WO2002102710A1 - Reactor catalítico de membrana para la descomposición del sulfuro de hidrógeno en hidrógeno y azufre y la separación de los productos de dicha composición - Google Patents
Reactor catalítico de membrana para la descomposición del sulfuro de hidrógeno en hidrógeno y azufre y la separación de los productos de dicha composición Download PDFInfo
- Publication number
- WO2002102710A1 WO2002102710A1 PCT/ES2001/000244 ES0100244W WO02102710A1 WO 2002102710 A1 WO2002102710 A1 WO 2002102710A1 ES 0100244 W ES0100244 W ES 0100244W WO 02102710 A1 WO02102710 A1 WO 02102710A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- hydrogen
- decomposition
- reactor
- porous membrane
- reactor according
- Prior art date
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 69
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical group S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 68
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 49
- 239000001257 hydrogen Substances 0.000 title claims abstract description 49
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 40
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 19
- 238000000354 decomposition reaction Methods 0.000 title claims description 42
- 238000000926 separation method Methods 0.000 title claims description 20
- 239000005864 Sulphur Substances 0.000 title abstract 2
- 239000000919 ceramic Substances 0.000 claims abstract description 56
- 239000003054 catalyst Substances 0.000 claims abstract description 37
- 239000007789 gas Substances 0.000 claims abstract description 24
- 238000005979 thermal decomposition reaction Methods 0.000 claims abstract description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 56
- 239000011593 sulfur Substances 0.000 claims description 24
- 229910052717 sulfur Inorganic materials 0.000 claims description 24
- 238000000034 method Methods 0.000 claims description 21
- 150000002431 hydrogen Chemical class 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 9
- 238000003421 catalytic decomposition reaction Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 3
- 239000011733 molybdenum Substances 0.000 claims description 3
- 230000007704 transition Effects 0.000 claims description 3
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical group [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 2
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 claims description 2
- 229910052804 chromium Inorganic materials 0.000 claims description 2
- 239000011651 chromium Substances 0.000 claims description 2
- 239000004927 clay Substances 0.000 claims description 2
- 239000011521 glass Substances 0.000 claims description 2
- CWQXQMHSOZUFJS-UHFFFAOYSA-N molybdenum disulfide Chemical group S=[Mo]=S CWQXQMHSOZUFJS-UHFFFAOYSA-N 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 229910052719 titanium Inorganic materials 0.000 claims description 2
- 239000010936 titanium Substances 0.000 claims description 2
- 229910052726 zirconium Inorganic materials 0.000 claims description 2
- 230000008569 process Effects 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000000203 mixture Substances 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 230000035699 permeability Effects 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910052723 transition metal Inorganic materials 0.000 description 2
- 150000003624 transition metals Chemical class 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 description 1
- 239000011324 bead Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 210000004907 gland Anatomy 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- PTISTKLWEJDJID-UHFFFAOYSA-N sulfanylidenemolybdenum Chemical compound [Mo]=S PTISTKLWEJDJID-UHFFFAOYSA-N 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/02—Inorganic material
- B01D71/04—Glass
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8612—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/88—Handling or mounting catalysts
- B01D53/885—Devices in general for catalytic purification of waste gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/02—Inorganic material
- B01D71/024—Oxides
- B01D71/025—Aluminium oxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J15/00—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor
- B01J15/005—Chemical processes in general for reacting gaseous media with non-particulate solids, e.g. sheet material; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/244—Concentric tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2475—Membrane reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
- B01J35/58—Fabrics or filaments
- B01J35/59—Membranes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0495—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by dissociation of hydrogen sulfide into the elements
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/04—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of inorganic compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/501—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by diffusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/18—Details relating to the spatial orientation of the reactor
- B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0405—Purification by membrane separation
- C01B2203/041—In-situ membrane purification during hydrogen production
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Definitions
- the invention relates to the treatment of gases containing hydrogen sulfide by decomposition of hydrogen sulfide into sulfur and hydrogen and the separation of said products by using a catalytic membrane reactor comprising a ceramic porous membrane, permeable to the passage of the hydrogen, on which a suitable catalyst for the decomposition of hydrogen sulfide into sulfur and hydrogen has been deposited.
- the usual treatment of residual hydrogen sulfide is based on the Klauss process, which includes the mutual reduction / oxidation between sulfur dioxide and hydrogen sulfide to produce water and elemental sulfur.
- Kameyama et al. [T. Kameyama et al., Int. J. Hydrogen Energy, Vol. 8, No. 1, 5-13, 1983] describe a catalytic membrane reactor for the catalytic decomposition of hydrogen sulfide consisting of a cylindrical body and a tubular ceramic membrane arranged coaxially therein.
- a suitable catalyst such as a sulphide of a transition metal, for example, molybdenum sulphide, and it is precisely in said space where the decomposition reaction of the hydrogen sulfide.
- the decomposition of hydrogen sulfide in this reactor takes place at 700-800 ° C.
- the invention faces the problem of developing a membrane catalytic reactor useful for the catalytic decomposition of hydrogen sulfide and the separation of the products of said decomposition that solves all or part of the aforementioned problems.
- the solution provided by the invention is based on the observation that it is possible, simultaneously, (i) to catalytically decompose hydrogen sulfide into sulfur and hydrogen and (ii) separate the products of said decomposition, by using a porous ceramic membrane on which a suitable catalyst has been deposited in the form of a layer. In this way, the catalytic decomposition of hydrogen sulphide is carried out simultaneously with the separation of the hydrogen formed thereby achieving that the reaction moves in the desired direction.
- a reactor as described in this description provides a decomposition of hydrogen sulfide in. sulfur and hydrogen improved together with, simultaneously, a separation of the products of said decomposition.
- said reactor is economical, can be used effectively at the industrial level and increases the production of hydrogen.
- the objective of this invention is a catalytic membrane reactor for the decomposition of hydrogen sulphide and the separation of decomposition products comprising a porous ceramic membrane on which a suitable catalyst has been deposited in the form of a layer.
- a further object of this invention is a process for the decomposition of hydrogen sulfide and, simultaneously, the separation of the products of said decomposition comprising the use of said reactor.
- Figure 1 is a schematic representation of the reactor object of this invention comprising a single ceramic porous membrane element.
- FIG. 2 is a schematic representation of the reactor object of this invention comprising several parallel ceramic porous membrane elements.
- the invention consists of a catalytic membrane reactor for the decomposition of hydrogen sulfide and the separation of the products of the decomposition, hereinafter reactor of the invention, comprising a body, a tubular ceramic porous membrane element arranged coaxially therein to remove hydrogen, and a catalyst for thermal decomposition of hydrogen sulfide into sulfur and hydrogen, in which said catalyst has been deposited directly on said tubular ceramic porous membrane element in the form of a layer.
- the reactor of the invention has the characteristic that the catalyst, instead of being located inside the reactor, is in the form of a thin layer or microlayer, deposited on the tubular ceramic porous membrane element.
- the catalyst instead of being located inside the reactor, is in the form of a thin layer or microlayer, deposited on the tubular ceramic porous membrane element.
- the reactor body of the invention may take any appropriate form, for example, it may be configured in a cylindrical shape and can be made of any suitable material that resists the temperatures at which it should work.
- the reactor body contains means for the entry of the feed gas (gas containing hydrogen sulfide) as well as means for the exit of hydrogen, sulfur and hydrogen sulfide that has not been decomposed.
- the tubular ceramic porous membrane element is an element configured in the form of a tube and manufactured from a ceramic porous membrane.
- a porous ceramic membrane any conventional ceramic porous membrane can be used, permeable to the passage of hydrogen but substantially impermeable to the passage of sulfur.
- the porous ceramic membrane includes a layer of selective permeability that allows the passage of hydrogen.
- the tubular ceramic porous membrane element comprises said first porous ceramic layer and said second selective ceramic layer.
- the porosity of said layers may vary within a wide range.
- said first layer may have a porosity between 1 and 2 ⁇ m, while the porosity of said second layer is less than 1 ⁇ m, for example, 0.2 ⁇ m.
- the tubular ceramic porous membrane element can be manufactured from any suitable material, for example, from any material commonly used in the production of porous ceramic membranes for use in catalytic membrane reactors for the decomposition of hydrogen sulfide.
- the material used in the manufacture of the tubular ceramic porous membrane element comprises Aluminum Dioxide, which may constitute the material of said second selective ceramic layer or layer previously referred to, and clay acting as binder and / or plasticizer.
- said ceramic tubular membrane element is a tubular element made of Vicor glass.
- the catalyst to be deposited on the surface of the tubular ceramic porous membrane element can be any conventional catalyst capable of catalytically decomposing hydrogen sulfide, preferably at a temperature between 400 ° C and 700 ° C.
- said catalyst is a metal selected from the transition elements, for example, chromium, molybdenum, nickel, titanium, zirconium, etc., optionally in the form of a derivative thereof, such as a salt.
- said catalyst is molybdenum sulfide and in which the thickness of this catalytic layer is up to 2 microns of molybdenum.
- the catalyst can be deposited on the surface of the tubular ceramic porous membrane element by any conventional method, for example, by deposition, spraying, impregnation or immersion in a solution or suspension containing said catalyst. More specifically, said catalyst can be deposited in the form of a thin layer by the sol-gel technique [sol
- the porosity of the catalyst layer can vary over a wide range. In a particular embodiment, the porosity of the catalytic layer is between 0.04 and 0.07 ⁇ m.
- the reactor of the invention may contain a single tubular ceramic porous membrane element or, alternatively, in other particular embodiments, it may contain two or more parallel tubular ceramic porous membrane elements installed in the reactor body. As can be seen in Figure 1, the reactor of the invention is constituted by a body (1), a tubular ceramic porous membrane element (2) with a selective layer (3) to the passage of hydrogen, and a catalyst layer ( 4) deposited directly on said selective layer (3).
- the tubular ceramic porous membrane element (2) is coaxially disposed within the body (1) of the reactor, so that the ends of the tubular ceramic porous membrane element (2) are hermetically isolated from the space between the body (1) and the outer wall of said tubular ceramic porous membrane element (2).
- the ends of the ceramic porous membrane element are fixed either by the end or by a junction of the gland type (cingulate) to the reactor body (1).
- the body (1) of the reactor also includes a conduit
- the reactor of the invention may also contain a package of an appropriate material, for example, of graphite-graviflex.
- the reactor of the invention operates as described below.
- the initial gas heated to a temperature between 400 ° C and 700 ° C, with a small overpressure, between 50.5-101 Pa (0.5-1 atm), travels into the reactor of the invention through of driving (5).
- the catalyst layer (4) deposited on the outer surface of the tubular ceramic porous membrane element (2) hydrogen sulfide decomposes into hydrogen and sulfur.
- the hydrogen separates directly from sulfur and hydrogen sulfide.
- the total effect of the separation of hydrogen from sulfur and hydrogen sulfide is determined by the contribution of catalytic conversion and the contribution of a separation factor of a selective layer (3) of the tubular ceramic porous membrane element (2) .
- the gas that penetrates through the wall of the tubular ceramic porous membrane element (2), composed of a mixture of hydrogen and the initial gas, is injected from the reactor through the conduit (6).
- the gas that has not penetrated through the wall of the tubular ceramic porous membrane element (2), composed of a mixture of non-decomposed hydrogen sulfide and gaseous sulfur, is injected outside through the conduit (7).
- This last gas mixture can be directed to another reactor of the invention and this operation can be repeated several times until the total decomposition of the initial hydrogen sulfide is achieved.
- the total effect that can be achieved of hydrogen sulfide decomposition and separation of the gas mixture obtained in a single step process is between 30% and 55% of the initial hydrogen sulfide content in the feed gas at reactor
- the reactor of the invention acts on a gas with a hydrogen sulphide content of approximately 4%, at a flow rate by volume of the initial gas of 1-100 hours "1 and the catalyst applied is a sulphide of a transition metal previously prepared in a medium of H 2 S, the total conversion of hydrogen sulfide into hydrogen and sulfur will be increased from 35% to 56%, depending on the temperature, in a single reactor operation of the invention
- the known catalytic effect using only the same catalyst, at temperatures between 400 ° C and 700 ° C and at the same Flow rate per initial gas volume, does not exceed a maximum of 40%.
- a characteristic of the reactor of the invention lies in the use of a catalyst directly deposited as a layer on an external selective layer of a tubular ceramic porous membrane element, thereby significantly reducing the necessary amount of catalyst, catalyst losses are reduced , the sintering of catalyst beads (necessary in other reactors) is eliminated and the total yield of the process is increased.
- the removal of hydrogen directly from the reaction zone through the porous ceramic membrane shifts the equilibrium of the decomposition in the desired direction. In this way, a total effect of decomposition and separation of products of said decomposition is achieved directly from the reaction zone, which results in an increase in the yield in different embodiments of the process.
- the invention also provides a process for the decomposition of hydrogen sulfide into sulfur and hydrogen and the separation of the products of said decomposition, hereinafter, the process of the invention, which comprises the use of at least one reactor of the invention.
- the process includes feeding the reactor with the hydrogen sulfide-containing gas, heated to a temperature between 400 ° C and 700 ° C, with a small overpressure, between 50.5 and 101 kPa (0.5-1 atm ).
- the gas containing the hydrogen sulphide is moved into the reactor of the invention and contacted with the catalyst, deposited in the form of a layer on the outer surface of the tubular ceramic porous membrane element, whereby hydrogen sulfide decomposes into hydrogen and sulfur.
- the hydrogen produced crosses the selective layer present in the tubular ceramic porous membrane element from which it can be removed. Sulfur and hydrogen sulfide that has not been decomposed leave the reactor through existing conduits in the reactor for this purpose.
- the process of the invention is suitable for the treatment of gases containing hydrogen sulphide, preferably gases with a hydrogen sulphide content between 1% and 96%.
- the invention can be applied in petroleum refining, for example, in the processing of so-called "acidic" gases, in the processing of gases, in the treatment of gases for removing hydrogen sulfide from mixtures containing it, in the treatment of gaseous leaks with a high content of hydrogen sulphide and also in other industries related to the decomposition of hydrogen sulfide into hydrogen and sulfur, with the subsequent separation of decomposition products.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Materials Engineering (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
MXPA03011640A MXPA03011640A (es) | 2001-06-15 | 2001-06-15 | Reactor catalitico de membrana para la descomposicion del sulfuro de hidrogeno en hidrogeno y azufre y la separacion de los productos de dicha descomposicion. |
BR0117052-0A BR0117052A (pt) | 2001-06-15 | 2001-06-15 | Reator de membrana catalìtica para quebrar sulfeto de hidrogênio em enxofre e hidrogênio e separar os produtos da quebra e processo para quebra catalìtica do mesmo |
CA002450938A CA2450938A1 (en) | 2001-06-15 | 2001-06-15 | Catalytic membrane reactor that is used for the decomposition of hydrogen sulphide into hydrogen and sulphur and the separation of the products of said decomposition |
EP20010940594 EP1411029A1 (en) | 2001-06-15 | 2001-06-15 | Catalytic membrane reactor that is used for the decomposition of hydrogen sulphide into hydrogen and sulphur and the separation of the products of said decomposition |
PCT/ES2001/000244 WO2002102710A1 (es) | 2001-06-15 | 2001-06-15 | Reactor catalítico de membrana para la descomposición del sulfuro de hidrógeno en hidrógeno y azufre y la separación de los productos de dicha composición |
CNA018235190A CN1541184A (zh) | 2001-06-15 | 2001-06-15 | 用于将硫化氢分解成氢和硫并将该分解产物分离的膜式催化反应器 |
US10/736,212 US20040141910A1 (en) | 2001-06-15 | 2003-12-15 | Catalytic membrane reactor for breaking down hydrogen sulphide into hydrogen and sulfur and separating the products of this breakdown |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/ES2001/000244 WO2002102710A1 (es) | 2001-06-15 | 2001-06-15 | Reactor catalítico de membrana para la descomposición del sulfuro de hidrógeno en hidrógeno y azufre y la separación de los productos de dicha composición |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/736,212 Continuation US20040141910A1 (en) | 2001-06-15 | 2003-12-15 | Catalytic membrane reactor for breaking down hydrogen sulphide into hydrogen and sulfur and separating the products of this breakdown |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2002102710A1 true WO2002102710A1 (es) | 2002-12-27 |
Family
ID=8244352
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/ES2001/000244 WO2002102710A1 (es) | 2001-06-15 | 2001-06-15 | Reactor catalítico de membrana para la descomposición del sulfuro de hidrógeno en hidrógeno y azufre y la separación de los productos de dicha composición |
Country Status (7)
Country | Link |
---|---|
US (1) | US20040141910A1 (es) |
EP (1) | EP1411029A1 (es) |
CN (1) | CN1541184A (es) |
BR (1) | BR0117052A (es) |
CA (1) | CA2450938A1 (es) |
MX (1) | MXPA03011640A (es) |
WO (1) | WO2002102710A1 (es) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8597383B2 (en) | 2011-04-11 | 2013-12-03 | Saudi Arabian Oil Company | Metal supported silica based catalytic membrane reactor assembly |
US9745191B2 (en) | 2011-04-11 | 2017-08-29 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
Families Citing this family (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA2488295A1 (en) * | 2002-06-04 | 2003-12-11 | University Of Wyoming | Membrane for hydrogen recovery from streams containing hydrogen sulfide |
US7648566B2 (en) * | 2006-11-09 | 2010-01-19 | General Electric Company | Methods and apparatus for carbon dioxide removal from a fluid stream |
US7966829B2 (en) * | 2006-12-11 | 2011-06-28 | General Electric Company | Method and system for reducing CO2 emissions in a combustion stream |
DE102008013041A1 (de) * | 2008-03-06 | 2009-09-10 | Volkswagen Ag | Reinigung eines Abgases |
WO2009132031A2 (en) * | 2008-04-21 | 2009-10-29 | Swapsol Corp. | Hydrogen sulfide conversion to hydrogen |
CN102824822B (zh) * | 2012-09-12 | 2014-12-31 | 南京工业大学 | 一种膜分离空气净化装置 |
CN105330290A (zh) * | 2015-10-19 | 2016-02-17 | 华南理工大学 | 一种用于h2s分解的混合导体陶瓷膜的制备及测试方法 |
GB201616517D0 (en) * | 2016-09-29 | 2016-11-16 | Akay Galip | Integrated intensified catalytic chemical conversion processes |
CN110124652B (zh) * | 2018-02-09 | 2022-02-11 | 中国石油化工股份有限公司 | 含有改性碳纳米管的分解硫化氢的催化剂及其制备方法和应用 |
CN110124651B (zh) * | 2018-02-09 | 2022-03-04 | 中国石油化工股份有限公司 | 含有碳纳米笼的分解硫化氢的催化剂及其制备方法和应用 |
CN110127602B (zh) * | 2018-02-09 | 2020-09-25 | 中国石油化工股份有限公司 | 应用催化剂分解硫化氢的方法 |
CN110124653B (zh) * | 2018-02-09 | 2022-03-04 | 中国石油化工股份有限公司 | 分解硫化氢的催化剂及其制备方法和应用 |
CN110734782B (zh) * | 2018-07-19 | 2021-07-23 | 中山市亿鼎杰纳米科技有限公司 | 一种劣质重油的加氢处理方法 |
IT201900006957A1 (it) * | 2019-05-17 | 2020-11-17 | Milano Politecnico | Forno per campi gas, per raffinerie e per il processo di reforming |
IL296627A (en) * | 2020-03-20 | 2022-11-01 | Standard H2 Inc | Process and apparatus for obtaining hydrogen and sulfur from hydrogen sulfide |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1996036422A1 (en) * | 1995-05-17 | 1996-11-21 | Parsons Process Group Inc. | Process for selective oxidation |
WO1999033748A1 (fr) * | 1997-12-29 | 1999-07-08 | Elf Exploration Production | Procede et catalyseur pour oxyder directement en soufre l'h2s contenu dans un gaz |
US5965100A (en) * | 1995-04-25 | 1999-10-12 | Khanmamedov; Tofik K. | Process for recovery of sulfur from an acid gas stream |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4039613A (en) * | 1973-10-29 | 1977-08-02 | Agency Of Industrial Science & Technology | Process for production of hydrogen and sulfur from hydrogen sulfide as raw material |
DE3925985C2 (de) * | 1989-08-05 | 1998-08-20 | Metallgesellschaft Ag | Verfahren zum Verbrennen eines H¶2¶S-haltigen Gases |
US5229102A (en) * | 1989-11-13 | 1993-07-20 | Medalert, Inc. | Catalytic ceramic membrane steam-hydrocarbon reformer |
US5843395A (en) * | 1997-03-17 | 1998-12-01 | Wang; Chi S. | Process for hydrogen production from hydrogen sulfide dissociation |
US6235417B1 (en) * | 1999-04-30 | 2001-05-22 | Her Majesty The Queen In Right Of Canada, As Represented By The Minister Of Natural Resources | Two-phase hydrogen permeation membrane |
CA2488295A1 (en) * | 2002-06-04 | 2003-12-11 | University Of Wyoming | Membrane for hydrogen recovery from streams containing hydrogen sulfide |
-
2001
- 2001-06-15 CA CA002450938A patent/CA2450938A1/en not_active Abandoned
- 2001-06-15 BR BR0117052-0A patent/BR0117052A/pt not_active Application Discontinuation
- 2001-06-15 WO PCT/ES2001/000244 patent/WO2002102710A1/es not_active Application Discontinuation
- 2001-06-15 CN CNA018235190A patent/CN1541184A/zh active Pending
- 2001-06-15 EP EP20010940594 patent/EP1411029A1/en not_active Withdrawn
- 2001-06-15 MX MXPA03011640A patent/MXPA03011640A/es not_active Application Discontinuation
-
2003
- 2003-12-15 US US10/736,212 patent/US20040141910A1/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5965100A (en) * | 1995-04-25 | 1999-10-12 | Khanmamedov; Tofik K. | Process for recovery of sulfur from an acid gas stream |
WO1996036422A1 (en) * | 1995-05-17 | 1996-11-21 | Parsons Process Group Inc. | Process for selective oxidation |
WO1999033748A1 (fr) * | 1997-12-29 | 1999-07-08 | Elf Exploration Production | Procede et catalyseur pour oxyder directement en soufre l'h2s contenu dans un gaz |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8597383B2 (en) | 2011-04-11 | 2013-12-03 | Saudi Arabian Oil Company | Metal supported silica based catalytic membrane reactor assembly |
US9745191B2 (en) | 2011-04-11 | 2017-08-29 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
US10071909B2 (en) | 2011-04-11 | 2018-09-11 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
US10093542B2 (en) | 2011-04-11 | 2018-10-09 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
US10252910B2 (en) | 2011-04-11 | 2019-04-09 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic structures |
US10252911B2 (en) | 2011-04-11 | 2019-04-09 | Saudi Arabian Oil Company | Auto thermal reforming (ATR) catalytic systems |
Also Published As
Publication number | Publication date |
---|---|
US20040141910A1 (en) | 2004-07-22 |
BR0117052A (pt) | 2004-07-27 |
EP1411029A1 (en) | 2004-04-21 |
CN1541184A (zh) | 2004-10-27 |
MXPA03011640A (es) | 2005-10-05 |
CA2450938A1 (en) | 2002-12-27 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
WO2002102710A1 (es) | Reactor catalítico de membrana para la descomposición del sulfuro de hidrógeno en hidrógeno y azufre y la separación de los productos de dicha composición | |
US7048778B2 (en) | Apparatus and method for separating gases | |
Wei et al. | Dense ceramic oxygen permeable membranes and catalytic membrane reactors | |
KR101376082B1 (ko) | 산화 반응기 및 산화 방법 | |
Pandey et al. | Membranes for gas separation | |
EP2138222A1 (en) | Method for pore size modification of an inorganic membrane by chemical vapor infiltration | |
JPS5814809B2 (ja) | 水素ガスの分離回収方法 | |
JPH067625A (ja) | 水素透過性複合金属膜を用いて水素を他のガスから分離する方法 | |
Zhao et al. | MXene assisted preparation of well-intergrown ZIF-67 membrane for helium separation | |
KR20120114261A (ko) | 실리카계 수소 분리 재료 및 그 제조 방법과 그것을 포함한 수소 분리 모듈 및 수소 제조 장치 | |
CA2488295A1 (en) | Membrane for hydrogen recovery from streams containing hydrogen sulfide | |
EP1829604A1 (en) | Composite oxygen conductive membrane | |
EP2384806B1 (en) | Feed gas contaminant removal process in oxygen ion transport membrane systems | |
JP7170825B2 (ja) | 分離方法 | |
Meng et al. | Microporous Silica Membrane Reactors | |
JP2023518475A (ja) | 硫化水素を水素ガス及び硫黄に変換する方法及び装置 | |
CN105056715A (zh) | 一种氢气分离装置 | |
Tago et al. | Preparation of hydrophilic silicalite-1 nanocrystal-layered membrane for separation of water from water–acetone solution by pervaporation | |
KR20230062049A (ko) | Sapo-34 제올라이트가 박막코팅된 기체분리 복합막 제조방법 및 이를 통해 제조되는 sapo-34 제올라이트 복합막 | |
CN118176055A (zh) | 沸石膜复合体、膜反应装置以及沸石膜复合体的制造方法 | |
CN116847924A (zh) | 沸石膜复合体、分离装置、膜反应装置以及沸石膜复合体的制造方法 | |
Basile et al. | Current Trends and Future Developments on (Bio-) Membranes: Modern Approaches in Membrane Technology for Gas Separation and Water Treatment | |
CN113508092A (zh) | 结晶性物质及膜复合体 | |
Deng | Application Oriented Low-dimensional Material Platforms for Energy and the Environment | |
KR20030026515A (ko) | 제올라이트를 이용한 기체 분리 장치 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CR CU CZ DE DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
DFPE | Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101) | ||
WWE | Wipo information: entry into national phase |
Ref document number: 10736212 Country of ref document: US Ref document number: 2450938 Country of ref document: CA Ref document number: PA/a/2003/011640 Country of ref document: MX |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2001274119 Country of ref document: AU Ref document number: 2001940594 Country of ref document: EP Ref document number: 43/KOLNP/2004 Country of ref document: IN |
|
WWE | Wipo information: entry into national phase |
Ref document number: 20018235190 Country of ref document: CN |
|
WWP | Wipo information: published in national office |
Ref document number: 2001940594 Country of ref document: EP |
|
REG | Reference to national code |
Ref country code: DE Ref legal event code: 8642 |
|
WWW | Wipo information: withdrawn in national office |
Ref document number: 2001940594 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: JP |