# US 2010/0137458 A1 · Gas to liquids plant with consecutive fischer-tropsch reactors and hydrogen make-up > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 2010/0137458 A1 - Document ID: US20100137458A1 - Status: Published application - Kind: A1 - Application number: 12/515,933 - Filed: 2007-11-23 - Published: 2010-06-03 - Earliest claimed: 2006-11-23 - Assignees: Gtl.F1 AG - Inventors: Rytter Erling - Web page: https://patentgrep.com/patent/US20100137458A1 ## CPC - C10G 2/332: {of the iron-group} - C10G 2/32: {with the use of catalysts} - C10G 2/34: {Apparatus, reactors} - C10G 2/342: {with moving solid catalysts} - 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 for converting synthesis gas to hydrocarbons, using a Fischer-Tropsch synthesis. Two F-T reactors are used in series with water removal between them and additional hydrogen added to the second reactor in an embodiment. ## Claims ### Claim at position 1 1-35. (canceled) ### Claim 36 A process for converting synthesis gas comprising hydrogen and carbon monoxide into hydrocarbons using a Fischer-Tropsch (F-T) synthesis reaction comprising: conveying a gas feed of hydrogen and carbon monoxide to a first F-T reactor; removing a hydrocarbon stream from the first F-T reactor; removing a first gaseous effluent stream from the first F-T reactor; conveying a portion of the first gas effluent stream to a second F-T reactor; adding an additional source of hydrogen to the second F-T reactor; removing a hydrocarbon stream from the second F-T reactor; and removing a second gaseous effluent stream from the second F-T reactor. ### Claim 37 (depends on 36) A process according to claim 36, further comprising separating water from the first gaseous effluent stream. ### Claim 38 (depends on 36) A process according to claim 36, further comprising separating water from the second gaseous effluent stream. ### Claim 39 (depends on 36) A process according to claim 36, further comprising adding an additional source of hydrogen to the first F-T reactor. ### Claim 40 (depends on 36) A process according to claim 36, wherein the additional source of hydrogen to the first F-T reactor is an external source. ### Claim 41 (depends on 36) A process according to claim 36, wherein the additional source of hydrogen to the second F-T reactor is an external source. ### Claim 42 (depends on 39) A process according to claim 39, wherein the additional source of hydrogen to the second F-T reactor is equal to or greater than the additional source of hydrogen to the first F-T reactor. ### Claim 43 (depends on 39) A process according claim 39, wherein each additional source of hydrogen is essentially pure hydrogen. ### Claim 44 (depends on 39) A process according to claim 39, wherein each additional source of hydrogen additionally includes inert constituents. ### Claim 45 (depends on 39) A process according to claim 39, wherein each additional source of hydrogen additionally includes CO, and a stoichiometric number (SN) and an H2/CO ratio are both greater than 2. ### Claim 46 (depends on 36) A process according to claim 36, wherein at least a portion of the additional hydrogen to the first and second F-T reactors is first produced in a steam reformer. ### Claim 47 (depends on 37) A process according to claim 37, further comprising recycling at least a portion of the dry first gaseous effluent stream after water removal to the first F-T reactor. ### Claim 48 (depends on 38) A process according to claim 38, further comprising recycling at least a portion of the second gaseous effluent stream to the first F-T reactor. ### Claim 49 (depends on 36) A process according to claim 36, wherein the first and second F-T reactors have different operating temperatures. ### Claim 50 (depends on 49) A process according to claim 49, wherein the operating temperature of the first F-T reactor is in a range of 200° to 260° C. and the operating temperature of the second F-T reactor is in a range of 190° to 250° C. ### Claim 51 (depends on 36) A process according to claim 36, wherein the partial pressure of water in the first F-T reactor is greater than a partial pressure of water in the second F-T reactor. ### Claim 52 (depends on 51) A process according to claim 51, wherein the partial pressure of water in the first reactor is below 6 bara and the partial pressure of water in the second F-T reactor is below 4 bara. ### Claim 53 (depends on 36) A process according to claim 36, wherein hydrogen conversion in both the first and second F-T reactors is ≧60%. ### Claim 54 (depends on 53) A process according to claim 53, wherein the hydrogen conversion in both F-T reactors is between 65% and 80%. ### Claim 55 (depends on 36) A process according to claim 36, wherein a total transverse cross-sectional area of the second F-T reactor is less than 50% of a total transverse cross-sectional area of the first F-T reactor. ### Claim 56 (depends on 55) A process according to claim 55, wherein a diameter of the second F-T reactor is less than 50% of a diameter of the first F-T reactor. ### Claim 57 (depends on 36) A process according to claim 36, wherein an FT loop conversion is larger than 90%. ### Claim 58 (depends on 57) A process according to claim 57, wherein the conversion is between 92% and 98%. ### Claim 59 (depends on 36) A process according to claim 36, wherein the second F-T reactor is common for at least two first F-T reactors. ### Claim 60 (depends on 36) A process according to claim 36, comprising more than two F-T reactors in series. ### Claim 61 (depends on 36) A process according to claim 36, wherein a main active catalytic component in the first and the second reactor is cobalt. ### Claim 62 (depends on 36) A process according to claim 36, wherein a synthesis gas is first produced from natural gas. ### Claim 63 (depends on 62) A process according to claim 62, wherein a synthesis gas is produced in an autothermal reformer, with or without pre-reforming of the natural gas. ### Claim 64 (depends on 63) A process according to claim 63, wherein an H2/CO ratio of the gas leaving the reformer is >1.9 and <2.0. ### Claim 65 (depends on 36) A process according to claim 36, wherein each F-T reactor is a three-phase slurry bubble column reactor. ### Claim 66 (depends on 5) A process according to claim 5, wherein an F-T reaction pressure in each F-T reactor is in the range of 10-60 bara. ### Claim 67 (depends on 66) A process according to claim 66, wherein the reaction pressure is in the range of 15 to 40 bara. ### Claim 68 (depends on 65) A process according to claim 65, wherein a superficial gas velocity in the first and second F-T reactors in the range of 5 to 60 cm/s. ### Claim 69 (depends on 68) A process according to claim 68, wherein the superficial gas velocity is in the range of 20 to 50 cm/s. ### Claim 70 (depends on 36) A process according to claim 36, wherein a product of the Fischer-Tropsch synthesis reaction is subsequently subjected to post-processing. ### Claim 71 (depends on 70) A process according to claim 70, wherein the post-processing is selected from the group consisting of de-waxing, hydro-isomerisation, hydro-cracking and combinations thereof.