CN110498416A - A kind of system that coal-fired plant boiler flue gas synchronizes recycling carbon dioxide and nitrogen - Google Patents
A kind of system that coal-fired plant boiler flue gas synchronizes recycling carbon dioxide and nitrogen Download PDFInfo
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- CN110498416A CN110498416A CN201910746695.0A CN201910746695A CN110498416A CN 110498416 A CN110498416 A CN 110498416A CN 201910746695 A CN201910746695 A CN 201910746695A CN 110498416 A CN110498416 A CN 110498416A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 195
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 96
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 94
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 81
- 239000003546 flue gas Substances 0.000 title claims abstract description 67
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000004064 recycling Methods 0.000 title claims abstract description 30
- 239000007789 gas Substances 0.000 claims abstract description 66
- 101150107050 PSA2 gene Proteins 0.000 claims abstract description 30
- 238000000746 purification Methods 0.000 claims abstract description 26
- 230000006835 compression Effects 0.000 claims abstract description 18
- 238000007906 compression Methods 0.000 claims abstract description 18
- 238000003860 storage Methods 0.000 claims abstract description 16
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 11
- 238000011068 loading method Methods 0.000 claims abstract description 11
- 230000001360 synchronised effect Effects 0.000 claims abstract description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229960004424 carbon dioxide Drugs 0.000 claims description 88
- 238000001179 sorption measurement Methods 0.000 claims description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- 238000001035 drying Methods 0.000 claims description 20
- 238000001816 cooling Methods 0.000 claims description 19
- 238000006477 desulfuration reaction Methods 0.000 claims description 19
- 230000023556 desulfurization Effects 0.000 claims description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 238000005057 refrigeration Methods 0.000 claims description 14
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 9
- 239000003463 adsorbent Substances 0.000 claims description 8
- 239000008246 gaseous mixture Substances 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 7
- 230000008569 process Effects 0.000 claims description 5
- 239000012535 impurity Substances 0.000 claims description 4
- 230000003139 buffering effect Effects 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 239000003507 refrigerant Substances 0.000 claims description 3
- 230000000087 stabilizing effect Effects 0.000 claims description 3
- 229910002090 carbon oxide Inorganic materials 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims 1
- 230000000903 blocking effect Effects 0.000 abstract description 5
- 239000003245 coal Substances 0.000 abstract description 4
- 239000003517 fume Substances 0.000 abstract description 4
- 238000012423 maintenance Methods 0.000 abstract description 3
- 238000004140 cleaning Methods 0.000 abstract description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 26
- 229910021529 ammonia Inorganic materials 0.000 description 13
- 238000000926 separation method Methods 0.000 description 5
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 235000011089 carbon dioxide Nutrition 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000002156 adsorbate Substances 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007717 exclusion Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- 241001212038 Arcola Species 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000009972 noncorrosive effect Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009418 renovation Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
- C01B21/045—Physical processing only by adsorption in solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/0014—Physical processing by adsorption in solids
-
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to gas cleaning and technical field is utilized, the system that especially a kind of fire coal boiler fume synchronizes recycling carbon dioxide and nitrogen.The system of the synchronous recycling carbon dioxide of this kind of coal-fired plant boiler flue gas and nitrogen, including flue gas pretreatment system, PSA1 system, PSA2 system, carbon dioxide compression purification system, carbon dioxide rectifying storage system and the high-purity nitrogen system of PSA system.The system of a kind of synchronous recycling carbon dioxide of fire coal boiler fume of the invention and nitrogen, the carbon emission amount of flue gas can be greatly reduced, it being capable of the carbon dioxide in recovered flue gas, nitrogen simultaneously, and the concentration of carbon dioxide, nitrogen can be purified to technical grade, wherein industrial grade carbon-dioxide liquefiable is stored to finished pot, and equipped with bottling pump, Loading Pump, convenient for externally conveying in a variety of manners, obtained technical grade nitrogen then can further pressurize as needed, it is concentrated use in for industrial park, equipment operation stability is high, is not likely to produce blocking, easy to maintenance.
Description
Technical field
The present invention relates to gas cleaning and technical field is utilized, especially a kind of fire coal boiler fume is synchronous to recycle titanium dioxide
The system of carbon and nitrogen.
Background technique
With the development of process of industrialization, China's carbon dioxide has been cured 10,000,000,000 tons as the discharge amount of exhaust gas every year.Dioxy
Change carbon source mainly have natural gas extraction and its burning, Ammonia Production, petroleum refining industry, steel industry, boiler combustion,
Coke and heavy oil combustion.The discharge of excessive carbon dioxide, will cause greenhouse effects, bring very big harm to environment.Therefore it controls
The discharge amount of carbon dioxide processed, and the carbon dioxide recovery to discharge, utilization, it has also become the problem of countries in the world are extremely paid close attention to.
Nitrogen is a kind of compressed coefficient and all very big gas of volume factor, and solubility is small in water, non-ignitable also because it is inert gas
It burns, it is nontoxic, non-corrosive；Frequently as the important gas source in industrial production, for protecting air and heat work instrument compressed gas source etc..
In recent years, China carry forward vigorously coal-fired arcola eliminate renovation, developing industry garden central heating form, with
This improves efficiency of energy utilization, reduces air pollution emission object.This is for the Thermal Power Enterprises of garden central heating, by right
The trapping of nitrogen in boiler smoke, and by means of piping lane in garden, by nitrogen centralizedly supply, it is whole can not only to reduce industrial park
Investment of the body to nitrogen production equipment can also increase profit, mutual reciprocity and mutual benefit for Thermal Power Enterprises；Simultaneously by boiler smoke
Collecting carbonic anhydride, recycling, sell in industries such as food processing, oil exploitations, further creates imitating for Thermal Power Enterprises and beat
Lower basis.
Chinese patent application CN107899376A discloses the joint trapping recycling of a kind of carbon dioxide in flue gas and nitrogen
Device and method, the device include smoke processing system, the first CO2 film separation unit, the 2nd CO2 film separation unit and N2 film
Separative unit.The device has the high enrichment degree to carbon dioxide, and can recycle nitrogen, avoids the wasting of resources.But the dress
Set it is not comprehensive to carbon dioxide and nitrogen treatment when in use, although trapping effect it is good cannot to carbon dioxide and nitrogen into
Row purification, and blocking is easy to produce in equipment use process, inconvenient maintenance after blocking.
Summary of the invention
The purpose of the present invention is to provide a kind of coal-fired plant boiler flue gases to synchronize the system for recycling carbon dioxide and nitrogen,
Overcome aforementioned the deficiencies in the prior art, simultaneously purifying carbon dioxide and nitrogen is thoroughly trapped comprehensively, to the carbon dioxide in flue gas
And nitrogen synchronizes recycling, greatly reduces carbon emission amount in flue gas, equipment operation stability is high, is not likely to produce blocking, repairs
It is convenient.
The technical scheme adopted by the invention to solve the technical problem is that:
A kind of system that coal-fired plant boiler flue gas synchronizes recycling carbon dioxide and nitrogen, including flue gas pretreatment system,
PSA1 system, PSA2 system, carbon dioxide compression purification system, carbon dioxide rectifying storage system, the high-purity nitrogen system of PSA system；
The flue gas pretreatment system is used for from boiler flue gas cool-down, dehydration；After PSA1 system is for pressure-variable adsorption pretreatment
Flue gas, nitrogen and oxygen is discharged；PSA2 system is used for the further pressure-variable adsorption of carbon dioxide in PSA1 system stripping gas
Purification；Carbon dioxide compression purification system goes moisture removal and corrosion for pressurized liquefied to PSA2 system carbon dioxide gas
Property impurity；Rectifying storage system is used to pass through rectifying column further essence purification to the carbon dioxide of CO 2 purification system output
Afterwards, in storage to finished pot；The high-purity nitrogen system of PSA system is used to become to what is excluded in PSA1 system containing nitrogen, oxygen flue gas
Pressure absorption, is discharged high pure nitrogen.
Further, the flue gas pretreatment system includes: air-introduced machine, the first cooler, water distributing can, wherein boiler smoke
Road is connected with air-introduced machine entrance by pipeline；First cooler hot arc entrance is exported with air-introduced machine to be connected by pipeline；Point
Water pot is exported with the first cooler hot arc to be connected by pipeline；Exhaust outlet at the top of first compressor inlet and water distributing can is logical
Piping is connected.
Further, the PSA1 system, by multiple adsorption tower groups at filling adsorbent in adsorption tower；Adsorption tower
Absorption is carried out and by oxygen, nitrogen by being expelled to gaseous mixture main pipe at the top of adsorption tower to carbon dioxide, inverse put stripping gas has suction
Attached tower bottom is discharged into stripping gas main pipe；In the process of running, every adsorption tower all needs experience absorption, presses in PSA1 system
Drop, inverse put, pressure rise, the working stage that finally boosts, the adsorption tower in PSA1 system according to actual needs, at partial adsorbates tower
In absorption phase, remaining adsorption tower is then in the regenerated different phase of bed body.PSA1 system adsorption tower passes through inverse put, finally will
The control of carbon dioxide volumetric concentration is in 40%-45% in stripping gas；PSA1 system stripping gas main pipe passes through pipeline and the second compression
Machine entrance is connected.
Further, first compressor outlet is connected by pipeline with PSA1 system inlet main pipe.
Further, the PSA2 system is by multiple adsorption tower groups at filling adsorbent in adsorption tower；PSA2 system
Inlet main pipe be connected by pipeline with the second compressor outlet；PSA2 system be can by by the second compressor convey by
The system that the stripping gas of PSA1 system output carries out pressure-variable adsorption, the stripping gas main pipe of PSA2 system are pumped by pipeline and vacuum
Mouth connection；The working stage that every adsorption tower all needs experience adsorb, equal pressure drop, vacuumize, pressure liter, finally boosts；PSA2 system
According to actual needs, partial adsorbates tower is in absorption phase to adsorption tower in system, and it is regenerated not that remaining adsorption tower is then in bed body
The same stage.PSA2 system adsorption tower is vacuumized by vacuum pump, finally that the volume that air carbon dioxide is desorbed in PSA2 system is dense
Degree control is 95%.
Further, the carbon dioxide compression purification system includes surge tank, the second cooler, water distributing can, third
Compressor, vacuum tank, desulfurization bed, drying bed, third cooler, forecooler, liquefier and refrigeration system, wherein surge tank entrance
Be connected by pipeline with vacuum pump outlet, to by vacuum pump conveying Lai the stripping gas of PSA2 system carry out buffering pressure stabilizing；The
Two cooler hot arc entrances are connected by pipeline with surge tank outlet, and water distributing can entrance passes through with the outlet of the second cooler hot arc
Pipeline is connected；Third compressor inlet is connected with the exhaust outlet at the top of water distributing can by pipeline；Third compressor outlet with
Vacuum tank entrance is connected by pipeline；Vacuum tank outlet is connected with desulfurization bed entrance by pipeline；Desulfurization bed is exported and is done
Dry bed entrance is connected by pipeline, and drying bed outlet is connected with third cooler hot arc entrance by pipeline；Third is cooling
The outlet of device hot arc is connected with forecooler hot arc entrance by pipeline, and the outlet of forecooler hot arc passes through pipe with liquefier hot arc entrance
Road is connected.
Further, the desulfurization bed in the carbon dioxide compression purification system is the sulphur for going in removing carbon dioxide
The complete set of equipments divided；Drying bed is the complete set of equipments for being dehydrated to carbon dioxide；It is complete to guarantee economy
Desulfurization bed apparatus, set of dry bed apparatus should all have attached generating apparatus again；Make desulfurization bed, filler regeneration in drying bed.
Further, the carbon dioxide rectifying storage system includes rectifying column, subcooler, finished pot, product car-loading
Pump, finished product bottling pump and refrigeration system, wherein rectifying column inlet exports with liquefier hot arc and is connected by pipeline；Subcooler heat
Section entrance is connected with rectifying tower bottom outlet；The liquid refrigerant that rectifier complete condenser is generated by refrigeration system into
Row cooling condensation；The outlet of rectifier complete condenser is connected by pipeline with finished pot bottom inlet, finished pot bottom inlet
It exports with subcooler hot arc and is connected by pipeline；Product car-loading pump intake, finished product bottling pump intake are respectively at finished product pot bottom
It is connected by pipeline.
Further, the forecooler cold-side inlet in the carbon dioxide compression purification system and rectifying column top vent
Mouth is connected by pipeline, the cooling capacity of rectifying column top vent is recycled, by the further cooling of carbon dioxide through third cooler
Cooling, and then improve the thermal efficiency and economy of whole system.
Further, the carbon dioxide compression purification system, the refrigeration system in rectifying storage system be simultaneously to
Second cooler, liquefier, rectifier complete condenser provide cold source, and are able to satisfy the gas in rectifier complete condenser
The complete set of equipments of liquid is condensed into the gas cooling in liquefier, refrigerant used in refrigeration system should meet national correlation
Environmental requirement.According to actual production place and condition, the cold source that cooler can not use refrigeration system to provide uses circulating cooling
Water carries out cooling, can save the investment to refrigeration system in this way.
Further, the high-purity nitrogen system of PSA system is by multiple adsorption tower groups arranged side by side at adsorption tower is filled with carbon point
Son sieve；The high-purity nitrogen system of PSA system is used to adsorb exclusion gaseous mixture at the top of PSA1 system adsorption tower, and high-purity in PSA system
Discharge concentration is the complete set of equipments of 99.9% high pure nitrogen at the top of nitrogen system adsorption tower；The inlet main pipe of the high-purity nitrogen system of PSA system
It is connected with the gaseous mixture main pipe of PSA1 system by pipeline.
The beneficial effects of the present invention are: compared with prior art, a kind of coal-fired plant boiler flue gas of the invention synchronizes back
The system for receiving carbon dioxide and nitrogen has the advantage that the synchronous recycling titanium dioxide of (1) coal-fired plant boiler flue gas of the invention
The system of carbon and nitrogen can greatly reduce the carbon emission amount of flue gas；(2) coal-fired plant boiler flue gas of the invention synchronizes back
The system for receiving carbon dioxide and nitrogen, can the carbon dioxide in recovered flue gas, nitrogen simultaneously, and can be by carbon dioxide, nitrogen
Concentration purify to technical grade, wherein industrial grade carbon-dioxide liquefiable is stored to finished pot, and equipped with bottling pump, entrucking
Pump, convenient for externally conveying in a variety of manners, obtained technical grade nitrogen then can further pressurize as needed, for industrial park collection
Middle use；(3) system of the synchronous recycling carbon dioxide of coal-fired plant boiler flue gas of the invention and nitrogen, equipment operation stability
Height is not likely to produce blocking, easy to maintenance.
Detailed description of the invention
Fig. 1 is the flow chart of the system of the synchronous recycling carbon dioxide of coal-fired plant boiler flue gas of the invention and nitrogen；
Fig. 2 is the flue gas pretreatment of the system of the synchronous recycling carbon dioxide of coal-fired plant boiler flue gas of the invention and nitrogen
The flow chart of system；
Fig. 3 is the pressurized carbon dioxide of the system of the synchronous recycling carbon dioxide of coal-fired plant boiler flue gas of the invention and nitrogen
The flow chart of contracting purification system；
Fig. 4 is the titanium dioxide carbon of the system of the synchronous recycling carbon dioxide of coal-fired plant boiler flue gas of the invention and nitrogen
Evaporate the flow chart of storage system；
Wherein, 1 flue gas pretreatment system, 101 air-introduced machines, 102 first coolers, 103 water distributing cans, 2PSA1 system,
3PSA2 system, 4 carbon dioxide compression purification systems, 401 surge tanks, 402 second coolers, 403 water distributing cans, the compression of 404 thirds
Machine, 405 vacuum tanks, 406 desulfurization beds, 407 drying beds, 408 third coolers, 409 forecoolers, 410 liquefiers, 5 rectifying storage
System, 501 rectifying columns, 502 subcoolers, 503 finished pots, 504 product car-loadings pump, 505 finished products bottling pump, 6PSA High Purity Nitrogen system
System, 7 first compressors, 8 second compressors, 9 vacuum pumps, 10 refrigeration systems.
Specific embodiment
In order to make the object, technical scheme and advantages of the embodiment of the invention clearer, below in conjunction with the embodiment of the present invention
In attached drawing, technical scheme in the embodiment of the invention is clearly and completely described.
Embodiment 1
The present invention is applied to reach national minimum discharge standard fire coal boiler fume trapping and recycling.It is coal-fired in the present embodiment
The flue gas condition of boiler are as follows: 50 DEG C of flue-gas temperature, carbon dioxide in flue gas content is 13%, and the content of nitrogen in flue gas is
71%, the content of oxygen is 6% in flue gas, and the content of sulfur dioxide in flue gas is 35mg/Nm3, nitrogen oxides in effluent contains
Amount is 50mg/Nm3, the content of vapor is 12% in flue gas.
As shown in Figure 1, the present invention includes flue gas pretreatment system 1, PSA1 system 2, PSA2 system 3, carbon dioxide compression
Purification system 4, carbon dioxide rectifying storage system 5, the high-purity nitrogen system 6 of PSA system.The flue gas pretreatment system 1 for pair
From boiler flue gas cool-down, dehydration；PSA1 system 2 is used for the pretreated flue gas of pressure-variable adsorption, and nitrogen and oxygen is discharged；PSA2
System 3 is for further adsorbing purification to the carbon dioxide in 2 stripping gas of PSA1 system；Carbon dioxide compression purification system 4 is used
In the carbon dioxide pressurization liquefaction to 3 desorption of PSA2 system, moisture removal and corrosive impurity are removed；Rectifying storage system 5 is used for
After being purified to the carbon dioxide of 4 output of CO 2 purification system by the further essence of rectifying column, in storage to pressurized tank；PSA
High-purity nitrogen system 6 is made for carrying out pressure-variable adsorption, discharge containing the oxygen in nitrogen, oxygen flue gas to what is excluded in PSA1 system 2
High pure nitrogen.
As shown in Fig. 2, the flue gas pretreatment system 1 includes: air-introduced machine 101, the first cooler 102, water distributing can
103, wherein boiler flue is connected with 101 entrance of air-introduced machine by pipeline；First cooler, 102 hot-side inlet and air-introduced machine
101 outlets are connected by pipeline, and flue gas is forced into 0.1Mpa by air-introduced machine 101 and introduces the first cooler 102, by the
Flue-gas temperature is cooled to 40 DEG C by 50 DEG C by one cooler 102；Water distributing can 103 is connected with the first cooler 102 by pipeline,
In the present embodiment, the first cooler 102 is cooling using industrial circulating water；Water distributing can 103 is after cooling by the first cooler 102
Moisture separation in flue gas；First compressor, 7 air inlet is connected with the exhaust outlet at 103 top of water distributing can by pipeline, and first
The dry flue gas excluded at the top of water distributing can 103 is forced into 1Mpa by compressor 7, is sent into the adsorption tower of PSA1 system 2.
In the present embodiment, the PSA1 system 2, by multiple adsorption tower groups at filling adsorbent in adsorption tower.PSA1
2 adsorption tower of system adsorbs the flue gas for having the conveying of the first compressor 7, and by oxygen, nitrogen etc. by excluding (top at the top of adsorption tower
Carbon dioxide gas containing 3%-5% in the mixed gas that portion excludes) to 2 gaseous mixture main pipe of PSA1 system, inverse put stripping gas
There is absorption tower bottom to be discharged into stripping gas main pipe.In the process of running, every adsorption tower all needs experience to inhale in PSA1 system (2)
Attached, equal pressure drop, inverse put, the working stage pressure liter, finally boosted.2 adsorption tower of PSA1 system is by inverse put, finally by stripping gas
Middle carbon dioxide volumetric concentration control is 45%；The pressure of stripping gas is 10-20Kpa.2 stripping gas main pipe of PSA1 system passes through pipe
Road is connected with 8 entrance of the second compressor, and the stripping gas in PSA1 system 2 is forced into 0.3Mpa and is delivered to by the second compressor 8
PSA2 system 3, the second compressor 8 in this programme are because there are surge phenomena for centrifugal compressor using centrifugal compressor
Guarantee in certain condition range can stable operation, the present embodiment uses three centrifugal compressors, and dual-purpose one is standby.
In the present embodiment, the PSA2 system 3 is made of side by side multiple adsorption towers, and adsorbent is filled in adsorption tower.
3 inlet main pipe of PSA2 system is connected by pipeline with the outlet of the second compressor 8.PSA2 system 3 is will to compress by second
The system adsorbed by the stripping gas of 2 output of PSA1 system that machine 8 conveys, the stripping gas main pipe of PSA2 system 3 pass through pipeline
It is connect with 9 entrance of vacuum pump, vacuum pump 9 uses Roots vaccum pump in the present embodiment；Every adsorption tower all needs experience to adsorb,
Pressure drop, the working stage for vacuumizing, pressure liter, finally boosting；The adsorption tower of PSA2 system 3 is vacuumized by vacuum pump 9, finally
The volumetric concentration that air carbon dioxide is desorbed in PSA2 system 3 is controlled 95%, the pressure of stripping gas is 10-15Kpa at this time.
As shown in figure 3, the carbon dioxide compression purification system 4 includes surge tank 401, the second cooler 402, Fen Shui
Tank 403, third compressor 404, vacuum tank 405, desulfurization bed 406, drying bed 407, third cooler 408, forecooler 409, liquid
Change device 410, wherein 401 entrance of surge tank is connected by the outlet of pipeline and vacuum pump 9, to by the conveying of vacuum pump 9 Lai PSA2
The stripping gas of system 3 carries out buffering pressure stabilizing, by pressure control within the scope of 0.11 ± 0.05Mpa；Second cooler, 402 hot arc
Entrance is connected by pipeline with the outlet of surge tank 401, and the second cooler 402 cools down to stripping gas, and temperature is dropped by 45 DEG C
To 25 DEG C, because cooling extent is big herein, and the mean temperature of this embodiment enforcement place recirculated cooling water whole year is 25 DEG C, can not
Meet the cooling requirement of stripping gas；The second cooler 402 is cooled down by the liquefied ammonia that Ammonia Refrigerating Equipment generates herein thus.Point
403 entrance of water pot is exported with 402 hot arc of the second cooler to be connected by pipeline, and water distributing can 403 will be in stripping gas after cooling
Moisture separation；404 import of third compressor is connected with the exhaust outlet at 403 top of water distributing can by pipeline, third compressor
404 pairs of drying stripping gas for having water distributing can 403 to be discharged carry out being forced into 2.5Mpa and are delivered to vacuum tank 405；Third compressor 404
Outlet is connected with 405 entrance of vacuum tank by pipeline, and the outlet of vacuum tank 405 is connected with 406 entrance of desulfurization bed by pipeline；
Desulfurization bed 406 adsorbs the corrosive elements such as sulphur content in stripping gas, to carry out pretreatment into drying bed 407；Desulfurization
406 outlet of bed is connected with 407 entrance of drying bed, and the desorption of moisture is precipitated because of the pressurization of third compressor 404 for 407 pairs of drying bed
Gas is adsorbed, and dry stripping gas is excluded, and the outlet of drying bed 407 is connected with 408 hot arc entrance of third cooler；Third is cold
But 408 hot arc of device outlet is connected with 409 hot arc entrance of forecooler, in order to improve the thermal efficiency, in forecooler 409 and drying bed
Third cooler 408 is provided between 407, dry stripping gas passes sequentially through third cooler 408, forecooler 409 to carry out
It is cooling.The temperature of stripping gas is down to 40 DEG C, in the present embodiment by 80 DEG C by third cooler 408, and third cooler 408 is used and followed
Ring water carries out just cooling to stripping gas；Forecooler 409 is cooled down twice the stripping gas just to cool down, at this time the temperature of stripping gas
35 DEG C are cooled to by 40 DEG C, forecooler 409 carries out secondary drop to stripping gas as cold source using the exhaust that do not coagulate at the top of rectifying column
Temperature, the cooling capacity of the not solidifying exhaust of recycling rectifying column.The outlet of 409 hot arc of forecooler is connected with 410 hot arc entrance of liquefier by pipeline
It connects, liquefier 410 will further be cooled down by the stripping gas of 409 reducing temperature twice of forecooler, and the temperature of stripping gas is down to -18 by 35 DEG C
DEG C, and finally liquefy；The liquefied ammonia that liquefier 410 is generated using Ammonia Refrigerating Equipment in the present embodiment is as cold source.
In the present embodiment, the desulfurization bed 406 in the carbon dioxide compression purification system 4 is for removing removing carbon dioxide
In sulphur content complete set of equipments；Drying bed 407 is the complete set of equipments for being dehydrated to carbon dioxide.The present embodiment
The middle bed body for being all made of temp.-changing adsorption using desulfurization bed 406, drying bed 407 removes moisture removal and corrosive impurity；It is economical to guarantee
Property, set of 406 equipment of desulfurization bed, 407 equipment of set of drying bed have attached generating apparatus again, make desulfurization bed 406, drying
Filler regeneration in bed 407；Desulfurization bed, drying bed are designed to the cylinder-shaped adsorbent bed of two same volumes, each absorption simultaneously
It is equipped with etc. the adsorbent of weight, two beds absorption and regenerative process alternate operation in bed, production is kept to be carried out continuously.
As shown in figure 4, the carbon dioxide rectifying storage system 5 includes rectifying column 501, subcooler 502, finished pot
503, product car-loading pump 504, finished product bottling pump 505, wherein 501 entrance of rectifying column and the outlet of 410 hot arc of liquefied gas pass through pipeline
It is connected, contains light component in the stripping gas through overcompression purification system 4, into after rectifying column 501, tower top separates argon gas, oxygen
The incoagulable gas such as gas, nitrogen (light component), tower bottom obtain the liquid CO 2 that purity reaches 99.9% or more；This embodiment
For investment reduction cost, spy uses using 501 bottom reboiler of rectifying column as the condenser in ammonia refrigeration system, will be by ammonia refrigeration
Gaseous ammonia in system after screw pump pressurization heating is cooled to saturation temperature, boils after the liquid absorption ammonia heat in reboiler
It rises, and completes circulation in tower；501 complete condenser of rectifying column is cooled down using the liquefied ammonia that Ammonia Refrigerating Equipment generates, in the present embodiment
The liquid that complete condenser condenses all flows back, and completes circulation in tower.502 hot arc entrance of subcooler and 501 tower bottom of rectifying column are arranged
Outlet is connected, and (gas phase carbon dioxide accounts for about 4% to the carbon dioxide that subcooler 502 excludes 501 bottom of rectifying column, remaining is
Liquid phase carbon dioxide) cool down and is down to -23 DEG C by -15 DEG C, obtain that there is certain degree of supercooling liquid phase carbon dioxide, at this time to convey
It is stored in finished pot 503, the liquefied ammonia that subcooler 502 is generated using Ammonia Refrigerating Equipment in the present embodiment is as cold source to liquid phase two
Carbonoxide is cooled down；503 bottom inlet of finished pot is connected with the outlet of subcooler 502；Product car-loading pumps 504 entrances, finished product
Bottling 505 entrances of pump are connected respectively at finished product pot bottom by pipeline, and product car-loading pump 504, finished product bottling pump 505 are used respectively
It is operated in by carbon dioxide entrucking, the bottling in finished pot 503.In the present embodiment, finished pot is designed as two, two finished pots
Between design have balance pipe；Product car-loading pump, finished product bottling pump are both designed as two, the using and the reserved, during operation easy to produce
Service work.
In the present embodiment, the high-purity nitrogen system 6 of the PSA system is by multiple adsorption tower groups at adsorption tower is filled with carbon point
Son sieve.The high-purity nitrogen system 6 of PSA system is used to adsorb exclusion gaseous mixture at the top of 2 adsorption tower of PSA1 system, and high in PSA system
Discharge concentration is the complete set of equipments of 99.9% high pure nitrogen, PSA High Purity Nitrogen system in the present embodiment at the top of 6 adsorption tower of purity nitrogen system
6 stripping gas of uniting can get the mixed gas that oxygen concentration is 36%., the inlet main pipe and PSA1 system of the high-purity nitrogen system 6 of PSA system
2 gaseous mixture main pipe is connected by pipeline.
In the present embodiment, pass through the system of the synchronous recycling carbon dioxide of coal-fired plant boiler flue gas and nitrogen, it is possible to reduce
The carbon emission amount of flue gas.It can the carbon dioxide in recovered flue gas, nitrogen simultaneously；And the concentration of carbon dioxide, nitrogen can be mentioned
It is pure to technical grade.Wherein industrial grade carbon-dioxide liquefiable is stored to finished pot, and equipped with bottling pump, Loading Pump, convenient for
Various forms externally conveys；Obtained technical grade nitrogen then can further pressurize as needed, and being delivered to chemical industry plant area and concentrating makes
Boiler combustion exhausted wind is introduced by the oxygen that PSA high-purity nitrogen generation system desorbs with, and then reduces going out for boiler system pressure fan
Power reduces boiler factory and runs power consumption.So far resource utilization can be obtained in the gas that flue gas separation and desorption go out.
Above-mentioned specific embodiment is only specific case of the invention, and scope of patent protection of the invention includes but is not limited to
The product form and style of above-mentioned specific embodiment, any claims of the present invention and any technical field of meeting
The appropriate changes or modifications that those of ordinary skill does it, all shall fall within the protection scope of the present invention.
Claims (10)
1. the system of a kind of synchronous recycling carbon dioxide of coal-fired plant boiler flue gas and nitrogen, it is characterised in that: including for pair
For the pretreated flue gas of pressure-variable adsorption and nitrogen is discharged in flue gas pretreatment system (1) from boiler flue gas cool-down and dehydration
The PSA1 system (2) of gas and oxygen is used for the further Pressure Swing Adsorption of carbon dioxide in PSA1 system (2) stripping gas
PSA2 system (3), for pressurized liquefied to PSA2 system (3) carbon dioxide gas and go the two of moisture removal and corrosive impurity
Carbonoxide compress purification system (4), for the carbon dioxide of carbon dioxide compression purification system (4) output by rectifying column into
After the purification of one step essence storage in finished pot rectifying storage system (5), for being discharged in PSA1 system (2) containing nitrogen and
The flue gas of oxygen carries out pressure-variable adsorption and the high-purity nitrogen system of PSA system (6) of high pure nitrogen is discharged.
2. the system that a kind of coal-fired plant boiler flue gas according to claim 1 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the flue gas pretreatment system (1) includes air-introduced machine (101), the first cooler (102) and water distributing can (103),
Boiler flue is connected with the air-introduced machine (101) entrance by pipeline, the first cooler (102) hot-side inlet and air-introduced machine
(101) outlet is connected by pipeline, and water distributing can (103) entrance is exported with the first cooler (102) hot arc to be connected by pipeline
It connects.
3. the system that a kind of coal-fired plant boiler flue gas according to claim 2 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the PSA1 system (2) is made of side by side multiple adsorption towers, and adsorbent, adsorption tower are filled in the adsorption tower
Absorption is carried out and by oxygen, nitrogen by being expelled to gaseous mixture main pipe at the top of adsorption tower to carbon dioxide, inverse put stripping gas has suction
Attached tower bottom is discharged into stripping gas main pipe；In the process of running, every adsorption tower all needs experience to adsorb, in PSA1 system (2)
Pressure drop, inverse put, the working stage pressure liter, finally boosted.
4. the system that a kind of coal-fired plant boiler flue gas according to claim 3 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the exhaust outlet at the top of water distributing can (103) in the flue gas pretreatment system (1) passes through pipeline and the first compressor
(7) air inlet is connected, and the gas outlet of first compressor (7) is connected by pipeline with PSA1 system (2) inlet main pipe
It connects.
5. the system that a kind of coal-fired plant boiler flue gas according to claim 4 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the PSA2 system (3) is made of side by side multiple adsorption towers, and adsorbent, every adsorption tower are filled in adsorption tower
The working stage for all needing experience experience adsorb, equal pressure drop, vacuumize, pressure liter, finally boost.
6. the system that a kind of coal-fired plant boiler flue gas according to claim 5 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: stripping gas main pipe is connected by pipeline with the entrance of the second compressor (8) in the PSA1 system (2), and second
The outlet of compressor (8) is connected by pipeline with the inlet main pipe in PSA2 system (3), PSA2 system (3) to pass through second
The stripping gas of PSA1 system (2) output that compressor (8) conveying comes carries out pressure-variable adsorption.
7. the system that a kind of coal-fired plant boiler flue gas according to claim 6 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the carbon dioxide compression purification system (4) includes surge tank (401), the second cooler (402), water distributing can
(403), third compressor (404), vacuum tank (405), desulfurization bed (406), drying bed (407), third cooler (408), pre-
The hot arc entrance of cooler (409), liquefier (410) and refrigeration system (10), the second cooler (402) passes through pipeline and surge tank
(401) outlet is connected, and the entrance of water distributing can (403) is exported with the second cooler (402) hot arc to be connected by pipeline；The
The import of three compressors (404) is connected with the exhaust outlet at the top of water distributing can (403) by pipeline；Third compressor (404)
Outlet is connected with the entrance of vacuum tank (405) by pipeline, and the outlet of vacuum tank (405) and the entrance of desulfurization bed (406) are logical
Piping is connected, and the outlet of desulfurization bed (406) is connected with the entrance of drying bed (407) by pipeline, drying bed (407)
Outlet is connected with the hot arc entrance of third cooler (408) by pipeline, the hot arc outlet and pre-cooling of third cooler (408)
The hot arc entrance of device (409) is connected by pipeline, and the outlet of forecooler (409) hot arc and the hot arc entrance of liquefier (410) are logical
Piping is connected；The stripping gas main pipe of the PSA2 system (3) is connect by pipeline with the entrance of vacuum pump (9), described slow
The entrance for rushing tank (401) is connected by pipeline with the outlet of vacuum pump (9), surge tank (401) to by vacuum pump (9) convey Lai
The stripping gas of PSA2 system (3) carry out buffering pressure stabilizing.
8. the system that a kind of coal-fired plant boiler flue gas according to claim 7 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the carbon dioxide rectifying storage system (5) includes rectifying column (501), subcooler (502), finished pot
(503), product car-loading pump (504), finished product bottling pump (505) and refrigeration system (10), wherein the entrance and liquid of rectifying column (501)
Change the outlet of device (410) hot arc to be connected by pipeline, the hot arc entrance and rectifying column (501) tower bottom outlet of subcooler (502)
It is connected, the complete condenser on rectifying column (501) top carries out cooling condensation by the liquid refrigerant that refrigeration system (10) generates, essence
It evaporates the outlet of tower (501) top complete condenser to be connected with finished pot (503) bottom inlet by pipeline, finished pot (503) bottom
Entrance is exported with subcooler (502) hot arc to be connected by pipeline；Product car-loading pump (504) entrance, finished product bottling pump (505) enter
Mouth is connected with finished pot (503) bottom by pipeline respectively；Forecooler in the carbon dioxide compression purification system (4)
(409) cold-side inlet is connected with rectifying column (501) top vent by pipeline, recycling rectifying column (506) top vent
Cooling capacity.
9. the system that a kind of coal-fired plant boiler flue gas according to claim 8 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: refrigeration system (10) in the carbon dioxide compression purification system (4) and rectifying storage system (5) is simultaneously to the
Two coolers (402), liquefier (410), rectifying column (501) top complete condenser provide cold source, and to be able to satisfy rectifying column
(501) the gas cooling in the gas in the complete condenser of top and liquefier (410) is condensed into the complete set of equipments of liquid.
10. the system that a kind of coal-fired plant boiler flue gas according to claim 9 synchronizes recycling carbon dioxide and nitrogen,
Be characterized in that: the high-purity nitrogen system of PSA system (6) is made of side by side multiple adsorption towers, and adsorption tower is filled with carbon molecular sieve,
Inlet main pipe in the high-purity nitrogen system of PSA system (6) is connected with the gaseous mixture main pipe of PSA1 system (2) by pipeline.
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| CN201910746695.0A CN110498416A (en) | 2019-08-14 | 2019-08-14 | A kind of system that coal-fired plant boiler flue gas synchronizes recycling carbon dioxide and nitrogen |
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| CN111514694A (en) * | 2020-04-29 | 2020-08-11 | 中国建材国际工程集团有限公司 | Glass flue gas recovery method |
| CN112938975A (en) * | 2021-02-18 | 2021-06-11 | 杭州京旺科技有限公司 | Carbon dioxide enrichment facility in flue gas |
| CN113028844A (en) * | 2021-04-02 | 2021-06-25 | 攀枝花攀钢集团设计研究院有限公司 | Blast furnace hot blast stove flue gas waste heat recovery device and recovery method |
| CN113975950A (en) * | 2021-11-04 | 2022-01-28 | 大连理工大学 | System and method for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method |
| CN115350581A (en) * | 2022-08-16 | 2022-11-18 | 西南化工研究设计院有限公司 | Method for capturing and comprehensively utilizing carbon dioxide |
| CN115364618A (en) * | 2022-08-16 | 2022-11-22 | 西南化工研究设计院有限公司 | Flue gas separation and comprehensive utilization method |
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| CN115350581A (en) * | 2022-08-16 | 2022-11-18 | 西南化工研究设计院有限公司 | Method for capturing and comprehensively utilizing carbon dioxide |
| CN116651839A (en) * | 2023-05-31 | 2023-08-29 | 江苏省特种设备安全监督检验研究院 | Automatic cleaning mechanism for boiler water level gauge |
| CN118031530A (en) * | 2024-04-11 | 2024-05-14 | 杭氧集团股份有限公司 | Device for producing liquid by using flue gas with low energy consumption and use method thereof |
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