CN112263890A - Flue gas waste heat utilization type carbon capture method and system - Google Patents

Flue gas waste heat utilization type carbon capture method and system Download PDF

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CN112263890A
CN112263890A CN202010946262.2A CN202010946262A CN112263890A CN 112263890 A CN112263890 A CN 112263890A CN 202010946262 A CN202010946262 A CN 202010946262A CN 112263890 A CN112263890 A CN 112263890A
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flue gas
adsorbent
gas
adsorption
regeneration
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常超
杨阳
高腾飞
徐冬
孙振新
徐妍
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Guodian New Energy Technology Research Institute Co ltd
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    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2256/22—Carbon dioxide
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
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Abstract

The invention belongs to the field of carbon capture, and discloses a flue gas waste heat utilization type carbon capture method, which comprises the following steps: deeply dewatering the flue gas to obtain deeply dewatered flue gas; adsorbing and capturing carbon dioxide in the deep dehydration flue gas by an adsorbent until the deep dehydration flue gas is saturated; then, the temperature of the adsorbent is raised by using hot flue gas without water removal, desorption and regeneration of the adsorbent under the negative pressure condition are accelerated, and carbon dioxide gas is released; collecting the desorbed gas as a product gas through the processes of cooling, purification, compression and the like; and finally, cooling the adsorbent by using a cooling medium, and performing the next carbon capture cycle. The flue gas is deeply dewatered before carbon capture, so that the water content in the flue gas entering the carbon capture stage is greatly reduced, the hot flue gas without dewatering is utilized to heat the adsorbent in the regeneration stage, the regeneration efficiency of the adsorbent is improved, the cyclic service life of the adsorbent in the subsequent carbon capture stage is ensured, the regeneration cost of the adsorbent is effectively reduced, and the regeneration energy consumption is reduced.

Description

Flue gas waste heat utilization type carbon capture method and system
Technical Field
The invention relates to the field of carbon capture, in particular to a flue gas waste heat utilization type carbon capture method and a flue gas waste heat utilization type carbon capture system.
Background
At present, the power supply of China is mainly based on thermal power, the installed capacity proportion of a thermal power generating set and the coal consumption of a coal-fired power plant are difficult to realize large-scale adjustment in a short period, and coal still occupies a dominant position in the energy structure of China. Therefore, under the dual action of the high-carbon energy structure and the rapid increase of energy demand, the carbon capture and sequestration technology CCS is a poor choice for realizing low-carbon development without affecting economic development and energy strategic safety. The carbon capture and sequestration are the only existing carbon capture and sequestration which can greatly reduce the emission of electric power and industrial CO2Discharge (up to 90%) technology. If the carbon capture and sequestration technology is not adopted, the overall cost for realizing the long-term goal of slowing down climate change in China will rise by 25 percent.
In recent years, the carbon capture technology is developed rapidly, and a large number of new technologies and new methods emerge. The alcohol amine absorption method is widely applied in the field of tail flue gas carbon capture of a thermal power plant at present, carbon dioxide in flue gas of the thermal power plant is chemically absorbed by using an alcohol amine solution, and then desorption is carried out in a heating mode. In recent years, high-temperature adsorption regeneration methods have the advantages of low corrosivity and the like, and are paid attention by researchers, and carbon dioxide is absorbed by metal oxides or salts of calcium, magnesium and the like under high-temperature conditions, but the methods still have the disadvantages of difficult regeneration, low absorption rate and the like. Therefore, the problems of high energy consumption and high cost of carbon capture generally exist in the prior art.
Disclosure of Invention
The invention provides a flue gas waste heat utilization type carbon capture method and a flue gas waste heat utilization type carbon capture system in order to reduce carbon capture cost.
The scheme of the invention is as follows:
in a first aspect, a flue gas waste heat utilization type carbon capture method is provided, which includes:
in the dewatering stage, deep dewatering is carried out on the flue gas to obtain deep dewatered flue gas;
in the adsorption stage, adsorbing and capturing carbon dioxide in the deep dehydration flue gas by an adsorbent until the carbon dioxide is saturated;
in the regeneration stage, the hot flue gas without water removal is used for heating the adsorbent, so that desorption and regeneration of the adsorbent under the negative pressure condition are accelerated, and carbon dioxide gas is released;
in the refining stage, the gas obtained by desorption of the adsorbent is cooled, purified and compressed and then collected into carbon dioxide product gas;
and in the cooling stage, the cooling medium is utilized to cool the adsorbent so as to carry out the next carbon capture cycle.
Preferably, the deep dehydration is performed on the flue gas, and the step of obtaining dehydrated flue gas is as follows:
carrying out gas-liquid separation on the flue gas to remove liquid drops;
cooling the flue gas from which the liquid drops are removed to obtain crude dehydrated flue gas;
carrying out secondary dehydration on the crude dehydrated flue gas to obtain refined dehydrated flue gas;
and carrying out third dehydration on the fine dehydrated flue gas to obtain deep dehydrated flue gas.
Preferably, the temperature of the flue gas is 45-55 ℃, and the water content in the flue gas is 12-18 wt%;
the first dehydration comprises: cooling the flue gas from which the liquid drops are removed to obtain crude dehydrated flue gas with the water content of 10-15 wt%;
the second dehydration comprises the step of contacting the roughly dehydrated flue gas with an adsorption medium, wherein the adsorption medium is at least one of silica gel, zeolite, silicon oxide and aluminum oxide, and the dew point temperature of the obtained finely dehydrated flue gas is-40 ℃ to-25 ℃;
the third dehydration comprises the following steps: and contacting the refined dehydrated flue gas with an absorbent, wherein the absorbent comprises calcium oxide, and the dew point temperature of the obtained deep dehydrated flue gas is-60 ℃ to-40 ℃.
Preferably, the adsorption stage adsorbs carbon dioxide in the deep dehydration flue gas at a temperature of 10-50 ℃ and a pressure of 1.1-2.0 atm.
Preferably, the adsorbent is one or more of 13X-APG zeolite, 13X-APG-IIA zeolite, 5A molecular sieve, amino mesoporous material, NaX, NaY zeolite, silicon-titanium molecular sieve, mesoporous material, metal organic framework material, silica gel, activated aluminum and carbon material.
Preferably, one or more layers of the adsorbent are filled in an adsorption tower, and after the deep dehydration flue gas is introduced into the adsorption tower, the adsorbent adsorbs carbon dioxide in the deep dehydration flue gas at the temperature of 10-50 ℃ and the pressure of 1.1-2.0 atm.
Preferably, the adsorbent is desorbed and regenerated in the regeneration stage by reducing the pressure of the adsorption tower by using a vacuum pump.
Preferably, the temperature of the hot flue gas without water removal in the regeneration stage is 90-150 ℃.
Preferably, the cooling medium is water, air or a low-temperature gas or liquid of other processes;
the temperature of the cooling medium is-30 ℃, and the temperature of the adsorbent is reduced to 30-60 ℃ by using the cooling medium, and then the next carbon capture cycle is carried out.
In a second aspect, a flue gas waste heat utilization type carbon capture system is provided, which is applied to the above method, and is characterized in that the system comprises:
the water removal device is used for deeply removing water from the flue gas to obtain deeply-dehydrated flue gas;
the adsorption and regeneration device is communicated with the water removal device and is used for adsorbing and capturing carbon dioxide in the deep-dehydration flue gas until the deep-dehydration flue gas is saturated through an adsorbent filled in the adsorption and regeneration device, and then introducing hot flue gas which is not subjected to water removal to heat the adsorbent, so that desorption and regeneration of the adsorbent under a negative pressure condition are accelerated, and carbon dioxide gas is released;
the refining device is communicated with the adsorption and desorption device and is used for receiving the gas desorbed by the adsorbent, cooling, purifying and compressing the gas, and collecting the gas as carbon dioxide product gas;
and the cooling device is communicated with the adsorption and desorption device and is used for introducing a cooling medium into the adsorption and desorption device and cooling the adsorbent by using the cooling medium so as to carry out the next carbon capture cycle.
Preferably, the adsorption and regeneration device continuously captures carbon dioxide gas in the flue gas by using a vacuum pressure-variable temperature-variable coupling process;
the adsorption and regeneration device comprises four adsorption towers which are arranged in parallel, and each adsorption tower sequentially realizes eight steps of adsorption, primary pressure equalization, temperature rise, desorption, blowing, secondary pressure equalization, pressurization and temperature reduction in one carbon capture cycle.
Compared with the prior art, the technical scheme of the invention has the following advantages and positive effects:
(1) the flue gas is deeply dewatered before carbon capture, so that the water content in the deep-dewatered flue gas entering a carbon capture stage subsequently is greatly reduced, low-energy-consumption operation in an adsorption stage is guaranteed, and the regeneration cost of the adsorbent is effectively reduced;
(2) the hot flue gas which is not dewatered is used for heating the adsorbent in the regeneration stage, so that the regeneration efficiency of the adsorbent is improved, and the regeneration energy consumption is reduced;
(3) the carbon capture method has low corrosivity, no secondary pollution and easy realization of automatic operation.
Additional features and advantages of the inventive arrangements are described in detail in the detailed description which follows.
Drawings
FIG. 1 is a sequence diagram of steps of a flue gas waste heat utilization type carbon capture method;
fig. 2 is a schematic process flow diagram of a flue gas waste heat utilization type carbon capture device.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating embodiments of the invention, are given by way of illustration and explanation only, not limitation.
In order to reduce the carbon capture energy consumption, the first aspect of the invention provides a flue gas waste heat utilization type carbon capture method, as shown in fig. 1, the method comprises the following steps:
and a water removal stage S100, which is used for deeply removing water from the flue gas to obtain deeply-dehydrated flue gas.
And an adsorption stage S200, namely adsorbing and capturing the carbon dioxide in the deep dehydration flue gas by an adsorbent until the deep dehydration flue gas is saturated.
And in the regeneration stage S300, the temperature of the adsorbent is raised by using hot flue gas without water removal, desorption and regeneration of the adsorbent under the negative pressure condition are accelerated, and carbon dioxide gas is released.
And a refining stage S400, wherein the gas obtained by desorbing the adsorbent is cooled, purified and compressed and then collected as carbon dioxide product gas.
And a cooling stage S500, in which the adsorbent is cooled by using a cooling medium so as to carry out the next carbon capture cycle.
In the scheme of the invention, the flue gas is deeply dewatered before adsorption and capture, so that the water content in the deeply dewatered flue gas entering the adsorption stage is greatly reduced, the carbon capture process is operated with low energy consumption, and the regeneration cost of the adsorbent is effectively reduced; in addition, the hot flue gas without water removal is utilized to heat the adsorbent in the regeneration stage, so that the regeneration efficiency of the adsorbent is improved, and the regeneration energy consumption is reduced.
Further, in the water removal step, the deep water removal is performed on the flue gas to obtain deep-dehydrated flue gas, and the method specifically comprises the following steps:
step (1), carrying out gas-liquid separation on the flue gas to remove liquid drops;
step (2) carrying out primary dehydration on the flue gas without liquid drops to obtain crude dehydrated flue gas;
performing secondary dehydration on the crude dehydrated flue gas to obtain refined dehydrated flue gas;
step (4) carrying out third dehydration on the fine dehydrated flue gas to obtain deep dehydrated flue gas;
in the step (1), the temperature of the flue gas is 45-55 ℃, and the water content in the flue gas is 12-18 wt%. According to a preferred embodiment, a steam-water separator is used for carrying out gas-liquid separation on the flue gas, so as to remove liquid drops, dust and the like in the flue gas.
In step (2), the first dehydration comprises: and cooling the flue gas from which the liquid drops are removed. Optionally, the flue gas from which the liquid drops are removed is cooled by a heat exchanger, the temperature of the obtained crude dehydrated flue gas is 40-48 ℃, and the water content in the crude dehydrated flue gas is 10-15 wt%, preferably 8-12 wt%.
In step (3), the second dehydration comprises: contacting the crude dehydrated flue gas with an adsorption medium. The adsorption medium is preferably at least one of silica gel, zeolite, silica and alumina, and the adsorption saturation amount of the adsorption medium is 5-45 wt%, preferably 15-30 wt%. The dew point temperature of the refined dehydrated smoke obtained after the second dehydration is-40 ℃ to-25 ℃, and the dew point temperature is preferably-40 ℃ to-30 ℃.
In step (4), the third dehydration comprises: contacting the refined dehydrated smoke with an absorbent. The absorbent is preferably calcium oxide, and the dosage of the absorbent is as follows: the dosage ratio of the calcium oxide in g to the refined dehydrated smoke in m3 is 10-100: 1, preferably 15 to 50: 1. the dew point temperature of deep dehydration smoke obtained after the third dehydration is-60 ℃ to-40 ℃, and preferably-60 ℃ to-50 ℃.
In addition, in order to improve the resource utilization rate, for example, silica gel used as an adsorption medium can be regenerated at high temperature and then put into the second dehydration process for recycling, and calcium oxide contacted with the refined dehydrated flue gas can also be sent to a wet desulphurization device for recycling.
Further, the adsorbent is one or more of 13X-APG zeolite, 13X-APG-IIA zeolite, 5A molecular sieve, amino mesoporous material, NaX, NaY zeolite, silicon-titanium molecular sieve, mesoporous material, metal organic framework material, silica gel, activated aluminum and carbon material.
In practical application, the adsorbent is filled in the adsorption tower in one or more layers, the deep dehydration flue gas is introduced into the adsorption tower, and the adsorbent is used for absorbing carbon dioxide gas in the deep dehydration flue gas under preset conditions. Illustratively, in the adsorption stage, the carbon dioxide in the deep dehydration flue gas is adsorbed under the conditions that the temperature is 10-50 ℃ and the pressure is 1.1-2.0 atm. The deep dehydration flue gas can also cool the adsorbent, thereby improving the capacity of the adsorbent for adsorbing and capturing carbon dioxide gas.
When the adsorbent is saturated with carbon dioxide gas, the adsorbent enters a regeneration stage, and desorption regeneration is performed on the adsorbent by reducing the pressure of the adsorption tower through a vacuum pump, so that carbon dioxide gas and other miscellaneous gases are released.
And in the regeneration stage, high-temperature flue gas before desulfurization is introduced into the adsorption tower, and the adsorbent is heated by the high-temperature flue gas, so that the temperature of the adsorbent is raised to the regeneration temperature, the adsorbent is promoted to desorb and regenerate, and the release of carbon dioxide gas is accelerated. Wherein the smoke temperature of the hot smoke without dewatering is 90-150 ℃, and the regeneration temperature of the adsorbent is 80-140 ℃.
In the refining stage, the gas obtained by desorption is cooled, purified, compressed and the like, and then is collected into product gas, and the product gas is high-purity carbon dioxide.
In the scheme of the invention, the cooling medium in the cooling stage is water, air or low-temperature gas or liquid obtained by other processes, and preferably, the temperature of the cooling medium is-30 ℃. And (3) introducing a cooling medium into the adsorption tower after the regeneration stage, cooling the regenerated adsorbent by using the cooling medium, and starting the next carbon capture cycle after the temperature of the adsorbent is reduced to 30-60 ℃.
Further, the present invention also provides a flue gas waste heat utilization type carbon capture system, as shown in fig. 2, the carbon capture system includes:
the water removal device S1 is used for deeply removing water from the flue gas to obtain deeply-dehydrated flue gas;
the adsorption and regeneration device S4 is communicated with the water removal device S1 and is used for adsorbing and capturing carbon dioxide in the deep-dehydration flue gas until the carbon dioxide is saturated by the adsorbent filled in the adsorption and regeneration device, and then introducing hot flue gas without water removal to heat the adsorbent, so that desorption and regeneration of the adsorbent under the negative pressure condition are accelerated, and carbon dioxide gas is released;
the refining device S2 is communicated with the adsorption and desorption device S4 and is used for receiving the gas desorbed by the adsorbent, cooling, purifying and compressing the gas to collect the gas as carbon dioxide product gas;
and the cooling device S5 is communicated with the adsorption and desorption device S4 and is used for introducing a cooling medium into the adsorption and desorption device S4 and cooling the adsorbent by using the cooling medium so as to carry out the next carbon capture cycle.
According to a preferred embodiment, as shown in fig. 2, the adsorption and regeneration device S4 of the present invention employs a vacuum pressure-swing temperature-change coupling process to continuously adsorb and capture CO in flue gas or other industrial tail gas2The gas comprises four adsorption towers (T1-T4) which are arranged in parallel, and each adsorption tower is automatically regulated by using a program control valve V1-V20 to sequentially realize eight steps of adsorption, primary pressure equalization, temperature rise, desorption, secondary pressure equalization, pressurization and temperature reduction in one carbon capture cycle.
Specifically, step (1) adsorption: adsorbing and trapping carbon dioxide in the flue gas by using an adsorbent under the conditions of temperature of 10-50 ℃ and pressure of 1.1-2 atm;
in this step, the deep-dehydrated flue gas with dew point temperature of-60 ℃ to-40 ℃ is introduced into an adsorption tower (the flue gas dehydration step is the method, and the description is omitted here), and the deep-dehydrated flue gas can cool the adsorbent at the same time; the cold materials are adsorbed, so that the adsorption and trapping efficiency is improved, the adsorbent in the adsorption tower can be cooled, the operation conditions are controlled, and the adsorption capacity is effectively ensured not to be reduced while the adsorbent is cooled;
step (2), primary pressure equalizing: carrying out pressure equalization with another adsorption tower with lower pressure for carrying out the operation of the step (6), wherein the pressure equalization comprises reverse or reverse pressure equalization, so that the pressure in the adsorption tower in the step is reduced to the normal pressure; the nitrogen gas of the weak adsorption component in the adsorption tower is discharged at the same time of pressure equalization, and the CO in the desorption gas is improved2The purity of (2);
step (3), heating: heating the adsorbent to desorb the adsorbent, including direct heating or indirect heating, such as heating the adsorbent by a heating medium or electrically heating the adsorbent to raise the temperature of the adsorbent in the adsorption tower to 80-150 ℃;
the adsorption tower is internally provided with a heat transfer element, such as a fin heater, a shell-and-tube heater and the like, and the heat transfer element heats the adsorbent after being electrified; the heating heat source can be low-grade waste heat of other processes of the plant, such as steam, hot gas or hot liquid; preferably, the heating medium can also be hot flue gas without water removal, and the temperature of the hot flue gas is 90-150 ℃;
and (4) desorption: reversely or reversely vacuumizing the adsorption tower by using a vacuum pump to desorb the adsorbent, wherein the vacuum pressure is 1 kPa-10 kPa; the gas obtained by desorption of the adsorbent enters a product gas tank for recovery and storage after the steps of cooling, purification, compression and the like;
purging in step (5): the product gas reversely sweeps the carbon dioxide gas remained in the adsorption tower; the purge gas can also comprise other carrier gases such as nitrogen and the like, but the dosage needs to be controlled to ensure the purity of the product gas;
step (6) secondary pressure equalizing: the pressure equalizing is carried out with another adsorber with higher pressure operated in the step (2), so that the power consumption of conveying equipment is saved;
pressurizing in step (7): pressurizing flue gas to the pressure in the tower during adsorption, pressurizing by using cold flue gas, and cooling the adsorbent while adsorbing;
and (8) cooling: direct, indirect or direct indirect simultaneous cooling of the adsorbent; the low-temperature tail gas flowing out of the other adsorption tower subjected to the operation in the step (1) can reversely pass through the regeneration adsorption tower to directly cool the adsorbent in the tower, and a cooling medium can be used for assisting in cooling the adsorbent bed layer, so that the cooling time is shortened; when the temperature of the adsorbent is reduced to 30-60 ℃, stopping operation, and then carrying out the next carbon capture cycle; the cooling medium is cold air, water, or low-temperature gas, liquid and the like of other processes, and preferably, the temperature of the cooling medium is-30 ℃ to 30 ℃.
In the adsorption/desorption circulation process, the coupling desorption pressure in the steps (3) to (5) is 1kPa to 10kPa, and the desorption temperature is 80 ℃ to 150 ℃; and (1) cooling the adsorbent by using deep-dehydration flue gas, and (8) cooling the adsorbent by using a cooling medium.
The carbon capture process is illustrated below by way of a specific example for the purpose of better understanding only of the present invention.
The carbon capture method in the embodiment of the invention specifically comprises the following steps:
introducing hot flue gas into a dewatering device S1, wherein the temperature of the hot flue gas is 50 ℃, the water content in the hot flue gas is 15 wt%, and the hot flue gas is subjected to gas-liquid separation and three dewatering processes in the dewatering device in sequence to finally obtain low-temperature and dry deep-dewatered flue gas, and the dew point temperature of the deep-dewatered flue gas is-55 ℃;
taking the working flow of the adsorption tower T1 as an example, opening valves V12, V16 and V20, introducing the deep-dehydration flue gas into the adsorption tower T1 from the bottom under the conditions of near normal pressure and normal temperature, filling the adsorption tower with adsorbents such as zeolite for trapping carbon dioxide gas, discharging the tail gas into a flue through valves V16 and V20, and closing the valve V12 after the adsorbents are saturated with carbon dioxide;
opening a vacuum pump P2 and a valve V3, directly feeding hot flue gas (the temperature is 140 ℃) which is not subjected to water removal into an adsorption tower T1 from a bypass of a water removal device S1, heating the adsorbent by using the hot flue gas, raising the temperature of the adsorbent to the regeneration temperature of 80-140 ℃, and accelerating the desorption of the adsorbent;
meanwhile, starting a vacuum pump P3 until the vacuum pressure in the adsorption tower T1 is 3KPa-6KPa, carrying out pressure reduction desorption on the adsorbent, reversely purging carbon dioxide gas remained in the adsorption tower T1 by using a small amount of nitrogen under the vacuum condition, and collecting discharged gas in a product gas tank S3 after the steps of cooling, purifying, compressing and the like in a refining device S2 to obtain high-purity carbon dioxide product gas;
and (3) pressurizing the regenerated adsorbent, opening valves V2, V3, V7 and V11, continuously introducing cold air with the temperature of-30 ℃ into the adsorption tower T1 by using a cooling device S5, cooling the adsorbent until the temperature of the adsorbent is reduced to 50-60 ℃, and then starting the next carbon capture cycle operation.
Compared with the prior art, the technical scheme of the invention has the following advantages and positive effects:
(1) the flue gas is deeply dewatered before carbon capture, so that the water content in the deeply dewatered flue gas entering a subsequent carbon capture stage is greatly reduced, low-energy-consumption operation of the subsequent carbon capture stage is ensured, and meanwhile, the regeneration cost of the adsorbent is effectively reduced;
(2) the dry and low-temperature deep-dehydration flue gas obtained after dehydration reduces the temperature of flue gas at the inlet of the desulfurizing tower, thereby reducing the water loss of the desulfurizing tower;
(3) the hot flue gas which is not dewatered is used for heating the adsorbent in the regeneration stage, so that the regeneration efficiency of the adsorbent is improved, and the regeneration energy consumption is reduced;
(4) the carbon capture method has low corrosivity, no secondary pollution and easy realization of automatic operation.
The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, but these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall into the protection scope of the invention.

Claims (10)

1. A flue gas waste heat utilization type carbon capture method is characterized by comprising the following steps:
in the dewatering stage, deep dewatering is carried out on the flue gas to obtain deep dewatered flue gas;
in the adsorption stage, adsorbing and capturing carbon dioxide in the deep dehydration flue gas by an adsorbent until the carbon dioxide is saturated;
in the regeneration stage, the hot flue gas without water removal is used for heating the adsorbent, so that desorption and regeneration of the adsorbent under the negative pressure condition are accelerated, and carbon dioxide gas is released;
in the refining stage, the gas obtained by desorption of the adsorbent is cooled, purified and compressed and then collected into carbon dioxide product gas;
and in the cooling stage, the cooling medium is utilized to cool the adsorbent so as to carry out the next carbon capture cycle.
2. The method according to claim 1, wherein the deep water removal of the flue gas to obtain dehydrated flue gas comprises:
carrying out gas-liquid separation on the flue gas to remove liquid drops;
cooling the flue gas from which the liquid drops are removed to obtain crude dehydrated flue gas;
carrying out secondary dehydration on the crude dehydrated flue gas to obtain refined dehydrated flue gas;
and carrying out third dehydration on the fine dehydrated flue gas to obtain deep dehydrated flue gas.
3. The method according to claim 2, wherein the temperature of the flue gas is 45-55 ℃, and the water content in the flue gas is 12-18 wt%;
the first dehydration comprises: cooling the flue gas from which the liquid drops are removed to obtain a crude dehydrated flue gas with the water content of 10-15 wt%;
the second dehydration comprises the step of contacting the roughly dehydrated flue gas with an adsorption medium, wherein the adsorption medium is at least one of silica gel, zeolite, silicon oxide and aluminum oxide, and the dew point temperature of the obtained finely dehydrated flue gas is-40 ℃ to-25 ℃;
the third dehydration comprises the following steps: and contacting the refined dehydrated flue gas with an absorbent, wherein the absorbent comprises calcium oxide, and the dew point temperature of the obtained deep dehydrated flue gas is-60 ℃ to-40 ℃.
4. The method of claim 1, wherein the adsorbent is one or more of zeolite 13X-APG, zeolite 13X-APG-IIA, molecular sieve 5A, amine-based mesoporous material, NaX, NaY zeolite, silicon titanium molecular sieve, mesoporous material, metal organic framework material, silica gel, activated aluminum, and carbon material.
5. The method according to claim 1, wherein one or more layers of the adsorbent are filled in an adsorption tower, and after the deep dehydration flue gas is introduced into the adsorption tower, the adsorbent adsorbs carbon dioxide in the deep dehydration flue gas under the conditions of the temperature of 10-50 ℃ and the pressure of 1.1-2.0 atm.
6. The method of claim 5, wherein the adsorbent is desorbed and regenerated by reducing the pressure of the adsorption column by a vacuum pump during the regeneration stage.
7. The method according to claim 1, characterized in that the temperature of the hot flue gases without water removal in the regeneration stage is 90-150 ℃.
8. The method of claim 1, wherein the cooling medium is water, air, or other cryogenic gas or liquid;
the initial temperature of the cooling medium is-30 ℃, and the cooling medium is utilized to reduce the temperature of the adsorbent to 30-60 ℃ and then the next carbon capture cycle is carried out.
9. A flue gas waste heat utilization type carbon capture system applied to the method of any one of claims 1 to 8, wherein the system comprises:
the water removal device is used for deeply removing water from the flue gas to obtain deeply-dehydrated flue gas;
the adsorption and regeneration device is communicated with the water removal device and is used for adsorbing and capturing carbon dioxide in the deep-dehydration flue gas until the deep-dehydration flue gas is saturated through an adsorbent filled in the adsorption and regeneration device, and then introducing hot flue gas which is not subjected to water removal to heat the adsorbent, so that desorption and regeneration of the adsorbent under a negative pressure condition are accelerated, and carbon dioxide gas is released;
the refining device is communicated with the adsorption and desorption device and is used for receiving the gas desorbed by the adsorbent and collecting the gas as a carbon dioxide product gas after cooling, purifying and compressing the gas;
and the cooling device is communicated with the adsorption and desorption device and is used for introducing a cooling medium into the adsorption and desorption device and cooling the adsorbent by using the cooling medium so as to carry out the next carbon capture cycle.
10. The system of claim 9, wherein the adsorption and regeneration device continuously captures carbon dioxide gas in the flue gas by using a vacuum pressure-swing temperature-change coupling process;
the adsorption and regeneration device comprises four adsorption towers which are arranged in parallel, and each adsorption tower sequentially realizes eight steps of adsorption, primary pressure equalization, temperature rise, desorption, blowing, secondary pressure equalization, pressurization and temperature reduction in one carbon capture cycle.
CN202010946262.2A 2020-09-10 2020-09-10 Flue gas waste heat utilization type carbon capture method and system Pending CN112263890A (en)

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