Plant for producing cement with thermal energy output

Abstract

The invention relates to a plant (100, 200, 300, 400) for producing cement clinker from a raw material, 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, calcining and sintering the raw material, which device can be composed of individual and successive devices, wherein at least one device (120, 220, 320, 420) for preheating, calcining and sintering the raw material is connected on the primary side to at least one heat exchanger (110, 210, 310, 410) located downstream in the gas flow direction and is supplied with exhaust gas. According to the invention, at least one heat exchanger (110, 210, 310, 410) located downstream in the gas flow direction is connected on the secondary side to a downstream device for separating and / or sequestering carbon dioxide (CO) from the exhaust gas. This plant configuration that abandons a raw material preheater allows the plant to be operated over-fueled such that the off-gas of the plant has sufficient heat for operating a coupling process for separating and / or sequestering carbon dioxide.

Description

Technical Field

[0001] The present invention relates to an apparatus for producing cement clinker from raw meal, the apparatus having at least one heat exchanger located downstream in the gas flow direction and at least one subsequent device in the material flow direction for preheating, calcining and sintering the raw meal, wherein the device may also consist of a series of independent devices, wherein the at least one device for preheating, calcining and sintering the raw meal is connected to the at least one heat exchanger located downstream in the gas flow direction on the primary side and is loaded with exhaust gas. Background Technology

[0002] To produce cement clinker from raw meal consisting of milled, silicate- and limestone-containing rocks, the raw meal undergoes different, sequential stages of heat treatment. In the first step, the raw meal is preheated using waste heat from subsequent heat treatment steps. The preheated raw meal is then deacidified or calcined to formally expel carbon dioxide (CO2) from the carbonates (-CO3) of the limestone-containing raw meal. Finally, the deacidified or calcined raw meal is sintered into cement clinker in a chemical solid-state reaction in a rotary kiln. Rapid cooling follows sintering to prevent the desired clinker phase in the cement clinker from transforming into other phases during cooling. The entire production process is a continuous optimization challenge to maintain the waste heat generated during the process. The desired goal is for the entire production process to supply only the heat corresponding to the enthalpy of formation from raw meal to cement clinker. In the process optimizations implemented in recent decades, the motivation has consistently been to minimize the heat demand generated by economically costly fuels. Subsequent optimization of the production process involves nitrogen removal from waste gas, specifically avoiding nitrogen oxides (NOx), which are recognized globally as a cause of observable acid rain, from the waste gas. XAnother optimization step in the current reform of the cement clinker production process is to avoid carbon dioxide (CO2) emissions, as previously mentioned, which are driven out by the raw materials. CO2 emissions from cement clinker production, along with CO2 from the combustion of fossil fuels, constitute a large portion of anthropogenic CO2 emissions. CO2 is considered a cause of currently observable global warming. Separating CO2 from industrial exhaust gases and subsequently sequestering it is a highly endothermic process. This means that separating and even sequestering CO2, whether by compressing and storing it in underground aquifers or by chemically converting it into a non-gaseous state during coupling processes, consumes energy. If this energy is obtained from other combustion processes in the generation of additional heat or electricity, this immediately produces further CO2 emissions, in which these CO2 emissions should also be separated. Since the current methods and corresponding equipment used to produce cement clinker are largely energy-efficient, it is not possible to obtain heat or electricity from such equipment on the necessary scale. To date, equipment and methods used to produce cement clinker have generated more carbon dioxide emissions than could be separated by utilizing available waste heat to run a so-called “capture process” (i.e., a subsequent separation process to avoid carbon dioxide (CO2) emissions).

[0003] An obvious solution to extract heat as energy for the capture process is to increase fuel input in known cement clinker production equipment and corresponding methods, thereby generating more waste heat. However, this additional fuel input raises the temperature within the equipment, significantly altering its energy balance. As a result, the optimizations implemented to date for denitrification will be reversed, and the production process will become unbalanced in many places within the equipment. Consequently, the quality of the produced cement clinker is expected to decline, as the desired clinker phase composition will change with the increased energy input, and the quality of denitrification will decrease. Summary of the Invention

[0004] Therefore, the object of the present invention is to provide an apparatus and a corresponding method for producing cement clinker, the energy balance of which allows the use of available waste heat to operate a subsequent capture process to separate and seal carbon dioxide (CO2) from the exhaust gas from the apparatus.

[0005] The objective of this invention is achieved by the apparatus according to claim 1 and the corresponding method according to claim 6. Further advantageous designs of the apparatus are described in the dependent claims of claim 1. Further advantageous designs of the method are described in the dependent claims of claim 6.

[0006] The equipment and corresponding methods described herein are based on abandoning the separate preheating of raw materials in equipment used for producing cement clinker. In equipment known to date for producing cement clinker, the heat present in the exhaust gas from the calcination and sintering unit is supplied to the cold raw materials in a separate device for this purpose, namely a preheater. Subsequently, the exhaust gas is forcefully cooled, and the raw materials are at a temperature slightly below the decomposition temperature of lime (CaCO3). This energy recovery allows the calcination and sintering unit, whether referring here to separate equipment components (such as circulating fluidized bed reactors, tubular reactors, or calciners and rotary kilns) or to a single equipment component (such as a long rotary kiln or furnace calciner), to operate with much less fuel because the raw materials have been preheated before arriving at one or more reactors. Here, the object of the present invention is not to maintain a low exhaust gas temperature as in the prior art, but to raise it to a level that allows the operation of coupled equipment for separating and / or sequestering carbon dioxide (CO2) using the heat contained in the exhaust gas. The purpose of this invention is not to make the equipment and corresponding method operate energy-efficiently with respect to the amount of cement clinker produced, but rather to operate energy-efficiently with respect to the amount of cement clinker produced and the separation of carbon dioxide (CO2). The concept of this invention does not preclude the use of the obtained waste heat after the separation of carbon dioxide (CO2) to compress it for storage or chemical conversion into other substances. Regarding conversion, methanol or chemical conversion into a solid could be considered.

[0007] Therefore, according to the concept of the invention, the at least one heat exchanger located downstream in the gas flow direction is connected on the secondary side to a downstream device for separating and / or storing carbon dioxide (CO2) from the exhaust gas. Here, the specific coupling process used is secondary. For example, it is conceivable to use an amine scrubber to wash the exhaust gas and subsequently store the separated carbon dioxide (CO2) or to produce methanol (CH3OH) from carbon dioxide (CO2) and hydrogen (H2) obtained by electrolysis of water (H2O), wherein the electrolysis is operated using electricity generated by steam. Here, the aforementioned steam is generated by heat in the exhaust gas from equipment used to produce cement clinker. According to the proposed scheme, the concept of "storage" includes storage to keep it at a storage location, or storage in the form of a chemical conversion into other substances, and optionally, the converted substances can be used for other purposes.

[0008] According to the concept of the invention, by regulating the fuel supply to at least one device for preheating, calcining and sintering, so much heat is generated by the primary combustion of secondary fuels that the separation and / or sequestration of carbon dioxide (CO2) just consumes this excess heat without leaving any residual energy.

[0009] The invention presented here is notable for its ability to implement increased fuel inputs with relatively low emissions and economic efficiency, particularly when producing cement clinker, especially by burning low-calorific-value or even low-quality fuels. Examples of low-calorific-value or even low-quality fuels include treated industrial waste and / or municipal solid waste, waste tires, solvent waste, or treated biomass. If the energy used to separate and / or contain the carbon dioxide (CO2) generated during cement clinker production is generated separately, air purification technologies would be very costly if this energy also required to be generated using low-calorific-value or low-quality fuels. Equipment for producing cement clinker burns these fuels in the presence of raw materials. Raw materials contribute significantly to nitrogen oxide (NOx) emissions. X It has a strong catalytic effect on the decomposition of volatile organic compounds (VOCs) and hazardous air pollutants (HAPs). It is even possible to use fuels that readily form furans and dioxins during combustion. Such fuels can be: polyvinyl chloride (PVC) waste, halogenated solvents, and other halogenated hydrocarbons. Typical equipment for producing cement clinker generally incorporates denitrification technology as well as technology to avoid dioxin and furan emissions. Non-volatile combustion residues, including heavy metals and solid combustion residues containing harmful substances, are adsorbed and embedded in the cement clinker, or the cement clinker encapsulates these harmful substances, thus preventing them from being emitted into the environment with the exhaust gas.

[0010] Although equipment used for producing cement clinker has well-established emission avoidance technologies, it has proven advantageous to arrange a regenerative thermal oxidation (RTO) reactor for hazardous substances between the heat exchanger (which is connected on the secondary side to downstream equipment for separating and / or storing carbon dioxide (CO2)) and the unit for preheating, calcining, and sintering raw materials. This reactor completely oxidizes volatile organic compounds and harmful air pollutants. To operate this RTO reactor, it has proven advantageous to adjust fuel use in the cement clinker production equipment based on the temperature of the exhaust gas, more specifically, the temperature of the exhaust gas flowing into the RTO reactor. This temperature should be between 800°C and 900°C, preferably about 850°C, with a tolerance of 20°C.

[0011] Using undried raw meal generally renders this type of calciner unsuitable. This calciner, acting as a gas flow reactor connected between a conventional raw meal preheater and a rotary kiln, is designed to receive preheated raw meal. The residence time of cold raw meal in such a calciner is insufficient to heat it and then deacidify it (calcination). It has proven advantageous to use tubular reactors, longer rotary kilns, or circulating fluidized bed reactors as devices for preheating, calcination, and sintering. In tubular reactors, the residence time of raw meal is significantly longer than in gas flow reactors, which are currently commonly used as calciners. Preheating, calcination, and sintering can all be performed in a rotary kiln. Very early equipment for producing cement clinker used longer rotary kilns to precisely accommodate these three steps. The disadvantage of long rotary kilns is the relatively high exhaust gas temperature, resulting in heat loss. However, the purpose of the device and method presented herein is precisely to maintain a high exhaust gas temperature so that this heat can be utilized during the coupling process.

[0012] Advantageously, depending on the operating mode of the rotary kiln, a tubular reactor is connected downstream of the kiln regarding gas flow. In operation with a superstoichiometric air supply (lambda > 1), the rotary kiln exhaust gas can be directly introduced into the reactor for the regenerative thermal oxidation of hazardous substances. However, if the rotary kiln operates with a substoichiometric air supply (lambda < 1), it is recommended that the exhaust gas be introduced as lean coal gas into the tubular reactor for conversion of fuel or pyrolysis gases present in the gas space.

[0013] As mentioned at the beginning, the secondary-side equipment for separating and / or storing carbon dioxide (CO2) generates electricity using a steam generator to produce electricity, which supplies the water electrolysis unit, wherein the hydrogen (H2) electrolysis unit is connected to a converter on the hydrogen side, in which exhaust gas containing carbon dioxide (CO2) cooled in a heat exchanger is converted into methanol (CH3OH). Attached Figure Description

[0014] The present invention will be further illustrated with reference to the following figures.

[0015] in:

[0016] Figure 1 A first design of an apparatus for producing cement clinker according to the present invention is shown.

[0017] Figure 2 A second design of an apparatus for producing cement clinker according to the present invention is shown.

[0018] Figure 3A third design of an apparatus for producing cement clinker according to the present invention is shown.

[0019] Figure 4 A fourth design of an apparatus for producing cement clinker according to the present invention is shown.

[0020] Figure 5 A fifth design of an apparatus for producing cement clinker according to the present invention is shown.

[0021] Figure 6 A sixth design of an apparatus for producing cement clinker according to the present invention is shown. Detailed Implementation

[0022] Figure 1A first design of an apparatus 100 for producing cement clinker according to the present invention is described. Viewed against the gas flow direction, the first design comprises a heat exchanger 110 (used to remove heat from the exhaust gas from apparatus 100 to a coupled process for separating and / or storing carbon dioxide (CO2)), an RTO reactor 130 (used for regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas of apparatus 100 and for converting harmful air pollutants (HAPs)). This is followed by a circulating fluidized bed reactor 140 as a device 120 for preheating, calcining, and sintering raw materials into cement clinker, wherein the circulating fluidized bed reactor 140 performs all three steps: preheating, calcining, and sintering. In this circulating fluidized bed reactor 140, primary and / or secondary fuels are introduced, which heat the circulating fluidized bed. The circulating fluidized bed can flow towards the RTO reactor 130 along the exhaust gas flow direction, where the solids in the circulating fluidized bed are separated by a cyclone separator 141 and returned to the circulating fluidized bed reactor 140. Raw meal sintered into cement clinker falls from the circulating fluidized bed into pipe 142 from the circulating fluidized bed reactor 140, where the hot cement clinker is transferred to a clinker cooler 150 and rapidly cooled there by quenching with atmospheric cooling air. The hot cooling air from the clinker cooler 150 is returned to the circulating fluidized bed reactor 140 through a tertiary air pipe 151. Thus, heat in the cement clinker is recovered into the process. An optional heat exchanger 111, shown here in the tertiary air pipe 151, directs the heat from the hot cooling air on the secondary side to a device 1000 for the separation and / or storage of carbon dioxide (CO2), where this heat is used as process heat to support the separation and / or storage of CO2. According to the concept of the invention, fuel / air supply can be introduced into the circulating fluidized bed reactor 140 based on the temperature of the exhaust gas before the RTO reactor 130 for regenerative thermal oxidation, and the reactor is designed such that the temperature there is preferably between 800°C and 900°C. The heat Q present in the exhaust gas of the equipment and transferable by heat exchanger 110 is sufficient to enable the separation and / or storage of carbon dioxide (CO2) from the exhaust gas using equipment present in the secondary loop of heat exchanger 110. The heat Q extracted from the exhaust gas of equipment 100 is used for separation or storage in the coupling process of equipment 1000 for separating and / or storing carbon dioxide (CO2), wherein separation and / or storage may also include chemical conversion to other chemical substances, such as methanol production in a converter.

[0023] Figure 2A second design of an apparatus 200 for producing cement clinker according to the present invention is depicted. Viewed against the gas flow direction, this second design comprises a heat exchanger 210 (used to remove heat from the exhaust gas from apparatus 200 to a coupled process for separating and / or storing carbon dioxide (CO2)), an RTO reactor 230 (used for regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas from apparatus 200 and for converting harmful air pollutants (HAPs)). Following this is a dust collector 252, which guides dust from the exhaust gas from the subsequently following rotary kiln 240 back to the rotary kiln feed chamber 260. After the dust collector 252 is the rotary kiln 240, which serves as a device 220 for preheating, calcining, and sintering raw meal into cement clinker. In this rotary kiln 240, the raw meal is preheated, calcined, and sintered. After passing through rotary kiln 240, the sintered cement clinker falls into clinker cooler 250, where it is quenched by atmospheric cooling air. The heated cooling air, as tertiary air, is introduced from clinker cooler 250 into the exhaust gas of rotary kiln 240 via tertiary air duct 251. Thus, the heat present in the hot cement clinker is recovered into the process. An optional heat exchanger 211, shown here in tertiary air duct 251, directs the heat from the hot cooling air on the secondary side to a device 1000 for the separation and / or storage of carbon dioxide (CO2), where this heat is used as process heat to support the separation and / or storage of CO2. According to the concept of the invention, the fuel / air supply can be introduced into rotary kiln 240 according to the temperature of the exhaust gas before the RTO reactor 230 for regenerative thermal oxidation, and is designed such that the temperature there is preferably between 800°C and 900°C. The heat Q present in the exhaust gas of the equipment and transferable by heat exchanger 210 is sufficient to enable the separation and / or storage of carbon dioxide (CO2) from the exhaust gas using equipment present in the secondary loop of heat exchanger 3210. The heat Q extracted from the exhaust gas of equipment 200 is used for separation or storage in the coupling process of equipment 1000 for separating and / or storing carbon dioxide (CO2), wherein separation and / or storage may also include chemical conversion to other chemical substances, such as methanol production in a converter.

[0024] Figure 3A third design of an apparatus for producing cement clinker according to the present invention is described. Viewed against the gas flow direction, this third design comprises a heat exchanger 310 (used to remove heat from the exhaust gas from apparatus 300 to a coupled process for separating and / or storing carbon dioxide (CO2)), an RTO reactor 330 (used for regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas from apparatus 300 and for converting harmful air pollutants (HAPs)). This is followed by a dust collector 352 to convey dust discharged with the exhaust gas from tubular reactor 340 into a subsequent tubular reactor 340, which then feeds into a clinker cooler 350. Following the dust collector 352 is a tubular reactor 340 serving as a preheating, calcination, and sintering apparatus 320, wherein these three process steps are carried out in the tubular reactor 340. Compared to existing gas flow reactors used as calciners, the tubular reactor 340 is characterized by a longer residence time. This residence time is sufficient to allow the fed raw meal to be not only preheated, calcined, and sintered. The cement clinker exiting the tubular reactor 340 then falls into a clinker cooler 350, where the hot cement clinker is quenched by atmospheric cooling air. The cooled air, heated here, is introduced into the tubular reactor 340 through a tertiary air duct 351 to recover the heat present in the hot cement clinker back into the process. An optional heat exchanger 311, shown here in the tertiary air duct 351, directs the heat from the hot cooling air on the secondary side to a device 1000 for the separation and / or sequestration of carbon dioxide (CO2), where this heat is used as process heat to support the separation and / or sequestration of CO2. According to the concept of the invention, fuel / air supply can be introduced into tubular reactor 340 based on the temperature of the exhaust gas before RTO reactor 330 for regenerative thermal oxidation, and is designed such that the temperature there is preferably between 800°C and 900°C. The heat Q present in the exhaust gas of the equipment and transferable by heat exchanger 310 is sufficient to enable the separation and / or storage of carbon dioxide (CO2) from the exhaust gas using equipment present in the secondary loop of heat exchanger 310. The heat Q extracted from the exhaust gas of equipment 300 is used for separation or storage in the coupling process of equipment 1000 for separating and / or storing carbon dioxide (CO2), wherein separation and / or storage may also include chemical conversion to other chemical substances, such as methanol production in a converter.

[0025] Figure 4A fourth design of an apparatus for producing cement clinker according to the present invention is shown. Viewed against the gas flow direction, this fourth design comprises a heat exchanger 410 (used to remove heat from the exhaust gas from apparatus 400 to a coupled process for separating and / or storing carbon dioxide (CO2)) and an RTO reactor 430 (used for regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas from apparatus 400 and for converting harmful air pollutants (HAPs)). Following the RT reactor 430 is a combination of a circulating fluidized bed reactor 440 and a tubular reactor 445. Together, these form a device 420 for preheating, calcination, and sintering. Here, raw material is fed into the circulating fluidized bed reactor 440, where preheating and calcination are performed. A portion of the fluidized bed in the circulating fluidized bed reactor 440 is returned to the circulating fluidized bed reactor 440 upon discharge via a cyclone separator 441. The preheated and calcined raw meal then falls into a subsequent tubular reactor 445 for the sintering process. The sintered raw meal, now cement clinker, then falls into a clinker cooler 450, where the still-hot cement clinker is quenched by rapid cooling with atmospheric air. The cooled air, heated here, is returned as tertiary air through a tertiary air conduit 451 to the circulating fluidized bed reactor 440 for recovering heat from the hot cement clinker into the process. An optional heat exchanger 411, shown here in the tertiary air conduit 451, directs the heat from the heated cooled air on the secondary side to a device 1000 for the separation and / or storage of carbon dioxide (CO2), where this heat is used as process heat to support the separation and / or storage of CO2. At the end of the clinker cooler 450, the still moderately hot cement clinker exits the device. According to the concept of the invention, fuel / air supply can be introduced into the circulating fluidized bed reactor 440 and tubular reactor 445 based on the temperature of the exhaust gas before the RTO reactor 430 for regenerative thermal oxidation, and is designed such that the temperature there is preferably between 800°C and 900°C. The heat Q present in the exhaust gas of the equipment and transferable by heat exchanger 410 is sufficient to enable the separation and / or storage of carbon dioxide (CO2) from the exhaust gas using equipment present in the secondary loop of heat exchanger 410. The heat Q extracted from the exhaust gas of equipment 400 is used for separation or storage in the coupling process of equipment 1000 for separating and / or storing carbon dioxide (CO2), wherein separation and / or storage may also include chemical conversion to other chemical substances, such as methanol production in a converter.

[0026] Figure 5A fifth design of an apparatus for producing cement clinker according to the present invention is shown. Viewed against the gas flow direction, this fifth design consists of a heat exchanger 510 (used to remove heat from the exhaust gas from apparatus 500 to a coupled process for separating and / or storing carbon dioxide (CO2)) and an RTO reactor 530 (used for regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas from apparatus 500 and for converting harmful air pollutants (HAPs)). Following the RT reactor 530 is a combination of a circulating fluidized bed reactor 540 and a rotary kiln 545. Here, both together serve as a device 520 for preheating, calcination, and sintering. Here, raw materials are fed to the circulating fluidized bed reactor 540, where preheating and calcination are performed. A portion of the fluidized bed in the circulating fluidized bed reactor 540 is returned to the circulating fluidized bed reactor 540 upon discharge via a cyclone separator 541. The preheated and calcined raw meal then falls into a subsequent rotary kiln 545 for sintering. The sintered raw meal, now cement clinker, then falls into a clinker cooler 550, where the still-hot clinker is quenched by rapid cooling with atmospheric air. The cooled air, heated here, is returned as tertiary air through a tertiary air conduit 551 to a circulating fluidized bed reactor 540 to recover heat from the hot cement clinker into the process. An optional heat exchanger 511, shown here in the tertiary air conduit 551, directs the heat from the heated cooled air on the secondary side to a device 1000 for the separation and / or sequestration of carbon dioxide (CO2), where this heat is used as process heat to support the separation and / or sequestration of CO2. At the end of the clinker cooler 550, the still moderately hot cement clinker exits the device. According to the concept of the invention, fuel / air supply can be introduced into the circulating fluidized bed reactor 540 and rotary kiln 545 based on the temperature of the exhaust gas before the RTO reactor 530 for regenerative thermal oxidation, and is designed such that the temperature there is preferably between 800°C and 900°C. The heat Q present in the exhaust gas of the equipment and transferable by heat exchanger 510 is sufficient to enable the use of equipment for separating and / or storing carbon dioxide (CO2) from the exhaust gas, which is present in the secondary loop of heat exchanger 410. The heat Q extracted from the exhaust gas of equipment 500 is used for separation or storage in the coupling process of equipment 1000 for separating and / or storing carbon dioxide (CO2), wherein separation and / or storage may also include chemical conversion to other chemical substances, such as methanol production in a converter.

[0027] Figure 6A sixth design of an apparatus 600 for producing cement clinker according to the present invention is shown. Viewed against the gas flow direction, this sixth design consists of a heat exchanger 610 (used to remove heat from the exhaust gas from apparatus 600 to a coupled process for separating and / or storing carbon dioxide (CO2)), an RTO reactor 630 (used for regenerative thermal oxidation of volatile organic compounds (VOCs) in the exhaust gas of apparatus 600 and for converting harmful air pollutants (HAPs)). This is followed by a tubular reactor 640, in which the hot raw material is preheated and calcined. Following the tubular reactor 640 is a rotary kiln 645, in which the calcined raw material is sintered. These two units, the tubular reactor 640 and the rotary kiln 640, are here a device 620 for preheating, calcination, and sintering. Raw meal is fed directly from tubular reactor 640 into rotary kiln feed chamber 260, where dust from the air exiting tubular reactor 640 is guided back to rotary kiln 645. In rotary kiln 645, the previously calcined raw meal is sintered into cement clinker. After passing through rotary kiln 645, the sintered cement clinker falls into clinker cooler 650, where it is quenched using atmospheric cooling air. Heated cooling air from clinker cooler 650 is guided as tertiary air through tertiary air duct 6 from clinker cooler 650 to tubular reactor 640 to recover heat from the hot cement clinker into the process. An optional heat exchanger 611, shown here in tertiary air duct 651, guides the heat from the hot cooling air on the secondary side to a device 1000 for the separation and / or storage of carbon dioxide (CO2), where this heat is used as process heat to support the separation and / or storage of CO2. According to the concept of the invention, fuel / air supply is introduced into tubular reactor 640 and / or rotary kiln 645 based on the temperature of the exhaust gas before the RTO reactor 630 for regenerative thermal oxidation, and is designed such that the temperature there is between 800°C and 900°C, preferably 850°C ± 20°C. The heat Q present in the exhaust gas of the equipment and transferable by heat exchanger 610 is sufficient to enable the use of equipment for separating and / or storing carbon dioxide (CO2) from the exhaust gas, present in the secondary loop of heat exchanger 110. The heat Q extracted from the exhaust gas of equipment 600 is used for separation or storage in the coupling process of equipment 1000 for separating and / or storing carbon dioxide (CO2), wherein separation and / or storage may also include chemical conversion to other chemical substances, such as methanol production in a converter.

[0028] List of reference numerals

[0029] 100 devices

[0030] 110 Heat Exchanger

[0031] 111 Heat Exchanger

[0032] 120 Apparatus for preheating, calcination and sintering

[0033] 130 Reactors for regenerative thermal oxidation

[0034] 140 circulating fluidized bed reactor

[0035] 141 Cyclone Separator

[0036] 142 Pipeline

[0037] 150 Clinker Cooler

[0038] 151 Tertiary Air Pipe

[0039] 200 devices

[0040] 210 Heat Exchanger

[0041] 211 Heat Exchanger

[0042] 220 Apparatus for preheating, calcination and sintering

[0043] 230 Reactor for regenerative thermal oxidation

[0044] 240 rotary kiln

[0045] 250 Clinker Cooler

[0046] 251 Tertiary Air Pipe

[0047] 252 Dust Collector

[0048] 260 Rotary Kiln Feed Chamber

[0049] 300 devices

[0050] 310 heat exchanger

[0051] 311 Heat Exchanger

[0052] 320 Apparatus for preheating, calcination and sintering

[0053] 330 Reactor for regenerative thermal oxidation

[0054] 340 tubular reactor

[0055] 350 Clinker Cooler

[0056] 351 Tertiary Air Pipe

[0057] 352 Dust Collector

[0058] 400 equipment

[0059] 410 Heat Exchanger

[0060] 411 Heat Exchanger

[0061] 420 Apparatus for preheating, calcination and sintering

[0062] 430 Reactor for regenerative thermal oxidation

[0063] 440 circulating fluidized bed reactor

[0064] 441 Cyclone Separator

[0065] 445 Tubular Reactor

[0066] 450 Clinker Cooler

[0067] 451 Tertiary Air Pipe

[0068] 500 devices

[0069] 510 heat exchanger

[0070] 511 Heat Exchanger

[0071] 520 Apparatus for preheating, calcination and sintering

[0072] 530 Reactor for regenerative thermal oxidation

[0073] 540 circulating fluidized bed reactor

[0074] 541 Cyclone Separator

[0075] 542 Pipeline

[0076] 545 Rotary Kiln

[0077] 550 Clinker Cooler

[0078] 551 Tertiary Air Pipe

[0079] 600 devices

[0080] 610 heat exchanger

[0081] 611 Heat Exchanger

[0082] 620 Apparatus for preheating, calcination and sintering

[0083] 630 Reactor for regenerative thermal oxidation

[0084] 640 tubular reactor

[0085] 642 Dust Collector

[0086] 640 tubular reactor

[0087] 645 Rotary Kiln

[0088] 650 Clinker Cooler

[0089] 651 Tertiary Air Pipe

[0090] 660 Rotary Kiln Feed Chamber

[0091] 1000 Equipment for separating and / or storing carbon dioxide (CO2)

[0092] Q Calories

Claims

1. An apparatus (100, 200, 300, 400, 500, 600) for producing cement clinker from raw materials, having - At least one heat exchanger (110, 210, 310, 410, 510, 610) located downstream of the gas flow direction and - At least one subsequent device (120, 220, 320, 420, 520, 620) in the material flow direction for preheating, calcining and sintering the raw meal, wherein the device may also consist of a series of independent devices. The at least one device (120, 220, 320, 420, 520, 620) for preheating, calcining, and sintering raw materials is connected on the primary side to the at least one heat exchanger (110, 210, 310, 410, 510, 610) located downstream of the gas flow direction and is loaded with exhaust gas. Its features are, The at least one heat exchanger (110, 210, 310, 410, 510, 610) located downstream of the gas flow direction is connected on the secondary side to a downstream device (1000) for separating and / or storing carbon dioxide (CO2) from the exhaust gas.

2. The device according to claim 1, Its features are, The apparatus used for preheating, calcination, and sintering is - Circulating fluidized bed reactor (140). - Rotary kiln (240, 340), or - Tubular reactor (440).

3. The device according to claim 2, Its features are, The tubular reactor (245) is connected to the rear of the rotary kiln in the direction of gas flow.

4. The device according to any one of claims 1 to 3, Its features are, The secondary-side equipment for separating and / or storing carbon dioxide (CO2) generates electricity using a steam generator to supply power to a water electrolysis unit, wherein the hydrogen (H2) electrolysis unit is connected on the hydrogen side to a converter in which carbon dioxide (CO2)-containing waste gas cooled in a heat exchanger is converted into methanol.

5. The device according to any one of claims 1 to 4, Its features are, A tertiary air duct (151, 251, 351, 451, 551, 651) is connected to a heat exchanger (111, 211, 311, 411, 511, 611), which guides the hot air from the clinker cooler (151, 251, 351, 451, 551, 651) back to the at least one device (120, 220, 320, 420, 520) for preheating, calcining, and sintering raw meal. The clinker cooler is connected in the material flow direction to the at least one device (120, 220, 320, 420, 520, 620) for preheating, calcining and sintering raw meal, wherein the heat exchanger (111, 211, 311, 411, 511, 611) is connected on the secondary side to the device (1000) connected to the rear for separating and / or storing carbon dioxide (CO2) from the exhaust gas.

6. A method for operating the apparatus according to claims 1 to 5, Its features are, The supply of excess fuel and atmospheric oxygen to the equipment used for preheating, calcining and sintering raw materials results in exhaust gas temperatures that allow the exhaust gas to carry just enough heat to enable the equipment used for separating and / or storing carbon dioxide (CO2) to precisely obtain the energy required for separating and / or storing the carbon dioxide (CO2) generated in the equipment used for producing cement clinker from raw materials.

7. The method according to claim 6, Its features are, - Adjust the fuel supply according to the exhaust gas temperature before the preheater.

8. The method according to claim 6 or 7, Its features are, - Treating waste gas from at least one of the devices (120, 220, 320, 420, 520, 620) for preheating, calcining, and sintering raw materials in reactors (130, 230, 330, 430, 530, 630) for regenerative thermal oxidation, and - The fuel supply is adjusted according to the exhaust gas temperature before the reactors (130, 230, 330, 430, 530, 630) used for regenerative thermal oxidation, wherein the exhaust gas temperature is between 800°C and 900°C, preferably 850°C, with an allowable deviation of 20°C.

9. The method according to any one of claims 6 to 8, Its features are, The fuel is mainly composed of secondary fuels, such as treated industrial waste and / or domestic waste, waste tires, solvent waste, or treated biomass.

10. The method according to any one of claims 6 to 9, Its features are, The sequestration also includes the chemical conversion of carbon dioxide (CO2) into other substances.

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