CN1137485A - Method for extracting elementary sulfur from containing H2S mixed gas - Google Patents
Method for extracting elementary sulfur from containing H2S mixed gas Download PDFInfo
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- CN1137485A CN1137485A CN 96102799 CN96102799A CN1137485A CN 1137485 A CN1137485 A CN 1137485A CN 96102799 CN96102799 CN 96102799 CN 96102799 A CN96102799 A CN 96102799A CN 1137485 A CN1137485 A CN 1137485A
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- Prior art keywords
- crouse
- waste gas
- claus plant
- gas
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- 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
-
- 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
- C01B17/0426—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 characterised by the catalytic conversion
-
- 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
- C01B17/0452—Process control; Start-up or cooling-down procedures of the Claus process
-
- 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
- C01B17/046—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 without intermediate formation of sulfur dioxide
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- 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)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Automation & Control Theory (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a method for extracting elemental sulfur (3, 9) from a mixed gas (1) containing H2S. The mixed gas (1) is firstly sent into Krause equipment (C) and desulfurated accompanying with elemental sulfur 3 generated; secondly, the sulfur compound in Krause waste gas is converted into H2S under the function of hydrogenation (H); next, the H2S in hydrogenated Krause waste gas (6) is directly catalyzed and oxidized (DO), and the elemental sulfur (9) is generated.
Description
The present invention relates to a kind of from a kind of H of containing
2Extract the method for elemental sulfur in the mixed gas of S, wherein, mixed gas at first is desulfurized and forms simultaneously elemental sulfur in a claus plant (Claus-Anlage), and its sulphur compound that also contains in Crouse's waste gas is converted into H by hydrogenization
2S, next, this hydrogenant Crouse waste gas carries out H again
2The catalytic direct oxidation of S also forms elemental sulfur.
Adopt claus plant to handle and contain H
2The mixed gas of S is well known for a long time.Claus plant is particularly suitable for handling rich H
2The gas of S.
Traditional claus plant comprises part and catalysed partial of a heat.The part of the heat in the claus plant is made up of a claus oven basically.In this claus oven, the H that contains in the raw-gas
2The part of S is burnt into SO under air fed condition
2What link to each other with the part of the heat of claus plant is a catalysed partial.If the catalysed partial of claus plant is by a plurality of, general two or ginseng catalytic Crouse's section are formed.Crouse's section of a claus plant heat extraction also comprises two or ginseng catalytic Crouse's section (i.e. two or a ginseng claus reaction device) outward, is represented as two sections or three sections claus plant usually.In catalytic Crouse's section, the SO that forms during burning
2Same H
2Claus reaction below S constitutes.
Be under the environmental stress that is becoming increasingly acute and for making every effort to further improve sulfur recovery rate, many methods that Crouse's waste gas (Claus tail gases) is handled have again been invented, although by Crouse's waste gas being handled again the volume increase that the sulfur recovery rate that improves can cause precious materials sulphur, to the further cleaning of Crouse's waste gas and the necessary expense of desulfurization considerably beyond the profit of the sulphur that increased production.
Up to the present known and can be divided into inferior point basically to the method for the significant purification of high sulfur recovery rate Crouse waste gas and reveal (Sub Dew Point) method (SDP method), circulation method (Recycle method) and direct oxidation method (Direktoxidation method).The article that the method for various purification Crouse waste gas is summarized for example has " waste-gas cleaning Technology " (" energy progress " the 6th volume second phase, 1986.6.P 84-90).As the example of direct oxidation method, the method that is exemplified has BSR/SELECTOX method, MODOP method or super Kraus process (SUPERCLAUS).The MODOP method was also done description in European patent EP-B1-0078690.
Simultaneously, publication is " from containing H
2Produce Lin De (LINDE) method of sulphur in the gas of S " (Lin Deke learns and technical report, the 64th volume, 1990.P 14-25) also disclose a kind of method (Fig. 9) of handling Crouse's waste gas by direct oxidation.Also has described CLINSULF
R-CLAUS method.In the method, one or more internal cooling reactors link to each other with claus oven and are installed on the position of claus reaction device of adiabatic operation.In addition, also can know, be used for the internal cooling reactor (CLINSULF of catalysis sulfur recovery from these publications
-reactor) can or even be lower than under the temperature of zero pour (CLINSULF-SSP method) of sulphur and using at the dew point that is lower than sulphur.
In the method for handling Crouse's waste gas, Crouse's waste gas at first is reduced or is hydrogenated in a reactor.What link to each other with hydrogenator generally is a quencher.After washing and dehydration, this waste gas is admitted to a direct oxidation reactor under the air supply condition in quencher, here, and H
2S is optionally according to the reaction formula (2) that direct oxidation was fit to is oxidized to elemental sulfur.As
Usually, the method for cited in the above processing Crouse waste gas in inferior dew point method (SDP), circulation method (Recycle) and direct oxidation method, is attached the waste gas that produces and will be sent into an after-burner after the sulfur recovery.
Verified, before direct oxidation to hydrogenation Crouse's waste gas to clean be well, but this has a shortcoming, promptly causes cost up.For carrying out hydrogenation, must in Crouse's waste gas, add a kind of hydrogenated gas, this makes sulphur compound, especially SO
2Be hydrogenated to H
2S becomes possibility.In reactor, remove sulphur compound such as SO
2Be hydrogenated to H
2Outside the S, COS and/or CS also take place simultaneously
2Hydrolysis.This causes, and in hydrogenation reactor or reduction reactor, the contained sulphur compound of all basically Crouse's waste gas all is converted to H
2S.Hydrogenated gas is produced by a device (RGG) that is called as the reducing gas producer usually.This is a kind of stove by stoichiometric operation, therein, and hydrocarbon polymer stoichiometric combustion, H simultaneously
2Be generated with CO.In the hydrogenation catalyst converter, by the CO conversion reaction, nearly all CO all generates H
2These H
2Can be used as hydrogenated gas simultaneously.
In addition, the reducing gas producer also makes mixed gas can adjust to the temperature of reaction for the needed hydrogenation catalyst converter of hydrogenation.This temperature is usually in about 280 ℃ scope.At high SO
2During content, the H in Crouse's waste gas
2/ CO should be so big, that is: make reducing gas producer band abundant inflammable gas work, so that the temperature that Crouse's waste gas is heated to is higher than the temperature of reaction of required hydrogenation catalyst converter.Thus, need additional heat exchanger that is used to regulate and control hydrogenation temperature, this is expensive on the one hand, and by this equipment the pressure-losses is increased on the other hand.
As one of two kinds of selections, except that the reducing gas producer, also can before the hydrogenation catalyst converter, locate to add H
2Produce such problem, i.e. a H thus
2Could supply to use to total equipment by pipe-line transportation when can't or only cost a lot of money usually.
The objective of the invention is to, a kind of method that starts described form is provided, this method comprises a claus plant, have Crouse's waste gas that next will purify in this equipment, sulfur recovery rate in this waste gas is at least 99%, and this method should be avoided the shortcoming of the prior art relevant with the hydrogenation of Crouse's waste gas.This method should be able to guarantee so high sulfur recovery rate when especially sulphur content fluctuates in raw-gas.In addition, it also should have the characteristics of simple and alap cost of investment of equipment and running cost.
Above-mentioned purpose will reach in the following manner, and promptly claus plant is pressed stoichiometric operation, and H in Crouse's waste gas
2The same SO of S
2Ratio between 3: 1 and 15: 1.
Wonderful discovery, although claus plant strictly also makes the sulphur productive rate of claus plant descend several percentage points by stoichiometric operation thus, the productive rate of this claus plant reduces and can be remedied by direct oxidation equipment.At H
2S and SO
2Ratio is as being 10: 1 o'clock, and the output of claus plant for example descends 2%.H in Crouse's waste gas
2The same SO of S
2This ratio be equivalent to leave H behind the claus oven basically approximately
2The same SO of S
2Ratio.In strict accordance with stoichiometric operation, want reductive sulfide just to significantly reduce by claus plant in Crouse's waste gas.Thus, the amount for the required hydrogenated gas of hydrogenation greatly reduces.With the method that the present invention proposes, therefore a reducing gas producer can provide required H without a doubt
2(direct or CO conversion) and the required heat of hydrogenation catalyst converter.In the method for the invention, do not exist and produce the too danger of high calorie.
Can adopt a kind of in most known Crouse's catalyst converters as the catalyst converter in the claus reaction device.With air or O
2Be transported in Crouse's section of heat, can regulate like this by an air dosage analysis device (ADL), promptly according to H in Crouse's waste gas of the present invention
2The same SO of S
2Ratio between 3: 1 and 15: 1.As preferred implementation of the present invention, H
2The same SO of S
2Ratio between 4: 1 and 12: 1, be preferably between 7: 1 and 11: 1.
The gas of extracting out from catalytic Crouse's section separates with elemental sulfur in a sulfur condenser.Crouse's waste gas of claus plant mixes with a kind of reducing gas and is admitted to hydrogenation reactor.Remove sulphur compound such as SO
2Be hydrogenated to H
2Outside the S, in reactor, also take place simultaneously COS and/CS
2Hydrolysis.This causes, and in hydrogenation reactor, in fact all contained sulphur compounds all have been converted to H in Crouse's waste gas
2S.As being used for sulphur compound hydrogenation and being hydrolyzed into H simultaneously
2The catalyst converter of S can adopt the catalyst converter of knowing.Especially the catalyst converter of Shi Heing is, contains those of cobalt and molybdenum.The catalyst converter of such kind for example, was disclosed by the BSR/SELECTOX method.After the hydrogenation, the major part of contained reaction water will be removed by cooling in Crouse's waste gas.
After these reaction water remove from hydrogenant Crouse waste gas, this Crouse's waste gas will mix with air or oxygen in a direct oxidation reactor and be converted to elemental sulfur by reaction formula (2).Wherein, H
2S/O
2Ratio was readjusted before entering the direct oxidation reactor by air dosage analysis device (Air DemandAnalyser) and by adding air or oxygen.For making H
2S becomes elemental sulfur by direct catalyzed oxidation, and all are known is used for this purpose catalyst converter and all can adopts.The result shows that those contain the TiO as active constituent
2Catalyst converter especially suitable for direct oxidation.For example, the catalyst converter of such kind was disclosed by European patent EP-B1-0078690.
The gas that comes out from the sulphur water cooler that is connected on the reactor back that is used for direct catalyzed oxidation, always also contain a spot of sulphur compound, therefore preferably these gases are carried out reignition, guarantee that thus still the sulphur component that contains of trace changed into and compares H in these waste gas before they are devoted in the atmosphere
2The SO that the S smell is more weak
2
The method that the present invention proposes also can adopt and be used for the claus plant that repeats to extract.An a kind of typical yields of two-section type claus plant is about 90-94%.After in the direct oxidation equipment that connects, about 90-96% of residue sulphur can be transformed.In this example, reduce although the method that the present invention proposes causes the productive rate of claus plant, in total method, sulfur recovery rate still can reach 99.0-99.6%.
If adopt a kind of internal cooling formula reactor as the direct oxidation reactor, will have advantage especially.Thus, make a temperature control accurately of direct oxidation reactor become possibility.In the reactor of adiabatic operation, in fact the temperature in the direct oxidation reactor is subjected to the very exothermic influence of the oxidizing reaction of carrying out according to reaction formula (2), and its temperature control is only by regulating the air or the O of Crouse's waste gas and/or adding
2Temperature determine that and internal cooling reactor makes and realizes that at this inside reactor temperature regulation and a control accurately becomes possibility.Especially on flow direction, can adjust a temperature section.The direct oxidation reactor also has last refrigerative catalyst stream in it becomes a mandarin the district, therefore, this reactor that is used for direct catalyzed oxidation is furnished with the catalyst converter device of an adiabatic operation on its flow direction.Wherein, the catalyzer that this adiabatic device comprises should be lower than 50% of catalyst volume content total in the direct oxidation reactor, preferably between 15-30%.
In the method that the present invention points out, its overall yield even can be enhanced astoundingly.Because claus plant, especially in refinery, often be under the state of Primordial Qi concentration surging, and in the method for the invention because the system that is made up of the direct oxidation equipment of claus plant and band internal cooling reactor is very little to the productive rate response fluctuation of claus plant, therefore this system is better than traditional equipment on its average, long term income, because discharge has reduced.Have the direct oxidation equipment of internal cooling reactor and the high-content H in Crouse's waste gas
2The S reaction, if the rate of recovery height of sulphur is the H in Crouse's waste gas
2It is also like this when S content is lower than about 7% content.A kind of H of a kind of typical Crouse's waste gas of claus plant of multistage
2S content is 1-2%.In the single hop claus plant, H
2The content of S is about 4-6%.Therefore, for method of the present invention, the claus plant of single hop also is fit to well.
Strictness according to the invention by claus plant is by the mode of stoichiometric operation, and sulfur recovery rate reduces 1.2-4%, therefore, and H in Crouse's waste gas
2S content is brought up to 5-7%.Simultaneously, have sulfur recovery rate in the direct oxidation equipment of internal cooling reactor and improve approximately 1%, therefore, sulfur recovery rate can be enhanced generally.
With reference to following Example, this point can be clearer and more definite.A kind of traditional method (optimum yields of claus plant) and a kind of method of moving by mode of the present invention have been listed in contrast in the table 1.What they adopted separately is a kind of a kind of single hop claus plant that has the direct oxidation of the Crouse's waste gas in an inner cooling reactor.
| Table 1: | Prior art | The present invention |
| H in the claus plant 2S is to SO 2Ratio | 2∶1 | 10∶1 |
| Sulfur recovery rate (claus plant) | 90％ | 87％ |
| Sulfur recovery rate (direct oxidation reaction) | 92％ | 96％ |
| Total sulfur recovery rate | 99.2％ | 99.48％ |
By described effect, the fluctuation of Crouse's raw-gas is able to balance, otherwise this fluctuation can cause the reduction of the productive rate of sulphur.
As expansion of the present invention, H in Crouse's waste gas
2S is to SO
2Ratio be at least 4: 1 o'clock, Crouse's waste gas does not need hydrogenation and directly is admitted to direct oxidation (reactor).When this situation is particularly suitable for after the two-part claus plant of kind below, that is, and when Crouse's raw-gas contains 90% H approximately
2During S, even they are at H
2S is also to reach one 90% sulfur recovery rate at 10: 1 o'clock to the ratio of SO2.COS that may exist and/or CS
2Can be without a doubt by catalytic conversion in the direct oxidation reactor by hydrolytic action.
In the method for the invention, the dehydration of the Crouse's waste gas after the claus plant can be cancelled.
Not only when Crouse's waste gas does not need hydrogenation and delivers to direct oxidation (reactor); And as the required H of hydrogenation
2When in claus plant, producing, reducing gas producer and/or reducing gas such as H
2Adding also can cancel.Especially when in claus oven, supplying with pure O
2The time, this situation is possible.Therefore, in claus oven among a small circle in, remove H
2A S part is oxidized to SO
2Also cause H outward,
2S directly changes into elemental sulfur and H
2
The invention will be further described below with reference to embodiment.
Fig. 1 a: sketch of method of the present invention.
A kind of 80 volume % H that for example contain
2The sour gas of S as Crouse's Primordial Qi, is admitted to claus plant C by pipeline 1.Air or oxygen is admitted to claus plant C by pipeline 2, and imports in the claus oven with the Crouse's Primordial Qi from pipeline 1.According to the present invention, in claus oven, the H that sour gas 1 is contained
2The part of S generates SO in strict accordance with stoichiometric(al) combustion
2This claus plant C also comprises one or two catalytic Crouse's sections.The elemental sulfur that extracts in claus plant C is condensed, and is taken away by pipeline 3.
Crouse's waste gas in the pipeline 4 is transfused to hydrogenation (device) H.Air dosage analysis device A measures H in Crouse's waste gas 4
2S is to SO
2Ratio.Air dosage analysis device A also bears air or O
2By pipeline 2 input claus ovens.Perhaps can be with H
2As reducing gas, mix with Crouse's waste gas by pipeline 4 before in hydrogenation (H).Should be by H
2The mixed gas of forming with Crouse's waste gas will be transfused to hydrogenation reactor, and at this, the compound of sulphur mainly is SO
2Hydrogenation takes place and be transformed into H
2S.If also contain COS and/or CS in Crouse's waste gas 4
2, so, they will be transformed into H simultaneously by hydrolysis reaction
2S.
Hydrogenation in the pipeline 6 Crouse's waste gas, after cooling and dehydration, with the air that is suitable for the direct oxidation amount or the O that measure by stoichiometry by air dosage analysis device A
2Mix by pipeline 7, and be input in the reactor DO of direct catalyzed oxidation.The direct oxidation reactor for example supplies water with pump house and directly cools off, and wherein, the top temperature of inside reactor should be adjusted to and be lower than 300 ℃, for example 290 ℃.And the reactor outlet temperature should be transferred to 230 ℃.The mixed gas that from the direct oxidation reactor, comes out will be in direct oxidation equipment DO with sulphur content from.The elemental sulfur that condensation goes out is taken away by pipeline 9.In the direct oxidation reactor, contained more than 90% of residue sulphur of Crouse's waste gas in the pipeline 6 is converted into elemental sulfur as 95%, and is recovered by pipeline 9.The Crouse's waste gas that separates with elemental sulfur will be drawn towards a for example unshowned after-burner by pipeline 8.
With method shown in Figure 1, according to long-term average result, generally, the 99.0-99.6% of 1 sulfur-bearing of sour gas is recovered with the form of elemental sulfur (3,9).
Claims (9)
1, from a kind of H that contains
2Extract the method for elemental sulfur in the mixed gas of S (1), wherein, mixed gas (1) at first carries out desulfurization and makes elemental sulfur (3) in a claus plant (C), then, contained sulphur compound borrows hydrogenization (H) to be converted to H in Crouse's waste gas (4)
2S, next, the Crouse's waste gas (6) that is hydrogenated carries out H
2The direct catalyzed oxidation (DO) of S is characterized in that to make elemental sulfur claus plant (C) will be operated by stoichiometric, and H in Crouse's waste gas
2S and SO
2Ratio between 3: 1 and 15: 1.
2, in accordance with the method for claim 1, it is characterized in that H in Crouse's waste gas (4)
2S and SO
2Ratio between 4: 1 and 12: 1, preferably between 7: 1 and 11: 1.
According to each described method of claim 1 or 2, it is characterized in that 3, directly catalyzed oxidation (DO) is to carry out in an inner colded reactor.
According to each described method of claim 1 to 3, it is characterized in that 4, claus plant comprises one-level just on catalysis progression.
5, according to each described method of claim 1 to 4, it is characterized in that H in Crouse's waste gas (4)
2S and SO
2Ratio be at least 4: 1 o'clock, this Crouse's waste gas (4) can not hydrogenation and directly carry out direct oxidation reaction (DO).
6, according to each described method of claim 1 to 5, it is characterized in that the dehydration cancellation of claus plant (C) Crouse's waste gas (4) afterwards.
7, according to claim 1,2,3, each described method of 6 and especially 5, it is characterized in that claus plant (C) should comprise multistage, preferably two-stage catalysis.
8, according to each described method of claim 1 to 7, it is characterized in that, for the required H of hydrogenation
2Can in claus plant, produce.
According to each described method of claim 1 to 8, it is characterized in that 9, by the stoichiometric operation of pressing of claus plant (C), the fluctuation of Crouse's raw-gas (1) does not cause the reduction of the productive rate of sulphur, and held stationary.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19510915.5 | 1995-03-24 | ||
| DE1995110915 DE19510915A1 (en) | 1995-03-24 | 1995-03-24 | Sulphur@ recovery from waste gas from Claus plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1137485A true CN1137485A (en) | 1996-12-11 |
Family
ID=7757696
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96102799 Pending CN1137485A (en) | 1995-03-24 | 1996-03-25 | Method for extracting elementary sulfur from containing H2S mixed gas |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN1137485A (en) |
| DE (1) | DE19510915A1 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101659400B (en) * | 2009-09-11 | 2011-02-16 | 山东迅达化工集团有限公司 | Catalyst combination process of sulfur recovering device |
| CN102556977A (en) * | 2010-12-30 | 2012-07-11 | 中国石油天然气股份有限公司 | Inner-cooling type direct oxidation sulfur recovery method and device |
| CN102847421A (en) * | 2012-09-24 | 2013-01-02 | 邵志辉 | Multistage oxidation reduction reactor |
| CN103359690A (en) * | 2012-04-03 | 2013-10-23 | 林德股份公司 | Method and apparatus for obtaining sulphur |
| CN103979500A (en) * | 2014-05-21 | 2014-08-13 | 中国石油集团工程设计有限责任公司 | Sulfur recovery and tail gas treatment system and technology for comprehensive hydrogen production |
| CN104524968A (en) * | 2014-12-16 | 2015-04-22 | 杨楠 | Claus tail gas deep purification catalytic reduction oxidation process and catalyst used by claus tail gas deep purification catalytic reduction oxidation process |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1186571A1 (en) * | 2000-09-12 | 2002-03-13 | Gastec N.V. | Process for the selective oxidation of hydrogen sulphide to elemental sulphur |
| EP1295848A1 (en) * | 2000-09-12 | 2003-03-26 | Gastec N.V. | Process for the selective oxidation of hydrogen sulphide to elemental sulphur |
| DE102010004062A1 (en) | 2010-01-05 | 2011-07-07 | Sterzel, Hans-Josef, Dr., 67125 | Sulfur made from the Claus process comprising elevated portions of polysulfanes and hydrogen sulfide, useful as heat transfer- and heat storage-liquid |
| ES2746552T3 (en) * | 2014-12-24 | 2020-03-06 | Axens | Removal of hydrogen sulfide and recovery of sulfur from a gas stream by direct catalytic oxidation and Claus reaction |
| US10195565B2 (en) | 2014-12-24 | 2019-02-05 | Prosernat | Removal of hydrogen sulfide and sulfur recovery from a gas stream by catalytic direct oxidation and claus reaction |
-
1995
- 1995-03-24 DE DE1995110915 patent/DE19510915A1/en not_active Withdrawn
-
1996
- 1996-03-25 CN CN 96102799 patent/CN1137485A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101659400B (en) * | 2009-09-11 | 2011-02-16 | 山东迅达化工集团有限公司 | Catalyst combination process of sulfur recovering device |
| CN102556977A (en) * | 2010-12-30 | 2012-07-11 | 中国石油天然气股份有限公司 | Inner-cooling type direct oxidation sulfur recovery method and device |
| CN102556977B (en) * | 2010-12-30 | 2013-12-04 | 中国石油天然气股份有限公司 | Inner-cooling type direct oxidation sulfur recovery method and device |
| CN103359690A (en) * | 2012-04-03 | 2013-10-23 | 林德股份公司 | Method and apparatus for obtaining sulphur |
| CN102847421A (en) * | 2012-09-24 | 2013-01-02 | 邵志辉 | Multistage oxidation reduction reactor |
| CN103979500A (en) * | 2014-05-21 | 2014-08-13 | 中国石油集团工程设计有限责任公司 | Sulfur recovery and tail gas treatment system and technology for comprehensive hydrogen production |
| CN103979500B (en) * | 2014-05-21 | 2015-09-09 | 中国石油集团工程设计有限责任公司 | The sulphur recovery of comprehensive hydrogen manufacturing and exhaust treatment system and technique |
| CN104524968A (en) * | 2014-12-16 | 2015-04-22 | 杨楠 | Claus tail gas deep purification catalytic reduction oxidation process and catalyst used by claus tail gas deep purification catalytic reduction oxidation process |
Also Published As
| Publication number | Publication date |
|---|---|
| DE19510915A1 (en) | 1996-09-26 |
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