CN107512717B - Process and equipment for preparing high-purity carbon dioxide combined with silicate cement calcination - Google Patents
Process and equipment for preparing high-purity carbon dioxide combined with silicate cement calcination Download PDFInfo
- Publication number
- CN107512717B CN107512717B CN201710907918.8A CN201710907918A CN107512717B CN 107512717 B CN107512717 B CN 107512717B CN 201710907918 A CN201710907918 A CN 201710907918A CN 107512717 B CN107512717 B CN 107512717B
- Authority
- CN
- China
- Prior art keywords
- carbon dioxide
- gas
- tower
- heat
- heater
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/60—Methods for eliminating alkali metals or compounds thereof, e.g. from the raw materials or during the burning process; methods for eliminating other harmful components
-
- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- 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
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
- Y02P40/18—Carbon capture and storage [CCS]
Abstract
The invention relates to a process and equipment for preparing high-purity carbon dioxide by combining with silicate cement calcination. Specifically, after the cloth bag dust collection process of the conventional cement calcination process, a high-purity carbon dioxide preparation process is added: the waste gas produced by cement enters an absorption tower in the form of raw gas after being dedusted by a bag dust collector, and then enters an analysis tower through a heat exchanger, a heater and a separator, and is decomposed into sodium carbonate, carbon dioxide and water in the analysis tower; the decomposed carbon dioxide gas is subjected to compression, liquefaction and rectification procedures to obtain industrial-grade high-purity carbon dioxide commodity. The invention is different from various technologies for preparing carbon dioxide gas by using fuel flue gas, and is an extension of the traditional cement sintering process, and the function of the extension part is to extract and rectify carbon dioxide in the exhaust gas to reach the industrial product standard, so that the carbon dioxide is a byproduct of the cement industry instead of the exhaust gas, and the carbon dioxide is directly converted into an industrial product in the cement production process, thereby having good economic and environmental benefits.
Description
Technical Field
The invention relates to a high-purity carbon dioxide preparation process and equipment combined with silicate cement calcination, belonging to an extension process of the silicate cement calcination process.
Background
The silicate cement calcining process is divided into a wet process and a dry process, and the chemical reaction principle is identical although the two process flows are different, namely, calcium carbonate is decomposed to obtain calcium oxide, and then the calcium oxide is calcined with other components to obtain cement clinker. The cement production process only uses calcium oxide (CaO) after decomposing calcium carbonate, and the decomposed carbon dioxide (CO) 2 ) Without any utilization, and becomes exhaust emission.
The preparation of high-purity carbon dioxide has various mature technologies at present, mainly including a solvent absorption method, a pressure swing adsorption method, a membrane permeation method, a direct compression low-temperature rectification method and the like. The solvent absorption method is classified into physical absorption method and chemical absorption method, the absorption method includes physical absorption method and chemical absorption method, physical-chemical comprehensive absorption method such as ammonia water method, ethanolamine method and thermal (potassium) alkali method, physical absorption method such as methanol method, propylene carbonate method, physical-chemical comprehensive absorption method such as sulfolane method, polyethylene glycol dimethyl ether method, etc. The newly developed methods are as follows: carbon dioxide recombination, electrochemical separation, and hydrate separation.
Raw materials for preparing high-purity carbon dioxide in China at the present stage comprise food fermentation, limestone calcination and natural high-purity air sources, and purification after direct limestone calcination and gas collection is one of the traditional production methods.
Disclosure of Invention
The invention aims to solve the technical problem of providing a high-purity carbon dioxide preparation process and equipment combined with silicate cement calcination, which integrate the silicate cement calcination process and the high-purity carbon dioxide preparation process, furthest utilize limestone raw materials and can simultaneously obtain cement clinker and high-purity carbon dioxide.
The technical scheme adopted for solving the technical problems is as follows:
the high-purity carbon dioxide preparation process combined with silicate cement calcination is characterized in that the high-purity carbon dioxide preparation process is added after a cloth bag dust collection procedure of a conventional cement calcination process, and specifically:
after dust removal of waste gas produced by cement is carried out by a bag dust collector, the waste gas enters an absorption tower in high-purity carbon dioxide gas making process equipment in the form of raw material gas; the waste gas is pretreated before entering the absorption tower, SO that the dust of the gas is further reduced, and SO is removed 2 The ingredients are cooled again;
the carbon dioxide in the raw material gas is absorbed in the absorption tower, and the chemical reaction formula of the absorption process in the tower is as follows: na (Na) 2 CO 3 +H 2 O+CO 2 ——→2NaHCO 3 ；
In the analysis tower, the rich liquid absorbing the carbon dioxide is decomposed into sodium carbonate, carbon dioxide and water again; the rich liquid is sent to an analysis tower to pass through a heat exchanger to exchange heat between lean liquid and rich liquid, then the rich liquid is heated to 100-120 ℃ by using waste heat of waste gas through a heater, and then the rich liquid is sent to the analysis tower to be decomposed into sodium carbonate, water and released carbon dioxide gas, so that new lean liquid is generated, and the chemical reaction formula is as follows:
2NaHCO 3 ——→Na 2 CO 3 +H 2 O+CO 2 ；
the decomposed carbon dioxide gas enters a compression liquefying and rectifying process after being separated from gas and water at the top of the analytic tower; the compressor compresses the gaseous carbon dioxide to a certain air pressure, and the gaseous carbon dioxide is liquefied and then enters a low-temperature rectification process to obtain high-purity carbon dioxide.
According to the process, the invention provides high-purity carbon dioxide preparation equipment combined with silicate cement calcination, which comprises a bag dust collector, an exhaust fan, a gas heat exchange boiler, a washing dust collector, a desulfurizing tower, a gas-water separator, an absorption tower, a heat exchanger, a cooler, a heater and an analysis tower, wherein the exhaust gas outlet of the bag dust collector is connected with the exhaust gas inlet of the gas heat exchange boiler, the exhaust gas outlet of the gas heat exchange boiler is connected with the raw material gas inlet of the washing dust collector, the gas outlet of the washing dust collector is connected with the gas inlet of the desulfurizing tower, the gas outlet of the desulfurizing tower is connected with the gas inlet of the gas-water separator, and the gas outlet of the gas-water separator is connected to the absorption tower through a Roots blower; the decarbonized gas outlet of the absorption tower is connected to the exhaust fan through a self-regulating valve; the rich liquid outlet of the absorption tower is connected with a heat exchanger, the rich liquid outlet heated by the heat exchanger is connected with a heater through a saturated alkali liquid conveying pipeline and a saturated alkali liquid conveying pump, the rich liquid outlet heated by the heater is connected with an analysis tower, and the high-purity carbon dioxide gas outlet of the analysis tower is connected with a compression liquefaction, rectification and compression canning production line; a heat-conducting medium circulating pump is arranged on a heat-conducting medium circulating pipeline between the gas-making heat exchange boiler and the heater; a hot sodium carbonate aqueous solution reflux pipeline and a reflux pump are arranged between the heat exchanger and the analytic tower, a cooler is arranged between the heat exchanger and the absorption tower, and a bypass valve is arranged between the heat exchange boiler and the regulating valve.
Compared with the prior art, the invention adopting the technical scheme has the beneficial effects that:
unlike various fuel fume producing carbon dioxide gas technology, the present invention is one extension of conventional cement burning process and has the function of calcining carbon dioxide (CO) in exhaust gas 2 ) Purifying to qualified industrial products, and becoming byproducts of the cement industry instead of exhaust gas, thereby achieving the purpose of fully utilizing limestone resources. Direct carbon dioxide (CO) conversion in cement manufacture 2 ) Is converted into available commodity and has good economic and environmental benefits.
The obvious difference between the invention and the technology for recovering carbon dioxide from flue gas is that: the source of carbon dioxide varies from source, the carbon dioxide source involved in the present invention comes from the decomposition of the cement raw material during the calcination process, with the result that one raw material is given two different industrial products, whereas the carbon dioxide involved in the flue gas recovery technology is produced by the combustion of fuel.
The remarkable difference between the invention and the technology for burning carbon dioxide by a lime kiln is that: different calcining processes are adopted to obtain different products. The invention utilizes one raw material to obtain two products of cement clinker and carbon dioxide at the same time, and the technology of firing carbon dioxide by a lime kiln only obtains carbon dioxide.
The obvious difference between the invention and the lime kiln comprehensive carbon dioxide recovery technology is that: different calcining processes are adopted to obtain different products. The invention obtains two products of cement clinker and carbon dioxide, and the products obtained by the lime kiln comprehensive carbon dioxide recovery technology are quicklime (CaO) and carbon dioxide.
The cement calcination process and the carbon dioxide preparation process are combined to form a continuous production line, and the process for simultaneously obtaining cement clinker and high-purity carbon dioxide is a remarkable characteristic of the invention.
The invention is another remarkable characteristic of the invention, which is different from the traditional cement production technology and the traditional carbon dioxide preparation and separation technology.
Further, the preferred scheme of the invention is as follows:
the heater is internally provided with two groups of heating pipelines, one group of heating pipelines is connected with the heat exchange boiler through a heat conducting medium pipeline and a heat conducting medium circulating pump, the other group of heating pipelines is connected with the afterburning boiler, and when the waste heat energy of the heat exchange boiler is insufficient for heating the rich liquid to the analysis temperature, the afterburning boiler provides heat energy for the heater. In particular, for plants with exhaust emission temperatures below 100 ℃, afterburner boilers should be added as supplemental heat sources.
Drawings
FIG. 1 is a schematic diagram of a high purity carbon dioxide production apparatus according to an embodiment of the present invention;
in the figure: 1-a cloth bag dust collector; 2-a heat exchange boiler; 3-a bypass valve; 4, washing a dust remover; 5-a desulfurizing tower; 6-a gas-water separator; 7-Roots blower; 8-an absorption tower; 9-adjusting the valve; 10-a heat exchanger; 11-a cooler; 12-a saturated alkali liquor conveying pump; 13-an analytical tower; 14-a reflux pump; 15-a heat conducting medium circulating pump; 16-afterburning boiler; 17-an exhaust fan; 18-heater.
Detailed Description
The invention will be further described with reference to the accompanying drawings and examples.
Referring to fig. 1 (the cement calcination process equipment at the present stage is omitted in the figure), the high-purity carbon dioxide preparation equipment combined with silicate cement calcination consists of equipment units such as a bag dust collector 1, an exhaust fan 17, a heat exchange boiler 2, a washing dust collector 4, a desulfurizing tower 5, a gas-water separator 6, an absorption tower 8, a heat exchanger 10, a heater 18, a resolving tower 13 and the like, wherein the exhaust gas outlet of the bag dust collector 1 is connected with the exhaust gas inlet of the heat exchange boiler 2, the exhaust gas outlet of the heat exchange boiler 2 is connected with the gas inlet of the washing dust collector 4, the raw material gas outlet of the washing dust collector 4 is connected with the gas inlet of the desulfurizing tower 5, the gas outlet of the desulfurizing tower 5 is connected with the gas inlet of the gas-water separator 6, and the gas outlet of the gas-water separator 6 is connected with the absorption tower 8 through a Roots blower 7; the decarbonizing gas outlet of the absorption tower 8 is connected to an exhaust fan 17 via a self-regulating valve 9; the rich liquid outlet of the absorption tower 8 is connected with a heat exchanger 10, the rich liquid of the heat exchanger 10 is connected to a heater 18 through a saturated alkali liquid conveying pump 12, the heater 18 is connected with a resolving tower 13, and the high-purity carbon dioxide gas outlet of the resolving tower 13 is connected to a compression liquefaction, rectification and compression canning production line; a heat-conducting medium circulating pump 15 is arranged on a heat-conducting medium circulating pipeline between the heat exchange boiler 2 and the heater 18; a hot sodium carbonate aqueous solution reflux pipeline and a reflux pump 14 are arranged between the heat exchanger 10 and the analysis tower 13, a cooler 11 is arranged between the heat exchanger 10 and the absorption tower 8, and a bypass valve 3 is arranged between the heat exchange boiler 2 and the regulating valve 9.
The heater 18 is internally provided with two groups of heating pipelines, one group is connected with the heat exchange boiler 2 through a heat conducting medium pipeline and a heat conducting medium circulating pump 15, the other group is connected with the afterburner 16, and when the waste heat energy of the heat exchange boiler 2 is insufficient for heating the rich liquid to the analysis temperature, the afterburner 16 provides heat energy for the heater 18.
The process flow for preparing high purity carbon dioxide in combination with the calcination of portland cement is described in detail below:
in the prior art, a bag dust collector 1 of an exhaust gas treatment process is directly connected with an exhaust fan 17, and a high-purity carbon dioxide preparation process is added between the bag dust collector 1 and the exhaust fan 17, so that the two processes are combined into a novel process capable of fully utilizing limestone.
Before the exhaust gas from cement production is discharged, the exhaust gas is subjected to dust removal treatment, and dust removal equipment is divided into two types, namely an electric dust collector and a cloth bag dust collector. The dust removing effect of the cloth bag dust collector is good and stable, and the dust content of the gas treated by the cloth bag dust collector is 30-100 mg/Nm 3 The carbon dioxide gas producing and extending process can be directly connected with the extending part of the invention, namely the carbon dioxide producing process, and if the carbon dioxide gas producing and extending process is an electric dust collector, the carbon dioxide gas producing and extending process can be closed through the bypass valve 3 after the electric dust collector is modified into a cloth bag dust collector or a primary cyclone dust collector is added and then connected with the extending part of the invention.
Gas desulfurization and purification:
after the two processes are connected, the waste gas enters a carbon dioxide preparation process in the form of raw material gas. The waste gas is filtered and dedusted by a bag dust collector 1, then enters a washing dust collector 4 by a heat exchange boiler 2, and is washed by top water spray SO as to obtain SO 2 The sulfurous acid and sulfuric acid which are formed by dissolving in water are collected at the bottom of the tower, the water is recycled after being treated, and the sulfurous acid and sulfuric acid which are remained in the fog enter into a desulfurizing tower 5 to be mixed with limestone (calcium carbonate CaCO) 3 ) Or calcium hydroxide (Ca (OH) 2 ) The reaction produces a mixture of sulphite and sulphate which is removed from the gas.
The purified gas is sent to an absorption tower 8 through a gas-water separator 6 by a Roots blower 7.
Carbon dioxide absorption:
the carbon dioxide in the raw material gas is absorbed in the absorption tower 8, the structural form of the tower is various, a plurality of layers of sieve plates can be adopted, the tower is a vertical cylinder formed by welding stainless steel plates, dozens of layers of tower plates are arranged in the tower, and each layer of tower plate is provided with a plurality of holes and a liquid flow pipe. The purified gas is sent from the bottom of the tower, passes through the sodium carbonate absorption liquid on the sieve plate layer by layer, rises to the top of the absorption tower, absorbs carbon dioxide and is discharged to the atmosphere through the regulating valve 9 and the exhaust fan 17. The sodium carbonate absorption solution (lean solution for short) is sent into the absorption tower 8 by the reflux pump 14, sprayed out by the spray header, guided to the sieve plate by the liquid flow pipe and flows to the bottom of the tower layer by layer under the action of gravity, and the sodium carbonate lean solution finally absorbs carbon dioxide and water to become sodium bicarbonate (rich solution for short) and flows into the bottom of the tower. The gas-liquid two-phase contact process in the tower is the absorption and reaction process. The countercurrent flow contact of the gas phase and the liquid phase in the absorption tower is beneficial to the absorption reaction. The rising speed of the air flow needs to be reasonably controlled, so that a better absorption effect is achieved, and the chemical reaction formula of the absorption process in the tower is as follows:
the absorption rate of sodium carbonate can reach about 40-60%, and the sodium carbonate can be higher after the activator is added. Strict control of reasonable process parameters is critical to improving absorption. The main parameters are recommended as follows:
(1) Sodium carbonate aqueous solution concentration 12%;
(2) The temperature of the absorption liquid on the tower is lower than 50 ℃ and is not higher than 60 ℃ at the highest;
(3) The pressure in the tower is 0.2Mpa.
Carbon dioxide analysis:
the high purity carbon dioxide is obtained in a desorption tower 13, and the function of the desorption tower 13 is to re-decompose the rich liquid absorbed with carbon dioxide into sodium carbonate and carbon dioxide (CO 2 ) And water (H) 2 O), the rich liquid (sodium bicarbonate solution) is sent to the desorption tower 13 by the saturated alkali liquid transfer pump 12, and heat exchange between the lean liquid and the rich liquid is performed by the heat exchanger 10. Because the rich liquid is required to have a higher temperature for decomposition in the tower, and the lean liquid needs to be cooled to below 50 ℃ before entering the absorption tower 8 again after exiting the tower. The rich solution is heated to 100 ℃ to 120 ℃ in a heater 18 and then enters a resolving tower 13 for decomposition to generate sodium carbonate and water, carbon dioxide gas is released, and a new lean solution (reduced sodium carbonate aqueous solution) is generated, wherein the chemical reaction formula is as follows:
the carbon dioxide gas generated after decomposition is subjected to gas-water separation at the top of the analysis tower 13 and then enters a high-purity carbon dioxide compression, liquefaction and rectification process, and the sodium carbonate solution is cooled by the heat exchanger 10 and the cooler 11 and then enters the absorption tower 8 again for recycling. The strict control of the relevant process parameters is the key to increase the desorption rate, and the main parameters are recommended as follows:
(1) The heating temperature of the heater is 100-120 ℃;
(2) The pressure in the analytical tower is 0.15Mpa;
the amount of sodium carbonate base is determined by the carbon dioxide production capacity, absorption rate and resolution.
Dehydrating, compressing and rectifying:
compression is an essential process in carbon dioxide production and is accomplished by a compressor. The carbon dioxide gas decomposed and separated by the analyzing tower 13 is dehydrated, compressed and liquefied and then subjected to low-temperature rectification to obtain industrial product-grade high-purity liquid or solid carbon dioxide.
The opening degree of the valve 9 is regulated, and the rotational speeds of the reflux pump 14, the saturated alkali liquid conveying pump 12, the Roots blower 7 and the heat conducting medium circulating pump 15 are changed, so that the production amount of high-purity carbon dioxide can be controlled.
The above examples are merely illustrative of the present invention. Those skilled in the art may make various modifications or additions to the described embodiments or substitutions thereof without departing from the spirit of the invention or exceeding the scope of the invention as defined in the accompanying claims.
Claims (3)
1. A process for preparing high-purity carbon dioxide combined with Portland cement calcination is characterized in that:
after the cloth bag dust collection process of the conventional cement calcination process, a high-purity carbon dioxide preparation process is added, and the method is characterized in that:
waste gas from cement production is dedusted by a bag dust collector (1) and then is wastedThe gas enters an absorption tower (8) in the high-purity carbon dioxide gas production process equipment in the form of raw gas; the waste gas is pretreated before entering the absorption tower (8) to further reduce dust and remove SO 2 The ingredients are cooled again;
the carbon dioxide in the raw material gas is absorbed in an absorption tower (8), and the chemical reaction formula of the absorption process in the tower is as follows: na (Na) 2 CO 3 +H 2 O+CO 2 ——→2NaHCO 3 ；
In the analyzing tower (13), the rich liquid absorbed with carbon dioxide is decomposed into sodium carbonate, carbon dioxide and water again; the rich liquid is sent to an analysis tower (13) to pass through a heat exchanger (10) to exchange heat between lean liquid and rich liquid, then the rich liquid is heated to 100-120 ℃ by a heater (18) by waste heat of waste gas, and then is sent to the analysis tower (13) to be decomposed into sodium carbonate, water and carbon dioxide gas to generate new lean liquid, wherein the chemical reaction formula is as follows:
2NaHCO 3 ——→Na 2 CO 3 +H 2 O+CO 2 ；
the decomposed carbon dioxide gas is subjected to gas-water separation at the top of an analysis tower (13) and then enters a compression liquefaction and rectification process; the compressor compresses the gaseous carbon dioxide to a certain air pressure, and the gaseous carbon dioxide is liquefied and then enters a low-temperature rectification process to obtain high-purity carbon dioxide.
2. The utility model provides a high purity carbon dioxide preparation equipment that combines together with portland cement calcination, includes cloth bag dust collector (1), exhaust fan (17) among the cement calcination equipment, its characterized in that: the system further comprises a heat exchange boiler (2), a washing dust remover (4), a desulfurizing tower (5), a gas-water separator (6), an absorption tower (8), a heat exchanger (10), a cooler (11), a heater (18) and an analysis tower (13), wherein an exhaust gas outlet of the cloth bag dust remover (1) is connected with an exhaust gas inlet of the heat exchange boiler (2), an exhaust gas outlet of the heat exchange boiler (2) is connected with a raw material gas inlet of the washing dust remover (4), a gas outlet of the washing dust remover (4) is connected with a gas inlet of the desulfurizing tower (5), a gas outlet of the desulfurizing tower (5) is connected with a gas inlet of the gas-water separator (6), and a gas outlet of the gas-water separator (6) is connected to the absorbing tower (8) through a Roots blower (7); the decarbonizing gas outlet of the absorption tower (8) is connected to an exhaust fan (17) through a self-regulating valve (9); the rich liquid outlet of the absorption tower (8) is connected with the heat exchanger (10), the rich liquid outlet heated by the heat exchanger (10) is connected with the heater (18) through a saturated alkali liquid conveying pipeline and a saturated alkali liquid conveying pump (12), the rich liquid outlet heated by the heater (18) is connected with the analysis tower (13), and the high-purity carbon dioxide gas outlet of the analysis tower (13) is connected to a compression liquefaction, rectification and compression canning production line; a heat-conducting medium circulating pump (15) is arranged on a heat-conducting medium circulating pipeline between the heat exchange boiler (2) and the heater (18); a hot sodium carbonate aqueous solution reflux pipeline and a reflux pump (14) are arranged between the heat exchanger (10) and the analysis tower (13), a cooler (11) is arranged between the heat exchanger (10) and the absorption tower (8), and a bypass valve (3) is arranged between the heat exchange boiler (2) and the regulating valve (9).
3. The high purity carbon dioxide production plant in combination with portland cement calcination according to claim 2, wherein: two groups of heating pipelines are arranged in the heater (18), one group is connected with the heat exchange boiler (2) through a heat conducting medium pipeline and a heat conducting medium circulating pump (15), the other group is connected with the afterburner boiler (16), and when the waste heat energy of the heat exchange boiler (2) is insufficient for heating the rich liquid to the analysis temperature, the afterburner boiler (16) provides heat energy for the heater (18).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710907918.8A CN107512717B (en) | 2017-09-29 | 2017-09-29 | Process and equipment for preparing high-purity carbon dioxide combined with silicate cement calcination |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710907918.8A CN107512717B (en) | 2017-09-29 | 2017-09-29 | Process and equipment for preparing high-purity carbon dioxide combined with silicate cement calcination |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107512717A CN107512717A (en) | 2017-12-26 |
| CN107512717B true CN107512717B (en) | 2023-08-11 |
Family
ID=60725566
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710907918.8A Active CN107512717B (en) | 2017-09-29 | 2017-09-29 | Process and equipment for preparing high-purity carbon dioxide combined with silicate cement calcination |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107512717B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110921667A (en) * | 2019-12-27 | 2020-03-27 | 天津健威泽节能环保科技股份有限公司 | System for capturing and purifying carbon dioxide in cement clinker production line and implementation method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101423214A (en) * | 2008-11-20 | 2009-05-06 | 武汉凯迪电力环保有限公司 | Method for catching carbon dioxide in generating plant flue gas by ammonia process and equipment thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005013952A (en) * | 2003-06-27 | 2005-01-20 | Toshiba Ceramics Co Ltd | Carbon dioxide absorber |
-
2017
- 2017-09-29 CN CN201710907918.8A patent/CN107512717B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101423214A (en) * | 2008-11-20 | 2009-05-06 | 武汉凯迪电力环保有限公司 | Method for catching carbon dioxide in generating plant flue gas by ammonia process and equipment thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107512717A (en) | 2017-12-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102000486B (en) | Method for catching carbon dioxide in flue gas by active sodium carbonate and apparatus thereof | |
| CN103303877B (en) | Many sources of the gas low concentration SO 2smoke comprehensive reclaims acid-making process flow process | |
| KR20220005074A (en) | Systems and methods for carbon capture | |
| WO2014026641A1 (en) | Apparatus and process using cao as carrier for cycled-capturing of carbon dioxide | |
| WO2013053235A1 (en) | Process for removing acid gas from flue gas by using waste heat of same | |
| CN106914117B (en) | Device suitable for continuously capturing carbon dioxide in cement kiln flue gas and generating electricity | |
| CN110743344B (en) | Method for removing low-concentration sulfur dioxide in flue gas and preparing sodium metabisulfite | |
| CN102698585B (en) | Method for recyling carbon dioxide in boiler flue gas | |
| CN1939840A (en) | Tail gas treatment and reutilization for calcium carbide stove | |
| CN114210177A (en) | Lime kiln flue gas carbon dioxide regulation and control and carbon capture system | |
| CN105749728B (en) | Method and apparatus for capturing carbon dioxide | |
| CN115350575A (en) | Method for eliminating industrial flue gas atmospheric pollutants and capturing, converting and utilizing carbon dioxide | |
| CN107512717B (en) | Process and equipment for preparing high-purity carbon dioxide combined with silicate cement calcination | |
| CN206652383U (en) | A kind of hydrate continuously traps CO in cement kiln flue gas2Change system | |
| CN116196734A (en) | Cement oxy-fuel combustion coupling flue gas carbon dioxide trapping and purifying device | |
| CN217220919U (en) | CO 2 And N 2 Composite trapping and purifying system | |
| CN216273131U (en) | IGCC system adopting solid oxide decarburization | |
| CN216159654U (en) | Carbon-based oxygen-enriched combustion system for cement kiln flue gas circulation | |
| CN210544174U (en) | System for simultaneously removing carbon dioxide and sulfur dioxide in flue gas | |
| CN114459236A (en) | Energy-saving cement kiln flue gas carbon capture method | |
| CN111748672B (en) | Short-process low-cost CO preparation method by converter gas2And high-value application system and process | |
| CN115055211A (en) | Methanol-to-olefin regeneration method with carbon dioxide zero emission and carbon monoxide byproduct | |
| CN204939342U (en) | The gasification methyl alcohol system of a kind of integrated utilizing waste heat for refrigeration and carbon trapping | |
| CN207330375U (en) | With the high-pureness carbon dioxide producing equipment that portland cement calcining is combined | |
| CN112110423A (en) | System and method for preparing acid from desulfurization waste liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20230712 Address after: 063000 No.7 Xingfu Road, Fengrun District, Tangshan City, Hebei Province Applicant after: CBMI CONSTRUCTION Co.,Ltd. Address before: Sinoma Construction Co., Ltd., No. 7, Longqing Street, Daxing District Economic and Technological Development Zone, Beijing 100176 Applicant before: Li Chenggang |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |