CN1088391C - Technological process for making gas desulfurization by adopting liquid-phase catalytic oxidation method and its equipment - Google Patents
Technological process for making gas desulfurization by adopting liquid-phase catalytic oxidation method and its equipment Download PDFInfo
- Publication number
- CN1088391C CN1088391C CN98114036A CN98114036A CN1088391C CN 1088391 C CN1088391 C CN 1088391C CN 98114036 A CN98114036 A CN 98114036A CN 98114036 A CN98114036 A CN 98114036A CN 1088391 C CN1088391 C CN 1088391C
- Authority
- CN
- China
- Prior art keywords
- gas
- desulfurizing tower
- tower
- desulfurizing
- carry out
- 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.)
- Ceased
Links
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 23
- 230000003647 oxidation Effects 0.000 title claims abstract description 21
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 19
- 239000007791 liquid phase Substances 0.000 title claims abstract description 16
- 238000006477 desulfuration reaction Methods 0.000 title claims description 36
- 230000023556 desulfurization Effects 0.000 title claims description 36
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 55
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 47
- 230000008929 regeneration Effects 0.000 claims abstract description 39
- 238000011069 regeneration method Methods 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 239000006260 foam Substances 0.000 claims abstract description 22
- 238000005406 washing Methods 0.000 claims abstract description 16
- 230000003068 static effect Effects 0.000 claims abstract description 13
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 13
- 239000011593 sulfur Substances 0.000 claims abstract description 13
- 238000002844 melting Methods 0.000 claims abstract description 10
- 230000008018 melting Effects 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 58
- 239000005864 Sulphur Substances 0.000 claims description 34
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 18
- -1 hydrogen sulfide sulfides Chemical class 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 230000011218 segmentation Effects 0.000 claims description 6
- 238000004134 energy conservation Methods 0.000 claims description 5
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 abstract description 7
- 239000000243 solution Substances 0.000 description 42
- 238000005516 engineering process Methods 0.000 description 17
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000002156 mixing Methods 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 239000006071 cream Substances 0.000 description 4
- 238000005188 flotation Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 241000282326 Felis catus Species 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- NINIDFKCEFEMDL-NJFSPNSNSA-N Sulfur-34 Chemical compound [34S] NINIDFKCEFEMDL-NJFSPNSNSA-N 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 1
- HYHCSLBZRBJJCH-UHFFFAOYSA-N sodium polysulfide Chemical compound [Na+].S HYHCSLBZRBJJCH-UHFFFAOYSA-N 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention relates to a technological method and an apparatus for desulfurizing sulfur-bearing gas by adopting a liquid-phase catalytic oxidation method. The sulfur-bearing gas is fed into the lower end of the washing section of a desulfurizing tower, desulfurizing liquid is sprinkled on the upper end of the desulfurizing tower, and the desulfurized gas is discharged out of the tower from the upper end. The desulfurizing liquid can be regenerated by a small-size high-efficiency and energy-saving static mixer at the regeneration section of the desulfurizing tower, and then the regenerated desulfurizing liquid is delivered into the upper end of the washing section of the desulfurizing tower by a circulating pump. For a large-size gas desulfurizing apparatus, the heat exchanger or the sulfur foam concentrator or the continuous sulfur melting facility, etc. of the desulfurizing liquid can be attached to the desulfurizing tower. The gas capable of being discharged after reaching the standard is desulfurized, the washing section and the regenerating section of the desulfurizing tower can be combined, and the circulating pump of the desulfurizing liquid is cancelled.
Description
The present invention is a kind of process and the device that adopts liquid phase catalytic oxidation to carry out desulfurization to the gas that contains the hydrogen sulfide sulfides.This technology belongs to the desulfur technology field.
With the gas that contains the hydrogen sulfide sulfides is adopted liquid phase catalytic oxidation carry out desulfurization be example typical process flow as shown in Figure 1.It is absorbent that liquid phase catalytic oxidation is selected weakly alkaline solution usually for use, adds oxygen carrier in the solution and plays catalytic action, changes into NaHS or sodium polysulfide with this hydrogen sulfide that is absorbed in the gas after reaction, and then is reoxidised into sulphur solution is regenerated.The gas 1 that contains the hydrogen sulfide sulfides enters the bottom of desulfurizing tower 2, from cat head spray doctor solution 3 to absorb hydrogen sulfide the gas etc.Gas 4 after the desulfurization leaves desulfurizing tower 2 from the top of tower.The doctor solution that has absorbed hydrogen sulfide goes out from tower bottom flow, enters reactive tank 6 through desulfurizing tower liquid seal trough 5.Reacted doctor solution is sent into regenerator 9 by circulating pump 7 pressurization and after heat exchanger 8 heating or cooling, with send into simultaneously at the bottom of the tower compressed air 10 from bottom to top and flow catalytic oxidation regeneration.Doctor solution after the regeneration is flowed out by the top of regenerator, returns desulfurizing tower through liquid level regulator 11 and recycles.The sulphur foam that regenerator 9 generates overflows the back from flowing into sulphur foam tank 12 from cat head, and the clear liquid 13 after the separation returns regenerative system, concentrates the sulphur cream that obtains through sulphur foam tank 12 and can get product sulphur 15 behind sulphur equipment 14 heating and meltings, and clear liquid 16 returns regenerative system.This flow process has that unit operating equipment is many, and floor space is big, construction investment height, power cost height, shortcoming such as secondary pollution is bigger.
Aspect the improvement of solution regeneration, the existing jet regeneration tank that adopts replaces regenerator.The doctor solution that enters reactive tank after the desulfurization is pumped into jet regeneration tank with rich solution, and regeneration utilizes the doctor solution injection and sucks through injector with air.Lean solution after the regeneration is removed the lean solution medial launder through liquid level regulator, returns desulfurizing tower by lean pump force feed doctor solution after heat exchanger heating or cooling.This flow process has to be utilized short jet regeneration tank to replace high regenerator, not to need to send with air compressor machine advantage such as air, but will set up equipment such as sulphur foam pump, rich solution pump and lean solution medial launder.
The object of the present invention is to provide the process and the device of the high gas sweetening of a kind of unit operations integrated level.This method adopts collection desulfurization and the gas sweetening equipment that is regenerated as one, and technological process is simple, and equipment is few, and floor space is little, saves construction investment, reduces power consumption, and secondary pollution is little; And when needs carry out desulfurization to big flow gas, be easier to satisfy production requirement to large-scale gas sweetening equipment high efficiencyization.
The objective of the invention is to realize by following method and apparatus.
A kind of process that adopts liquid phase catalytic oxidation to carry out desulfurization to the gas that contains the hydrogen sulfide sulfides, be after sulfurous gas is sent into desulfurizing tower, sulfide is absorbed by doctor solution in the tower, gas goes out tower from cat head after the desulfurization, the desulfurization rich solution recycles behind the oxidation regeneration in this tower, and it is characterized in that looking on desulfurizing tower it needs segmentation to carry out or the regeneration of gas scrubbing desulfurization and doctor solution is carried out in not segmentation.
The present invention can adopt according to actual conditionses such as places and the sulphur foam be concentrated or facility such as continuous sulfur melting is attached to process on the desulfurizing tower.
For realizing above-mentioned process, the inventive system comprises desulphurization plant, sulphur foam concentrator, equipment such as the heat exchange of molten sulphur equipment and fluid and pressurized delivered is characterized in that looking it and need have that sectional carries out or the desulfurizing tower of gas scrubbing desulfurization and desulfurization regeneration is carried out in not segmentation on desulfurizing tower.
Device of the present invention also can adopt helping oxygen supply gas or being desulfurized gas dispersion is carried out GAS ABSORPTION reaction in liquid phase static mixer of energy-conservationization, small-sized efficientization in desulfurizing tower.
Device of the present invention also can adopt according to actual conditionses such as places and the sulphur foam be concentrated or facility such as continuous sulfur melting is attached on the desulfurizing tower.
Method and apparatus of the present invention has the following advantages and good effect:
1. integrated, the high efficiency of desulfurizer.Realized the integrated of the washing of gas sweetening and desulfurization regeneration equipment, also can further the heat exchange facility of doctor solution, the enrichment facility of sulphur foam or the molten sulphur facility in borderland of small-sized efficientization be attached on the big large desulfurization tower for the treatment of capacity.Therefore, can simplify technological process, reduce process equipment, dwindle floor space, save construction investment, thereby can diffuse the secondary pollution of emission point minimizing by minimizing equipment, and when needs carry out desulfurization to big flow gas, be easier to satisfy production requirement large-scale gas sweetening unit high efficiency to atmosphere.
2. cut down the consumption of energy.When in desulfurizing tower, adopt help the GAS ABSORPTION reaction, energy-conservation, efficiently during static mixer, the regenerator technology of more former employing, because of the liquid level of its regenerative sulfur binding liquid far below liquid level corresponding in the former technology, so can significantly reduce the compressed-air actuated energy consumption of sending into the desulfurization regeneration device bottom; Also more former employing has the energy consumption of jet regeneration tank technology of more high-lift rich solution pump low.
Below in conjunction with accompanying drawing the present invention is described in further detail.
Fig. 1 is the production technology sketch of prior art;
Fig. 2 is for adopting a routine sketch of production technology of the present invention;
Fig. 3 is for adopting another routine sketch of production technology of the present invention.
As shown in Figure 2: send into from the lower end that is positioned at desulfurizing tower 17 upper wash sections 18 contain the hydrogen sulfide sulfides be desulfurized gas 19, the upper end spray doctor solution 20 of washing section 18 is to absorb the sulfide in the gas 19.The gas 21 that is desulfurized after the washing leaves desulfurizing tower 17 from the upper end of washing section 18.The bottom of washing section 18 can have the function of reactive tank 6 in the former process unit and be provided with fluid-tight facility 22.The regenerator section 23 that the desulfurization rich solution that has absorbed sulfide enters desulfurizing tower 17 bottoms by these fluid-tight facility 22 gravity flows.The desulfurization rich solution can adopt the different oxidation flotation regenerations that contacts with oxygen-containing gas.For example, when the gas-liquid static mixer 24 that adopts energy-conservation small-sized efficientization makes the desulfurization rich solution obtain regeneration, the desulfurization rich solution flows automatically into the bottom of the static mixing parts 25 of static blender 24, enters static mixing parts 25 from bottom to top with the oxygen supply gas 26 of sending into this place simultaneously and flows catalytic oxidation regeneration.Static mixing parts 25 can adopt single-piece according to the requirement of production technology, also can use by many serial or parallel connections.After desulfurization injection after the regeneration is flowed out by the top of static mixing parts 25, can flow automatically to the bottom cycle regeneration of static mixer downwards along the periphery of static mixing parts 25.When adopting even bubbling regeneration, the fluid-tight facility of desulfurization rich solution through the washing section bottom flows automatically to the regenerator section of desulfurizing tower downwards, and with the oxygen-containing gas catalytic oxidation regeneration of sending into regenerator section simultaneously; When adopting the jet regeneration mode, the desulfurization rich solution can adopt through rich solution and be pumped into the regenerator section that can utilize doctor solution injection face to suck with air regeneration that is furnished with injector; The desulfurization rich solution also can adopt the regeneration of forced ventilation flotation such as dumped packing, ripple packing, disperser.Regenerator section 23 can be taked different liquid levels to detect and regulate facility 27 its liquid levels of control.Weary gas 28 after the participation desulfurization rich solution oxidation reaction leaves regenerator section voluntarily and effluxes, in case of necessity row discharging more after treatment.The sulphur foam 29 that the regeneration flotation generates is processed processing from delivering to the independent sulphur foam concentrator that is provided with 12 identical with former technology after regeneration facility napex overflows with molten magnetic sulphur equipment 14, and this is no longer given unnecessary details.If adopt the large desulfurization device, sulphur foam enrichment facility or molten sulfur facility can not put with the desulfurizing tower merging.Like this, the sulphur foam that generates through the regeneration flotation can flow into sulphur foam enrichment facility 30 certainly, the sulphur cream 31 that obtains after the sulphur foam solution concentrates is sent into the continuous sulfur melting facility 33 of the small-sized efficientization that hangs on the desulfurizing tower wall by pump 32, can get product sulphur 34 behind the heating and melting.Lean solution 37 after the clear liquid 35 that molten sulphur equipment is discharged, sulphur foam enrichment facility 30 isolated doctor solutions 36 and the regeneration of desulfurization rich solution can be recycled by washing section 18 upper ends of sending into desulfurizing tower 17 after circulating pump 38 pressurizations again in the lump.The heat exchange facility 39 of doctor solution can independently be provided with, and also can be attached to desulfurizing tower to the large desulfurization device.
For collection desulfurization and the desulfurizing tower 17 that is regenerated as one, also regenerator section 23 can be arranged in the top of desulfurizing tower 17, the bottom is the washing section 18 of desulfurizing tower 17.There is storage liquid function the bottom of washing section 18 and is provided with liquid seal device 22.The layout of other facility and above-mentioned technology are basic identical.When the enrichment facility 30 of sulphur foam is high-order when arranging and can satisfy the pressure needs of the gravity flow of sulphur cream and molten sulphur, can cancel the sulphur cream pressurized delivered pump 32 before the molten sulphur equipment.
For the waste gas that contains hydrogen sulfide 19 that discharges in the production process, when it just is discharged after desulfurization reaches environment protectment protection, above-mentioned technological process can be simplified, the function that is about to the washing section 18 of above flow process desulfurizing tower 17 is incorporated in regenerator section 23.As shown in Figure 3, can send into simultaneously from the bottom of desulfurizing tower 17 contain the hydrogen sulfide sulfides be desulfurized gas 19 and regeneration air 26, washing, purifying be desulfurized gas 19 and participate in doctor solution 20 oxidation reactions after the mist 28 of the weary gas of regeneration can efflux voluntarily from the top of desulfurizing tower 17, can efflux after treatment in case of necessity.The collection of the oxidation regeneration of doctor solution 20, sulphur foam 29 concentrates, the production of molten sulfur 34 etc. is basic identical with above-mentioned technological process.Adopt this flow process to have and can utilize shorter desulfurizing tower 17, and can adopt intermittently used low discharge doctor solution delivery pump 40 to replace the doctor solution circulation spring 38 of aforementioned flow process, this pump 40 mainly is used as carries sulphur foam enrichment facility 30 isolated doctor solutions 36.
The main distinction of method and apparatus of the present invention and former technology have following some:
1. the equipment of the desulfurization of process of desulfurizing gases and regenerating section has been realized integrated.
The desulfurization of former process unit and regenerating section contain equipment such as desulfurizing tower 2, liquid seal trough 5, reactive tank 6, regenerator (groove) 9.
Technology of the present invention is integrated into a desulfurizing tower 17 with the multiple devices of former process unit desulfurization and regenerating section.
2. can adopt gas-liquid mixed parts 25 energy-conservation, small-sized efficientization in the part that desulfurizing tower plays palingenesis.
The reclaim equiment of former process unit has adopted reclaim equiments such as the regenerator 9 of even bubble type or jet regeneration tank.
The regeneration facility 23 of technology of the present invention still can adopt to have static mixers 24 energy-conservation, the small-sized efficient characteristics except that can adopting modes such as the even bubbling regeneration that is similar to former technology or jet regeneration.
3. can be attached on the desulfurizing tower 17 of technology of the present invention according to the equipment such as continuous sulfur melting 14 of actual conditionses such as place for large-scale gas sweetening unit doctor solution heat exchange 8, sulphur foam concentrated 12 or the small-sized efficient of former technology.
Claims (8)
1. process that adopts liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides, be after sulfurous gas (19) is sent into desulfurizing tower (17), sulfide is absorbed by doctor solution in the tower (20), gas after the desulfurization (21) ejects tower from tower (17), the desulfurization rich solution recycles behind the oxidation regeneration in this tower (17), and it is characterized in that looking on desulfurizing tower (17) it needs segmentation (18,23) to carry out or the regeneration of gas (19) washing desulphurization and doctor solution (20) is carried out in not segmentation.
2. a kind of process that adopts liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides according to claim 1 is characterized in that adopting the process that sulphur foam enrichment facility (30) is attached to desulfurizing tower (17).
3. a kind of process that adopts liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides according to claim 1 and 2 is characterized in that adopting the process that continuous sulfur melting facility (33) is attached to desulfurizing tower (17).
4. one kind is used the described process of claim 1 and the custom-designed process unit that adopts liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides, it is characterized in that adopting sectional (18,23) to carry out or desulfurizing tower (17) that gas (19) washing desulphurization liquid (20) regeneration is carried out in not segmentation.
5. a kind of process unit that adopts liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides according to claim 4 is characterized in that adopting in desulfurizing tower (17) energy-conservation the helping oxygen supply gas (26) or be desulfurized gas (19) of small-sized efficient to be dispersed in the static mixer (24) that carries out the GAS ABSORPTION reaction in the liquid phase.
6. according to claim 4 or 5 described a kind of process units that adopt liquid catalytic to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides, it is characterized in that and sulphur foam enrichment facility (30) can be attached to desulfurizing tower (17).
7. according to claim 4 or 5 described a kind of process units that adopt liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides, it is characterized in that continuous sulfur melting facility (33) being attached to desulfurizing tower (17).
8. a kind of process unit that adopts liquid phase catalytic oxidation to carry out gas sweetening to the gas that contains the hydrogen sulfide sulfides according to claim 6 is characterized in that continuous sulfur melting facility (33) being attached to desulfurizing tower (17).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98114036A CN1088391C (en) | 1998-06-02 | 1998-06-02 | Technological process for making gas desulfurization by adopting liquid-phase catalytic oxidation method and its equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98114036A CN1088391C (en) | 1998-06-02 | 1998-06-02 | Technological process for making gas desulfurization by adopting liquid-phase catalytic oxidation method and its equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1237474A CN1237474A (en) | 1999-12-08 |
| CN1088391C true CN1088391C (en) | 2002-07-31 |
Family
ID=5223718
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98114036A Ceased CN1088391C (en) | 1998-06-02 | 1998-06-02 | Technological process for making gas desulfurization by adopting liquid-phase catalytic oxidation method and its equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1088391C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101597522B (en) * | 2009-06-29 | 2011-02-23 | 朱春阳 | Desulfuration processing method of coke oven gas and special device thereof |
| CN101987976B (en) * | 2009-07-30 | 2013-06-26 | 鞍钢集团工程技术有限公司 | Desulfurizing tower for gas desulfuration by using liquid phase catalytic oxidation |
| CN102115044B (en) * | 2011-01-24 | 2013-03-06 | 江苏中显集团有限公司 | Device for preparing sulfur dioxide by directly burning raw sulfur |
| CN106000094A (en) * | 2016-08-01 | 2016-10-12 | 江苏揽山环境科技股份有限公司 | Desulfurization reaction tower and desulfurization process |
| CN111001294A (en) * | 2019-12-17 | 2020-04-14 | 西安润川环保科技有限公司 | Energy-saving regeneration process method used in wet oxidation desulfurization process |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0781832A1 (en) * | 1995-12-27 | 1997-07-02 | Institut Francais Du Petrole | Process for the complete treatment of natural gas on a production site |
-
1998
- 1998-06-02 CN CN98114036A patent/CN1088391C/en not_active Ceased
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0781832A1 (en) * | 1995-12-27 | 1997-07-02 | Institut Francais Du Petrole | Process for the complete treatment of natural gas on a production site |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1237474A (en) | 1999-12-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201832555U (en) | Optimized two-circulating flue gas dust removal and desulfurization device | |
| CN1007963B (en) | Installation for wet-removal of sulphur from flue gas | |
| CN108686485A (en) | A kind of reproducible efficient suspension bed desulfurization technique | |
| CN108686474A (en) | A kind of high-efficiency desulfurization and regeneration integral system using suspension bed | |
| CN108686489A (en) | A kind of suspension bed wet desulfurizing process | |
| JPS62183835A (en) | Method and device for desulfurizing gas containing hydrogen sulfide | |
| CN1088391C (en) | Technological process for making gas desulfurization by adopting liquid-phase catalytic oxidation method and its equipment | |
| CN105664693A (en) | Sulfuric acid tail gas desulphurization apparatus by oxidation process and usage method thereof | |
| CN202270473U (en) | Carbon black tail gas desulfurization device | |
| CN201832552U (en) | Dual-alkali sintering flue gas desulfurization device | |
| CN201214046Y (en) | Ammonia process desulphurizing device for reducing ammonia escape | |
| CN104190221A (en) | Desulphurization method, device and system for acid gas containing H2S, COS, CS2 and other gases | |
| CN2825082Y (en) | Double-circulating double-alkali processed wet type desulfurization device | |
| CN209352837U (en) | Integral biological desulfurizer | |
| CN205868002U (en) | Flue gas desulfurization reaction tower | |
| CN214426458U (en) | Blast furnace gas desulfurization system | |
| CN208049710U (en) | A kind of tower Complexing Iron desulfurizer and Complexing Iron desulphurization system | |
| CN203229500U (en) | Desulfurizing liquid cyclic regeneration slot | |
| CN101596399B (en) | Self-suction oxidation desulfuration process and device thereof | |
| CN109022049A (en) | A kind of desulfurization device and method for removing hydrogen sulfide in coal gas integrated with regeneration | |
| CN108744943A (en) | A kind of desulphurization plant and its sulfur removal technology | |
| CN201015726Y (en) | Segmented sodium calcium double alkali desulfurization device | |
| CN208642304U (en) | A kind of desulphurization plant | |
| CN107805525A (en) | A kind of desulphurization system and its sulfur method suitable for methane purification | |
| CN106000094A (en) | Desulfurization reaction tower and desulfurization process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: ANSTEEL ENGINEERING TECHNOLOGY CORPORATION LIMITED Free format text: FORMER OWNER: ANSHAN STEEL COMPANY LIMITED Effective date: 20110927 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 114001 ANSHAN, LIAONING PROVINCE TO: 114021 ANSHAN, LIAONING PROVINCE |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20110927 Address after: 114021, Liaoning Anshan District, Tiexi Province Anshan Iron and steel plant main entrance Patentee after: Ansteel Engineering Technology Corporation Limited Address before: 114001 No. 31 Shengli Road, Tiedong District, Liaoning, Anshan Patentee before: Anshan Steel Company Limited |
|
| DD01 | Delivery of document by public notice |
Addressee: Anshan Steel Company Limited Document name: Notification of Passing Examination on Formalities |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20020731 Termination date: 20170602 |
|
| IW01 | Full invalidation of patent right | ||
| IW01 | Full invalidation of patent right |
Decision date of declaring invalidation: 20160623 Decision number of declaring invalidation: 29337 Granted publication date: 20020731 |