Vacuum phase change condensation and carbon capture cooperative system and operation method

Abstract

The invention discloses a vacuum phase change condensation and carbon capture cooperative system and an operation method, and belongs to the technical field of energy conservation and consumption reduction of coal-fired units. The system is mainly composed of a condenser body, a CO2 absorbent supply device, a corrugated pipe type elastic condenser, a product recovery and reuse device and other core assemblies. According to the system, the vacuum environment of the condenser body is maintained through the vacuum pump, and efficient phase-change condensation of working media is achieved. The CO2 absorbent supply device is in closed communication with the condenser body, high-activity CO2 absorbent is continuously conveyed into the condenser, the absorbent and CO2 carried in steam are promoted to be subjected to efficient chemical reaction, and stable carbonate products are directionally generated. The mixed product with carbonate treated by the condenser is subjected to efficient solid-liquid separation through the centrifugal separator, and the obtained carbonate product can be directionally conveyed to the desulfurization tower to be recycled as a high-quality desulfurization agent, so that gradient utilization of resources is realized, the desulfurization process cost is remarkably reduced, and meanwhile, the environmental emission of solid wastes is reduced.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of coal-fired unit energy saving and consumption reduction, and particularly relates to a vacuum phase change condensation and carbon capture collaborative system and an operation method. BACKGROUND

[0002] In the industrial production processes of electric power, chemical industry and the like, a condenser is usually required to operate in a vacuum environment to improve condensation efficiency as a core equipment for realizing phase change condensation of a working medium. At the same time, these industrial processes produce a large amount of tail gas containing carbon dioxide, and carbon capture technology has become a key means for reducing greenhouse gas emissions. However, on the one hand, the traditional carbon capture system needs to independently set up a reaction device, which not only increases the equipment investment and operation and maintenance cost, but also lacks an effective collaborative working mechanism with the condensation system, resulting in low overall energy efficiency; on the other hand, the internal vacuum degree of the condenser is easily affected by working condition fluctuations, and this instability directly affects the carbon capture reaction and reduces the absorption efficiency of carbon dioxide; furthermore, the existing technology has a rough treatment method for reaction products generated in the carbon capture process, which are usually disposed as waste, failing to realize the recycling of resources and causing serious waste of resources. In addition, the existing system lacks intelligent control means and cannot automatically adjust the operating parameters according to the real-time working conditions, further restricting the overall performance of the system. These problems seriously affect the economy and environmental benefits of industrial waste gas treatment. SUMMARY

[0003] The purpose of the present application is to overcome the shortcomings of the prior art, and to provide a vacuum phase change condensation and carbon capture collaborative system and an operation method, so as to solve the problems of the traditional carbon capture technology and the condensation process being independent of each other, high operation cost, poor capture efficiency and waste of product resources in the prior art.

[0004] To achieve the above-mentioned purpose, the following technical solutions are adopted in the present application: A vacuum phase change condensation and carbon capture collaborative system, comprising a CO2 absorbent storage tank, a condenser and a centrifugal separator. The condenser is provided with a steam input port, and a steam pipeline is communicated with the steam input port. A CO2 absorbent output port is arranged in the condenser, and the CO2 absorbent output port is communicated with the CO2 absorbent storage tank. The CO2 absorbent output port is arranged beside the steam input port. The output pipe of the condenser is communicated with the centrifugal separator. The centrifugal separator is provided with two output pipelines, one of which is communicated with a desulfurization tower, and the other of which is communicated with a cooling water system. A cooling water pipe is arranged in the condenser, and cooling water is introduced into the cooling water pipe. The condenser is further communicated with a vacuum pump.

[0005] Further improvements of the present application are as follows: Preferably, the steam input port is arranged at the upper end of the condenser, and the CO2 absorbent output port is annularly arranged around the steam input port.

[0006] Preferably, the CO2 absorbent output port is provided with a porous nozzle.

[0007] Preferably, the cooling water pipe is a corrugated pipe.

[0008] Preferably, the cooling water pipe is arranged in the condenser in a spiral or serpentine shape and is arranged below the steam input port and the CO2 absorbent output port.

[0009] Preferably, a metering pump is arranged between the CO2 absorbent output port and the CO2 absorbent storage tank.

[0010] Preferably, a steam flow meter or a CO2 concentration sensor is arranged on the steam pipeline, the steam flow meter or the CO2 concentration sensor is electrically connected with a PLC controller, and the PLC controller is electrically connected with the metering pump.

[0011] Preferably, a capacitive vacuum gauge is arranged in the condenser.

[0012] Preferably, the PLC controller is electrically connected with the vacuum pump and the capacitive vacuum gauge.

[0013] A method for operating the above-mentioned vacuum phase change condensation and carbon capture synergistic system, comprising the following steps: S1, starting the vacuum pump to maintain the vacuum degree inside the condenser at 0.01 MPa; S2, the CO2 absorbent storage tank injects CO2 absorbent into the condenser through the CO2 absorbent output port; S3, steam is condensed into water in the condenser, and the absorbent reacts with CO2 carried in the steam to generate carbonate; S4, the mixture obtained by the reaction enters the centrifugal separator, and the mixture is separated into carbonate and condensed water by the centrifugal separator, the carbonate is dried and input into the desulfurization tower, and the condensed water flows back to the cooling water system.

[0014] Compared with the prior art, the present application has the following beneficial effects: The application discloses a vacuum phase change condensation and carbon capture system, which integrates CO2 capture chemical reaction into the physical process of steam phase change condensation. The system mainly comprises a condenser body, a CO2 absorbent supply device, a corrugated tube type elastic condenser, a product recovery and recycling device and the like. The system maintains the vacuum environment of the condenser body through a vacuum pump to realize efficient phase change condensation of the working medium. The CO2 absorbent supply device is in closed communication with the condenser body and continuously supplies high-activity CO2 absorbent into the condenser to promote the efficient chemical reaction between the absorbent and CO2 carried in the steam and to direct the generation of stable carbonate products. The mixed products with carbonates after the condenser treatment are subjected to efficient solid-liquid separation through a centrifugal separator, and the obtained carbonate products can be directed to a desulfurization tower for recycling as high-quality desulfurizing agent, which realizes the cascade utilization of resources, significantly reduces the desulfurization process cost and reduces the environmental emission of solid waste. The system has the following advantages: (1) The vacuum phase change condensation and carbon capture process are organically integrated to form an integrated system in cooperative operation.

[0015] (2) The long-term stable operation of the system is ensured through the corrugated tube type elastic structure.

[0016] (3) A complete product resource recycling closed loop is constructed, and the generated carbonates are recycled as desulfurizing agent for the boiler system. In particular, the system utilizes the ideal low-temperature environment provided by the condensation process to make the CO2 capture process no longer exist as an independent "attached" process with high energy consumption, but naturally integrate into the key link of the condensation process. The energy utilization and carbon emission reduction are synergistically enhanced, the energy consumption demand and equipment investment cost of the carbon capture process are essentially reduced, and the system has significant technical and economic advantages. BRIEF DESCRIPTION OF DRAWINGS

[0017] Figure 1 is a system structure diagram of the application; Wherein: 1, CO2 absorbent storage tank; 2, metering pump; 3, condenser; 4, cooling water pipe; 5, spray head; 6, steam pipeline; 7, vacuum pump; 8, output pipe; 9, centrifugal separator. DETAILED DESCRIPTION

[0018] The application will be further described in detail below with reference to the drawings: The embodiments of the application are described in detail below, and examples of the embodiments are shown in the drawings, wherein the same or similar reference numerals represent the same or similar elements or elements with the same or similar functions throughout. The embodiments described below with reference to the drawings are exemplary and are only used to explain the application and cannot be understood as a limitation of the application.

[0019] The condenser and the carbon capture system in the industrial production process usually operate independently, resulting in high equipment investment and operation cost, and insufficient coordination between the two. The internal vacuum degree of the condenser is easily affected by the working condition fluctuation, the carbon capture reaction condition is difficult to stabilize, and the generated product is often treated as waste, without realizing resource utilization. For example, in the field of electric power or chemical industry, the tail gas containing carbon dioxide needs to be treated by a separately arranged carbon capture device, increasing the equipment complexity and energy consumption.

[0020] The application discloses a vacuum phase change condensation and carbon capture coordination system, comprising a CO2 absorbent storage tank 1, a condenser 3 and a centrifugal separator 9. The steam input port of the condenser 3 is communicated with a steam pipeline 6, and the condenser 3 is provided with a CO2 absorbent output port, which is communicated with the CO2 absorbent storage tank 1 and is arranged beside the steam input port. The CO2 absorbent output port is used for spraying the CO2 absorbent obtained from the CO2 absorbent storage tank 1 into the interior of the condenser 3.

[0021] The output pipe 8 of the condenser 3 is communicated with the centrifugal separator 9, and the centrifugal separator 9 is provided with two output pipelines, one of which is communicated to a desulfurization tower, and the other is communicated to a cooling water recovery place. The condenser 3 is provided with a cooling water pipe 4 in the interior, and the cooling water pipe 4 is communicated with cooling water; and the condenser 3 is further communicated with a vacuum pump 7.

[0022] The CO2 absorbent storage tank 1 is used for storing alkaline solution or amine absorbent, and can be a sealed container made of corrosion-resistant material, connected with the condenser through a pipeline to realize continuous supply of absorbent, pressurized and injected into the condenser 3 through a metering pump, and the flow range is 100-500 kg / h. The body of the condenser 3 adopts a horizontal shell and tube structure, and the inside is maintained at a vacuum degree of 0.01 MPa by a vacuum pump for phase change condensation of steam; the steam input port of the condenser 3 is flange-connected with a steam pipeline for stable input of high-temperature steam. The centrifugal separator 9 realizes gas-liquid-solid three-phase separation by centrifugal force generated by high-speed rotation, and can adopt a horizontal spiral unloading structure, and the separated liquid can be returned to the cooling water circulation system, and the solid product is transported to the desulfurization tower for resource utilization. The specific process is that the steam containing carbon dioxide enters the condenser 3 through a pipeline and fully contacts with the absorbent 3 sprayed from the absorbent output port. In the vacuum environment, the steam is rapidly condensed to release latent heat, and the carbon dioxide in the steam reacts with the carbon dioxide absorbent to generate carbonate. The mixture of condensed liquid and reaction product flows into the centrifugal separator 9, and after separation, the solid product is transported to the desulfurization tower as a desulfurizing agent, and the liquid part is returned to the cooling water system for recycling. The cooling water pipe continuously brings in circulating water to take away the condensation heat, and the vacuum pump 7 adjusts the internal pressure in real time to ensure the stability of the reaction conditions. The present application realizes the synchronous performance of steam condensation and carbon dioxide absorption, the reaction product can be effectively separated and resource utilization, and the solid waste treatment pressure is reduced.

[0023] In some embodiments of the present application, the steam input port is arranged at the upper end of the condenser 3, and the CO2absorbent output port is arranged annularly around the steam input port. Arranging the steam input port at the upper end of the condenser 3 means that the steam inlet is located in the top region of the condenser, which can be achieved by connecting a vertical pipe or an inclined pipe to the top of the condenser. This arrangement facilitates the downward diffusion of steam under the action of gravity and the full contact of the absorbent. The annular arrangement of the CO2absorbent output port around the steam input port means that a plurality of absorbent outlets are arranged in a ring around the steam inlet. This can be achieved by using a ring-shaped pipe or a multi-hole nozzle array around the steam inlet. This structure can uniformly cover the steam diffusion path with absorbent and enhance the contact efficiency of gas-liquid two-phase. When the CO2-containing steam enters from the steam input port at the upper end of the condenser, it diffuses downward in a vacuum environment. At this time, the annularly distributed CO2absorbent output port uniformly sprays the absorbent to the steam diffusion area, forming an absorbent atomization layer around the steam flow. The steam and the absorbent continue to contact during the diffusion process, and the CO2is captured by the absorbent and reacts. This layout avoids the problem of uneven coverage of the absorbent caused by local concentration of steam, and at the same time, the downward flow direction of the steam and the spray of the absorbent can be used to achieve large-area contact and prolong the reaction time. The present application directly covers the steam diffusion area with the annularly distributed absorbent outlet, without the need for flow guiding devices to achieve immediate contact between the steam and the absorbent. At the same time, the natural diffusion path formed by the high arrangement of the steam inlet reduces the escape of unreacted steam.

[0024] In some embodiments of the present application, the CO2absorbent output port is provided with a multi-hole nozzle. The multi-hole nozzle is a atomization device with a plurality of small holes, which can be realized by using a metal sintered porous structure or a ceramic microporous structure. Its function is to disperse the CO2absorbent into fine droplets and increase the contact area with the steam. Specifically, during the operation of the condenser, the multi-hole nozzle uniformly atomizes the CO2absorbent from the CO2absorbent storage tank to form a droplet group. These droplets fully contact with the high-temperature CO2-containing steam entering the steam input port, and the latent heat released by phase change condensation accelerates the chemical reaction between the absorbent and CO2. Due to the atomization effect of the multi-hole structure, the uniformity of the absorbent droplet distribution is improved, avoiding the problem of local high concentration or insufficient reaction caused by traditional single-hole injection.

[0025] In some embodiments of the present application, the cooling water pipe 4 is a corrugated pipe, with both ends connected to the condenser body through flanges. The corrugated pipe refers to a tubular component with a continuous undulating corrugated structure on the surface, which can be made of stainless steel or corrosion-resistant alloy material, and further can be made of 316L austenitic stainless steel corrugated pipe. The corrugated structure of the corrugated pipe can increase the heat exchange area, and at the same time form a turbulent effect through the gap between the corrugations to enhance the heat exchange efficiency between the cooling water and the steam. The undulating structure also allows the pipe to produce axial extension deformation when it expands and contracts with temperature changes, avoiding stress concentration caused by temperature changes.

[0026] In some embodiments of the present application, the cooling water pipe 4 is arranged in a spiral or serpentine manner in the condenser 3, and is arranged below the steam input port and the CO2 absorbent output port. The spiral or serpentine arrangement refers to the arrangement of the cooling water pipe in a continuous curved form inside the condenser, which can be formed by mechanically bending metal pipe material into a regular wave shape or spiral shape structure. This form can increase the contact area between steam and cooling pipe by lengthening the cooling water flow path. Arranged below the steam input port and the absorbent output port means that the cooling pipe is located at a downstream position of the steam inlet and the absorbent spraying area, so that the steam contacts the cooling pipe when it flows downward after being fully mixed with the absorbent. Specifically, the steam and the CO2 absorbent are mixed in the upper part of the condenser and flow downward due to gravity. The spiral or serpentine arranged cooling pipe forms multiple layers of staggered heat exchange surfaces, and the CO2 carried by the steam continuously contacts the surface of the cooling pipe during the downward movement. The cooling water flows in the pipe in the opposite direction, absorbs the latent heat released by the condensation of the steam through the pipe wall, and at the same time reduces the temperature of the mixed gas to promote the CO2 absorption reaction. The curved form of the cooling pipe causes turbulence in the steam flow path, prolonging the residence time of the gas in the condenser.

[0027] In some embodiments of the present application, a metering pump 2 is arranged between the CO2 absorbent output port and the CO2 absorbent storage tank 1. The metering pump 2 refers to a pump body device capable of accurately controlling the delivery amount of fluid, which can be realized by using a plunger type or diaphragm type structure, and its function is to adjust the injection amount of carbon dioxide absorbent per unit time to ensure the stable mixing ratio of the absorbent and the carbon dioxide containing steam. During the operation of the condenser 3, when the steam enters the condenser 3 through the steam pipeline, the metering pump 2 dynamically adjusts the supply rate of the absorbent according to the preset parameters or real-time feedback signals (such as steam flow or carbon dioxide concentration). For example, when the steam flow increases, the metering pump can simultaneously increase the output amount of the absorbent to avoid the decrease of carbon dioxide capture efficiency caused by insufficient amount of absorbent; on the contrary, when the steam flow decreases, the amount of absorbent can be reduced to reduce the operation cost. In this way, the system can automatically match the supply of absorbent with the steam working condition, while reducing the manual adjustment error.

[0028] In some embodiments of the present application, a steam flow meter or a CO2 concentration sensor is provided on the steam pipeline 6, which is electrically connected to a PLC controller, and the PLC controller is electrically connected to the metering pump 2. The steam flow meter refers to a device for measuring the volume flow of steam in the steam pipeline, which can be realized by a turbine flow meter or an orifice flow meter. By monitoring the steam flow in real time, the PLC controller can provide the basis for adjusting the operating parameters of the metering pump.

[0029] The CO2 concentration sensor refers to a device for detecting the CO2 content in the steam, which can be realized by a non-dispersive infrared sensor or an electrochemical sensor. By feeding back the CO2 concentration data in real time, the PLC controller can dynamically adjust the supply amount of the absorbent.

[0030] The PLC controller refers to a programmable logic controller, which can be realized by an industrial modular controller. By receiving sensor signals and executing a pre-set control algorithm, the PLC controller can realize closed-loop control of the start-stop frequency or output flow of the metering pump.

[0031] When the steam flow meter detects an increase in steam flow or the CO2 concentration sensor detects an increase in CO2 concentration, the PLC controller will send a control signal to the metering pump to increase the supply amount of the absorbent. Conversely, when the steam flow decreases or the CO2 concentration decreases, the PLC controller will correspondingly reduce the supply amount. This dynamic adjustment mechanism allows the absorbent usage to match the real-time working conditions, avoiding excess or deficiency.

[0032] In some embodiments of the present application, a capacitive vacuum gauge is provided in the condenser 3. This device can monitor the change in internal vacuum of the condenser in real time and feed back the data to the control system, with a measurement range of 0.001-0.1 MPa.

[0033] Specifically, after installing a capacitive vacuum gauge inside the condenser 3, its measurement end is directly exposed to the condensing cavity environment. When the vacuum degree changes, the electrical signal output by the capacitive vacuum gauge is transmitted to the PLC controller through a wire. According to the pre-set vacuum degree threshold range, the PLC controller sends start-stop or power adjustment instructions to the vacuum pump, for example, starts the vacuum pump when the detected vacuum degree is lower than the set value, and stops running when the set value is reached. This process forms a closed-loop control, which maintains the internal vacuum of the condenser within the optimal range required for carbon capture reaction. The present application realizes real-time and accurate monitoring of the vacuum degree of the condenser, effectively suppressing the deviation of the vacuum degree caused by sudden changes in steam flow or fluctuations in cooling water temperature. The stability of the vacuum environment ensures that the contact time between the CO2 absorbent and the steam remains constant, avoiding the problem of reduced absorbent utilization rate caused by fluctuations in vacuum degree in traditional systems, thereby improving the carbon capture efficiency.

[0034] In some embodiments of the present application, the PLC controller is electrically connected with the vacuum pump and the capacitive vacuum gauge. The capacitive vacuum gauge continuously monitors the pressure data inside the condenser and transmits the pressure signal to the PLC controller. When the detected pressure value exceeds the preset range, the PLC controller calculates the power adjustment amount of the vacuum pump through the PID algorithm and sends a frequency conversion control signal to the vacuum pump. The vacuum pump automatically adjusts the rotating speed according to the received signal, and the internal pressure of the condenser returns to the set value by changing the air exhaust rate.

[0035] In some embodiments of the present application, a dryer is arranged in the centrifugal separator 9. The carbonates after the solid-liquid separation unit mainly include calcium carbonate and magnesium carbonate, which are dried by a hot air dryer (temperature 80-100℃) for drying treatment. The dried carbonates are transported to the boiler desulfurization tower. The dryer removes the residual moisture on the surface and inside of the solid product by hot air circulation or vacuum suction, so that the product reaches a dry state that can be recycled. The dried product after treatment can be directly transported to the resource utilization link without the need for additional drying equipment. This scheme can effectively improve the drying efficiency of carbon capture products, avoid the problems of caking or deterioration caused by high product humidity, ensure that the products can be directly used for resource utilization, and reduce the generation of industrial waste.

[0036] The second aspect of the present application discloses a running method of a vacuum phase change condensation and carbon capture synergistic system, comprising the following steps: 1) Start the vacuum pump of the condenser body to stabilize the internal vacuum degree at 0.01 MPa; 2) The metering pump sprays the absorbent to the corrugated pipe type elastic condenser through the annular porous nozzle, and the spraying amount is 300 kg / h; 3) The steam is condensed into water in the corrugated pipe type elastic condenser, and the absorbent reacts with CO2 (volume fraction 5-15%) carried in the steam to generate carbonates; 4) When the vacuum degree fluctuates (such as ±0.002 MPa), the corrugated pipe compensates for the pressure change by stretching and deforming to maintain stable reaction conditions; 5) The mixture (carbonates + unreacted absorbent + condensed water) after the reaction enters the centrifugal separator, the separated carbonates are dried by hot air (90℃), and then sent to the boiler desulfurization tower by the screw conveyor, as a desulfurizer to react with SO2, realizing the recycling.

[0037] The present application adopts a vacuum phase change condensation and carbon capture synergistic system, realizes the integrated design of vacuum phase change condensation and carbon capture, saves a separate carbon capture reaction device, reduces equipment investment and energy consumption; the corrugated pipe type elastic condenser can effectively compensate for the change of vacuum degree, ensuring the stability of carbon capture efficiency; the carbonate product is reused as a desulfurizer, realizing the recycling of resources, reducing the desulfurization cost, and reducing the discharge of waste.

[0038] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential," etc., indicating orientation or positional relationships, are based on the orientation or positional relationships shown in the accompanying drawings and are only for the convenience of describing the invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the invention. Furthermore, features defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this invention, unless otherwise stated, "a plurality of" means two or more. In the description of this invention, "above" or "below" a second feature may include direct contact between the first and second features, or it may include contact between the first and second features not being in direct contact but through another feature between them.

[0039] In the description of this invention, the terms "above," "over," and "on top" for the first feature and the second feature include the first feature being directly above or diagonally above the second feature, or simply indicating that the first feature is at a higher horizontal level than the second feature.

[0040] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0041] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "illustrative embodiment," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples.

[0042] Although embodiments of the invention have been shown and described, those skilled in the art will understand that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.

[0043] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A vacuum phase transition condensation and carbon capture synergic system, characterized in that, The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

2. The system of claim 1, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

3. The system of claim 1, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

4. The system of claim 1, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

5. The system of claim 1, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

6. The system of claim 1, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

7. The system of claim 6, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

8. The system of claim 7, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

9. The system of claim 8, wherein the system is configured to operate in a vacuum. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet.

10. A method of operating a system for simultaneous phase change condensation and carbon capture as defined in claim 1, wherein, The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside the steam inlet. The condenser (3) is connected with a steam pipeline (6), and the condenser (3) is provided with a CO2 absorbent outlet, which is connected with the CO2 absorbent storage tank (1) and is arranged beside

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