# US 2023/0054650 A1 · Flexible production of gasoline and jet fuel in alkylation reactor > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 2023/0054650 A1 - Document ID: US20230054650A1 - Status: Published application - Kind: A1 - Application number: 17/980,493 - Filed: 2022-11-03 - Published: 2023-02-23 - Earliest claimed: 2019-05-24 - Assignees: Lummus Technology Inc. - Applicants: Lummus Technology LLC - Inventors: Zan Liu; Jackeline Medina Bolívar; Maurice Korpelshoek; Romain Lemoine; Manoj Som - Web page: https://patentgrep.com/patent/US20230054650A1 ## CPC - B01J 19/004: {Multifunctional apparatus for automatic manufacturing of various chemical products (sequential reactions B01J19/0046)} - B01J 19/0013: {Controlling the temperature of the process} - C07C 2/62: with acids - C07C 7/005: {Processes comprising at least two steps in series} - C10G 29/205: {by reaction with hydrocarbons added to the hydrocarbon oil} - C10L 1/06: for spark ignition - B01J 2219/00051: Controlling the temperature - B01J 2219/00164: controlling the flow - C10G 2400/02: Gasoline - C10G 2400/08: Jet fuel - C10L 2200/0423: Gasoline - C10L 2200/043: Kerosene, jet fuel - C10L 2270/023: for gasoline engines - C10L 2270/04: for turbines, planes, power generation - B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS - C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS - 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 - C10L: FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS ## Abstract Systems and processes for the flexible production of gasoline and jet fuel via alkylation of C4 and C5 olefins. ## Claims ### Claim 1 A system for flexible production of gasoline and jet fuel, the system comprising: an alkylation reaction zone comprising one or more reactors for reacting C4 olefins, C5 olefins, C6 olefins, C4-C5 olefins, or C4-C6 olefins with C4-C6 isoparaffins in the presence of sulfuric acid alkylation catalyst to produce a hydrocarbon effluent and a spent acid stream; a flow line for providing C4 olefins to the alkylation reaction zone; a flow line for providing C5 olefins to the alkylation reaction zone; a flow line for providing fresh acid alkylation catalyst to the alkylation reaction zone; a deisobutanizer for separating the hydrocarbon effluent into an isobutane fraction, a n-butane fraction, and a C5+ fraction; a deisopentanizer for separating the C5+ fraction into an isopentane fraction and a C6+ fraction; a splitter for separating the C6+ fraction into a light alkylate overhead fraction and a heavy alkylate bottoms fraction; a flow system for recycling the isobutane fraction to the alkylation reaction zone, recovering the isobutane fraction as an isobutane product, and both recycling a portion of the isobutane fraction to the alkylation reaction zone and recovering a portion of the isobutane fraction as an isobutane product; a flow system for recycling the isopentane fraction to the alkylation reaction zone, recovering the isopentane fraction as an isopentane product, and both recycling a portion of the isopentane fraction to the alkylation reaction zone and recovering a portion of the isopentane fraction as an isopentane product; a flow system for recycling the light alkylate fraction to the alkylation reaction zone, recovering the light alkylate as a light alkylate product, and both recycling a portion of the light alkylate fraction to the alkylation reaction zone and recovering a portion of the light alkylate fraction as a light alkylate product. ### Claim 2 (depends on 1) The system of claim 1, further comprising a flow line for providing C6 olefins to the alkylation reaction zone. ### Claim 3 (depends on 1) The system of claim 1, further comprising a control system configured to adjust a flow rate of each of the C4 olefins, C5 olefins, the recycle isobutane fraction, the isopentane recycle fraction, and the light alkylate recycle fraction to the alkylation reaction zone to selectively increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone. ### Claim 4 (depends on 3) The system of claim 3, wherein the control system is further configured to adjust a reaction temperature of the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone. ### Claim 5 (depends on 3) The system of claim 3, wherein the control system is further configured to adjust a flow rate of fresh acid catalyst to the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone. ### Claim 6 (depends on 3) The system of claim 3, wherein the control system is further configured to adjust operating conditions in the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone, wherein the operating conditions are selected from one or more of acid strength, temperature, space velocity, mixing intensity, recycle isobutane to olefin ratio and recycle isopentane to olefin ratio. ### Claim 7 (depends on 3) The system of claim 3, further comprising a flow line for recovering the C5+ fraction as a gasoline product fraction. ### Claim 8 A system for flexible production of gasoline and jet fuel, the system comprising: an alkylation reaction zone comprising one or more reactors for reacting C4 olefins, C5 olefins, C6 olefins, C4-C5 olefins, or C4-C6 olefins with isoparaffins in the presence of sulfuric acid alkylation catalyst to produce a hydrocarbon effluent and a spent acid stream; a flow line for providing C4 olefins to the alkylation reaction zone; a flow line for providing C5 olefins to the alkylation reaction zone; a flow line for providing fresh acid alkylation catalyst to the alkylation reaction zone; a deisobutanizer for separating the hydrocarbon effluent into an isobutane fraction, a n-butane fraction, and a C5+ fraction; a deisopentanizer for separating the C5+ fraction into an isopentane fraction and a C6+ fraction; a splitter for separating the C6+ fraction into a light alkylate overhead fraction and a heavy alkylate bottoms fraction; a flow system for recycling the isobutane fraction to the alkylation reaction zone, recovering the isobutane fraction as an isobutane product, and both recycling a portion of the isobutane fraction to the alkylation reaction zone and recovering a portion of the isobutane fraction as an isobutane product; a flow system for recycling the isopentane fraction to the alkylation reaction zone, recovering the isopentane fraction as an isopentane product, and both recycling a portion of the isopentane fraction to the alkylation reaction zone and recovering a portion of the isopentane fraction as an isopentane product; and a control system configured to adjust a flow rate of each of the C4 olefins, C5 olefins, the recycle isobutane fraction, and the isopentane recycle fraction to the alkylation reaction zone to selectively increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone. ### Claim 9 (depends on 8) The system of claim 8, further comprising a flow line for providing C6 olefins to the alkylation reaction zone. ### Claim 10 (depends on 8) The system of claim 8, wherein the control system is further configured to adjust a reaction temperature of the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone. ### Claim 11 (depends on 8) The system of claim 8, wherein the control system is further configured to adjust a flow rate of fresh acid catalyst to the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone. ### Claim 12 (depends on 8) The system of claim 8, wherein the control system is further configured to adjust operating conditions in the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone, wherein the operating conditions are selected from one or more of acid strength, temperature, space velocity, mixing intensity, recycle isobutane to olefin ratio and recycle isopentane to olefin ratio. ### Claim 13 (depends on 8) The system of claim 8, further comprising a flow system for recycling the light alkylate fraction to the alkylation reaction zone, recovering the light alkylate as a light alkylate product, and both recycling a portion of the light alkylate fraction to the alkylation reaction zone and recovering a portion of the light alkylate fraction as a light alkylate product. ### Claim 14 (depends on 13) The system of claim 13, wherein the control system is further configured to adjust a flow rate of the light alkylate recycle fraction to the one or more reactors in the alkylation reaction zone to increase or decrease a ratio of gasoline to jet fuel range hydrocarbons produced in the alkylation reaction zone ### Claim 15 (depends on 8) The system of claim 8, further comprising a flow line for recovering the C5+ fraction as a gasoline product fraction. ### Claim 16 (depends on 15) The system of claim 15, wherein the control system is further configured to shut down and start up the depentanizer and the splitter when maximizing the gasoline product fraction or minimizing the gasoline product fraction, respectively. ### Claim 17 (canceled) ### Claim 18 (canceled) ### Claim 19 (canceled) ### Claim 20 (canceled) ### Claim 21 (canceled) ### Claim 22 (canceled) ### Claim 23 A system for flexible production of gasoline and jet fuel, including operating the process in a gasoline production mode, a jet fuel production mode, and a co-production mode, the system comprising: an alkylation reaction zone comprising: a C4 alkylation reactor for reacting isobutane and butenes in the presence of sulfuric acid alkylation catalyst to produce a first alkylation effluent and a spent acid stream; a C5 alkylation reactor for reacting isopentane and pentenes in the presence of sulfuric acid alkylation catalyst to produce a second alkylation effluent and a second spent acid stream; a flow line for providing the isobutane and the butenes to the C4 alkylation reactor; a flow line for providing the isopentane and the pentenes to the C5 alkylation reactor; a flow line for providing fresh acid alkylation catalyst to the alkylation reaction zone; a debutanizer for separating the first hydrocarbon effluent and the second hydrocarbon effluent into an isobutane fraction, a n-butane fraction, and a C5+ fraction; a depentanizer for separating the C5+ fraction into an isopentane fraction and a C6+ fraction; an alkylate splitter for separating the C6+ fraction into a light alkylate overhead fraction and a heavy alkylate bottoms fraction; a flow system for recycling the isobutane fraction to both of the C4 alkylation reactor and the C5 alkylation reactor when operating in the gasoline production mode, and recovering the isobutane fraction when operating the jet fuel production mode, and feeding the isobutane fraction to the C4 alkylation reactor when operating in the co-production mode; a flow system for bypassing the depentanizer and the splitter when operating in the gasoline production mode, and feeding the isopentane fraction to both of the C4 and C5 alkylation reactors when operating the jet fuel production mode, and feeding the isopentane fraction to the C5 alkylation reactor when operating in the co-production mode; and a control system configured to adjust a flow rate of the isobutane and the butenes to the C4 alkylation reactor to the C4 alkylation reactor, a flow rate of the isopentane and the pentenes to the C5 alkylation reactor, a flow rate of the C4 recycled isobutane fraction to the C4 alkylation reactor, a flow rate of the C5 recycled isobutane fraction to the C5 alkylation reactor, and a flow rate of the recycled isopentane fraction to the C5 alkylation reactor to selectively operate in the gasoline production mode, the jet fuel production mode, or a co-production mode. ### Claim 24 (depends on 23) The system of claim 23, wherein the control system is further configured to maintain the sulfuric acid alkylation catalyst in the C4 alkylation reactor at a concentration range titrating as 87 to 95 wt % sulfuric acid/water mixtures, and maintain the sulfuric acid alkylation catalyst in the C5 alkylation reactor at a concentration range titrating as 80 to 95 wt % sulfuric acid/water mixtures. ### Claim 25 (depends on 23) The system of claim 23, wherein the control system is further configured to operate the C4 and C5 alkylation reactors at a lower temperature during jet fuel mode than during gasoline production mode; and operating the C4 and C5 alkylation reactors at a lower acid strength during jet fuel mode than during gasoline production mode. ### Claim 26 (depends on 23) The system of claim 23, wherein the control system is further configured to shut down and start up the depentanizer and the splitter when operating in the gasoline production mode or operating in the jet fuel production mode, respectively.