GB1073727A - Method of reacting a gas and a liquid - Google Patents
Method of reacting a gas and a liquidInfo
- Publication number
- GB1073727A GB1073727A GB2913864A GB2913864A GB1073727A GB 1073727 A GB1073727 A GB 1073727A GB 2913864 A GB2913864 A GB 2913864A GB 2913864 A GB2913864 A GB 2913864A GB 1073727 A GB1073727 A GB 1073727A
- Authority
- GB
- United Kingdom
- Prior art keywords
- slurry
- catalyst
- reactor
- gaseous
- particulate solids
- 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
Links
Classifications
-
- 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
- B01J8/224—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 the particles being subject to a circulatory movement
- B01J8/228—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 the particles being subject to a circulatory movement externally, i.e. the particles leaving the vessel and subsequently re-entering it
Abstract
<FORM:1073727/C4-C5/1> A gaseous reactant and a slurry comprising a liquid reactant and a finely-divided catalyst are passed upwards through a mass of particulate solids in reactor 9, thereby expanding the mass by at least 10% in volume. A major proportion of the slurry is recycled from above the upper level 12 of the expanded mass, by internal standpipe 30 and pump 32. Effluent from the reaction is separated at 16 into a gaseous phase, containing gaseous reactant and reaction products, and a slurry phase, from which catalyst is recovered at 22, optionally regenerated, and returned to the mixer 2. Surplus reactant may also be recovered from the line 17 and returned to inlet 5. Alternatively the separator 16 may be dispensed with, gaseous and slurry phases being withdrawn from different ports at the top of reactor 9. Screen 13 prevents particulate solids leaving reactor 9, but alternatively the reactor may widen at the top to reduce the upward velocity. The particulate solids may be inert Al2O3, SiC, glass, quartz, slag or fireclay pellets of 1/32 to 1/2 inch diameter. Alternatively, they may be catalysts, identical to or different from the slurry catalyst, or ion exchange resin or zeolite adsorbent, whereby some reaction product is removed from the reactor, e.g. by a regeneration line 26, 27. In hydro-desulphurization of heavy oils the particulate solids may be a cracking catalyst (clay or silica gel) and the slurry comprises a hydrogenation catalyst (95% iron oxide, 5% chromium oxide). In partial hydrogenation of fats and oils a slurry of nickel catalyst is passed through pellets of nickel catalyst.ALSO:<PICT:1073727/C2/1> A gaseous reactant and a slurry comprising a liquid reactant and a finely divided catalyst are passed upwards through a mass of particulate solids in reactor 9, thereby expanding the mass by at least 10% in volume. A major proportion of the slurry is recycled from above the upper level 12 of the expanded mass, by internal standpipe 30 and pump 32. Effluent from the reaction is separated at 16 into a gaseous phase, containing gaseous reactant and reaction products, and a slurry phase, from which catalyst is recovered at 22, optionally regenerated, and returned to the mixer 2. Surplus reactant may also be recovered from the line 17 and returned to inlet 5. Alternatively the separator 16 may be dispensed with, gaseous and slurry phases being withdrawn from different ports at the top of reactor 9. Screen 13 prevents particulate solids leaving reactor 9, but alternatively the reactor may widen at the top to reduce the upward velocity. The particulate solids may be inert Al2O3, SiC, glass, quartz, slag or fireclay pellets of 1/32 to 1/2 inch diameter. Alternatively they may be catalysts, identical to or different from the slurry catalyst, or ion exchange resin or zeolite adsorbent, whereby some reaction produce is removed from the reactor, e.g. by a regeneration line 26, 27. Reactions mentioned are hydrogenation of aldehydes and ketones using a zinc, copper or cadmium chromite catalyst to produce alcohols; production of aniline by reacting gaseous NH3 with a slurry of cuprous oxide in chlorobenzene; chlorination of benzene to produce chlorobenzene using ferric chloride catalyst; oxidation of naphthalene or anthracene to phthalic anhydride or anthraquinone respectively, with air, using a vanadium oxide catalyst; and esterification by contacting ethanol vapour with a slurry of molten maleic anhydride and zirconium oxide catalyst.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB2913864A GB1073727A (en) | 1964-07-15 | 1964-07-15 | Method of reacting a gas and a liquid |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB2913864A GB1073727A (en) | 1964-07-15 | 1964-07-15 | Method of reacting a gas and a liquid |
Publications (1)
Publication Number | Publication Date |
---|---|
GB1073727A true GB1073727A (en) | 1967-06-28 |
Family
ID=10286768
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB2913864A Expired GB1073727A (en) | 1964-07-15 | 1964-07-15 | Method of reacting a gas and a liquid |
Country Status (1)
Country | Link |
---|---|
GB (1) | GB1073727A (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4250141A (en) | 1977-12-16 | 1981-02-10 | Gambro Dialysatoren Gmbh & Co. Kg | Column for the removal of undesired substances from a liquid mixture |
EP0402019A2 (en) * | 1989-06-07 | 1990-12-12 | Chemical Research & Licensing Company | Distillation column reactor |
CN111013501A (en) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
-
1964
- 1964-07-15 GB GB2913864A patent/GB1073727A/en not_active Expired
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4250141A (en) | 1977-12-16 | 1981-02-10 | Gambro Dialysatoren Gmbh & Co. Kg | Column for the removal of undesired substances from a liquid mixture |
EP0402019A2 (en) * | 1989-06-07 | 1990-12-12 | Chemical Research & Licensing Company | Distillation column reactor |
EP0402019A3 (en) * | 1989-06-07 | 1992-11-19 | Chemical Research & Licensing Company | Distillation column reactor |
CN111013501A (en) * | 2019-10-25 | 2020-04-17 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
CN111013501B (en) * | 2019-10-25 | 2021-09-14 | 河北美邦工程科技股份有限公司 | Slurry bed continuous hydrogenation reaction device and method |
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