http://rdf.ncbi.nlm.nih.gov/pubchem/patent/GB-638873-A
Outgoing Links
| Predicate | Object |
|---|---|
| assignee | http://rdf.ncbi.nlm.nih.gov/pubchem/patentassignee/MD5_bfef54e7e18f717965268e6f73da19af |
| classificationCPCInventive | http://rdf.ncbi.nlm.nih.gov/pubchem/patentcpc/B01J8-28 |
| classificationIPCInventive | http://rdf.ncbi.nlm.nih.gov/pubchem/patentipc/B01J8-28 |
| filingDate | 1947-06-17^^<http://www.w3.org/2001/XMLSchema#date> |
| publicationDate | 1950-06-14^^<http://www.w3.org/2001/XMLSchema#date> |
| publicationNumber | GB-638873-A |
| titleOfInvention | Improvements in the conversion of fluid reactants in the presence of subdivided solid catalyst particles |
| abstract | In a process and apparatus for conversion of fluid reactants in the presence of subdivided solid catalyst particles by supplying catalyst and reactant to the lower portion of a reaction zone, maintaining therein, by upward passage of reactant and reaction products, a fluidized dense phase bed of catalyst superimposed by a light phase region, and withdrawing reaction products from the light phase region, the contaminated catalyst passes laterally from the upper portion of the fluidized bed through a substantially vertical partition having a series of vertically spaced fixed and non-adjustable <PICT:0638873/III/1> openings into an adjacent stripping zone and downwardly therethrough in a dense fluidized state countercurrent to a stream of stripping fluid, e.g. steam, flue gas, or inert gas, lateral flow of catalyst into the stripping zone from the lower portions of the fluidized bed through the openings in the partition being precluded by maintaining a higher particle concentration in the stripping zone than in the reaction zone, and stripped catalyst is withdrawn from the lower portion of the stripping zone. For cracking gas oil to high octane gasoline, the oil is fed in at 16 in Fig. 1, and entrains catalyst from regenerator 3 at 42 and passes to dense bed, maintained at 455-525 DEG C., 0.34-1.7 atmospheres, and density 320-560 kgms. per cu.m., in reactor 1, whence catalyst is withdrawn through slotted plate 29 into first stripping zone 31, wherein the catalyst level is lower than, and density greater than, that in reactor 1, e.g. 400-632 kgms. per cu.m., and wherein the catalyst passes countercurrent to steam injected at 32. The stripped volatiles and reaction products pass from reactor 1 through cyclone separator 11. The catalyst stream flows to second stripping zone 35 countercurrent to steam injected at 37, wherein catalyst density is greater or less than that in reactor 1, e.g. 320-632 kgms. per cu.m., and whence stripped volatiles also feed into reactor 1 at 39. Finally, the catalyst passes to dense bed, maintained at 540-620 DEG C., 0.68-2 atmospheres, and density 240-480 kgms. per cu.m., in regenerator 3, wherein it is contacted, before recycling to the reactor, with oxygen-containing gas admitted at 26, waste gases being withdrawn through cyclone separator 20. Perforated distribution plates 18, 33, 38, 28, are provided in reactor 1, first stripping zone 31, second stripping zone 35 and regenerator 3 respectively, to give good contact between catalyst and gases. The cross-sectional area of the first stripping zone should be less than that of the reaction zone, but the stripping zone may extend below the bottom of the dense bed in reactor 1, and the second stripping zone may be omitted. Specification 574,064 is referred to. The Specification as open to inspection under Sect. 91 comprises also the use of a cylindrical partition to give an annular reaction zone or stripping zone. This subject-matter does not appear in the Specification as accepted. |
| isCitedBy | http://rdf.ncbi.nlm.nih.gov/pubchem/patent/DE-948054-C http://rdf.ncbi.nlm.nih.gov/pubchem/patent/GB-2116451-A |
| priorityDate | 1945-09-29^^<http://www.w3.org/2001/XMLSchema#date> |
| type | http://data.epo.org/linked-data/def/patent/Publication |
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