WO2014026641A1 - Appareil et procédé utilisant le cao comme vecteur pour la capture par cycles de dioxyde de carbone - Google Patents

Appareil et procédé utilisant le cao comme vecteur pour la capture par cycles de dioxyde de carbone Download PDF

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Publication number
WO2014026641A1
WO2014026641A1 PCT/CN2013/081642 CN2013081642W WO2014026641A1 WO 2014026641 A1 WO2014026641 A1 WO 2014026641A1 CN 2013081642 W CN2013081642 W CN 2013081642W WO 2014026641 A1 WO2014026641 A1 WO 2014026641A1
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Prior art keywords
cao
carbon dioxide
gas
carbonization
carbonization tower
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PCT/CN2013/081642
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English (en)
Chinese (zh)
Inventor
白玉龙
王昀睿
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西安瑞驰节能工程有限责任公司
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Publication of WO2014026641A1 publication Critical patent/WO2014026641A1/fr

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    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/18—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the invention relates to the field of carbon dioxide emission reduction, and specifically relates to an apparatus and a process for recycling carbon dioxide by using CaO as a carrier.
  • Carbon dioxide (co 2 ) is one of the main components of greenhouse gases that cause global climate change. The contribution rate to the greenhouse effect is as high as 55%. climate change caused by greenhouse gas emissions such as 0) 2 has become the focus of attention around the world. problem. Carbon capture and storage technology (CCS technology) refers to a technology that captures and separates carbon dioxide from relevant concentrated emission sources and stores it in various ways to avoid its release into the atmosphere. It is the most effective response to climate change. One of the technical paths.
  • post-combustion capture refers to a method of capturing 0 2 in the flue gas after combustion, including pressure swing adsorption, membrane separation, physical absorption and chemical absorption, etc., which can be directly applied to existing production equipment, and input. Relatively few, the principle is simple, and the scope of application is wide.
  • the alcohol amine method represented by MEA utilizes an alkaline aqueous solution having a hydroxyl group and an amine group as a solvent, and captures C0 2 through an absorption tower and a regeneration tower constituent system, and is currently studied and used more and more mature chemicals.
  • the absorption method has a high removal rate of 0 2 and can be adapted to treat a mixed gas with a low partial pressure of C0 2 , but the absorbent used in the method is highly corrosive to the system, and has high regeneration energy consumption, and is prone to oxidation and thermal degradation.
  • the ammonia water absorption method has the advantages of low material cost, strong ability to absorb C0 2 , low energy consumption for regeneration, low sensitivity of the absorbent to other gas components, and low corrosivity to the system.
  • Calcium-based absorbent cycle calcination/carbonation reaction captures CO 2 using inexpensive and resource-rich limestone, dolomite, etc. as a 0 2 absorbent, which has good technical and economical properties and has received extensive attention in recent years.
  • the method of capturing CO 2 by the method adopts a double fluidized bed reactor (absorption reactor and regeneration reactor), and material exchange between two reactors is realized through a connecting pipe, in which CaO and C0 2 occur in the absorption reactor.
  • the gas-solid reaction absorbs the low concentration of C0 2 in the mixed flue gas to form CaC0 3 (the reaction formula is CaO+ C0 2 ⁇ CaC0 3 ).
  • the combustion of coal by pure oxygen combustion causes CaCO 3 to decompose to form CaO and high.
  • the concentration of C0 2 (reaction formula is CaC0 3 ⁇ CaO + C0 2 ), in which CaO is reused for the absorption reactor, while collecting the high concentration of CO 2 produced. Due to the limitations of the gas-solid reaction, using conventional firing cycles / trapping carbonation Method 2 C0, when the reaction was carried out to a certain extent, the surface of the particles generated CaO & dense product layer 03 be internal to the granules further C0 2 Diffusion creates an obstruction and lowers the overall reaction rate. After multiple cycles of absorption and calcination, the internal pores of the adsorbent particles are clogged and the specific surface area is decreased, which will cause the activity of the calcium-based absorbent to decrease.
  • the patent still uses the dual fluidized bed combined with the pure oxygen combustion of biomass fuel to realize the regeneration of the adsorbent, which greatly reduces the amount of exhaust gas in the production process, but the technology of pure oxygen combustion is difficult, investment and operating costs. Both are high, and this method can not solve the external air entering the reactor caused by the poor sealability of the fluidized bed reactor. Part, causing a problem of reduced purity of co 2 .
  • an apparatus for cyclically capturing carbon dioxide by using CaO as a carrier comprising a purification device connected to a pipeline and a carbonization tower, wherein the carbonization tower is connected by a pipeline with a sedimentation separator, a centrifuge, a dryer, a metering device, and a closed-loop type calcination a furnace, a material storage tank, a bucket elevator, a ashing machine, a coarse paddle and a hydrocyclone, wherein the hydrocyclone is connected to the carbonization tower; the annular calciner is connected to the water cooling heat exchanger through the pipeline a compressor, a condenser, and a 0 2 storage tank; the settling separator, the centrifuge, and the ashing machine are respectively connected to the return pool through a pipe.
  • the purge gas outlet of the purification device is connected to the bottom gas inlet of the carbonization tower through a pressurizing machine;
  • the carbonization tower is connected to the settling separator by a transfer pump a;
  • the settling separator Connected to the centrifuge by a transfer pump b;
  • the coarse paddle is connected to the hydrocyclone by a transfer pump c;
  • the hydrocyclone is connected to the carbonization tower through a transfer pump d;
  • the closed loop type calcining furnace is connected to the water-cooled heat exchanger by a pump e;
  • the reuse pool is connected to the ash machine by a transfer pump f.
  • the bottom of the carbonization tower chamber is provided with a gas distributor, and the upper portion is provided with a gas baffle, a gas discharge port and a carbonizer inlet.
  • the annular calciner is a fully enclosed calciner, in which a radiant heating component is disposed, and the radiant heating component uses an electric heating radiant tube and a heating radiant tube for isolating the flue gas. Or microwave to heat the radiant tube.
  • the bucket elevator side is provided with a discharger, and the ashing machine is connected to the bottom of the discharger.
  • the present invention also provides a process for recycling carbon dioxide by using CaO as a carrier, including The following steps:
  • Step A Flue gas purification treatment: Introduce the flue gas into the purification device to remove harmful gases and impurities such as S0 2 , NO x , heavy metals, dioxins and fly ash.
  • the main component of the purified flue gas is C0 2 And N 2 ;
  • Step B and carbonizing: the purified flue gas treatment by a pressing machine, and then enters the carbonation tower via an inlet through the gas distribution bottom of the carbonation tower, wherein, C0 2 carbonation of milk of lime solution inside the column carbonation reaction
  • the CaC0 3 paddle and H 2 0 are generated to complete the absorption process of C0 2 in the flue gas.
  • the main chemical reaction formula for this step is:
  • N 2 is discharged into the atmosphere by a gas baffle barrier from the gas discharge port at the top of the carbonization tower;
  • Step C Carbide product CaC0 3 treatment:
  • the CaC0 3 pulp produced by the carbonization reaction is separately separated by a sedimentation separator, dehydrated by a centrifuge, and dried by a dryer to form a finished light calcium carbonate, and the finished light calcium is metered and transported to a full-closed closed loop shape.
  • Step D C0 2 desorption:
  • the finished light calcium & 0 3 is decomposed by high temperature calcination in a ring-shaped calciner under complete air isolation to obtain CaO and high-purity C0 2 gas which can be subsequently used for calcination; the main chemical reaction in this step
  • the formula is:
  • Step E CaO digestion: The calcined product CaO is transported to a storage bin and cooled to below 60 degrees, sent to a bucket elevator, and centrifugally unloaded through a discharger. The ashing machine; the CaO and the ashing machine are mixed with the hot water from the water-cooling heat exchanger and the clean water of the reused pool, and then the coarse milk slurry is discharged into the coarse paddle; the main chemical reaction formula of this step is:
  • Step F lime milk blending and refining: The lime milk in the coarse paddle is transported to a hydrocyclone for purification to obtain a lime emulsion paddle; Step G, lime milk recycling and utilization: the refined lime milk slurry obtained by the refining is sent to the carbonization tower to supplement the carbonization agent required for the carbonization tower;
  • Step H high purity 0 2 storage (sealed) Storage:
  • the upper gaseous product C0 2 gas in the closed-loop type calcining furnace is sent to the water-cooled heat exchanger via a heat-resistant pipe, cooled to 50 ° C; after cooling, the high-purity 0 2 gas passes through the compressor
  • the function of the condenser is converted into a liquid C0 2 finished product, which is transported by a closed pipe to a storage tank of 0 2 storage. After storage, it can be used in food processing, beverage, fire prevention and other fields. It can also be injected into deep saline or marine water by more mature C0 2 storage technology.
  • the volume concentrations of C0 2 and N 2 in the flue gas after the purification treatment in step A are 10-30% and 70-90%, respectively.
  • the supernatant obtained by sedimentation separation and centrifugal dehydration in step C enters the reuse pool, and the water used in the reuse pool can be reused for the CaO digestion process in the step E as needed.
  • the calcining temperature of the annular calciner in step D is 1000-1400 °C.
  • &0) 3 can be rapidly and completely decomposed into C0 2 gas and CaO.
  • the calcined CaCO ⁇ equipment is excellent in air insulation and can realize high temperature calcination of the annular calciner to ensure the purity of the collected CO 2 .
  • step H the generated high-temperature high-purity CO 2 is cooled by a jacket cold water heat exchange method, cooled to 50 ° C, and the obtained hot water is returned to the step E.
  • the CaO digestion process is preferably, in step H, the generated high-temperature high-purity CO 2 is cooled by a jacket cold water heat exchange method, cooled to 50 ° C, and the obtained hot water is returned to the step E.
  • the process and equipment provided by the invention have the following beneficial effects: (1) Compared with the prior method, the carbon capture material used in the invention has low cost, low corrosivity to the system, and energy conservation; (2) Ca(OH) 2 The emulsion has a high absorption rate for C0 2 and has obvious advantages over the solid absorbent; (3) Calcination of CaC0 3 under completely isolated air conditions, the purity of C0 2 obtained by the capture can reach 99% or more, which is favorable for C0 2 Subsequent use and treatment; (4) The entire system is closed, the calcium absorbent and water are recycled, which greatly reduces the operation and maintenance costs.
  • 1 is a flow chart of an apparatus for cyclically capturing carbon dioxide by using CaO as a carrier in an embodiment of the present invention.
  • 2 is a process flow diagram of an embodiment of the present invention.
  • Figure 1 shows an apparatus for cyclically capturing carbon dioxide using CaO as a carrier, comprising a purification device 1 for exhaust gas purification connected in series via a pipeline; a carbonization tower 3 for CO 2 absorption; and a carbonization product CaC0 3 pre- Treated sedimentation separator 5, centrifuge 7, dryer 8; closed closed loop calciner 10 for desorption of 0 2 ; material storage tank 11 for bucket calcination to be recycled for carbonization process, bucket elevator 12.
  • Ash machine 13 coarse paddle 14 for lime milk refining, hydrocyclone 16; water-cooled heat exchanger 19 for C0 2 storage, compressor 20, condenser 21, C0 2 storage tank 22; Among them, the sedimentation separator 5, the centrifuge 7 and the ashing machine 13 are connected to the recycling pool 23 through pipes, respectively.
  • the purge gas outlet of the purification device 1 is connected to the bottom gas inlet of the carbonization tower 3 via a pressurizing machine 2; the bottom of the carbonization tower is provided with a gas distributor 3a, the upper portion is provided with a gas baffle 3b, a gas discharge port 3c and carbonization 3D agent inlet; the carbonation tower liquid discharge port 3 a 4 and the inlet of the sedimentation separator 5 is connected via a feed pump; b 6 feed pump connected to the bottom of the sedimentation separator 5, CaC0 3 enriched liquid delivered to the The centrifuge 7 inlet; the centrifuge 7 solid discharge port is connected to the dryer 8 inlet, the dryer 8 dry material outlet is connected to the metering device 9 material inlet, the metering device 9 outlet and the closed loop The material inlets of the calciner 10 are connected; the gas inlet of the transfer pump e 18 is connected to the gas collection port of the closed closed loop calciner 10, and the high purity CO 2 gas is sent to the water-cooled heat exchanger 19, The outlet of the
  • the sedimentation separator 5 the supernatant outlet of the centrifuge 7 is connected to the inlet of the recovery pool 23, and the outlet of the recovery pool 23 is passed through the conduit and the transfer pump f. 24, the inlet is connected, the pipe is connected with a valve 24a, and the return water outlet of the transfer pump f 24 is connected to the clean water inlet of the ashing machine 13.
  • the hot water displaced by the water-cooled heat exchanger 19 is connected to the clean water inlet of the ashing machine 13 through a pipe.
  • the closed loop type calcining furnace 10 is a fully enclosed calcining furnace in which a radiant heating part 10a is provided, and the radiant heating part 10a is electrically heated to illuminate the tube and to isolate the flue gas. Heat the radiant tube or microwave to heat the radiant tube.
  • the bucket elevator 12 side is provided with a discharger 12a, and the ashing machine 13 is attached to the bottom of the discharger 12a.
  • Step A the flue gas cleaning process: the flue gas purification device 1 is introduced through a pipe, the flue gas S0 2, NO x, heavy metals, dioxins, and other harmful gases and fly ash removed impurities obtained under the action of the purification apparatus 1
  • the main components of the purified flue gas are C0 2 and N 2 , and the volume concentration is 15% and 78%.
  • Step B carbonization: The pressure of the gas at the outlet of the purification device 1 is increased by the pressurization of the pressurization 2 to enhance the mass transfer effect in the carbonization process.
  • the purified flue gas enters the carbonization tower 3 via the gas distributor 3a through the inlet at the bottom of the carbonization tower 3.
  • the gas rises from the bottom up, the carbon dioxide and carbonization tower 3
  • the internal lime milk solution undergoes a rapid chemical reaction, and carbon dioxide is rapidly absorbed to form & 0 3 and H 2 0, while N 2 does not react with the lime milk during the ascending flow, and collects gas at the top of the carbonization tower 3
  • the baffle 3b is blocked and finally discharged into the atmosphere by the gas discharge port 3c at the top of the carbonization tower.
  • Step C treatment of carbonized product CaC0 3 :
  • the CaC0 3 paddle produced by the carbonization reaction has a high water content, and it is not suitable to directly recover the C0 2 by calcination.
  • the transfer pump a 4 transports the carbonized CaC0 3 slurry to the settling separator 5, and under the action of gravity, the water and the solid CaCO ⁇ in the slurry are initially separated; the transfer pump b 6 will settle the solid at the bottom of the separator 5 CaC0 3 suspension is transported to the centrifuge 7, the centrifuge 7 uses a high-speed rotating drum to generate centrifugal force to trap the solid particles in the suspension in the drum and automatically discharged into the dryer 8 under the force of the machine;
  • the dryer 8 further removes the moisture contained in the solid CaC0 3 having a moisture content of about 35% by heating by hot air, flue gas or infrared rays, and the moisture content of the outlet material is about 0.3%, which satisfies the requirements of the subsequent calcination process
  • Step D C0 2 Desorption:
  • the finished light calcium carbonate is decomposed by high temperature calcination under conditions of complete air isolation, and the calcined products are CaO and C0 2 .
  • the heat is generated by the radiant heating component 10a which is completely insulated from the air in the closed-loop type calcining furnace 10, and the calcination zone temperature in the furnace is 1000-1400 ° C, and the calcined products CaO and C0 2 are obtained; due to the special structure in the closed-loop calcining furnace 10, the furnace The concentration of C0 2 gas in the space is 98-99.8%.
  • Step E CaO digestion:
  • the closed solid-state material CaO is transported to the material storage bin 11 for cooling, and the material temperature is reduced to below 60 degrees, and the conveying device transports it to the bucket elevator 12; the bucket elevator 12
  • the powdery CaO material is vertically raised to a certain height, and is quickly centrifugally unloaded to the ashing machine 13 by the action of the unloader 12a; in the ashing machine 13, the CaO material and the hot water from the water-cooling heat exchanger 19 in the machine And the water from the reuse pool 23 is mixed, and the digestion reaction is carried out to produce a coarse slurry of lime milk.
  • the coarse slurry of the lime milk is discharged into the coarse paddle 14 and the coarse paddle 14 is The milk concentration of lime is 30%.
  • Step F lime milk refining:
  • the conveying pump c 15 sends the coarse milk coarse paddle in the coarse paddle 14 to the refining device
  • the preparative-cyclone separator 16 is refined, and the refined lime milk solution has high activity and moderate concentration, and is suitable for re-entering the carbonization tower 3 to adsorb C0 2 in the power plant exhaust gas.
  • the coarse paddle tank 14 is provided with a stirring device 14a, which is beneficial to the subsequent lime milk refining and carbonization reaction.
  • Step G lime milk recycling:
  • the refined lime milk slurry obtained by the refining is sent to the carbonizing agent inlet 3d by the transfer pump d 17 to supplement the carbonized absorbent inside the carbonization tower 3.
  • Step H high purity 0 2 storage (sealed) storage:
  • the high-purity C0 2 gas produced by the upper gaseous product outlet of the closed-loop type calcining furnace 10 has a purity of 98.0-99.8%, a temperature of about 200 ° C, and a pump e 21 Under the action, it is sent to the water-cooled heat exchanger 19 through the heat-resistant pipe for cooling. After cooling, the gas temperature is lowered to 50 ° C; after cooling, the high-purity C0 2 gas is converted into the liquid C0 2 finished product by the action of the compressor 20 and the condenser 21, It is conveyed to the C0 2 storage tank 22 by a closed pipe for subsequent use.

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  • Organic Chemistry (AREA)
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  • Biomedical Technology (AREA)
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  • Life Sciences & Earth Sciences (AREA)
  • Inorganic Chemistry (AREA)
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Abstract

La présente invention concerne un procédé qui utilise le CaO comme vecteur pour la capture par cycles de dioxyde de carbone. Le procédé comprend : étape A, traitement de purification des gaz d'échappement ; étape B, carbonisation ; étape C, traitement de produit carbonisé CaCO3 ; étape D, désorption de CO2 ; étape E, digestion de CaO ; étape F, affinage de lait de chaux ; étape G, recyclage de lait de chaux ; et étape H, stockage (ou séquestration) du CO2 à haute pureté. Un appareil, qui utilise du CaO comme vecteur pour la capture par cycles du dioxyde de carbone dans un gaz de combustion, comprend, connectés par le biais de canalisations et d'un système de transport de matériau, un appareil de purification, une tour de carbonisation, un séparateur de sédimentation, une centrifugeuse, un séchoir, un appareil de mesure, un four de calcination annulaire, un entrepôt de stockage de matériau, un élévateur à godets, un digesteur de chaux, une cuve à suspensions grossières et un séparateur hydrocyclone. Le procédé affiche des conditions matures, des étapes simples et une haute efficacité pour la capture du CO2, tandis que l'appareil qui met en œuvre le procédé présente une structure compacte, de faibles investissements et opérations et de très bonnes perspectives d'application industrielle.
PCT/CN2013/081642 2012-08-17 2013-08-16 Appareil et procédé utilisant le cao comme vecteur pour la capture par cycles de dioxyde de carbone WO2014026641A1 (fr)

Applications Claiming Priority (2)

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CN201210292710.7 2012-08-17
CN201210292710.7A CN102773006B (zh) 2012-08-17 2012-08-17 一种以CaO为载体循环捕集二氧化碳的设备及工艺

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CN110921667A (zh) * 2019-12-27 2020-03-27 天津健威泽节能环保科技股份有限公司 一种水泥熟料生产线捕集纯化二氧化碳的系统及实现方法

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CN103638808B (zh) * 2013-11-15 2016-10-05 华南理工大学 利用碳酸酐酶催化石灰乳富集糖厂烟道气中二氧化碳的方法
TWI499449B (zh) * 2014-10-27 2015-09-11 Ind Tech Res Inst 二氧化碳捕獲裝置與方法
CN105822901B (zh) * 2016-05-29 2018-11-13 济南科慧页岩化工技术有限公司 一种捕集、利用冶金产生co2的管道及其铺设工作方法
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CN106345265B (zh) * 2016-08-26 2019-02-05 华北电力大学 集成二次碳化过程氧化钙循环脱碳系统的燃煤电站系统
CN108213042B (zh) * 2018-01-02 2020-10-23 巴彦淖尔市飞尚铜业有限公司 中和压滤渣及分级机石灰渣回收利用装置
CN108439406B (zh) * 2018-04-23 2020-03-27 中国科学院上海应用物理研究所 一种回收并电解co2制备co的方法及装置
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