CN114907033A

CN114907033A - Production of cement clinker and CO-production of liquid CO by oxy-fuel combustion 2 System and method

Info

Publication number: CN114907033A
Application number: CN202210774521.7A
Authority: CN
Inventors: 陈昌华; 代中元; 林敏燕; 武晓萍; 万夫伟
Original assignee: Tianjin Cement Industry Design and Research Institute Co Ltd; China National Building Material Group Co Ltd CNBM
Current assignee: Tianjin Cement Industry Design and Research Institute Co Ltd; China National Building Material Group Co Ltd CNBM
Priority date: 2022-07-01
Filing date: 2022-07-01
Publication date: 2022-08-16
Anticipated expiration: 2042-07-01
Also published as: CN114907033B

Abstract

The invention discloses a method for producing cement clinker and CO-producing liquid CO by oxy-fuel combustion ₂ The system comprises a cement calcination main system, a total oxygen combustion sub-system and CO ₂ A trapping and purifying system, wherein in the pre-decomposition step, the main system and the subsystems run in parallel; in the rotary kiln, the calcined raw materials generated by the main system and the subsystem are simultaneously fed into the kiln to produce cement clinker; mutual interference between the main system and the subsystem is reduced. In the total oxygen combustion subsystem, the raw material decomposition process is divided into a primary combustion area and a secondary combustion area which are connected in series for operation, so that the raw material is fully decomposed, and NO is inhibited from being combusted by pulverized coal _X Releasing; the subsystem takes circulating air in a grading manner, so that the heat recovery is promoted while the safety of pulverized coal conveying is ensured, the energy consumption is reduced, and the carbon enrichment is realized. CO in enriched flue gas by sub-system oxy-fuel combustion ₂ Then through CO ₂ Liquid CO preparation by capture and purification system ₂ Realize the cementCarbon emission reduction and low-cost online preparation of CO in production process ₂ The product has good social and economic benefits.

Description

Production of cement clinker and CO-production of liquid CO by oxy-fuel combustion 2 System and method

Technical Field

The invention relates to the technical field of cement burning, in particular to a method for producing cement clinker and CO-producing liquid CO by oxy-fuel combustion ₂ Systems and methods of (1).

Background

Fossil energy is taken as the most main energy source in the world, and huge CO is brought by the consumption process of the fossil energy ₂ Emissions become an important source of emissions for the greenhouse effect. The current situation of rich coal, poor oil and little gas in China determines that the proportion of coal in the structure of primary energy in China is difficult to change in a short time. In recent years, the total carbon emission amount in China exceeds the United states, the carbon dioxide emission state becomes the largest carbon dioxide emission state in the world, and the carbon emission reduction situation is very severe.

The total oxygen combustion is based on the existing industrial kiln system, high-purity oxygen is used to replace combustion air, and simultaneously, the medium flow and heat transfer characteristics of a hearth are adjusted by adopting flue gas circulation, so that CO with the volume concentration of up to 80 percent can be obtained ₂ Flue gas, thereby capturing and purifying CO at low cost ₂ Permanent sealing or resource utilization, and realization of large-scale industrial CO ₂ Enrichment and emission reduction. The existing analysis shows that compared with other carbon capture modes, the oxy-fuel combustion technology has the advantages of investment cost, operation cost and CO ₂ The method has the advantages of emission reduction cost, large scale, compatibility with the prior art and the like.

The existing oxy-fuel combustor is mostly used for float glass kiln, glass fiber kiln, steel rolling heating furnace, forging furnace, heat treatment furnace and the like, and the fuel is mainly natural gas. Coal-fired oxy-fuel burners are less industrially used, chinese patent publication No. CN101825278A proposes an oxygen-enriched burner, and US patent No. US20110126780a1 proposes an oxy-fuel fired boiler pulverized coal burner, which are mainly directed to oxy-fuel combustion of coal-fired power generation boilers. As for the cement industry kiln, the production arrangement and the reaction conditions of the cement industry kiln are greatly different from those of glass and thermal power kilns, and special design needs to be carried out on a cooler, system air and the like, the actual case of operating a pure oxygen combustion technology does not exist in the cement industry at present.

A large amount of carbon dioxide is generated in the cement production process, and according to statistics, 0.6-0.7 t of carbon dioxide is discharged when 1t of cement is produced.

Carbon dioxide in the cement kiln waste gas mainly comes from the following two aspects:

1. carbon dioxide generated in fuel combustion flue gas accounts for about 40%;

2. the carbon dioxide produced by decomposition of the carbonate in the feedstock is present in a proportion of about 60%.

The carbon capture and sequestration technology is the most feasible new technology for reducing carbon dioxide emission in the cement industry at present, wherein the oxy-fuel combustion technology has a better development prospect in the carbon capture and sequestration technology.

Oxy-fuel combustion refers to the combustion of fuel by using industrial oxygen instead of air, so that the fuel can be combusted more completely, and compared with air combustion, oxy-fuel combustion has the following advantages:

1) compared with the air combustion, the oxy-fuel combustion process has the advantages that about 79% of nitrogen in the air does not participate in the combustion any more, so that the flame temperature can be increased;

2) the content of nitrogen in the flue gas is low, the combustion product is a triatomic product, the heat transfer effect of a triatomic substance is higher than that of a diatomic substance, and the heating efficiency is improved;

3) the nitrogen does not participate in smoke discharge any more, so that the smoke quantity can be greatly reduced, and the heat loss of the smoke discharge is reduced.

At present, the oxy-fuel combustion technology is widely applied to float glass and glass fiber kilns, is still in the research and development stage in the cement industry, and the cement industry mainly adopts the oxy-fuel combustion technology in decomposing furnaces and rotary kilns.

In the oxy-fuel combustion process of the high-oxygen concentration cement kiln, oxygen and circulating flue gas are required to be introduced into the kiln to replace air as combustion gas, but how to inject the oxygen and the circulating flue gas into the cement kiln is a key technical difficulty. In a conventional oxy-fuel combustion system, oxygen and circulating flue gas are generally mixed, and the mixed gas is transported through a pipeline and injected into a cement kiln. However, in the high oxygen concentration oxy-fuel combustion system, if the air supply mode that oxygen and circulating flue gas are mixed firstly and the mixed gas is transported through a pipeline and then injected into the cement kiln is adopted, a serious safety problem exists. Because in the flue gas circulation system, even if the bag-type dust remover is arranged to remove dust from the circulating flue gas, a small amount of carbon-containing particles with small particle sizes are still carried in the flue gas, if high-concentration industrial oxygen (with volume fraction of about 80-95%) and the circulating flue gas are directly mixed and transported according to a conventional method, the small amount of carbon-containing particles carried in the circulating flue gas are easy to ignite and burn after encountering pure oxygen, once the mixed gas burns in a pipeline, a serious safety accident is caused, the equipment body is endangered, and meanwhile, the safety of operating personnel is threatened. Chinese patent publication No. CN105650628A proposes an oxygen-enriched combustion device of a circulating fluidized bed and an oxygen-enriched combustion air supply method thereof, wherein oxygen and circulating flue gas are not mixed before entering a furnace body, are respectively conveyed in respective pipelines, and are supplied with air at a plurality of positions of the furnace body with different heights, thereby solving the safety problem in the oxygen conveying and mixing process. However, the air supply mode of the patent only aims at the circulating fluidized bed, and is not applicable to the oxy-fuel combustion of the cement kiln.

In addition, because the fuel combustion and the raw material decomposition process in the cement decomposing furnace are coupled, the combustion temperature in the hearth of the decomposing furnace is relatively low, generally 900-1100 ℃, if the medium-low temperature circulating flue gas (generally below 400 ℃) out of the burning system directly enters the decomposing furnace, the temperature of the combustion area in the decomposing furnace is difficult to maintain above the ignition temperature of the pulverized coal, and the flame in the decomposing furnace is unstable and even flameout. Therefore, it is necessary to raise the temperature of the oxygen and the circulating flue gas before introducing the oxygen and the circulating flue gas into the cement decomposing furnace. Under the condition of oxygen enrichment and carbon enrichment, as the theoretical combustion temperature of the fuel is greatly improved, the safety and pollutant emission of a combustion device also face great challenges, and the main problems are as follows: 1) the problems of deflagration, unstable combustion and furnace wall ablation easily occur in the combustion device; 2) NO is easy to cause in the combustion process when the flame temperature rises in the oxygen-rich state _X The emission is increased, and the negative effect of flue gas denitration of a subsequent waste gas treatment system is increasedAnd (4) loading.

Therefore, the development of the carbon capture technology for the local oxy-fuel combustion flue gas of the cement kiln, which has reliable technology and low operation cost and does not influence the existing production operation working condition, is a more practical and feasible method for carbon emission reduction in the cement industry. However, the following problems still exist at present:

1) when the total oxygen combustion carbon enrichment system is in an ignition stage, the air combustion working condition is used for ignition and temperature rise so as to reduce the consumption of industrial oxygen; or when the carbon dioxide-rich flue gas output needs to be suspended under an abnormal working condition, the problem that the running state is rapidly switched from the local oxy-fuel combustion state to the air combustion state is faced;

2) the local oxy-fuel combustion carbon enrichment subsystem and the cement production main system have poor process compatibility and mutually interfere;

3) the pipeline safety problem is caused by the ignition and combustion of residual carbon particles in the flue gas and industrial oxygen in a mixed conveying mode of medium-low temperature circulating flue gas and industrial oxygen;

4) the processes of raw material decomposition heat absorption and combustion heat release are coupled, and medium-low temperature circulating flue gas is directly introduced into a decomposing furnace, so that the problems that fuel is difficult to ignite, flame is unstable, and flameout is easy to occur in the combustion process are caused;

5) the middle-low temperature circulating flue gas is directly introduced into the decomposing furnace, and the raw materials of the decomposing furnace are difficult to lift by wind due to small working condition air quantity, so that the problem of material collapse is caused.

In addition, carbon dioxide is a valuable resource which can be utilized, is widely applied in various fields such as chemical industry, food industry, mechanical processing, oil exploitation and the like, and is an important method for reducing the emission of carbon dioxide by recycling. Thus. Provides a method for CO-producing liquid CO in the production of cement clinker ₂ The product system reduces carbon emission in the cement production process, and does not influence the yield and quality of a cement production line; with CO ₂ The production cost of the product is low, the recovery rate is high, the product purity is high, and the quality is stable, which is a problem to be solved urgently by technical personnel in the field.

Disclosure of Invention

The invention aims to solve the problems in the prior art and provides a method for producing cement clinker and CO-producing liquid CO by oxy-fuel combustion ₂ In a system and a method, the systemThe system mainly comprises a cement calcination main system, a total oxygen combustion sub-system and CO ₂ The gathering and purifying system is composed of a subsystem full oxygen combustion for enriching CO in flue gas in the process of producing cement clinker ₂ Then through CO ₂ Liquid CO preparation by capture and purification system ₂ Can realize carbon emission reduction and low-cost on-line preparation of CO in the cement production process ₂ The product has good social and economic benefits.

The invention is realized by the way that the cement clinker is produced by oxy-fuel combustion and liquid CO is CO-produced ₂ The system comprises a cement calcination main system, a oxy-fuel combustion sub-system and CO ₂ A trapping and purifying system;

the total oxygen combustion subsystem consists of a sub-preheater unit, a self-enrichment furnace, a flue gas preheating unit, a Venturi throat, a sub-high-temperature fan, a cooler, a sub-dust collector, a medium-temperature circulating fan, a medium-temperature circulating flue gas supply pipeline, a low-temperature circulating fan, a low-temperature circulating flue gas supply pipeline, a fuel supply pipeline and an industrial oxygen supply pipeline;

a feeding pipe of a penultimate sub cyclone cylinder of the sub-preheater unit is connected with a raw material feeding pipe of the self-enrichment furnace, a feeding pipe of a last-stage sub cyclone cylinder of the sub-preheater unit is connected with a kiln tail smoke chamber of a main cement calcination system, and an outlet air pipe at the top of the sub-preheater unit is sequentially provided with a sub-high temperature fan, a cooler, a sub-dust collector and a sub-exhaust fan; the medium-temperature circulating fan is arranged on a medium-temperature circulating flue gas supply pipeline, one end of the medium-temperature circulating flue gas supply pipeline is connected with a pipeline between the sub high-temperature fan and the cooler, and the other end of the medium-temperature circulating flue gas supply pipeline is connected with the flue gas preheating unit; the low-temperature circulating fan is arranged on a low-temperature circulating flue gas supply pipeline, one end of the low-temperature circulating flue gas supply pipeline is connected with a pipeline of a gas outlet of the sub dust collector, and the other end of the low-temperature circulating flue gas supply pipeline is connected with a fuel supply pipeline;

the flue gas preheating unit is used for preheating low-temperature circulating flue gas and medium-temperature circulating flue gas to over 900 ℃ through fuel; the bottom flue gas outlet of the flue gas preheating unit is connected with the bottom inlet of the venturi throat, the top outlet of the venturi throat is connected with the bottom of the cylinder of the self-enrichment furnace, and the top outlet of the self-enrichment furnace is connected with the inlet of the last-stage cyclone cylinder;

the fuel supply pipeline is respectively connected with the flue gas preheating unit and a coal injection pipe at the upper part of the Venturi throat, and the industrial oxygen supply pipeline is respectively connected with the flue gas preheating unit and an oxygen pipe at the lower part of the Venturi throat;

the CO is ₂ The trapping and purifying system comprises a water distribution tank, a drying bed, an adsorption bed, a refrigerator and a rectifying tower which are sequentially connected and arranged on an outlet pipeline of the sub-exhaust fan, a top gas outlet of the rectifying tower is sequentially connected with a condenser and a gas-liquid separator, a liquid outlet of the gas-liquid separator is connected with the rectifying tower, a bottom liquid outlet of the rectifying tower is connected with an inlet of a reboiler, a gas outlet of the reboiler is connected with the rectifying tower, and a liquid outlet of the reboiler is connected with a liquid CO ₂ The storage tank is connected.

And (3) preheating and decomposing a part of the cement raw materials to the total oxygen combustion subsystem, and returning the decomposed raw materials to a rotary kiln of the cement calcination main system to calcine to produce cement clinker. The total oxygen combustion subsystem is provided with a preheating furnace and a self-enrichment furnace, the fuel is pulverized coal, the combustion-supporting air is industrial oxygen, and combustion flue gas and CO generated by decomposition of raw materials ₂ Form CO-rich gas with concentration of more than 80% ₂ Flue gas. Rich in CO ₂ Flue gas in CO ₂ The gathering and purifying system is used for preparing CO after dehydration, drying, desulfurization, denitrification and condensation rectification in sequence ₂ Liquid CO with mass fraction of more than 99% ₂ And (5) producing the product.

Preferably, the flue gas preheating unit comprises a burner and a preheating furnace, the burner is mounted at the top of the preheating furnace, the head of the burner extends into the preheating furnace, the burner comprises an oil pipe, an inner primary air pipe, a coal pipe and an outer primary air pipe which are coaxially sleeved from inside to outside in sequence, and a central oil gun channel, an inner primary air channel, a coal powder channel and an outer primary air channel are sequentially formed in the burner from inside to outside; the tail parts of the inner primary air pipe and the outer primary air pipe are both connected with an industrial oxygen supply pipeline, and the tail part of the coal pipe is connected with a fuel supply pipeline;

the head ports of the oil pipe, the coal pipe and the outer primary air pipe are aligned to form the head of the burner; a distance H0 is reserved between the head of the inner primary air pipe and the head of the burner, so that the inner primary air channel and the coal powder channel form an air-coal premixing channel at the head of the burner; an air-coal premixing adjusting ring which can move back and forth along the axial direction of the burner is arranged between the inner primary air channel and the pulverized coal channel, so that the length of the air-coal premixing channel can be adjusted between 0 and H0;

the preheating furnace consists of a spiral-flow chamber, a reducing section and a hearth from top to bottom, wherein the spiral-flow chamber is of a volute structure, so that flue gas entering from an inlet of the spiral-flow chamber enters in a volute tangential spiral flow;

and a fuel-rich area positioned in the center of the hearth, an oxygen-rich area positioned outside the fuel-rich area and a carbon-rich area positioned between the oxygen-rich area and the furnace wall are formed in the preheating furnace.

Further preferably, the air-coal premixing adjusting ring is arranged on the inner side wall of the inner primary air pipe.

Further preferably, the inlet of the inner primary air channel and the outlet of the outer primary air channel are provided with a swirler.

Further preferably, a refractory material layer is arranged outside the outer primary air channel.

Further preferably, flow controllers are respectively arranged on the industrial oxygen supply pipelines connected with the oxygen pipes at the lower parts of the inner primary air pipe, the outer primary air pipe and the venturi throat.

Further preferably, a burner mounting hole is formed in the center of the top cover of the cyclone chamber, and the head of the burner extends into the cyclone chamber through the burner mounting hole.

Further preferably, the inner diameter of the reducing section is gradually increased from top to bottom.

Preferably, a medium-temperature circulating air valve is arranged on a medium-temperature circulating flue gas supply pipeline at an inlet of the medium-temperature circulating fan, and a low-temperature circulating air valve is arranged on a low-temperature circulating flue gas supply pipeline at an inlet of the low-temperature circulating fan.

Preferably, the venturi throat pipe is divided into a lower contraction section, a throat area high-speed section and an upper expansion section from bottom to top, the lower contraction section is inserted into the oxygen pipe, the oxygen pipe is inserted into the venturi throat pipe in a downward inclination manner to be close to the axial center of the venturi throat pipe, and an included angle between the oxygen pipe and the horizontal direction is 30-60 degrees, so that the industrial oxygen and the circulating flue gas are uniformly mixed; the coal injection pipe is inserted into the upper expansion section and is inserted to be close to the inner wall of the upper expansion section, so that circulating flue gas and coal powder are mixed at a vortex low-pressure area formed outside the upper expansion section; the number of the oxygen pipes and the number of the coal injection pipes are respectively 2-4, and the oxygen pipes and the coal injection pipes are symmetrically arranged along the circumference.

Preferably, the raw material feeding pipe is arranged at the bottom of the column of the self-enriching furnace.

Preferably, a compressor set and a surge tank are sequentially arranged on a pipeline between the outlet of the water diversion tank and the inlet of the drying bed.

Production of cement clinker and CO-production of liquid CO by oxy-fuel combustion ₂ The method adopts a main cement calcination system and a total oxygen combustion subsystem to run in parallel to carry out air combustion and partial total oxygen combustion, and the flow paths of raw materials are in parallel connection without cross in a preheating pre-decomposition link; in the clinker calcining link, two raw materials decomposed by a cement calcining main system and a total oxygen combustion subsystem enter a rotary kiln to be calcined together to prepare cement clinker;

in the total oxygen combustion subsystem, raw meal is fed into a sub-preheater unit, is preheated by the sub-preheater unit, is fed into a self-enrichment furnace for predecomposition, and then enters a rotary kiln for calcination; the smoke from the enrichment furnace is subjected to heat exchange through a sub-preheater unit under the air draft of a sub-high-temperature fan, and part of the smoke is returned to the preheating furnace as medium-temperature circulating smoke; after the residual flue gas is cooled and dust-collected, one part of the residual flue gas is used as low-temperature circulating flue gas, and the rest part of the residual flue gas is rich in CO ₂ Flue gas enters CO ₂ The gathering and purifying system is used for preparing CO after dehydration, drying, desulfurization, denitrification and condensation rectification ₂ Liquid CO with mass fraction of more than 99% ₂ And (5) producing the product.

Preferably, the pre-decomposition raw meal in the self-enrichment furnace is decomposed by adopting a mode of twice total oxygen combustion carbon enrichment, and the method comprises the following specific steps:

the method comprises the following steps: taking low-temperature circulating flue gas from a pipeline of a gas outlet of the sub-dust collector, wherein the low-temperature circulating flue gas carries pulverized coal to enter a pulverized coal channel of the combustor; industrial oxygen enters an inner primary air channel and an outer primary air channel of the burner respectively in two paths, industrial oxygen in the inner primary air channel enters in a swirling mode, industrial oxygen in the outer primary air channel is ejected in a swirling mode, the supply amount of the industrial oxygen meets the oxygen amount required by combustion of pulverized coal in the preheating furnace, and the pulverized coal is stably combusted in the preheating furnace after being ejected;

taking medium-temperature circulating flue gas from a pipeline between a sub high-temperature fan and a cooler, introducing the medium-temperature circulating flue gas into a cyclone chamber of a preheating furnace in a tangential cyclone manner, and making the medium-temperature circulating flue gas move downwards along the wall under the centrifugal force of the cyclone chamber at the top; the pulverized coal and the industrial oxygen are sprayed out from the burner and then are ignited and combusted in the preheating furnace, so that a fuel-rich area positioned in the center of the hearth, an oxygen-rich area positioned outside the fuel-rich area and a carbon-rich area positioned between the oxygen-rich area and the furnace wall are formed in the space in the preheating furnace; the combustion heat of the pulverized coal raises the temperature of the middle-low temperature circulating flue gas to over 900 ℃;

step two: the high-temperature circulating flue gas with the temperature of over 900 ℃ of the flue gas outlet preheating unit reversely moves upwards;

step three: the high-temperature circulating flue gas enters a Venturi throat, and industrial oxygen is sprayed into the inlet of the Venturi throat to increase the oxygen concentration of the central area to be more than 30%; spraying coal powder into the outlet of the venturi throat, wherein the outlet gas forms jet flow, and a vortex low-pressure area is formed on the outer side of the upper part of the venturi throat under the action of the jet flow;

step four: the coal powder enters the self-enrichment furnace along with the circulating flue gas to burn and release heat, raw materials are fed into a raw material feeding pipe of the self-enrichment furnace, so that the raw materials are decomposed in the self-enrichment furnace, and CO is released ₂ Self-enriched furnace flue gas dry basis CO ₂ The concentration is more than 80%, and the temperature is 850-1000 ℃.

Further preferably, the fineness of the coal dust is controlled to be 80um, and the screen residue is lower than 20%; the oxygen concentration of the industrial oxygen is not lower than 80%; the temperature of the low-temperature circulating flue gas is lower than 150 ℃, and CO is ₂ Concentration higher than 60%, O ₂ The concentration is lower than 10%; the temperature of the medium-temperature circulating flue gas is lower than 400 ℃, and CO is ₂ Concentration higher than 60%, O ₂ The concentration is less than 10%。

Preferably, according to the combustion characteristics of the pulverized coal, the length of the air-coal premixing channel is adjusted by adjusting the air-coal premixing adjusting ring, and/or the ignition and flame stability of the pulverized coal are enhanced by adjusting the amount of industrial oxygen entering the inner primary air channel and the outer primary air channel, so that the pulverized coal is stably combusted in the preheating furnace after being sprayed.

Preferably, in the third step, the average wind speed of the section of the throat area high-speed section of the venturi throat pipe is 25-50 m/s, the average wind speed of the section of the outlet of the upper expansion section is 5-15 m/s, and the wind speed of the throat area high-speed section is more than 2 times of the wind speed of the outlet of the upper expansion section.

Preferably, liquid CO is produced ₂ The process of the product is as follows: rich in CO ₂ The flue gas is primarily dehydrated through a water distribution tank, the dehydrated flue gas enters a compressor unit for pressurization, and the dehydrated flue gas enters a drying bed for dehydration and drying after passing through a pressure stabilizing tank; the dried flue gas enters an adsorption bed to remove SO _X And NO _X Impurities; the carbon dioxide-rich flue gas out of the adsorption bed enters a refrigerator for refrigeration and then enters a rectifying tower; in the rectifying tower, light component impurities and a small amount of carbon dioxide are separated out at the top of the rectifying tower, the separated mixed gas is treated by a condenser to condense the carbon dioxide into liquid again, the liquid carbon dioxide returns to the rectifying tower after passing through a gas-liquid separator, and the rest gas is discharged out of the system; the liquid carbon dioxide at the bottom of the rectifying tower enters a reboiler, impurities dissolved in the carbon dioxide are returned to the rectifying tower, and the liquid carbon dioxide discharged from the reboiler is conveyed to the liquid CO ₂ And (4) storage tank.

The invention has the advantages and positive effects that:

1. the main system and the sub-system are operated in parallel to perform air combustion and local oxy-fuel combustion, the main system and the sub-system are operated in parallel in the preheating and predecomposition link of the firing kiln tail, and the calcined raw materials generated by the main system and the sub-system are simultaneously fed into the rotary kiln to produce cement clinker in the clinker calcining link, so that the mutual interference between the main system and the sub-system is reduced; the total oxygen combustion subsystem adopts classified circulating air taking, and medium temperature circulating air is taken between a sub high-temperature fan and a coolerThe circulating air (150-400 ℃) is directly fed into the preheating furnace, and the low-temperature circulating air (lower than 150 ℃) is taken from the sub-dust collector and used as pulverized coal conveying air, so that the heat recovery is promoted while the safety of pulverized coal conveying is ensured, the energy consumption is reduced, and the carbon enrichment is realized; rich in CO ₂ The flue gas enters CO at the same time ₂ The gathering and purifying system is used for preparing CO after dehydration, drying, desulfurization, denitrification and condensation rectification ₂ Liquid CO with mass fraction of more than 99% ₂ The product realizes carbon emission reduction in the cement production process and the low-cost on-line preparation of liquid CO ₂ The product has good social and economic benefits.

2. In the total-oxygen combustion subsystem, the raw material is pre-decomposed into a primary combustion area and a secondary combustion area which are operated in series, raw material is not fed into the primary combustion area where a combustor and a preheating furnace are located, coal powder is conveyed through low-temperature circulating flue gas, industrial oxygen is divided into two parts to supply air inside and outside a coal powder channel, and the medium-temperature circulating flue gas supplies air from a swirling chamber of the preheating furnace to an adherence wall, so that the flame stability of the coal powder in the preheating furnace is realized, the wall of the preheating furnace is not ablated, and the low NO is realized _X Discharging and fully burning off the coal dust, and heating the middle-low temperature circulating flue gas to above 900 ℃ in a preheating furnace; in the secondary combustion zone where the Venturi throat and the self-enrichment furnace are positioned, the secondary combustion zone carries out material operation, high-temperature circulating flue gas is introduced into the bottom of the secondary combustion zone, industrial oxygen and coal powder are sprayed in the secondary combustion zone to decompose raw materials, jet flow is formed through the arranged Venturi throat to support the materials, the problem of furnace wall high-temperature skinning caused by raw material collapse and local explosion of the coal powder is solved, NO (nitric oxide) generated by coal powder combustion is inhibited _X Releasing to ensure that the temperature of flue gas is 850-1000 ℃ during self-enrichment furnace, and dry basis CO is generated ₂ The concentration is more than 80 percent, and the full decomposition of the raw material is realized.

3. According to the combustor provided by the invention, the industrial oxygen is not contacted with the coal powder and the circulating flue gas in the conveying process, and the coal conveying air for conveying the coal powder adopts the low-temperature circulating flue gas at the temperature of less than 150 ℃, so that the spontaneous combustion of unburned carbon particles in the circulating flue gas is avoided, and the safety problem of spontaneous combustion caused by the mixed conveying of the industrial oxygen and the coal powder in an oxy-fuel combustion subsystem is solved.

4. According to the burner provided by the invention, the air-coal premixing adjusting ring which can move back and forth along the axial direction of the burner is additionally arranged between the inner primary air channel and the coal powder channel, so that the length of the air-coal premixing channel can be flexibly adjusted, whether industrial oxygen and coal powder are premixed in the burner or not can be adjusted according to the combustion characteristics of the coal powder, the problems of unstable flame and even flameout are avoided, and the ignition and flame stability of coal are enhanced; or the problem that the head of the burner is burnt out when the flame is tempered to the premixing area due to the excessively high flame burning speed is avoided, the deflagration and the tempering of the pulverized coal are prevented, and the ignition and the flame stability of the pulverized coal are enhanced on the premise of no tempering.

5. The burner provided by the invention can adjust the amount of industrial oxygen entering the inner primary air channel and the outer primary air channel according to the combustion characteristics of the pulverized coal, thereby preventing the deflagration and the tempering of the pulverized coal and strengthening the ignition and flame stability of the pulverized coal; and the outer primary air is high-speed rotational flow air, so that the flame stability is further enhanced.

6. According to the preheating furnace provided by the invention, the medium-temperature circulating flue gas (150-400 ℃) enters from the cyclone chamber at the top of the preheating furnace and flows downwards in a wall-attached rotary mode in the cyclone chamber, and a low-temperature protective gas film is formed in front of the furnace wall and the flame due to the relatively low temperature and low oxygen content of the medium-temperature circulating flue gas, so that the refractory material on the wall surface of the preheating furnace is effectively protected, and the flame is prevented from being ablated.

7. According to the venturi throat, the pulverized coal is located in the upper expansion area of the venturi throat, the industrial oxygen is introduced into the lower contraction area of the venturi throat, and the industrial oxygen and the circulating flue gas are uniformly mixed through the venturi throat and then are contacted with the pulverized coal, so that the pulverized coal deflagration caused by high local oxygen concentration in the self-enrichment furnace is prevented, and the wall surface of the self-enrichment furnace is prevented from being skinned; the gas at the outlet of the venturi throat forms jet flow, so that a vortex low-pressure area is formed at the outer side of the upper expansion section under the action of the jet flow, the circulating flue gas and the pulverized coal are back-mixed in the area, the oxygen concentration of the circulating flue gas at the outer side is relatively low, and NO (nitric oxide) generated by pulverized coal combustion is inhibited _X And (4) releasing.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without creative efforts.

FIG. 1 shows the production of cement clinker with CO-production of liquid CO by oxy-fuel combustion according to an embodiment of the present invention ₂ A process flow diagram of the system of (1);

FIG. 2 is a process flow diagram of an oxy-fuel combustion subsystem provided by an embodiment of the present invention;

FIG. 3 is a schematic structural diagram of a flue gas preheating unit provided in the embodiment of the present invention;

FIG. 4 is a schematic structural diagram of a preheating furnace provided in an embodiment of the present invention;

FIG. 5 is a schematic view of a cyclone chamber according to an embodiment of the present invention;

FIG. 6 is a first schematic structural diagram of a burner provided in an embodiment of the present invention;

FIG. 7 is a schematic structural view of section A-A of FIG. 6;

FIG. 8 is a schematic structural diagram II of a burner according to an embodiment of the present invention;

FIG. 9 is a schematic structural view of the section B-B of FIG. 8;

FIG. 10 is a schematic structural view of a venturi throat provided in accordance with an embodiment of the present invention;

FIG. 11 is a top view of a venturi throat provided by embodiments of the present invention.

Wherein: g 1-technical oxygen; g 2-medium temperature circulating flue gas; g 3-low temperature circulating flue gas; g 4-CO-Rich ₂ Flue gas; g 5-rectifying column vent gas; f-pulverized coal; a-a fuel rich zone; b-an oxygen-rich zone; a C-carbon rich region; h-length of the air-coal premixing area; m-raw meal; k-cement clinker; w-separating water;

1-cement calcination primary system; 101-a first stage main cyclone; 102-a second stage main cyclone; 103-third stage main cyclone; 104-a fourth stage main cyclone; 105-a fifth stage main cyclone; 106-main decomposing furnace; 107-kiln tail smoke chamber; 108-a rotary kiln; 109-a cooling machine; 110-a kiln head burner; 111-tertiary air pipe; 112-a main high temperature fan; 113-a zipper machine; 114-a clinker repository;

2-a oxy-fuel combustion subsystem;

201-first stage sub-cyclone; 202-second stage sub-cyclone; 203-third stage sub-cyclones; 204-a fourth stage sub-cyclone; 205-fifth stage sub-cyclone;

206-self-enriching furnace; 2061-raw meal feed tube;

207-venturi throat; 2071-lower contraction section; 2072-throat area high speed section; 2073-an upper dilating segment; 2074-an oxygen tube; 2075-coal injection pipe;

208-preheating furnace; 2081-a swirl chamber; 2082-a reducer section; 2083-hearth; 20811-swirl chamber inlet; 20812-cyclone chamber top cap; 20813-burner mounting holes;

209-a burner; 2091-central oil gun passage; 2092-inner primary air cyclone; 2093-inner primary air passage; 2094-pulverized coal passage; 2095-outer primary air passage; 2096-outer primary air cyclone; 2097-air-coal premixing passage; 2098-air-coal premixing adjusting ring; 2099-layer of refractory material;

210-a high temperature fan; 211-medium temperature circulating fan; 212-medium temperature circulating air valve; 213-a cooler; 214-sub dust collector; 215-sub-ventilator; 216-low temperature circulating fan; 217-low temperature circulating air valve; 218-a pulverized coal bunker; 219-inner primary air flow controller; 220-outer primary air flow controller; 221-secondary air flow controller;

3-CO ₂ a capture purification system; 301-a water separation tank; 302-compressor train; 303-pressure stabilizing tank; 304-a drying bed; 305-an adsorption bed; 306-a refrigerator; 307-a rectifying tower; 308-a condenser; 309-gas-liquid separator; 310-a reboiler; 311-liquid CO ₂ And (4) storage tank.

Detailed Description

The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

Examples

Referring to FIGS. 1 to 11, the present embodiment provides a method for producing cement clinker and CO-producing liquid CO by oxy-fuel combustion ₂ The system consists of a cement calcination main system 1, a total oxygen combustion subsystem 2 and a CO2 trapping and purifying system 3, wherein two-stage to seven-stage preheaters can be adopted as preheater units of the cement calcination main system 1 and the total oxygen combustion subsystem 2, and a five-stage preheater is taken as an example for the embodiment.

The cement calcination main system 1 comprises a main preheater unit, a main decomposing furnace 106, a kiln tail smoke chamber 107, a rotary kiln 108, a cooler 109, a kiln head burner 110, a tertiary air pipe 111, a main high-temperature fan 112, a zipper machine 113 and a clinker storage warehouse 114, wherein the main preheater unit is a five-stage cyclone preheater, and a main high-temperature fan, a main dust collector, a main exhaust fan and a chimney are sequentially arranged on an outlet air pipe at the top of the main preheater unit. Raw materials entering the cement calcining main system 1 are fed into an outlet air pipe of the second-stage main cyclone 102 through a pipeline to perform gas-solid heat exchange, and enter the first-stage main cyclone 101 under the driving of airflow; after gas-solid separation is performed in the first-stage main cyclone 101, the material is fed into an outlet air pipe of the third-stage main cyclone 103 from a feeding pipe of the first-stage main cyclone 101. In the above manner, the second stage main cyclone 102, the third stage main cyclone 103 and the fourth stage main cyclone 104 are entered in sequence. The raw material gas-solid separated by the fourth stage main cyclone 104 enters the main decomposing furnace 106, the decomposition of the raw material (the decomposition of calcium carbonate in the raw material into calcium oxide) is completed in the main decomposing furnace 106, the decomposed raw material enters the fifth stage main cyclone 105 along with the airflow, and the raw material is fed into the kiln tail smoke chamber 107 after the gas-solid separation.

Referring to fig. 2, the total oxygen combustion subsystem 2 is composed of a sub-preheater unit, a self-enrichment furnace 206, a flue gas preheating unit, a venturi throat 207, a sub-high temperature fan 210, a cooler 213, a sub-dust collector 214, a medium temperature circulating fan 211, a medium temperature circulating flue gas supply pipeline, a low temperature circulating fan 216, a low temperature circulating flue gas supply pipeline, a fuel supply pipeline and an industrial oxygen supply pipeline, and the sub-preheater unit is also a five-stage cyclone preheater. The discharge pipe of the fourth stage cyclone 204 of the sub-preheater unit is connected with the raw material feeding pipe 2061 of the self-enrichment furnace 206, the top outlet of the self-enrichment furnace 206 is connected with the inlet of the fifth stage cyclone 205, and the discharge pipe of the fifth stage cyclone 205 of the sub-preheater unit is connected with the kiln tail smoke chamber 107 of the main cement calcination system 1. Raw materials entering the total oxygen combustion subsystem 2 are fed into an outlet air pipe of the second-stage sub-cyclone 202 through a pipeline to perform gas-solid heat exchange, and enter the first-stage sub-cyclone 201 under the driving of airflow; after gas-solid separation in the first stage cyclone 201, the material is fed into the outlet air pipe of the third stage cyclone 203 from the feeding pipe of the first stage cyclone 201. In the above manner, the second stage sub-cyclone 202, the third stage sub-cyclone 203 and the fourth stage sub-cyclone 204 are entered in sequence. The raw material after gas-solid separation by the fourth stage cyclone 204 enters the self-enrichment furnace 206, the decomposition of the raw material is completed in the self-enrichment furnace 206, the decomposed raw material enters the fifth stage cyclone 205 along with the airflow, and the raw material is fed into the kiln tail smoke chamber 107 after gas-solid separation.

The raw materials of the cement calcination main system 1 and the raw materials of the oxy-fuel combustion subsystem 2 enter the kiln tail smoke chamber 107 together, are calcined into cement clinker in the rotary kiln 108, and the high-temperature clinker is cooled by the cooler 109 and then is conveyed to a clinker storage warehouse 114 through the zipper 113.

The sub high-temperature fan 210, the cooler 213, the sub dust collector 214 and the sub exhaust fan 215 are sequentially arranged on an outlet air pipe at the top of the sub preheater unit; the medium temperature circulating fan 211 is arranged on the medium temperature circulating flue gas supply pipeline, one end of the medium temperature circulating flue gas supply pipeline is connected with the pipeline between the sub high temperature fan 210 and the cooler 213, the other end of the medium temperature circulating flue gas supply pipeline is connected with the flue gas preheating unit, and a medium temperature circulating air valve 212 is arranged on the medium temperature circulating flue gas supply pipeline at the inlet of the medium temperature circulating fan 211; the low-temperature circulating fan 216 is arranged on a low-temperature circulating flue gas supply pipeline, one end of the low-temperature circulating flue gas supply pipeline is connected with a pipeline of a gas outlet of the sub dust collector 214, the other end of the low-temperature circulating flue gas supply pipeline is connected with a fuel supply pipeline, and a low-temperature circulating air valve 217 is arranged on the low-temperature circulating flue gas supply pipeline at the inlet of the low-temperature circulating fan 216; the bottom flue gas outlet of the flue gas preheating unit is connected with the bottom inlet of the venturi throat 207, and the top outlet of the venturi throat 207 is connected with the bottom of the cylinder of the self-enrichment furnace 206; the fuel supply pipeline is respectively connected with the flue gas preheating unit and the coal injection pipe 2075 at the upper part of the venturi throat 207, and the industrial oxygen supply pipeline is respectively connected with the flue gas preheating unit and the oxygen pipe 2074 at the lower part of the venturi throat 207.

The flue gas from the enrichment furnace 206 is subjected to heat exchange through a sub-preheater unit under the air draft of a sub-high temperature fan 210, and part of the flue gas is returned to the preheating furnace 208 as medium-temperature circulating air; after the residual flue gas is cooled and dust-collected by the cooler 213, part of the residual flue gas is used as low-temperature circulating air, and the rest is rich in CO ₂ The flue gas enters the CO2 capture purification system 3.

Referring to fig. 1, the CO2 capturing and purifying system 3 includes a water separation tank 301, a compressor unit 302, a surge tank 303, a drying bed 304, an adsorption bed 305, a refrigerator 306 and a rectification tower 307 which are sequentially connected to an outlet pipeline of a sub-ventilator 215, a top gas outlet of the rectification tower 307 is sequentially connected to a condenser 308 and a gas-liquid separator 309, a liquid outlet of the gas-liquid separator 309 is connected to the rectification tower 307, a bottom liquid outlet of the rectification tower 307 is connected to an inlet of a reboiler 310, a gas outlet of the reboiler 310 is connected to the rectification tower 307, and a liquid outlet of the reboiler 310 is connected to a storage tank 2 for liquid CO 2.

The temperature of the low-temperature circulating flue gas g3 is lower than 150 ℃, and the main component of the low-temperature circulating flue gas is CO ₂ ，CO ₂ Concentration (volume fraction) higher than 60%, O ₂ The concentration is lower than 10%; the temperature of the medium-temperature circulating flue gas g2 is lower than 400 ℃, and the main component of the medium-temperature circulating flue gas is CO ₂ ，CO ₂ Concentration higher than 60%, O ₂ The concentration is less than 10%. The fuel used is pulverized coal F, and the fineness is controlled to 80um and the screen residue is lower than 20 percent. The oxidant used for combustion is industrial oxygen g1, and the concentration of industrial oxygen g1 is not less than 80%.

Referring to fig. 3, the flue gas preheating unit is used for preheating low-temperature circulating flue gas g3 and medium-temperature circulating flue gas g2 to above 900 ℃ by using fuel; the flue gas preheating unit comprises a burner 209 and a preheating furnace 208, the burner 209 is installed at the top of the preheating furnace 208, the head of the burner 209 extends into the preheating furnace 208, and the preheating furnace 208 is used for heating medium-temperature circulating flue gas g2 and low-temperature circulating flue gas g 3.

The burner 209 is a cylindrical structure, see fig. 6, and comprises an oil pipe, an inner primary air pipe, a coal pipe and an outer primary air pipe which are coaxially sleeved from inside to outside in sequence, wherein four channels are formed inside, and a central oil gun channel 2091, an inner primary air channel 2093, a coal powder channel 2094 and an outer primary air channel 2095 are respectively arranged from inside to outside. The head ports of the oil pipe, the coal pipe and the outer primary air pipe are aligned to form the head of the burner 209; a distance H0 is reserved between the head of the inner primary air pipe and the head of the burner 209, so that the inner primary air passage 2093 and the coal powder passage 2094 form an air-coal premixing passage 2097 at the head of the burner 209; an air-coal premixing adjusting ring 2098 which can move back and forth along the axial direction of the burner 209 is arranged between the inner primary air channel 2093 and the coal dust channel 2094, so that the length of the air-coal premixing channel 2097 can be adjusted between 0 and H0. The air-coal premixing adjusting ring 2098 of this embodiment is disposed on the inner wall of the inner primary air duct.

Referring to fig. 4 and 5, the preheating furnace 208 is composed of a cyclone chamber 2081, a reducer section 2082 and a hearth 2083 from top to bottom. The swirl chamber 2081 is of a volute structure, so that the flue gas entering from the inlet 20811 of the swirl chamber enters in a volute tangential swirl manner. A burner mounting hole 20813 is arranged in the center of the swirl chamber top cover 20812, the burner 209 is mounted at the top of the preheating furnace 208 through the burner mounting hole 20813, and the head of the burner 209 extends into the swirl chamber 2081. A refractory material layer 2099 is arranged outside the outer primary air channel 2095 of the burner 209 for heat insulation, so as to prevent the flame radiation in the preheating furnace 208 from transferring heat to the burner 209, so that the internal temperature of the burner 209 is overhigh and the industrial oxygen g1 oxidizes wall steel in the conveying process in the burner 209. The circumference of the cross section of the cyclone chamber 2081 is smaller than the circumference of the hearth 2083, and the inner diameter of the reducing section 2082 is gradually increased from top to bottom, so that the circular flue gas cyclone operation can fully cover the circumferential direction of the furnace wall.

Referring to fig. 10 and 11, the bottom outlet of the furnace 2083 is connected to the bottom of the venturi throat 207 through a pipe, and the top of the venturi throat 207 is connected to the bottom of the column of the self-enrichment furnace 206; the raw material feeding pipe 2061 is provided at the bottom of the column of the self-enriching furnace 206. The venturi throat 207 is divided into a lower contraction section 2071, a throat high-speed section 2072 and an upper expansion section 2073 from bottom to top, the lower contraction section 2071 is inserted into the oxygen pipe 2074, the oxygen pipe 2074 is inserted into the axial center of the venturi throat 207 in a downward inclination manner, an included angle between the oxygen pipe 2074 and the horizontal direction is 30-60 degrees, so that the industrial oxygen g1 and the circulating flue gas are uniformly mixed, and the insertion depth of the embodiment is 300-1000 mm; the upper expanding section 2073 is inserted into the coal injection pipe 2075, and the coal injection pipe 2075 is horizontally inserted to be close to the inner wall of the upper expanding section 2073, so that the circulating flue gas and the coal powder are mixed at a vortex low-pressure area formed outside the upper expanding section 2073, and the insertion depth of the embodiment is 100-500 mm; the number of the oxygen pipes 2074 and the number of the coal injection pipes 2075 are 2-4 respectively, and the oxygen pipes and the coal injection pipes are symmetrically arranged along the circumference. In this embodiment, the oxygen pipes 2074 and the coal injection pipes 2075 are all provided with 2 branches, and 4 branches are uniformly distributed in the circumferential direction.

In the total oxygen combustion subsystem 2, the fuel supply pipeline is divided into two paths and is respectively connected with a coal pipe and a coal injection pipe 2075 at the upper part of the venturi throat 207; the low-temperature circulating flue gas supply pipeline is connected with a fuel supply pipeline; the medium-temperature circulating flue gas supply pipeline is connected with an inlet of the cyclone chamber 2081; the industrial oxygen g1 supply pipeline is divided into three paths, which are respectively connected with the outer primary air pipe, the inner primary air pipe and the oxygen pipe 2074 at the lower part of the venturi throat 207, and the industrial oxygen g1 supply pipelines connected with the outer primary air pipe, the inner primary air pipe and the oxygen pipe 2074 at the lower part of the venturi throat 207 are respectively provided with a flow controller. Pulverized coal F is introduced into a fuel supply pipeline, industrial oxygen g1 is introduced into an industrial oxygen g1 supply pipeline, low-temperature circulating flue gas g3 is introduced into a low-temperature circulating flue gas supply pipeline, and medium-temperature circulating flue gas g2 is introduced into a medium-temperature circulating flue gas supply pipeline.

Since the position of the air-coal premixing adjustment ring 2098 can be moved back and forth axially along the burner 209, the length of the air-coal premixing passage 2097 can be adjusted before 0H 0. The distance between the head of the air-coal premixing adjusting ring 2098 and the head of the burner 209 is set to be H, when H is larger than 0, the inner primary air (i.e., the industrial oxygen g1) in the inner primary air passage 2093 and the coal conveying air (i.e., the low-temperature circulating flue gas g3) in the coal powder passage 2094 are premixed into one stream in the air-coal premixing passage 2097 (i.e., a premixing area), and the stream passes through the air-coal premixing passage 2097 and is ejected out of the burner 209. The larger the length of the air-coal premixing passage 2097, the stronger the premixing degree, and the more uniform the contact of the pulverized coal F with the industrial oxygen g 1.

Referring to fig. 6 and 7, when the fuel is a fire-retardant coal (such as anthracite), if there is no air-coal premixing passage 2097, the pulverized coal and the industrial oxygen g1 are independently ejected from the two passages of the burner 209, and the coal air is the low-temperature circulating flue gas g3, which may cause insufficient oxygen supply during the combustion of the pulverized coal, causing flame instability and even flameout. By adjusting the air-coal premixing adjusting ring 2098 additionally arranged between the inner primary air passage 2093 and the coal dust passage 2094, the industrial oxygen g1 and the coal dust F are premixed in the combustor 209, so that the coal dust F can be contacted with the industrial oxygen g1 in advance before being sprayed out, and the ignition and flame stability of the coal can be enhanced. When the inner primary air enters the air-coal premixing passage 2097, the inner primary air is rotational flow, the coal powder passage 2094 is direct flow, and in the air-coal premixing passage 2097, the inner primary air collides with coal conveying air under the action of rotational flow centrifugal force, so that the premixing effect of the industrial oxygen g1 and the coal powder F is improved.

For medium-flammability coal, the length H of the premixing area can be flexibly adjusted by the air-coal premixing adjusting ring 2098, so as to enhance the ignition and flame stability of the coal without tempering.

Referring to fig. 8 and 9, for combustible coal, if the industrial oxygen g1 and the pulverized coal F are premixed in advance in the burner 209, the problem that the flame burns too fast, the flame is tempered to the premixing area, and the head of the burner 209 is burned out exists. At this time, the tempering problem can be solved by adjusting the position of the air-coal premixing adjusting ring 2098, namely, the air-coal premixing adjusting ring 2098 is inserted to a depth to the outlet of the burner 209, so that a premixing area disappears, four channels are arranged at the outlet of the burner 209, the industrial oxygen g1 and the coal powder F are not premixed in the burner 209 and are sprayed out from the respective channels, because the coal powder F and the industrial oxygen g1 are mutually isolated before being sprayed out, the flame cannot be tempered into the channel of the burner 209, the state is a non-premixing mode combustion, the burner is suitable for the coal quality easy to catch fire and burn, and the head of the burner 209 can be prevented from being burnt out.

In addition, the industrial oxygen flow of the inner primary air passage 2093 can be adjusted by the inner primary air flow controller 219, when the coal is inflammable, the industrial oxygen flow of the inner primary air passage 2093 is reduced, the industrial oxygen g1 premixed with the pulverized coal is reduced, the oxygen concentration in the inner primary air outlet is reduced, and the pulverized coal is prevented from explosion and backfire. When the coal is difficult to burn, the flow of the industrial oxygen g1 of the inner primary air channel 2093 is increased, and the flame stability of pulverized coal ignition is enhanced.

Production of cement clinker and CO-production of liquid CO by oxy-fuel combustion ₂ The method adopts a cement calcination main system 1 and a total oxygen combustion subsystem 2 to run in parallel to carry out air combustion and partial total oxygen combustion, and the flow paths of raw materials are in parallel connection without crossing in a preheating pre-decomposition link; in the clinker calcining link, two raw materials decomposed by the cement calcining main system 1 and the oxy-fuel combustion subsystem 2 enter the rotary kiln 108 to be calcined together to prepare cement clinker;

in the oxy-fuel combustion subsystem 2, raw meal is fed to a sub-preheater unit, preheated by the sub-preheater unit and fed to the self-enrichment furnace 206 for pre-decompositionThen enters a rotary kiln 108 for calcination; the flue gas from the enrichment furnace 206 is subjected to heat exchange through a sub-preheater unit under the air draft of a sub-high temperature fan 210, part of the flue gas out of the sub-preheater unit is returned to the preheating furnace 208 as medium-temperature circulating flue gas g2, the rest of the flue gas is cooled by a cooler 213 and dust is collected by a sub-dust collector 214, one part of the flue gas is used as low-temperature circulating flue gas g3, the rest of the flue gas is rich in carbon dioxide and enters a CO2 capturing and purifying system 3 through a sub-exhaust fan 215, and CO is prepared after dehydration, drying, desulfurization, denitrification, condensation and rectification ₂ Liquid CO with mass fraction of more than 99% ₂ And (5) producing the product.

The oxy-fuel combustion subsystem 2 adopts a mode of two times of oxy-fuel combustion in series to carry out pulverized coal combustion and raw material decomposition, and comprises the following specific steps:

the method comprises the following steps: taking low-temperature circulating flue gas g3 from a pipeline of a gas outlet of the sub dust collector 214, wherein the low-temperature circulating flue gas g3 carries pulverized coal F to enter a pulverized coal channel 2094 of the combustor 209; the industrial oxygen g1 is divided into two parts to enter an inner primary air channel 2093 and an outer primary air channel 2095 of the burner 209 respectively, the industrial oxygen g1 of the inner primary air channel 2093 enters in a swirling mode, the industrial oxygen g1 in the outer primary air channel 2095 is ejected in a swirling mode, the supply amount of the industrial oxygen g1 meets the oxygen amount required by combustion of coal dust in the preheating furnace 208, and the coal dust is stably combusted in the preheating furnace 208 after being ejected.

Step two: taking medium-temperature circulating flue gas g2 from a pipeline between the sub high-temperature fan 210 and the cooler 213, introducing the medium-temperature circulating flue gas g2 into a cyclone chamber 2081 of the preheating furnace 208 in a tangential cyclone manner, and making the flue gas move downwards along the wall under the centrifugal force of a top cyclone chamber 2081; the pulverized coal and industrial oxygen g1 are sprayed out from the burner 209 and then ignited and combusted in the preheating furnace 208, so that a fuel-rich area A positioned in the center of the hearth 2083, an oxygen-rich area B positioned outside the fuel-rich area and a carbon-rich area C positioned between the oxygen-rich area and the furnace wall are formed in the space in the preheating furnace 208; the combustion heat of the pulverized coal raises the temperature of the middle-low temperature circulating flue gas to over 900 ℃.

Step three: the high-temperature circulating flue gas which is discharged from the preheating furnace 208 and has the temperature of over 900 ℃ moves upwards in a reverse direction.

Step four: the high-temperature circulating flue gas enters the Venturi throat 207, and industrial oxygen g1 is sprayed into a lower contraction section 2071 at the inlet of the Venturi throat 207, so that the oxygen concentration in the central area is increased to be more than 30%; the pulverized coal is sprayed into the upper expanding section 2073 at the outlet of the venturi throat 207, and the outlet gas forms jet flow, so that a vortex low-pressure area is formed outside the upper expanding section 2073 under the action of the jet flow.

Step five: the coal powder enters the self-enriching furnace 206 along with the circulating flue gas to burn and release heat, raw materials are fed into a raw material feeding pipe 2061 at the bottom of the column of the self-enriching furnace 206, so that the raw materials are decomposed in the self-enriching furnace 206, and CO is released ₂ Self-enriched furnace 206 flue gas dry basis CO ₂ The concentration is more than 80 percent, and the temperature is 850-1000 ℃.

In the whole cement burning process, cement raw materials are divided into 2 parts, the 1 st part is fed into a main preheater unit of a main cement burning system 1, enters a main decomposing furnace 106 for decomposition after being preheated, and then enters a rotary kiln 108 for burning; the 2 nd part is fed into a sub-preheater unit of the oxy-fuel combustion subsystem 2, is preheated and then fed into a self-enrichment furnace 206 for decomposition, and then enters a rotary kiln 108 for calcination. The coal powder is divided into 3 parts, the 1 st part is fed into a rotary kiln 108 through a kiln head burner 110 and is used for calcining cement clinker; part 2 is fed to the main decomposition furnace 106 for raw meal decomposition; the part 3 is divided into 2 groups, one group is fed into a flue gas preheating unit of the total oxygen combustion subsystem 2 and is used for circulating flue gas to heat; the other group is fed to the self-enrichment furnace 206 of the oxy-fuel combustion subsystem 2 for raw meal decomposition.

In oxy-fuel combustion subsystem 2, a central oil gun passage 2091 in the center of burner 209 is used for ignition of preheat furnace 208. The two

primary air passages

2093 and 2095 feed industrial oxygen g1 in an amount to meet the oxygen demand for combustion of the pulverized coal in preheat furnace 208. An inner primary air cyclone 2092 is arranged at the inlet of the inner primary air channel 2093, so that the industrial oxygen g1 entering the inlet of the inner primary air channel 2093 flows downwards in a rotating way under the action of the inner primary air cyclone 2092; the outer primary air passage 2095 is located outside the pulverized coal passage 2094, and an outer primary air cyclone 2096 is arranged at an outlet of the outer primary air passage 2095, so that the industrial oxygen g1 in the outer primary air passage 2095 is sprayed out in a high-speed rotational flow mode under the action of the outer primary air cyclone 2096, and the stability of flame in the preheating furnace 208 can be enhanced.

And taking air from an outlet pipeline of the sub-high temperature fan 210, wherein 150-400 ℃ medium temperature circulating flue gas g2 enters from an inlet 20811 of the cyclone chamber and flows downwards along the wall surface in a rotating manner. Because the industrial oxygen g1 is used as an oxidant, the oxygen content is increased relatively to air, the corresponding flame temperature is relatively high, the high-temperature zone can reach more than 1300 ℃, and when the flame contacts the side wall of the preheating furnace 208, the burning loss of the refractory material on the furnace wall surface is easily caused. The medium-temperature circulating flue gas g2 enters the preheating furnace 208 in a swirling manner, and due to the relatively low temperature and low oxygen content, a low-temperature protective gas film is formed in front of the furnace wall and the flame, so that the wall surface refractory material of the preheating furnace 208 is effectively protected from being ablated by the flame.

Taking air from the sub-dust collector 214, taking low-temperature circulating flue gas g3 with the temperature below 150 ℃ as air for conveying pulverized coal, and circulating flue gas CO at low temperature ₂ The concentration is not lower than 60%, and the coal powder is fed into a coal powder channel 2094 of the burner 209 through low-temperature circulating flue gas g 3; the industrial oxygen g1 is divided into two parts to enter the burner 209, wherein one part of the industrial oxygen g1 enters the inner primary air channel 2093 of the burner 209 in a swirling manner, the flow rate of the industrial oxygen is controlled by the inner primary air flow controller 219, the other part of the industrial oxygen g1 enters the outer primary air channel 2095 of the burner 209 in a swirling manner, the flow rate of the industrial oxygen is controlled by the outer primary air flow controller 220, the supply amount of the industrial oxygen g1 meets the oxygen amount required by the combustion of the pulverized coal in the preheating furnace 208, and the combustion of the pulverized coal in the preheating furnace 208 is stable after the pulverized coal is sprayed out; the medium-temperature circulating flue gas g2 tangentially enters from a cyclone chamber inlet 20811 of the preheating furnace 208 in a cyclone manner and moves downwards along the wall under the centrifugal force of a top cyclone chamber 2081; a fuel-rich area A positioned in the center of the hearth 2083, an oxygen-rich area B positioned outside the fuel-rich area and a carbon-rich area C positioned between the oxygen-rich area and the furnace wall are formed in the space in the preheating furnace 208; the pulverized coal F and industrial oxygen g1 (oxygen concentration is not less than 80%) are sprayed out from the burner 209 and then ignited and combusted in the preheating furnace 208, the pulverized coal combustion heat enables the flue gas out of the preheating furnace 208 to flow out from the bottom of the preheating furnace 208 through regulating and controlling the coal feeding amount, the temperature is above 900 ℃, and CO in the flue gas is CO ₂ The concentration is more than 60%. The advantages of the air supply mode are as follows: 1) the coal powder F and the industrial oxygen g1 are not mixed in the conveying process, and the coal powder is conveyed by low-temperature circulating flue gas g3, so that the problem is solvedThe safety problem of spontaneous combustion caused by mixed transportation of the industrial oxygen g1 and the coal powder F in the oxy-fuel combustion subsystem 2 is solved; 2) the medium-temperature circulating flue gas g2 directly enters the preheating furnace 208 and moves downwards along the wall, so that the gas film is protected before the pulverized coal combustion flame and the wall, and the wall can be prevented from being burnt by the high-temperature flame.

The air supply mode of the flue gas preheating unit provided by the invention is as follows: the low-temperature circulating flue gas g3 is used as coal conveying air for conveying coal powder; the medium-temperature circulating flue gas g2 is supplied with air from a cyclone chamber 2081 of the preheating furnace 208; two industrial oxygen g1 are used as inner primary air to supply air at the inner side of the coal powder channel 2094, whether the two industrial oxygen g1 are premixed with the coal powder in advance is determined according to the combustion characteristics of the coal powder, and the two industrial oxygen g1 are ejected out at the outer side of the coal powder channel 2094 in a high-speed rotational flow mode to be used as outer primary air. So that three zones, namely a fuel-rich zone a, can be established in the space in preheating furnace 208, and located in the center of furnace 2083; the oxygen-enriched area B is positioned outside the fuel-enriched area; and the carbon-rich area C is positioned between the fuel-rich area and the furnace wall. The advantages of the zone combustion method are as follows: 1. the peroxide coefficient in the fuel-rich area is less than 1, and the fuel-rich area is a reducing atmosphere and can inhibit the generation of NOx; 2. the carbon-rich region is mainly CO ₂ And the gas temperature is relatively low, so that the furnace wall surface can be protected, and flame can be prevented from burning the furnace wall.

The high-temperature circulating flue gas out of the preheating furnace 208 passes through the pipeline and then moves vertically upwards, enters the venturi throat 207, industrial oxygen g1 is sprayed into a lower contraction section 2071 at the inlet of the venturi throat 207, so that the oxygen concentration of a central area is increased to be above 30%, the average wind speed of the cross section of a throat high-speed section 2072 is 25-50 m/s, the average wind speed of the cross section of an outlet of an upper expansion section 2073 is 5-15 m/s, and the wind speed of the throat high-speed section 2072 is more than 2 times of that of the outlet of the upper expansion section 2073. The high temperature circulating flue gas continues to move upwards, the gas at the outlet of the venturi throat 207 forms jet flow, the coal powder is sprayed into the upper expansion section 2073 through the coal spraying pipe 2075, a vortex low-pressure area is formed outside the upper expansion section 2073 under the action of the jet flow, the circulating flue gas and the coal powder are back mixed in the area, the oxygen concentration of the circulating flue gas at the outer side is relatively low, and NO is inhibited from being burnt by the coal powder _X And (4) releasing.

The pulverized coal injected from the coal injection pipe 2075 moves upward along with the circulating flue gas and is combusted in the self-enrichment furnace 206 as secondary combustion. Raw material is fed from the bottom of the column of the self-enrichment furnace 206The raw material feed pipe 2061 is positioned above the coal injection pipe 2075. The full decomposition of raw meal is realized in the self-enrichment furnace 206, and CO is released ₂ The temperature of the flue gas from the enrichment furnace 206 is 850-1000 ℃, and the dry-based CO of the flue gas from the enrichment furnace 206 ₂ The concentration is more than 80%.

The flue gas from the enrichment furnace 206 is subjected to heat exchange through a sub-preheater unit under the air draft of a sub-high temperature fan 210, and part of the flue gas is returned to the preheating furnace 208 as medium-temperature circulating flue gas g 2; after the residual flue gas is cooled by the cooler 213 and dust is collected, one part of the residual flue gas is used as low-temperature circulating flue gas g3, and the rest part of the residual flue gas is rich in CO ₂ The flue gas enters a CO2 capturing and purifying system 3 for purification.

The critical temperature of the carbon dioxide is 31.4 ℃, the critical pressure is 7.28MPa, and the normal-pressure boiling point is-78.4 ℃. Rich in CO ₂ The impurities in the flue gas mainly comprise N ₂ 、O ₂ 、CO、H ₂ O、SO _X 、NO _X And the like. Among them, heavy component impurities having high boiling points, e.g. H ₂ O、SO _X 、NO _X And the like, can be dissolved in liquid carbon dioxide during liquefaction and separation, and needs to be removed before liquefaction and rectification. The carbon dioxide rich flue gas entering the CO2 capturing and purifying system 3 contains N ₂ 、O ₂ 、SO _X 、NO _X And the components such as water vapor and the like need to be removed.

In this example, it is rich in CO ₂ The flue gas is firstly subjected to preliminary dehydration through a water separation tank 301, the flue gas after water separation enters a compressor unit 302 for pressurization, the flue gas after water separation enters a drying bed 304 for dehydration and drying after passing through a pressure stabilizing tank 303, and the flue gas after drying enters an adsorption bed 305 for removing SO _X And NO _X Impurities. The adsorbent bed 305 is loaded with an adsorbent, the loading amount of the adsorbent is different according to the amount of impurities in the flue gas, and different adsorbents are separated by a screen. When the flue gas passes through the adsorption bed 305, the impurities are absorbed by the adsorbent, and when the adsorption amount reaches saturation, the adsorbent needs to be regenerated. The number of the adsorption beds 305 is 2 or more, and when one adsorption bed 305 is in an adsorption operation state, the other adsorption bed 305 is in a regeneration state, so that the continuous production process can be ensured.

The carbon dioxide rich flue gas exiting the adsorption bed 305 enters refrigerationThe machine 306 is used for refrigerating, the refrigerating machine 306 is a screw type or piston type refrigerating machine driven by a motor, and the refrigerant is liquid ammonia or Freon. The flue gas is cooled and condensed from a gaseous state to a liquid state, and enters the rectifying tower 307. The rectifying tower 307 is a packed tower, which is filled with corrugated plates or wire mesh to carry packing. Since the boiling point of the light component impurity is lower than that of carbon dioxide, the light component impurity N ₂ 、O ₂ CO, a small amount of carbon dioxide and the like are separated out at the top of the rectifying tower 307, the separated mixed gas is processed by the condenser 308 to condense the carbon dioxide into liquid again, the liquid carbon dioxide returns to the rectifying tower 307 after passing through the gas-liquid separator 309, and the rest gas is the vent gas g5 of the rectifying tower and is discharged out of the system. The bottom of the rectifying tower 307 is provided with a reboiler 310, the reboiler 310 drives out impurities dissolved in carbon dioxide by heating, gas-liquid mass transfer is carried out through a packing layer in the tower, light component impurities are gradually concentrated on the top of the tower and are continuously discharged out of the tower. The liquid carbon dioxide from the reboiler 310 is transported to a liquid CO2 storage tank 311 through a pipeline, and the purity is more than 99%.

In conclusion, the main system 1 and the total oxygen combustion subsystem 2 for air combustion and local total oxygen combustion are operated in parallel, and the main system and the subsystems are operated in parallel in a preheating and predecomposition link at the tail of a firing kiln; in the rotary kiln, the calcined raw materials generated by the main system and the subsystem are simultaneously fed into the kiln to produce cement clinker; mutual interference between the main system and the subsystems, such as mutual wind channeling, pressure fluctuation interference and the like, is reduced. Secondly, when partial total oxygen combustion is carried out, the total oxygen combustion subsystem 2 divides raw materials into a primary combustion area and a secondary combustion area which are connected in series for operation, coal powder is conveyed through low-temperature circulating flue gas, raw materials are not fed into the primary combustion area, industrial oxygen is divided into two parts to supply air to the inner side and the outer side of a coal powder channel, medium-temperature circulating flue gas is fed into a preheating furnace from an inlet of a cyclone chamber of the preheating furnace, the medium-temperature and low-temperature circulating flue gas is heated to more than 900 ℃ in the preheating furnace, the flame stability of the coal powder in the preheating furnace is realized, the furnace wall of the preheating furnace is not ablated, and low NO is realized _X The problems of difficult ignition of fuel, unstable flame and easy flameout in the combustion process when the medium-low temperature circulating flue gas is directly connected into the decomposing furnace can be solved, and the safety problem of spontaneous combustion and ignition caused by mixed transportation is avoidedTitle to be obtained; the secondary combustion zone is operated by material feeding, high-temperature circulating flue gas is introduced into the secondary combustion zone, industrial oxygen and coal powder are sprayed into the secondary combustion zone to decompose raw materials, and the material is supported by the venturi throat jet flow, so that the problem of furnace wall high-temperature skinning caused by raw material collapse and local deflagration of the coal powder is solved, NO in the combustion of the coal powder is inhibited _X Releasing; the temperature of the flue gas of the self-enrichment furnace is 850-1000 ℃, and the dry basis CO is ₂ The concentration is more than 80 percent, and the full decomposition of the raw material is realized. And thirdly, when local oxy-fuel combustion is carried out, circulating air is taken from the oxy-fuel combustion subsystem 2 in a grading mode, medium-temperature circulating air (150-400 ℃) is taken from a position between the sub high-temperature fan and the cooler and directly enters the preheating furnace, and low-temperature circulating air (lower than 150 ℃) is taken from a position behind the sub dust collector and used as pulverized coal conveying air, so that the heat recovery is improved, the energy consumption is reduced, and the carbon enrichment is realized while the safety of pulverized coal conveying is ensured. Finally, rich in CO ₂ The flue gas simultaneously enters a CO2 capturing and purifying system 3, and CO is prepared after dehydration, drying, desulfurization, denitrification and condensation and rectification ₂ Liquid CO with mass fraction of more than 99% ₂ The product realizes carbon emission reduction in the cement production process and the low-cost on-line preparation of liquid CO ₂ The product has good social and economic benefits.

Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. Production of cement clinker and CO-production of liquid CO by oxy-fuel combustion ₂ The system is characterized by comprising a cement calcination main system, a oxy-fuel combustion sub-system and CO ₂ A trapping and purifying system;

the CO is ₂ The trapping purification system comprises a water distribution tank, a drying bed, an adsorption bed, a refrigerator and a rectifying tower which are sequentially connected and arranged on an outlet pipeline of the sub-exhaust fan, wherein a top gas outlet of the rectifying tower is sequentially connected with a condenser and a gas-liquid separator, a liquid outlet of the gas-liquid separator is connected with the rectifying tower, a bottom liquid outlet of the rectifying tower is connected with an inlet of a reboiler, a gas outlet of the reboiler is connected with the rectifying tower, and the reboiler isWith liquid CO ₂ The storage tank is connected.

2. The oxy-fuel combustion of claim 1 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that the flue gas preheating unit comprises a burner and a preheating furnace, the burner is arranged at the top of the preheating furnace, the head of the burner extends into the preheating furnace, the burner comprises an oil pipe, an inner primary air pipe, a coal pipe and an outer primary air pipe which are coaxially sleeved from inside to outside in sequence, so that a central oil gun channel, an inner primary air channel, a coal powder channel and an outer primary air channel are formed in the burner from inside to outside in sequence; the tail parts of the inner primary air pipe and the outer primary air pipe are both connected with an industrial oxygen supply pipeline, and the tail part of the coal pipe is connected with a fuel supply pipeline;

3. The oxy-fuel combustion of claim 2 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that the air-coal premixing adjusting ring is arranged on the inner side wall of the inner primary air pipe.

4. The oxy-fuel combustion of claim 2 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that the inlet of the inner primary air channel and the outlet of the outer primary air channel are both provided with a swirler; and a refractory material layer is arranged outside the outer primary air channel.

5. The oxy-fuel combustion of claim 2 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that flow controllers are respectively arranged on the industrial oxygen supply pipelines connected with the oxygen pipes at the lower parts of the inner primary air pipe, the outer primary air pipe and the venturi throat.

6. The oxy-fuel combustion of claim 2 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that a burner mounting hole is formed in the center of a top cover of the cyclone chamber, and the head of the burner extends into the cyclone chamber through the burner mounting hole; the inner diameter of the reducing section is gradually increased from top to bottom.

7. The oxy-fuel combustion of claim 1 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that a medium-temperature circulating air valve is arranged on a medium-temperature circulating flue gas supply pipeline at an inlet of the medium-temperature circulating fan, and a low-temperature circulating air valve is arranged on a low-temperature circulating flue gas supply pipeline at an inlet of the low-temperature circulating fan.

8. Oxy-fuel combustion as claimed in claim 1Production of cement clinker with CO-production of liquid CO ₂ The system is characterized in that the venturi throat pipe is divided into a lower contraction section, a throat area high-speed section and an upper expansion section from bottom to top, the lower contraction section is inserted into the oxygen pipe, the oxygen pipe is inserted into the position close to the axial center of the venturi throat pipe in a downward inclination manner, and an included angle between the oxygen pipe and the horizontal direction is 30-60 degrees, so that industrial oxygen and circulating flue gas are uniformly mixed; the coal injection pipe is inserted into the upper expansion section and is inserted to be close to the inner wall of the upper expansion section, so that circulating flue gas and coal powder are mixed at a vortex low-pressure area formed outside the upper expansion section; the number of the oxygen pipes and the number of the coal injection pipes are respectively 2-4, and the oxygen pipes and the coal injection pipes are symmetrically arranged along the circumference.

9. The oxy-fuel combustion of claim 1 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that the raw material feeding pipe is arranged at the bottom of the column body of the self-enriching furnace.

10. The oxy-fuel combustion of claim 1 for the CO-production of cement clinker with liquid CO ₂ The system is characterized in that a compressor set and a surge tank are sequentially arranged on a pipeline between the outlet of the water diversion tank and the inlet of the drying bed.

11. Production of cement clinker with CO-production of liquid CO by oxy-fuel combustion based on the system of any one of claims 1 to 10 ₂ The method is characterized in that a cement calcination main system and a total oxygen combustion sub-system are operated in parallel to carry out air combustion and local total oxygen combustion, and in a preheating pre-decomposition link, the flow paths of raw materials are connected in parallel without crossing; in the clinker calcining link, two raw materials decomposed by a cement calcining main system and a total oxygen combustion subsystem enter a rotary kiln to be calcined together to prepare cement clinker;

in the oxy-fuel combustion subsystem, raw materials are fed into a sub-preheater unit, preheated by the sub-preheater unit, fed into a self-enrichment furnace for predecomposition, and then fed into a rotary kiln for calcination; the smoke from the enrichment furnace is subjected to heat exchange through the sub-preheater unit under the air draft of the sub-high temperature fan, and part of the smoke is subjected to heat exchange through the sub-preheater unitThe flue gas is used as medium-temperature circulating flue gas and returns to the preheating furnace; after the residual flue gas is cooled and dust-collected, one part of the residual flue gas is used as low-temperature circulating flue gas, and the rest part of the residual flue gas is rich in CO ₂ Flue gas enters CO ₂ The gathering and purifying system is used for preparing CO after dehydration, drying, desulfurization, denitrification and condensation rectification ₂ Liquid CO with mass fraction of more than 99% ₂ And (5) producing the product.

12. The oxy-fuel combustion of claim 11 for CO-production of cement clinker with liquid CO ₂ The method is characterized in that the pre-decomposed raw material in the self-enrichment furnace is decomposed by adopting a mode of twice total oxygen combustion carbon enrichment, and the specific steps are as follows:

13. Oxy-fuel combustion cement clinker CO-production of liquid CO according to claim 11 or 12 ₂ The method is characterized in that the fineness of the coal dust is controlled to be 80um, and the screen residue is lower than 20 percent; the oxygen concentration of the industrial oxygen is not lower than 80%; the temperature of the low-temperature circulating flue gas is lower than 150 ℃, and CO is ₂ Concentration higher than 60%, O ₂ The concentration is lower than 10%; the temperature of the medium-temperature circulating flue gas is lower than 400 ℃, and CO is ₂ Concentration higher than 60%, O ₂ The concentration is less than 10%.

14. Oxy-fuel combustion cement clinker CO-production of liquid CO according to claim 12 ₂ The method is characterized in that according to the combustion characteristics of the coal dust, the length of the air-coal premixing channel is adjusted by adjusting the air-coal premixing adjusting ring, and/or the ignition and flame stability of the coal dust are enhanced by adjusting the amount of industrial oxygen entering the inner primary air channel and the outer primary air channel, so that the coal dust is stably combusted in the preheating furnace after being sprayed out.

15. Oxy-fuel combustion cement clinker CO-production of liquid CO according to claim 12 ₂ The method is characterized in that in the third step, the average wind speed of the section of the throat area high-speed section of the Venturi throat pipe is 25-50 m/s, the average wind speed of the outlet section of the upper expansion section is 5-15 m/s, and the wind speed of the throat area high-speed section is more than 2 times of the wind speed of the outlet of the upper expansion section.

16. The oxy-fuel combustion of claim 11 for CO-production of cement clinker with liquid CO ₂ Characterized in that liquid CO is produced ₂ The process of the product is as follows: rich in CO ₂ The flue gas is primarily dehydrated through a water distribution tank, the dehydrated flue gas enters a compressor unit for pressurization, and the dehydrated flue gas enters a drying bed for dehydration and drying after passing through a pressure stabilizing tank; the dried flue gas enters an adsorption bed to remove SO _X And NO _X Impurities; the carbon dioxide-rich flue gas out of the adsorption bed enters a refrigerator for refrigeration and then enters a rectifying tower; in the rectifying tower, light component impurities and a small amount of carbon dioxide are separated out at the top of the rectifying tower, the separated mixed gas is treated by a condenser to condense the carbon dioxide into liquid again, the liquid carbon dioxide returns to the rectifying tower after passing through a gas-liquid separator, and the rest gas is discharged out of the system; the liquid carbon dioxide at the bottom of the rectifying tower enters a reboiler, impurities dissolved in the carbon dioxide are returned to the rectifying tower, and the liquid carbon dioxide discharged from the reboiler is conveyed to the liquid CO ₂ And (4) storage tank.