# US 10,864,509 B2 · Regenerated catalyst cooling method > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 10,864,509 B2 - Document ID: US10864509B2 - Status: Granted - Kind: B2 - Application number: 16/820,425 - Filed: 2020-03-16 - Published: 2020-07-09 - Granted: 2020-12-15 - Earliest claimed: 2015-01-06 - Applicants: Qunzhu Li - Inventors: Qunzhu Li - Web page: https://patentgrep.com/patent/US10864509B2 ## CPC - B01J 38/32: Indirectly heating or cooling material within regeneration zone or prior to entry into regeneration zone - B01J 8/1836: {Heating and cooling the reactor (B01J8/42 takes precedence)} - B01J 38/30: in gaseous suspension, e.g. fluidised bed - C10G 3/60: {Controlling or regulating the processes} - C10G 11/182: {Regeneration} - F28D 7/1607: {with particular pattern of flow of the heat exchange media, e.g. change of flow direction (F28D7/1623, F28D7/1638, F28D7/1661, F28D7/1676, F28D7/1692 take precedence)} - B01J 2208/00132: Tubes - F28D 2021/0022: {for chemical reactors} - F28D 2021/0075: {for syngas or cracked gas cooling systems} - B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS - C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES - F28D: HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT (fluid heaters having heat generating means and heat transferring means F24H; furnaces F27; details of heat-exchange apparatus of general) ## Abstract The present invention provides a method of cooling a regenerated catalyst and a device thereof, which employs low-line-speed operation, wherein a range of the superficial gas velocity is 0.005-0.7 m/s, wherein at least one fluidization wind distributor is provided, wherein the main fluidization wind enters the dense bed layer of the catalyst cooler from the distributor, and the heat removal load of the catalyst cooler and/or the temperature of the cold catalyst is controlled by adjusting the fluidization wind quantity. The method and a device thereof of the present invention has an extensive application range, and can be extensively used for various fluid catalytic cracking processes, including heavy oil catalytic cracking, wax oil catalytic cracking, light hydrocarbon catalytic conversion and the like, or used for other gas-solid fluidization reaction charring processes, including residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, flexicoking and the like. ## Claims ### Claim 1 A method of cooling a regenerated catalyst, comprising providing a catalyst cooler comprising a catalyst outlet, at least one fluidization medium distributor, heat exchange tubes, a dense phase fluidized bed, and a catalyst inlet; providing hot catalyst particles, wherein the hot catalyst particles enter from the catalyst inlet, flow downwardly through the dense fluidized bed, and are cooled by pipe wall of the heat exchange tubes, and the cooled catalyst flows out from the catalyst outlet at its bottom; and feeding a fluidized medium from the at least one fluidization medium distributor at the bottom, wherein the fluidized medium flows upwardly through the dense phase fluidized bed, along with a removed gas that is entrained by the hot catalyst particles from a regenerator, and returns to the regenerator. ### Claim 2 (depends on 1) The method of claim 1, further comprising: adjusting a flow rate of the fluidized medium and/or adjusting a flow rate of the cooled catalyst leaving the catalyst cooler so as to control a heat removal load of the catalyst cooler and/or a temperature of the cooled catalyst. ### Claim 3 (depends on 1) The method of claim 1, wherein the catalyst cooler is provided inside or outside a regenerator; and the catalyst cooler is provided with one, two or more catalyst outlets, for transporting the cooled catalyst to the regenerator and/or transporting the cooled catalyst to reaction zones of one, two or more riser reactors and/or one, two or more fluidized bed reactors; wherein a superfacial gas velocity of the fluidized medium is in a range of from 0.005 m/s to 0.7 m/s. ### Claim 4 (depends on 3) The method of claim 3, wherein the superfacial gas velocity is in a range of from 0.01 m/s to 0.3 m/s. ### Claim 5 (depends on 3) The method of claim 3, wherein the superfacial gas velocity is in a range from 0.05 m/s to 0.15 m/s. ### Claim 6 (depends on 1) The method of claim 1, wherein the method is used for a fluid cracking process; wherein the regenerated catalyst that enters the catalyst cooler is a regenerated catalyst or partially regenerated catalyst with any carbon content, or is a spent catalyst, or is contact agent or coking particles with any carbon content. ### Claim 7 (depends on 6) The method of claim 6, wherein the fluid cracking process is selected from the group consisting of heavy oil catalytic cracking, wax oil catalytic cracking, and light hydrocarbon catalytic conversion. ### Claim 8 (depends on 1) The method of claim 1, wherein the method is used for a gas-solid fluidization reaction charring process; wherein the regenerated catalyst that enters the catalyst cooler is a regenerated catalyst or partially regenerated catalyst with any carbon content, or is a spent catalyst. ### Claim 9 (depends on 8) The method of claim 8, wherein the gas-solid fluidization reaction charring process is selected from the group consisting of residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, and flexicoking. ### Claim 10 (depends on 2) The method of claim 2, wherein the method is used for a fluid cracking process or a gas-solid fluidization reaction charring process; wherein the regenerated catalyst that enters the catalyst cooler is a regenerated catalyst or partially regenerated catalyst with any carbon content, or is a spent catalyst, or is contact agent or coking particles with any carbon content. ### Claim 11 (depends on 3) The method of claim 3, wherein the method is used for a fluid cracking process or a gas-solid fluidization reaction charring process; wherein the regenerated catalyst that enters the catalyst cooler is a regenerated catalyst or partially regenerated catalyst with any carbon content, or is a spent catalyst, or is contact agent or coking particles with any carbon content. ### Claim 12 (depends on 4) The method of claim 4, wherein the method is used for a fluid cracking process or a gas-solid fluidization reaction charring process; wherein the regenerated catalyst that enters the catalyst cooler is a regenerated catalyst or partially regenerated catalyst with any carbon content, or is a spent catalyst, or is contact agent or coking particles with any carbon content. ### Claim 13 (depends on 5) The method of claim 5, wherein the method is used for a fluid cracking process or a gas-solid fluidization reaction charring process; wherein the regenerated catalyst that enters the catalyst cooler is a regenerated catalyst or partially regenerated catalyst with any carbon content, or is a spent catalyst, or is contact agent or coking particles with any carbon content. ### Claim 14 (depends on 10) The method of claim 10, wherein the fluid cracking process is selected from the group consisting of heavy oil catalytic cracking, wax oil catalytic cracking, and light hydrocarbon catalytic conversion; or the gas-solid fluidization reaction charring process is selected from the group consisting of residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, and flexicoking. ### Claim 15 (depends on 11) The method of claim 11, wherein the fluid cracking process is selected from the group consisting of heavy oil catalytic cracking, wax oil catalytic cracking, and light hydrocarbon catalytic conversion; or the gas-solid fluidization reaction charring process is selected from the group consisting of residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, and flexicoking. ### Claim 16 (depends on 12) The method of claim 12, wherein the fluid cracking process is selected from the group consisting of heavy oil catalytic cracking, wax oil catalytic cracking, and light hydrocarbon catalytic conversion; or the gas-solid fluidization reaction charring process is selected from the group consisting of residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, and flexicoking. ### Claim 17 (depends on 13) The method of claim 13, wherein the fluid cracking process is selected from the group consisting of heavy oil catalytic cracking, wax oil catalytic cracking, and light hydrocarbon catalytic conversion; or the gas-solid fluidization reaction charring process is selected from the group consisting of residual oil pretreating, methanol to olefin, methanol to aromatics, fluid coking, and flexicoking.