CN113120906A - Cement production carbon capture device and process for local calcium circulation coupling waste disposal - Google Patents
Cement production carbon capture device and process for local calcium circulation coupling waste disposal Download PDFInfo
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- 239000002699 waste material Substances 0.000 title claims abstract description 73
- 239000004568 cement Substances 0.000 title claims abstract description 59
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 40
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 239000011575 calcium Substances 0.000 title claims abstract description 36
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 55
- 239000002994 raw material Substances 0.000 claims abstract description 39
- 238000004227 thermal cracking Methods 0.000 claims abstract description 25
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- 239000007789 gas Substances 0.000 claims description 30
- 239000000463 material Substances 0.000 claims description 25
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- 239000000779 smoke Substances 0.000 claims description 18
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- 235000012054 meals Nutrition 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 239000000446 fuel Substances 0.000 claims description 11
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- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000010802 sludge Substances 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 5
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- 239000010920 waste tyre Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 abstract description 10
- 239000012535 impurity Substances 0.000 abstract description 6
- 238000013461 design Methods 0.000 abstract description 5
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 2
- 239000003513 alkali Substances 0.000 abstract description 2
- 229910052717 sulfur Inorganic materials 0.000 abstract description 2
- 239000011593 sulfur Substances 0.000 abstract description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract 1
- 238000010000 carbonizing Methods 0.000 abstract 1
- 239000000460 chlorine Substances 0.000 abstract 1
- 229910052801 chlorine Inorganic materials 0.000 abstract 1
- 238000010304 firing Methods 0.000 abstract 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 13
- 239000000292 calcium oxide Substances 0.000 description 13
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 12
- 230000009467 reduction Effects 0.000 description 11
- 238000006722 reduction reaction Methods 0.000 description 11
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 229910000019 calcium carbonate Inorganic materials 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000012528 membrane Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
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- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 229910000413 arsenic oxide Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
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- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910001392 phosphorus oxide Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
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Images
Classifications
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- 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
- 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
- C04B7/364—Avoiding environmental pollution during cement-manufacturing
- C04B7/367—Avoiding or minimising carbon dioxide emissions
-
- 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
Abstract
The invention discloses a cement production carbon capture device and a process for local calcium circulation coupling waste disposal, belonging to the cross technical field of cement production, calcium circulation carbon capture and waste cooperative disposal. The carbon trapping process is to utilize CaO-CaCO between decomposing furnace and carbonizing furnace3CO completion of the CaO cycle2Trapping, adopting off-line decomposing furnace design to avoid SO generated in the processes of clinker firing and raw material preheating2And chlorine alkali sulfur and other impurities enter the decomposing furnace module. Meanwhile, the waste is combined for cooperative treatment to reduce the temperature of the flue gas, the rate and the efficiency of CaO carbon fixation are improved, and NOx generated by the rotary kiln is reduced by using waste thermal cracking products, so that the CO in the flue gas is reduced under the condition of air combustion2Self-enrichment and multi-pollutant cooperative control to reduce subsequent CO2The difficulty of purification and reutilization is obviously improved, and the popularization of carbon capture and reutilization in the cement industry is promoted.
Description
Technical Field
The invention relates to the crossed technical field of cement production, calcium circulation carbon capture and solid waste cooperative treatment, in particular to a cement production carbon capture device and a process for local calcium circulation coupling waste treatment.
Background
Along with the rapid development of national economy, Chinese CO2The emission is increased year by year, the emission reaches 94.3 hundred million tons in 2017, wherein the cement industry is CO in China2One of the major sources of emissions (about 20.0 million tons per year, about 21%). Therefore, the pressure of carbon emission reduction in China is extremely high, and the reduction of carbon emission in the cement industry is particularly important and urgent.
Carbon emission reduction in the cement industry is mainly realized by purifying and trapping flue gas, and the current main trapping process comprises the following steps: chemical absorption, membrane separation, pure oxygen combustion, and calcium circulation. The chemical absorption method is that the flue gas of the cement kiln is pressurized, and then hot potassium solution, ammonia water or organic amine and other liquid are adopted to absorb CO2Then the water is desulfurized and removed by a desulfurizing bed and a drying bed, and phosphorus, arsenic and Nitrogen Oxides (NO) are removed by a solid adsorbentx) The impurities are equal, and the industrial grade or food grade CO is finally obtained2. The membrane separation method utilizes the selectivity of the membrane to the diameter of gas molecules, partial gas passes through the molecular membrane under the action of certain pressure, and further CO is realized2Enrichment and separation. The pure oxygen combustion method is to improve the combustion efficiency of fuel and reduce NO by oxygen combustion supportingxDischarge and greatly improve CO in the flue gas2Concentration for carbon capture. The calcium circulation law is that CaO abundantly existing in the cement kiln system is utilized to absorb CO2Formation of CaCO3Then decomposing again in the decomposing furnace to release CO2And trapped, i.e. by "CaO-CaCO3Circulation of-CaO for CO in cement kiln flue gas2Self-enrichment of (1).
In summary, a large amount of chemical reagents and membrane materials are needed when the chemical absorption and membrane separation method is adopted for carbon capture, and the flue gas is required to be pressurized and decompressed, so that the carbon capture cost is greatly increased. In addition, the cement kiln has large flue gas flow, high dust and acid gas content, and the membrane separation method is difficult to be continuous and highCarrying out CO in flux2The separation and purification greatly shorten the cycle life of the absorbent. The pure oxygen environment cost of the whole system of the cement kiln is extremely high, and the industrial popularization difficulty is extremely high. Because of the large amount of CaO in the cement kiln, the calcium cycle has the potential of realizing high-efficiency carbon capture, but the carbon fixation activity of CaO is obviously reduced under multiple cycles, and SO released by sulfide decomposition in the process of preheating raw meal2Can participate in the gas circulation of the cement kiln system, resulting in CO in the flue gas2The concentration of the cement kiln is reduced, and the difficulty in treating and capturing the tail end of the cement kiln smoke is greatly improved. In addition, the temperature of the kiln tail flue gas in the novel dry-method cement kiln system is as high as about 1200 ℃, which is obviously higher than CaCO3The decomposition temperature of the catalyst obviously reduces the CO capture by CaO circulation2Capacity and efficiency; NOx produced during fuel combustion can also increase CO2The difficulty of purification and trapping finally hinders the popularization and application of the local calcium circulation process in the field of cement kiln flue gas carbon trapping.
Disclosure of Invention
In order to solve the technical problems mentioned in the background technology, the invention provides a cement production carbon capture device and a process for local calcium circulation coupling waste disposal.
The technical scheme adopted by the invention is as follows: a cement production carbon capture device for local calcium circulation coupling waste disposal comprises a preheater-carbonization furnace-rotary kiln module, an off-line decomposition furnace module and an auxiliary and purification device, wherein the preheater-carbonization furnace-rotary kiln module comprises a first series of cyclone preheaters, a carbonization furnace, a second series of cyclone preheaters, a waste drying and thermal cracking device, a waste feeding device, a smoke chamber, a rotary kiln, a tertiary air pipe and a cooler; the off-line decomposing furnace module comprises a decomposing furnace, a third series of cyclone preheaters, a second air distribution device and a booster fan; the auxiliary and purifying device comprises a first SNCR device, a second SNCR device, a first air dividing device, a first material dividing device, a second material dividing device, a first heat exchange device, a second heat exchange device, a condensation and dehydration device, and a CO-rich device2The device comprises a gas collecting and storing device, a dust removing device, an SCR device and a flue gas discharging device;
the number of stages of the cyclone separators of the first series of cyclone preheaters is 4-7, the number of stages of the cyclone separators of the second series of cyclone preheaters is 1-2, and the number of stages of the cyclone separators of the third series of cyclone preheaters is 1-2.
According to the gas flow direction of the cement production carbon collecting device coupled with the local calcium circulation and the waste cooperative treatment, in the cement production carbon collecting device, a tertiary air pipe of a rotary kiln is divided into two paths through a first air distribution device, wherein one path enters a preheater-carbonization furnace-rotary kiln module and is connected with an air outlet of a smoke chamber and an air inlet of a second series of cyclone preheaters, and the other path enters an off-line decomposing furnace system and is directly connected with an inlet of a decomposing furnace;
the outlet of the waste drying and thermal cracking device is connected with the air inlet pipe of the second series of cyclone preheaters;
preferably, a first SNCR device is additionally arranged at the waste drying and thermal cracking device to reduce NOx emission;
an air inlet of the carbonization furnace is connected with an air outlet of the second series of cyclone preheaters;
the air inlet of the first series of cyclone preheaters is connected with the air outlet of the carbonization furnace;
the air outlet of the first series of cyclone preheaters is sequentially connected with the second heat exchange device, the dust removal device, the SCR device and the flue gas discharge device;
raw meal is fed into a first-stage cyclone separator air inlet pipe of a first series of cyclone preheaters through a raw meal feeding device, and a discharge port of a penultimate second-stage cyclone separator of the first series of cyclone preheaters is connected with a carbonization furnace. Preferably, the carbonization furnace is provided with a multi-stage necking structure, a feeding hole is arranged above each stage of necking structure, so that multi-point feeding can be realized, the heat exchange efficiency is improved, and the heat emitted by the carbonization reaction is fully utilized to preheat the raw materials;
the discharge port of the first-last cyclone separator of the first series of cyclone preheaters is connected with the air inlet pipe of the first-last cyclone separator of the second series of cyclone preheaters;
the discharge port of the second series of cyclone preheaters is connected with the decomposing furnace through a first material distributing device. Preferably, the decomposing furnace is provided with a multi-stage necking structure, a feeding hole is formed above each stage of necking structure, multi-point feeding can be achieved, and the decomposition reaction rate and efficiency of calcium carbonate are improved.
The decomposing furnace is connected with a feeding port of a third series of cyclone preheaters; the outlet of the decomposing furnace is connected with an air inlet pipe of a third series of cyclone preheaters, and the discharge port of the third series of cyclone preheaters is respectively connected with the carbonization furnace and the kiln tail of the rotary kiln through a second material distributing device to control the proportion of calcium oxide used for local calcium circulation;
preferably, an SNCR device is additionally arranged at the decomposing furnace to reduce NOx emission;
the lower part of the smoke chamber is connected with the tail of the rotary kiln, and the head of the rotary kiln is connected with a burner and a cooler.
An off-line decomposing furnace and local calcium circulation coupled cement production carbon capture process comprises the following steps:
the tertiary air of the cement kiln is divided into two paths by the first air dividing device, wherein one path of tertiary air enters the preheater-carbonization furnace-rotary kiln module, and the other path of tertiary air enters the off-line decomposition furnace module.
Cement raw materials are fed in an air inlet pipeline of a first-stage cyclone separator of the first series of cyclone preheaters, the heat exchange between the raw materials and flue gas fully occurs in the first series of cyclone preheaters, the cement raw materials enter a carbonization furnace from a penultimate cyclone separator of the first series of cyclone preheaters for further heat exchange, the temperature of gas in the carbonization furnace is reduced, and the carbonization reaction is favorably carried out.
Waste is fed into a waste feeding device in front of the waste drying and thermal cracking device, and kiln tail high-temperature flue gas and the waste are utilized to carry out sufficient heat exchange so as to dry the waste and reduce the temperature of the flue gas, thereby being beneficial to improving CO in a carbonization furnace2Capture efficiency and rate. Meanwhile, the thermal cracking of wastes is promoted, strong reducing components such as ammonia gas, hydrogen gas and hydrocarbon substances are released, NOx generated by fuel combustion is efficiently reduced, the source emission reduction of cement kiln pollutants is realized, and the CO in the flue gas is further improved2And (4) concentration.
The waste drying and thermal cracking device is provided with a multi-stage necking structure, and the heat exchange efficiency of waste and high-temperature gas is improved by utilizing the spouting effect of the necking structure, so that the air inlet temperature of the carbonization furnace is reduced, the yield of strong reduction components is improved, and the carbon sequestration efficiency and the source emission reduction NOx efficiency are improved.
The waste is one or more of domestic garbage, water treatment sludge, river sludge and waste tires.
Hot raw materials and waste drying after gas-solid separation by a first-last-stage cyclone separator of the first series of cyclone preheaters and air outlet of a thermal cracking device enter an air inlet pipeline of the second series of cyclone preheaters together, the air inlet temperature of the carbonization furnace is further reduced through heat exchange, and a foundation is laid for improving the carbonization reaction rate and efficiency. In addition, SO released by the thermal decomposition of the sulphides contained in the raw meal during the preheating process2Is discharged along with the flue gas, thereby reducing SO2The content of the impurity gas enters an off-line decomposing furnace module so as to obtain high-purity CO2。
The decomposing furnace is provided with a multi-stage necking structure, and a feeding hole is formed above each stage of necking structure. After the gas-solid separation of the flue gas through the second series of cyclone preheaters, hot raw materials are fed into the feed inlets at different positions of the decomposing furnace through the first separating and distributing device in a multi-point mode, so that the decomposing rate and the decomposing efficiency of the calcium carbonate are improved.
The first material distributing device is arranged on a pipeline connecting the second series of cyclone preheaters and the decomposing furnace and is used for adjusting the quantity of hot raw materials entering different parts of the decomposing furnace.
And decomposing furnace burners are arranged at different positions of the decomposing furnace and used for uniformly injecting fuel, so that the temperature field distribution of the decomposing furnace is uniform.
The decomposing furnace burners are all positioned above each stage of reducing structure of the decomposing furnace, are lower than the feed inlet and are used for injecting fuel.
The thermal raw meal is decomposed in a decomposing furnace to produce a large amount of CO2NO in small amountxRemoving by adopting an SNCR device, after gas-solid separation by a third series of cyclone preheaters, enabling the flue gas to enter a second air dividing device and be divided into two paths, and enabling one path to sequentially pass through a first heat exchange device and a condensation water removal device to obtain CO-rich flue gas2Gas, into rich CO2A gas collection and storage device; the other path of the flue gas enters the decomposing furnace again through the booster fan for flue gas circulation.
The second wind-dividing device is arranged on the third series of rotary shaftsOn the air outlet pipeline of the air preheater for regulating the entering of rich CO2Gas collection and storage device or the gas amount circulated by the flue gas of the decomposing furnace.
After gas-solid separation of the hot raw material containing a large amount of CaO by a third series of cyclone preheaters, the hot raw material is divided into two paths by a second material distribution device, the first path of hot raw material is fed into an air inlet pipe of a carbonization furnace, is quickly carbonized in a flue gas environment of 600-850 ℃, and CO in the flue gas is captured by local calcium circulation between the carbonization furnace and a decomposing furnace2. The second path of hot raw material is fed into the tail of the rotary kiln and enters the rotary kiln to participate in the burning of clinker.
The method has the following beneficial effects: the decomposing furnace module of the novel dry-method cement kiln is designed in an off-line mode, wastes are introduced into the preheater-carbide furnace-rotary kiln module, the temperature of kiln tail flue gas is reduced, the source emission reduction of NOx is realized, and the CO is improved2The capture rate and efficiency are improved, and the flue gas CO of the cement kiln is further promoted2To reduce CO2Difficulty in recycling.
Drawings
The invention is further illustrated with reference to the following figures and examples:
fig. 1 is a block diagram showing the structure of a cement production carbon capture device with local calcium circulation coupled with waste disposal.
Description of reference numerals: 1-a first series of cyclone preheaters, 2-a second series of cyclone preheaters, 3-a third series of cyclone preheaters, 4-a carbonization furnace, 5-a first SNCR device, 6-a smoke chamber, 7-a rotary kiln, 8-a rotary kiln burner, 9-a cooler, 10-a first air distribution device, 11-a first material distribution device, 12-a decomposition furnace, 13-a decomposition furnace burner, 14-a second SNCR device, 15-a second air distribution device, 16-a first heat exchange device, 17-a condensation water removal device and 18-rich CO2The system comprises a gas collecting and storing device, a 19-booster fan, a 20-raw material feeding device, a 21-second heat exchange device, a 22-dust removal device, a 23-SCR device, a 24-flue gas exhaust device, a 25-tertiary air pipe, a 26-second material dividing device, a 27-waste drying and thermal cracking device and a 28-waste feeding device.
Detailed Description
Reference will now be made in detail to the present preferred embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to like elements throughout.
In the description of the present invention, it should be understood that the orientation or positional relationship referred to in the description of the orientation, such as the upper, lower, front, rear, left, right, etc., is based on the orientation or positional relationship shown in the drawings, and is only for convenience of description and simplification of description, and does not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
In the description of the present invention, the meaning of a plurality of means is one or more, the meaning of a plurality of means is two or more, and larger, smaller, larger, etc. are understood as excluding the number, and larger, smaller, inner, etc. are understood as including the number. If the first and second are described for the purpose of distinguishing technical features, they are not to be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated or implicitly indicating the precedence of the technical features indicated.
In the description of the present invention, unless otherwise expressly limited, the terms "connected" and "connected" are to be construed broadly, e.g., as meaning a fixed connection, a removable connection, or an integral connection; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. In the description of the present invention, the terms "injection" and "injection" refer to the introduction of said gaseous or solid material into a desired location by various means known to those skilled in the art, the terms "injection" and "injection" being used interchangeably.
In the description of the present invention, unless otherwise explicitly limited, terms such as arrangement, installation, connection and the like should be understood in a broad sense, and those skilled in the art can reasonably determine the specific meanings of the above terms in the present invention in combination with the specific contents of the technical solutions.
The terms appearing below are explained first:
SNCR: selective non-catalytic reduction; SCR: and (4) selective catalytic reduction.
As shown in fig. 1, an embodiment of the present invention provides a cement production carbon capture device for local calcium circulation coupling waste disposal, where the cement production carbon capture device includes a first series of cyclone preheaters 1, a second series of cyclone preheaters 2, a third series of cyclone preheaters 3, a carbonization furnace 4, a first SNCR device 5, a smoke chamber 6, a rotary kiln 7, a rotary kiln burner 8, a cooler 9, a first air distribution device 10, a first material distribution device 11, a decomposition furnace 12, a decomposition furnace burner 13, a second SNCR device 14, a second air distribution device 15, a first heat exchange device 16, a condensation and water removal device 17, a CO-rich device 172The system comprises a gas collecting and storing device 18, a booster fan 19, a raw material feeding device 20, a second heat exchange device 21, a dust removal device 22, an SCR device 23, a flue gas exhaust device 24, a tertiary air pipe 25, a second material distribution device 26, a waste drying and thermal cracking device 27 and a waste feeding device 28.
The number of stages of the cyclone separators of the first series of cyclone preheaters 1 is 4, the number of stages of the cyclone separators of the second series of cyclone preheaters 2 is 1, and the number of stages of the cyclone separators of the third series of cyclone preheaters 3 is 1.
In the carbon trapping device for cement production, the tertiary air pipe 25 is divided into two paths by the first air dividing device 10, wherein one path enters the preheater-carbonization furnace-rotary kiln module and is connected with the air outlet of the smoke chamber 6 and the air inlet of the waste drying and thermal cracking device 27; the other path enters an off-line decomposing furnace module and is directly connected with an inlet of the decomposing furnace 12;
the outlet of the waste drying and thermal cracking device 27 is connected with the air inlet pipe of the second series cyclone preheater 2; preferably, the waste drying and thermal cracking unit 27 is additionally provided with a first SNCR unit 5 to reduce NOx emission.
An air inlet of the carbonization furnace 4 is connected with an air outlet of the second series of cyclone preheaters 2; the air inlet of the first series of cyclone preheaters 1 is connected with the air outlet of the carbonization furnace 4; the air outlet of the first series of cyclone preheaters 1 is connected with the second heat exchange device 21, the dust removal device 22, the SCR device 23 and the flue gas exhaust device 24 in sequence.
Raw meal is fed into the air inlet pipe of the first-stage cyclone separator of the first series of cyclone preheaters 1 through a raw meal feeding device 20, and the discharge port of the penultimate second-stage cyclone separator of the first series of cyclone preheaters 1 is connected with a carbonization furnace 4. Preferably, the raw meal can be fed at multiple points, the heat exchange efficiency is improved, and the heat released by the carbonization reaction is fully utilized to preheat the raw meal; the carbonization furnace 4 has a multi-stage necking structure, and gas-solid full contact is realized through spouting many times, so that the carbonization rate and efficiency are improved.
The discharge port of the first-last cyclone separator of the first series of cyclone preheaters 1 is connected with the air inlet pipe of the first-last cyclone separator of the second series of cyclone preheaters 2.
The discharge port of the second series cyclone preheater 2 is connected with the decomposing furnace 12 through the first material distributing device 11, and preferably, the materials can be fed at multiple points, so that the decomposition reaction rate and efficiency of the calcium carbonate are improved.
The decomposing furnace 12 is connected with an air inlet pipe of the third series of cyclone preheaters 3; the outlet of the decomposing furnace 12 is connected with the air inlet pipe of the third series of cyclone preheaters 3, the discharge port of the third series of cyclone preheaters 3 is respectively connected with the carbonization furnace 4 and the kiln tail of the rotary kiln 7 through a second material distributing device 26, and the proportion of calcium oxide used for local calcium circulation is controlled.
Preferably, a second SNCR device 14 is added to the decomposition furnace 12 to reduce NOx emissions.
The lower part of the smoke chamber 6 is connected with the kiln tail of the rotary kiln 7, and the kiln head of the rotary kiln 7 is connected with a rotary kiln combustor 8 and a cooler 9.
A cement production carbon capture process coupling local calcium circulation and waste cooperative treatment specifically comprises the following steps:
the tertiary air of the cement kiln is divided into two paths by the first air dividing device 10, one path of tertiary air enters the preheater-carbonization furnace-rotary kiln module, and the other path of tertiary air enters the off-line decomposition furnace module.
The raw material feed arrangement 20 feeding of cement raw material at first order cyclone air inlet duct department of first series cyclone preheater 1 fully takes place heat exchange with the flue gas in first series cyclone preheater 1, gets into carbonization furnace 4 further heat exchange from the second last cyclone of first series cyclone preheater 1, reduces the interior gas temperature of carbonization furnace 4, is favorable to going on of carbonization reaction.
Waste is fed into a waste feeding device 28 in front of the waste drying and thermal cracking device 27, kiln tail high-temperature flue gas and the waste are utilized to perform sufficient heat exchange, so that the waste is dried, the temperature of the flue gas at the outlet of the waste drying and thermal cracking device 27 is reduced, the thermal cracking of the waste is promoted, strong reducing components such as ammonia gas, hydrogen gas and hydrocarbon substances are released, NOx generated by fuel combustion is efficiently reduced, the source emission reduction of pollutants in the cement kiln is realized, and the CO in the flue gas is further improved2And (4) concentration.
The waste drying and thermal cracking device 27 has a multi-stage necking structure, and improves the heat exchange efficiency of waste and high-temperature gas by utilizing the spouting effect of the necking structure so as to reduce the air inlet temperature of the carbonization furnace and improve the yield of strong reducing components, thereby improving the carbon fixation efficiency and the source emission reduction NOx efficiency.
The waste is a mixture of domestic garbage, water treatment sludge, river sludge and waste tires.
Hot raw materials and waste dried after gas-solid separation by the last-to-last stage cyclone separator of the first series of cyclone preheaters 1 and the outlet air of the thermal cracking device 27 enter an air inlet pipeline of the second series of cyclone preheaters 2 together, the inlet air temperature of the carbonization furnace is further reduced through heat exchange, and a foundation is laid for improving the carbonization reaction rate and efficiency. In addition, SO released by the thermal decomposition of the sulphides contained in the raw meal during the preheating process2Is discharged along with the flue gas, thereby reducing SO2The content of the impurity gas enters an off-line decomposing furnace module so as to obtain high-purity CO2。
The decomposing furnace 12 is provided with a multi-stage necking structure, and a feeding hole is arranged above each stage of necking structure. After the gas-solid separation of the flue gas through the second series of cyclone preheaters 2, hot raw materials are fed into the feed inlets at different positions of the decomposing furnace 12 through the first material distributing device 11 at multiple points so as to improve the decomposition rate and efficiency of the calcium carbonate.
The first distributing device 11 is arranged on the pipeline connecting the second series of cyclone preheaters 2 and the decomposing furnace 12 and is used for adjusting the quantity of hot raw meal entering different parts of the decomposing furnace 12.
The decomposing furnace burners 13 are arranged at different positions of the decomposing furnace 12 and used for uniformly injecting fuel, so that the uniform distribution of the temperature field of the decomposing furnace 12 is ensured.
The decomposing furnace burners 13 are all positioned above each stage of reducing structure of the decomposing furnace 12, are lower than the feed inlet, and are used for injecting fuel.
The decomposition of the hot raw meal in the decomposing furnace 12 produces a large amount of CO2NO in small amountxRemoving by a second SNCR device 14, after gas-solid separation by a third series of cyclone preheaters 3, the flue gas enters a second air distribution device 15 and is divided into two paths, and one path of flue gas passes through a second heat exchange device 16 and a condensation water removal device 17 in sequence to obtain CO-rich flue gas2Gas, into rich CO2A gas collection and storage device 18; the other path of the flue gas enters the decomposing furnace again for circulation through a booster fan 19.
The second air dividing device 15 is arranged on an air outlet pipeline of the third series of cyclone preheaters 3 and is used for adjusting the entering of rich CO2Gas collection and storage device 18 or the amount of gas circulated by the flue gas of decomposition furnace 12.
After gas-solid separation of the hot raw material containing a large amount of CaO by the third series of cyclone preheaters 3, the hot raw material is divided into two paths by the second material distribution device 26, the first path of hot raw material is fed into the air inlet pipe of the carbonization furnace 4, is rapidly carbonized in the smoke environment of 600-850 ℃, and CO in smoke is captured by local calcium circulation between the carbonization furnace 4 and the decomposition furnace 122. The second path of hot raw material is fed into the tail of the rotary kiln 7 and enters the rotary kiln 7 to participate in the burning of clinker.
The invention relates to a cement production carbon capture process and device with local calcium circulation and waste cooperative treatment coupled, which are applied to the cross technical field of cement production and calcium circulation carbon capture. Compared with the prior art, the invention has the following advantages and effects:
1) an off-line design of a decomposing furnace module is adopted, and the temperature of tertiary air and O are utilized2The high content of the catalyst can reduce the air demand and energy consumption of the decomposing furnace; through the circulation of the flue gas of the decomposing furnace, the gas-solid two-phase fluidization in the decomposing furnace is realized under the condition of not increasing the amount of the flue gas, and CaCO is improved3The decomposition efficiency is further improved, and the CO in the gas is further improved2Thereby realizing CO in the flue gas of the cement kiln2Is self-enriched at high concentration. Through the coupling of local calcium circulation and an off-line decomposing furnace, the flue gas CO is realized under the traditional air combustion condition2Self-enrichment obviously improves the technical economy.
2) The off-line design of the decomposing furnace module in the cement kiln system prevents volatile substances such as chlor-alkali sulfur and the like generated in the rotary kiln from entering the decomposing furnace module; on the other hand, SO released by decomposition of sulfide in raw material in the first series of preheaters2When the impurity gas can not enter the decomposing furnace module, the separating decomposing furnace module is favorable for obtaining the CO with ultrahigh concentration and purity2The difficulties of subsequent purification, utilization and the like are further reduced by the smoke.
3) The amount of CaO entering the local calcium circulation of the carbonization furnace and the amount of CaO entering the rotary kiln are regulated and controlled by a material distribution device at the outlet of the third series of cyclone preheaters, the CaO entering a calcium circulation system is dynamically updated, and the CO is maintained by the CaO2The absorption activity of the calcium carbonate realizes the calcium circulation to CO2The continuous and high-efficiency trapping effect is achieved.
4) The waste is dried and thermally cracked at high temperature by using the flue gas, the temperature of the flue gas is reduced, and then the waste enters a second series of cyclone preheaters, the temperature of raw materials is improved through gas-solid heat exchange, and the temperature of the flue gas counted into a carbonization furnace is further reduced. Simultaneously, raw materials are fed into the carbonization furnace at multiple points, and heat released by carbonization is absorbed through heat exchange to reduce the temperature of flue gas, thereby reducing CaCO in the carbonization furnace3The resolubilization rate of the catalyst is improved, and the carbonization reaction rate is improved. In addition, the waste is thermally cracked to release strong reducing components such as ammonia gas, hydrogen gas, hydrocarbon substances and the like, NOx generated by fuel combustion can be efficiently reduced, namely, source emission reduction of cement kiln pollutants is realized by CO-processing the waste, and CO in flue gas is further improved2And (4) concentration.
5) The decomposing furnace adopts a multi-stage necking structure design, exerts the spouting effect to make the materials fully contact with the combustion-supporting gas, improves the combustion efficiency and improves the CO2The generation amount is controlled, the generation of NOx and CO is controlled, the temperature field in the decomposing furnace is uniformly distributed by utilizing the multi-stage injection of hot raw materials and fuel, the local overheating is avoided, and the equipment is ensuredThe operation is safe.
6) The decomposing furnace and the smoke chamber air outlet are both provided with SNCR devices to realize NO in smokexThe content of impurity gas in the flue gas is reduced, and CO is ensured2Is enriched at a high concentration.
In summary, the invention provides the off-line design of the decomposing furnace module based on the characteristics of high calcium content, gas-solid flow direction and dynamic characteristics of the cement kiln system, and realizes the CO in the cement kiln system by matching materials with a temperature field and using waste treatment for cooperation in parallel connection2The method has the advantages that the carbon capture potential of the novel dry-method cement kiln is fully developed due to high-concentration enrichment and stable capture, the resource recycling of the cement kiln smoke is facilitated, the harm reduction treatment of wastes can be realized, and the sustainable development of the cement industry is powerfully promoted.
While the embodiments of the present invention have been described in detail with reference to the drawings, the present invention is not limited to the above embodiments, and various changes can be made without departing from the spirit of the present invention within the knowledge of those skilled in the art.
Claims (7)
1. The cement production carbon capture device for local calcium circulation coupling waste disposal is characterized by comprising a preheater-carbonization furnace-rotary kiln module, an off-line decomposition furnace module and an auxiliary and purification device, wherein the preheater-carbonization furnace-rotary kiln module comprises a raw material feeding device (20), a first series of cyclone preheaters (1), a carbonization furnace (4), a second series of cyclone preheaters (2), a waste drying and thermal cracking device (27), a waste feeding device (28), a smoke chamber (6), a rotary kiln (7), a rotary kiln combustor (8), a tertiary air pipe (25) and a cooler (9); the off-line decomposing furnace module comprises a decomposing furnace (12), a decomposing furnace burner (13), a third series of cyclone preheaters (3), a second air distribution device (15) and a booster fan (19); the auxiliary and purifying device comprises a first SNCR device (5), a second SNCR device (14), a first air dividing device (10), a first material dividing device (11), a second material dividing device (26), a first heat exchange device (16), a second heat exchange device (21), a condensation and water removal device (17), a CO-rich gas2Gas collecting and storing deviceA device (18), a dust removal device (22), an SCR device (23) and a flue gas discharge device (24);
the tertiary air pipe (25) is divided into two paths through the first air distribution device (10), wherein one path enters the preheater-carbonization furnace-rotary kiln module and is connected with the air outlet of the smoke chamber (6) and the air inlet of the waste drying and thermal cracking device (27); the other path enters an off-line decomposing furnace module and is directly connected with an inlet of a decomposing furnace (12);
the outlet of the waste drying and thermal cracking device (27) is connected with the air inlet pipe of the second series of cyclone preheaters (2); the first SNCR device (5) is arranged at the waste drying and thermal cracking device (27);
an air inlet of the carbonization furnace (4) is connected with an air outlet of the second series of cyclone preheaters (2); the air inlet of the first series of cyclone preheaters (1) is connected with the air outlet of the carbonization furnace (4); the air outlets of the first series of cyclone preheaters (1) are sequentially connected with a second heat exchange device (21), a dust removal device (22), an SCR device (23) and a flue gas discharge device (24);
raw materials are fed into an air inlet pipe of a first-stage cyclone separator of a first series of cyclone preheaters (1) through a raw material feeding device (20), a discharge port of a penultimate second-stage cyclone separator of the first series of cyclone preheaters (1) is connected with a carbonization furnace (4), and hot raw materials can be fed at multiple points;
the discharge port of the first-last-stage cyclone separator of the first series of cyclone preheaters (1) is connected with the air inlet pipe of the first-last-stage cyclone separator of the second series of cyclone preheaters (2); the discharge hole of the second series of cyclone preheaters (2) is connected with the decomposing furnace (12) through a first material distributing device (11); the outlet of the decomposing furnace (12) is connected with the air inlet pipe of the third series of cyclone preheaters (3), and the discharge port of the third series of cyclone preheaters (3) is respectively connected with the carbonization furnace (4) and the kiln tail of the rotary kiln (7) through a second material distribution device (26); a second SNCR device (14) is arranged at the decomposition furnace (12);
the lower part of the smoke chamber (6) is connected with the kiln tail of the rotary kiln (7), and the kiln head of the rotary kiln (7) is connected with a rotary kiln combustor (8) and a cooler (9).
2. The local calcium looping coupled waste disposal cement producing carbon capture plant of claim 1, wherein: the number of stages of cyclone separators of the first series of cyclone preheaters (1) is 4-7, the number of stages of cyclone separators of the second series of cyclone preheaters (2) is 1-2, and the number of stages of cyclone separators of the third series of cyclone preheaters (3) is 1-2.
3. The local calcium looping coupled waste disposal cement producing carbon capture plant of claim 1, wherein: the carbonization furnace (4) is provided with a multi-stage necking structure, and a feeding hole is formed above each stage of necking structure.
4. The local calcium looping coupled waste disposal cement producing carbon capture plant of claim 1, wherein: the decomposing furnace (12) is provided with a multi-stage necking structure, and a feeding hole is formed above each stage of necking structure.
5. The local calcium looping coupled waste disposal cement producing carbon capture plant of claim 4, wherein: a plurality of decomposing furnace burners (13) are arranged on the decomposing furnace (12), and the decomposing furnace burners (13) are all arranged above each stage of reducing structure of the decomposing furnace (12) and are arranged below the feeding hole.
6. The local calcium looping coupled waste disposal cement producing carbon capture plant of claim 1, wherein: the waste is one or more of domestic garbage, water treatment sludge, river sludge and waste tires.
7. The capture process of the cement production carbon capture device by local calcium circulation coupled waste disposal is characterized by comprising the following steps of:
the tertiary air of the cement kiln is divided into two paths by a first air dividing device (10), one path of tertiary air enters a preheater-carbonization furnace-rotary kiln module, and the other path of tertiary air enters an off-line decomposing furnace module;
cement raw materials are fed into a raw material feeding device (20) at an air inlet pipeline of a first-stage cyclone separator of a first series of cyclone preheaters (1), the raw materials and smoke fully generate heat exchange in the first series of cyclone preheaters (1), and the heat exchange enters a carbonization furnace (4) from a penultimate second-stage cyclone separator of the first series of cyclone preheaters (1);
feeding waste into a waste feeding device (28) in front of the waste drying and thermal cracking device (27), and performing sufficient heat exchange between the kiln tail high-temperature flue gas and the waste to dry the waste and reduce the temperature of the flue gas at the outlet of the waste drying and thermal cracking device (27);
hot raw materials and waste dried after gas-solid separation by a first-stage cyclone separator arranged at the last of the first series of cyclone preheaters (1) and the outlet air of the thermal cracking device (27) enter an air inlet pipeline of a second series of cyclone preheaters (2) together; after gas-solid separation of the flue gas is carried out by the second series of cyclone preheaters (2), hot raw materials are fed into feed inlets at different positions of the decomposing furnace (12) at multiple points by the first material distributing device (11);
the decomposition of the hot raw meal in the decomposing furnace (12) produces a large amount of CO2A small amount of fuel type NOx is removed by a second SNCR device (14), after gas-solid separation is carried out by a third series of cyclone preheaters (3), the flue gas enters a second air dividing device (15) and is divided into two paths,
one path of the water passes through a first heat exchange device (16) and a condensation water removal device (17) in sequence to obtain CO-rich water2Gas, into rich CO2A gas collection and storage device (18); the other path of the flue gas enters the decomposing furnace again through a booster fan (19) for circulation;
after gas-solid separation of a large amount of CaO-containing hot raw materials by a third series of cyclone preheaters (3), the hot raw materials are divided into two paths by a second material distribution device (26), the first path of hot raw materials are fed into an air inlet pipe of a carbonization furnace (4), are quickly carbonized in a flue gas environment at 600-850 ℃, and CO in the flue gas is captured by local calcium circulation between the carbonization furnace (4) and a decomposition furnace (12)2(ii) a The second path of hot raw material is fed into the kiln tail of the rotary kiln (7) and enters the rotary kiln (7) to participate in the burning of clinker.
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