CN116477854A - Lime kiln equipment based on carbon emission reduction and control method thereof - Google Patents
Lime kiln equipment based on carbon emission reduction and control method thereof Download PDFInfo
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- CN116477854A CN116477854A CN202310551266.4A CN202310551266A CN116477854A CN 116477854 A CN116477854 A CN 116477854A CN 202310551266 A CN202310551266 A CN 202310551266A CN 116477854 A CN116477854 A CN 116477854A
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- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 137
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 137
- 239000004571 lime Substances 0.000 title claims abstract description 137
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims description 62
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 236
- 239000003546 flue gas Substances 0.000 claims abstract description 236
- 239000000779 smoke Substances 0.000 claims abstract description 85
- 239000007789 gas Substances 0.000 claims abstract description 77
- 238000003860 storage Methods 0.000 claims abstract description 62
- 238000001816 cooling Methods 0.000 claims description 108
- 239000000446 fuel Substances 0.000 claims description 79
- 238000002485 combustion reaction Methods 0.000 claims description 59
- 239000000428 dust Substances 0.000 claims description 50
- 238000001354 calcination Methods 0.000 claims description 35
- 238000001514 detection method Methods 0.000 claims description 34
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 31
- 229910052760 oxygen Inorganic materials 0.000 claims description 31
- 239000001301 oxygen Substances 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 20
- 235000019738 Limestone Nutrition 0.000 claims description 19
- 239000006028 limestone Substances 0.000 claims description 19
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 16
- 238000010992 reflux Methods 0.000 claims description 15
- 230000000740 bleeding effect Effects 0.000 claims description 13
- 239000007921 spray Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 230000005540 biological transmission Effects 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- 238000000354 decomposition reaction Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 4
- 239000002699 waste material Substances 0.000 abstract description 11
- 238000011084 recovery Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 63
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 50
- 239000000292 calcium oxide Substances 0.000 description 27
- 238000004519 manufacturing process Methods 0.000 description 26
- 235000012255 calcium oxide Nutrition 0.000 description 25
- 239000003245 coal Substances 0.000 description 25
- 238000002156 mixing Methods 0.000 description 14
- 239000002817 coal dust Substances 0.000 description 13
- 238000004364 calculation method Methods 0.000 description 10
- 239000012535 impurity Substances 0.000 description 8
- 238000009825 accumulation Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000003517 fume Substances 0.000 description 5
- 239000000843 powder Substances 0.000 description 5
- 239000012159 carrier gas Substances 0.000 description 4
- 239000002826 coolant Substances 0.000 description 4
- 239000000112 cooling gas Substances 0.000 description 4
- 230000005855 radiation Effects 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 238000010790 dilution Methods 0.000 description 3
- 239000012895 dilution Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000002159 abnormal effect Effects 0.000 description 2
- 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
- 238000009826 distribution Methods 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 238000005338 heat storage Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 230000003139 buffering effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 229940098458 powder spray Drugs 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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
- C04B2/00—Lime, magnesia or dolomite
- C04B2/10—Preheating, burning calcining or cooling
- C04B2/12—Preheating, burning calcining or cooling in shaft or vertical furnaces
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
A lime kiln plant based on carbon emission reduction, comprising a double-hearth lime kiln. The double-hearth lime kiln comprises two hearths which are arranged in a mirror image mode, and a connecting channel is arranged between the two hearths. Kiln top valves are arranged at the upper parts of the two hearths. The kiln top valve is respectively connected with the hearth, the combustion-supporting air pipeline or the flue gas discharge pipeline. The flue gas exhaust pipeline is respectively connected with a finished pipeline and a circulating pipeline, wherein the finished pipeline is connected to CO 2 And the finished product system, the circulating pipeline is connected to the hearth. The storage pipeline is separated from the circulating pipeline and connected to the buffer tower. The invention is provided with the CO with the slow storage tower 2 Recovery system, the extension of slow storage tower can prevent lime kiln tail gas CO 2 When the concentration is low, only the resource waste of the external discharge can be realized, and the CO in the smoke can be improved through the smoke circulation 2 Concentration of CO 2 Gradually enriching, while producing lime, high-purity CO 2 And (3) gas.
Description
Technical Field
The invention relates to a lime production device and method, in particular to lime kiln equipment based on carbon emission reduction and a control method thereof, and belongs to the technical field of lime production.
Background
Lime is an important industrial raw material and has wide application in the fields of metallurgy, construction and the like. The domestic lime yield in 2020 is about 3 hundred million tons, and the industrial scale is huge. At the same time, however, lime production results in large amounts of CO 2 And (5) discharging. Statistically, 1kg lime produced 1.1kg CO 2 Emission, so as to estimate the CO emitted to the atmosphere in the lime production process in China 2 The total amount exceeds 3 hundred million tons/year, and low CO is developed under the background of carbon emission reduction in the whole industry 2 The discharged lime production process and technology become hot spots and difficulties in technical research in the field.
The double-chamber lime shaft kiln is industrial lime production equipment with wider application and advanced technology at present, and can obtain extremely high heat efficiency by adopting a double-chamber heat storage calcination process. The heat required by the calcining step is provided by adopting a mode of directly supplying heat through fossil fuel combustion, the cooling step adopts normal-temperature air as a refrigerant medium, and the preheating step uses high-temperature flue gas generated by the calcining and cooling steps as a heat source. The process design can fully utilize the waste heat of the flue gas, and has higher fuel utilization efficiency. However, since the calcination flue gas is mixed with the cooling air, N in the tail gas 2 The impurity gases are more, so that CO in the exhaust gas is caused 2 The concentration is low, generally only 20 to 30 percent, so that CO in the tail gas is reduced 2 The difficulty of the enrichment and trapping technology is high, and the cost is high. Resulting in CO in tail gas of lime kiln at present 2 The enrichment and trapping are almost zero, and serious greenhouse gas emission and resource waste are generated.
Fig. 3 is a schematic view of the structure of the two-chamber lime kiln which is most widely used at the present stage. The kiln mainly comprises two kiln bores which are mirror images of each other, and a connecting channel for communicating gas is arranged between the two kiln bores. The middle part of the kiln chamber is provided with a buried pulverized coal spray gun, the side part is provided with a channel for entering combustion-supporting air and discharging smoke, the bottom part is provided with a cooling air pipeline, the top part is provided with a smoke pipeline, and the tail part of the smoke pipeline is provided with a smoke pipelineThe end is connected with a dust remover. In the production process, lime material is fed into combustion chamber from the top of kiln chamber, and combustion-supporting air (O) 2 ：21％，N 2 : 79%) are fed into the combustion chamber from the side, and the pulverized coal is fed into the combustion chamber by a conveying wind (O) 2 ：21％，N 2 : 79%) is fed into combustion chamber from coal powder spray gun, coal powder is burnt in combustion chamber to produce high-temperature flue gas, lime material is heated, lime material is quickly heated and decomposed to produce CaO and CO 2 . The high-temperature CaO produced moves downward and is cooled by the cooling air (O 2 ：21％，N 2 : 79%) is cooled to below 100 ℃ and discharged from the bottom of the hearth, thus forming the finished CaO product. The high-temperature air generated by cooling the high-temperature CaO and the high-temperature flue gas generated by calcining enter the heat accumulation chamber from the connecting channel, heat exchange is carried out on the high-temperature air and the high-temperature flue gas with the cold material in the heat accumulation chamber, the temperature is reduced to about 120 ℃ and then the high-temperature air and the high-temperature flue gas are discharged from a flue gas outlet at the top, and the high-temperature flue gas is discharged into the surrounding environment after dust removal and purification through a dust remover at the tail end of a flue gas pipeline. And the two kiln bores have periodic exchange roles, so that the continuous calcination of lime is completed.
Under the existing equipment structure, a large amount of O is introduced into the system in the combustion-supporting, cooling and pulverized coal conveying links 2 And N 2 Impurity gases (relative to by-product CO) 2 In other words), leading to CO in the exhaust fumes 2 The content is very low, generally only 20 to 30%. CO 2 Enrichment and trapping cost and CO in flue gas 2 Initial concentration is inversely related to CO 2 The lower the concentration, the higher the enrichment capture cost. Tail gas CO produced by lime under existing equipment 2 Too low concentration results in high enrichment and trapping cost, which becomes a constraint for CO in the lime production process 2 The main obstacle for recycling.
Disclosure of Invention
For the above prior art due to CO 2 CO caused by high difficulty in enrichment and trapping 2 The invention provides lime kiln equipment based on carbon emission reduction and a control method thereof. In the scheme of the invention, the flue gas discharge pipeline of the lime kiln is respectively connected with a finished pipeline and a circulating pipeline, and the finished pipeline is connected to CO 2 The finished product system is used as CO 2 The finished product is directly produced, and the circulating pipeline is connected to the hearth to obtain CO required by each working procedure of the hearth 2 Gas and its preparation methodRealizing self-circulation supply, avoiding the introduction of external air into N 2 CO of the impurity components 2 Is used for dilution of the sample. The circulating pipeline is also provided with a separating storage pipeline which is connected to the slow storage tower, and the slow storage tower can prevent the tail gas CO of the lime kiln 2 When the concentration is insufficient, only the resource waste of the discharged gas can be avoided, and the CO in the flue gas can be improved through the flue gas circulation 2 Concentration of CO in flue gas 2 The concentration is gradually enriched, thereby achieving the purpose of ensuring the product quality. Therefore, the scheme of the invention can greatly improve the tail gas CO in the lime production process 2 Concentration, high purity CO is obtained while lime is produced 2 Gaseous byproducts.
According to a first embodiment of the invention, a lime kiln plant based on carbon reduction is provided.
A lime kiln plant based on carbon emission reduction, comprising a double-hearth lime kiln. The double-hearth lime kiln comprises two hearths which are arranged in a mirror image mode, and a connecting channel is arranged between the two hearths. Kiln top valves are arranged at the upper parts of the two hearths. The kiln top valve is respectively connected with the hearth, the combustion-supporting air pipeline or the flue gas discharge pipeline. The flue gas exhaust pipeline is respectively connected with a finished pipeline and a circulating pipeline, wherein the finished pipeline is connected to CO 2 And the finished product system, the circulating pipeline is connected to the hearth. The storage pipeline is separated from the circulating pipeline and connected to the buffer tower.
In the invention, the middle part of the hearth is provided with a buried fuel spray gun. The circulating pipeline is divided into three pipelines, namely a cooling air pipeline, a fuel air conveying pipeline and a combustion-supporting flue gas pipeline. Wherein, the cooling air pipeline is connected to the cooling air inlet of furnace bottom, and fuel delivery pipe is connected to the entry of fuel spray gun, and combustion-supporting flue gas pipeline is connected to the entry of combustion-supporting air pipeline. The combustion-supporting air pipeline is also connected with an oxygen conveying pipeline.
Preferably, the combustion-supporting air pipeline is provided with a mixer. The mixer comprises two inlets and an outlet, wherein the outlet of the mixer is connected with the kiln top valve through a combustion-supporting air pipeline, and the two inlets of the mixer are respectively connected with a combustion-supporting flue gas pipeline and an oxygen conveying pipeline.
In the invention, the diffusing pipeline and the reflux pipeline are connected to the slow storage tower. The return line is connected to the circulation line and the connection location is located on the circulation line downstream of the location of the split storage line.
Preferably, the storage line is provided with an inlet valve. And a short-circuit valve is arranged on the circulating pipeline and between the storage pipeline and the reflux pipeline.
Preferably, the bleeding pipe is provided with a bleeding valve. The reflux pipeline is provided with a reflux valve.
Preferably, the lime kiln equipment further comprises a flue gas distributor arranged at the connection position of the flue gas discharge pipeline, the finished product pipeline and the circulating pipeline.
Preferably, a flow divider is provided at a position where three pipes are branched from the circulation pipe.
In the invention, a cooling device is arranged on the cooling air pipeline. Preferably, the cooling device is a water bath or an air cooler.
In the invention, a dust remover is arranged on the flue gas discharge pipeline. Preferably, the dust remover is an electric dust remover or a cloth bag dust remover.
Preferably, the flue gas exhaust pipeline is provided with CO at the downstream of the dust remover 2 Concentration detection means.
Preferably, a pressure detection device is installed on the buffer tower. In the present application, CO 2 The related detecting means such as the concentration detecting means and the pressure detecting means are not shown in the drawings.
According to a second embodiment of the invention, a control method of lime kiln equipment based on carbon emission reduction is provided.
A method of controlling a lime kiln plant based on carbon emission reduction or a method of controlling a lime kiln plant according to the first embodiment to produce lime, the method comprising the steps of:
1) Limestone material enters from the top of the hearth, and pure oxygen and circulating flue gas which are conveyed by an oxygen conveying pipeline and a combustion-supporting flue gas pipeline are mixed in a mixer to form O 2 With CO 2 Combustion-supporting air of the mixed gas is sent into a hearth from a kiln top valve through a combustion-supporting air pipeline, and fuel is delivered into an air pipe by fuelThe circulating flue gas conveyed by the flue gas conveying way is used as a carrier to be sent into a hearth from a fuel spray gun, fuel and combustion air are combusted and released in the hearth to form high-temperature flue gas, limestone materials are heated and are calcined and decomposed to generate CaO and release CO 2 And (3) gas.
2) And the cooling air pipeline sends the circulating flue gas cooled by the cooling device into the bottom of the hearth, the cooling air cools the generated high-temperature CaO, and the cooled CaO is discharged from the bottom of the hearth to obtain the finished lime.
3) The high-temperature waste gas formed by cooling and the high-temperature flue gas formed by calcining enter another hearth through the connecting channel, the high-temperature flue gas passes through a cold lime stone bed in the hearth, the lime stone bed is preheated and heated, the temperature of the flue gas is reduced to form low-temperature hot air, and the low-temperature hot air enters a flue gas discharge pipeline from a kiln top valve at the top of the hearth.
4) The low-temperature hot air is dedusted by a deduster to obtain CO as the main component 2 Is then based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure state of the product requirement and the buffer tower is further determined to be respectively fed into the CO 2 The flue gas amount of the finished product system, the slow storage tower and the flow divider can realize the preparation of high-purity CO while producing lime 2 And (3) gas.
In the present invention, in step 4), the method is based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure state of the product requirement and the buffer tower is further determined to be respectively fed into the CO 2 The flue gas amount of the finished product system, the buffer tower and the diverter specifically comprises the following substeps:
401 The circulation smoke quantity respectively required by the cooling air pipeline, the fuel air conveying pipeline and the combustion-supporting smoke pipeline in the system is obtained, so that the circulation smoke quantity required by the flow divider is obtained.
402 Through CO 2 Concentration detection device measures CO in flue gas at position of flue gas distributor 2 Concentration and judgment of CO 2 Whether the concentration reaches high purity CO 2 Product requirements.
a) If CO 2 The concentration reaches the standard, and whether the pressure in the buffer tower is further judged by the pressure detection deviceThe lower limit is exceeded.
If the pressure in the buffer tower is detected to exceed the lower limit, the corresponding valve is operated, so that clean flue gas after dust removal is sent into the splitter according to the circulating flue gas amount required by the splitter, and the residual flue gas enters CO 2 A finished product system.
If the pressure in the buffer tower is detected not to exceed the lower limit, clean flue gas after dust removal completely enters CO 2 In the finished product system, the circulating smoke volume required by the diverter is provided by the buffer storage tower.
b) If CO 2 If the concentration does not reach the standard, the pressure detection device is used for further judging whether the pressure in the buffer tower reaches the upper limit.
If the pressure in the slow storage tower is detected to reach the upper limit, the corresponding valve is operated, so that clean flue gas after dust removal is sent into the flow divider according to the circulating flue gas amount required by the flow divider, the residual flue gas enters the slow storage tower, and the slow storage tower simultaneously discharges the corresponding flue gas amount through the discharge pipeline.
If the pressure in the buffer tower is detected to be not up to the upper limit, clean flue gas after dust removal is sent into the flow divider according to the circulating flue gas amount required by the flow divider, and the residual flue gas enters the buffer tower.
In the present invention, the substep 401) specifically includes:
(1) and (3) calculating cooling air quantity according to the quantity of the finished lime obtained in the step (2), and obtaining the circulating smoke quantity required by the cooling air pipeline.
(2) And calculating fuel supply quantity according to the quantity of the finished lime, and calculating fuel delivery air quantity according to the fuel supply quantity, so as to obtain the circulating smoke quantity required by the fuel delivery air pipeline.
(3) According to the fuel supply amount and O 2 With CO 2 CO in combustion-supporting air of mixed gas 2 And O 2 The pure oxygen amount required by the oxygen transmission pipeline and the circulating smoke amount required by the combustion-supporting smoke pipeline are calculated and obtained.
(4) According to the steps (1) - (3), the amount of circulating smoke required by the diverter is obtained.
Preferably, the O in step 1) 2 With CO 2 O in combustion-supporting air of mixed gas 2 Is of volume of (1)The ratio is 27-31%, CO 2 The volume ratio of (3) is 69-73%.
Aiming at the problem that CO is produced in the existing lime production process 2 CO caused by high difficulty in enrichment and trapping 2 The invention provides lime kiln equipment based on carbon emission reduction, which solves the problems of large emission and resource waste. The lime kiln equipment comprises a double-hearth lime kiln, and mainly comprises two hearths which are mirror images of each other, wherein a connecting channel for mutually communicating gas is arranged between the two hearths. One of the hearths is a combustion hearth, comprising a calcination hearth positioned at the upper part and a cooling hearth positioned at the lower part, and the other hearth is a heat storage hearth, namely a preheating hearth of the lime kiln (two hearths have periodic exchange roles, so that continuous calcination of lime is completed). Kiln top valves are arranged at the upper parts of the two hearths. Wherein, the kiln top valve of the combustion chamber is connected with the combustion chamber and the combustion-supporting air pipeline and is used for accommodating the entry of combustion-supporting air; the kiln top valve of the heat accumulation chamber is connected with the hearth and the smoke exhaust pipeline and is used for accommodating smoke exhaust. The flue gas exhaust pipeline is respectively connected with a finished pipeline and a circulating pipeline, and the finished pipeline is connected to CO 2 The finished product system is used as CO 2 The finished product is directly produced, and the circulating pipeline is connected to the hearth to obtain CO required by each working procedure of the hearth 2 The self-circulation supply of the gas is realized, that is, the self-circulation supply of the flue gas required by each procedure in the system is realized through the flue gas circulation, thereby avoiding the introduction of the external air into N 2 CO of the impurity components 2 Is used for dilution of the sample. The circulating pipeline is also provided with a separating storage pipeline which is connected to the slow storage tower, and the slow storage tower can prevent the tail gas CO of the lime kiln 2 When the concentration is low, only the resource waste of the external discharge can be realized, and the CO in the smoke can be improved through the smoke circulation 2 Concentration of CO in flue gas 2 The concentration is gradually enriched, thereby achieving the purpose of ensuring the product quality. Therefore, the invention can greatly improve the tail gas CO in the lime production process 2 Concentration, high purity CO is obtained while lime is produced 2 Gaseous byproducts.
In the invention, a buried fuel spray gun (such as a pulverized coal spray gun) is arranged in the middle part of the hearth (namely the calcination hearth) as a combustion hearth, and the circulating pipeline is divided into a cooling air pipeline, a fuel air conveying pipeline and a combustion-supporting flue gasThree branches of the pipeline. Wherein the cooling air duct is connected to the bottom of the combustion chamber (i.e. the cooling air inlet of the cooling chamber). The fuel delivery air conduit is connected to a fuel lance. The combustion-supporting flue gas pipeline is connected to the inlet of the combustion-supporting air pipeline, and the oxygen conveying pipeline is connected to the combustion-supporting air pipeline at the same time. Thus, in the scheme of the invention, the combustion air required by the calcination chamber is changed from the common air combustion air into O 2 With CO 2 The oxygen-enriched combustion-supporting air formed by mixing is changed into CO from common air as the cooling medium adopted by the cooling chamber 2 The main component of the high-temperature flue gas generated by the calcination chamber and the cooling chamber is CO based on the air flow 2 Gas, avoiding the introduction of O during fuel combustion and air-based cooling in the prior art 2 And N 2 CO of the impurity components 2 Is diluted to realize CO 2 Enrichment of gas greatly improves CO in tail gas of lime production 2 Concentration. Therefore, the invention can recycle the high temperature flue gas (namely high purity CO) generated by the calcination chamber and the cooling chamber 2 Gas) is respectively used for mixing cooling gas, fuel conveying and combustion-supporting air after the limestone material is preheated by the preheating chamber, thereby realizing the CO required by the working procedures of mixing the cooling gas, the fuel conveying carrier gas, the combustion-supporting air and the like in the system 2 Self-circulation supply of gas, while producing lime, obtaining high-purity CO 2 And (3) gas. In addition, a cooling device (such as a water bath or an air cooler) is further arranged on the cooling air pipeline, namely, the flue gas discharged after preheating the materials is cooled and then is conveyed to a cooling process as a cooling medium, so that the cooling effect on the high-temperature CaO generated by calcination is enhanced, and the obtained finished lime is completely cooled.
Preferably, in order to strengthen the mixing effect of the combustion-supporting air, the mixer is additionally arranged on the combustion-supporting air pipeline. Two inlets of the mixer are respectively connected with the combustion-supporting flue gas pipeline and the oxygen conveying pipeline, and an outlet of the mixer is connected with the combustion-supporting flue gas pipeline. CO respectively conveyed by a combustion-supporting flue gas pipeline and an oxygen conveying pipeline 2 The control of the amount of the gas and the oxygen realizes the control of CO in the combustion-supporting air formed after the mixing in the mixer 2 Concentration of gas and oxygenAnd controlling, so that the combustion-supporting air meeting the requirements is conveyed to the calcination chamber through the combustion-supporting air pipeline.
Generally, CO 2 The invention breaks the routine, changes the traditional air combustion-supporting air into O in the calcining chamber 2 With CO 2 Oxygen-enriched combustion-supporting wind formed by mixing the gases. First, the air combustion air is replaced with O 2 With CO 2 Combustion-supporting air of the mixed gas can avoid N in the air 2 CO of the impurity components 2 The product after combustion of the fuel is mainly CO 2 Further improving CO in the flue gas generated in the calcination process 2 Is a concentration of (2); second, O 2 With CO 2 The combustion-supporting air of the mixed gas is compared with the air combustion-supporting air, and the inert components of the mixed gas and the air combustion-supporting air are CO respectively 2 And N 2 And CO 2 And N 2 The two were different in thermal properties (CO 2 Has a specific heat capacity of about 840j/kg-K, N 2 Has a specific heat capacity of about 740 j/kg-K), and N 2 And O 2 Equidiatomic molecules have weak radiation capability and CO 2 The 3-atom molecule has strong radiation capability, namely O is adopted 2 -CO 2 Compared with air, the radiation capability of the smoke generated by the combustion-supporting of the mixed gas is stronger, and the heat transfer with the material is also stronger, so that the O in the scheme of the application 2 With CO 2 The combustion-supporting air of the mixed gas can better meet the heat transfer in lime kiln equipment and improve the production efficiency. In addition, if pure oxygen is used as the combustion air, O is likely to occur 2 Unreacted completion, i.e. the presence of introduced O during combustion of the fuel 2 CO of the impurity components 2 Dilution conditions; meanwhile, pure oxygen is adopted as combustion improver, so that the combustion temperature of fuel can be greatly improved, the flame temperature is up to 1700 ℃ or even higher, and the CaCO is greatly exceeded 3 The upper limit of the calcination temperature (1050 ℃) of the product CaO is easy to form overmelt on the surface of the finished product CaO, so that the quality of the product is reduced; meanwhile, the smoke volume generated by pure oxygen combustion is only 1/5-1/4 of that generated by the traditional air combustion supporting, and the great reduction of the smoke volume is not beneficial to heat exchange between the smoke and limestone materials, so that the calcination rate and the calcination effect are affected; likewise, CO 2 And O 2 Different in thermal physical properties, CO 2 Specific heat of (2)With a capacity significantly greater than O 2 Specific heat capacity of (2), i.e. introducing CO into combustion air 2 The components can ensure the heat transfer of the system, promote the calcination effect and greatly improve the CO in the tail gas in the lime production process 2 Concentration, realizes the production of lime and simultaneously, CO 2 The recycling of the gas effectively overcomes the problem of CO in the existing lime production process 2 Large discharge and resource waste.
In the present application, in view of the control of the combustion temperature, in the porous medium space combustion of a lime kiln, in order to maintain the combustion temperature similar to that of air combustion supporting, a proper combustion atmosphere is maintained, the calcination effect and the product quality are ensured, and the gas combustion furnace is characterized in that 2 With CO 2 In the combustion-supporting air formed by mixing the gases, O 2 The concentration (volume ratio) of (C) is generally maintained at 27-31%, CO 2 The volume ratio of (3) is 69-73%. Wherein the specific concentration value is related to the fuel type and heating value. For example, when using a typical fuel blast furnace gas on a lime kiln, O 2 The concentration of (2) is about 27 to 28%.
In the invention, the lime kiln flue gas circulation system can be subjected to a process of converting unsteady state into steady state during the starting process. At the beginning, CO in the flue gas 2 The concentration is lower, and CO is carried out along with the smoke circulation 2 The concentration gradually increased to a stable value. Flue gas CO generated in this unsteady state process 2 Lower concentration if directly fed into CO 2 The quality of the finished product can be affected if the finished product is directly discharged, and the resource waste can be caused. Thus, the invention provides a CO with a buffer tower 2 Recovery system, the flue gas in the unsteady state process enters the buffer tower, and the high-concentration flue gas in the steady state process enters CO 2 The finished product system is arranged in such a way that not only is the resource waste prevented, but also the product quality is ensured.
In addition, in the lime production process, abnormal working conditions and the like can also occur. Generally, under normal working conditions, the CO after the smoke circulation of the application 2 The concentration meets the product requirement (CO can be used for 2 Concentration detection device for detection), at this time, a part of flue gas is sent into the lime kiln to ensure normal raw materialsThe product (lime cooling, fuel carrier, combustion air mixing medium, etc.), and the rest part of the product completely enters CO 2 A finished product system. Under abnormal working conditions, the CO after the smoke is circulated 2 At this time, part of the flue gas enters the lime kiln to ensure normal production (lime cooling, fuel carrier, combustion-supporting air mixing medium and the like), and the rest of the flue gas is sent to a slow storage tower for storage. CO after the flue gas is circulated 2 After the concentration meets the product requirement, at the moment, all or part of high-concentration CO 2 The flue gas directly enters CO 2 And the finished product system ensures that the smoke entering the hearth in normal production circulation is provided by the buffer tower in whole or in part. So arranged, the low CO in the buffer tower can be recycled through the flue gas of the hearth 2 Purifying the flue gas with high concentration into high CO 2 Flue gas with concentration for realizing CO 2 Is completely recovered.
The invention is also connected with a diffusing pipeline and a reflux pipeline on the slow storage tower. Wherein, the diffusing pipeline is directly connected with the atmosphere and is used for storing CO in the tower 2 When the storage capacity reaches the limit value (the storage capacity can be judged by a pressure detection device on the slow storage tower), the external diffusion and pressure relief are realized. The reflux pipeline returns to the circulating pipeline for re-delivering the gas in the buffer tower to the lime kiln system for circulation, and further purifying CO 2 . For ease of control, the present application provides a bleed valve on the bleed line, a return valve on the return line, and an inlet valve on the storage line. The utility model provides a still on circulating line, be located between storage pipeline and the return line and set up the short circuit valve for do not pass through the direct circulation of slow storage tower with the flue gas and get into lime kiln system.
The invention is provided with the smoke distributor at the connection position of the smoke discharge pipeline of the lime kiln, the finished product pipeline and the circulating pipeline, and the adjustment of the smoke distributor realizes that the smoke discharged after the lime kiln preheating process is in CO 2 Flow distribution between the finished product system and the flue gas self-circulation. Correspondingly, the invention is provided with the flow divider at the positions of the three pipelines of the cooling air pipeline, the fuel air conveying pipeline and the combustion-supporting flue gas pipeline on the circulating pipeline, and realizes that the circulating flue gas is respectively used as cooling air and fuel for conveying through the adjustment of the flow dividerCarrier gas, and on-demand distribution for combustion air mixing.
Lime production using the lime kiln equipment, during the production process, limestone material (CaCO as main component) 3 ) Is fed from the top of the hearth, and the industrial pure oxygen and the circulating flue gas (the main component is CO 2 And unreacted O 2 ) Mixing in combustion-supporting air mixer to form O with a certain concentration 2 -CO 2 The mixed gas is fed from a kiln top valve position, and fuel (such as coal dust) is fed into the hearth from a fuel spray gun (such as coal dust spray gun) arranged in the middle of the hearth by taking circulating smoke as carrier gas. The fuel and the combustion air are burnt in the hearth to release heat and form high-temperature flue gas, the materials are rapidly heated to the reaction temperature (about 1050 ℃) by utilizing a convection and radiation heat exchange mode, and the calcination and decomposition are completed, so that quicklime (CaO) is generated and CO is released 2 . And (3) taking the circulating flue gas as cooling air of a cooling medium to be fed from the bottom of the hearth, cooling the high-temperature quicklime to below 100 ℃, and discharging the high-temperature quicklime from the bottom of the hearth to form finished lime. The high-temperature exhaust gas formed after cooling is sent into the heat accumulation chamber through the connecting channel together with the high-temperature flue gas formed by calcining. After passing through the cold lime material bed in the heat accumulating chamber, the high temperature fume is cooled to 130-150 deg.c and enters the fume exhaust pipeline from the kiln top valve in the top of the heat accumulating chamber. At this time, the flue gas contains a large amount of dust, and the main component of the flue gas is CO after passing through a dust remover (a bag-type dust remover after an electric dust remover and the like) 2 Is a clean flue gas. The flue gas after dust removal is according to CO 2 Whether the content reaches high purity CO 2 The product requirement and the pressure state in the buffer tower are determined to be respectively fed into the CO 2 The ratio of flue gas from the final product system to the buffer tower. And part of the flue gas which does not reach the concentration requirement enters a buffer storage tower for buffering for standby, and the other part of the flue gas is directly sent into a flow divider. The diverter sends the flue gas into the cooling air pipeline, the fuel air conveying pipeline and the combustion-supporting flue gas pipeline respectively. A water bath (or air cooler) is provided on the cooling air duct to cool the flue gas to about 20 ℃. By the system, the lime kiln is formed to contain a large amount of CO 2 The gas flue gas is further enriched and purified in a flue gas circulation mode, and the flue gas and pure oxygen are used as combustion-supporting agents, and the flue gas is used as fuel carrier gas, so that N is completely eradicated 2 Inlet stoneAsh kiln system for producing high purity CO while quicklime is being produced 2 And (3) gas.
The invention also provides a method for purifying CO by adopting a lime kiln tail gas circulation method based on the lime kiln equipment 2 Is provided. The specific control flow is as follows:
401 The circulation smoke quantity respectively required by the cooling air pipeline, the fuel air conveying pipeline and the combustion-supporting smoke pipeline in the system is obtained, so that the circulation smoke quantity required by the flow divider is obtained. The method specifically comprises the following steps:
(1) And calculating cooling air quantity according to the obtained finished lime product, and obtaining the circulating smoke quantity required by the cooling air pipeline. The specific calculation process is as follows:
neglecting the heat dissipation loss in the cooling process, the high-temperature CaO transfers heat to the cooling air, so that the cooling air is provided with:
Q l ·C p,x ·Δt l ＝m cao ·C p,cao ·Δt cao 。
the required cooling air volume can be obtained by the method:
wherein: q (Q) l The amount of circulating smoke required for cooling the air duct. m is m cao Is the amount of finished lime. C (C) p,cao Is the specific heat capacity of calcium oxide. Δt (delta t) cao For cooling the lime product, 900-1000 deg.c is used. C (C) p,x Is the specific heat capacity of the circulating flue gas. Δt (delta t) l For cooling the temperature rise of the circulating flue gas before and after cooling, the temperature is generally 500-900 ℃.
(2) And calculating fuel supply quantity according to the quantity of the finished lime, and calculating fuel delivery air quantity according to the fuel supply quantity, so as to obtain the circulating smoke quantity required by the fuel delivery air pipeline. The specific calculation process is as follows:
pulverized coal supply amount:
m c ＝k c ·m cao 。
wherein: m is m c The coal dust supply amount. k (k) c Coal required for production of unit CaO productsThe specific value of the powder quantity is related to the thermal efficiency of the hearth and the calorific value of the pulverized coal, and the typical value is 0.125-0.150 kg/kg-CaO.
Fuel delivery air volume:
Q s ＝k s ·m c 。
wherein: q (Q) s The circulating smoke amount needed by the fuel air conveying pipeline is provided. k (k) s The specific value of the air quantity required for conveying the pulverized coal per unit mass is related to the physical properties such as the granularity and the viscosity of the pulverized coal, and is generally 2-5 Nm 3 Kg-pulverized coal.
The two methods are combined:
Q s ＝k s ·k c ·m cao 。
(3) according to the fuel supply amount and O 2 -CO 2 CO in combustion-supporting air of mixed gas 2 And O 2 Concentration of (e.g. O in combustion air 2 The volume ratio is 27%, CO 2 The volume ratio is 73 percent), and the pure oxygen amount required by the oxygen transmission pipeline and the circulating smoke amount required by the combustion-supporting smoke pipeline are calculated. The specific calculation process is as follows:
in the calculation process, it is considered that O is supplied 2 The amount is just equivalent to the theoretical oxygen demand consumed by the combustion of the pulverized coal, and the main component in the circulating flue gas is CO 2 In which small amounts of unreacted O may be present 2 Negligible (concentration typically not exceeding 2-3%). Then there are:
Q o ＝k o ·m c 。
wherein: q (Q) o The amount of pure oxygen required for the oxygen delivery conduit. k (k) o The theoretical oxygen demand required for burning the pulverized coal per unit mass is generally 1.75 to 2Nm depending on the kind of pulverized coal and the like 3 Kg-pulverized coal. Q (Q) z The circulating smoke quantity X required by the combustion-supporting smoke pipeline co2 And X O2 CO in combustion-supporting air 2 And O 2 Generally 73% and 27%.
(4) According to the steps (1) - (3), the amount of circulating smoke required by the diverter is obtained. The specific calculation process is as follows:
Q tot ＝Q l +Q s +Q z 。
wherein: q (Q) tot The amount of circulating smoke required for the diverter.
402 Through CO 2 Concentration detection device measures CO in flue gas at position of flue gas distributor 2 Concentration and judgment of CO 2 Whether the concentration reaches high purity CO 2 Product requirements. Generally, high purity CO 2 CO of the product 2 Concentration requirements of more than 90%, CO for special purposes 2 Concentration requirement is more than 95%, the high purity CO 2 CO of the product 2 The concentration requirements may be set according to specific needs.
a) If CO 2 And if the concentration reaches the standard, further judging whether the pressure in the buffer tower exceeds the lower limit or not through a pressure detection device.
If the pressure in the buffer tower is detected to exceed the lower limit, corresponding valves (a short-circuit valve is opened, an inlet valve, a bleeding valve and a reflux valve are closed) are operated, so that clean flue gas after dust removal is sent into the flow divider according to the circulating flue gas amount required by the flow divider, and the residual flue gas enters CO 2 A finished product system.
If the pressure in the buffer tower is detected not to exceed the lower limit, clean flue gas after dedusting completely enters CO after the reflux valve is opened, the inlet valve, the short-circuit valve and the bleeding valve are closed 2 In the finished product system, the circulating smoke volume required by the diverter is provided by the buffer storage tower. If the amount of the smoke stored in the buffer tower is insufficient to provide the circulating smoke amount required by the flow divider, the insufficient part is replenished by the clean smoke after dust removal, and the step of exceeding the lower limit of the pressure in the buffer Chu Da is returned.
b) If CO 2 If the concentration does not reach the standard, the pressure detection device is used for further judging whether the pressure in the buffer tower reaches the upper limit.
If the pressure in the slow storage tower is detected to reach the upper limit, corresponding valves (an inlet valve, a short-circuit valve and a bleeding valve are opened, and a reflux valve is closed) are operated, so that clean flue gas after dust removal is sent into the flow divider according to the circulating flue gas amount required by the flow divider, and the residual flue gas enters the slow storage tower and is discharged out of the slow storage tower through the bleeding pipeline.
If the pressure in the slow storage tower is detected to be not up to the upper limit, clean flue gas after dust removal (opening an inlet valve, a short-circuiting valve, closing a diffusing valve and a reflux valve) is sent into the flow divider according to the circulating flue gas amount required by the flow divider, and the residual flue gas enters the slow storage tower. If the remaining flue gas amount exceeds the amount of the flue gas stored in the buffer tower, the excess flue gas is discharged through the discharge pipe, and the pressure in the buffer Chu Da reaches the upper limit.
Through the control flow, the unreachable CO can be obtained 2 The flue gas with the concentration requirement is directionally circulated, so that CO in the flue gas 2 Gradually enriching the concentration until the concentration reaches the product requirement.
In the present application, the height of the double chamber lime kiln is 3-100 meters, preferably 4-80 meters, more preferably 5-70 meters, preferably 6-65 meters, still more preferably 8-60 meters.
In the present application, the outer diameter of one hearth of the double-hearth lime kiln is 0.5 to 10 m, preferably 1 to 8 m, more preferably 1.5 to 7 m, preferably 2 to 6 m, and even more preferably 2.5 to 5 m.
Compared with the prior art, the invention has the following beneficial technical effects:
1. the invention is provided with the CO with the slow storage tower 2 Recovery system, the extension of slow storage tower can prevent lime kiln tail gas CO 2 When the concentration is low, only the resource waste of the external discharge can be realized, and the CO in the smoke can be improved through the smoke circulation 2 Concentration of CO 2 Gradually enriching, while producing lime, high-purity CO 2 And (3) gas.
2. The invention changes the common air combustion-supporting air in the calcining process into O 2 With CO 2 Oxygen-enriched combustion-supporting air formed by mixing gases, and changing the cooling medium of the cooling procedure from common air to CO 2 Air flow, thereby avoiding N in the prior art 2 CO of the impurity components 2 Is diluted and greatly extractedTail gas CO from high lime production process 2 Concentration, i.e. CO is achieved while lime is being produced 2 Is used for recycling.
3. The invention uses two high temperature CO generated in the calcining process and the cooling process 2 The gas is mixed and preheated, and then is split for downstream cooling gas, coal powder conveying, combustion-supporting air mixing and high-purity CO 2 Yield of finished product by CO 2 The enrichment and circulation of the gas can realize the CO required by the working procedures of cooling gas, fuel conveying carrier gas, combustion-supporting air mixing and the like in the system 2 Self-circulation supply of gas while obtaining high purity CO 2 Gas, thereby effectively overcoming the CO in the prior lime production process 2 Large discharge and resource waste.
4. The invention provides a method for purifying CO by adopting a lime kiln tail gas circulation method on the basis of adding a slow storage tower 2 Through flexible smoke circulation control, CO in the smoke is realized 2 The circulating enrichment of the method not only prevents the resource waste, but also achieves the purpose of ensuring the product quality.
Drawings
FIG. 1 is a schematic diagram of a lime kiln equipment based on carbon emission reduction;
FIG. 2 is a flow chart of a method of controlling a lime kiln plant based on carbon emission reduction in accordance with the present invention;
fig. 3 is a schematic structural view of a prior art double chamber lime kiln.
Reference numerals:
1: a double-hearth lime kiln; 101: a furnace; 102: a connection channel; 103: a kiln top valve; 104: a fuel lance; 2: CO 2 A finished product system; 3: slow Chu Da; 4: a mixer; 5: a flue gas distributor; 6: a shunt; 7: a cooling device; 8: a dust remover;
k1: an inlet valve; k2: a shorting valve; k3: a bleed valve; and K4: a return valve;
L1: a combustion air duct; l2: a flue gas discharge duct; l3: a finished product pipeline; l4: a circulation pipe; l401: a cooling air duct; l402: a fuel air supply pipeline; l403: a combustion-supporting flue gas pipeline; l5: a storage pipeline; l6: an oxygen delivery conduit; l7: a bleeding pipe; l8: and a return line.
Detailed Description
The following examples illustrate the technical aspects of the invention, and the scope of the invention claimed includes but is not limited to the following examples.
According to a first embodiment of the invention, a lime kiln plant based on carbon reduction is provided.
A lime kiln installation based on carbon emission reduction, comprising a double chamber lime kiln 1. The double-hearth lime kiln 1 comprises two hearths 101 which are arranged in a mirror image mode, and a connecting channel 102 is arranged between the two hearths 101. The upper parts of both hearths 101 are provided with kiln top valves 103. The kiln top valve 103 is respectively connected with the hearth 101, the combustion air pipeline L1 or the flue gas discharge pipeline L2. The flue gas discharge pipeline L2 is respectively connected with a finished pipeline L3 and a circulating pipeline L4, wherein the finished pipeline L3 is connected to CO 2 The finishing system 2, the circulation line L4 is connected to the furnace 101. A storage line L5 branched from the circulation line L4 is connected to the buffer tower 3.
In the present invention, the middle of the furnace 101 is provided with a buried fuel lance 104. The circulating pipeline L4 is divided into three pipelines, namely a cooling air pipeline L401, a fuel conveying air pipeline L402 and a combustion-supporting flue gas pipeline L403. Wherein the cooling air duct L401 is connected to a cooling air inlet at the bottom of the furnace 101, the fuel delivery air duct L402 is connected to an inlet of the fuel lance 104, and the combustion-supporting flue gas duct L403 is connected to an inlet of the combustion-supporting air duct L1. The combustion-supporting air pipeline L1 is also connected with an oxygen conveying pipeline L6.
Preferably, the combustion air duct L1 is provided with a mixer 4. The mixer 4 comprises two inlets and an outlet, wherein the outlet of the mixer 4 is connected with the kiln top valve 103 through a combustion air pipeline L1, and the two inlets of the mixer 4 are respectively connected with a combustion flue gas pipeline L403 and an oxygen conveying pipeline L6.
In the invention, the diffusing pipeline L7 and the reflux pipeline L8 are connected to the buffer tower 3. The return line L8 is connected to the circulation line L4, and the connection position is located downstream of the position on the circulation line L4 where the storage line L5 is branched.
Preferably, the storage line L5 is provided with an inlet valve K1. A shorting valve K2 is provided in the circulation line L4 between the storage line L5 and the return line L8.
Preferably, the bleeding pipe L7 is provided with a bleeding valve K3. The return pipe L8 is provided with a return valve K4.
Preferably, the lime kiln equipment further comprises a flue gas distributor 5 arranged at the connection position of the flue gas discharge pipeline L2 with the finished product pipeline L3 and the circulating pipeline L4.
Preferably, a flow divider 6 is provided at a position where three pipes are branched from the circulation pipe L4.
In the present invention, the cooling air duct L401 is provided with a cooling device 7. Preferably, the cooling device 7 is a water bath or an air cooler.
In the present invention, the flue gas discharge duct L2 is provided with a dust collector 8. Preferably, the dust remover 8 is an electric dust remover or a cloth bag dust remover.
Preferably, a CO is provided on the flue gas discharge line L2 downstream of the dust separator 8 2 Concentration detection means.
Preferably, the buffer tower 3 is provided with a pressure detecting device.
Example 1
As shown in fig. 1, a lime kiln installation based on carbon reduction comprises a double chamber lime kiln 1. The double-hearth lime kiln 1 comprises two hearths 101 which are arranged in a mirror image mode, and a connecting channel 102 is arranged between the two hearths 101. One hearth is a combustion hearth and comprises a calcination hearth and a cooling hearth, and the other hearth is a heat accumulation hearth, namely a preheating hearth. The two hearths 101 periodically exchange roles to complete the continuous calcination of lime.
The upper parts of both hearths 101 are provided with kiln top valves 103. Wherein, the kiln top valve arranged on the combustion chamber is connected with the combustion chamber and the combustion-supporting air pipeline L1. And a kiln top valve arranged on the heat accumulation chamber is connected with the furnace chamber and the smoke exhaust pipeline L2. The flue gas discharge pipeline L2 is respectively connected with a finished pipeline L3 and a circulating pipeline L4, wherein the finished pipeline L3 is connected to CO 2 The finishing system 2, the circulation line L4 is connected to the furnace 101. A storage line L5 branched from the circulation line L4 is connected to the buffer tower 3.
Example 2
Example 1 was repeated except that the middle portion of the furnace 101 (i.e., the calcination chamber) as the combustion chamber was provided with the buried fuel lance 104. The circulating pipeline L4 is divided into three pipelines, namely a cooling air pipeline L401, a fuel conveying air pipeline L402 and a combustion-supporting flue gas pipeline L403. Wherein the cooling air duct L401 is connected to a cooling air inlet at the bottom of the furnace 101, the fuel delivery air duct L402 is connected to an inlet of the fuel lance 104, and the combustion-supporting flue gas duct L403 is connected to an inlet of the combustion-supporting air duct L1. The combustion-supporting air pipeline L1 is also connected with an oxygen conveying pipeline L6.
Example 3
Example 2 was repeated except that the combustion air duct L1 was provided with a mixer 4. The mixer 4 comprises two inlets and an outlet, wherein the outlet of the mixer 4 is connected with the kiln top valve 103 through a combustion air pipeline L1, and the two inlets of the mixer 4 are respectively connected with a combustion flue gas pipeline L403 and an oxygen conveying pipeline L6.
Example 4
Example 3 was repeated except that a bleed line L7 and a return line L8 were connected to the buffer tower 3. The return line L8 is connected to the circulation line L4, and the connection position is located downstream of the position on the circulation line L4 where the storage line L5 is branched.
Example 5
Example 4 was repeated except that the storage line L5 was provided with an inlet valve K1. A shorting valve K2 is provided in the circulation line L4 between the storage line L5 and the return line L8.
Example 6
Example 5 was repeated except that the bleeding valve K3 was provided on the bleeding pipe L7. The return pipe L8 is provided with a return valve K4.
Example 7
Example 6 was repeated except that the lime kiln equipment further included a flue gas distributor 5 provided at the connection position of the flue gas discharge duct L2 with the product duct L3 and the circulation duct L4.
Example 8
Example 7 was repeated except that a flow divider 6 was provided at a position where three pipes were branched off from the circulation pipe L4.
Example 9
Example 8 was repeated except that the cooling air duct L401 was provided with the cooling device 7. The cooling device 7 is a water bath.
Example 10
Example 8 was repeated except that the cooling air duct L401 was provided with the cooling device 7. The cooling device 7 is an air cooler.
Example 11
Example 9 was repeated except that the dust remover 8 was provided on the fume exhaust line L2. The dust remover 8 is an electric dust remover.
Example 12
Example 10 was repeated except that the dust collector 8 was provided on the fume exhaust line L2. The dust remover 8 is a cloth bag dust remover.
Example 13
Example 12 was repeated except that CO was provided on the flue gas discharge line L2 downstream of the dust separator 8 2 Concentration detection means.
Example 14
Example 13 was repeated except that a pressure detecting device was installed on the buffer tower 3.
Example 15
A control method of a lime kiln plant based on carbon emission reduction, using the lime kiln plant described in embodiment 14, comprising the steps of:
1) Limestone material enters from the top of the hearth 101, and pure oxygen and circulating flue gas conveyed by the oxygen conveying pipeline L6 and the combustion-supporting flue gas pipeline L403 are mixed in the mixer 4 to form O 2 With CO 2 Combustion air of mixed gas is fed into the hearth 101 from a kiln top valve 103 through a combustion air pipeline L1, coal dust is fed into the hearth 101 from a fuel spray gun 104 by taking circulating flue gas conveyed by a fuel conveying air pipeline L402 as a carrier, the coal dust and the combustion air are combusted and released heat in the hearth 101 to form high-temperature flue gas, limestone materials are heated to raise temperature and complete calcination and decomposition, caO is generated and CO is released 2 And (3) gas.
2) The cooling air duct L401 feeds the circulating flue gas cooled by the cooling device 7 from the bottom of the furnace 101, the cooling air cools the high-temperature CaO generated, and the cooled CaO is discharged from the bottom of the furnace 101 to obtain the lime product.
3) The high-temperature exhaust gas formed by cooling and the high-temperature flue gas formed by calcining enter the other hearth 101 through the connecting channel 102, the high-temperature flue gas passes through a lime stone bed cooled in the hearth 101, the lime stone bed is preheated and heated, the temperature of the flue gas is reduced to form low-temperature hot air, and the low-temperature hot air enters the flue gas discharge pipeline L2 from the kiln top valve 103 at the top of the hearth 101.
4) The low-temperature hot air is dedusted by a deduster 8 to obtain a main component of CO 2 Is then based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure conditions of the product demand and buffer tower 3 are determined to be fed into the CO respectively 2 The flue gas amount of the finished product system 2, the buffer tower 3 and the diverter 6 can realize the preparation of high-purity CO while producing lime 2 And (3) gas.
Example 16
As shown in FIG. 2, example 15 is repeated except that in step 4) the method is performed based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure conditions of the product demand and buffer tower 3 are determined to be fed into the CO respectively 2 The flue gas amount of the finished product system 2, the buffer tower 3 and the diverter 6 specifically comprises the following substeps:
401 The circulation smoke amount required by the cooling air pipeline L401, the fuel conveying air pipeline L402 and the combustion-supporting smoke pipeline L403 in the system is obtained, so that the circulation smoke amount required by the flow divider 6 is obtained.
402 Through CO 2 The concentration detection means measure the CO in the flue gas at the location of the flue gas distributor 5 2 Concentration and judgment of CO 2 Whether the concentration reaches high purity CO 2 Product requirements.
a) If CO 2 And if the concentration reaches the standard, further judging whether the pressure in the buffer tower 3 exceeds the lower limit or not through a pressure detection device.
If the pressure in the buffer tower 3 is detected to exceed the lower limit, the corresponding valve is operated, so that clean flue gas after dust removal is sent into the splitter 6 according to the circulating flue gas amount required by the splitter 6, and the residual flue gas enters CO 2 The finished system 2.
If the pressure in the buffer tower 3 is detected not to exceed the lower limit, clean flue gas after dust removal completely enters CO 2 The amount of circulating flue gas required by the finished product system 2 and the splitter 6 is provided by the buffer tower 3.
b) If CO 2 If the concentration does not reach the standard, the pressure detection device is used for further judging whether the pressure in the buffer tower 3 reaches the upper limit.
If the pressure in the slow storage tower 3 is detected to reach the upper limit, the corresponding valve is operated, so that clean flue gas after dust removal is sent into the flow divider 6 according to the circulating flue gas amount required by the flow divider 6, the residual flue gas enters the slow storage tower 3, and the slow storage tower 3 discharges the corresponding flue gas amount through the discharge pipeline L7.
If the pressure in the slow storage tower 3 is detected to be not up to the upper limit, clean flue gas after dust removal is sent into the flow divider 6 according to the circulating flue gas amount required by the flow divider 6, and the residual flue gas enters the slow storage tower 3.
Example 17
Example 16 is repeated except that the substep 401) specifically includes:
(1) and (3) calculating cooling air quantity according to the quantity of the finished lime obtained in the step (2), and obtaining the circulating smoke quantity required by the cooling air pipeline L401.
(2) And calculating the coal dust supply quantity according to the quantity of the finished lime, and calculating the fuel conveying air quantity according to the coal dust supply quantity, so as to obtain the circulating smoke quantity required by the fuel conveying air pipeline L402.
(3) According to the coal powder supply quantity and O 2 With CO 2 CO in combustion-supporting air of mixed gas 2 And O 2 The pure oxygen amount required for obtaining the oxygen transmission pipeline L6 and the circulating smoke amount required for the combustion-supporting smoke pipeline L403 are calculated. Wherein O is 2 With CO 2 O in combustion-supporting air of mixed gas 2 Is 27% by volume, CO 2 Is 73% by volume.
(4) According to steps (1) - (3), the amount of circulating smoke required for the flow divider 6 is obtained.
Application example 1
The control method of example 17 was used for lime production, comprising the steps of:
1) Limestone material enters from the top of the hearth 101, and pure oxygen and circulating flue gas conveyed by the oxygen conveying pipeline L6 and the combustion-supporting flue gas pipeline L403 are mixed in the mixer 4 to form O 2 With CO 2 Combustion air of mixed gas is fed into the hearth 101 from a kiln top valve 103 through a combustion air pipeline L1, coal dust is fed into the hearth 101 from a fuel spray gun 104 by taking circulating flue gas conveyed by a fuel conveying air pipeline L402 as a carrier, the coal dust and the combustion air are combusted and released heat in the hearth 101 to form high-temperature flue gas, limestone materials are heated to raise temperature and complete calcination and decomposition, caO is generated and CO is released 2 And (3) gas.
2) The cooling air duct L401 feeds the circulating flue gas cooled by the cooling device 7 from the bottom of the furnace 101, the cooling air cools the high-temperature CaO generated, and the cooled CaO is discharged from the bottom of the furnace 101 to obtain the lime product.
3) The high-temperature exhaust gas formed by cooling and the high-temperature flue gas formed by calcining enter the other hearth 101 through the connecting channel 102, the high-temperature flue gas passes through a lime stone bed cooled in the hearth 101, the lime stone bed is preheated and heated, the temperature of the flue gas is reduced to form low-temperature hot air, and the low-temperature hot air enters the flue gas discharge pipeline L2 from the kiln top valve 103 at the top of the hearth 101.
4) The low-temperature hot air is dedusted by a deduster 8 to obtain a main component of CO 2 Is then based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure conditions of the product demand and buffer tower 3 are determined to be fed into the CO respectively 2 The flue gas amount of the finished product system 2, the buffer tower 3 and the diverter 6 can realize the preparation of high-purity CO while producing lime 2 And (3) gas.
In step 4), the method is based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure conditions of the product demand and buffer tower 3 are determined to be fed into the CO respectively 2 The flue gas amount of the finished product system 2, the buffer tower 3 and the diverter 6 specifically comprises the following substeps:
401 The circulation smoke amount required by the cooling air pipeline L401, the fuel conveying air pipeline L402 and the combustion-supporting smoke pipeline L403 in the system is obtained, so that the circulation smoke amount required by the flow divider 6 is obtained.
The substep 401) specifically includes:
(1) and (3) calculating cooling air quantity according to the quantity of the finished lime obtained in the step (2), and obtaining the circulating smoke quantity required by the cooling air pipeline L401. The specific calculation process is as follows:
neglecting the heat dissipation loss in the cooling process, the high-temperature CaO transfers heat to the cooling air, so that the cooling air is provided with:
Q l ·C p,x ·Δt l ＝m cao ·C p,cao ·Δt cao 。
the required cooling air volume can be obtained by the method:
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wherein: q (Q) l The amount of circulating smoke required for cooling the air duct. m is m cao M is the amount of finished lime cao ＝25000kg/h。C p,cao Specific heat capacity of calcium oxide, C p,cao ＝0.7kJ/(kg·℃)。Δt cao For cooling the temperature drop of the finished lime before and after the lime is cooled, delta t cao ＝950℃。C p,x To circulate the specific heat capacity of the flue gas, C p,x ＝1.4kJ/(m 3 ·℃)。Δt l For cooling the temperature rise of the circulating flue gas before and after deltat l ＝800℃。
(2) And calculating the coal dust supply quantity according to the quantity of the finished lime, and calculating the fuel conveying air quantity according to the coal dust supply quantity, so as to obtain the circulating smoke quantity required by the fuel conveying air pipeline L402. The specific calculation process is as follows:
pulverized coal supply amount:
m c ＝k c ·m cao ＝3250kg/h。
wherein: m is m c The coal dust supply amount. k (k) c The amount of coal fines k required for the production of a unit CaO product c ＝0.130kg/kg-CaO。
Fuel delivery air volume:
Q s ＝k s ·m c 。
Wherein: q (Q) s Is burnt byAnd the circulating smoke amount required by the material conveying and air supplying pipeline. k (k) s The conveying air quantity k required for conveying unit mass of coal dust s ＝2Nm 3 Kg-pulverized coal.
The two methods are combined:
Q s ＝k s ·k c ·m cao ＝6500m 3 /h。
(3) according to the coal powder supply quantity and O 2 With CO 2 CO in combustion-supporting air of mixed gas 2 And O 2 The pure oxygen amount required for obtaining the oxygen transmission pipeline L6 and the circulating smoke amount required for the combustion-supporting smoke pipeline L403 are calculated. Wherein O is 2 With CO 2 O in combustion-supporting air of mixed gas 2 Is 27% by volume, CO 2 Is 73% by volume. The specific calculation process is as follows:
in the calculation process, it is considered that O is supplied 2 The amount is just equivalent to the theoretical oxygen demand consumed by the combustion of the pulverized coal, and the main component in the circulating flue gas is CO 2 In which small amounts of unreacted O may be present 2 And neglected. Then there are:
Q o ＝k o ·m c ＝5688m 3 /h。
wherein: q (Q) o The amount of pure oxygen required for the oxygen delivery conduit. k (k) o Theoretical oxygen demand, k, required for burning unit mass of pulverized coal o ＝1.75Nm 3 Kg-pulverized coal. Q (Q) z The circulating smoke quantity X required by the combustion-supporting smoke pipeline co2 And X O2 CO in combustion-supporting air 2 And O 2 Concentration of X co2 ＝73％，X O2 ＝27％。
(4) According to steps (1) - (3), the amount of circulating smoke required for the flow divider 6 is obtained. The specific calculation process is as follows:
Q tot ＝Q l +Q s +Q z ＝36721m 3 /h。
wherein: q (Q) tot Is divided intoThe amount of circulating smoke required by the flow device.
402 Through CO 2 The concentration detection means measure the CO in the flue gas at the location of the flue gas distributor 5 2 Concentration and judgment of CO 2 Whether the concentration reaches high purity CO 2 Product requirements. In this example, high purity CO 2 Product requirement CO 2 The concentration is more than 95 percent.
Due to CO 2 The concentration detection device detects CO 2 At a concentration of 82%, obviously, CO 2 The concentration does not reach the standard, and at this time, whether the pressure in the buffer tower 3 reaches the upper limit is further judged by the pressure detection device.
Because the pressure detection device detects that the pressure in the buffer tower 3 does not reach the upper limit, clean flue gas after dedusting is sent into the splitter 6 according to the circulating flue gas amount required by the splitter 6 calculated in the step 401), and the residual flue gas enters the buffer tower 3.
Application example 2
Application example 1 was repeated except for CO 2 The concentration detection device detects CO in the flue gas at the position of the flue gas distributor 5 2 At a concentration of 91%, i.e. CO 2 The concentration does not reach the standard, and at this time, whether the pressure in the buffer tower 3 reaches the upper limit is further judged by the pressure detection device.
Since the pressure detection device detects that the pressure in the buffer tower 3 reaches the upper limit, that is, the pressure reaches the pressure when the bottle is full, the corresponding valve is operated, so that clean flue gas after dust removal is sent into the flow divider 6 according to the circulating flue gas amount required by the flow divider 6 calculated in the step 401), the residual flue gas enters the buffer tower 3, and the buffer tower 3 discharges the corresponding flue gas amount through the discharge pipeline L7.
Application example 3
Application example 1 was repeated except for CO 2 The concentration detection device detects CO in the flue gas at the position of the flue gas distributor 5 2 The concentration is more than 98%, namely CO 2 The concentration reaches the standard, and at this time, whether the pressure in the buffer tower 3 exceeds the lower limit is further judged by the pressure detection device.
Because the pressure detection device detects that the pressure in the buffer tower 3 does not exceed the lower limit, clean flue gas after dust removal at the momentAll enter CO 2 The amount of circulating smoke required by the diverter 6 calculated in step 401) of the finishing system 2 is provided by the buffer tower 3.
Application example 4
Application example 1 was repeated except for CO 2 The concentration detection device detects CO in the flue gas at the position of the flue gas distributor 5 2 Concentration > 99%, i.e. CO 2 The concentration reaches the standard, and at this time, whether the pressure in the buffer tower 3 exceeds the lower limit is further judged by the pressure detection device.
Since the pressure detection device detects that the pressure in the buffer tower 3 exceeds the lower limit, namely the pressure reaches the pressure when the bottle is empty, the corresponding valve is operated at the moment, so that clean flue gas after dust removal is sent into the splitter 6 according to the circulating flue gas amount required by the splitter 6 calculated in the step 401), and the residual flue gas enters CO 2 The finished system 2.
Claims (10)
1. Lime kiln equipment based on carbon emission reduction, its characterized in that: the lime kiln equipment comprises a double-chamber lime kiln (1); the double-hearth lime kiln (1) comprises two hearths (101) which are arranged in a mirror image mode, and a connecting channel (102) is arranged between the two hearths (101); the upper parts of the two hearths (101) are provided with kiln top valves (103); the kiln top valve (103) is respectively connected with the hearth (101), the combustion air pipeline (L1) or the flue gas discharge pipeline (L2); the flue gas discharge pipeline (L2) is respectively connected with the finished product pipeline (L3) and the circulating pipeline (L4), wherein the finished product pipeline (L3) is connected to CO 2 A finishing system (2), a circulation pipe (L4) being connected to the furnace (101); a storage pipeline (L5) is separated from the circulating pipeline (L4) and connected to the buffer tower (3).
2. Lime kiln equipment according to claim 1, characterized in that: the middle part of the hearth (101) is provided with a buried fuel spray gun (104); the circulating pipeline (L4) is divided into three pipelines, namely a cooling air pipeline (L401), a fuel air conveying pipeline (L402) and a combustion-supporting flue gas pipeline (L403); the cooling air pipeline (L401) is connected to a cooling air inlet at the bottom of the hearth (101), the fuel air conveying pipeline (L402) is connected to an inlet of the fuel spray gun (104), and the combustion-supporting flue gas pipeline (L403) is connected to an inlet of the combustion-supporting air pipeline (L1); an oxygen conveying pipeline (L6) is also connected to the combustion-supporting air pipeline (L1);
preferably, a mixer (4) is arranged on the combustion air pipeline (L1); the mixer (4) comprises two inlets and an outlet, wherein the outlet of the mixer (4) is connected with the kiln top valve (103) through a combustion-supporting air pipeline (L1), and the two inlets of the mixer (4) are respectively connected with a combustion-supporting flue gas pipeline (L403) and an oxygen conveying pipeline (L6).
3. Lime kiln equipment according to claim 1 or 2, characterized in that: the slow Chu Da (3) is connected with a diffusing pipeline (L7) and a reflux pipeline (L8); the return line (L8) is connected to the circulation line (L4), and the connection point is located downstream of the point on the circulation line (L4) at which the storage line (L5) branches off.
4. A lime kiln plant according to claim 3, characterized in that: an inlet valve (K1) is arranged on the storage pipeline (L5); a short-circuit valve (K2) is arranged on the circulating pipeline (L4) and between the storage pipeline (L5) and the reflux pipeline (L8); and/or
A bleeding valve (K3) is arranged on the bleeding pipeline (L7); the reflux pipeline (L8) is provided with a reflux valve (K4).
5. Lime kiln equipment according to any of claims 2-4, characterized in that: the lime kiln equipment also comprises a flue gas distributor (5) arranged at the connection position of the flue gas discharge pipeline (L2), the finished product pipeline (L3) and the circulating pipeline (L4); and/or
And a diverter (6) is arranged at the position of the circulating pipeline (L4) for separating three pipelines.
6. Lime kiln equipment according to any of claims 2-5, characterized in that: a cooling device (7) is arranged on the cooling air pipeline (L401); preferably, the cooling device (7) is a water bath or an air cooler; and/or
A dust remover (8) is arranged on the flue gas discharge pipeline (L2); preferably, the dust remover (8) is an electric dust remover or a cloth bag dust remover.
7. The lime kiln equipment of claim 6, wherein: the flue gas discharge pipeline (L2) is provided with CO at the downstream of the dust remover (8) 2 A concentration detection device; and/or
And the buffer Chu Da (3) is provided with a pressure detection device.
8. A method of controlling a lime kiln plant based on carbon emission reduction or a method of controlling a lime kiln plant according to any one of claims 1-7 to produce lime, the method comprising the steps of:
1) Limestone material enters from the top of the hearth (101), pure oxygen and circulating flue gas which are conveyed by an oxygen conveying pipeline (L6) and a combustion-supporting flue gas pipeline (L403) are mixed in a mixer (4) to form O 2 With CO 2 Combustion air of the mixed gas is fed into the hearth (101) from a kiln top valve (103) through a combustion air pipeline (L1), fuel is fed into the hearth (101) from a fuel spray gun (104) by taking circulating flue gas conveyed by a fuel conveying and air supplying pipeline (L402) as a carrier, the fuel and the combustion air are combusted in the hearth (101) to release heat and form high-temperature flue gas, limestone materials are heated to rise temperature and complete calcination and decomposition, caO is generated and CO is released 2 A gas;
2) The cooling air pipeline (L401) is used for feeding the circulating flue gas cooled by the cooling device (7) from the bottom of the hearth (101), cooling the generated high-temperature CaO by cooling air, and discharging the cooled CaO from the bottom of the hearth (101) to obtain finished lime;
3) The high-temperature exhaust gas formed by cooling and the high-temperature flue gas formed by calcining enter another hearth (101) through a connecting channel (102), the high-temperature flue gas passes through a lime stone bed cooled in the hearth (101), the lime stone bed is preheated and heated, the temperature of the flue gas is reduced to form low-temperature hot air, and the low-temperature hot air enters a flue gas discharge pipeline (L2) from a kiln top valve (103) at the top of the hearth (101);
4) The low-temperature hot air is dedusted by a deduster (8) to obtain a main component of CO 2 Is then based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure conditions of the product demand and buffer tower (3) are further determined to be respectively fed into the CO 2 Finished product system (2) and slow storage tower(3) And the flue gas amount of the flow divider (6), thereby realizing the preparation of high-purity CO while producing lime 2 And (3) gas.
9. The control method according to claim 8, characterized in that: in step 4), the method is based on the CO in the flue gas 2 Whether or not the concentration of (C) reaches high purity CO 2 The pressure conditions of the product demand and buffer tower (3) are further determined to be respectively fed into the CO 2 The flue gas amount of the finished product system (2), the buffer tower (3) and the diverter (6) specifically comprises the following substeps:
401 The circulation smoke quantity required by a cooling air pipeline (L401), a fuel air conveying pipeline (L402) and a combustion-supporting smoke pipeline (L403) in the system is obtained, so that the circulation smoke quantity required by the flow divider (6) is obtained;
402 Through CO 2 The concentration detection device measures CO in the flue gas at the position of the flue gas distributor (5) 2 Concentration and judgment of CO 2 Whether the concentration reaches high purity CO 2 Product requirements;
a) If CO 2 If the concentration reaches the standard, further judging whether the pressure in the buffer tower (3) exceeds the lower limit or not through a pressure detection device;
If the pressure in the buffer tower (3) is detected to exceed the lower limit, the corresponding valve is operated, so that clean flue gas after dust removal is sent into the splitter (6) according to the circulating flue gas amount required by the splitter (6), and the residual flue gas enters CO 2 A finishing system (2);
if the pressure in the buffer tower (3) is detected not to exceed the lower limit, clean flue gas after dust removal completely enters CO 2 The finished product system (2) is characterized in that the circulating smoke volume required by the diverter (6) is provided by the buffer tower (3);
b) If CO 2 If the concentration does not reach the standard, further judging whether the pressure in the buffer tower (3) reaches the upper limit or not through a pressure detection device;
if the pressure in the slow storage tower (3) is detected to reach the upper limit, operating a corresponding valve, so that clean flue gas after dust removal is sent into the flow divider (6) according to the circulating flue gas amount required by the flow divider (6), the residual flue gas enters the slow storage tower (3), and the slow storage tower (3) discharges the corresponding flue gas amount through a discharge pipeline (L7);
if the pressure in the slow storage tower (3) is detected to be not up to the upper limit, clean flue gas after dust removal is sent into the flow divider (6) according to the circulating flue gas amount required by the flow divider (6), and the residual flue gas enters the slow storage tower (3).
10. The control method according to claim 9, characterized in that: the substep 401) specifically includes:
(1) Calculating cooling air quantity according to the amount of the finished lime obtained in the step 2), and obtaining the circulating smoke quantity required by a cooling air pipeline (L401);
(2) calculating fuel supply quantity according to the quantity of the finished lime and calculating fuel delivery air quantity according to the fuel supply quantity to obtain the circulating smoke quantity required by a fuel delivery air supply pipeline (L402);
(3) according to the fuel supply amount and O 2 With CO 2 CO in combustion-supporting air of mixed gas 2 And O 2 Calculating the pure oxygen amount required by the oxygen transmission pipeline (L6) and the circulating smoke amount required by the combustion-supporting smoke pipeline (L403);
(4) obtaining the circulating smoke volume required by the flow divider (6) according to the steps (1) - (3);
preferably, the O in step 1) 2 With CO 2 O in combustion-supporting air of mixed gas 2 The volume ratio of (2) is 27-31%, CO 2 The volume ratio of (3) is 69-73%.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116628576A (en) * | 2023-07-26 | 2023-08-22 | 中南大学 | Intelligent production yield monitoring method for heat carrier lime kiln |
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|---|---|---|---|---|
| CN105000811A (en) * | 2015-07-24 | 2015-10-28 | 东北大学 | Parallel flow heat accumulating type lime kiln production technology based on CO2 accumulation |
| CN207079173U (en) * | 2017-04-17 | 2018-03-09 | 王长春 | A kind of full recovery CO2 lime kiln device |
| CN108355420A (en) * | 2018-03-18 | 2018-08-03 | 上海柯来浦能源科技有限公司 | A kind of limekiln flue gas recirculation system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105000811A (en) * | 2015-07-24 | 2015-10-28 | 东北大学 | Parallel flow heat accumulating type lime kiln production technology based on CO2 accumulation |
| CN207079173U (en) * | 2017-04-17 | 2018-03-09 | 王长春 | A kind of full recovery CO2 lime kiln device |
| CN108355420A (en) * | 2018-03-18 | 2018-08-03 | 上海柯来浦能源科技有限公司 | A kind of limekiln flue gas recirculation system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116628576A (en) * | 2023-07-26 | 2023-08-22 | 中南大学 | Intelligent production yield monitoring method for heat carrier lime kiln |
| CN116628576B (en) * | 2023-07-26 | 2023-10-13 | 中南大学 | Intelligent production yield monitoring method for heat carrier lime kiln |
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