Cement manufacturing plant with thermal energy recovery function

Abstract

A plant (100, 200, 300, 400) for producing cement clinker from raw materials, comprising at least one heat exchanger (110, 210, 310, 410) located downstream in the direction of gas flow, and at least one device (120, 220, 320, 420) for preheating, firing and sintering raw materials that follow in the direction of material flow, wherein the device can consist of a plurality of individual and continuous devices, and at least one device for preheating, firing and sintering raw materials is connected to the at least one heat exchanger located downstream in the direction of gas flow on the primary side and supplied with exhaust gas. [Solution] The secondary side of at least one of the heat exchangers (110, 210, 310, 410) located downstream of the gas flow is connected to a downstream system for separating and / or storing carbon dioxide (CO2) from the exhaust gas. A raw material preheater is not required, the system can operate with a fuel surplus, and as a result the exhaust gas from the system has enough heat to operate a combined process for separating and / or storing carbon dioxide.

Description

TECHNICAL FIELD

[0001] The present invention relates to a plant for producing cement clinker from raw meal, which plant comprises at least one heat exchanger located downstream in the gas flow direction, and at least one apparatus for preheating, calcining and sintering the raw material that follows in the raw material flow direction, this apparatus can be constituted by a separate apparatus or successive separate apparatuses, and at least one of the apparatuses for preheating, calcining and sintering the above raw material is connected on the primary side to at least one heat exchanger located downstream in the direction of the gas flow, and is supplied with exhaust gas.

BACKGROUND ART

[0002] To produce cement clinker from raw material powder made from crushed lime and silicate-containing rock, the raw material powder undergoes several consecutive heat treatment stages. In the first stage, the raw material powder is preheated using waste heat from subsequent heat treatment processes. Next, the preheated raw material powder is deoxidized or calcined to remove carbon dioxide (CO2) from carbonate (CO3) in the calcareous raw material powder. Finally, the deoxidized or calcined raw material powder is sintered in a rotary kiln by a solid-phase reaction to produce cement clinker. After sintering, rapid cooling is performed. This is to prevent the desired clinker phase in the cement clinker from changing to other phases during cooling. The entire manufacturing process is continuously optimized to retain waste heat within the process. The desired goal is to supply only an amount of heat to the entire manufacturing process that corresponds to the enthalpy required to produce cement clinker from the raw material powder. The motivation behind the optimization of this process, which has been carried out over the past several decades, has always been to minimize the heat demand arising from economically expensive fuels. Subsequent optimization of the manufacturing process involves denitrification of exhaust gases, i.e., avoiding nitrogen oxides (NOx) in the exhaust gases. NOx is recognized as a cause of acid rain, which is observed globally. An optimization step that is an innovation challenge in the cement clinker manufacturing process is avoiding the emission of carbon dioxide (CO2) from raw materials. CO2 emissions associated with cement clinker manufacturing, along with CO2 from the combustion of fossil fuels, account for a large portion of anthropogenic carbon dioxide emissions. CO2 is considered one of the causes of global warming that is currently observed. Methods of recovering and storing carbon dioxide (CO2) from industrial exhaust gases are highly endothermic processes. This means that energy is consumed in both recovery and storage, whether by compression and storage in underground aquifers or by chemical conversion of carbon dioxide (CO2) into non-gaseous substances in a complex process. If this energy is used to generate heat or electricity in further combustion processes, further carbon dioxide (CO2) is emitted, which also needs to be recovered.Current cement clinker manufacturing processes and corresponding plants are largely optimized for energy efficiency, making it impossible to generate the required amount of heat and electricity from such plants. Existing cement clinker manufacturing plants and processes emit more carbon dioxide than can be recovered with the waste heat available to operate so-called "recovery processes," i.e., downstream separation processes designed to reduce carbon dioxide (CO2) emissions.

[0003] One solution to obtain heat as energy for the recovery process is to increase the fuel input in existing cement clinker manufacturing plants and related processes, thereby generating more waste heat. However, this additional fuel input raises the plant temperature and significantly alters the energy balance. As a result, the optimizations previously achieved for the denitrification reaction are overturned, and the balance of the production process is disrupted at many points within the plant. With the increase in energy input, the desired clinker phase composition changes, and the efficiency of the denitrification reaction decreases, resulting in a decline in the quality of the resulting cement clinker. [Overview of the project] [Problems that the invention aims to solve]

[0004] The object of the present invention is to propose a cement clinker manufacturing plant and related processes with an energy balance that makes available waste heat available for downstream recovery processes for separating and storing carbon dioxide (CO2) from the plant's exhaust gases. [Means for solving the problem]

[0005] The above-mentioned problems of the present invention are solved by the system described in claim 1 and the corresponding method described in claim 6. Further advantageous embodiments of the system are provided in the dependent claims of claim 1. Further advantageous embodiments of the method are provided in the dependent claims of claim 6.

[0006] The plant and corresponding process described in this invention are based on eliminating the need to separately preheat raw materials in a cement clinker manufacturing plant. In conventional cement clinker manufacturing plants, the heat contained in the exhaust gas of the calcination and sintering equipment is transferred to the cold raw materials in a separate dedicated device, namely a preheater. As a result, the exhaust gas is cooled considerably, and the temperature of the raw materials becomes slightly lower than the decomposition temperature of limestone (CaCO3). This energy recovery allows firing and sintering equipment (whether composed of separate plant elements such as circulating fluidized bed reactors, tubular reactors, or firing furnaces and rotary kilns, or a single plant element such as a long rotary kiln or pot firing furnace) to operate with significantly less fuel because the raw materials enter the reactor already preheated. The objective of the present invention is not to keep the exhaust gas temperature low as in the prior art, but to raise the exhaust gas temperature to a level that can operate a linked system for separating and / or storing carbon dioxide (CO2) using the heat contained in the exhaust gas. The objective of the present invention is not to operate the plant and corresponding processes in an energy-efficient manner with respect to cement clinker emissions, but to operate the method for separating cement clinker emissions and carbon dioxide (CO2) with high energy efficiency. The present invention does not rule out the possibility of using the recovered waste heat after carbon dioxide (CO2) recovery to compress and store or chemically convert it into other substances. Methanol can be used as a conversion material and can also be chemically converted into a solid.

[0007] In this invention, at least one heat exchanger located downstream in the direction of gas flow is connected on the secondary side to a downstream system for separating and / or storing carbon dioxide (CO2) from the exhaust gas. The specific coupling process used in this invention is of secondary importance. Examples of coupling processes include cleaning the exhaust gas using an amine scrubber and storing the separated carbon dioxide (CO2), or producing methanol (CH3OH) from hydrogen (H2) and carbon dioxide (CO2) obtained by electrolyzing water (H2O) using an electric current generated by steam. The steam mentioned above is generated using the heat of the exhaust gas from a cement clinker manufacturing plant. In this concept, "storage" includes both storage where a substance is left in a storage location and storage where a substance is chemically converted into another substance and stored for use in other applications as needed.

[0008] In this invention, more heat is generated by adjusting the fuel supply to at least one apparatus for preheating, firing, and sintering, primarily by burning secondary fuel. The excess heat can be consumed by the separation and / or storage of carbon dioxide (CO2), so that no residual energy remains.

[0009] A key feature of this invention is that it enables the increase in fuel input during cement clinker production, particularly when burning low-calorie or low-quality fuels, in a cost-effective manner with relatively low emissions. Examples of low-calorie and low-quality fuels include processed industrial waste, household waste, used tires, solvent waste, and processed biomass. If energy is generated separately to recover and / or store carbon dioxide (CO2) produced during cement clinker production, the cost of air pollution control technology becomes very high if that energy is also generated using low-calorie or low-quality fuels. In cement clinker production plants, cement clinker is burned in the presence of raw material powders. These raw material powders have a strong catalytic effect on the decomposition of nitrogen oxides (NOx), volatile organic compounds (VOCs), and hazardous air pollutants (HAPs). It is also possible to use fuels that tend to produce furans and dioxins during combustion. Such fuels include polyvinyl chloride (PVC) waste, halogenated solvents, and other halogenated hydrocarbons. Conventional cement clinker manufacturing plants generally already incorporate denitrification technologies and technologies to prevent the emission of dioxins and furans. Non-volatile combustion residues, such as solid combustion residues containing heavy metals and pollutants, can be adsorbed onto the cement clinker and incorporated into it, or the cement clinker can contain these pollutants, preventing their release into the environment with exhaust gases.

[0010] Cement clinker manufacturing plants are equipped with advanced technologies to avoid emissions. However, to safely control and neutralize the increased emissions resulting from excessive fuel use, it has proven advantageous to place a regenerative thermal oxidation (RTO) reactor for pollutants, which oxidizes volatile organic compounds and harmful air pollutants, between a heat exchanger connected to the secondary side of a downstream system for separating and / or storing carbon dioxide (CO2) and the equipment for preheating, firing, and sintering the raw material powder. It has also been found that, in order to operate the regenerative thermal oxidation reactor for pollutants, it is advantageous to adjust the fuel input in the cement clinker manufacturing plant according to the exhaust gas temperature at the point where the exhaust gas flows into the regenerative thermal oxidation reactor for pollutants. This temperature needs to be 800°C to 900°C, preferably around 850°C (with a tolerance of 20°C).

[0011] Conventional calcination furnaces, which are installed as fluidized bed reactors between a raw material preheating device and a rotary kiln, are designed to handle preheated raw material powders and are therefore generally unsuitable when using unheated raw material powders. The residence time of cold raw material powders in this type of calcination furnace is insufficient to heat the raw material powders and then deoxidize (calcinate) them. In this case, it has proven advantageous to use tubular reactors, longer rotary kilns, or circulating fluidized bed reactors as equipment for preheating, calcination, and sintering. The residence time of raw material powders in tubular reactors is significantly longer than in fluidized bed reactors used as calcination furnaces in general use today. Rotary kilns can be used for preheating, calcination, and sintering. In the very early cement clinker manufacturing plants, longer rotary kilns were used to perform these three steps. The disadvantage of long rotary kilns is that the exhaust gas temperature is relatively high, resulting in heat loss. However, in the plants and processes described in this invention, it is precisely the purpose to maintain a high exhaust gas temperature and utilize that heat in the co-process.

[0012] Depending on the rotary kiln's operating mode, it may be advantageous to install the tubular reactor downstream of the rotary kiln in terms of gas flow. When operating with an excess air supply (λ>1), the exhaust gas from the rotary kiln can be directly supplied to the regenerative thermal oxidation reactor for pollutants. On the other hand, when operating with an insufficient air supply (λ<1), it is recommended to supply the exhaust gas from the rotary kiln as a low-grade gas to the tubular reactor and react the fuel gas or pyrolysis gas remaining in the gas head.

[0013] As mentioned earlier, a secondary system for capturing and / or storing carbon dioxide (CO2) can generate electricity using a steam generator. This electricity is supplied to a water electrolyzer connected to a reformer on the hydrogen (H2) side. In the reformer, the exhaust gas containing carbon dioxide (CO2) cooled in the heat exchanger is converted to methanol (CH3OH).

[0014] The present invention will be described in more detail with reference to the following drawings. [Brief explanation of the drawing]

[0015] [Figure 1] A diagram showing a first embodiment of a cement clinker manufacturing plant according to the present invention. [Figure 2] A diagram showing a second embodiment of the cement clinker manufacturing plant according to the present invention. [Figure 3] A diagram showing a third embodiment of the cement clinker manufacturing plant according to the present invention. [Figure 4] A diagram showing a fourth embodiment of the cement clinker manufacturing plant according to the present invention. [Figure 5] A diagram showing a fifth embodiment of the cement clinker manufacturing plant according to the present invention. [Figure 6] A diagram showing a sixth embodiment of the cement clinker manufacturing plant according to the present invention. [Modes for carrying out the invention]

[0016] Figure 1 is a schematic diagram showing a first embodiment of a cement clinker manufacturing plant 100 according to the present invention. Viewed with respect to the direction of gas flow, this first embodiment includes a heat exchanger 110 that transfers heat from the exhaust gas of the plant 100 to a coupling process for the separation and / or storage of carbon dioxide (CO2), and an RTO reactor 130 that performs regenerative thermal oxidation of volatile organic compounds (VOCs) and conversion of hazardous air pollutants (HAPs) in the exhaust gas of the plant 100. Following this, a circulating fluidized bed reactor 140 is provided as an apparatus 120 for producing cement clinker by preheating, firing, and sintering the raw materials. All three steps of preheating, firing, and sintering are carried out within this circulating fluidized bed reactor 140.

[0017] Primary and / or secondary fuels are introduced into the circulating fluidized bed reactor 140 to heat the circulating fluidized bed. The circulating fluidized bed can flow toward the RTO reactor 130 in the direction of the exhaust gas flow, and solids separated from the circulating fluidized bed are separated by cyclone 141 and returned to the circulating fluidized bed reactor 140. The sintering raw material powder for cement clinker falls from the circulating fluidized bed of the circulating fluidized bed reactor 140 into a lower line 142, and the hot cement clinker is sent from there to the clinker cooler 150, where it is rapidly cooled by atmospheric cooling air. The hot cooling air from the clinker cooler 150 is returned to the circulating fluidized bed reactor 140 via a tertiary air line 151.

[0018] This allows heat within the cement clinker to be recovered and fed back into the process. An optional heat exchanger 111, shown in the tertiary air line 151, transfers heat from high-temperature cooling air to a secondary system 1000 for carbon dioxide (CO2) separation and / or storage, where the heat obtained is used as process heat to support carbon dioxide (CO2) separation and / or storage. In this invention, the fuel / air supply to the circulating fluidized bed reactor 140 can be delivered to the regenerative thermal oxidation reactor 140 based on the exhaust gas temperature upstream of the RTO reactor 130, which is 800°C to 900°C, preferably 850°C (tolerance 20°C). The available heat Q in the exhaust gas of the system that can be transferred by the heat exchanger 110 is sufficient heat to remove carbon dioxide (CO2) from the exhaust gas by the system for separating and / or storing carbon dioxide (CO2) from the exhaust gas, which is located in the secondary circuit of the heat exchanger 110. The heat Q extracted from the exhaust gas of plant 100 is used in the coupling process of plant 1000 for the separation and / or storage of carbon dioxide (CO2). In this case, the separation and / or storage also includes the production of methanol in a reformer and chemical conversion to other chemicals.

[0019] Figure 2 shows a second embodiment of the cement clinker manufacturing plant 200 according to the present invention. Viewed with respect to the direction of gas flow, this second embodiment has a heat exchanger 210 that transfers heat from the exhaust gas of the plant 200 to a coupling process for the separation and / or storage of carbon dioxide (CO2), and an RTO reactor 230 that performs regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas of the plant 200 and conversion of hazardous air pollutants (HAPs). Following this is a dust collector 252, which returns dust from the exhaust gas of the subsequent rotary kiln 240 to the rotary kiln inlet chamber 260. After the dust collector 252 is the rotary kiln 240, which functions as a device 220 that preheats, fires, and sinters the raw materials to make cement clinker. In the rotary kiln 240, the raw materials are preheated, fires, and sintered. The sintered cement clinker that has passed through the rotary kiln 240 falls into the clinker cooler 250, where it is rapidly cooled by atmospheric cooling air. The heated cooling air is then fed from the clinker cooler 250 as tertiary air through the tertiary air duct 251 to the exhaust gas of the rotary kiln 250. This recovers the heat contained in the high-temperature cement clinker, which can then be reused in the process. An optional heat exchanger 211, shown within the tertiary air line 251, transfers heat from the hot cooling air to a secondary system 1000 for the separation and / or storage of carbon dioxide (CO2). In this system, the heat is used as process heat to support the separation and / or storage of carbon dioxide (CO2). In this invention, the fuel / air supply to the rotary kiln 240 can be directed to a regenerative thermal oxidation stage upstream of the RTO reactor 230, depending on the exhaust gas temperature, which is 800°C to 900°C, preferably 850°C (tolerance 20°C). The available heat Q in the exhaust gas of the system that can be transferred by the heat exchanger 210 is sufficient to remove carbon dioxide (CO2) from the exhaust gas by a system located in the secondary circuit of the heat exchanger 210 that separates and / or stores carbon dioxide (CO2) from the exhaust gas. The heat Q extracted from the exhaust gas of plant 200 is used in the coupling process of plant 1000 for the separation and / or storage of carbon dioxide (CO2).In this case, separation and / or storage may also include the production of methanol in a reformer and chemical conversion to other chemicals. Carbon dioxide (CO2) can be separated and / or stored from the exhaust gas. Heat Q extracted from the exhaust gas of plant 200 is used in a coupling process for the separation and / or storage of carbon dioxide (CO2) in plant 1000. In this case, separation and / or storage may also include chemical conversion to other chemicals, such as the production of methanol in a reformer.

[0020] Figure 3 shows a third embodiment of the cement clinker manufacturing plant according to the present invention. Viewed with respect to the direction of gas flow, this third embodiment consists of a heat exchanger 310 for transferring heat to a coupling process for the separation and / or storage of carbon dioxide (CO2) from the exhaust gas of plant 300, and an RTO reactor 330 for the regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas of plant 300 and the conversion of hazardous air pollutants (HAPs). A dust collector 352 is provided thereafter to remove dust discharged from the tubular reactor 340 along with the exhaust gas and send it through the next tubular reactor 340 to the clinker cooler 350. Following the dust collector 352 is a tubular reactor 340, which is designed as a device 320 for preheating, firing, and sintering. These three process steps are carried out within the tubular reactor 340. Compared to fluidized bed reactors used as firing furnaces in conventional technology, the tubular reactor 340 is characterized by a longer residence time within the reactor. This residence time is sufficient for preheating, firing, and sintering the raw materials. The cement clinker exiting the tubular reactor 340 falls into the clinker cooler 350, where the high-temperature cement clinker is cooled by cooling air from the atmosphere. The cooling air heated in this process is sent to the tubular reactor 340 via the tertiary air line 351 to recover the heat present in the high-temperature cement clinker and reuse it in the process. An optional heat exchanger 311, shown within the tertiary air line 351, transfers heat from the high-temperature cooling air to a secondary system 1000 for the separation and / or storage of carbon dioxide (CO2), where the heat obtained is used as process heat to support the separation and / or storage of carbon dioxide (CO2). In this invention, the fuel / air supply to the tubular reactor 340 can be delivered to the regenerative thermal oxidation reactor 340 based on the exhaust gas temperature upstream of the RTO reactor 330, where the temperature is 800°C to 900°C, preferably 850°C (tolerance 20°C). The heat Q available in the plant's exhaust gas, which can be transferred via the heat exchanger 310, is sufficient to extract carbon dioxide (CO2) from the exhaust gas using a system in the secondary circuit of the heat exchanger 310 that separates and / or stores carbon dioxide (CO2) from the exhaust gas.The heat Q extracted from the exhaust gas of Plant 300 is used in the coupling process of Plant 1000 for the separation and / or storage of carbon dioxide (CO2). In this case, the separation and / or storage may also include the production of methanol in a reformer and chemical conversion to other chemicals.

[0021] Figure 4 shows a fourth embodiment of a cement clinker manufacturing plant according to the present invention. With respect to the direction of gas flow, this fourth embodiment consists of a heat exchanger 410 that transfers heat to a coupling process for separating and / or storing carbon dioxide (CO2) from the exhaust gas of plant 400, and an RTO reactor 430 that performs regenerative thermal oxidation of volatile organic compounds (VOCs) and conversion of hazardous air pollutants (HAPs) in the exhaust gas of plant 400. Downstream of the RTO reactor 430, a circulating fluidized bed reactor 440 and a tubular reactor 445 are combined. These reactors function as a preheating, calcination, and sintering apparatus 420. In the circulating fluidized bed reactor 440, raw materials are introduced and preheated and calcined. In this process, a portion of the fluidized bed material in the circulating fluidized bed reactor 440 is returned to the reactor via a cyclone 441 upon discharge. The preheated and calcined raw material powder flows into the subsequent tubular reactor 445 to undergo the sintering process. The raw material powder, sintered to become cement clinker, flows into the clinker cooler 450, where the high-temperature cement clinker is rapidly cooled by the atmosphere. The cooling air heated in this process flows into the circulating fluidized bed reactor 440 via the tertiary air line 451, where heat is recovered from the high-temperature cement clinker and reintroduced into the process. An optional heat exchanger 411, shown within the tertiary air line 451, transfers heat from the high-temperature cooling air to a secondary system 1000 for the separation and / or storage of carbon dioxide (CO2), where the aforementioned heat is used as process heat to support the separation and / or storage of carbon dioxide (CO2). The still moderately hot cement clinker is discharged from the system at the end of the clinker cooler 450. In this invention, the fuel / air supply to the circulating fluidized bed reactor 440 and the tubular reactor 445 is set to 800°C to 900°C, preferably 850°C (tolerance 20°C), depending on the exhaust gas temperature upstream of the regenerative thermal oxidation (RTO) reactor 430. The available heat Q in the exhaust gas of the system that can be transferred by the heat exchanger 410 is sufficient to remove carbon dioxide (CO2) from the exhaust gas by a system that separates and / or stores carbon dioxide (CO2) from the exhaust gas, which is located in the secondary circuit of the heat exchanger 410.Heat Q extracted from the exhaust gas of plant 400 is used in the integrated process of plant 1000 for carbon dioxide (CO₂) capture and / or storage. In this case, the aforementioned capture and / or storage may also include methanol production in a reformer and chemical conversion into other chemical substances.

[0022] Figure 5 shows a fifth embodiment of a cement clinker manufacturing plant according to the present invention. With respect to the direction of gas flow, this fifth embodiment consists of a heat exchanger 510 that transfers heat from the exhaust gas of plant 500 to a coupling process for the separation and / or storage of carbon dioxide (CO2), and an RTO reactor 530 that performs regenerative thermal oxidation of volatile organic compounds (VOCs) and conversion of hazardous air pollutants (HAPs) in the exhaust gas of plant 500. Downstream of the RTO reactor 530 are a circulating fluidized bed reactor 540 and a rotary kiln 545. These function as equipment 520 for preheating, calcination, and sintering. In the circulating fluidized bed reactor 540, raw materials are fed in, preheated, and calcined. In this process, a portion of the fluidized bed in the circulating fluidized bed reactor 540 is returned to the reactor via a cyclone 541 upon discharge. The preheated and calcined raw materials are then fed into the subsequent rotary kiln 545 for the sintering process. The raw materials sintered into cement clinker are fed into a clinker cooler 550, where the still-hot cement clinker is rapidly cooled by the atmosphere. The cooling air heated in this process returns to the circulating fluidized bed reactor 540 via a tertiary air line 551, where heat is recovered from the hot cement clinker and reintroduced into the process. Here, an optional heat exchanger 511, shown within the tertiary air duct 551, transfers heat from the hot cooling air to a secondary system 1000 for the separation and / or storage of carbon dioxide (CO2), which is used as process heat to support the separation and / or storage of carbon dioxide (CO2). At the end of the clinker cooler 550, the still moderately hot cement clinker is discharged from the system. In this invention, the fuel / air supply to the circulating fluidized bed reactor 540 and rotary kiln 545 is provided to the regenerative thermal oxidation reactor depending on the exhaust gas temperature upstream of the RTO reactor 530. The temperature there can be set to 800°C to 900°C, preferably 850°C with a tolerance of 20°C. The heat Q available in the plant's exhaust gas that can be transferred through the heat exchanger 510 is sufficient to capture and / or store carbon dioxide (CO2) from the exhaust gas using a system located in the secondary circuit of the heat exchanger 510.The heat Q extracted from the exhaust gas of Plant 500 is used in the coupling process of Plant 1000 for the capture and / or storage of carbon dioxide (CO2). This capture and / or storage may also include the production of methanol in a reformer and chemical conversion to other chemicals.

[0023] Figure 6 shows a sixth embodiment of the cement clinker manufacturing plant 600 according to the present invention. Viewed with respect to the direction of gas flow, this sixth embodiment consists of a heat exchanger 610 that transfers heat from the exhaust gas of the plant 600 to a coupling process for the separation and / or storage of carbon dioxide (CO2), and an RTO reactor 630 that performs regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas of the plant 600 and conversion of hazardous air pollutants (HAPs). A tubular reactor 640 is located downstream of the RTO reactor 630. In this tubular reactor 640, high-temperature raw materials are preheated and calcined. Downstream of the tubular reactor 640 is a rotary kiln 645 in which the calcined raw materials are sintered. The tubular reactor 640 and the rotary kiln 640 together constitute an apparatus 620 that performs preheating, calcination, and sintering. Raw materials are supplied directly from the tubular reactor 640 to the rotary kiln inlet chamber 660, and dust in the air discharged from the tubular reactor 640 is also returned to the rotary kiln 645. In the rotary kiln 645, the pre-fired raw materials are sintered to form cement clinker. The sintered cement clinker that has passed through the rotary kiln 645 falls into the clinker cooler 650, where it is rapidly cooled by cooling air from the atmosphere. The heated cooling air from the clinker cooler 650 is sent from the clinker cooler 650 as tertiary air through the tertiary air line 651 to the tubular reactor 640, where heat is recovered from the hot cement clinker and reused in the process. An optional heat exchanger 611, shown within the tertiary air line 651, transfers heat from the hot cooling air to a secondary system 1000 for carbon dioxide (CO2) separation and / or storage. This heat is used as process heat to support carbon dioxide (CO2) separation and / or storage. In this invention, the fuel / air supply to the tubular reactor 640 and / or rotary kiln 645 is directed to the regenerative thermal oxidation stage upstream of the RTO reactor 630, based on the exhaust gas temperature. The temperature there is 800°C to 900°C, preferably 850°C (with a tolerance of 20°C).The available heat Q in the system exhaust gas transferred by the heat exchanger 610 is of a sufficient amount to remove carbon dioxide (CO2) from the exhaust gas by the system for separating and / or storing carbon dioxide (CO2) from the exhaust gas arranged in the secondary circuit of the heat exchanger 110. The heat Q extracted from the exhaust gas of the plant 600 is used in the coupling process of the plant 1000 for the separation and / or storage of carbon dioxide (CO2). In this case, the separation and / or storage may also include the production of methanol in a reformer and chemical conversion into other chemical substances. [Description of Symbols]

[0024] 100 Plant 110 Heat exchanger 111 Heat exchanger 120 Preheating, calcining and sintering apparatus 130 Regenerative thermal oxidation reactor 140 Circulating fluidized bed reactor 141 Cyclone 142 Pipeline 150 Clinker cooler 151 Tertiary air line 200 Plant 210 Heat exchanger 210 Heat exchanger 220 Preheating, calcining and sintering apparatus 230 Regenerative thermal oxidation reactor 240 Rotary kiln 252 Dust collector 260 Rotary kiln inlet chamber 300 Plant 310 Heat exchanger 311 Heat exchanger 320 Preheating, calcining and sintering apparatus 330 Regenerative thermal oxidation reactor 340 Tubular reactor 350 Clinker cooler 351 Tertiary air line 352 Dust collector 400 Plant 410 Heat exchanger 411 Heat exchanger 420 Preheating, firing, and sintering apparatus 430 Regenerative thermal oxidation reactor 440 Circulating fluidized bed reactor 441 Cyclone 445 Tubular reactor 450 Clinker condenser 451 Tertiary Air Line 500 Systems 510 heat exchanger 520 Preheating, firing, and sintering apparatus 530 Regenerative thermal oxidation reactor 540 Circulating fluidized bed reactor 542 pipelines 541 Cyclone 550 Clinker condenser 551 Tertiary air duct 610 Heat exchanger 611 Heat exchanger 620 Preheating, firing, and sintering apparatus 630 Regenerative thermal oxidation reactor 640 Tubular reactor 642 Dust collector 645 Rotary Kiln 650 Clinker condenser 651 Tertiary air duct 660 Rotary Kiln Inlet Chamber 1000 Carbon Dioxide (CO2) Capture and Storage Systems Q Heat

Claims

1. The following — At least one heat exchanger (110, 210, 310, 410, 510, 610) located downstream in the direction of the gas flow, — Apparatus (120, 220, 320, 420, 520, 620) for preheating, firing, and sintering at least one raw material, configured as individual devices or a series of individual devices, and positioned downstream in the direction of the raw material flow. In a plant (100, 200, 300, 400, 500, 600) for producing cement clinker from raw materials, the plant is equipped with, and at least one of the apparatus (120, 220, 320, 420, 520, 620) for preheating, firing, and sintering the above raw materials is connected to at least one heat exchanger (110, 210, 310, 410, 510, 610) located downstream in the direction of the gas flow on the primary side, to which exhaust gas is supplied, At least one heat exchanger (110, 210, 310, 410, 510, 610) located downstream in the direction of the gas flow described above is configured to allow carbon dioxide (CO2) from the exhaust gas on the secondary side. 2 A plant characterized by being connected to a downstream system (1000) for separating and / or storing )

2. The above-mentioned apparatus for preheating, firing, and sintering, Circulating fluidized bed reactor (140), Rotary kiln (240, 340) or Tubular reactor (440) The plant according to claim 1, characterized in that it is the same as the plant according to claim 1.

3. The plant according to claim 2, characterized in that the tubular reactor (245) is connected downstream of the rotary kiln (240) in the direction of the gas flow.

4. Carbon dioxide (CO2) 2 A secondary system for separating and / or storing hydrogen (H) generates electricity using a steam generator for electrical energy production, which powers a water electrolysis apparatus. 2 The electrolysis apparatus for hydrogen is connected to a reformer on the hydrogen side, and in the reformer, carbon dioxide (CO2) cooled in a heat exchanger is processed. 2 The plant according to any one of claims 1 to 3, characterized in that exhaust gas containing ) is converted to methanol.

5. The high-temperature gas from the clinker coolers (151, 251, 351, 451, 551, 651) located downstream in the material flow direction of the apparatus (120, 220, 320, 420, 520, 620) for preheating, firing, and sintering the above-mentioned at least one raw material powder is returned to the apparatus (10, 220, 320, 420, 520, 620) for preheating, firing, and sintering the above-mentioned at least one raw material powder. A tertiary air line (151, 251, 351, 451, 551, 651) is provided, and at least one apparatus (10, 220, 320, 420, 520, 620) for preheating, firing, and sintering raw material powder is connected to a heat exchanger (111, 211, 311, 411, 511, 611), and the secondary side of this heat exchanger (111, 211, 311, 411, 511, 611) is connected to exhaust gas and carbon dioxide (CO2). 2 The plant according to any one of claims 1 to 4, which is connected to a downstream system (1000) for separating and / or storing )

6. Excess fuel and atmospheric oxygen are supplied to the apparatus for preheating, firing, and sintering the above raw material powder, and as a result, the exhaust gas is carbon dioxide (CO2) produced in the system for manufacturing cement clinker from the raw material powder. 2 The amount of energy required to separate and / or store carbon dioxide (CO2) is precisely measured. 2 A method of operating the plant according to any one of claims 1 to 5, characterized in that the exhaust gas temperature becomes such that it accurately carries a sufficient amount of heat to supply to a system for separating and / or storing )

7. The method according to 6, characterized in that the amount of fuel supplied is adjusted according to the exhaust gas temperature upstream of the preheater.

8. The method according to 6 or 7, characterized in that exhaust gas from at least one of the above-mentioned devices (120, 220, 320, 420, 520, 620) is treated in a regenerative thermal oxidation reactor (130, 230, 330, 430, 530, 630), and the fuel supply is adjusted to 800°C to 900°C, preferably 850°C (tolerance of 20°C), depending on the exhaust gas temperature upstream of the regenerative thermal oxidation reactor (130, 230, 330, 430, 530, 630).

9. The method according to any one of claims 6 to 8, characterized in that the fuel mainly consists of a secondary fuel containing treated industrial waste and / or household waste, used tires, solvent waste, or treated biomass.

10. The above storage is carbon dioxide (CO2) 2 The method according to any one of claims 6 to 9, characterized in that it also includes chemically converting ) into other substances.

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