CN100430315C - Equipment and method for treating exhaust gas for carbon bisulfide preparing process - Google Patents
Equipment and method for treating exhaust gas for carbon bisulfide preparing process Download PDFInfo
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- CN100430315C CN100430315C CNB2006101273800A CN200610127380A CN100430315C CN 100430315 C CN100430315 C CN 100430315C CN B2006101273800 A CNB2006101273800 A CN B2006101273800A CN 200610127380 A CN200610127380 A CN 200610127380A CN 100430315 C CN100430315 C CN 100430315C
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- gas
- sulphur
- tail gas
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- 238000000034 method Methods 0.000 title claims abstract description 60
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title claims description 37
- 238000011084 recovery Methods 0.000 claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims abstract description 10
- 238000001816 cooling Methods 0.000 claims abstract description 10
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 118
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 59
- 239000005864 Sulphur Substances 0.000 claims description 47
- 238000006243 chemical reaction Methods 0.000 claims description 23
- 238000004519 manufacturing process Methods 0.000 claims description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 13
- 238000010521 absorption reaction Methods 0.000 claims description 12
- 229910052717 sulfur Inorganic materials 0.000 claims description 12
- 239000011593 sulfur Substances 0.000 claims description 12
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 8
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 8
- 238000003795 desorption Methods 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 239000003345 natural gas Substances 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 5
- 230000003197 catalytic effect Effects 0.000 claims description 4
- 235000009508 confectionery Nutrition 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 description 10
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- KRKNYBCHXYNGOX-UHFFFAOYSA-K Citrate Chemical compound [O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O KRKNYBCHXYNGOX-UHFFFAOYSA-K 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- HRZFUMHJMZEROT-UHFFFAOYSA-L sodium disulfite Chemical group [Na+].[Na+].[O-]S(=O)S([O-])(=O)=O HRZFUMHJMZEROT-UHFFFAOYSA-L 0.000 description 2
- 235000010262 sodium metabisulphite Nutrition 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- RNUBFUJXCFSMQP-UHFFFAOYSA-N borol-2-one Chemical compound O=C1B=CC=C1 RNUBFUJXCFSMQP-UHFFFAOYSA-N 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Classifications
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- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to a tail gas processing device and method, concretely a tail gas processing device and method in the CS2 preparing course, adopting a mode of integrating multistage Claus combustion furnace with low-temperature Claus process to process the tail gas, and makes gross recovery of S up to 99.5% above; and in the whole operating course, the catalyst regeneration and cooling are both completed by the system itself, so that the energy comsuption is low, pollution is less, and the exhausted tail gas can completely meet the requirements of national related effluent stardards, and the whole operating course is controlled by PLC program controller, thus implementing continous operation and reducing workers'labor strength.
Description
Technical field
The present invention relates to a kind of tail gas processing device and method, be specially tail gas processing device and method in a kind of carbon disulphide manufacture process.
Background technology
As everyone knows, the production equipment output that the methane method is produced dithiocarbonic anhydride is big, the tail gas amount is also big, one ton of dithiocarbonic anhydride of every preparation generates about one ton of hydrogen sulfide simultaneously during reaction, all adopt the claus process recovery sulphur at present both at home and abroad, sulphur returns the production equipment of dithiocarbonic anhydride as raw material then, it also is the traditional technology of always using, Crouse's roasting kiln reclaims hydrogen sulfide and has adopted the borolon catalyzer to replace natural aluminum ore, improved efficient, Crouse's roasting kiln is transformed by original one-level and changes multistage conversion into, makes transformation efficiency bring up to 95%-98% by 81%.Raising along with methane method production technology, the tail gas recycle aspect has also adopted new Technology, tail gas after Crouse's recovery is reclaimed again, technological approaches according to claus tail-gas clean-up technology, can substantially it be divided three classes: low-temperature Claus class, reduction class and oxidation class, reduction class technology can satisfy the harshest requirement of environmental protection, but invest relatively big, normally 2-2.5 times of the investment of low-temperature Claus class, this type of technology adopts in the petrochemical industry imported unit of Chinese large-sized a lot; What oxidation class process application was more is Sodium Pyrosulfite method and Citrate trianion method, and the sulfur dioxide recovery rate of Sodium Pyrosulfite method is not very high, also have waste liquid waste water simultaneously and produce, and the sulfur dioxide recovery rate of Citrate trianion method is higher relatively, but cost is very big; Though and low-temperature Claus has advantages such as little, the main technical process of investment is short, device is simple, but in the reaction of in each low-temperature Claus reactor, being gone through absorption, heating, three processes of cooling, must be equipped with special process furnace and cool furnace, cause the waste of heat in the system, also increased the cost input simultaneously.
Summary of the invention
The above-mentioned defective that the present invention exists for the low-temperature Claus technology that solves in the existing dithiocarbonic anhydride exhaust gas recovery system and tail gas processing device and method in the lower carbon disulphide manufacture process of a kind of economical rationality, production cost is provided.
The present invention adopts following technical scheme to realize: tail gas processing device in the carbon disulphide manufacture process, comprise at least three claus reaction devices, reactor lower part is connected with the tail gas inlet branch that communicates with the Claus tail gases house steward respectively, be connected with sulphur output tube and cold air output tube on the tail gas inlet branch respectively, the other end of sulphur output tube is connected with the front portion of sulfur condenser, the afterbody of sulfur condenser with catch the sulphur device and be connected, catching sulphur device top is connected with incinerator by pipeline, the incinerator afterbody communicates with gas-gas heat exchanger, the other end of cold air output tube communicates with gas-gas heat exchanger, also be provided with hot gas input house steward on the gas-gas heat exchanger, reactor head is provided with the hot gas inlet branch that communicates with the hot gas input house steward the other end, the hot gas inlet branch of every reactor communicates respectively, on the described every pipeline valve is housed all.
Reactor head of the present invention is respectively equipped with the nitrogen input tube, can allocate rare gas element simultaneously into and cool off when blast-cold is operated.
Utilize above-mentioned described equipment to finish exhaust gas treating method in the carbon disulphide manufacture process, comprise the removal process of hydrogen sulfide mixed gas in Crouse's roasting kiln and multistage catalytic converter, tail gas after the recovery enters the low-temperature Claus system, tail gas through the Crouse system enters in three claus reaction devices at least, reaction absorption hockets respectively, heating, the blast-cold operation, reaction adsorption operations temperature is under the dew point of sulphur, the gas that wherein takes place after the absorption reaction is used to cool off the reactor that just has been heated desorb, make it reach next time temperature of reaction, gas behind the cooling reactor enters the low-temperature Claus gas-gas heat exchanger and utilizes the tail gas heat quantity of Crouse's incinerator to be heated, the interior also heatable catalyst bed of reactor that gas after the heating enters firm generation absorption reaction operation again makes catalyst regeneration, make the sulphur desorption under comparatively high temps that adsorbs in the catalyzer, to realize the intermittent process continuous operation.The quantity of claus reaction device of the present invention can be determined according to the size of throughput.The vent gas treatment of Crouse of the present invention system adopts solid catalysis low-temperature Claus technology, catalyst system therefor is CT6-4 catalyzer or catalyzer of the same type, carry out below being reflected at the dew-point temperature of sulphur, the sulphur that reclaims accumulates and is adsorbed on the solid catalyst, regularly switch regeneration, adopt the tail gas heat quantity of Crouse's incinerator of system self to heat up during regeneration, to accumulate the liquid-state sulfur that is adsorbed on the solid catalyst takes out of, make catalyzer recover active, process gas after reaction was adsorbed in the reusing system after regeneration was finished is standby with cooling catalyst, and this solid catalysis low-temperature Claus system recoveries rate can reach about 85-90%.
Sulphur behind the desorption of the present invention enters sulfur condenser cooling back and reclaims, and the gas that is entrained with a small amount of sulphur is sent into the burning of Crouse's incinerator through catching after the sulphur device captures sulphur, and stack gas is high altitude discharge after the gas-gas heat exchanger heat exchange.
The alternately handoff procedure of the reaction absorption of carrying out in the claus reaction device of the present invention, heating, blast-cold operation is by the control of PLC sequence controller, can realize that technological process is long-term, safety, steady running, alleviates operator's working strength.
The interior temperature of reactor of carrying out adsorption operations of the present invention is controlled at 120-150 ℃, and the best is 135-150 ℃, and the Heating temperature during catalyst regeneration is 280-350 ℃, and the best is 290-310 ℃.
Compared with prior art, the present invention adopts multistage Crouse's roasting kiln to handle tail gas with the mode that low-temperature Claus technology combines, and the total yield of sulphur is reached more than 99.5%; And the regeneration and the cooling of catalyzer finished by system self in the entire operation process, not only energy consumption is low, pollution is few, discharge tail gas can reach the requirement of the relevant emission standard of country fully, and the entire operation process is controlled by the PLC sequence controller, realize continuous operation, reduced working strength of workers.
Description of drawings
Fig. 1 is a process flow sheet of the present invention
1,2,3-reactor 4-gas-gas heat exchanger 5-incinerator 6-sulfur condenser 7-catches sulphur device 8-Claus tail gases house steward 9-tail gas inlet branch 10-sulphur output tube 11-cold air output tube 12-hot gas input house steward 13-hot gas inlet branch 14-nitrogen input tube 15-chimney 16-Sweet natural gas input tube among the figure:
Embodiment
Tail gas processing device in the carbon disulphide manufacture process, comprise at least three claus reaction devices 1,2,3, reactor lower part is connected with the tail gas inlet branch 9 that communicates with Claus tail gases house steward 8 respectively, be connected with sulphur output tube 10 and cold air output tube 11 on the tail gas inlet branch 9 respectively, the other end of sulphur output tube 10 is connected with the front portion of sulfur condenser 6, the afterbody of sulfur condenser 6 with catch sulphur device 7 and be connected, catching sulphur device 7 tops is connected with incinerator 5 by pipeline, incinerator 5 afterbodys communicate with gas-gas heat exchanger 4, the other end of cold air output tube 11 communicates with gas-gas heat exchanger 4, also be provided with hot gas input house steward 12 on the gas-gas heat exchanger 4, reactor head is provided with the hot gas inlet branch 13 that communicates with hot gas input house steward 12 the other ends, the hot gas inlet branch 13 of every reactor communicates respectively, on the described every pipeline valve is housed all; Reactor head is respectively equipped with nitrogen input tube 14; Gas-gas heat exchanger 4 afterbodys are connected with blowdown stack 15, and incinerator 5 front portions are connected with Sweet natural gas input tube 16.
Utilize above-mentioned described equipment to finish exhaust gas treating method in the carbon disulphide manufacture process, comprise the removal process of hydrogen sulfide mixed gas in Crouse's roasting kiln and multistage catalytic converter, the hydrogen sulfide mixed gas that the present invention will be sent here by refined unit feeds Crouse's incinerator and ratio earlier and regulates air after measuring in the stove internal combustion, partial vulcanization hydrogen is converted into elemental sulfur, after reclaiming heat, waste heat boiler enters condenser recovering liquid sulphur, and the hydrogen sulfide that will remain in the process gas continues to reclaim elemental sulfur through three grades of catalytic converters and supporting condenser, and the rate of recovery of sulphur is reached more than 96.5%.Tail gas after the recovery enters the low-temperature Claus system, the tail gas of Crouse system feeds in the low-temperature Claus reactor, at three low-temperature Claus reactors 1,2, reaction absorption hockets respectively in 3, heating, the blast-cold operation, service temperature is under the sulphur dew point of sulphur, the gas that wherein takes place after the absorption reaction is used to cool off the reactor that just has been heated desorb, make it reach next time temperature of reaction, gas behind the cooling reactor enters the low-temperature Claus gas-gas heat exchanger and utilizes the high-temperature tail gas heat of Crouse's incinerator to be heated, gas after the heating enters in the reactor of the adsorption operations that just reacted again and makes catalyst regeneration, make the sulphur desorption under comparatively high temps that adsorbs in the catalyzer, realized the intermittent process continuous operation; Sulphur behind the desorption enters sulfur condenser 6 cooling backs and reclaims, and the gas that is entrained with a small amount of sulphur is sent into 5 burnings of Crouse's incinerator through catching after sulphur device 7 captures sulphur, by through 80 meters high aiutage qualified discharge, so far the total yield of sulphur reaches more than 99.5% stack gas after gas-gas heat exchanger 4 heat exchange.
Shown in process flow sheet, with reactor 1 is example, Claus tail gases is through Claus tail gases house steward 8, tail gas inlet branch 9 enters reactor 1 absorption that further reacts, temperature of reaction is 120-150 ℃, reacted gas enters reactor 2, blast-cold catalyzer wherein, introduce the further blast-cold of part nitrogen by nitrogen input tube 14 in case of necessity, gas enters low-temperature Claus gas-gas heat exchanger 4 from reactor 2 through supercool gas output tube 11 then, the tail gas heat quantity gas heating of utilizing Crouse's incinerator 5 therein is to 280-450 ℃, temperature and flow can be regulated by regulated valve, part gas can directly go incinerator 5 emptying, the gas that is heated to 280-450 ℃ is through hot gas input house steward 12, hot gas inlet branch 13 enters reactor 3, wherein reacted deactivated catalyzer with heating, make the sulphur that adsorbs in catalyzer desorption and enter sulfur condenser 6 under comparatively high temps through sulphur output tube 10, gas is cooled to below the dew-point temperature of sulphur, sulphur becomes liquid, the gas that is entrained with a small amount of sulphur is sent into the 5 burning back emptyings of Crouse's incinerator after catching sulphur device 7, so far finish the flow process of low-temperature Claus.Above-mentioned said process realizes by the PLC sequence controller.
Crouse's incinerator is that the air of using the Sweet natural gas sent here through Sweet natural gas input tube 16 and air-blaster to send here is chewed by burning at burner and sent into the stove internal combustion, produce high temperature and exhaust temperature is elevated to more than 650 ℃, trace hydrogen sulfide in the tail gas is oxidized to sulfurous gas, after incinerator tail gas reclaims heat by the low-temperature Claus gas-gas heat exchanger, through 80 meters chimney 15 emptyings.
Claims (8)
1, tail gas processing device in a kind of carbon disulphide manufacture process, it is characterized in that comprising at least three claus reaction devices (1,2,3), reactor lower part is connected with the tail gas inlet branch (9) that communicates with Claus tail gases house steward (8) respectively, be connected with sulphur output tube (10) and cold air output tube (11) on the tail gas inlet branch (9) respectively, the other end of sulphur output tube (10) is connected with the front portion of sulfur condenser (6), the afterbody of sulfur condenser (6) with catch sulphur device (7) and be connected, catching sulphur device (7) top is connected with incinerator (5) by pipeline, incinerator (5) afterbody communicates with gas-gas heat exchanger (4), the other end of cold air output tube (11) communicates with gas-gas heat exchanger (4), also be provided with hot gas input house steward (12) on the gas-gas heat exchanger (4), reactor head is provided with the hot gas inlet branch (13) that communicates with hot gas input house steward (12) the other end, the hot gas inlet branch (13) of every reactor communicates respectively, on the described every pipeline valve is housed all.
2, tail gas processing device in the carbon disulphide manufacture process according to claim 1 is characterized in that reactor head is respectively equipped with nitrogen input tube (14).
3, tail gas processing device in the carbon disulphide manufacture process according to claim 1 and 2 is characterized in that gas-gas heat exchanger (4) afterbody is connected with blowdown stack (15), and incinerator (5) front portion is connected with Sweet natural gas input tube (16).
4, utilize equipment as claimed in claim 1 to finish exhaust gas treating method in the carbon disulphide manufacture process, comprise the removal process of hydrogen sulfide mixed gas in Crouse's roasting kiln and multistage catalytic converter, tail gas after the recovery enters the low-temperature Claus system, it is characterized in that entering at least three claus reaction devices (1 through the tail gas of low-temperature Claus system, 2,3) in, reaction absorption hockets respectively, heating, the blast-cold operation, reaction adsorption operations temperature is under the sulphur dew point, the gas that wherein takes place after the absorption reaction is used to cool off the reactor that just has been heated desorb, make it reach next time temperature of reaction, gas behind the cooling reactor enters gas-gas heat exchanger (4) and utilizes the tail gas heat quantity of incinerator (5) to be heated, the interior also heatable catalyst bed of reactor that gas after the heating enters firm generation absorption reaction operation again makes catalyst regeneration, make the sulphur desorption under comparatively high temps that adsorbs in the catalyzer, to realize the intermittent process continuous operation.
5, the treatment process of tail gas in the carbon disulphide manufacture process according to claim 4, it is characterized in that the sulphur behind the desorption enters sulfur condenser (6) cooling back recovery, and the gas that is entrained with a small amount of sulphur is sent into incinerator (5) burning through catching after sulphur device (7) captures sulphur, and stack gas is high altitude discharge after gas-gas heat exchanger (4) heat exchange.
6, the treatment process of tail gas in the carbon disulphide manufacture process according to claim 4, the alternately handoff procedure of the reaction absorption that it is characterized in that carrying out in the claus reaction device, heating, blast-cold operation is to be controlled by the PLC sequence controller.
7, the treatment process of tail gas in the carbon disulphide manufacture process according to claim 4 is characterized in that the interior temperature of reactor of reacting adsorption operations is controlled at 120-150 ℃, and the Heating temperature during catalyst regeneration is 280-450 ℃.
8, the treatment process of tail gas in the carbon disulphide manufacture process according to claim 4 is characterized in that allocating into simultaneously nitrogen when blast-cold is operated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101273800A CN100430315C (en) | 2006-09-18 | 2006-09-18 | Equipment and method for treating exhaust gas for carbon bisulfide preparing process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101273800A CN100430315C (en) | 2006-09-18 | 2006-09-18 | Equipment and method for treating exhaust gas for carbon bisulfide preparing process |
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| CN1935646A CN1935646A (en) | 2007-03-28 |
| CN100430315C true CN100430315C (en) | 2008-11-05 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101503693B (en) * | 2009-03-03 | 2011-04-06 | 中国农业科学院生物技术研究所 | Halimodendron halodendron ERF transcription factor cDNA sequence, expression vector and use thereof |
| CN102192515A (en) * | 2010-03-10 | 2011-09-21 | 中国石油天然气股份有限公司 | Forced mixed tail gas burning furnace |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100523653C (en) * | 2007-08-27 | 2009-08-05 | 武汉云鹤定宇制冷科技有限公司 | Adsorption refrigerating system with two and above generators |
| CN101829484B (en) * | 2010-05-27 | 2012-06-06 | 重庆紫光化工股份有限公司 | Tail gas recovery method of carbon bisulfide refining system |
| CN107298443A (en) * | 2017-07-28 | 2017-10-27 | 阳城县绿色铸造研发中心 | Carbon disulfide gasification reacting furnace sulphur feeding device |
| CN108557773A (en) * | 2018-04-18 | 2018-09-21 | 陕西未来能源化工有限公司 | A kind of Crouse's temperature control system and its method |
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| CN1048201A (en) * | 1989-06-19 | 1991-01-02 | 克鲁普科普斯有限公司 | The working method of Cross unit |
| CN1226873A (en) * | 1997-04-24 | 1999-08-25 | 埃勒夫勘探产品公司 | Method for eliminating H2S, SO2, COS and/or CS2 sulphur compounds, contained in sulphur factory waste gas with recuperation of said compounds in form of sulphur |
| US6962680B1 (en) * | 2000-10-18 | 2005-11-08 | Jgc Corporation | Method and apparatus for removing sulfur compound in gas containing hydrogen sulfide, mercaptans, carbon dioxide and aromatic hydrocarbon |
-
2006
- 2006-09-18 CN CNB2006101273800A patent/CN100430315C/en active Active - Reinstated
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1048201A (en) * | 1989-06-19 | 1991-01-02 | 克鲁普科普斯有限公司 | The working method of Cross unit |
| CN1226873A (en) * | 1997-04-24 | 1999-08-25 | 埃勒夫勘探产品公司 | Method for eliminating H2S, SO2, COS and/or CS2 sulphur compounds, contained in sulphur factory waste gas with recuperation of said compounds in form of sulphur |
| US6962680B1 (en) * | 2000-10-18 | 2005-11-08 | Jgc Corporation | Method and apparatus for removing sulfur compound in gas containing hydrogen sulfide, mercaptans, carbon dioxide and aromatic hydrocarbon |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101503693B (en) * | 2009-03-03 | 2011-04-06 | 中国农业科学院生物技术研究所 | Halimodendron halodendron ERF transcription factor cDNA sequence, expression vector and use thereof |
| CN102192515A (en) * | 2010-03-10 | 2011-09-21 | 中国石油天然气股份有限公司 | Forced mixed tail gas burning furnace |
| CN102192515B (en) * | 2010-03-10 | 2012-11-14 | 中国石油天然气股份有限公司 | Forced mixed tail gas burning furnace |
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| CN1935646A (en) | 2007-03-28 |
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Free format text: FORMER OWNER: SHANGHAI BAIJIN CHEMICAL GROUP CO., LTD. Owner name: SHANGHAI BAIJIN CHEMICAL GROUP CO., LTD. Free format text: FORMER OWNER: KONG QINGRAN Effective date: 20110801 |
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Effective date of registration: 20110801 Address after: 200122 Pudong New Area Zhang Yang Road, No. 707 life insurance building, floor, Shanghai, 26 Patentee after: Shanghai Baijin Chemical Group Co.,Ltd. Address before: 200122 Pudong New Area Zhang Yang Road, No. 707 life insurance building, floor, Shanghai, 26 Co-patentee before: Shanghai Baijin Chemical Group Co.,Ltd. Patentee before: Kong Qingran |
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Effective date of registration: 20170317 Address after: 261300 Changyi Coastal Economic Development Zone, Shandong, China, Weifang Patentee after: SHANDONG JINDIAN CHEMICAL CO.,LTD. Address before: 200122 Pudong New Area Zhang Yang Road, No. 707 life insurance building, floor, Shanghai, 26 Patentee before: Shanghai Baijin Chemical Group Co.,Ltd. |
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Granted publication date: 20081105 Termination date: 20190918 |
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Correction item: termination of patent right due to unpaid annual fee Correct: Revocation of the patent right False: Patent right to terminate Number: 37-02 Volume: 36 |
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Former decision: Patent right to terminate Former decision publication date: 20200911 |
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