CN117339354A

CN117339354A - Parameter adjusting method and device of carbon capture system, storage medium and electronic equipment

Info

Publication number: CN117339354A
Application number: CN202311127285.0A
Authority: CN
Inventors: 任斌; 龚海艇; 陈臻; 李偲; 王振; 季伟
Original assignee: CHN Energy Taizhou Power Generation Co Ltd
Current assignee: CHN Energy Taizhou Power Generation Co Ltd
Priority date: 2023-09-01
Filing date: 2023-09-01
Publication date: 2024-01-05

Abstract

The disclosure relates to a parameter adjusting method and device of a carbon trapping system, a storage medium and electronic equipment, and is applied to the technical field of carbon trapping. In the method, the control quantity of the carbon trapping system is obtained, and the target alcohol amine liquid circulation quantity flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower are controlled according to the control quantity and the standard value of the carbon dioxide content discharged by the carbon trapping absorption tower. The control amount includes a flow rate of flue gas entering the absorber or a target yield of carbon dioxide produced by the regenerator. Even if the carbon dioxide yield requirement is changed in the production process, the process parameters of the carbon capture system can be automatically adjusted by changing the control quantity. Through the control quantity and the standard value of the carbon dioxide content in the tail gas, the flue gas flow, the alcohol amine liquid circulation quantity and the steam flow can be kept at the optimal ratio, so that the actual yield of the carbon dioxide of the carbon capture system is controlled to meet the target yield of the carbon dioxide. Therefore, the production energy consumption of the carbon capture system can be reduced.

Description

Parameter adjusting method and device of carbon capture system, storage medium and electronic equipment

Technical Field

The disclosure relates to the technical field of carbon capture, in particular to a parameter adjusting method and device of a carbon capture system, a storage medium and electronic equipment.

Background

The flue gas carbon dioxide trapping technology adopts a chemical absorption method with an alcohol amine solution as an absorbent, and carbon trapping can be realized by adopting the alcohol amine absorption method, so that high-concentration carbon dioxide gas can be produced. In the normal operation process of the carbon dioxide capturing device, due to the change of factors such as carbon content of flue gas, carbon dioxide absorption capacity of an absorbent, carbon dioxide yield adjustment and the like, the operation parameters of the carbon dioxide capturing device need to be adjusted at any time so as to ensure the safe operation of the carbon dioxide capturing device.

In general, the adjustment of process parameters in the carbon capture system is performed by manual adjustment, and the adjustment of the process parameters depends on the experience of the operator. By the aid of the parameter control method, the carbon capture system cannot adjust parameters according to the operation conditions in time, so that the carbon capture system cannot operate under the lowest energy consumption working condition for a long time. Thus, the production energy consumption of the carbon capture system is increased.

Disclosure of Invention

Based on the above problems, the present disclosure provides a method and apparatus for adjusting parameters of a carbon capture system, a storage medium, and an electronic device, which can reduce production energy consumption of the carbon capture system.

The embodiment of the application discloses the following technical scheme:

in a first aspect, the present disclosure provides a method of parameter adjustment for a carbon capture system, the method being applied to an alcohol amine absorption carbon capture system, the system comprising: a carbon capture absorber, a carbon capture regenerator, the method comprising:

acquiring control quantity of a carbon capture system, wherein the control quantity comprises the flow of flue gas entering the carbon capture absorption tower or the target yield of carbon dioxide generated by the carbon capture regeneration tower;

and controlling the circulation amount of the target alcohol amine liquid flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower according to the control amount and the standard value of the carbon dioxide content in the tail gas discharged by the carbon trapping absorption tower.

Optionally, the control amount comprises a flow of flue gas into the carbon capture absorber;

and controlling the circulation amount of the target alcohol amine liquid flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower according to the control amount and the standard value of the carbon dioxide content in the tail gas discharged by the carbon trapping absorption tower, wherein the method comprises the following steps:

determining the circulation quantity demand of the alcohol amine liquid according to the flue gas flow;

determining a carbon dioxide content compensation value according to an actual value of the carbon dioxide content in the tail gas and a standard value of the carbon dioxide content in the tail gas;

And controlling the target alcohol amine liquid circulation amount flowing through the carbon capture absorption tower and the target steam flow flowing through the carbon capture regeneration tower according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand.

Optionally, the determining the required amount of the circulated alcohol amine liquid according to the flue gas flow comprises the following steps:

determining a flue gas carbon content correction coefficient according to the current actual carbon content value of the flue gas and the standard carbon content value of the flue gas;

determining standard flue gas flow corresponding to the flue gas flow according to the carbon content correction coefficient of the flue gas;

and determining the required quantity of the alcohol amine liquid circulation quantity according to the relation between the standard flue gas flow and the carbon dioxide desorbed by the absorbent, wherein the mapping relation between the standard flue gas flow and the alcohol amine liquid circulation quantity is indicated in the relation between the carbon dioxide desorbed by the absorbent.

Optionally, the controlling the target alcohol amine liquid circulation amount flowing through the carbon capture absorption tower and the target steam flow flowing through the carbon capture regeneration tower according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand includes:

determining the target alcohol amine liquid circulation amount according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand;

Determining steam flow demand according to the target alcohol amine liquid circulation quantity;

and obtaining target steam flow according to the steam flow demand, the pressure compensation value of the carbon capture regeneration tower and the temperature compensation value of the carbon capture regeneration tower.

Optionally, the method further comprises:

determining a rich liquid level compensation value according to the current rich liquid level and a preset rich liquid level, wherein the rich liquid is an alcohol amine liquid in which carbon dioxide is absorbed in the carbon capture absorption tower;

determining the target opening of the rich liquid flow regulating valve according to the target alcohol amine liquid circulation quantity;

and adjusting the opening of the rich liquid flow regulating valve according to the rich liquid level compensation value and the target opening.

Optionally, the method further comprises:

determining a target opening degree of a lean solution flow regulating valve according to the target alcohol amine solution circulation amount, wherein the lean solution is alcohol amine solution which does not absorb carbon dioxide in the carbon capture regeneration tower;

determining a lean solution flow compensation value according to the target lean solution flow and the current lean solution flow;

and adjusting the opening of the lean liquid flow regulating valve according to the lean liquid flow compensation value and the target opening.

Optionally, the control amount comprises a target yield of carbon dioxide produced by the carbon capture regeneration column;

determining a target flue gas flow according to the target yield of the carbon dioxide and a standard value of the carbon dioxide content in the tail gas;

determining the circulation quantity of the target alcohol amine liquid according to the target yield of the carbon dioxide and the standard value of the carbon dioxide content in the tail gas;

and determining the target steam flow according to the target alcohol amine liquid circulation quantity.

Optionally, the determining the target flue gas flow according to the target yield of the carbon dioxide and the standard value of the carbon dioxide content in the tail gas includes:

determining the flue gas flow demand according to the target yield of the carbon dioxide;

determining a first compensation value according to an actual value of the carbon dioxide content in the tail gas and a standard value of the carbon dioxide content in the tail gas;

And determining the target flue gas flow according to the standard flue gas flow and the first compensation value.

Optionally, the determining the target alcohol amine liquid circulation amount according to the target yield of the carbon dioxide and the standard value of the carbon dioxide content in the tail gas comprises:

determining the circulation quantity demand of the alcohol amine liquid according to the target yield of the carbon dioxide;

determining a second compensation value according to the actual value of the carbon dioxide content in the tail gas and the standard value of the carbon dioxide content in the tail gas;

and obtaining the target alcohol amine liquid circulation amount according to the alcohol amine liquid circulation amount demand and the second compensation value.

Optionally, the determining the target steam flow according to the target alcohol amine liquid circulation amount includes:

determining the steam flow demand according to the target alcohol amine liquid circulation quantity;

obtaining a carbon dioxide yield compensation value according to the target yield of carbon dioxide and the current yield of carbon dioxide;

and determining a target steam flow according to the steam flow demand, the carbon dioxide yield compensation value, the pressure compensation value of the carbon capture regeneration tower and the temperature compensation value of the carbon capture regeneration tower.

Optionally, the method further comprises:

determining a target rich liquid flow according to the rich liquid level compensation value and the target alcohol amine liquid circulation quantity;

and adjusting the opening of the rich liquid flow adjusting valve according to the target rich liquid flow and the current rich liquid flow.

Optionally, the method further comprises:

determining a lean liquid level compensation value according to the current lean liquid level and a preset lean liquid level, wherein the lean liquid is alcohol amine liquid which does not absorb carbon dioxide in the carbon capture regeneration tower;

determining a target lean solution flow according to the lean solution liquid level compensation value and the target alcohol amine solution circulation quantity;

and adjusting the opening of the lean solution flow adjusting valve according to the target lean solution flow and the current lean solution flow.

In a second aspect, the present disclosure provides a parameter adjustment device for a carbon capture system, comprising:

the acquisition module is used for acquiring control quantity of the carbon capture system, wherein the control quantity comprises the flow of flue gas entering the carbon capture absorption tower or the target yield of carbon dioxide generated by the carbon capture regeneration tower;

and the control module is used for controlling the target alcohol amine liquid circulation quantity flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower according to the control quantity and the standard value of the carbon dioxide content in the tail gas discharged by the carbon trapping absorption tower.

In a third aspect, the present disclosure provides a non-transitory computer-readable storage medium having stored thereon a computer program which, when executed by a processor, implements the steps of the method for parameter adjustment of a carbon capture system provided in the first aspect.

In a fourth aspect, the present disclosure provides an electronic device that, when executed, performs the steps of the method for adjusting parameters of the carbon capture system provided in the first aspect.

The technical scheme provided by the embodiment of the disclosure can comprise the following beneficial effects:

in the method, the control quantity of the carbon trapping system is obtained, and the target alcohol amine liquid circulation quantity flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower are controlled according to the control quantity and the standard value of the carbon dioxide content discharged by the carbon trapping absorption tower. Wherein the control amount includes a flow rate of flue gas entering the carbon capture absorber or a target yield of carbon dioxide produced by the carbon capture regenerator. Even if the carbon dioxide yield requirement is changed in the production process, the process parameters of the carbon capture system can be automatically adjusted by changing the control quantity, so that the automation level is improved. Through the control quantity and the standard value of the carbon dioxide content in the tail gas, the flue gas flow, the alcohol amine liquid circulation quantity and the steam flow can be kept at the optimal ratio, so that the actual yield of the carbon dioxide of the carbon capture system is controlled to meet the target yield of the carbon dioxide. Therefore, the production energy consumption of the carbon capture system can be reduced.

Additional features and advantages of the present disclosure will be set forth in the detailed description which follows.

Drawings

The accompanying drawings are included to provide a further understanding of the disclosure, and are incorporated in and constitute a part of this specification, illustrate the disclosure and together with the description serve to explain, but do not limit the disclosure. In the drawings:

fig. 1 is a schematic structural diagram of a flue gas washing unit and a carbon dioxide absorbing unit of an alcohol amine absorption carbon capturing system according to an embodiment of the present disclosure;

FIG. 2 is a schematic diagram of a carbon dioxide stripping regeneration unit of an alcohol amine absorption carbon capture system according to an embodiment of the present disclosure;

FIG. 3 is a flow chart of a method for parameter adjustment of a carbon capture system provided in an embodiment of the present disclosure;

FIG. 4 is a flow chart for controlling a target alcohol amine liquid circulation amount and a target steam flow when the control amount is a flue gas flow provided by an embodiment of the present disclosure;

FIG. 5 is a flow chart for controlling the amount of circulated alcohol amine liquid required when the control amount is the flow of flue gas according to the embodiment of the present disclosure;

FIG. 6 is a flow chart for controlling a target flue gas flow when the control amount is a target yield of carbon dioxide, provided by an embodiment of the present disclosure;

FIG. 7 is a flow chart for controlling the circulation amount of a target alcohol amine liquid when the control amount is the target production amount of carbon dioxide, provided in an embodiment of the present disclosure;

FIG. 8 is a flow chart for controlling a target steam flow when the control amount is a target production of carbon dioxide, provided by an embodiment of the present disclosure;

FIG. 9 is a schematic structural diagram of a parameter adjustment device of a carbon capture system according to an embodiment of the present disclosure;

fig. 10 is a schematic structural diagram of an electronic device according to an embodiment of the disclosure.

Detailed Description

In order to enable those skilled in the art to more clearly understand the technical solutions of the present disclosure, the following first describes application scenarios of the solutions of the present disclosure.

The flue gas carbon dioxide trapping technology adopts a chemical absorption method with an alcohol amine solution as an absorbent, and carbon trapping can be realized by adopting the alcohol amine absorption method, so that high carbon dioxide trapping rate can be realized, high-concentration carbon dioxide gas can be produced, and low absorbent regeneration heat consumption can be realized. The alcohol amine absorption method carbon capture system is shown in figures 1 and 2, and mainly comprises the following parts: a flue gas washing unit, a carbon dioxide absorbing unit and a carbon dioxide stripping regeneration unit.

In the carbon dioxide absorption unit, the flue gas is pressurized by a fan from the top of the water washing tower 1, enters the lower part of the carbon dioxide absorption tower 2, contacts with a compound amine solvent from top to bottom, and removes more than ninety percent of carbon dioxide in the flue gas. A water washing section is arranged at the top of the absorption tower to catch amine mist carried in the flue gas, and the water balance of the system is maintained by condensing the water in the flue gas. The tail gas is directly discharged into the atmosphere from the top of the tower after being washed by water in a washing section. Carbon dioxide absorption is an exothermic reaction and the heat evolved during absorption must be removed to prevent the temperature of the absorbent from rising, resulting in a decrease in the absorbent capacity of the absorbent. At the same time, the temperature rise can also cause the diffusion of water in the amine liquid into the flue gas, so that the water loss in the system is caused. In order to remove heat generated in the absorption process, a cooler 3 is arranged in the middle section of the carbon dioxide absorption tower, and part of the absorbent is cooled through heat exchange and then returned to the absorption tower, so that the absorbent is maintained to be absorbed at a lower temperature, the performance of the absorbent and the carbon dioxide removal rate in the flue gas are improved, and the water balance of the whole system is maintained.

In the carbon dioxide stripping regeneration system, the rich liquid after absorbing carbon dioxide flows out from the bottom of the absorption tower, is divided into two parts by a rich liquid pump 4, one part is directly sent to the top of the regeneration tower 6 to serve as washing liquid to reduce the water vapor content at the top of the regeneration tower, and the other part is sent to a lean rich liquid heat exchanger 5 to recover heat and then enters from the middle upper part of the regeneration tower. Both rich liquids desorb part of the carbon dioxide by stripping and then enter a boiler 7, so that the carbon dioxide in the rich liquids is further desorbed. The desorbed carbon dioxide and water vapor are extracted from the top of the regeneration tower and are cooled and separated to remove water, thus obtaining carbon dioxide product gas.

In the normal operation process of the carbon dioxide capturing device, due to the change of factors such as carbon content of flue gas, carbon dioxide absorption capacity of an absorbent, carbon dioxide yield adjustment and the like, the operation parameters of a carbon dioxide capturing system need to be adjusted at any time so as to ensure the safe operation of the carbon dioxide capturing device.

Among the operating parameters of the carbon capture system, the main process parameters include absorber inlet flue gas volume, alkanolamine liquid circulation volume, and desorption steam flow.

Specifically, under normal conditions, the carbon dioxide content in the flue gas is stable, and the larger the flue gas flow rate is, the more carbon dioxide gas can be trapped. When the flow rate of the flue gas is too large, carbon dioxide which cannot be absorbed in the flue gas is discharged along with the tail gas at the top of the absorption tower, and the carbon content in the tail gas is increased, so that the trapping rate is reduced. Meanwhile, under certain temperature and pressure, the solubility of the carbon dioxide in the alcohol amine liquid is certain, and if the circulation amount of the absorbent is too small, the absorption efficiency is low, and the yield of the carbon dioxide is insufficient; if the amount of the absorbent to be circulated is too large, the energy consumption for regenerating carbon dioxide increases. Under the influence of the flue gas volume flow/absorption liquid volume flow and the alcohol amine liquid circulation volume, nm3/m3 (gas-liquid ratio) influences the gas-liquid mass transfer process of the absorption tower, and further influences the regeneration heat consumption of the carbon capture system.

In addition, for the regeneration tower, the desorption is facilitated due to the high temperature, but the degradation of the alcohol amine liquid can be caused by the excessive temperature, so that the corrosion is increased, and the energy consumption is increased. Therefore, the temperature at the bottom of the regeneration tower is controlled by the flow rate of the desorption steam fed into the falling film boiler of the regeneration tower. The steam input is too small, the sensible heat and the heat dissipation specific gravity of the solution are increased, and the energy consumption is reduced; the steam input is overlarge, the workload is reduced, the water evaporation capacity is increased, and the energy consumption is increased.

Specific embodiments of the present disclosure are described in detail below with reference to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the disclosure, are not intended to limit the disclosure.

It should be noted that, all actions for acquiring signals, information or data in the present disclosure are performed under the condition of conforming to the corresponding data protection rule policy of the country of the location and obtaining the authorization given by the owner of the corresponding device.

References to "first", "second", etc. in the designations of "first", "second", etc. in the embodiments of the present disclosure are used to make a designation and do not represent a sequential "first", "second".

Currently, the main process parameters in the carbon capture system are adjusted manually, and the adjustment of the process parameters depends on the experience of the operating personnel. By the aid of the parameter control method, the carbon capture system cannot adjust parameters in time according to the operation working conditions, so that the carbon capture system cannot operate under the lowest energy consumption working condition for a long time, the unit carbon dioxide capture energy consumption is higher than a design value, and the carbon dioxide content in tail gas deviates from a preset standard value. Thus, the production energy consumption of the carbon capture system is increased. Meanwhile, the workload of operation operators is large, and the processing of abnormal working conditions depends on the skills and operation level of the operators, so that the long-period safe, stable and economical operation of the carbon capture system is not facilitated.

In order to solve the above-described problems, the present disclosure provides the following embodiments. FIG. 3 is a flow chart illustrating a method of parameter adjustment for a carbon capture system, according to an exemplary embodiment. As shown in fig. 3, the method includes:

in step 11, a control amount of the carbon capturing system is acquired.

In the process of capturing carbon dioxide in the flue gas by the carbon capturing system, the flue gas is input into the carbon capturing absorption tower, the carbon dioxide in the flue gas is absorbed by the alcohol amine liquid in the carbon capturing absorption tower, and the steam in the carbon capturing regeneration tower can desorb the carbon dioxide in the alcohol amine liquid, so that the carbon dioxide is produced, and the regeneration of the carbon dioxide is realized.

Specifically, in the present embodiment, a control amount of the carbon capturing system is obtained, wherein the control amount includes a flow rate of flue gas entering the carbon capturing absorption tower or a target yield of carbon dioxide produced by the carbon capturing regeneration tower. The flow rate of the flue gas entering the carbon capture absorption tower can be controlled in an open-loop regulation mode to control the yield of carbon dioxide of the carbon capture system, and the target yield of the carbon dioxide generated by the carbon capture regeneration tower can be controlled in a closed-loop regulation mode to control the yield of the carbon dioxide of the carbon capture system.

The main process parameters of the carbon capture system are automatically adjusted through the control quantity, so that the carbon capture system can be kept to operate under the working condition of minimum energy consumption, and the production energy consumption of the carbon capture system is reduced.

In step 12, the target alcohol amine liquid circulation amount flowing through the carbon capture absorption tower and the target steam flow flowing through the carbon capture regeneration tower are controlled according to the control amount and the standard value of the carbon dioxide content in the tail gas discharged from the carbon capture absorption tower.

Specifically, the carbon dioxide yield of the carbon trapping system is related to the flue gas flow and the carbon dioxide content in the tail gas, and the alcohol amine liquid circulation amount and the steam flow of main technological parameters in the carbon trapping system are controlled, so that the carbon trapping system can be kept to operate under the working condition of the lowest energy consumption, and the production energy consumption of the carbon trapping system is reduced.

In the method, the control quantity of the carbon trapping system is obtained, and the target alcohol amine liquid circulation quantity flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower are controlled according to the control quantity and the standard value of the carbon dioxide content discharged by the carbon trapping absorption tower. Wherein the control amount includes a flow rate of flue gas entering the carbon capture absorber or a target yield of carbon dioxide produced by the carbon capture regenerator. Even if the carbon dioxide yield requirement is changed in the production process, the process parameters of the carbon capture system can be automatically adjusted by changing the control quantity, so that the automation level is improved. Through the control quantity and the standard value of the carbon dioxide content in the tail gas, the flue gas flow, the alcohol amine liquid circulation quantity and the steam flow can be kept at the optimal ratio, so that the actual yield of the carbon dioxide of the carbon capture system is controlled to meet the target yield of the carbon dioxide. Therefore, the production energy consumption of the carbon capture system can be reduced. In addition, the working intensity of operation operators can be reduced, and the safety and the economy of the carbon capture system are improved.

In one possible embodiment, when the control amount is a flow rate of flue gas entering the carbon capture absorption tower, an exemplary implementation manner of controlling the target alcohol amine liquid circulation amount flowing through the carbon capture absorption tower and the target steam flow rate flowing through the carbon capture regeneration tower according to the control amount and a standard value of carbon dioxide content in the tail gas discharged from the carbon capture absorption tower may include:

referring to fig. 4, fig. 4 is a flowchart for controlling the target alcohol amine liquid circulation amount and the target steam flow rate when the control amount is the flue gas flow rate.

In step 41, the alcohol amine liquid circulation amount demand is determined according to the flue gas flow.

Specifically, the alcohol amine liquid is used as an absorbent to absorb carbon dioxide in the flue gas, and according to the content of the carbon dioxide in the flue gas flow flowing into the carbon capture absorption tower, the amount of the alcohol amine liquid needed by the flowing flue gas can be determined for cyclic absorption.

In step 42, a carbon dioxide content compensation value is determined according to the actual value of the carbon dioxide content in the tail gas and the standard value of the carbon dioxide content in the tail gas.

Specifically, PID (proportional integral derivative) adjustment is performed by using the actual value and the standard value to obtain a carbon dioxide content compensation value, so that the actual value can be equal to or close to the standard value.

The carbon dioxide content in the tail gas can influence the carbon dioxide yield, and when the actual value deviates from the standard value, the requirement of the alcohol amine liquid for absorbing the carbon dioxide in the flue gas cannot meet the current working condition, and the requirement of the alcohol amine liquid for absorbing the carbon dioxide in the flue gas needs to be regulated by utilizing the carbon dioxide content compensation value.

In step 43, the target alcohol amine liquid circulation amount flowing through the carbon capturing absorber and the target steam flow flowing through the carbon capturing regenerator are controlled according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand.

Specifically, the carbon dioxide content compensation value in the tail gas discharged by the carbon capture absorption tower is utilized to correct the alcohol amine liquid circulation quantity demand, and the target alcohol amine liquid circulation quantity flowing through the carbon capture absorption tower is controlled; the target alcohol amine liquid circulation amount can be used for determining the steam flow demand of desorption carbon dioxide, then the steam flow demand is corrected, and the target steam flow flowing through the carbon capture regeneration tower is determined.

Illustratively, determining the alcohol amine liquid circulation amount demand according to the flue gas flow may include:

referring to fig. 5, fig. 5 is a flow chart for controlling the required amount of the circulated amount of the alcohol amine liquid when the control amount is the flow rate of the flue gas.

In step 51, a flue gas carbon content correction coefficient is determined according to the actual carbon content value of the current flue gas and the standard carbon content value of the flue gas.

As an example, the ratio of the actual carbon content value of the current flue gas to the standard carbon content value of the flue gas is used as the flue gas carbon content correction coefficient.

In step 52, a standard flue gas flow corresponding to the flue gas flow is determined based on the flue gas carbon content correction factor.

In the actual operation process of the carbon capture system, the carbon content of the inflowing flue gas may not meet the preset standard value of the carbon content of the flue gas. In this way, it may be marked that the flow rate of the flowing flue gas cannot meet the required carbon dioxide yield, and at this time, the flow rate of the flowing flue gas needs to be subjected to standardized correction according to the carbon content correction coefficient of the flue gas, so as to obtain the corresponding standard flow rate of the flue gas.

As an example, the carbon content correction coefficient of the flue gas is multiplied by the input flue gas flow, and the flue gas flow is subjected to standardized correction, so that the corresponding standard flue gas flow can be determined.

In step 53, the alcohol amine liquid circulation amount demand is determined according to the relation between the standard flue gas flow and the absorbent desorption carbon dioxide.

Specifically, according to the relation of desorbing carbon dioxide by the absorbent, the required quantity of the alcohol amine liquid circulation quantity corresponding to the standard flue gas flow, namely the required alcohol amine liquid circulation quantity for absorbing carbon dioxide in the standard flue gas flow, can be determined. As mentioned above, the flow of flue gas into the carbon capture system may not meet the required carbon dioxide production, and thus, the flue gas flow is modified in a standardized manner. Therefore, the required quantity of the alcohol amine liquid circulation quantity determined by the standard flue gas flow can more accurately meet the carbon dioxide yield when absorbing the carbon dioxide in the flue gas, and the energy consumption of the carbon capture system can be reduced.

Illustratively, controlling the target alcohol amine liquid circulation amount flowing through the carbon capture absorber and the target steam flow flowing through the carbon capture regenerator according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand in the tail gas may include:

and determining the target alcohol amine liquid circulation amount according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand.

Specifically, determining the carbon dioxide content compensation value may enable an actual value of the carbon dioxide content in the tail gas discharged from the carbon capture absorption tower to be close to or equal to a standard value of the carbon dioxide content in the tail gas. Further, the setting of the standard value of the carbon dioxide content in the tail gas can be used for adjusting the carbon dioxide yield, so that the carbon dioxide content compensation value can be used for correcting the alcohol amine liquid circulation quantity required quantity and determining the target alcohol amine liquid circulation quantity. For example, if the carbon dioxide content compensation value is positive, the actual value is smaller than the standard value, and when the alcohol amine liquid circulation amount requirement operates under the current working condition, excessive absorption of carbon dioxide in the flue gas is caused, the alcohol amine liquid circulation amount requirement needs to be reduced by utilizing the carbon dioxide content compensation value, and the target alcohol amine liquid circulation amount is determined; otherwise, the same is true.

And then, determining the steam flow demand according to the target alcohol amine liquid circulation amount.

Specifically, after the target alcohol amine liquid circulation amount is determined, the alcohol amine liquid is used as an absorbent to absorb carbon dioxide in the flue gas in the carbon capture system. After absorbing carbon dioxide, the alcohol amine liquid needs to be desorbed by steam in a carbon capture regeneration tower to produce carbon dioxide. And determining the steam flow demand corresponding to the target alcohol amine liquid circulation amount according to a preset mapping relation between the target alcohol amine liquid circulation amount and the steam flow so as to desorb the carbon dioxide.

And obtaining the target steam flow according to the steam flow demand, the pressure compensation value of the carbon capture regeneration tower and the temperature compensation value of the carbon capture regeneration tower.

Specifically, when the pressure and temperature of the carbon capture regeneration tower exceed the preset normal ranges, excessive steam input into the carbon capture regeneration tower may be caused, and the safety and economy of the carbon capture system may be affected. Therefore, the pressure compensation value of the carbon capture regeneration tower and the temperature compensation value of the carbon capture regeneration tower are needed to be utilized to timely adjust the steam flow demand to obtain the target steam flow, so that the pressure and the temperature of the carbon capture regeneration tower are kept in the normal range, and the safety and the economy of a carbon capture system are improved.

Wherein the pressure compensation value of the carbon capture regeneration column and the temperature compensation value of the carbon capture regeneration column may be determined by:

if the current temperature of the lean solution at the bottom of the carbon capture regeneration tower exceeds the preset temperature, a temperature difference between the current temperature and the preset temperature can be determined, and the temperature difference is used as a temperature compensation value. The lean solution is alcohol amine solution which does not absorb carbon dioxide in the carbon capture regeneration tower.

If the current pressure of the carbon capture regeneration tower exceeds the preset pressure, a pressure difference between the current pressure and the preset pressure can be determined, and the pressure difference is used as a pressure compensation value.

In addition, it is also necessary to determine that the target steam flow does not exceed the high limit value. The high limit value is determined according to the rich liquid flow rate in the carbon capture absorption tower, so that the excessive steam flow rate can be prevented, and the safety of the carbon capture system can be improved. When the temperature and pressure of the carbon capturing and regenerating tower are higher than the normal range, explanation of alcohol amine liquid is caused, corrosion is increased, energy consumption is increased, and the increase of target steam flow is required to be forbidden.

In one possible embodiment, an exemplary implementation of the method may further include:

and determining a rich liquid level compensation value according to the current rich liquid level and the preset rich liquid level. Wherein the rich liquid is an alcohol amine liquid in which carbon dioxide is absorbed in the carbon capture absorption tower.

Specifically, the compensation value of the rich liquid level can be determined according to the difference value between the current rich liquid level and the preset rich liquid level, so that the rich liquid flow can be adjusted in time, the liquid level of the carbon capture absorption tower is kept in a preset normal range, and the safety and stability of the carbon capture system can be improved. As an example, when the current rich liquid level is lower than the preset rich liquid level, the flow rate of the rich liquid needs to be correspondingly reduced; when the current rich liquid level is higher than the preset rich liquid level, the rich liquid flow needs to be correspondingly increased.

And then determining the target opening degree of the rich liquid flow regulating valve according to the target alcohol amine liquid circulation amount.

Specifically, the target opening degree of the rich liquid flow regulating valve is determined according to a preset mapping relation between the target alcohol amine liquid circulation amount and the opening degree of the rich liquid flow regulating valve.

Specifically, the opening of the rich liquid flow regulating valve is regulated, that is, the rich liquid flow is regulated, so that the current rich liquid level can be changed, and the current rich liquid level is close to or equal to the preset rich liquid level. In this embodiment, the target alcohol amine liquid circulation amount may be the target rich liquid flow rate. The opening of the rich liquid flow regulating valve is controlled by the target alcohol amine liquid circulation amount, so that the rich liquid flow can be changed.

and determining the target opening of the lean solution flow regulating valve according to the target alcohol amine solution circulation amount. The lean solution is alcohol amine solution which does not absorb carbon dioxide in the carbon capture regeneration tower.

Specifically, according to a preset mapping relation between the target alcohol amine liquid circulation amount and the opening of the lean liquid flow regulating valve, determining the target opening of the lean liquid flow regulating valve.

And then, determining a lean solution flow compensation value according to the target lean solution flow and the current lean solution flow.

Specifically, in this embodiment, the target alcohol amine liquid circulation amount may be taken as the target lean liquid flow, and the current lean liquid flow may be directly measured by a detection device in the carbon capture regeneration tower. And taking the difference value between the current lean solution flow and the target lean solution flow as a lean solution flow compensation value.

And adjusting the opening of the lean solution flow regulating valve according to the lean solution flow compensation value and the target opening.

Specifically, the opening of the lean solution flow rate regulating valve is adjusted, that is, the lean solution flow rate is adjusted so that the current lean solution flow rate is equal to or close to the target lean solution flow rate. For example, when the lean flow rate compensation value is positive, it is indicated that the current lean flow rate is smaller than the target lean flow rate, that is, the opening degree of the lean flow rate regulating valve should be opened large. According to the mapping relation between the lean solution flow compensation value and the target opening, the opening of the lean solution flow regulating valve is regulated, and when the opening of the regulating valve reaches the target opening, the current opening is kept unchanged; otherwise, the same is true.

In addition, since the circulation amount of the alcohol amine liquid in the carbon capturing system is fixed, when the rich liquid level in the carbon capturing absorption tower is high, it means that the lean liquid level in the carbon capturing regeneration tower is low, so in this embodiment, the rich liquid level is selectively controlled to be adjusted to a preset value, and the relative lean liquid level is also set to be at the preset value.

In one possible embodiment, when the control amount is a target yield of carbon dioxide, an exemplary implementation of the operating feasibility restriction on the target yield of carbon dioxide to the carbon capture system may include:

during actual operation of the carbon capture system, changes may be required to the carbon dioxide production, requiring the target production of carbon dioxide to be entered into the carbon capture system. Meanwhile, since the input target yield may exceed the operation capacity of the carbon capture system, it is necessary to limit the target yield, and the safety and stability of the carbon capture system may be improved.

Specifically, a target yield of carbon dioxide is obtained, and if the target yield exceeds a preset target yield threshold interval, the target yield is adjusted so that the target yield is within the threshold interval. The target yield threshold interval can be preset based on the minimum output of the normal operation of the carbon capture system and the maximum output of the normal operation of the carbon capture system.

In addition, if the target yield is equal to a preset yield high limit value of the target yield threshold interval, the increase of the target yield is forbidden; and if the target yield is equal to the yield low limit value of the preset target yield threshold interval, prohibiting reducing the target yield. For example, when the carbon capture system reaches a maximum output, possibly the steam flow regulating valve opening reaches a maximum, then the increase of the target yield is prohibited; when the carbon capture system reaches a minimum output, which may be as low as the fan surge region, the target yield is prohibited from being reduced.

Meanwhile, in order to put the carbon capture system in a safe operation state, when the target yield of carbon dioxide is changed, the time for producing carbon dioxide is correspondingly changed. Specifically, the production time of the target yield is adjusted according to a preset change rate, wherein the change rate is used for indicating the speed of the current yield reaching the target yield. Wherein the rate of change is fixed, and can prevent the unstable condition of the carbon capture system caused by the too fast production rate.

In one possible embodiment, when the control amount is the target yield of carbon dioxide, an exemplary implementation of controlling the target alcohol amine liquid circulation amount flowing through the carbon capture absorber and the target steam flow rate flowing through the carbon capture regenerator according to the control amount and the standard value of the carbon dioxide content in the tail gas discharged from the carbon capture absorber may include:

And determining the target flue gas flow according to the target yield of carbon dioxide and the standard value of the carbon dioxide content in the tail gas.

Specifically, the standard flue gas flow corresponding to the flue gas flow can be determined according to the target yield of carbon dioxide. When the actual value of the carbon dioxide content in the tail gas discharged from the carbon capture absorption tower deviates from the standard value, PID (proportion integration differentiation) adjustment is performed by utilizing the actual value and the standard value to obtain a first compensation value so that the actual value can be equal to or close to the standard value. And determining the target flue gas flow according to the first compensation value and the standard flue gas flow. The first compensation value is a compensation value of the carbon dioxide content in the tail gas.

And then, determining the circulation quantity of the target alcohol amine liquid according to the target yield of the carbon dioxide and the standard value of the carbon dioxide content in the tail gas.

Specifically, the required quantity of the circulation quantity of the alcohol amine liquid can be determined according to the target yield of the carbon dioxide, and when the actual value of the carbon dioxide content in the tail gas discharged from the carbon capture absorption tower deviates from the standard value, PID (proportion integration differentiation) adjustment is performed by using the actual value and the standard value to obtain a second compensation value, so that the actual value can be equal to or close to the standard value. And determining the target alcohol amine liquid circulation amount according to the second compensation value and the alcohol amine liquid circulation amount demand. The second compensation value is a compensation value of the carbon dioxide content in the tail gas.

For example, if the carbon dioxide content compensation value is positive, the actual value is smaller than the standard value, and when the alcohol amine liquid circulation amount requirement operates under the current working condition, excessive absorption of carbon dioxide in the flue gas is caused, the alcohol amine liquid circulation amount requirement needs to be reduced by utilizing the carbon dioxide content compensation value, and the target alcohol amine liquid circulation amount is determined; otherwise, the same is true.

And then, determining the target steam flow according to the target alcohol amine liquid circulation amount.

Specifically, the steam flow demand can be determined according to the target alcohol amine liquid circulation amount, and the target steam flow can be determined by adjusting the steam flow demand through the deviation of the carbon dioxide yield and the pressure and temperature of the carbon capture regeneration tower.

For example, if the pressure compensation value of the carbon capturing and regenerating tower is negative, it may be indicated that the current pressure is greater than the preset pressure, and when the steam flow demand operates under the current working condition, the safety of the carbon capturing system will be affected, and the steam flow demand needs to be reduced by using the pressure compensation value of the carbon capturing and regenerating tower, so as to determine the target steam flow; the temperature compensation value of the carbon capture regeneration tower is the same.

Illustratively, determining the target flue gas flow based on the target yield of carbon dioxide and the standard value of carbon dioxide content in the tail gas may include:

Referring to fig. 6, fig. 6 is a flow chart for controlling a target flue gas flow rate when the control amount is a target yield of carbon dioxide.

In step 61, the flue gas flow demand is determined based on the target yield of carbon dioxide.

Specifically, the carbon dioxide produced by the carbon capture system is obtained by absorbing and desorbing carbon dioxide in the flue gas, so that the target yield of the carbon dioxide and the flue gas flow have a preset mapping relation. And determining the flue gas flow demand corresponding to the target yield according to the preset mapping relation.

In step 62, a flue gas carbon content correction coefficient is determined according to the actual carbon content value of the current flue gas and the standard carbon content value of the flue gas.

In step 63, the standard flue gas flow corresponding to the flue gas flow is determined according to the flue gas carbon content correction coefficient.

In step 64, a first compensation value is determined based on the actual value of the carbon dioxide content in the exhaust gas and the standard value of the carbon dioxide content in the exhaust gas.

Specifically, in the present embodiment, the target production amount is used as the control amount, and the carbon dioxide production amount is controlled by closed-loop adjustment. Meanwhile, the carbon dioxide yield is related to the carbon dioxide content in the tail gas and the flue gas flow, so that when the actual value of the carbon dioxide content in the tail gas deviates from the standard value, the first compensation value, namely the compensation value of the carbon dioxide content in the tail gas, can be used for adjusting the target flue gas flow.

In step 65, a target flue gas flow is determined based on the standard flue gas flow and the first compensation value.

Specifically, the target flue gas flow rate may be maintained in a suitable range according to the standard flue gas flow rate and the first compensation value. As mentioned above, the flow of flue gas into the carbon capture system may not meet the required carbon dioxide production, and thus, the flue gas flow is modified in a standardized manner. Meanwhile, when the actual value of the carbon dioxide content in the tail gas deviates from the standard value, the fact that the carbon dioxide yield cannot reach the target yield is indicated, and the first compensation value can be used for participating in adjusting the flue gas flow. Therefore, the target flue gas flow is kept in a proper range, the carbon dioxide yield can be met more accurately, and the energy consumption of the carbon capture system can be reduced.

Illustratively, determining the target alcohol amine liquid circulation amount according to the standard value of the carbon dioxide content in the tail gas may include:

referring to fig. 7, fig. 7 is a flowchart for controlling the circulation amount of the objective alcohol amine liquid when the control amount is the objective production amount of carbon dioxide.

In step 71, the alcohol amine liquid circulation amount demand is determined based on the target carbon dioxide production.

Specifically, the alcohol amine liquid is used as an absorbent for absorbing carbon dioxide in the flue gas, so that the target yield of the carbon dioxide and the circulation amount of the alcohol amine liquid have a preset mapping relation. And determining the required quantity of the alcohol amine liquid circulation quantity corresponding to the target yield according to a preset mapping relation.

In step 72, a second compensation value is determined based on the actual value of the carbon dioxide content in the exhaust gas and the standard value of the carbon dioxide content in the exhaust gas.

Specifically, in the present embodiment, the target production amount is used as the control amount, and the carbon dioxide production amount is controlled by feedback adjustment. Meanwhile, when the carbon content of the carbon dioxide in the tail gas deviates from the standard value, the circulation amount of the alcohol amine liquid in the carbon capture absorption tower is not matched with the carbon dioxide to be absorbed.

Therefore, when the actual value of the carbon dioxide content in the tail gas deviates from the standard value, the second compensation value, namely the compensation value of the carbon dioxide content in the tail gas, can be used for adjusting the circulation quantity of the target alcohol amine liquid. For example, when the actual value of the carbon dioxide content in the tail gas is higher than the standard value, it is indicated that the alcohol amine liquid circulated in the carbon capturing and absorbing tower cannot fully absorb the carbon dioxide in the flue gas, and the circulation amount of the alcohol amine liquid needs to be increased.

In step 73, a target alcohol amine liquid circulation amount is obtained according to the alcohol amine liquid circulation amount demand and the second compensation value.

Specifically, the target alcohol amine liquid circulation amount can be kept in a proper range according to the alcohol amine liquid circulation amount demand amount and the second compensation value. When the actual value of the carbon dioxide content in the tail gas deviates from the standard value, the alcohol amine liquid can not fully absorb the carbon dioxide in the flue gas or the alcohol amine liquid can excessively absorb the carbon dioxide in the flue gas, so that the carbon dioxide yield can not reach the target yield, and the second compensation value can be used for participating in adjusting the circulation quantity demand of the alcohol amine liquid. Therefore, the circulation amount of the target alcohol amine liquid is kept in a proper range, the carbon dioxide yield can be met more accurately, and the energy consumption of the carbon capture system can be reduced.

Meanwhile, the target flue gas flow and the target alcohol amine liquid circulation are controlled through the carbon dioxide content in the tail gas, so that the operation working condition can be kept at a good gas-liquid ratio, the energy consumption of the carbon capture system is reduced, and the economy of the carbon capture system is improved.

Illustratively, determining the target steam flow based on the target alkanolamine liquid circulation amount may include:

referring to fig. 8, fig. 8 is a flowchart for controlling a target steam flow rate when the control amount is a target production amount of carbon dioxide.

In step 81, a steam flow demand is determined based on the target alkanolamine liquid circulation amount.

Specifically, the carbon dioxide absorbed by the alcohol amine liquid is produced by steam desorption, so that a preset mapping relation exists between the target alcohol amine liquid circulation amount and the steam flow required by desorption of the carbon dioxide. The target alcohol amine liquid circulation quantity is combined with a preset mapping relation, so that the steam flow demand quantity can be determined.

In step 82, a carbon dioxide production offset value is obtained based on the target production of carbon dioxide and the current production of carbon dioxide.

Specifically, when the current yield of carbon dioxide has deviation from the target yield, PID adjustment is performed by using the current yield and the target yield to obtain a carbon dioxide yield compensation value. And adjusting the steam flow demand by using the carbon dioxide yield compensation value so that the target steam flow desorbs the target yield of the carbon dioxide. For example, when the current production of carbon dioxide is insufficient, it is indicated that the steam flow demand is small, and the steam for desorption needs to be increased; and similarly, reducing steam in the opposite direction.

In step 83, a target steam flow is determined based on the steam flow demand, the carbon dioxide production offset, the pressure offset of the carbon capture regeneration column, and the temperature offset of the carbon capture regeneration column.

The method for determining the pressure compensation value of the carbon capture regeneration tower and the temperature compensation value of the carbon capture regeneration tower are the same as those of the present embodiment, and will not be described again.

Specifically, closed-loop feedback adjustment is performed on the steam flow demand, and when the current yield of carbon dioxide deviates from the target yield, the steam flow demand is adjusted by using the carbon dioxide yield compensation value. Meanwhile, when the temperature and the pressure of the carbon capture regeneration tower deviate from the normal range, the steam flow demand input into the carbon capture regeneration tower deviates from the actual demand under the working condition, and the safety of the carbon capture regeneration tower can be influenced. It is therefore necessary to adjust the steam flow demand in accordance with the pressure compensation value and the temperature compensation value. After the adjustment compensation, the target steam flow can be determined.

and determining a rich liquid level compensation value according to the current rich liquid level and the preset rich liquid level.

Specifically, the carbon capture absorption tower has an excessively high rich liquid level, which is easy to cause rich liquid backflow, and the pump is easy to pump out when the rich liquid level is excessively low. The method for determining the rich liquid level compensation value is consistent with the present embodiment, and will not be described in detail herein.

And then, determining the target rich liquid flow according to the rich liquid level compensation value and the target alcohol amine liquid circulation quantity.

Specifically, in this embodiment, the circulation amount of the alcohol amine liquid is taken as the rich liquid flow, the rich liquid flow is adjusted according to the rich liquid level compensation value of the carbon capturing and absorbing tower, and the target rich liquid flow is determined.

And then, according to the target rich liquid flow and the current rich liquid flow, adjusting the opening of the rich liquid flow adjusting valve.

Specifically, the rich liquid flow rate adjusting valve controls the magnitude of the rich liquid flow rate, and if the current rich liquid flow rate deviates from the target rich liquid flow rate, the opening degree of the rich liquid flow rate adjusting valve needs to be adjusted so that the current rich liquid flow rate is equal to or close to the target rich liquid flow rate.

The rich liquid level of the carbon trapping absorption tower can be kept in a normal range by adjusting the flow of the rich liquid, so that the safety and stability of a carbon trapping system are improved.

and determining a lean liquid level compensation value according to the current lean liquid level and the preset lean liquid level.

Specifically, the excessive high liquid level of the lean liquid in the carbon capture regeneration tower easily causes the solution to be unable to circulate, and when the liquid level is too low, the pump is caused to be emptied and the normal operation is not possible. The method for determining the rich liquid level compensation value is the same as the method for adjusting the lean liquid level in this embodiment, and will not be described in detail here.

And then, determining the target lean liquid flow according to the lean liquid level difference and the target alcohol amine liquid circulation amount.

Specifically, in this embodiment, the alcohol amine liquid circulation amount is taken as the lean liquid flow, the lean liquid flow is adjusted according to the lean liquid level compensation value of the carbon capture regeneration tower, and the target lean liquid flow is determined.

And then, according to the target lean solution flow and the current lean solution flow, adjusting the opening of the lean solution flow adjusting valve.

Specifically, the lean solution flow rate adjusting valve controls the magnitude of the lean solution flow rate, and if the current lean solution flow rate deviates from the target lean solution flow rate, the opening degree of the lean solution flow rate adjusting valve needs to be adjusted so that the current lean solution flow rate is equal to or close to the target lean solution flow rate.

The lean liquid level of the carbon capture regeneration tower can be kept in a normal range by adjusting the flow of the lean liquid, so that the safety and stability of a carbon capture system are improved.

Based on the same inventive concept, the embodiment of the present disclosure further provides a parameter adjusting device of a carbon capture system, as shown in fig. 9, the parameter adjusting device 90 of the carbon capture system includes an obtaining module 91 and a control module 92:

an acquisition module 91 for acquiring a control amount of the carbon capturing system, the control amount including a flow rate of flue gas entering the carbon capturing absorption tower or a target yield of carbon dioxide generated by the carbon capturing regeneration tower;

and the control module 92 is used for controlling the target alcohol amine liquid circulation amount flowing through the carbon capture absorption tower and the target steam flow flowing through the carbon capture regeneration tower according to the control amount and the standard value of the carbon dioxide content in the tail gas discharged from the carbon capture absorption tower.

Optionally, the control amount includes a flow of flue gas into the carbon capture absorber, and the control module 92 includes:

the first determining submodule is used for determining the circulation demand of the alcohol amine liquid according to the flue gas flow;

the second determining submodule is used for determining a carbon dioxide content compensation value according to the actual value of the carbon dioxide content in the tail gas and the standard value of the carbon dioxide content in the tail gas;

And the first control submodule is used for controlling the target alcohol amine liquid circulation quantity flowing through the carbon trapping absorption tower and the target steam flow flowing through the carbon trapping regeneration tower according to the carbon dioxide content compensation value and the alcohol amine liquid circulation quantity demand.

Optionally, the first determining submodule is configured to:

Optionally, the first control submodule is configured to:

Optionally, the apparatus further includes a first rich liquid flow adjusting module, including:

the third determining submodule is used for determining a rich liquid level compensation value according to the current rich liquid level and a preset rich liquid level, wherein the rich liquid is an alcohol amine liquid with carbon dioxide absorbed in the carbon capture absorption tower;

a fourth determining submodule, configured to determine a target opening degree of the rich liquid flow regulating valve according to the target alcohol amine liquid circulation amount;

and the first regulating submodule is used for regulating the opening of the rich liquid flow regulating valve according to the rich liquid level compensation value and the target opening.

Optionally, the apparatus 90 further includes a first lean solution flow adjustment module, including:

a fifth determining submodule, configured to determine a target opening of a lean solution flow regulating valve according to the target alcohol amine solution circulation amount, where the lean solution is an alcohol amine solution that does not absorb carbon dioxide in the carbon capture regeneration tower;

a sixth determining submodule, configured to determine a lean solution flow compensation value according to the target lean solution flow and the current lean solution flow;

and the second regulating submodule is used for regulating the opening of the lean liquid flow regulating valve according to the lean liquid flow compensation value and the target opening.

Optionally, the control amount includes a target yield of carbon dioxide produced by the carbon capture regeneration tower, and the control module 92 includes:

A seventh determining submodule, configured to determine a target flue gas flow according to the target yield of carbon dioxide and a standard value of carbon dioxide content in the tail gas;

an eighth determining submodule, configured to determine a circulation volume of the target alcohol amine solution according to a target yield of the carbon dioxide and a standard value of a carbon dioxide content in the tail gas;

and the ninth determination submodule is used for determining target steam flow according to the target alcohol amine liquid circulation quantity.

Optionally, the seventh determining submodule is configured to:

Optionally, the eighth determining submodule is configured to:

Optionally, the ninth determining submodule is configured to:

Optionally, the apparatus 90 further includes a second rich liquid flow adjustment module, including:

a tenth determination submodule, configured to determine a rich liquid level compensation value according to a current rich liquid level and a preset rich liquid level, where the rich liquid is an olamine solution in which carbon dioxide is absorbed in the carbon capture absorption tower;

an eleventh determination submodule, configured to determine a target rich liquid flow according to the rich liquid level compensation value and the target alkanolamine liquid circulation amount;

And the third regulating submodule is used for regulating the opening of the rich liquid flow regulating valve according to the target rich liquid flow and the current rich liquid flow.

Optionally, the apparatus 90 further includes a second lean solution flow adjustment module, including:

a twelfth determination submodule, configured to determine a lean solution level compensation value according to a current lean solution level and a preset lean solution level, where the lean solution is an alcohol amine solution that does not absorb carbon dioxide in the carbon capture regeneration tower;

a thirteenth determining submodule, configured to determine a target lean solution flow according to the lean solution level compensation value and the target alkanolamine solution circulation amount;

and the fourth regulating submodule is used for regulating the opening of the lean solution flow regulating valve according to the target lean solution flow and the current lean solution flow.

The specific manner in which the various modules perform the operations in the apparatus of the above embodiments have been described in detail in connection with the embodiments of the method, and will not be described in detail herein.

Fig. 10 is a block diagram of an electronic device 1000, shown in accordance with an exemplary embodiment. For example, the electronic device 1000 may be provided as a server. Referring to fig. 10, the electronic device 1000 includes a processor 1022, which may be one or more in number, and a memory 1032 for storing computer programs executable by the processor 1022. The computer programs stored in memory 1032 may include one or more modules each corresponding to a set of instructions. Further, processor 1022 may be configured to execute the computer program to perform the parameter tuning method of the carbon capture system described above.

In addition, the electronic device 1000 may also include a power component 1026 and a communication component 1050, the power component 1026 may be configured to perform power management of the electronic device 1000, and the communication component 1050 may be configured to enable communication of the electronic device 1000, such as wired or wireless communication. In addition, the electronic device 1000 may also include an input/output (I/O) interface 1058. The electronic device 1000 may operate based on an operating system stored in memory 1032.

In another exemplary embodiment, a computer readable storage medium is also provided, comprising program instructions which, when executed by a processor, implement the steps of the method of parameter adjustment of a carbon capture system described above. For example, the non-transitory computer readable storage medium may be the memory 1032 including program instructions described above that are executable by the processor 1022 of the electronic device 1000 to perform the method of parameter adjustment of the carbon capture system described above.

In another exemplary embodiment, a computer program product is also provided, comprising a computer program executable by a programmable apparatus, the computer program having code portions for performing the above-described method of parameter adjustment of a carbon capture system when executed by the programmable apparatus.

The preferred embodiments of the present disclosure have been described in detail above with reference to the accompanying drawings, but the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solutions of the present disclosure within the scope of the technical concept of the present disclosure, and all the simple modifications belong to the protection scope of the present disclosure.

Other embodiments of the disclosure will be apparent to those skilled in the art from consideration of the specification and practice of the disclosure. This disclosure is intended to cover any adaptations, uses, or adaptations of the disclosure following the general principles of the disclosure and including such departures from the present disclosure as come within known or customary practice within the art to which the disclosure pertains. It is intended that the specification and examples be considered as exemplary only, with a true scope and spirit of the disclosure being indicated by the following claims.

Moreover, any combination between the various embodiments of the present disclosure is possible as long as it does not depart from the spirit of the present disclosure, which should also be construed as the disclosure of the present disclosure.

Claims

1. A method of parameter adjustment for a carbon capture system, the method being applied to an alcohol amine absorption carbon capture system, the system comprising: the method comprises the steps of:

2. The method of parameter tuning of a carbon capture system of claim 1, wherein the control quantity comprises a flue gas flow rate into the carbon capture absorber;

3. The method for adjusting parameters of a carbon capture system according to claim 2, wherein determining the alcohol amine liquid circulation amount demand from the flue gas flow rate comprises:

4. The method for adjusting parameters of a carbon capturing system according to claim 2, wherein the controlling the target alcohol amine liquid circulation amount flowing through the carbon capturing absorber and the target steam flow flowing through the carbon capturing regenerator according to the carbon dioxide content compensation value and the alcohol amine liquid circulation amount demand amount comprises:

5. The method of parameter tuning of a carbon capture system of claim 2, further comprising:

6. The method of parameter tuning of a carbon capture system of claim 2, further comprising:

7. The method of parameter tuning of a carbon capture system of claim 1, wherein the control quantity comprises a target yield of carbon dioxide produced by the carbon capture regeneration tower;

8. The method for adjusting parameters of a carbon capture system according to claim 7, wherein determining a target flue gas flow rate based on the target yield of carbon dioxide and a standard value of carbon dioxide content in the exhaust gas comprises:

9. The method for adjusting parameters of a carbon capture system according to claim 7, wherein determining the target alkanolamine solution circulation amount based on the target yield of carbon dioxide and a standard value of carbon dioxide content in the tail gas comprises:

10. The method for adjusting parameters of a carbon capture system according to claim 7, wherein determining a target steam flow from the target alkanolamine liquid circulation amount comprises:

11. The method of parameter tuning of a carbon capture system of claim 5, further comprising:

12. The method of parameter tuning of a carbon capture system of claim 5, further comprising:

13. A parameter tuning device for a carbon capture system, the device comprising:

14. A non-transitory computer readable storage medium having stored thereon a computer program, characterized in that the program when executed by a processor realizes the steps of the method according to any of claims 1-12.

15. An electronic device, comprising:

a memory having a computer program stored thereon;

a processor for executing the computer program in the memory to implement the steps of the method of any one of claims 1-12.