CA1093281A - Method of removing hydrogen sulfide from gases, and for obtaining elemental sulfur - Google Patents
Method of removing hydrogen sulfide from gases, and for obtaining elemental sulfurInfo
- Publication number
- CA1093281A CA1093281A CA287,897A CA287897A CA1093281A CA 1093281 A CA1093281 A CA 1093281A CA 287897 A CA287897 A CA 287897A CA 1093281 A CA1093281 A CA 1093281A
- Authority
- CA
- Canada
- Prior art keywords
- hydrogen sulfide
- gases
- gas
- elemental sulfur
- hydrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000007789 gas Substances 0.000 title claims abstract description 72
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 229910000037 hydrogen sulfide Inorganic materials 0.000 title claims abstract description 52
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000005201 scrubbing Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 229910052717 sulfur Inorganic materials 0.000 claims description 10
- 239000011593 sulfur Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 239000000571 coke Substances 0.000 claims 1
- 239000002912 waste gas Substances 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 239000002918 waste heat Substances 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- 229940032330 sulfuric acid Drugs 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- 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
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0456—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process the hydrogen sulfide-containing gas being a Claus process tail gas
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Environmental & Geological Engineering (AREA)
- Inorganic Chemistry (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
- Industrial Gases (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
The disclosure describes a method of removing hydrogen sulfide from gases, particularly coke-oven gases and for obtain-ing elemental sulfur. Hydrogen sulfide is washed out of the gases in a scrubbing unit which uses a scrubbing solution and is expelled from the scrubbing solution by adding water vapor thereto. The resulting vapours, consisting mainly of hydrogen sulfide are fed to a Claus plant in which most of the hydrogen sulfide is converted into elemental sulfur. The gases leaving the Claus plant are hydrogenated to form hydrogenated waste gases. The latter are cooled to form a condensate and are added to the gas to be purified before reaching the hydrogen sulfide scrubbing unit. This method is less expensive than known methods and provides a thorough environmental protection.
The disclosure describes a method of removing hydrogen sulfide from gases, particularly coke-oven gases and for obtain-ing elemental sulfur. Hydrogen sulfide is washed out of the gases in a scrubbing unit which uses a scrubbing solution and is expelled from the scrubbing solution by adding water vapor thereto. The resulting vapours, consisting mainly of hydrogen sulfide are fed to a Claus plant in which most of the hydrogen sulfide is converted into elemental sulfur. The gases leaving the Claus plant are hydrogenated to form hydrogenated waste gases. The latter are cooled to form a condensate and are added to the gas to be purified before reaching the hydrogen sulfide scrubbing unit. This method is less expensive than known methods and provides a thorough environmental protection.
Description
The invention relates to a method of removing hydrogen sulfide from gases, more particularly coke-oven gas, and obtain-ing elemental sulfur.
Gas-oven gas, like natural gas and refinery gases, normally contains relatively large amounts of hydrogen sulfide~
When the gases are subsequently treated, either to form synthesis gas or to be distributed and burnt, the hydrogen sulfide has to be removed~ When the gases are desulfurized by the "oxidation"
method, hydrogen sulfide is oxidized in the liquid phase to form elemental sulfur. In the'heutralization" method, in which the hydrogen sulfide occurs in the regeneration step, it is converted into sulfuric acid in a sulfuric-acid plant or into elemental sulfur in a Claus plant. For economical reasons, the afore-mentioned Claus plants usually include two stages, i.e.
they have two catalyst stages.
Two-stage Claus plants reach a sulfur conversion rate of about 94%. They are therefore equipped with an after-burn-ing chamber, in which the remaining hydrogen sulfide is burnt to form sulfur dioxide. In this manner, about 6% of the scrubbed hydrogen sulfide is released into the atmosphere in the form of sulfur dioxide. For environmental reasons, this process is no longer up to date.
In the aforementioned Claus plants, it is known to replace the after-burning unit by a hydrogenation stage and to re-hydrogenate the sulfur compounds present in the waste gas from the Claus oven into hydrogen sulfide, using coke-oven gas.
- The hydrogen sulfide is then scrubbed in a downstream hydrogen-sulfide scrubbing unit, before the remaining gases are after-burned and introduced into the chimney of the Claus plant.
It is an object of the present invention to provide an even more thorough environmental protection by using a less 1093Z8~
expensive method.
The invention is based on a method of removing hydrogen sulfide from gases, more particularly coke-oven gas, and for obtaining elemental sulfur, wherein the hydrogen sulfide is washed out of the gases in a scrubbing unit using a scrubbing solution, and is expelled from the scrubbing solution by adding water vapour thereto, whereupon the vapours, consisting mainly of hydrogen sulfide, are fed to a Claus plant in which most of the hydrogen sulfide is converted into elemental sulfur and the gases leaving the Claus plant are hydrogenated. According to the invention, the hydrogenated waste gases are cooled and added to the gas to be purified before it reaches the hydrogen sulfide scrubbing unit.
Thus, the residual gases from the Claus plant are heated by adding hot hydrogenation gases and the sulfur compounds are reduced to hydrogen sulfide in a reactor. After the waste heat has been made available for use, downstream of the reactor, the gases are introduced into a direct cooler. After leaving the cooler, they still contain a large amount of hydrogen sulfide and are added to the crude gas to be d~sulfurized, before entering the hydrogen sulfide scrubbing unit.
According to the invention, the condensate produced by cooling the hydrogenated gas is supplied to the separating unit, in which the hydrogen sulfide is expelled from the scrubb-ing solution by adding water-vapour. Preferably, according to another feature of the invention, the process is in two stages, the gases being cooled first in an indirect cooler and then in a direct cooler.
In accordance with a broad aspect of the invention, there is provided a method for removing hydrogen sulfide from gases and for obtaining elemental sulfur comprising scrubbing the gases with a scrubbing solution in a hydrogen-sulfide ~3 - _ 1~93281 scrubber whereby hydrogen sulfide is scrubbed out of the gases, expelling the hydrogen sulfide from the scrubbing solution in a deacidifier using water vapor, convering the hydrogen sulfide from the deacidifier in a reaction chamber to form reaction products of elemental sulfur and residual sulfur-bearing gases, hydrogenating the residual sulfur-bearing gases passing from the reaction chamber to form hydrogen sulfide gas and water vapor, cooling the thus-formed hydrogen sulfide gas and water vapor to recover condensed water, supplying at least a portion of the condensed water to said deacidifier, and mixing the cooled hydrogen sulfide gas with the gases passing into said hydrogen-sulfide scrubber.
The invention will now be explained in greater detail with reference to the annexed drawing in which, The FIGURE is a diagram illustrating a preferred - 2a -embodiment of the invention.
The gas to be desulfurized flows through line 61 into a scrubbing unit 62, in which it is largely freed from hydrogen sulfide. The purified gas leaves the hydrogen sulfide scrubbing unit 62 through line 63. The scrubbing solution is supplied through line 55 to a deacidifier 56, into which water vapour is introduced through line 57. The expelled acid gases leave the deacidifier 56 through line 59 and are cooled in cooler 60 to a temperature of about 50 to 70C. The deacidified waste water is withdrawn from the deacidifier through line 58 and is either returned to the scrubber or is sent for further treatment to an ammonia separating unit.
The vapours, which mainly contain hydrogen sulfide, are conveyed through line 10 to a Claus plant. The gas is divided into two partial streams in a 1:3 ratio. The smaller stream is conveyed through line 11 to the combustion-chamber 15 of the Claus plant, to which air is supplied through lines 13 and 14. The flue gases leaving chamber 15 flow through line 16 to a waste-heat boiler 17 for producing water-vapour, and through line 18 (after the ga.ses containing the remaining hydrogen sul-fide have been added) to a first reactor 19 filled with a catalyst, in which the actual conversion into elementary sulfur occurs. The reaction between hydrogen sulfide and hydrogen dioxide continues until equilibrium is reached. The gas leaving the reactor is conveyed through line 20 to a waste-heat boiler 21, in which the sulfur condenses out. The resulting water vapour is withdrawn through line 22.
Next, the cooled process gas is supplied through line 23 to a combustion chamber 24, which is also supplied with the required amount of air through lines 25, 26 and with the required amount of heating gas through lines 28 and 29. The hot process gases 109328~.
are then conveyed through line 30 to a second reactor 31, which contains the same catalyst as reactor 19.
The heat liberated in reactor 31 is used in a waste-heat boiler 33, supplied with hot process gases through line 32, to produce water-vapour which is withdrawn through line 34. The sulfur particles entrained through line 35 by the gas leaving boiler 33 is separated in a sulfur separator and cooler 36.
After leaving cooler 36, the residual gas from the Claus plant is sent through line 37 and is mixed with a hot hydrogenation gas. The hydrogenation gas is produced in a combustion chamber 39, which is supplied with coke-oven gas through line 38 and with a sub-stoichiometric quantity of air through line 27. The hot hydrogenation gases leave the combustion chamber through line 40 and, together with the residual gases from the Claus plant, flow through a line 41 to a hydrogenation reactor 42, in which the sulfur dioxide and the elemental sulfur present in the gas is hydrogenated into hydrogen sulfide.
After hydrogenation, the gas is conveyed through line 43 to a waste-heat boiler 44, where some of its heat is withdrawn.
The resulting water vapour is withdrawn through line 45. The gas is further cooled to ambient temperature in a direct cooler 47, which is supplied with gases through line 4~. The water for cooling the gas is supplied to the cooler through line 53, and the resulting hot water is conveyed through line 49 to a pump 50 and recycled to cooler 47 through a line 51 and an indirect cooler 52. Excess water produced by the condensation of water vapour from the process gases is conveyed through line 54 to deacidifier 56, where the hydrogen sulfide in the condensate is expelled and recycled.
The cooled process gases, which contain about 10 to 15 g hydrogen sulfide per Nm3, leave cooler 47, travel along 1093Z~31 line 48, and are mixed with the coke-oven gas before entering scrubber 62 and are desulfurized in the downstream scrubber.
Consequently, no waste gas escapes from the Claus plant. Since the waste gas from the Claus plant is mixed with the coke-oven gas, the calorific value of the coke-oven gas is reduced by about 2%. ~owever, this method increases the efficiency of a Claus plant to 100%, relative to sulfur. The process does not yield any waste gas or water harmful to the environment.
Gas-oven gas, like natural gas and refinery gases, normally contains relatively large amounts of hydrogen sulfide~
When the gases are subsequently treated, either to form synthesis gas or to be distributed and burnt, the hydrogen sulfide has to be removed~ When the gases are desulfurized by the "oxidation"
method, hydrogen sulfide is oxidized in the liquid phase to form elemental sulfur. In the'heutralization" method, in which the hydrogen sulfide occurs in the regeneration step, it is converted into sulfuric acid in a sulfuric-acid plant or into elemental sulfur in a Claus plant. For economical reasons, the afore-mentioned Claus plants usually include two stages, i.e.
they have two catalyst stages.
Two-stage Claus plants reach a sulfur conversion rate of about 94%. They are therefore equipped with an after-burn-ing chamber, in which the remaining hydrogen sulfide is burnt to form sulfur dioxide. In this manner, about 6% of the scrubbed hydrogen sulfide is released into the atmosphere in the form of sulfur dioxide. For environmental reasons, this process is no longer up to date.
In the aforementioned Claus plants, it is known to replace the after-burning unit by a hydrogenation stage and to re-hydrogenate the sulfur compounds present in the waste gas from the Claus oven into hydrogen sulfide, using coke-oven gas.
- The hydrogen sulfide is then scrubbed in a downstream hydrogen-sulfide scrubbing unit, before the remaining gases are after-burned and introduced into the chimney of the Claus plant.
It is an object of the present invention to provide an even more thorough environmental protection by using a less 1093Z8~
expensive method.
The invention is based on a method of removing hydrogen sulfide from gases, more particularly coke-oven gas, and for obtaining elemental sulfur, wherein the hydrogen sulfide is washed out of the gases in a scrubbing unit using a scrubbing solution, and is expelled from the scrubbing solution by adding water vapour thereto, whereupon the vapours, consisting mainly of hydrogen sulfide, are fed to a Claus plant in which most of the hydrogen sulfide is converted into elemental sulfur and the gases leaving the Claus plant are hydrogenated. According to the invention, the hydrogenated waste gases are cooled and added to the gas to be purified before it reaches the hydrogen sulfide scrubbing unit.
Thus, the residual gases from the Claus plant are heated by adding hot hydrogenation gases and the sulfur compounds are reduced to hydrogen sulfide in a reactor. After the waste heat has been made available for use, downstream of the reactor, the gases are introduced into a direct cooler. After leaving the cooler, they still contain a large amount of hydrogen sulfide and are added to the crude gas to be d~sulfurized, before entering the hydrogen sulfide scrubbing unit.
According to the invention, the condensate produced by cooling the hydrogenated gas is supplied to the separating unit, in which the hydrogen sulfide is expelled from the scrubb-ing solution by adding water-vapour. Preferably, according to another feature of the invention, the process is in two stages, the gases being cooled first in an indirect cooler and then in a direct cooler.
In accordance with a broad aspect of the invention, there is provided a method for removing hydrogen sulfide from gases and for obtaining elemental sulfur comprising scrubbing the gases with a scrubbing solution in a hydrogen-sulfide ~3 - _ 1~93281 scrubber whereby hydrogen sulfide is scrubbed out of the gases, expelling the hydrogen sulfide from the scrubbing solution in a deacidifier using water vapor, convering the hydrogen sulfide from the deacidifier in a reaction chamber to form reaction products of elemental sulfur and residual sulfur-bearing gases, hydrogenating the residual sulfur-bearing gases passing from the reaction chamber to form hydrogen sulfide gas and water vapor, cooling the thus-formed hydrogen sulfide gas and water vapor to recover condensed water, supplying at least a portion of the condensed water to said deacidifier, and mixing the cooled hydrogen sulfide gas with the gases passing into said hydrogen-sulfide scrubber.
The invention will now be explained in greater detail with reference to the annexed drawing in which, The FIGURE is a diagram illustrating a preferred - 2a -embodiment of the invention.
The gas to be desulfurized flows through line 61 into a scrubbing unit 62, in which it is largely freed from hydrogen sulfide. The purified gas leaves the hydrogen sulfide scrubbing unit 62 through line 63. The scrubbing solution is supplied through line 55 to a deacidifier 56, into which water vapour is introduced through line 57. The expelled acid gases leave the deacidifier 56 through line 59 and are cooled in cooler 60 to a temperature of about 50 to 70C. The deacidified waste water is withdrawn from the deacidifier through line 58 and is either returned to the scrubber or is sent for further treatment to an ammonia separating unit.
The vapours, which mainly contain hydrogen sulfide, are conveyed through line 10 to a Claus plant. The gas is divided into two partial streams in a 1:3 ratio. The smaller stream is conveyed through line 11 to the combustion-chamber 15 of the Claus plant, to which air is supplied through lines 13 and 14. The flue gases leaving chamber 15 flow through line 16 to a waste-heat boiler 17 for producing water-vapour, and through line 18 (after the ga.ses containing the remaining hydrogen sul-fide have been added) to a first reactor 19 filled with a catalyst, in which the actual conversion into elementary sulfur occurs. The reaction between hydrogen sulfide and hydrogen dioxide continues until equilibrium is reached. The gas leaving the reactor is conveyed through line 20 to a waste-heat boiler 21, in which the sulfur condenses out. The resulting water vapour is withdrawn through line 22.
Next, the cooled process gas is supplied through line 23 to a combustion chamber 24, which is also supplied with the required amount of air through lines 25, 26 and with the required amount of heating gas through lines 28 and 29. The hot process gases 109328~.
are then conveyed through line 30 to a second reactor 31, which contains the same catalyst as reactor 19.
The heat liberated in reactor 31 is used in a waste-heat boiler 33, supplied with hot process gases through line 32, to produce water-vapour which is withdrawn through line 34. The sulfur particles entrained through line 35 by the gas leaving boiler 33 is separated in a sulfur separator and cooler 36.
After leaving cooler 36, the residual gas from the Claus plant is sent through line 37 and is mixed with a hot hydrogenation gas. The hydrogenation gas is produced in a combustion chamber 39, which is supplied with coke-oven gas through line 38 and with a sub-stoichiometric quantity of air through line 27. The hot hydrogenation gases leave the combustion chamber through line 40 and, together with the residual gases from the Claus plant, flow through a line 41 to a hydrogenation reactor 42, in which the sulfur dioxide and the elemental sulfur present in the gas is hydrogenated into hydrogen sulfide.
After hydrogenation, the gas is conveyed through line 43 to a waste-heat boiler 44, where some of its heat is withdrawn.
The resulting water vapour is withdrawn through line 45. The gas is further cooled to ambient temperature in a direct cooler 47, which is supplied with gases through line 4~. The water for cooling the gas is supplied to the cooler through line 53, and the resulting hot water is conveyed through line 49 to a pump 50 and recycled to cooler 47 through a line 51 and an indirect cooler 52. Excess water produced by the condensation of water vapour from the process gases is conveyed through line 54 to deacidifier 56, where the hydrogen sulfide in the condensate is expelled and recycled.
The cooled process gases, which contain about 10 to 15 g hydrogen sulfide per Nm3, leave cooler 47, travel along 1093Z~31 line 48, and are mixed with the coke-oven gas before entering scrubber 62 and are desulfurized in the downstream scrubber.
Consequently, no waste gas escapes from the Claus plant. Since the waste gas from the Claus plant is mixed with the coke-oven gas, the calorific value of the coke-oven gas is reduced by about 2%. ~owever, this method increases the efficiency of a Claus plant to 100%, relative to sulfur. The process does not yield any waste gas or water harmful to the environment.
Claims (2)
1. A method for removing hydrogen sulfide from gases and for obtaining elemental sulfur comprising scrubbing the gases with a scrubbing solution in a hydrogen-sulfide scrubber where-by hydrogen sulfide is scrubbed out of the gases, expelling the hydrogen sulfide from the scrubbing solution in a deacidifier using water vapor, converting the hydrogen sulfide from the deacidifier in a reaction chamber to form reaction products of elemental sulfur and residual sulfur-bearing gases, hydrogenat-ing the residual sulfur-bearing gases passing from the reaction chamber to form hydrogen sulfide gas and water vapor, cooling the thus-formed hydrogen sulfide gas and water vapor to recover condensed water, supplying at least a portion of the condensed water to said deacidifier, and mixing the cooled hydrogen sul-fide gas with the gases passing into said hydrogen-sulfide scrubber.
2. The method of claim 1 wherein said first-mentioned gases comprise coke oven gas and in which hydrogen sulfide is converted to elemental sulfur in a Claus plant.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19762644617 DE2644617A1 (en) | 1976-10-02 | 1976-10-02 | METHOD FOR REMOVING SULFUR HYDROGEN FROM GASES AND FOR RECOVERING ELEMENTAL SULFUR |
| DEP2644617.3 | 1976-10-02 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1093281A true CA1093281A (en) | 1981-01-13 |
Family
ID=5989552
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA287,897A Expired CA1093281A (en) | 1976-10-02 | 1977-09-30 | Method of removing hydrogen sulfide from gases, and for obtaining elemental sulfur |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS5358994A (en) |
| BE (1) | BE859261A (en) |
| CA (1) | CA1093281A (en) |
| DE (1) | DE2644617A1 (en) |
| FR (1) | FR2366218A1 (en) |
| GB (1) | GB1533209A (en) |
| IT (1) | IT1091140B (en) |
| SE (1) | SE7710971L (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3047830A1 (en) * | 1980-12-18 | 1982-07-15 | Linde Ag, 6200 Wiesbaden | METHOD FOR CLEANING A GAS FLOW |
| DE3143400A1 (en) * | 1981-11-02 | 1983-06-01 | Mobil Oil Corp., 10017 New York, N.Y. | METHOD FOR REDUCING THE SULFUR CONTENT IN GAS FLOWS WITH ELEMENTAL SULFUR |
| GB8804728D0 (en) * | 1988-02-29 | 1988-03-30 | Shell Int Research | Process for removing h2s from gas stream |
| DE102013008852A1 (en) * | 2013-05-23 | 2014-11-27 | Linde Aktiengesellschaft | Process and apparatus for treating a sulfur-containing exhaust gas from a sulfur recovery |
-
1976
- 1976-10-02 DE DE19762644617 patent/DE2644617A1/en not_active Withdrawn
-
1977
- 1977-09-29 JP JP11617777A patent/JPS5358994A/en active Pending
- 1977-09-30 BE BE181359A patent/BE859261A/en not_active IP Right Cessation
- 1977-09-30 CA CA287,897A patent/CA1093281A/en not_active Expired
- 1977-09-30 GB GB40653/77A patent/GB1533209A/en not_active Expired
- 1977-09-30 IT IT51218/77A patent/IT1091140B/en active
- 1977-09-30 SE SE7710971A patent/SE7710971L/en unknown
- 1977-10-03 FR FR7729715A patent/FR2366218A1/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5358994A (en) | 1978-05-27 |
| DE2644617A1 (en) | 1978-04-06 |
| FR2366218A1 (en) | 1978-04-28 |
| GB1533209A (en) | 1978-11-22 |
| SE7710971L (en) | 1978-04-03 |
| IT1091140B (en) | 1985-06-26 |
| BE859261A (en) | 1978-01-16 |
| FR2366218B1 (en) | 1983-07-22 |
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Legal Events
| Date | Code | Title | Description |
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| MKEX | Expiry |