CN206240324U - It is a kind of to remove cos, carbon disulfide device simultaneously - Google Patents
It is a kind of to remove cos, carbon disulfide device simultaneously Download PDFInfo
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- CN206240324U CN206240324U CN201621153197.3U CN201621153197U CN206240324U CN 206240324 U CN206240324 U CN 206240324U CN 201621153197 U CN201621153197 U CN 201621153197U CN 206240324 U CN206240324 U CN 206240324U
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- fixed bed
- bed reaction
- reaction tower
- tower
- pump
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- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title claims description 31
- 238000006243 chemical reaction Methods 0.000 claims abstract description 93
- 239000007921 spray Substances 0.000 claims abstract description 36
- 238000001816 cooling Methods 0.000 claims abstract description 27
- 230000008929 regeneration Effects 0.000 claims abstract description 26
- 238000011069 regeneration method Methods 0.000 claims abstract description 26
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 17
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 claims abstract description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 8
- 239000011593 sulfur Substances 0.000 claims description 8
- 239000002918 waste heat Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 abstract description 21
- 238000000034 method Methods 0.000 abstract description 15
- 238000006555 catalytic reaction Methods 0.000 abstract description 6
- 230000008439 repair process Effects 0.000 abstract description 4
- 238000003915 air pollution Methods 0.000 abstract description 2
- 238000000605 extraction Methods 0.000 abstract 1
- 230000010354 integration Effects 0.000 abstract 1
- 239000007791 liquid phase Substances 0.000 abstract 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 24
- 238000006477 desulfuration reaction Methods 0.000 description 10
- 239000007789 gas Substances 0.000 description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 7
- 239000003546 flue gas Substances 0.000 description 7
- 230000007062 hydrolysis Effects 0.000 description 7
- 238000006460 hydrolysis reaction Methods 0.000 description 7
- 239000005864 Sulphur Substances 0.000 description 6
- 239000002826 coolant Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 230000023556 desulfurization Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 241000370738 Chlorion Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Abstract
The utility model discloses a kind of while removing cos, the device of carbon disulfide, belong to Air Pollution Control field.Device described in the utility model includes the heat-exchange system being made up of cooling tower and fixed bed reaction tower, the co-catalysis system being made up of stripper, spray column and communicating pipe, the continuous operational system being made up of two fixed bed reaction towers, the catalyst regeneration system being made up of heat-exchange system and regeneration spray system etc. are constituted.Fixed bed reaction tower I described in the utility model and fixed bed reaction tower II are in the stage of catalytic reaction and catalyst regeneration respectively, the continuous operation of system is ensure that by the exchange-column shift of magnetic valve, can be transferred to the elemental sulfur on decaying catalyst surface in liquid phase by regenerative process simultaneously, it is easy to the extraction of elemental sulfur in subsequent process, the device has high integration and automaticity.
Description
Technical field
The utility model is related to a kind of while removing cos, the device of carbon disulfide, belongs to Air Pollution Control field.
Background technology
As main organic sulfur, COS, CS2It is widely present in industrial smoke, for example yellow phosphoric tail gas, blast furnace tail gas etc..
Atmospheric environment is discharged into during industrial production and use, serious pollution and harm can be caused to environment and human body, industry
Micro CS in production2With COS to the toxic effect of catalyst, its catalytic effect and service life is set to be influenceed by serious,
CS2Also H can be generated by slow hydrolysis with COS2S, corrodes production equipment, is not only brought to industrial production very big
Economic loss, and equipment investment and product cost are increased, while COS and CS2Discharge be also waste to Sulphur ressource.
Catalyzed hydrolytic methods remove COS and CS2Principle be：COS and CS2Changed into vapor reaction on a catalyst
H2S, then H2S is removed in follow-up workshop section, and the reaction temperature of catalyzing hydrolysis is generally below 200 DEG C, and energy consumption is relatively low, secondary
Reaction is less, and contains the vapor needed for hydrolytic process in most of unstripped gas.At the same time, low-temperature catalyzed hydrolysis COS and
CS2Process can avoid the generation of the side reactions such as unstripped gas cracking, methanation, so the method turns into removing COS and CS at present2Grind
Study carefully one of focus in field.
Chinese patent CN 102886203A disclose the invention of " a kind of method of flue gas desulfurizing and hydrargyrum-removing ".The invention will contain
The water of chlorion is sprayed into circulating fluidized bed dry desulfuration demercuration dust arrester, then flue gas is purified.The method have compared with
Desulfuration efficiency high, but the sulfur-containing compound of removing is SO2, and without catalyst step for regeneration.Chinese patent CN
103432861A discloses the invention of " sintering desulfuration white-smoke-removing system and its technological process ".The invention is according to desulfurization, water removal, drop
The order of temperature is purified to white cigarette.The method is with desulfuration efficiency and relatively low energy consumption higher, but the Containing Sulfur of removing
Compound is SO2, and without catalyst step for regeneration.Chinese patent CN 103657368A disclose a kind of " simultaneous SO_2 and NO removal demercuration
The invention of dry-method fume gas purification method and device ".The invention removes SO by the way of absorption2, reduction mode remove NOx,
The mode of oxidation removes Hg.The method has desulfurization denitration demercuration efficiency higher, but the sulfur-containing compound of removing is SO2,
And without catalyst step for regeneration.Cos are removed while involved by the utility model, the device of carbon disulfide has efficiently
Desulfuration efficiency, and high degree of automation, integrated level be high, continuously-running, heat utilization ratio are high, sulfur recovery is convenient.
At present, on being strengthened with dilute sulfuric acid while removing cos, the device of carbon disulfide has not seen report.
The content of the invention
The purpose of this utility model is to provide a kind of while removing cos, the device of carbon disulfide, including waste heat pot
Stove 1, cooling tower 2, stripper 3, fixed bed reaction tower I 4, fixed bed reaction tower II 5, spray column 6, heat exchange pump I 7, heat exchange pump II
8th, regeneration pump 9, spray pump 10, communicating pipe 11, agitator 12, heat exchange jacket 13；Waste heat boiler 1 is connected with cooling tower 2, cooling tower
2 connect with stripper 3；Stripper 3 is connected with fixed bed reaction tower I 4 and fixed bed reaction tower II 5 respectively by three-way magnetic valve
It is logical；Fixed bed reaction tower I 4 and fixed bed reaction tower II 5 are connected by three-way magnetic valve with spray column 6；Stripper 3 and spray column
By connecting communicating pipe 11, the lower end of spray column 6 is connected by spray pump 10 with the top of spray column 6 for 6 lower end；Cooling tower 2,
Fixed bed reaction tower I 4, the inwall of fixed bed reaction tower II 5 are equipped with heat exchange jacket 13；Regeneration water tank passes through regeneration pump 9 and consolidates
Fixed bed reaction tower I 4 is connected with the top of fixed bed reaction tower II 5, fixed bed reaction tower I 4 and the bottom of fixed bed reaction tower II 5 with
Sulfur recovery facility is connected；The outlet of heat exchange pump II 8 is connected with the top of the internal heat chuck of cooling tower 2, is changed inside cooling tower 2
The bottom of thermal jacket by exchange heat pump I 7 respectively with fixed bed reaction tower I 4 and the top of the internal heat chuck of fixed bed reaction tower II 5
Portion connects, and the bottom of fixed bed reaction tower I 4 and the internal heat chuck of fixed bed reaction tower II 5 is by three-way magnetic valve and heat exchange
The entrance connection of pump II 8.
The bottom of stripper described in the utility model 3 and spray column 6 is respectively provided with agitator 12.
Fixed bed reaction tower I 4 described in the utility model, the inside of fixed bed reaction tower II 5 set regeneration flusher, bottom
Portion sets reservoir.
Principle of the present utility model：
Cooling tower 2 and fixed bed reaction tower I 4 and the composition heat-exchange system of fixed bed reaction tower II 5, cooling tower 2 absorb flue gas
Heat and be delivered in coolant, coolant after intensification flows into fixed bed reaction tower I 4 and fixed bed reaction tower II 5 is simultaneously put
Heat, maintains catalyst in a suitable reaction temperature, and the coolant after heat release is absorbed heat again in returning to cooling tower 2, from
And carry out recuperated cycle.
11 groups of co-catalysis systems of stripper 3, spray column 6 and communicating pipe are into from fixed bed reaction tower I 4 and fixed bed reaction
The accessory substance SO that tower II 5 is produced2Dilute sulfuric acid is formed in spray column, dilute sulfuric acid is back in stripper 3 by communicating pipe 11 again,
Dilute sulfuric acid in stripper 3 increases during fixed bed reaction tower I 4 and fixed bed reaction tower II 5 are brought into the presence of stripper
Strong catalyzing hydrolysis effect, so as to reach promoting catalysis.
Heat-exchange system and regeneration spray system composition regenerative system, regeneration enter the fixation in the regenerative process stage with water
Bed reaction tower II 5 and fixed bed reaction tower I 4, the sulfate and sulphur of catalyst surface are rinsed to bottom under spray effect
Reservoir, while catalyst is dried under the heating of heat-exchange system, the waste liquid in reservoir is carried for follow-up sulphur
Take operation.
Fixed bed reaction tower I 4 and the composition continuous operational system of fixed bed reaction tower II 5, when a fixed bed reaction tower I 4
During in course of reaction state, another fixed bed reaction tower II 5 is in the state of regenerative process 5 under the control of magnetic valve, often
Can automatically switch the working condition residing for two towers every certain hour magnetic valve, so as to reach the function of continuous operation.
Using hydrolyst, by micro water vapor in flue gas and O2, make COS, CS2Catalyzing hydrolysis are H simultaneously2S, has
The accessory substance SO produced under the conditions of oxygen2Continue to be oxidized to sulfuric acid in operation is sprayed, the dilute sulfuric acid of generation enters catalysis with air-flow
Operation, so as to strengthen desulfuration efficiency, desulfurization reaction temperature is：60 ~ 100 DEG C, COS and CS2Removal efficiency is higher than 90%, main anti-
Should be as follows：
The beneficial effects of the utility model：
（1）The heat-exchange system being made up of cooling tower and fixed bed reaction tower, efficiently make use of the temperature of flue gas itself, no
Catalyst is set to reach suitable reaction temperature by needing extra heat source；
（2）The co-catalysis system being made up of stripper, spray column and communicating pipe, can be by accessory substance SO2Recycle, produce
Dilute sulfuric acid enhanced effect can be played to catalyzing hydrolysis process；
（3）The catalyst regeneration system being made up of heat-exchange system and regeneration spray system, can be provided using heat-exchange system
Heat flash baking is carried out to catalyst, improve the utilization ratio of heat, the sulphur that contains in the waste liquid produced after regeneration
Sulphur can be reused；
（4）The agitator of spray column and stripper bottom is used to adjust the dilute sulfuric acid concentration in reservoir and reservoir between
Balance.
（5）The continuous operational system being made up of two fixed bed reaction towers, can utilize same set of heat-exchanger rig and regeneration
Device is catalyzed and regenerative process, can exchange-column shift characteristic, reaction system is continuously worked, and automaticity
High, integrated level is high.
Brief description of the drawings
Fig. 1 is the structural representation of device described in the utility model；
In figure：1- waste heat boilers；2- cooling towers；3- strippers；4- fixed bed reactions tower I；5- fixed bed reactions tower II；6-
Spray column；7- heat exchange pumps I；8- heat exchange pumps II；9- regeneration pumps；10- spray pumps；11- communicating pipes；12- agitators；13- heat exchange folders
Set.
Specific embodiment
The utility model is described in further detail with reference to specific embodiment, but the utility model protection domain is not limited
In content as described below.
Embodiment 1
Cos, carbon disulfide device, including waste heat boiler 1, cooling tower are removed described in the utility model embodiment simultaneously
2nd, stripper 3, fixed bed reaction tower I 4, fixed bed reaction tower II 5, spray column 6, heat exchange pump I 7, heat exchange pump II 8, regeneration pump 9,
Spray pump 10, communicating pipe 11, agitator 12, heat exchange jacket 13；Waste heat boiler 1 is connected with cooling tower 2, cooling tower 2 and stripper 3
Connection；Stripper 3 is connected with fixed bed reaction tower I 4 and fixed bed reaction tower II 5 respectively by three-way magnetic valve；Fixed bed is anti-
Tower I 4 and fixed bed reaction tower II 5 is answered to be connected with spray column 6 by three-way magnetic valve；The lower end of stripper 3 and spray column 6 passes through
Communicating pipe 11 is connected, and the lower end of spray column 6 is connected by spray pump 10 with the top of spray column 6；Cooling tower 2, fixed bed reaction
Tower I 4, the inwall of fixed bed reaction tower II 5 are equipped with heat exchange jacket 13；Regeneration water tank is by regeneration pump 9 and fixed bed reaction tower I
4 connect with the top of fixed bed reaction tower II 5, fixed bed reaction tower I 4 and the bottom of fixed bed reaction tower II 5 and Sulfur recycling installment
Put connection；The outlet of heat exchange pump II 8 is connected with the top of the internal heat chuck of cooling tower 2, the bottom of the internal heat chuck of cooling tower 2
Portion is connected by top of the pump I 7 respectively with fixed bed reaction tower I 4 and the internal heat chuck of fixed bed reaction tower II 5 that exchange heat, Gu
The bottom of fixed bed reaction tower I 4 and the internal heat chuck of fixed bed reaction tower II 5 is entered by three-way magnetic valve with the pump II 8 that exchanges heat
Mouth connection；The bottom of stripper 3 and spray column 6 is respectively provided with agitator 12；In fixed bed reaction tower I 4, fixed bed reaction tower II 5
Setting regeneration flusher, bottom set reservoir, as shown in Figure 1.
The use process of the present embodiment described device：
（1）Waste heat boiler 1 is first passed through by the high-temperature flue gas after pre- dust removal process be cooled to 150 DEG C, then by cooling tower 2
Heat exchange is carried out, flue-gas temperature is down to 60 DEG C, coolant is increased to 60 DEG C.
（2）It is 0.01mol/L by molar concentration in stripper 3 by the gas after cooling again by the effect of stripper 3
Dilute sulfuric acid bring into fixed bed reaction tower I 4 and fixed bed reaction tower II 5.
（3）Step（1）It is middle to absorb heat and the coolant inflow fixed bed reaction tower I 4 and fixed bed of 60 DEG C after heating up
In the heat exchange jacket of reaction tower II 5, the temperature of catalyst in fixed bed reaction tower I 4 and fixed bed reaction tower II 5 is brought up to 60
℃。
（4）The gas for carrying dilute sulfuric acid secretly is anti-in fixed bed reaction tower I 4 and the interior generation catalyzing hydrolysis of fixed bed reaction tower II 5
Should.
（5）The SO of generation2Enter spray column 6 with air-flow and produce sulfuric acid, sulfurous acid, sulfuric acid and sulfurous acid are by communicating pipe 11
Stripper 3 is back to, purified gas is discharged from outlet.
（6）Coolant reenters cooling tower 2 after heat release in fixed bed reaction tower I 4 and the chuck of fixed bed reaction tower II 5
Recycle.
（7）Regeneration water flows into fixed bed reaction tower I 4 and fixed bed reaction tower II 5 rinses decaying catalyst, by catalyst
The sulfate and elemental sulfur on surface are taken out of into sulphur recovery operation, by the catalyst after washing under the heat effect of chuck
Flash baking, forms regenerated catalyst.
The present embodiment used catalyst is by the activated-carbon catalyst Fe/AC of iron oxide modified.
By the device to sulfur-containing smoke gas（CS2Concentration 40ppm, COS concentration 500ppm, O2Concentration 1%, air speed 80000h-1）
Carry out desulfurization, 100% CS2Clearance and 100% COS clearances respectively reach 600min and 540min.This shows dress
Put with good desulfurized effect.
Claims (3)
1. a kind of at the same remove cos, the device of carbon disulfide, it is characterised in that：Including waste heat boiler（1）, cooling tower（2）、
Stripper（3）, fixed bed reaction tower I（4）, fixed bed reaction tower II（5）, spray column（6）, heat exchange pump I（7）, heat exchange pump II
（8）, regeneration pump（9）, spray pump（10）, communicating pipe（11）, agitator（12）, heat exchange jacket（13）；Waste heat boiler（1）With cooling
Tower（2）Connection, cooling tower（2）With stripper（3）Connection；Stripper（3）By three-way magnetic valve respectively with fixed bed reaction tower I
（4）With fixed bed reaction tower II（5）Connection；Fixed bed reaction tower I（4）With fixed bed reaction tower II（5）By three-way magnetic valve
With spray column（6）Connection；Stripper（3）And spray column（6）Lower end pass through communicating pipe（11）Connection, spray column（6）Lower end
By spray pump（10）With spray column（6）Top connection；Cooling tower（2）, fixed bed reaction tower I（4）, fixed bed reaction tower II
（5）Inwall be equipped with heat exchange jacket（13）；Regeneration water tank passes through regeneration pump（9）With fixed bed reaction tower I（4）It is anti-with fixed bed
Answer tower II（5）Top connection, fixed bed reaction tower I（4）With fixed bed reaction tower II（5）Bottom connects with sulfur recovery facility
It is logical；Heat exchange pump II（8）Outlet and cooling tower（2）The top connection of internal heat chuck, cooling tower（2）Internal heat chuck
Bottom is by the pump I that exchanges heat（7）Respectively with fixed bed reaction tower I（4）With fixed bed reaction tower II（5）The top of internal heat chuck
Connection, fixed bed reaction tower I（4）With fixed bed reaction tower II（5）The bottom of internal heat chuck passes through three-way magnetic valve and changes
Heat pump II（8）Entrance connection.
2. cos, the device of carbon disulfide are removed simultaneously according to claim 1, it is characterised in that：Stripper（3）And spray
Drench tower（6）Bottom be respectively provided with agitator（12）.
3. cos, the device of carbon disulfide are removed simultaneously according to claim 1, it is characterised in that：Fixed bed reaction tower I
（4）, fixed bed reaction tower II（5）Inside set regeneration flusher, bottom set reservoir.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621153197.3U CN206240324U (en) | 2016-10-31 | 2016-10-31 | It is a kind of to remove cos, carbon disulfide device simultaneously |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621153197.3U CN206240324U (en) | 2016-10-31 | 2016-10-31 | It is a kind of to remove cos, carbon disulfide device simultaneously |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206240324U true CN206240324U (en) | 2017-06-13 |
Family
ID=58996867
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621153197.3U Expired - Fee Related CN206240324U (en) | 2016-10-31 | 2016-10-31 | It is a kind of to remove cos, carbon disulfide device simultaneously |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206240324U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106621796A (en) * | 2016-10-31 | 2017-05-10 | 昆明理工大学 | Method and device for simultaneously removing carbonyl sulfide and carbon disulfide |
| CN113117470A (en) * | 2021-05-12 | 2021-07-16 | 昆明理工大学 | Method for tail gas desulfurization and sulfur recycling in low-temperature methanol washing process |
| CN114471108A (en) * | 2022-02-14 | 2022-05-13 | 北京科技大学 | Synchronous decarbonization denitration of industry flue gas and waste heat recovery utilize's device |
-
2016
- 2016-10-31 CN CN201621153197.3U patent/CN206240324U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106621796A (en) * | 2016-10-31 | 2017-05-10 | 昆明理工大学 | Method and device for simultaneously removing carbonyl sulfide and carbon disulfide |
| CN106621796B (en) * | 2016-10-31 | 2023-06-13 | 昆明理工大学 | Method and device for simultaneously removing carbonyl sulfide and carbon disulfide |
| CN113117470A (en) * | 2021-05-12 | 2021-07-16 | 昆明理工大学 | Method for tail gas desulfurization and sulfur recycling in low-temperature methanol washing process |
| CN114471108A (en) * | 2022-02-14 | 2022-05-13 | 北京科技大学 | Synchronous decarbonization denitration of industry flue gas and waste heat recovery utilize's device |
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