CA2130661C - Method of conducting catalytic converter multi-phase reaction - Google Patents
Method of conducting catalytic converter multi-phase reaction Download PDFInfo
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- CA2130661C CA2130661C CA002130661A CA2130661A CA2130661C CA 2130661 C CA2130661 C CA 2130661C CA 002130661 A CA002130661 A CA 002130661A CA 2130661 A CA2130661 A CA 2130661A CA 2130661 C CA2130661 C CA 2130661C
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- slurry
- filtrate
- filter member
- pressure differential
- catalyst
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Links
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 title abstract description 14
- 230000003197 catalytic effect Effects 0.000 title description 5
- 239000002002 slurry Substances 0.000 claims abstract description 55
- 239000000706 filtrate Substances 0.000 claims abstract description 31
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 239000000047 product Substances 0.000 claims abstract description 22
- 239000000376 reactant Substances 0.000 claims abstract description 15
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 13
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 13
- 238000004891 communication Methods 0.000 claims abstract description 7
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 6
- 239000012263 liquid product Substances 0.000 claims abstract description 6
- 238000013019 agitation Methods 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 19
- 230000010355 oscillation Effects 0.000 claims description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 6
- 230000033001 locomotion Effects 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 3
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 9
- 239000000446 fuel Substances 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 24
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 14
- 239000002245 particle Substances 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 230000015572 biosynthetic process Effects 0.000 description 7
- 238000002474 experimental method Methods 0.000 description 7
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 239000011148 porous material Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000002407 reforming Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 235000019198 oils Nutrition 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 244000068988 Glycine max Species 0.000 description 1
- 235000010469 Glycine max Nutrition 0.000 description 1
- 244000020551 Helianthus annuus Species 0.000 description 1
- 235000003222 Helianthus annuus Nutrition 0.000 description 1
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000011437 continuous method Methods 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000010685 fatty oil Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000013529 heat transfer fluid Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 230000002706 hydrostatic effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229940057995 liquid paraffin Drugs 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000003264 margarine Substances 0.000 description 1
- 235000013310 margarine Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 150000002828 nitro derivatives Chemical class 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 235000019809 paraffin wax Nutrition 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 235000019271 petrolatum Nutrition 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- -1 shortening Substances 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/11—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements
- B01D29/114—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements arranged for inward flow filtration
- B01D29/115—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor with bag, cage, hose, tube, sleeve or like filtering elements arranged for inward flow filtration open-ended, the arrival of the mixture to be filtered and the discharge of the concentrated mixture are situated on both opposite sides of the filtering element
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/60—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration
- B01D29/605—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor integrally combined with devices for controlling the filtration by level measuring
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D29/00—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor
- B01D29/88—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices
- B01D29/92—Filters with filtering elements stationary during filtration, e.g. pressure or suction filters, not covered by groups B01D24/00 - B01D27/00; Filtering elements therefor having feed or discharge devices for discharging filtrate
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/006—Separating solid material from the gas/liquid stream by filtration
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
-
- 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
- C07C1/06—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen in the presence of organic compounds, e.g. hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- 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
- C10G2/342—Apparatus, reactors with moving solid catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
- B01D36/001—Filters in combination with devices for the removal of gas, air purge systems
-
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A method of conducting a continuous multi-phase catalytic reaction such as the conversion of syngas to higher hydrocarbon fuels. Gaseous reactants are introduced via a gas permeable plate (15) into a slurry (16) which includes the product and a finely divided catalyst. The liquid product is separated from the remainder of the slurry by means of a filter unit (13) including a filter member (22). A
pressure differential is established across the filter member (22) by means of a constant level device (23) within the filter unit which maintains a level of filtrate (32) within the filter unit (22) below the level of the slurry (16). The slurry (16) is maintained in a constant state of agitation by the introduction of the gaseous components as a steam of bubbles. Fluctuations in the pressure differential across the filter member (22) prevent the filter member from clogging, and the gas space (28, 29) is above the filtrate (32) and the slurry (16) are in communication.
pressure differential is established across the filter member (22) by means of a constant level device (23) within the filter unit which maintains a level of filtrate (32) within the filter unit (22) below the level of the slurry (16). The slurry (16) is maintained in a constant state of agitation by the introduction of the gaseous components as a steam of bubbles. Fluctuations in the pressure differential across the filter member (22) prevent the filter member from clogging, and the gas space (28, 29) is above the filtrate (32) and the slurry (16) are in communication.
Description
..,WO 93/.16796 PCT/N093/00031 2130~f ~.
METHOD OF CONDOGTING CATALYTIC CONVERTER
MDLTI-PHABE REACTION
The present invention relates to a method of conducting a continuous multi-phase catalytic reaction and is particularly, though not exclusively, applicable to the catalytic conversion of syngas, produced by the reforming of methane, to hydrocarbon fuels, by a Fischer-Tropsh type of synthesis. Other reaction systems to which the method is applicable include various slurry reactions for~the production of petrochemicals, the production of oxygenates from synthesis gas and dehydrogenation reactions.
Three-phase catalytic reaction systems are used in a number of chemical processes and their application in the petrochemical industry appears to be increasing. Of the three-phase systems in use, mechanically agitated, loop and bubble column slurry reactors contain small catalyst particles dispersed in the liquid. In most.
applications, the liquid will have to be separated from the slurry to remove liquid products or for . catalyst regeneration purposes. In those cases where the liquid is an inert medium, occasionally, it may have to be replaced due to degradation or the build-up of impurities.
Mechanically agitated'slurry reactors are particularly convenient for batch process due to the low mass-transfer and heat resistance. These features also make them suitable for the determination of reaction kinetics in the laboratory. A serious disadvantage and limitation of this reactor type, ., ., 213oss1 however, is the difficulty in the separation of catalyst particles in any continuous operation.
Commercially, it is only mechanically agitated reactors that are used in the hydrogenation of double bonds in oils from cottonseed, soybean, corn, sunflower etc. By employing a nickel catalyst, the products include margarine, shortening, soap and greases. The choice of reactor is based on the low diffusivities and high viscosities of the fatty oils. Fixed-bed operation has been proposed due to the advantage of completely catalyst-free products without filtration.
A number of other hydrogenation reactions are also ' carried out in~ agitated reactors, e.g. the hydrogenation of nitrocompounds.
Tie operation of bubble column slurry reactors is simple, since mechanically moving parts are avoided.
Combined with the low diffusional resistance and efficient heat transfer, these reactors are attractive for many industrial processes. However, solid-liquid separation is usually performed outside the reactor in elaborate filtering and settling systems. The catalyst slurry ~is to be recycled to the reactor, sometimes with the use of a slurry pump. Thus, serious problems may be encountered in the continuous operation of bubble column slurry reactors.
As world oil resources diminish it is becoming more attractive to use natural gas as an energy source and methods of upgrading this to higher hydrocarbon fuels are increasing in importance.
It is therefore an object of the invention to provide a continuous method of conducting a multi-phase catalytic reaction which does not suffer the drawbacks of the prior art.
It is a particular obj ect of the invention to provide such a process which is well suited to use in the conversion of natural gas via syngas to diesel fuel.
According to the invention, there is provided a method of conducting a continuous multi-phase catalytic reaction in which the product includes at least one liquid component and the catalyst is a finely divided solid, the method comprising:
introducing reactants into a slurry of reactants, product and catalyst in a reactor vessel; separating the liquid product from the remainder of the slurry by means of a filter member;
establishing a mean pressure differential of from 1 to 1000mBar across the filter member; causing fluctuations or oscillations about the mean pressure differential; and maintaining the slurry in state of constant agitation by introducing gaseous components into the slurry as a stream or swarm of bubbles.
Such a method is relatively simple yet effective. The separation step, generally considered to be particularly problematic, is achieved without undue complication and under proper operating conditions the filter member is self-cleaning.
The reactants may be CO and H2, for example from the reforming of methane. The reaction may then be a catalytic conversion by a Fisher-Tropsch synthesis, producing methanol and higher hydrocarbons.
Preferably, the gaseous components include any gaseous reactants. Preferably, the slurry is maintained in a turbulent state by the gas bubbles.
Preferably, a pressure differential is achieved by applying an excess pressure to the slurry side of the filter member and/or by applying a negative pressure to WO 93/16796 ~~ PCT/N093/04031 the product (filtrate) side of the filter member.
Preferably, the pressure differential is achieved, at least in part by maintaining the slurry at a level above the level of the product on the filtrate side of the filter member, by means of a constant level device on the filtrate side of the filter member. The pressure differential should not be allowed to increase beyond a fairly low maximum limit since the filter unit would otherwise tend to clog. Preferably, communication between the space above the slurry and .the space above the filtrate prevents the build-up of pressure differentials in excess of that corresponding to the hydrostatic pressure.
The pressure fluctuations or oscillations may be . achieved in various ways. The pressure fluctuations or oscillations may be carried out by the turbulent motion of the slurry in the reactor and/or by gas bubbles rising on the outside of the member, which may themselves give rise to turbulent flow conditions.
This may be transferred or enhanced perhaps by resonance effects to the filtrate, preferably by way of communication between the gas volume above and the slurry anal the gas volume above the filtrate.
Alternatively, the pressure fluctuation may be achieved by applying a pulsating pressure to the gas volume above the filtrate.
The pressure fluctuation value may be of the order of the pressure differential, for example from 10 to 200% of the pressure differential. The actual value of the pressure differential may be from 1 to 1000mBar, preferably 2 to 50m8ar. Very good operational results may be obtained in the range of 2 to lOmBar in the case of a Fischer-Tropsch conversion of syngas to .,. S.. 44~: <,tF..
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' S 7.T . R'~ V ... .. ;1 ...r~, ,;,' .,. .1 ..... 4 e. . . . . ~ , ,'f- . ., ~ . . . .. ,.... S°"...
~1~i3~~~2...,...0r,...~...~.tW..i~~.uN.s_5~.4~~4~W~._._G~~SIJ.l ..\ ..
1.~...M\.,....~~5,.~...~~L~..l. .. .W.,..,.v...., 4...'i.. t.:1'k;v.kiu... , :.: ~1.,.W ' . . .l'.:., . . . ,... ...
21.3oss1 ,.;:i;,. . ,.
hydrocarbon products.
The filter member is preferably in the form of a filter unit which defines internally the filtrate zone and which includes a filter element separating the filtrate from the slurry. Preferably the filter element is generally cylindrical and its axis is generally vertical in use though~it may be inclined by as much as 10° or even 30° to the vertical. The member material and, catalyst are preferably selected so that the maximum hole or pore size in the filter element is .of the same order of magnitude as the catalyst particle.size, the particle size preferably being not ' less than half the pore size. However, it would be possible for the catalyst particle size ~to be larger than the maximum pore size, with the pore size being of the same magnitude or less.
The invention also extends to a method of converting natural gas (methane) to higher hydrocarbon fuels'which involves initially reforming the methane to produce carbon monoxide~and hydrogen, subjecting the.
CO and H2 to catalytic~conversion by a Fischer-Tropsch synthesis using the method mentioned above to form higher hydrocarbon fuels such as liquid paraffin waxes, and subsequently separating and/or cracking these products to produce the~required range of hydrocarbons.
The mechanism of the Fischer-Tropsch synthesis is probably quite complicated but the formation of hydrocarbons can be summarised as follows:-nC0 + (2n+1) H2 - CnH2n+2 + nH2O
. A preferred catalyst and process is described in WO 93/16796 ~ ~ ' ' . PCT/N093/00031 EP-A-313375.
When diesel fuel is produced in this way it is vastly superior to conventional diesel in terms of its quality and properties. Firstly, it contains no sulphur or aromatics, which is important from an environmental point of view. Secondly, it has a very high cetane number and can therefore be blended with lower grades of diesel fractions in order to give a product which meets premium range standards.. Thirdly, it contains virtually no harmful compounds that .generate soot when burned and needs fewer additives for problem free use at low temperatures.
~ ~ The invention may be carried into practice in various ways and some embodiments will now be described by way.aof example with reference to the accompanying drawings, in which: .
Figure 1 is a schematic section through a three-phase slurry reactor for performing a method in accordance with the invention:
Figure 2 is a simplified schematic section through a part of a reactor showing an alternative system for achieving the fluctuations in pressure:.
.Figures 3 , 4 and 5 are views similar to Figure 2 showing three ways of adjusting the pressure differential across the filter member.
Figures 6 and 7 are views similar to Figures 3 to 5, showing two further variants.
The reactor vessel 11 in Figure 1 comprises an outer casing 12 defining the reactor vessel 11 and within the casing 12 a filter unit 13. The housing 12 has a gas inlet 14 at the bottom which, in the case of a syngas conversion process, would constitute the reactant inlet. Above the gas inlet 14, there is a gas delivery device such as a gas-permeable frit plate 15 which supports the slurry 16 in the reactor vessel lI, and at the top of the casing 12, a gas outlet 17. The gas outlet 17 is controlled by a~ choke or valve 18.
The casing also has an inlet 19 and an outlet 21 for the slurry.
The filter unit 13 comprises a generally vertical cylindrical filter element 22 in contact with the slurry 16. The filter element is in the form of a fine meshed screen though it could alternatively comprise helically wound metal threads, sintered metal particles or narrowly separated fine vertical threads. It houses a constant level device in the form of a vertical pipe 23 which terminates below the top of the filter unit 13. The pipe 23 leads to a filtrate outlet 24 which in turn leads to a collector 25 and to an outlet valve 26.
A tube 27 extends from the space 28 within the filter unit 13 above the top of the pipe 23 to the space 29 within the top of the reactor 11 above the slurry 16.
An opening 31 in the tube 27 connects the two spaces 28,29.
In operation, gaseous reactants are introduced to the reactor vessel 11 via the inlet 14 and the plate 15. The reactants form bubbles in the slurry 16 which pass upwards past the filter unit 13. The slurry 16 consists of a liquid phase of the reaction products and a catalyst in finely divided form. The gaseous reactants react as they contact the catalyst, thus adding to the products in the slurry.
At the same time, the products pass through the filter element 22 to form a product filtrate 32 which is free of catalyst. Any gaseous products and unreacted reactants can be vented through the outlet 17 WO 93/16796 ':'~ ~ PCI'/N093/00031 21.30661 and subsequently treated and/or recycled. The product filtrate 32 leaves the filter unit 13 via the constant level device 23 and outlet 24 and is collected in the collector 25 for regulated continuous or periodic removal.
The difference in level between the slurry 16 and the product filtrate 32, determined by the constant level device, results in a pressure differential across the filter element 22. This helps to convey the liquid product through the filter element 22.
. It might be expected that, under these conditions, the catalyst would clog the filter element, however, ~ this is found not to be the case,- provided that the pressure differential ~is not too great. The introduction of the reactants together with the connection of the gas spaces 28, 29, and the generally turbulent conditions in the reactor vessel 11 combine to cause fluctuations in the pressure differential across the filter element 22. These in turn cause fluctuations in the liquid flow through the filter element 22 resulting in an anti-clogging effect. This may be enhanced by the movement of the gas bubbles past the surface of the filter element 22.
An alternative embodiment is shown in Figure 2.
In this case the filter unit 41 has no tube 27 connecting the space 28 to the space 29 in the reactor . (not shown,. Instead, a cylinder. and piston assembly 421 is connected to the space 28. By reciprocating the piston, a pulsating pressure is produced resulting~in the desired fluctuation in the pressure differential across the filter element 22. This arrangement can of course be used in conjunction with the embodiment shown in Figure 1. Communication between the spaces above WO 93/16796 . 213066. ~ p~/N093/00031 the slurry and the filtrate may be provided by a tube (not shown] having a restriction or choke limiting the ' transmission of pressure pulses to the space above the slurry, which would otherwise have tended to eliminate the net effect of the reciprocating piston. The tube would nevertheless control the static pressure differential., The constant level device 23 can be made adjustable in order to provide a degree of control over the pressure differential across the filter element 22.
Three ways in which this can be achieved are shown in Figures 3, 4 and 5.
~ In the filter unit 51 of Figure 3, both the vertical pipe 52 and the tube.53 are slidably mounted with respect to the filter unit 51: In the filter unit 61 of Figure 4, the vertical pipe 62 is slidably mounted but the tube 63 is fixed relative to the filter unit 61. In the filter unit of Figure 5, the tube 73 is fixed, and the vertical pipe 72 is slidably mounted within a fixed sleeve 74. .Thus, the level of the filtrate 32 remains fixed relative to the filter unit 71 as it is raised or lowered. .
The variants shown in Figures 3 to 5 can be combined with either of the embodiments shown in Figures 1 and 2.
In the reactor 81 shown in Figure 6, the outlet 84 from the filter unit 83 has an upward loop 85 to ensure that the filter unit 83 is filled with liquid. In the reactor 91 shown in Figure ?, there is a tube 97 connecting the gas space in the reactor to the filtrate. The outlet 94 extends to the bottom of the filter unit 93 and there is an optional connection 96 between the outlet 94 and the space in the reactor.
WO 93/16796 NCT/'.V093/00031 This connection 96 would tend to prevent any siphon effect and allow any gas remaining in the filtrate to escape. Again, the filter unit 93 will be filled with filtrate.
In all the illustrate embodiments, the geometries of the reactor, the communication means (eg. the tube 27) and the filtrate section may be varied in size and in order to optimise the pressure fluctuations by exploiting resonance-like effects.
The invention will now be further illustrated in .the following Examples which were conducted on a laboratory scale.
~ ,EXAMPLE T
A stainless steel tube, with a diameter of 4.8cm and a height of approximately 2 meters was filled with a hydrocarbon liquid and a fine powdered catalyst. The tube was operated as a slurry bubble column by bubbling gas through the slurry.
A filter unit was placed in the upper part of the reactor. The filter unit was _ made of S.ika stainless .steel sintered metal cylinder Type R20 produced by the company Pressmetall Krebsoge GmbH. The filter unit had an outer diameter of 2.5cm, a height of 25cm, and an average pore sire of 20 Vim.
In this particular experiment, the reactor was filled with a slurry consisting of a poly o~-olefin liquid and approximately 10 weight % of a fine powdered cobalt on alumina catalyst. The particle size ranged from 30 to 150 hum. The catalyst was kept suspended by gas bubbling through the liquid. The gas was a mixture of H2, CO arid N2 of varying composition, and was fed with a superficial gas~velocity of 4cm/s. The temperature in the reactor was 230°C, and the pressure WO 93/ 16796 2i30f si PCT/N093/00031 v . ~:~ , was 30 bar (3x106Pa).
The filtrate level inside the slurry was set approximately half way up in the valve.
The liquid formed by the Fischer-Tropsch reaction ~ in the reactor was withdrawn through the filter unit.
In addition, a poly 4~-olefin liquid fed to the reactor was also withdrawn through the filter unit. The liquid withdrawal varied from 320 to 2.5 g/h depending on the formation rate of the liquid product, and the feeding rate of the hydrocarbon liquid. The experiment lasted approximately 400, hours, and a total amount of liquid of 30 litres was withdrawn through the filter unit.
The liquid level in the reactor was constant during the experiment, and no colour indicating presence of solid particles could be observed in the liquid.
EXAMPLE II
A glass tube, with a diameter of 22cm and a height of 2.5 meters was filled with hydrocarbon liquid (Monsanto heat transfer fluid, MCS 2313), and a fine alumina powder (average particle diameter approximately 75~m). The content of alumina was approximately 15% by weight. The tube was operated as a slurry bubble column (SBC) by bubbling gas through the slurry.
A filter member without a connection tube between the gas volume above the slurry phase and the gas volume above the product phase was placed in the upper part of the SBC. The filter member was made of a Sika fil 10 stainless steel sintered metal cylinder produced by Sintermetallwerk Krebsoge GmbH. The sinter cylinder had an outer diameter of 2.5cm, a height of 20cm, and an average pore size of l0~um.
In this particular experiment the slurry level was set to be at the top of the sinter cylinder. The WO 93/16796 . , ;, .Z ~ ; PCT/N093/00031 pressure amplitude in the SBC was measured to be 6mBar, the pressure drop across the sinter metal wall was approximately 3-4 mBar (300-400Pa). The temperature in the slurry was 200C, the pressure was 1 Bar (105Pa) and the gas velocity was approximately 6cm/s.
At the start of the experiment, the flow of the filtrate through the sinter metal cylinder was about 1000m1 per minute. After 4 hours the flow was reduced to zero due to clogging of the sinter metal wall on the slurry side.
. When a similar experiment was carried out in an apparatus in which communication between the. gas volumes was provided by a piece of pipe acting as a connection tube, the initial flow rate .was maintained essentially a.t the same level throughout the experiment.
METHOD OF CONDOGTING CATALYTIC CONVERTER
MDLTI-PHABE REACTION
The present invention relates to a method of conducting a continuous multi-phase catalytic reaction and is particularly, though not exclusively, applicable to the catalytic conversion of syngas, produced by the reforming of methane, to hydrocarbon fuels, by a Fischer-Tropsh type of synthesis. Other reaction systems to which the method is applicable include various slurry reactions for~the production of petrochemicals, the production of oxygenates from synthesis gas and dehydrogenation reactions.
Three-phase catalytic reaction systems are used in a number of chemical processes and their application in the petrochemical industry appears to be increasing. Of the three-phase systems in use, mechanically agitated, loop and bubble column slurry reactors contain small catalyst particles dispersed in the liquid. In most.
applications, the liquid will have to be separated from the slurry to remove liquid products or for . catalyst regeneration purposes. In those cases where the liquid is an inert medium, occasionally, it may have to be replaced due to degradation or the build-up of impurities.
Mechanically agitated'slurry reactors are particularly convenient for batch process due to the low mass-transfer and heat resistance. These features also make them suitable for the determination of reaction kinetics in the laboratory. A serious disadvantage and limitation of this reactor type, ., ., 213oss1 however, is the difficulty in the separation of catalyst particles in any continuous operation.
Commercially, it is only mechanically agitated reactors that are used in the hydrogenation of double bonds in oils from cottonseed, soybean, corn, sunflower etc. By employing a nickel catalyst, the products include margarine, shortening, soap and greases. The choice of reactor is based on the low diffusivities and high viscosities of the fatty oils. Fixed-bed operation has been proposed due to the advantage of completely catalyst-free products without filtration.
A number of other hydrogenation reactions are also ' carried out in~ agitated reactors, e.g. the hydrogenation of nitrocompounds.
Tie operation of bubble column slurry reactors is simple, since mechanically moving parts are avoided.
Combined with the low diffusional resistance and efficient heat transfer, these reactors are attractive for many industrial processes. However, solid-liquid separation is usually performed outside the reactor in elaborate filtering and settling systems. The catalyst slurry ~is to be recycled to the reactor, sometimes with the use of a slurry pump. Thus, serious problems may be encountered in the continuous operation of bubble column slurry reactors.
As world oil resources diminish it is becoming more attractive to use natural gas as an energy source and methods of upgrading this to higher hydrocarbon fuels are increasing in importance.
It is therefore an object of the invention to provide a continuous method of conducting a multi-phase catalytic reaction which does not suffer the drawbacks of the prior art.
It is a particular obj ect of the invention to provide such a process which is well suited to use in the conversion of natural gas via syngas to diesel fuel.
According to the invention, there is provided a method of conducting a continuous multi-phase catalytic reaction in which the product includes at least one liquid component and the catalyst is a finely divided solid, the method comprising:
introducing reactants into a slurry of reactants, product and catalyst in a reactor vessel; separating the liquid product from the remainder of the slurry by means of a filter member;
establishing a mean pressure differential of from 1 to 1000mBar across the filter member; causing fluctuations or oscillations about the mean pressure differential; and maintaining the slurry in state of constant agitation by introducing gaseous components into the slurry as a stream or swarm of bubbles.
Such a method is relatively simple yet effective. The separation step, generally considered to be particularly problematic, is achieved without undue complication and under proper operating conditions the filter member is self-cleaning.
The reactants may be CO and H2, for example from the reforming of methane. The reaction may then be a catalytic conversion by a Fisher-Tropsch synthesis, producing methanol and higher hydrocarbons.
Preferably, the gaseous components include any gaseous reactants. Preferably, the slurry is maintained in a turbulent state by the gas bubbles.
Preferably, a pressure differential is achieved by applying an excess pressure to the slurry side of the filter member and/or by applying a negative pressure to WO 93/16796 ~~ PCT/N093/04031 the product (filtrate) side of the filter member.
Preferably, the pressure differential is achieved, at least in part by maintaining the slurry at a level above the level of the product on the filtrate side of the filter member, by means of a constant level device on the filtrate side of the filter member. The pressure differential should not be allowed to increase beyond a fairly low maximum limit since the filter unit would otherwise tend to clog. Preferably, communication between the space above the slurry and .the space above the filtrate prevents the build-up of pressure differentials in excess of that corresponding to the hydrostatic pressure.
The pressure fluctuations or oscillations may be . achieved in various ways. The pressure fluctuations or oscillations may be carried out by the turbulent motion of the slurry in the reactor and/or by gas bubbles rising on the outside of the member, which may themselves give rise to turbulent flow conditions.
This may be transferred or enhanced perhaps by resonance effects to the filtrate, preferably by way of communication between the gas volume above and the slurry anal the gas volume above the filtrate.
Alternatively, the pressure fluctuation may be achieved by applying a pulsating pressure to the gas volume above the filtrate.
The pressure fluctuation value may be of the order of the pressure differential, for example from 10 to 200% of the pressure differential. The actual value of the pressure differential may be from 1 to 1000mBar, preferably 2 to 50m8ar. Very good operational results may be obtained in the range of 2 to lOmBar in the case of a Fischer-Tropsch conversion of syngas to .,. S.. 44~: <,tF..
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hydrocarbon products.
The filter member is preferably in the form of a filter unit which defines internally the filtrate zone and which includes a filter element separating the filtrate from the slurry. Preferably the filter element is generally cylindrical and its axis is generally vertical in use though~it may be inclined by as much as 10° or even 30° to the vertical. The member material and, catalyst are preferably selected so that the maximum hole or pore size in the filter element is .of the same order of magnitude as the catalyst particle.size, the particle size preferably being not ' less than half the pore size. However, it would be possible for the catalyst particle size ~to be larger than the maximum pore size, with the pore size being of the same magnitude or less.
The invention also extends to a method of converting natural gas (methane) to higher hydrocarbon fuels'which involves initially reforming the methane to produce carbon monoxide~and hydrogen, subjecting the.
CO and H2 to catalytic~conversion by a Fischer-Tropsch synthesis using the method mentioned above to form higher hydrocarbon fuels such as liquid paraffin waxes, and subsequently separating and/or cracking these products to produce the~required range of hydrocarbons.
The mechanism of the Fischer-Tropsch synthesis is probably quite complicated but the formation of hydrocarbons can be summarised as follows:-nC0 + (2n+1) H2 - CnH2n+2 + nH2O
. A preferred catalyst and process is described in WO 93/16796 ~ ~ ' ' . PCT/N093/00031 EP-A-313375.
When diesel fuel is produced in this way it is vastly superior to conventional diesel in terms of its quality and properties. Firstly, it contains no sulphur or aromatics, which is important from an environmental point of view. Secondly, it has a very high cetane number and can therefore be blended with lower grades of diesel fractions in order to give a product which meets premium range standards.. Thirdly, it contains virtually no harmful compounds that .generate soot when burned and needs fewer additives for problem free use at low temperatures.
~ ~ The invention may be carried into practice in various ways and some embodiments will now be described by way.aof example with reference to the accompanying drawings, in which: .
Figure 1 is a schematic section through a three-phase slurry reactor for performing a method in accordance with the invention:
Figure 2 is a simplified schematic section through a part of a reactor showing an alternative system for achieving the fluctuations in pressure:.
.Figures 3 , 4 and 5 are views similar to Figure 2 showing three ways of adjusting the pressure differential across the filter member.
Figures 6 and 7 are views similar to Figures 3 to 5, showing two further variants.
The reactor vessel 11 in Figure 1 comprises an outer casing 12 defining the reactor vessel 11 and within the casing 12 a filter unit 13. The housing 12 has a gas inlet 14 at the bottom which, in the case of a syngas conversion process, would constitute the reactant inlet. Above the gas inlet 14, there is a gas delivery device such as a gas-permeable frit plate 15 which supports the slurry 16 in the reactor vessel lI, and at the top of the casing 12, a gas outlet 17. The gas outlet 17 is controlled by a~ choke or valve 18.
The casing also has an inlet 19 and an outlet 21 for the slurry.
The filter unit 13 comprises a generally vertical cylindrical filter element 22 in contact with the slurry 16. The filter element is in the form of a fine meshed screen though it could alternatively comprise helically wound metal threads, sintered metal particles or narrowly separated fine vertical threads. It houses a constant level device in the form of a vertical pipe 23 which terminates below the top of the filter unit 13. The pipe 23 leads to a filtrate outlet 24 which in turn leads to a collector 25 and to an outlet valve 26.
A tube 27 extends from the space 28 within the filter unit 13 above the top of the pipe 23 to the space 29 within the top of the reactor 11 above the slurry 16.
An opening 31 in the tube 27 connects the two spaces 28,29.
In operation, gaseous reactants are introduced to the reactor vessel 11 via the inlet 14 and the plate 15. The reactants form bubbles in the slurry 16 which pass upwards past the filter unit 13. The slurry 16 consists of a liquid phase of the reaction products and a catalyst in finely divided form. The gaseous reactants react as they contact the catalyst, thus adding to the products in the slurry.
At the same time, the products pass through the filter element 22 to form a product filtrate 32 which is free of catalyst. Any gaseous products and unreacted reactants can be vented through the outlet 17 WO 93/16796 ':'~ ~ PCI'/N093/00031 21.30661 and subsequently treated and/or recycled. The product filtrate 32 leaves the filter unit 13 via the constant level device 23 and outlet 24 and is collected in the collector 25 for regulated continuous or periodic removal.
The difference in level between the slurry 16 and the product filtrate 32, determined by the constant level device, results in a pressure differential across the filter element 22. This helps to convey the liquid product through the filter element 22.
. It might be expected that, under these conditions, the catalyst would clog the filter element, however, ~ this is found not to be the case,- provided that the pressure differential ~is not too great. The introduction of the reactants together with the connection of the gas spaces 28, 29, and the generally turbulent conditions in the reactor vessel 11 combine to cause fluctuations in the pressure differential across the filter element 22. These in turn cause fluctuations in the liquid flow through the filter element 22 resulting in an anti-clogging effect. This may be enhanced by the movement of the gas bubbles past the surface of the filter element 22.
An alternative embodiment is shown in Figure 2.
In this case the filter unit 41 has no tube 27 connecting the space 28 to the space 29 in the reactor . (not shown,. Instead, a cylinder. and piston assembly 421 is connected to the space 28. By reciprocating the piston, a pulsating pressure is produced resulting~in the desired fluctuation in the pressure differential across the filter element 22. This arrangement can of course be used in conjunction with the embodiment shown in Figure 1. Communication between the spaces above WO 93/16796 . 213066. ~ p~/N093/00031 the slurry and the filtrate may be provided by a tube (not shown] having a restriction or choke limiting the ' transmission of pressure pulses to the space above the slurry, which would otherwise have tended to eliminate the net effect of the reciprocating piston. The tube would nevertheless control the static pressure differential., The constant level device 23 can be made adjustable in order to provide a degree of control over the pressure differential across the filter element 22.
Three ways in which this can be achieved are shown in Figures 3, 4 and 5.
~ In the filter unit 51 of Figure 3, both the vertical pipe 52 and the tube.53 are slidably mounted with respect to the filter unit 51: In the filter unit 61 of Figure 4, the vertical pipe 62 is slidably mounted but the tube 63 is fixed relative to the filter unit 61. In the filter unit of Figure 5, the tube 73 is fixed, and the vertical pipe 72 is slidably mounted within a fixed sleeve 74. .Thus, the level of the filtrate 32 remains fixed relative to the filter unit 71 as it is raised or lowered. .
The variants shown in Figures 3 to 5 can be combined with either of the embodiments shown in Figures 1 and 2.
In the reactor 81 shown in Figure 6, the outlet 84 from the filter unit 83 has an upward loop 85 to ensure that the filter unit 83 is filled with liquid. In the reactor 91 shown in Figure ?, there is a tube 97 connecting the gas space in the reactor to the filtrate. The outlet 94 extends to the bottom of the filter unit 93 and there is an optional connection 96 between the outlet 94 and the space in the reactor.
WO 93/16796 NCT/'.V093/00031 This connection 96 would tend to prevent any siphon effect and allow any gas remaining in the filtrate to escape. Again, the filter unit 93 will be filled with filtrate.
In all the illustrate embodiments, the geometries of the reactor, the communication means (eg. the tube 27) and the filtrate section may be varied in size and in order to optimise the pressure fluctuations by exploiting resonance-like effects.
The invention will now be further illustrated in .the following Examples which were conducted on a laboratory scale.
~ ,EXAMPLE T
A stainless steel tube, with a diameter of 4.8cm and a height of approximately 2 meters was filled with a hydrocarbon liquid and a fine powdered catalyst. The tube was operated as a slurry bubble column by bubbling gas through the slurry.
A filter unit was placed in the upper part of the reactor. The filter unit was _ made of S.ika stainless .steel sintered metal cylinder Type R20 produced by the company Pressmetall Krebsoge GmbH. The filter unit had an outer diameter of 2.5cm, a height of 25cm, and an average pore sire of 20 Vim.
In this particular experiment, the reactor was filled with a slurry consisting of a poly o~-olefin liquid and approximately 10 weight % of a fine powdered cobalt on alumina catalyst. The particle size ranged from 30 to 150 hum. The catalyst was kept suspended by gas bubbling through the liquid. The gas was a mixture of H2, CO arid N2 of varying composition, and was fed with a superficial gas~velocity of 4cm/s. The temperature in the reactor was 230°C, and the pressure WO 93/ 16796 2i30f si PCT/N093/00031 v . ~:~ , was 30 bar (3x106Pa).
The filtrate level inside the slurry was set approximately half way up in the valve.
The liquid formed by the Fischer-Tropsch reaction ~ in the reactor was withdrawn through the filter unit.
In addition, a poly 4~-olefin liquid fed to the reactor was also withdrawn through the filter unit. The liquid withdrawal varied from 320 to 2.5 g/h depending on the formation rate of the liquid product, and the feeding rate of the hydrocarbon liquid. The experiment lasted approximately 400, hours, and a total amount of liquid of 30 litres was withdrawn through the filter unit.
The liquid level in the reactor was constant during the experiment, and no colour indicating presence of solid particles could be observed in the liquid.
EXAMPLE II
A glass tube, with a diameter of 22cm and a height of 2.5 meters was filled with hydrocarbon liquid (Monsanto heat transfer fluid, MCS 2313), and a fine alumina powder (average particle diameter approximately 75~m). The content of alumina was approximately 15% by weight. The tube was operated as a slurry bubble column (SBC) by bubbling gas through the slurry.
A filter member without a connection tube between the gas volume above the slurry phase and the gas volume above the product phase was placed in the upper part of the SBC. The filter member was made of a Sika fil 10 stainless steel sintered metal cylinder produced by Sintermetallwerk Krebsoge GmbH. The sinter cylinder had an outer diameter of 2.5cm, a height of 20cm, and an average pore size of l0~um.
In this particular experiment the slurry level was set to be at the top of the sinter cylinder. The WO 93/16796 . , ;, .Z ~ ; PCT/N093/00031 pressure amplitude in the SBC was measured to be 6mBar, the pressure drop across the sinter metal wall was approximately 3-4 mBar (300-400Pa). The temperature in the slurry was 200C, the pressure was 1 Bar (105Pa) and the gas velocity was approximately 6cm/s.
At the start of the experiment, the flow of the filtrate through the sinter metal cylinder was about 1000m1 per minute. After 4 hours the flow was reduced to zero due to clogging of the sinter metal wall on the slurry side.
. When a similar experiment was carried out in an apparatus in which communication between the. gas volumes was provided by a piece of pipe acting as a connection tube, the initial flow rate .was maintained essentially a.t the same level throughout the experiment.
Claims (11)
1. A method of conducting a continuous multi-phase catalytic reaction in which the product includes at least one liquid component and the catalyst is a finely divided solid, the method comprising: introducing reactants into a slurry (16) of reactants, product and catalyst in a reactor vessel (11);
separating the liquid product (32) as a filtrate from the remainder of the slurry (16) by means of a filter member (13);
establishing a mean pressure differential of from 1 to 1000mBar across the filter member (13); causing fluctuations or oscillations about the mean pressure differential; and maintaining the slurry (16) in state of constant agitation by introducing gaseous components into the slurry (16) as a stream of bubbles.
separating the liquid product (32) as a filtrate from the remainder of the slurry (16) by means of a filter member (13);
establishing a mean pressure differential of from 1 to 1000mBar across the filter member (13); causing fluctuations or oscillations about the mean pressure differential; and maintaining the slurry (16) in state of constant agitation by introducing gaseous components into the slurry (16) as a stream of bubbles.
2. A method as claimed in Claim 1, in which the gaseous components include gaseous reactants.
3. A method as claimed in Claim 1 or Claim 2, in which the slurry (16) is maintained in a turbulent state by the gas bubbles.
4. A method as claimed in any one of Claims 1 to 3, in which the pressure differential is achieved by maintaining the slurry (16) at a level above the level of the product (32) on the filtrate side of the filter member (13).
5. A method as claimed in any one of Claims 1 to 3, in which the pressure differential is achieved by maintaining the slurry (16) at a level above the level of the product (32) on the filtrate side of the filter member (13) by means of a constant level device on the filtrate side of the filter member (13).
6. A method as claimed in any one of Claims 1 to 5, in which the slurry has turbulent motion and the fluctuations or oscillations are caused by the turbulent motion of the slurry (16).
7. A method as claimed in any one of Claim 1 to 5, in which there is a gas volume (28) above the filtrate and the fluctuations or oscillations are achieved by applying a pulsating pressure to the gas volume (28) above the filtrate (32).
8. A method as claimed in any one of Claims 1 to 7, in which a gas space (29) above the slurry (16) is in communication with the filtrate (32) or any gas volume (28) above the filtrate (32).
9. A method as claimed in any one of Claims 1 to 8, in which the mean differential pressure is less than 50mBar.
10. A method as claimed in any one of Claims 1 to 9, in which the fluctuations or oscillations are in the range of from 10% to 200% of the mean pressure differential.
11. A method as claimed in any one of Claims 1 to 10, in which the reactants are CO and H2, the catalyst is a Fisher-Tropsch catalyst and the products are methanol and higher hydrocarbons.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
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GB929203959A GB9203959D0 (en) | 1992-02-25 | 1992-02-25 | Method of conducting catalytic converter multi-phase reaction |
GB9203959.3 | 1992-02-25 | ||
PCT/NO1993/000031 WO1993016796A1 (en) | 1992-02-25 | 1993-02-24 | Method of conducting catalytic converter multi-phase reaction |
Publications (2)
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CA2130661A1 CA2130661A1 (en) | 1993-08-26 |
CA2130661C true CA2130661C (en) | 2005-04-26 |
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CA002130661A Expired - Lifetime CA2130661C (en) | 1992-02-25 | 1993-02-24 | Method of conducting catalytic converter multi-phase reaction |
Country Status (15)
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US (1) | US5422375A (en) |
EP (1) | EP0627959B2 (en) |
CN (1) | CN1056322C (en) |
AT (1) | ATE151663T1 (en) |
AU (1) | AU664430B2 (en) |
CA (1) | CA2130661C (en) |
DE (1) | DE69309911T3 (en) |
DK (1) | DK0627959T4 (en) |
DZ (1) | DZ1664A1 (en) |
GB (1) | GB9203959D0 (en) |
MX (1) | MX9301054A (en) |
MY (1) | MY108982A (en) |
NO (1) | NO300120B1 (en) |
RU (1) | RU2108146C1 (en) |
WO (1) | WO1993016796A1 (en) |
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CA2038773C (en) * | 1990-04-04 | 1999-06-08 | Kym B. Arcuri | Slurry fischer-tropsch process with co/ti02 catalyst |
-
1992
- 1992-02-25 GB GB929203959A patent/GB9203959D0/en active Pending
-
1993
- 1993-02-24 DZ DZ930017A patent/DZ1664A1/en active
- 1993-02-24 DE DE69309911T patent/DE69309911T3/en not_active Expired - Lifetime
- 1993-02-24 WO PCT/NO1993/000031 patent/WO1993016796A1/en active IP Right Grant
- 1993-02-24 EP EP93905653A patent/EP0627959B2/en not_active Expired - Lifetime
- 1993-02-24 CN CN93103457A patent/CN1056322C/en not_active Expired - Lifetime
- 1993-02-24 AT AT93905653T patent/ATE151663T1/en not_active IP Right Cessation
- 1993-02-24 RU RU94040360A patent/RU2108146C1/en active
- 1993-02-24 AU AU36496/93A patent/AU664430B2/en not_active Expired
- 1993-02-24 DK DK93905653T patent/DK0627959T4/en active
- 1993-02-24 CA CA002130661A patent/CA2130661C/en not_active Expired - Lifetime
- 1993-02-24 US US08/021,783 patent/US5422375A/en not_active Expired - Lifetime
- 1993-02-24 MY MYPI93000334A patent/MY108982A/en unknown
- 1993-02-25 MX MX9301054A patent/MX9301054A/en unknown
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1994
- 1994-08-24 NO NO943122A patent/NO300120B1/en not_active IP Right Cessation
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DE69309911T3 (en) | 2001-08-02 |
MX9301054A (en) | 1994-01-31 |
AU664430B2 (en) | 1995-11-16 |
NO300120B1 (en) | 1997-04-14 |
EP0627959B2 (en) | 2000-12-20 |
DE69309911D1 (en) | 1997-05-22 |
EP0627959B1 (en) | 1997-04-16 |
RU2108146C1 (en) | 1998-04-10 |
DZ1664A1 (en) | 2002-02-17 |
WO1993016796A1 (en) | 1993-09-02 |
DK0627959T3 (en) | 1997-05-26 |
NO943122D0 (en) | 1994-08-24 |
CN1078486A (en) | 1993-11-17 |
GB9203959D0 (en) | 1992-04-08 |
DK0627959T4 (en) | 2001-01-08 |
AU3649693A (en) | 1993-09-13 |
EP0627959A1 (en) | 1994-12-14 |
US5422375A (en) | 1995-06-06 |
MY108982A (en) | 1996-11-30 |
RU94040360A (en) | 1996-07-27 |
CN1056322C (en) | 2000-09-13 |
NO943122L (en) | 1994-08-24 |
ATE151663T1 (en) | 1997-05-15 |
DE69309911T2 (en) | 1997-07-24 |
CA2130661A1 (en) | 1993-08-26 |
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