CN1213131C - Integrated method and device of high temperature coal gas desulfur and dust removing - Google Patents
Integrated method and device of high temperature coal gas desulfur and dust removing Download PDFInfo
- Publication number
- CN1213131C CN1213131C CN 03146770 CN03146770A CN1213131C CN 1213131 C CN1213131 C CN 1213131C CN 03146770 CN03146770 CN 03146770 CN 03146770 A CN03146770 A CN 03146770A CN 1213131 C CN1213131 C CN 1213131C
- Authority
- CN
- China
- Prior art keywords
- bed
- gas
- dust
- sweetening agent
- high temperature
- 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 - Fee Related
Links
Images
Abstract
The present invention relates to an integrated method for desulfurizing and dusting high-temp coal gas. A metal oxide desulfurizing agent is used as a filtering medium and a filter of a compound moving particle bed. Particles downwards move at a certain speed, and gas penetrates through a particle layer in the transverse direction. The purpose that gas sulfide and fly ash are simultaneously eliminated is achieved by means of the sulfurization reaction of the desulfurizing agent and the filtration function of the particle layer. The compound particle moving bed uses a partition plate and a material sealing structure for dividing a bed body into an upper layer and lower layer, and gas passes through the particle layer in a baffling mode from bottom to top. The present invention has the advantages of high filtering efficiency, high desulfurization rate, high utilizing rate of the desulfurizing agent, continuous process, stable operation, small occupation area of devices, etc.
Description
Technical field:
The invention belongs to a kind of high temperature gas cleaning method and apparatus, be specifically related to method and equipment thereof that a kind of composite particles moving-bed is realized the coal gas of high temperature desulphurizing and dust-removing integral.
Background technology:
Coal fired power generation is the effective means that realizes coal high-efficiency, clean utilization.(Integrated Gasification Combined Cycle IGCC) will become main flow generation technology of new generation with its high-level efficiency, oligosaprobic characteristics to integrated coal gasification combined cycle.Unavoidably there are dust and H in the fuel gas that gasification produces
2S, COS sulfides (H
2S accounts for 90%), these components can be denuded upstream device by burn into, cause environmental pollution.Therefore, high temperature coal gas purification prolongs service life of equipment to improving whole generating efficiency, reduces environmental pollution and plays an important role.High temperature coal gas purification mainly comprises desulfurization and dedusting two portions, and according to the purification process of routine, desulfurization and dedusting are unit operations independently, must be respectively through independent device strainer and desulphurization reactor are finished separately.In recent years, in conjunction with the characteristics of deep bed filter, as dust separating retention mass, desulfurization and dust removal process are finished through an operating unit becomes a developing direction with sorbent particle.Developed a kind of multilayer gas-solid cross-flow granular bed desulphurization and dust removal integrated device (" Gas Cleaningat High Temperature ", Pergamon Press, 1986) as Japanese Kawasaki heavy industry.The major advantage of cross-flow moving bed desulphurization reactor is that bed resistance is little, and is big by the cross section, bed volume utilization ratio height, stable operation; Shortcoming is that the sorbent particle conversion profile is big, is difficult to make full use of.The major advantage of moving granular bed Depth Filtration is to filter high cycle speed, can constant pressure filtration, and need not the blowback operation; Shortcoming is the long-pending rate of catching of fine dust low, is difficult to reach the system purification index.Surface filter has high efficiency of dust collection, but needs frequent blowback operation, system architecture complexity.Patent CN1236660 discloses the method and apparatus of a kind of mating surface filtration and granular layer Depth Filtration advantage, fine dust is caught long-pending efficient height, need not blowback operate, has good application prospects, but can not realize removing simultaneously solid-state and gaseous pollutant, and when handling corrosive gases, easily cause the corrosion of screen plate, influence equipment steady running.
Summary of the invention:
The object of the present invention is to provide a kind of operate continuously, efficiency of dust collection height, sweetening effectiveness is good, the equipment working cost is low coal gas of high temperature desulphurizing and dust-removing integral method and equipment thereof.
The present invention adopts by two-layer up and down and cross-flow moving bedly constitutes, the coal gas of high temperature that contains dust and sulfide from bottom to top in the baffling mode by metal oxide desulfurizer particulate bed is housed, metal oxide desulfurizer enters in the moving granular bed strainer by gravity, sulfide in the coal gas by with sweetening agent in the vulcanization reaction of active constituent be removed, the inertial impaction that dust produces when then streaming sorbent particle in the moving granular bed by gas, hold back, sedimentation, effects such as diffusion are caught to amass, vulcanizing completely sweetening agent is carrying secretly and is entering in the powder dust separating device after dust reduces pressure together, contain the filter method that the coal gas of high temperature of dust and sulfide has adopted the particle Depth Filtration to combine with surface filtration, gas is from being equipped with the pneumatic outlet of surface filtration plate.The coal gas of high temperature that contains dust and sulfide reaches the purpose that removes gaseous sulphide and dust simultaneously.
Desulphurizing and dust-removing integral method of the present invention comprises the steps:
With the metal oxide desulfurizer particle of particle diameter 0.5～9mm, the hopper of packing into is used N
2Be forced into system pressure, enter in the compound moving granular bed by gravity, 400～600 ℃ of temperature, under pressure 0.1～4MPa condition, the coal gas of high temperature that contains dust and sulfide is horizontally through the sorbent particle layer with 0.1～0.3m/s gas speed, sorbent particle is under removal device control, move down with 15-50cm/h speed, vulcanizing completely sweetening agent is carrying secretly and is entering in the powder dust separating device after dust reduces pressure together, the sorbent particle of removing dust is through e Foerderanlage, enter counter-flow moving bed regeneration reactor, utilize air and water vapour, at normal pressure, realize the regeneration of sweetening agent under 600～750 ℃ of conditions, regeneration tail gas is handled with maturation method, and the sweetening agent after the regeneration is sent in the hopper together with additional fresh sweetening agent, carries out next operation cycle.
Aforesaid metal oxide desulfurizer is the granular ferric oxide of moulding, zinc ferrite, zinc titanate sweetening agent, spherical alumina, silica supported ferrimanganic sweetening agent, and the rotary drum physical strength is 95～99%.
For realizing foregoing invention, designed a kind of specific complex moving-bed device, it is by housing, gas inlet, gas exit, the sweetening agent inlet, the sweetening agent outlet is formed, it is characterized in that having in body of heater and the sweetening agent inlet, it is desulfurizing agent bed that the sweetening agent outlet is connected, and desulfurizing agent bed top is last cross-flow moving bed, the middle part is bunk bed layered material envelope section, the bottom cross-flow moving bed one side over against gas exit the surface filtration plate is housed for cross-flow moving bed down, and the one side corresponding with the surface filtration plate is equipped with the venetian blind type air dividing plate, the venetian blind type air dividing plate is housed over against gas inlet direction both sides on down cross-flow moving bed, between bunk bed layered material envelope section and the housing last lower chamber division plate is arranged, gas inlet is positioned under the lower chamber division plate, and gas exit is positioned on the lower chamber division plate.
For guaranteeing the gas proper flow, prevent bed gas blowby up and down, the material that is provided with that drifts between the movable bed in upper and lower fault seals section, and material envelope section highly is cross-flow moving bed down 2～5 times.
Following cross-flow moving bed thickness of bed layer is 1～3 times of upper strata moving-bed.
Described surface filtration plate is resistant to elevated temperatures sintered metal plates or ceramic filter plate.
The present invention compared with prior art has following advantage:
1. adopt two-layer cross-flow moving bed frame mode up and down.In the operating process, lower floor's cross-flow bed utilizes the sweetening agent realization thick desulfurization of gas and the dedusting of partial reaction, and sweetening agent is made full use of; Upper strata cross-flow bed is realized smart desulfurization operations, guarantees high desulfuration efficiency, has overcome the low shortcoming of traditional cross-flow bed sorbent utilization.
2. consider the dynamics and the filtration characteristics of sweetening agent desulphurization reaction, lower floor's moving-bed thickness of bed layer can be designed to 1～3 times of upper strata moving-bed as required.This design can guarantee thick desulfurization stage, and gas and sweetening agent have enough duration of contact.On the other hand, the low particle rate travel of lower floor has improved the Depth Filtration effect, and the particle translational speed of last floor height can improve the cleaning effect of particle to surperficial screen plate.
3. the present invention can make coal gas of high temperature desulfurization and dust removal operation finish by an operating unit, and floor space reduces, thereby has reduced the facility investment and the working cost of high temperature coal gas purification.
Embodiment:
The present invention is described in further detail below in conjunction with drawings and Examples.
Fig. 1 is a composite particles moving-bed desulphurizing and dust-removing integral process flow diagram.
Fig. 2 is a composite particles moving-bed structural representation.
Fig. 3 is a composite particles moving-bed A-A structural representation.
As shown in the figure, the 1st, hopper, the 2nd, the feed control valve, the 3rd, last surge tank, the 4th, compound moving granular bed, the 5th, the control motor, the 6th, particle moves down speed control unit, and the 7th, following surge tank, the 8th, the blanking control valve, the 9th, aggregate bin, the 10th, dust and sorbent particle separator, the 11st, sweetening agent e Foerderanlage, the 12nd, the sweetening agent regeneration reactor, the 13rd, pneumatic outlet collection chamber, the 14th, last lower chamber division plate, the 15th, gas inlet air chamber, the 16th, particle logistics rectifying block, the 17th, cross-flow moving bed down, the 18th, gas communication chamber, the 19th, bunk bed layered material envelope section, the 20th, go up cross-flow moving bed, the 21st, last window shutter sparger, the 22nd, surface filtration plate, the 23rd, gas exit, 24 raw gass inlet, the 25th, subtract (adding) to press mouthful, the 26th, subtract (adding) to press mouthful, 27 be fresh or regenerate after sorbent particle, the 28th, the sweetening agent inlet, the 29th, the sweetening agent outlet, 30 is the dust that captures from gas, 31 is sweetening agent regenerative response gas air and water vapour, 32 is the sweetening agent regeneration tail gas, the 33rd, following air inlet side window shutter, the 34th, the side window shutter of giving vent to anger down, the 35th, plate washer.
Have in the body of heater and desulfurizing agent entrance 28, it is desulfurizing agent bed that desulfurizing agent outlet 29 is connected, and takes off Sulphur agent bed top is upper cross-flow moving bed 20, and the middle part is bunk bed layered material envelope section 19, and the bottom is lower mistake The movable bed 17 that drifts, upper cross-flow moving bed 20 one sides over against gas exit 23 are equipped with the surface filtration plate 22, the one side corresponding with surface filtration plate 22 is equipped with venetian blind type air dividing plate 21, moves in lower cross-flow Over against gas inlet 24 direction both sides venetian blind type air dividing plate 33,34 is housed on the movable bed 17, up and down Between bed material envelope section 19 and the housing upper lower chamber demarcation strip 14 is arranged, about gas inlet 24 is positioned at Under the air chamber demarcation strip 14, gas exit 23 is positioned on the lower chamber demarcation strip 14.
Embodiment 1
Sweetening agent is the particulate iron oxide high temperature desulfuration agent, particle diameter 0.5-3mm.Operational condition is: 500～550 ℃ of service temperatures, working pressure 1MPa (gauge pressure).Oxygen/humidified blast coal gas consists of (percentage by volume): H
2Content 28%, CO content 25%, N
2Content 6%, CH
4Content 1%, CO
2Content 16%, H
2O content 24%.Dust concentration 5.2g/Nm in the raw gas
3, H
2S concentration 6000ppmv.At first, with ferric oxide desulfurizing agent for high-temp gas particle pack into hopper 1 and composite particles bed 4, N
2Be forced into 1.0MPa, then, introduce high temperature rough gas, cross bed gas speed control, start removal device 6, the about 36cm/h of control sweetening agent rate travel built in about 0.15m/s by inlet mouth 24.Gas enters lower floor's moving-bed through air inlet chamber 15, contacts with the sorbent particle cross-flow that moves down, and finishes thick desulfurization and dedusting operation, and sweetening agent is transformed fully.The gas of rough purification enters upper strata moving-bed 20 through communication chamber 18, carries out smart desulfurization and further dedusting, again through surface filtration plate 22, and further smart dedusting, purified gas is discharged by clean gas outlet 23 through collection chamber 13.Vulcanizing completely, sweetening agent enters aggregate bin 9 by removal device 6 controls together with the dust that is captured, reach a certain amount of after, closed control valve 8 enters separator 10 after pressure-reduction outlet 26 decompression, the separated discharge of dust, sorbent particle is then sent into regeneration reactor 12 by lift 11, at normal pressure, under 700 ℃ of conditions, by air and water vapour regeneration, send into storage hopper 1 through the regenerated sorbent particle, after pressurization mouthful 25 pressurizations, recycle.After treating that bed pressure drop is stable, measure dust and sulfide concentration in the Purge gas.Through stable operation in 8 hours, dust concentration can be stabilized in 20mg/Nm in the Purge gas
3Below, H
2S concentration can be stabilized in 100～150ppmv.Sreen analysis shows that the above dust of particle diameter 5 μ m can all remove.
The air air blast produces coal gas of high temperature, and coal gas consists of (percentage by volume): H
2Content 15%, CO content 13%, N
2Content 46%, CH
4Content 1%, CO
2Content 10%, H
2O content 15%.Dust concentration 6.4g/Nm in the raw gas
3, H
2S concentration 3000ppmv.The about 25cm/h of control sweetening agent rate travel crosses bed gas speed control built in about 0.1m/s, and all the other are with example 1.Dust concentration can be stabilized in 20mg/Nm in the Purge gas
3Below, H
2S concentration can be stabilized in 30～100ppmv.The above dust of particle diameter 5 μ m all removes.
Embodiment 3
The about 18cm/h of control sweetening agent rate travel, all the other are with example 2.Dust concentration can be stabilized in 10mg/Nm in the Purge gas
3Below, H
2S concentration can be stabilized in 70～150ppmv.The above dust of particle diameter 5 μ m all removes.
Embodiment 4
Sweetening agent is a particulate state ferrous acid zinc high temperature desulfuration agent, particle diameter 0.5-3mm.The air air blast produces coal gas of high temperature, the about 18cm/h of control sweetening agent rate travel, and all the other are with example 2.Dust concentration can be stabilized in 10mg/Nm in the Purge gas
3Below, H
2S concentration can be stabilized in 20～50ppmv.The above dust of particle diameter 5 μ m all removes.
Claims (5)
1. a coal gas of high temperature desulphurizing and dust-removing integral method is characterized in that comprising the steps:
Metal oxide desulfurizer particle with particle diameter 0.5～9mm, the hopper of packing into, be forced into system pressure with N2, enter in the compound moving granular bed by gravity, 400～600 ℃ of temperature, under pressure 0.1～4MPa condition, the coal gas of high temperature that contains dust and sulfide is horizontally through the sorbent particle layer with 0.1～0.3m/s gas speed, and sorbent particle moves down with 15-50cm/h speed under removal device control, vulcanizing completely sweetening agent is carrying secretly and is entering in the powder dust separating device after dust reduces pressure together, the sorbent particle of removing dust enters counter-flow moving bed regeneration reactor through e Foerderanlage, utilizes air and water vapour, at normal pressure, realize the regeneration of sweetening agent under 600～750 ℃ of conditions, regeneration tail gas is handled with maturation method, and the sweetening agent after the regeneration is sent in the hopper together with additional fresh sweetening agent, carry out next operation cycle
Wherein metal oxide desulfurizer is the granular ferric oxide of moulding, zinc ferrite, zinc titanate sweetening agent, spherical alumina, silica supported ferrimanganic sweetening agent, and the rotary drum physical strength is 95～99%.
2. a kind of coal gas of high temperature desulphurizing and dust-removing integral method equipment used as claimed in claim 1, it is characterized in that it is by housing, gas inlet (24), gas exit (23), sweetening agent inlet (28), sweetening agent outlet (29) is formed, have in the body of heater and sweetening agent inlet (28), it is desulfurizing agent bed that sweetening agent outlet (29) is connected, desulfurizing agent bed top is last cross-flow moving bed (20), the middle part is bunk bed layered material envelope section (19), the bottom is following cross-flow moving bed (17), upward cross-flow moving bed (20) are equipped with surface filtration plate (22) over against the one side of gas exit (23), the one side corresponding with surface filtration plate (22) is equipped with venetian blind type air dividing plate (21), in following cross-flow moving bed (17) venetian blind type air dividing plate (33) (34) is housed over against gas inlet (24) direction both sides upward, between bunk bed layered material envelope section (19) and the housing last lower chamber division plate (14) is arranged, gas inlet (24) is positioned under the lower chamber division plate (14), and gas exit (23) is positioned at up and down on the bed division plate (14).
3. a kind of coal gas of high temperature desulphurizing and dust-removing integral method equipment used as claimed in claim 2 is characterized in that described surface filtration plate (22) is resistant to elevated temperatures sintered metal plates or ceramic filter plate.
4. a kind of coal gas of high temperature desulphurizing and dust-removing integral method equipment used as claimed in claim 2 is characterized in that described bunk bed layered material envelope section (19) highly is following cross-flow moving bed (17) 2～5 times.
5. a kind of coal gas of high temperature desulphurizing and dust-removing integral method equipment used as claimed in claim 2 is characterized in that described cross-flow moving bed (17) thickness of bed layer down is last cross-flow moving bed (20) 1～3 times.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03146770 CN1213131C (en) | 2003-06-25 | 2003-06-25 | Integrated method and device of high temperature coal gas desulfur and dust removing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03146770 CN1213131C (en) | 2003-06-25 | 2003-06-25 | Integrated method and device of high temperature coal gas desulfur and dust removing |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1478872A CN1478872A (en) | 2004-03-03 |
| CN1213131C true CN1213131C (en) | 2005-08-03 |
Family
ID=34156115
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03146770 Expired - Fee Related CN1213131C (en) | 2003-06-25 | 2003-06-25 | Integrated method and device of high temperature coal gas desulfur and dust removing |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1213131C (en) |
Families Citing this family (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1331573C (en) * | 2004-12-22 | 2007-08-15 | 唐华 | Moving bed dry process desulphurization unit and method in intermittent type |
| US7618558B2 (en) * | 2005-04-15 | 2009-11-17 | Haldor Topsoe A/S | Process for cleaning gases from gasification units |
| CN100443144C (en) * | 2006-07-31 | 2008-12-17 | 煤炭科学研究总院 | A fume desulfurizing and absorbent regenerative coupling device |
| CN101544914B (en) * | 2009-03-31 | 2012-11-14 | 中国科学院山西煤炭化学研究所 | Method and device for thermally desulfurizing by synthesis gas dry method and reclaiming sulfur |
| CN101683602B (en) * | 2009-06-03 | 2012-05-09 | 赛鼎工程有限公司 | Moving bed reactor device with catalyst capable of reacting continuously and being regenerated and use method thereof |
| CN101880553B (en) * | 2010-06-22 | 2013-03-13 | 沈阳航空航天大学 | Integrated medium-high temperature coal gas purification method and device suitable for coal-based gas |
| TWI419732B (en) | 2011-02-22 | 2013-12-21 | Iner Aec Executive Yuan | Compact two-stage granular moving-bed apparatus |
| CN102908841B (en) * | 2012-10-16 | 2016-06-01 | 哈尔滨瑞格能源环境技术发展有限责任公司 | For method and the device of the purification of low-temperature pyrolysis coal gas dust removal |
| CN102961945A (en) * | 2012-11-29 | 2013-03-13 | 中南大学 | System with integrated functions of high-temperature flue gas dedusting, desulfurization and denitrification |
| CN103242873B (en) * | 2013-05-30 | 2015-06-17 | 神华集团有限责任公司 | Pyrolyzer |
| CN103265978B (en) * | 2013-05-31 | 2014-07-30 | 陕西煤业化工技术研究院有限责任公司 | Integrated system and method for catalytic cracking and dust removal of medium-and-low temperature dry distillation coal gas |
| US9418953B2 (en) | 2014-01-13 | 2016-08-16 | Taiwan Semiconductor Manufacturing Company, Ltd. | Packaging through pre-formed metal pins |
| CN104073298B (en) * | 2014-06-30 | 2016-08-24 | 中国天辰工程有限公司 | A kind of reduce the apparatus and method of content of ashes in brown coal hydrogasification synthesis gas |
| CN104096429A (en) * | 2014-07-26 | 2014-10-15 | 淮北市森化碳吸附剂有限责任公司 | Slanting grid type dust-removing and desulphurizing integrated device |
| WO2017084062A1 (en) * | 2015-11-19 | 2017-05-26 | 冯李荣 | Environment-friendly hot natural gas output apparatus |
| CN108430604A (en) * | 2016-04-11 | 2018-08-21 | 日挥株式会社 | The processing system of exhaust gas |
| CN107456824A (en) * | 2017-06-16 | 2017-12-12 | 中国石油大学(华东) | Moving bed stratum granulosum becomes press filtering device |
| CN108264024B (en) * | 2018-02-12 | 2021-11-16 | 上海米素环保科技有限公司 | Combined method and device suitable for deep dehydration of working solution in hydrogen peroxide preparation by anthraquinone process |
| CN108283874A (en) * | 2018-04-25 | 2018-07-17 | 武汉都市环保工程技术股份有限公司 | A kind of cross-current type three-level moving-bed active coke desulphurization denitration purifying column |
| CN110898567B (en) * | 2019-04-23 | 2021-11-09 | 江苏集萃工业过程模拟与优化研究所有限公司 | Moving bed particle dust removal device and method capable of automatically adjusting speed of filter material |
| CN112316987A (en) * | 2019-08-05 | 2021-02-05 | 中国石油化工股份有限公司 | Desulfurization method of carbon deposition low-carbon alkane dehydrogenation catalyst |
| CN110772983A (en) * | 2019-11-11 | 2020-02-11 | 中国科学院山西煤炭化学研究所 | Device and method for low-temperature denitration of flue gas |
| CN114317041B (en) * | 2021-11-26 | 2023-07-25 | 清华大学 | Desulfurizing tower and desulfurizing method |
| CN114272744A (en) * | 2021-12-09 | 2022-04-05 | 西南化工研究设计院有限公司 | Moving bed device and process for dry flue gas desulfurization |
| CN115093886B (en) * | 2022-07-31 | 2023-12-22 | 中国石油化工股份有限公司 | Circulating moving bed process method and device for desulfurizing and dedusting gasified synthetic gas |
-
2003
- 2003-06-25 CN CN 03146770 patent/CN1213131C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1478872A (en) | 2004-03-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1213131C (en) | Integrated method and device of high temperature coal gas desulfur and dust removing | |
| KR101250702B1 (en) | Method for cleaning exhaust gases produced by a sintering process for ores and/or other metal-containing materials in metal production | |
| US5547648A (en) | Removing SOx, NOX and CO from flue gases | |
| US4764355A (en) | Process for removal of solid and gaseous noxious matter from hot gases | |
| CN104107617B (en) | Contaminant removal from a gas stream | |
| US3505008A (en) | Separation of fly ash and sulfur dioxide from flue gases | |
| US5811066A (en) | Method and device for scrubbing flue gases | |
| US20070217979A1 (en) | Method For Reducing Heavy Metals In Flue Gases | |
| CN115141660B (en) | Dry type fine desulfurization system and method for blast furnace gas | |
| CN112191070B (en) | Activated carbon adsorption process | |
| CN109806723A (en) | A kind of cross-flow type activated coke moving bed sintering flue gas purifying tower | |
| CA1304912C (en) | Gas/solid contact method for removing sulfur oxides from gases | |
| CN1033508A (en) | Dry cleaning contains the method and apparatus that mixes the harmful components flue gas | |
| CN1090518C (en) | Fluid-bed sweetening | |
| EP0399416B1 (en) | Method for removal of dust contained in a gas and for reaction of a toxic component of said gas | |
| US8177886B2 (en) | Use of oxygen concentrators for separating N2 from blast furnace gas | |
| CN2582724Y (en) | Twing cyclone impact type cyclone plate exhaust gas purifying device | |
| CN207776939U (en) | A kind of purification vehicle exhaust equipment | |
| CN112933910A (en) | Moving bed coupling absorption desulfurization method based on flue gas semidry method | |
| CN113777242B (en) | Method for detecting activity based on cerium-based adsorbent | |
| JPS6064618A (en) | Solid-gas catalytic reaction apparatus | |
| CN111019716B (en) | Device and method for cooperatively controlling and recovering mercury and sulfur in coal gas | |
| CN213253734U (en) | Granule burnt desulfurization weary burnt device of recycling | |
| CN215463101U (en) | Automatic discharging and filling system of clean adsorption-desorption purification device | |
| CN109569192A (en) | A kind of dry type desulfurizing denitration dust collecting integral equipment |
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 | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20050803 Termination date: 20150625 |
|
| EXPY | Termination of patent right or utility model |