# US 5,347,061 A · Process for producing gasoline having lower benzene content and distillation end point > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 5,347,061 A - Document ID: US5347061A - Status: Granted - Kind: A - Application number: 08/028,057 - Filed: 1993-03-08 - Granted: 1994-09-13 - Earliest claimed: 1993-03-08 - Assignees: Mobil Oil Corporation - Inventors: Mohsen N. Harandi; Hartley Owen; Paul H. Schipper - Web page: https://patentgrep.com/patent/US5347061A ## CPC - C10G 35/095: containing crystalline alumino-silicates, e.g. molecular sieves {(C10G35/065 takes precedence)} - C10G 45/64: containing crystalline alumino-silicates, e.g. molecular sieves - C10G 59/02: plural serial stages only - 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 ## Abstract A process is disclosed for upgrading reformate and/or light FCC gasoline by substantially reducing the amount of benzene in the gasoline product while simultaneously reducing the gasoline ASTM distillation End Point. The process comprises the fractionation of reformate to recover that fraction, C.sub.7 -C.sub.8 hydrocarbons, directly useful in gasoline without further conversion. A heavy bottom fraction comprising C.sub.9 + aromatic and non-aromatic hydrocarbons is recovered and a C.sub.6 fraction rich in benzene. The total C.sub.6 fraction and a portion of the C.sub.9 + fraction are converted by alkylation, transalkylation and cracking in contact with acidic metallosilicate catalyst particles to gasoline boiling range materials rich in alkylaromatics. Following debutanization or depentanization of the conversion product, the fraction containing unconverted benzene is recycled to the reformate fractionator. ## Claims ### Claim 1 A process for the production of gasoline having reduced benzene content and lower boiling end point, comprising: a) introducing reformer effluent into a fractionation system for separation and recovery of an overhead stream comprising C.sub.5 - hydrocarbons, a bottom stream comprising C.sub.9 + alkylaromatic and non-aromatic hydrocarbons, a stream comprising benzene rich C.sub.6 hydrocarbons, and a stream comprising C.sub.7 -C.sub.8 hydrocarbons; b) passing said benzene rich C.sub.6 stream and a portion of said C.sub.9 + hydrocarbon stream to a hydrocarbon cracking and alkylation reactor containing acidic shape selective metallo-silicate catalyst particles under cracking, alkylation and transalkylation conversion conditions whereby a portion of said benzene is converted to C.sub.7 + alkylaromatics and a portion of said C.sub.9 + hydrocarbons is converted to lower molecular weight hydrocarbons; c) recycling effluent from said reactor to said fractionation tower to separate and recycle unconverted benzene and unconverted C.sub.9 + hydrocarbons whereby the production of C.sub.7 -C.sub.9 alkylaromatics is maximized. ### Claim 2 (depends on 1) The process of claim 1 including the further step of separating said effluent by first passing said effluent to a debutanizer or depentanizer and recycling said debutanizer or depentanizer C.sub.5 + or C.sub.6 + bottom stream to said fractionation tower. ### Claim 3 (depends on 1) The process of claim 1 wherein said conversion conditions comprise temperature between 300.degree. C. and 500.degree. C., pressure between 100 kPA and 1400 kPa and weight hourly space velocity between 0.1 and 10. ### Claim 4 (depends on 3) The process of claim 3 wherein said conversion conditions comprise temperature between 370.degree. C. and 455.degree. C., pressure between 350 kPa and 700 kPa and weight hourly space velocity between 1 and 5. ### Claim 5 (depends on 1) The process of claim 1 wherein said catalyst comprises crystalline aluminosilicate. ### Claim 6 (depends on 5) The process of claim 5 wherein said catalyst is selected from the group consisting of ZSM-5, ZSM-11 , ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, MCM-22, MCM-36, zeolite Beta and TEA mordenite. ### Claim 7 (depends on 1) The process of claim 1 wherein said reformer effluent is separated into an overhead stream comprising C.sub.6 - hydrocarbons, a bottom stream comprising C.sub.10 + alkylaromatic and non-aromatic hydrocarbons, and a stream comprising C.sub.7 -C.sub.9 hydrocarbons, whereby a portion of said C.sub.10 + alkylaromatic and non-aromatic hydrocarbons is converted to lower molecular weight hydrocarbons. ### Claim 8 (depends on 1) The process of claim 1 including introducing into said reactor an additional feedstream comprising C.sub.5 -C.sub.6 oleflnic gasoline containing less than 3 weight percent benzene whereby said benzene is converted to C.sub.7 + aikylaromatics and olefin content of said gasoline is reduced. ### Claim 9 A process for the combined upgrading of reformate and light C.sub.5 + olefinic gasoline to provide low boiling end point gasoline having reduced benzene and olefins content, comprising: a) introducing reformer effluent into a fractionation tower for separation and recovery of an overhead stream comprising C.sub.6 - hydrocarbons, a bottom stream comprising C.sub.9 + alkylaromatic and non-aromatic hydrocarbons , a stream comprising benzene rich C.sub.6 hydrocarbons, and a stream comprising C.sub.7 -C.sub.8 hydrocarbons; b) passing said benzene rich C.sub.6 stream, a portion of said C.sub.9 + hydrocarbon stream and a feedstream comprising C.sub.5 + light olefinic gasoline to a hydrocarbon cracking and alkylation reactor containing acidic shape selective metallosilicate catalyst particles under cracking, alkylation and transalkylation conversion conditions whereby a portion of said benzene is converted to C.sub.7 + alkylaromatics, a portion of said C.sub.9 + hydrocarbons is converted to lower molecular weight hydrocarbons and olefins are lowered; c) recycling effluent from said reactor to said fractionation tower to separate and recycle unconverned benzene and unconverted C.sub.9 + hydrocarbons whereby the production of C.sub.7 -C.sub.9 alkylaromatics is maximized. ### Claim 10 (depends on 9) The process of claim 9 including the further step of separating said effluent by first passing said effluent into a debutanizer or depentanizer and recycling said debutanizer or depentanizer C.sub.5 + or C.sub.6 + bottom stream to said fractionation tower. ### Claim 11 (depends on 9) The process of claim 9 wherein said conversion conditions comprise temperature between 300.degree. C. and 500.degree. C., pressure between 100 kPA and 1400 kPa and weight hourly space velocity between 0.1 and 10. ### Claim 12 (depends on 11) The process of claim 11 wherein said conversion conditions comprise temperature between 370.degree. C. and 455.degree. C., pressure between 350 kPa and 700 kPa and weight hourly space velocity between 1 and 5. ### Claim 13 (depends on 9) The process of claim 9 wherein said catalyst comprises crystalline aluminosilicate. ### Claim 14 (depends on 13) The process of claim 13 wherein said catalyst is selected from the group consisting of ZSM-5, ZSM-11 , ZSM-12, ZSM-23, ZSM-35, ZSM-48, zeolite Beta and TEA mordenite. ### Claim 15 A process for the production of C.sub.5 + gasoline having reduced benzene content and lower boiling end point, comprising: (a) introducing a feedstream comprising C.sub.5 + gasoline boiling range olefinic hydrocarbons rich in benzene and C.sub.9 + alkylaromatic hydrocarbons into a hydrocarbon cracking and alkylation reactor containing acidic shape selective metallosilicate catalyst particles under cracking, alkylation and transalkylation conversion conditions whereby a portion of said benzene is converted to C.sub.7 + alkylaromatics and a portion of said C.sub.9 + hydrocarbons is converted to lower molecular weight hydrocarbons; (b) introducing effluent from said reactor into a fractionation system for separation and recovery of an overhead stream comprising C.sub.4 - or C.sub.5 - hydrocarbons, a bottom stream comprising C.sub.9 + alkylaromatic rich hydrocarbons, a stream comprising benzene rich C.sub.6 hydrocarbons, and a stream comprising C.sub.7 -C.sub.8 hydrocarbons; c) recycling a portion of said bottom stream and a portion of said fractionator C.sub.6 hydrocarbon stream to said reactor. ### Claim 16 (depends on 15) The process of claim 15 wherein said conversion conditions comprise temperature between 300.degree. C. and 500.degree. C., pressure between 100 kPA and 1400 kPa and weight hourly space velocity between 0.1 and 10. ### Claim 17 (depends on 16) The process of claim 16 wherein said conversion conditions comprise temperature between 370.degree. C. and 455.degree. C., pressure between 350 kPa and 700 kPa and weight hourly space velocity between 1 and 5. ### Claim 18 (depends on 15) The process of claim 15 wherein said catalyst comprises crystalline aluminosilicate. ### Claim 19 (depends on 18) The process of claim 18 wherein said catalyst is selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-22, ZSM-23, ZSM-35, ZSM-48, MCM-22, MCM-36, zeolite Beta and TEA mordenite.