# US 5,334,792 A · Combined paraffin isomerization/ring opening process for c5+naphtha > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 5,334,792 A - Document ID: US5334792A - Status: Granted - Kind: A - Application number: 07/958,826 - Filed: 1992-10-09 - Granted: 1994-08-02 - Earliest claimed: 1992-10-09 - Assignees: Mobil Oil Corporation - Inventors: Kenneth J. Del Rossi; David J. Dovedytis; David J. Esteves; Mohsen N. Harandi; Albin Huss, Jr. - Web page: https://patentgrep.com/patent/US5334792A ## CPC - C10G 59/02: plural serial stages only - Y10S 585/94: Opening of hydrocarbon ring - 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 - Y10S: TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS ## Abstract There is provided a process for ring opening of aromatics and cycloaliphatics, as well as isomerization of aliphatics. The feedstream to this process comprises hydrocarbons having 6 carbon atoms. The process involves the use of at least two reactors connected in series. The first reactor contains a zeolite catalyst and is operated under conditions which particularly promote ring opening. The catalyst in this first reactor may comprise zeolite Beta and platinum. A downstream reactor is operated under conditions to promote isomerization of aliphatics. The catalyst in the second reactor may comprise alumina, platinum and a chloride component. ## Claims ### Claim 1 A process for ring opening and isomerization of C.sub.5 + naphtha hydrocarbons, said process comprising the steps of: (a) passing C.sub.5 + naphtha hydrocarbons comprising at least 10 wt. % C.sub.6 cyclic hydrocarbons to a fractionation zone; (b) withdrawing a sidecut comprising C.sub.6 hydrocarbons and a majority of said C.sub.6 cyclic hydrocarbons entering said fractionation zone; (c) charging said sidecut along with hydrogen to a first reaction zone, wherein said hydrocarbons and hydrogen are contacted with a catalyst comprising a zeolite and a hydrogenation component at a temperature and pressure sufficient to saturate benzene and open cyclic hydrocarbons contained in said hydrocarbons; (d) withdrawing an overhead from said fractionation zone comprising C.sub.5 hydrocarbons and a minority of said C.sub.6 cyclic hydrocarbons entering said fractionation zone; and (e) mixing said overhead with hydrocarbon product from said first reaction zone and charging to a second reaction zone, wherein hydrocarbons are contacted with an isomerization catalyst at a temperature and pressure sufficient to isomerize paraffins, and wherein said second reaction zone temperature is lower than said first reaction zone temperature. ### Claim 2 (depends on 1) A process according to claim 1, wherein said zeolite is an aluminosilicate zeolite having a Constraint Index of 12 or less. ### Claim 3 (depends on 1) A process according to claim 1, wherein said zeolite is Zeolite Beta. ### Claim 4 (depends on 1) A process according to claim 1, wherein the reaction conditions in the first reaction zone include a temperature of at least 150.degree. C., a pressure of from 50 to 1500 psig and a weight hourly space velocity of from 0.1 to 50 hr.sup.-1. ### Claim 5 (depends on 4) A process according to claim 4, wherein the reaction conditions in the second reaction zone include a temperature of from about 40.degree. to 180.degree. C., a pressure of from 50 to 1500 psig and a weight hourly space velocity of from 0.1 to 50 hr.sup.-1. ### Claim 6 (depends on 1) A process according to claim 1, wherein at least 10 wt. % of the cyclic hydrocarbon rings charged into said first reaction zone are opened in step (a). ### Claim 7 (depends on 1) A process according to claim 1, wherein the catalyst in the second reaction zone comprises alumina, from 0.1 to 1.0. wt. % platinum, and from 2 to 20 wt. % of a chloride component. ### Claim 8 (depends on 7) A process according to claim 7, wherein a chloride concentration of from 30 to 300 ppm is maintained in said second reaction zone. ### Claim 9 A process for ring opening and isomerization of hydrocarbons, said process comprising the steps of: (a) passing hydrocarbons comprising C.sub.6 cyclic hydrocarbons to a fractionation zone; (b) withdrawing a sidecut comprising C.sub.6 hydrocarbons and a majority of said C.sub.6 cyclic hydrocarbons entering said fractionation zone; (c) charging said sidecut along with hydrogen to a first reaction zone, wherein said hydrocarbons and hydrogen are contacted with a catalyst comprising a zeolite and a hydrogenation component at a temperature and pressure sufficient to saturate benzene and open cyclic hydrocarbons contained in said hydrocarbons; (d) withdrawing an overhead from said fractionation zone comprising C.sub.5 hydrocarbons and a minority of said C.sub.6 cyclic hydrocarbons entering said fractionation zone; (e) mixing said overhead with hydrocarbon product from said first reaction zone and charging to a second reaction zone, wherein hydrocarbons are contacted with an isomerization catalyst at a temperature and pressure sufficient to isomerize paraffins, and wherein said second reaction zone temperature is lower than said first reaction zone temperature; (f) removing hydrogen from effluent of said second reaction zone and recycling to said first reaction zone; and (g) recovering a third stream from said fractionation zone comprising C.sub.7 hydrocarbons. ### Claim 10 (depends on 9) A process according to claim 9, wherein said zeolite is an aluminosilicate zeolite having a Constraint Index of 12 or less. ### Claim 11 (depends on 10) A process according to claim 10, wherein said zeolite has an intersecting pore system. ### Claim 12 (depends on 9) A process according to claim 9, wherein said zeolite is Zeolite Beta. ### Claim 13 (depends on 9) A process according to claim 9, wherein said catalyst in the first reaction zone and the catalyst in the second reaction zone each comprise platinum. ### Claim 14 (depends on 9) A process according to claim 9, wherein C.sub.5 hydrocarbons are cofed into the reaction zone of step (c) . ### Claim 15 (depends on 9) A process according to claim 9, wherein at least 25 wt. % of the cyclic hydrocarbon rings charged into said first reaction zone are opened in step (c). ### Claim 16 (depends on 9) A process according to claim 9, wherein the catalyst in the second reaction zone comprises alumina, from 0.1 to 1.0. wt. % platinum, and from 2 to 20 wt. % of a chloride component. ### Claim 17 (depends on 16) A process according to claim 16, wherein a chloride concentration of from 30 to 300 ppm is maintained in said second reaction zone. ### Claim 18 A process for ring opening and isomerization of hydrocarbons, said process comprising the steps of: (a) passing hydrocarbons comprising C.sub.6 cyclic hydrocarbons to a fractionation zone; (b) withdrawing a sidecut comprising C.sub.6 hydrocarbons and a majority of said C.sub.6 cyclic hydrocarbons entering said fractionation zone; (c) charging said sidecut along with hydrogen to a first reaction zone, wherein said hydrocarbons and hydrogen are contacted with a catalyst comprising a zeolite and a hydrogenation component at a temperature and pressure sufficient to saturate benzene and open cyclic hydrocarbons contained in said hydrocarbons; (d) withdrawing an overhead from said fractionation zone comprising C.sub.5 hydrocarbons and a minority of said C.sub.6 cyclic hydrocarbons entering said fractionation zone; (e) mixing said overhead with hydrocarbon product from said first reaction zone and charging to a second reaction zone, wherein hydrocarbons are contacted with an isomerization catalyst at a temperature and pressure sufficient to isomerize paraffins, and wherein said second reaction zone temperature is less than about 230.degree. C.; (f) recovering an effluent from said second reaction zone comprising unconverted C.sub.5 + hydrocarbons in a product separation zone and recycling to said second reaction zone; (g) removing hydrogen from effluent of said second reaction zone and recycling to said first reaction zone; and (h) recovering a third stream from said fractionation zone comprising C.sub.7 hydrocarbons. ### Claim 19 (depends on 18) A process according to claim 18, wherein said zeolite has a Constraint Index of 12 or less. ### Claim 20 (depends on 18) A process according to claim 18, wherein said zeolite is Zeolite Y or Zeolite Beta. ### Claim 21 (depends on 18) A process according to claim 18, wherein said zeolite is Zeolite Beta. ### Claim 22 (depends on 18) A process according to claim 18, wherein the catalyst in the second reaction zone comprises alumina, from 0.1 to 1.0. wt. % platinum, and from 2 to 20 wt. % of a chloride component. ### Claim 23 (depends on 22) A process according to claim 22, wherein a chloride concentration of from 30 to 300 ppm is maintained in said second reaction zone. ### Claim 24 (depends on 18) A process according to claim 18, wherein at least 50 wt. % of the cyclic hydrocarbon rings charged into said first reaction zone are opened in step (c). ### Claim 25 (depends on 1) A process according to claim 1, wherein feed to said first reaction zone is reduced by about 50 vol. % in comparison to feed to said fractionation zone.