceous product in a conversion reactor, by catalytic reaction of carbon monoxide with hydrogen at elevated temperature and pressure, which reactor is provided with inlet means for synthesis gas, and product outlet means, wherein inert bodies are arranged in the reactor space above the catalyst.
18. Reactor as claimed in claim 17, wherein the inert bodies contain hydrogen releasable therefrom when the pressure in the reactor falls below the working pressure.
19. Reactor as claimed in claim 18, wherein the inert bodies comprise an interfacial membrane permeable to hydrogen and impermeable to carbon monoxide.
20. Reactor as claimed in claim 17, 18 or 19, wherein the inert bodies comprise material which absorbs hydrogen under reaction conditions and desorbs from under shut-down conditions.
21. Reactor as claimed in claim 17, 18 or 19, wherein inert, bodies are arranged in the reactor space under the catalyst.
22. Process as claimed in claim 6, wherein the inert bodies are spherical bodies.
23. Reactor as claimed in claim 12, wherein the inert bodies are spherical bodies.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8817407A GB2223237B (en) | 1988-07-21 | 1988-07-21 | Shut-down process for a fischer-tropsch reactor, and said reactor |
| GB8817407 | 1988-07-21 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1333006C true CA1333006C (en) | 1994-11-15 |
Family
ID=10640883
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000605253A Expired - Fee Related CA1333006C (en) | 1988-07-21 | 1989-07-10 | Shut-down process for a fischer-tropsch reactor, and said reactor |
Country Status (7)
| Country | Link |
|---|---|
| AU (1) | AU616777B2 (en) |
| CA (1) | CA1333006C (en) |
| GB (1) | GB2223237B (en) |
| MY (1) | MY105129A (en) |
| NO (1) | NO892957L (en) |
| NZ (1) | NZ229992A (en) |
| ZA (1) | ZA895495B (en) |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB9014417D0 (en) * | 1990-06-28 | 1990-08-22 | Shell Int Research | A process for the preparation of hydrocarbons,a process for the shutdown of a reactor for carrying out said process and a reactor to be used therefor |
| US5286455A (en) * | 1990-06-18 | 1994-02-15 | Shell Oil Company | Process for the preparation of hydrocarbons |
| GB2246576A (en) * | 1990-06-28 | 1992-02-05 | Shell Int Research | A process for the preparation of hydrocarbons, a process for the shutdown of a reactor for carrying out said process and a reactor to be used therefor |
| ITMI20031777A1 (en) * | 2003-09-18 | 2005-03-19 | Enitecnologie Spa | PROCEDURE FOR THE MANAGEMENT OF A REACTOR SUITABLE FOR HETEROGENEOUS REACTIONS IN COMBINATIONS WITH REACTIONS WHICH ARE CARRIED OUT IN THREE-PHASE SYSTEMS |
| US20050175519A1 (en) * | 2004-02-06 | 2005-08-11 | Rogers William A.Jr. | Microchannel compression reactor |
| FR2878845B1 (en) * | 2004-12-03 | 2007-01-12 | Inst Francais Du Petrole | PROCESS FOR PROVISIONALLY INTERRUPTING A FISCHER-TROPSCH TYPE REACTION IN A THREE-PHASE BED REACTOR |
| DE102005050526A1 (en) * | 2005-10-21 | 2007-04-26 | Choren Industries Gmbh | Method for holding a Fischer-Tropsch synthesis |
| GB0725140D0 (en) * | 2007-12-24 | 2008-01-30 | Compactgtl Plc | Catalytic Reactor |
| WO2010063850A1 (en) * | 2008-12-16 | 2010-06-10 | Shell Internationale Research Maatschappij B.V. | High-speed stop in a fischer-tropsch process |
| WO2010069925A1 (en) * | 2008-12-16 | 2010-06-24 | Shell Internationale Research Maatschappij B.V. | High-speed stop in fischer-tropsch process |
| JP5615838B2 (en) * | 2008-12-16 | 2014-10-29 | シエル・インターナシヨナル・リサーチ・マートスハツペイ・ベー・ヴエー | Fast stop in the Fischer-Tropsch process |
| EP3009186A1 (en) | 2014-10-15 | 2016-04-20 | Haldor Topsøe A/S | A reactor system with means for catalyst protection during trips or shut-down |
| CN107551961B (en) * | 2017-11-03 | 2022-10-25 | 河北科技大学 | High-temperature high-pressure slurry bed reaction device |
| GB202019079D0 (en) | 2020-12-03 | 2021-01-20 | Johnson Matthey Davy Technologies Ltd | Method for shutting down a fischer-tropsch reactor |
| GB2622936A (en) | 2022-09-09 | 2024-04-03 | Johnson Matthey Davy Technologies Ltd | Method for controlling a process comprising a steam system coupled to a reactor system |
| GB202306773D0 (en) | 2023-05-09 | 2023-06-21 | Johnson Matthey Davy Technologies Ltd | Method for controlling a process comprising a steam system coupled to a fischer-tropsch reactor system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4544781A (en) * | 1985-01-09 | 1985-10-01 | Mobil Oil Corporation | Control of temperature exotherms in the conversion of methanol to gasoline hydrocarbons |
-
1988
- 1988-07-21 GB GB8817407A patent/GB2223237B/en not_active Expired - Fee Related
-
1989
- 1989-07-10 CA CA000605253A patent/CA1333006C/en not_active Expired - Fee Related
- 1989-07-19 NO NO89892957A patent/NO892957L/en unknown
- 1989-07-19 AU AU38254/89A patent/AU616777B2/en not_active Ceased
- 1989-07-19 NZ NZ229992A patent/NZ229992A/en unknown
- 1989-07-19 MY MYPI89000976A patent/MY105129A/en unknown
- 1989-07-19 ZA ZA895495A patent/ZA895495B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| NO892957L (en) | 1990-01-22 |
| MY105129A (en) | 1994-08-30 |
| ZA895495B (en) | 1990-04-25 |
| NZ229992A (en) | 1990-08-28 |
| GB2223237A (en) | 1990-04-04 |
| AU3825489A (en) | 1990-01-25 |
| AU616777B2 (en) | 1991-11-07 |
| GB2223237B (en) | 1992-09-16 |
| GB8817407D0 (en) | 1988-08-24 |
| NO892957D0 (en) | 1989-07-19 |
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