# US 2013/0158327 A1 · Hydrocarbon dehydrogenation with inert diluent > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 2013/0158327 A1 - Document ID: US20130158327A1 - Status: Published application - Kind: A1 - Application number: 13/328,931 - Filed: 2011-12-16 - Published: 2013-06-20 - Earliest claimed: 2011-12-16 - Assignees: Uop LLC - Inventors: Laura E. Leonard; Andrea G. Bozzano; Gavin P. Towler - Web page: https://patentgrep.com/patent/US20130158327A1 ## CPC - C07C 5/333: Catalytic processes - C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS ## Abstract A hydrocarbon dehydrogenation process includes providing the hydrocarbon feed to a reactor. The hydrocarbon feed includes at least one hydrocarbon selected from light paraffins, heavy paraffins, or combinations thereof. The process further includes introducing an inert diluent into the feed stream, contacting the feed stream and the inert diluent with a catalyst in the reactor, and flowing an effluent stream out of the reactor. ## Claims ### Claim 1 A process for dehydrogenation of a hydrocarbon feed, comprising: providing the hydrocarbon feed in a feed stream to an inlet of a reactor, the hydrocarbon feed comprising at least one hydrocarbon selected from light paraffins or heavy paraffins; introducing an inert diluent into the feed stream; contacting the feed stream and the inert diluent with a catalyst in the reactor under dehydrogenation reaction conditions; and removing an effluent stream from the reactor at an outlet. ### Claim 2 (depends on 1) The process of claim 1 wherein said effluent stream comprises at least one of a mono-olefin and a di-olefin. ### Claim 3 (depends on 1) The process of claim 1 wherein the reactor outlet has an absolute pressure in a range of 0 to about 350 kPa. ### Claim 4 (depends on 1) The process of claim 1, wherein the inert diluent is methane, nitrogen, helium, argon, or a combination thereof. ### Claim 5 (depends on 1) The process of claim 1, wherein the at least one hydrocarbon is the light paraffins, wherein the feed stream further comprises hydrogen, and wherein the light paraffins comprise at least one of propane, butane and pentane, the feed stream having a ratio of hydrogen to the light paraffins in a range of about 0.1:1 to about 1.0:1 on a molar basis. ### Claim 6 (depends on 5) The process of claim 5 wherein a ratio of inert diluent to light paraffin is in a range of about 0.1:1 to about 3.0:1 on a molar basis. ### Claim 7 (depends on 1) The process of claim 1, wherein the at least one hydrocarbon is the heavy paraffins, wherein the feed stream further comprises hydrogen, and wherein the heavy paraffins comprise at least one C6-C20 paraffin, the feed stream having a ratio of hydrogen to the heavy paraffins in a range of about 0.1:1 to about 10:1 on a molar basis. ### Claim 8 (depends on 1) The process of claim 1 wherein the reactor is operated at or above atmospheric pressure. ### Claim 9 (depends on 1) The process of claim 1 wherein the reactor comprises a reactor zone having at least two reactors in series, the reactor zone having a reactor zone inlet corresponding to an inlet of a first reactor in the reactor zone and a reactor zone outlet corresponding to an outlet of a last reactor in the reactor zone. ### Claim 10 (depends on 9) The process of claim 9 further comprising heating an effluent stream from one reactor before it enters the next reactor. ### Claim 11 (depends on 1) The process of claim 1 further comprising heating the feed stream. ### Claim 12 (depends on 1) The process of claim 1 wherein a yield of hydrocarbon per pass is increased compared to a yield of hydrocarbon per pass without the inert diluent. ### Claim 13 (depends on 1) The process of claim 1 further comprising separating at least one vapor phase and at least one liquid phase from the effluent stream in a separation zone. ### Claim 14 (depends on 13) The process of claim 13 further comprising separating a portion of the inert diluent from the vapor stream for recycling to the feed stream. ### Claim 15 (depends on 13) The process of claim 13 further comprising separating a portion of hydrogen from the vapor phase for recycling to the feed stream. ### Claim 16 (depends on 13) The process of claim 13 wherein the separation zone includes a first separation system and a second separation system. ### Claim 17 A process for dehydrogenating a light paraffin feed, comprising: providing the light paraffin feed to an inlet of a reactor, the light paraffin feed comprising hydrogen and at least one light paraffin of propane, butane or pentane; introducing at least one inert diluent selected from methane and nitrogen into the light paraffin feed; contacting the light paraffin feed and the inert diluent with a catalyst in the reactor under dehydrogenation reaction conditions; and removing an effluent stream from the reactor at an outlet; wherein the light paraffin feed has a ratio of hydrogen to light paraffin in a range of 0.1:1 to 1.0:1 on a molar basis and a ratio of inert diluent to light paraffin in a range of about 0.1:1 to about 3.0:1 on a molar basis. ### Claim 18 (depends on 17) The process of claim 17 wherein the reactor outlet pressure is in a range of 0 to about 175 kPa. ### Claim 19 A process for dehydrogenating a heavy paraffin feed, comprising: providing the heavy paraffin feed to an inlet of a reactor, the heavy paraffin feed comprising hydrogen and at least one C6-C20 paraffin; introducing at least one inert diluent selected from methane and nitrogen into the heavy paraffin feed; contacting the heavy paraffin feed and the inert diluent with a catalyst in the reactor under dehydrogenation reaction conditions; and removing an effluent stream from the reactor at an outlet; wherein the heavy paraffin feed has a ratio of hydrogen to heavy paraffin in a range of 0.1:1 to 10:1 on a molar basis and a ratio of inert diluent to paraffin in a range of about 0.1:1 to about 3.0:1 on a mole basis. ### Claim 20 (depends on 19) The process of claim 19 wherein the reactor outlet pressure is in a range of 0 to about 350 kPa.