GB873832A - Method of and apparatus for carrying out reactions between gases and liquids or fusible solids in fluidised beds - Google Patents
Method of and apparatus for carrying out reactions between gases and liquids or fusible solids in fluidised bedsInfo
- Publication number
- GB873832A GB873832A GB2500156A GB2500156A GB873832A GB 873832 A GB873832 A GB 873832A GB 2500156 A GB2500156 A GB 2500156A GB 2500156 A GB2500156 A GB 2500156A GB 873832 A GB873832 A GB 873832A
- Authority
- GB
- United Kingdom
- Prior art keywords
- gas
- pipe
- oil
- perforated wall
- inlet
- 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
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
-
- 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
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/245—Spouted-bed technique
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/26—Fuel gas
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/28—Propane and butane
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
873,832. Gas manufacture. GAS COUNCIL. Aug. 15, 1957 [Aug. 15, 1956], No. 25001/56. Class 55 (2). Apparatus for carrying out reactions in a fluidized bed between gases and liquid or fusible materials which are liable under the action of heat to produce deposits or cause the agglomeration of particles in the fluidized bed, comprises a reaction vessel 10, Fig. 1, having a frustoconical lower portion 11 tapering downwardly from the full width of the vessel to the outer edge of a perforated wall 12, there being a gas inlet 13 in the perforated wall, with an atomizing nozzle 15, situated at or near the opening of the inlet 13 for directing atomized liquid upwardly into the incoming gas, and a chamber 18, surrounding the inlet 13, for introducing gas through the perforated wall 12 into the reaction vessel. The apparatus may be used in a process for the gasification of hydrocarbon-containing oils, such as petroleum oil or an oil or tar obtained by the distillation of coal, as in Specification 830,960 wherein the oil is subjected to interaction with hydrogen to produce a gas containing gaseous hydrocarbons. Particulate material from the fluidized bed 21 flows through the conduit 22 and is carried upwardly by the hydrogenating gas through conduit 14 back into the bed 21. A small amount of the hydrogenating gas is supplied through a pipe 17 for atomizing the oil which enters through pipe 16. About 75 to 90% of the gas is introduced at a velocity of 25 to 30 feet per second through the inlet 13. The remainder of the gas passes through pipe 19, chamber 18, and perforated wall 12, to enter the vessel 10 at a velocity of about 6 inches per second. In a modification, Fig. 2, an annular frusto-conical portion 31 forming the lower end of vessel 30, is bounded at its base by an annular perforated wall 32. The frusto-conical portion 31 surrounds the central vertical conduit 33 through which particulate material flows from the bed 55 to be returned through a plurality of gas supply conduits 40. A perforated baffle 53 separates the upper portion 54 of the fluidized bed from the main portion 55. The hydrogenating gas passes through pipe 36 and coil 37, to be heated by the portion 54 of the fluidized bed, and passes through pipe 38 to an annular header 39 which supplies the conduits 40. A plurality of gas inlets 34 are arranged in an annulus around the conduit 33, each inlet being supplied through a conduit 40. Nozzles 35 in the inlets 34 are supplied with oil through a pipe 45, annular header 46 and pipes 47, a small amount of gas entering from pipe 38 through pipe 43 and header 44. A branch pipe 41 and annular header 42 supply the gas through the perforated wall 32. In an example Kuwait crude petroleum oil was preheated to 300‹ C. and atomized by means of part of the hydrogenating gas preheated to 350‹ C. 90% of the gas was supplied at a velocity of approximately 25 feet per second through the main inlet and the remaining 10% at a velocity of 0.35 feet per second through the perforated wall, the hydrogenating gas being preheated to 505‹ C. and the temperature range in the fluidized bed, consisting of coke particles, being 780‹ C. to 820‹ C. The gas produced has the following average percentage by volume, carbon dioxide 0.3, unsaturated hydrocarbons 0.15, hydrogen 57.45, carbon monoxide 1.15, saturated hydrocarbons 39.2, nitrogen 1.75. A single reaction vessel having a plurality of oil and gas inlets may be divided into two or more separate compartments by vertical partitions so that different oils may be treated in different compartments. When two compartments are provided oil may be treated in one compartment and the tar condensed from the gas produced may be treated in the other compartment. Or three compartments may be used, the third being supplied with particulate material containing deposited carbon which is gasified. The higher temperatures required for hydrogenation of the tar and deposited carbon may be produced by admitting air or oxygen with the hydrogenating gas.
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB2500156A GB873832A (en) | 1956-08-15 | 1956-08-15 | Method of and apparatus for carrying out reactions between gases and liquids or fusible solids in fluidised beds |
FR1187028D FR1187028A (en) | 1956-08-15 | 1957-08-16 | Process and apparatus for the reaction between gases and liquids or fusible products in fluidized beds, in particular for the gasification of oils containing hydrocarbons |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB2500156A GB873832A (en) | 1956-08-15 | 1956-08-15 | Method of and apparatus for carrying out reactions between gases and liquids or fusible solids in fluidised beds |
Publications (1)
Publication Number | Publication Date |
---|---|
GB873832A true GB873832A (en) | 1961-07-26 |
Family
ID=10220618
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB2500156A Expired GB873832A (en) | 1956-08-15 | 1956-08-15 | Method of and apparatus for carrying out reactions between gases and liquids or fusible solids in fluidised beds |
Country Status (2)
Country | Link |
---|---|
FR (1) | FR1187028A (en) |
GB (1) | GB873832A (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3484219A (en) * | 1965-08-17 | 1969-12-16 | Gas Council | Process and apparatus for performing chemical reactions |
WO2008080788A2 (en) * | 2006-12-29 | 2008-07-10 | Basell Poliolefine Italia S.R.L. | Process and apparatus for drying a polymer |
CN110249454A (en) * | 2017-01-23 | 2019-09-17 | 巴斯夫欧洲公司 | The method for manufacturing cathode material and the reactor suitable for carrying out the method |
-
1956
- 1956-08-15 GB GB2500156A patent/GB873832A/en not_active Expired
-
1957
- 1957-08-16 FR FR1187028D patent/FR1187028A/en not_active Expired
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3484219A (en) * | 1965-08-17 | 1969-12-16 | Gas Council | Process and apparatus for performing chemical reactions |
WO2008080788A2 (en) * | 2006-12-29 | 2008-07-10 | Basell Poliolefine Italia S.R.L. | Process and apparatus for drying a polymer |
WO2008080788A3 (en) * | 2006-12-29 | 2008-11-20 | Basell Poliolefine Srl | Process and apparatus for drying a polymer |
CN103483471A (en) * | 2006-12-29 | 2014-01-01 | 巴塞尔聚烯烃意大利有限责任公司 | Process and apparatus for drying a polymer |
CN103483471B (en) * | 2006-12-29 | 2022-02-11 | 巴塞尔聚烯烃意大利有限责任公司 | Method and apparatus for drying polymers |
CN110249454A (en) * | 2017-01-23 | 2019-09-17 | 巴斯夫欧洲公司 | The method for manufacturing cathode material and the reactor suitable for carrying out the method |
US11133503B2 (en) | 2017-01-23 | 2021-09-28 | Basf Corporation | Process for making cathode materials, and reactor suitable for carrying out said process |
CN110249454B (en) * | 2017-01-23 | 2023-09-29 | 巴斯夫欧洲公司 | Method for producing cathode material and reactor suitable for carrying out said method |
Also Published As
Publication number | Publication date |
---|---|
FR1187028A (en) | 1959-09-04 |
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