# US 10,245,547 B2 · Sulfur removal system > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 10,245,547 B2 - Document ID: US10245547B2 - Status: Granted - Kind: B2 - Application number: 15/485,776 - Filed: 2017-04-12 - Published: 2018-10-18 - Granted: 2019-04-02 - Earliest claimed: 2017-04-12 - Assignees: King Fahd University of Petroleum and Minerals - Applicants: King Fahd University of Petroleum and Minerals - Inventors: Tawfik Abdo Saleh Awadh; Saddam Ahmed Al-Hammadi - Web page: https://patentgrep.com/patent/US10245547B2 ## CPC - B01D 53/0423: {Beds in columns} - B01D 53/02: by adsorption, e.g. preparative gas chromatography {(solid sorbent compositions B01J20/00, preparation of inorganic compounds or elements C01)} - B01D 53/08: according to the "moving bed" method - B01D 53/12: according to the "fluidised technique" - B01J 20/0225: {Compounds of Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt} - B01J 20/0237: {Compounds of Cu} - B01J 20/20: comprising free carbon; comprising carbon obtained by carbonising processes - C10G 25/003: {Specific sorbent material, not covered by C10G25/02 or C10G25/03} - C10G 25/09: according to the "fluidised bed" technique - B01D 2253/102: Carbon - B01D 2253/112: Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106 - B01D 2253/25: Coated, impregnated or composite adsorbents - B01D 2256/24: Hydrocarbons - B01D 2257/306: Organic sulfur compounds, e.g. mercaptans - B01D 2259/40083: Regeneration of adsorbents in processes other than pressure or temperature swing adsorption - B01D 2259/402: using two beds - C10G 2300/202: Heteroatoms content, i.e. S, N, O, P - B01D: SEPARATION (separating solids from solids by wet methods B03B, B03D; by pneumatic jigs or tables B03B; by other dry methods B07; magnetic or electrostatic separation of solid materials from solid materials or fluids, separation by high-voltage electric fields B03C; centrifuges, vortex apparatus B04; presses per se for squeezing-out liquid from liquid-containing material B30B9/02; treatment of water C02F, e.g. softening by ion-exchange C02F1/42; {arrangements of air intake cleaners in gas turbine plants F02C7/05} ; arrangements or mounting of filters in air-conditioning, air-humidification or ventilation F24F13/28) - B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS - 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 sulfur removal system including a first reactor and a second reactor that are located in series to one another each having an adsorbent that includes cobalt and copper on an activated carbon support, a method of desulfurizing a sulfur-containing hydrocarbon stream via the sulfur removal system, and a method of making the adsorbent. Various embodiments of the sulfur removal system, the desulfurizing method, and the method of making the adsorbent is also provided. ## Claims ### Claim 1 A sulfur removal system, comprising: a first reactor comprising a first vessel having a first internal cavity with a first adsorbent bed that contains a first adsorbent, a first inlet located proximal to a bottom of the first vessel, and a first outlet located proximal to a top of the first vessel; wherein the first reactor is a fluidized-bed reactor; and a second reactor comprising a second vessel having a second inlet, a second outlet, and a second internal cavity with a second adsorbent bed that contains a second adsorbent, wherein the first and the second adsorbents comprise cobalt and copper on an activated carbon support, wherein the first adsorbent bed has a cross-sectional area that is substantially the same as a cross-sectional area of the first vessel, and wherein the second inlet is fluidly connected to the first outlet via a connecting line. ### Claim 2 (depends on 1) The system of claim 1, wherein the first and the second adsorbents are substantially the same. ### Claim 3 (depends on 1) The system of claim 1, further comprising a lower mesh structure located in the first internal cavity and proximal to the bottom of the first vessel and an upper mesh structure located in the first internal cavity and proximal to the top of the first vessel, defining the first adsorbent bed. ### Claim 4 (depends on 3) The system of claim 3, wherein the first adsorbent has a particle size in the range of 0.5 to 10 mm, and wherein the lower and the upper mesh structures have a mesh size of less than 0.5 mm. ### Claim 5 (depends on 1) The system of claim 1, wherein the second reactor is a fixed-bed reactor. ### Claim 6 (depends on 5) The system of claim 5, wherein the second inlet is located proximal to a top of the second vessel and the second outlet is located proximal to a bottom of the second vessel. ### Claim 7 (depends on 5) The system of claim 5, wherein the second inlet is located proximal to a bottom of the second vessel and the second outlet is located proximal to a top of the second vessel. ### Claim 8 (depends on 1) The system of claim 1, further comprising: a liquid reservoir located upstream of and fluidly connected to the first inlet via a solvent line, wherein the liquid reservoir is configured to deliver a solvent to the first and the second internal cavities to regenerate the first and the second adsorbents. ### Claim 9 (depends on 1) A method of desulfurizing a sulfur-containing hydrocarbon stream with the sulfur removal system of claim 1, comprising: delivering the sulfur-containing hydrocarbon stream to the first inlet and contacting the sulfur-containing hydrocarbon stream with the first adsorbent to form a partially desulfurized hydrocarbon stream; and delivering the partially desulfurized hydrocarbon stream to the second inlet and contacting the partially desulfurized hydrocarbon stream with the second adsorbent to form a desulfurized hydrocarbon stream. ### Claim 10 (depends on 9) The method of claim 9, wherein the sulfur-containing hydrocarbon stream is contacted with the first adsorbent at a temperature of 15 to 35° C. and a pressure of 0.9 to 1.1 atm, and wherein the partially desulfurized hydrocarbon stream is contacted with the second adsorbent at a temperature of 15 to 35° C. and a pressure of 0.9 to 1.1 atm. ### Claim 11 (depends on 9) The method of claim 9, wherein the sulfur-containing hydrocarbon stream comprises at least one sulfur compound selected from the group consisting of a thiophene, a benzothiophene, a dibenzothiophene, a methyl benzothiophene, a methyl dibenzothiophene, and a dimethyl dibenzothiophene. ### Claim 12 (depends on 9) The method of claim 9, wherein a concentration of sulfur compounds in the sulfur-containing hydrocarbon stream is at least 50 ppm, and wherein a concentration of sulfur compounds in the desulfurized hydrocarbon stream is no more than 5 ppm. ### Claim 13 (depends on 9) The method of claim 9, wherein the sulfur removal system further comprises a liquid reservoir located upstream of and fluidly connected to the first inlet via a solvent line, the method further comprising: delivering a solvent to the first inlet to regenerate the first adsorbent and the second inlet to regenerate the second adsorbent. ### Claim 14 (depends on 13) The method of claim 13, wherein the first adsorbent is regenerated within the first reactor and the second adsorbent is regenerated within the second reactor. ### Claim 15 (depends on 13) The method of claim 13, further comprising: delivering an inert gas to the first inlet to evaporate the solvent, after delivering the solvent. ### Claim 16 (depends on 15) The method of claim 15, wherein the inert gas is nitrogen gas with a temperature in the range of 150 to 350° C., which is delivered with a flow rate of 0.02 to 5 L/min.