CN217473172U

CN217473172U - Analysis system

Info

Publication number: CN217473172U
Application number: CN202221562185.1U
Authority: CN
Inventors: 王宇; 姚同林; 蒋俊彦; 张明珠; 刘常峰; 施嘉冬; 史少君; 吴洁; 石中玉; 季瑛珠; 王艳
Original assignee: SHANGHAI QIYAO EXPANDER CO Ltd
Current assignee: Shanghai Qiyao Energy Saving Technology Co ltd
Priority date: 2022-06-21
Filing date: 2022-06-21
Publication date: 2022-09-23
Anticipated expiration: 2032-06-21

Abstract

The application discloses analytic system includes: a resolution tower; a rich liquid input line; the lean solution reboiling pipeline is connected with the lean solution reboiling outlet and the lean solution reboiling inlet; a steam output pipeline, wherein the inlet end of the steam output pipeline is communicated with the steam outlet and is provided with a compressor, a reboiler and a gas-liquid separator which are sequentially arranged along the flowing direction of the steam outlet, and part of the reboiler is arranged on the lean liquid reboiling pipeline so that the mixed steam output pipeline and the lean liquid reboiling pipeline exchange heat with each other in the reboiler; and the condensate return pipeline is connected with the condensate outlet end of the gas-liquid separator and the condensate return inlet, and is provided with a first heat exchanger, and part of the first heat exchanger is arranged on the rich liquid input pipeline so that the condensate return pipeline and the rich liquid input pipeline exchange heat with each other in the first heat exchanger. The problem of the fresh steam of current analytic system and the big consumption of top of the tower cooling water can be solved.

Description

Analysis system

Technical Field

The application relates to the technical field of energy conservation and environmental protection, in particular to an analytic system.

Background

The flue gas generated in the production process of enterprises such as iron and steel, metallurgy, chemical industry and the like contains a large amount of SO ₂ (sulfur dioxide). In order to avoid air pollution, the desulfurization process is an essential step in flue gas treatment. Flue gas desulfurization techniques are classified into dry methods and wet methods according to the reaction state of the desulfurization process. In the wet desulphurization process, SO in the flue gas is treated by using organic amine solution ₂ The absorption method can ensure that the discharged flue gas reaches the standard, and avoids air pollution; at the same time, the above-mentioned SO is absorbed ₂ In organic amine solution (hereinafter referred to as "pregnant solution") (SO) ₂ Can also be separated out through analytic reaction, can realize the recycling of organic amine solution, and can also obtain SO with higher purity ₂ The method is used for producing sulfuric acid or sulfur and realizing resource recovery.

Usually, the rich solution is subjected to a desorption reaction in a desorption column. In the desorption tower, SO in the rich liquid ₂ Heated to separate out, thereby the organic amine solution (hereinafter referred to as barren liquor) is produced at the bottom of the desorption tower, and the SO-containing organic amine solution is produced at the top of the desorption tower ₂ (target gas) and condensing agent vapor. In practical process, continuously heating the barren liquor at the bottom of the desorption tower by using a reboiler to ensure that the temperature is maintained in a temperature range required by the desorption reaction; at the same time, it is necessary to condense the mixed steam for separation into cooled SO ₂ Gas and condensate.

In the prior art, external fresh steam is generally used as a heat source to be input into the reboiler, and the mixed steam is directly cooled by a cooling water heat exchanger. The research of the prior analytic process relates to the research of optimizing the cascade heat exchange of the mixed steam at the top of the analytic tower and the barren solution at the bottom of the analytic tower, for example, the research is carried out on the process of preheating the rich solution feed so as to reduce the consumption of circulating cooling water. However, the existing analysis system still needs to continuously consume a large amount of fresh steam and cooling water at the top of the tower, and the problem of high energy consumption still exists.

Therefore, it is desirable to design an analytic system to solve the above problems.

SUMMERY OF THE UTILITY MODEL

The application provides an analytic system to solve current analytic system and need continuously consume a large amount of live steam, and the scheduling problem that the energy consumption is high.

To achieve the above object, in one aspect, the present application provides a parsing system, including:

the desorption tower is provided with a rich liquid inlet, a mixed steam outlet, a condensate reflux inlet, a barren liquid reboiling outlet and a barren liquid reboiling inlet;

a rich liquid input pipeline, wherein the outlet end of the rich liquid input pipeline is connected with the rich liquid inlet;

a lean solution reboiling pipeline connected between the lean solution reboiling outlet and the lean solution reboiling inlet;

a mixed steam output pipeline, the inlet end of which is communicated with the mixed steam outlet and is provided with a compressor, a reboiler and a gas-liquid separator which are arranged in sequence along the flowing direction of the mixed steam outlet, wherein part of the reboiler is arranged on the lean solution reboiling pipeline, and the mixed steam output pipeline and the lean solution reboiling pipeline exchange heat with each other in the reboiler;

and the condensate return pipeline is connected between the liquid outlet end of the gas-liquid separator and the condensate return inlet and is provided with a first heat exchanger, part of the first heat exchanger is arranged on the rich liquid input pipeline, and the condensate return pipeline and the rich liquid input pipeline exchange heat with each other in the first heat exchanger.

Optionally, in some embodiments of the present application, the compressor is a screw compressor, a roots compressor, or a centrifugal compressor.

Optionally, in some embodiments herein, a reboiler pump is provided on the lean liquid reboiling line, the reboiler pump being located on the lean liquid reboiling line between the reboiler and the lean liquid reboiling outlet and the lean liquid reboiling inlet.

Optionally, in some embodiments of the present application, a target gas output pipeline is further included, and an inlet end of the target gas output pipeline is connected with a gas outlet end of the gas-liquid separator.

Optionally, in some embodiments of the present application, a reflux pump is provided on the condensate return line, the reflux pump being located between the gas-liquid separator and the first heat exchanger along the condensate return line.

Optionally, in some embodiments herein, the desorber further has a lean liquid outlet;

the analysis system further comprises a barren liquor output pipeline, and the inlet end of the barren liquor output pipeline is connected with the barren liquor outlet.

Optionally, in some embodiments of the present application, a second heat exchanger is further included, and the second heat exchanger is disposed on the rich liquid input pipeline and the lean liquid output pipeline to exchange heat between the lean liquid output pipeline and the rich liquid input pipeline.

Optionally, in some embodiments of the present application, the first heat exchanger is in series downstream of the second heat exchanger on the rich liquid input line; or,

the rich liquid input pipeline is provided with two rich liquid input branches which are connected in parallel with the rich liquid inlet, the first heat exchanger is arranged on the lean liquid output pipeline and one of the rich liquid input branches, and the second heat exchanger is arranged on the lean liquid output pipeline and the other of the rich liquid input branches.

Optionally, in some embodiments of the present application, a lean liquid pump is provided on the lean liquid output line, along which the lean liquid pump is located between the second heat exchanger and the desorber.

Optionally, in some embodiments of the present application, the system further comprises a compensation line, an inlet end of the compensation line is connected to an external refrigerant source or to a portion of the condensate return line between the gas-liquid separator and the first heat exchanger, and an outlet end of the compensation line is connected to the mixed vapor output line and upstream of the reboiler.

Optionally, in some embodiments of the present application, the reboiler further comprises a reboiling steam input line, an inlet end of the reboiling steam input line is connected to an external steam source, and an outlet end of the reboiling steam input line is connected to the steam output line and is located between the compressor and the reboiler, so as to selectively provide steam of the external steam source to the reboiler.

Optionally, in some embodiments of the present application, the apparatus further comprises a condenser connected between the mixed vapor outlet of the desorption tower and the gas-liquid inlet of the gas-liquid separator, for condensing the mixed vapor flowing out of the desorption tower.

Compared with the prior art, the analysis system has the advantages that the compressor, the reboiler and the gas-liquid separator are sequentially arranged on the output pipeline of the mixed steam, the liquid outlet end of the gas-liquid separator is connected to the condensate reflux inlet through the condensate reflux pipeline, and the temperature grade of the whole mixture of the analysis tower is improved by means of the compressor, so that the mixed steam can be used as a heat source of the reboiler to heat the lean solution in the lean solution reboiling pipeline; meanwhile, the lean solution of the lean solution reboiling pipeline condenses the mixed steam of the steam output pipeline into target gas and condensate, and the purpose of condensate reflux can be achieved by further means of the first heat exchanger.

Drawings

In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the description of the embodiments are briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.

Fig. 1 is a schematic diagram of a parsing system according to a first embodiment of the present application.

Fig. 2 is a schematic partial structure diagram of a parsing system according to a second embodiment of the present application.

The main reference numbers in the drawings accompanying the present specification are as follows:

1-analytic System; 10-a resolution tower; 20-rich liquid input line; 201-a first rich liquid input branch; 202-a second rich liquid input branch; 30-lean liquor output line; 31-a second heat exchanger; 32-a barren liquor pump; 40-lean solution reboiling pipeline; 401-a first reboiling branch; 402-a second reboiling branch; 41-reboiling pump; 50-mixed steam output pipeline; 51-a compressor; 52-a reboiler; 53-gas-liquid separator; 60-a condensate return line; 61-a first heat exchanger; 62-a reflux pump; 70-target gas output line; 80-a compensation pipeline; 90-reboiling steam input pipeline.

Detailed Description

The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only a part of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.

In the description of the present application, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, merely for convenience of description and simplicity of description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed in a particular orientation, and be operated, and thus, are not to be construed as limiting the present application.

The terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present application, "a plurality" means two or more unless otherwise specified.

In the description of the present application, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; they may be mechanically coupled, directly coupled, indirectly coupled through intervening media, or may be interconnected between two elements. The specific meaning of the above terms in the present application can be understood in a specific case by those of ordinary skill in the art.

For better understanding of the scheme of the present application, before describing the present application, it is necessary to make a brief explanation of some terms used in the description of the present application, and "rich liquid" means an absorbent that absorbs a target gas. "lean liquid" means an absorbent that does not absorb the target gas or an absorbent that has desorbed all or part of the absorbed target gas.

As shown in fig. 1, the present embodiment provides a desorption system 1, which includes a desorption tower 10, a rich liquid input line 20, a lean liquid reboiling line 40, a mixed vapor output line 50, and a condensate return line 60. Wherein the desorber 10 has a rich liquid inlet, a mixed vapor outlet, a condensate reflux inlet, a lean liquid reboiling outlet, and a lean liquid reboiling inlet. The outlet end of the rich liquid input line 20 is connected to the rich liquid inlet. The lean liquid reboiling line 40 is connected between the lean liquid reboiling outlet and the lean liquid reboiling inlet. The inlet end of the mixed steam outlet line 50 communicates with the mixed steam outlet, and has a compressor 51, a reboiler 52, and a gas-liquid separator 53 arranged in this order in the flow direction thereof. A part of the reboiler 52 is provided in the lean liquid reboiling line 40, and the mixed steam output line 50 and the lean liquid reboiling line 40 exchange heat with each other in the reboiler 52. The condensate return line 60 is connected between the liquid outlet end of the gas-liquid separator 53 and the condensate return inlet, and is provided with a first heat exchanger 61. Part of the first heat exchanger 61 is arranged on the rich liquid feed line 20, and the condensate return line 60 and the rich liquid feed line 20 exchange heat with each other in the first heat exchanger 61.

According to the desorption reaction, the product of the desorption tower 10 is high-temperature mixed steam and lean liquid. Wherein the mixed vapor includes a condensing agent vapor and the target gas. For example, the condensing agent may be water, and the corresponding condensed steam is water vapor. Further combining said target gas as SO ₂ The product of the desorption tower 10 is gas SO ₂ Gas and water vapor.

In the embodiment in which "the mixed steam output line 50 and the lean liquid reboiling line 40 exchange heat with each other in the reboiler 52", the reboiler 52 uses the mixed steam in the mixed steam output line 50 as a heat medium and uses the lean liquid in the lean liquid reboiling line 40 as a refrigerant, so that the mixed steam in the mixed steam output line 50 raises the temperature of the lean liquid in the lean liquid reboiling line 40 and the lean liquid in the lean liquid reboiling line 40 condenses the mixed steam in the mixed steam output line 50 into the target gas and the condensate in the reboiler 52.

In the embodiment in which the condensate return line 60 and the rich liquid inlet line 20 exchange heat with each other in the first heat exchanger 61, the first heat exchanger 61 uses the condensate in the condensate return line 60 as a heating medium and the rich liquid in the rich liquid inlet line 20 as a cooling medium, so that the condensate in the condensate return line 60 heats the rich liquid in the rich liquid inlet line 20 and the rich liquid in the rich liquid inlet line 20 cools the condensate in the condensate return line 60.

Thus far, in the analysis system 1 of the present application: the mixed steam of the desorption tower 10 firstly flows into the mixed steam output pipeline 50 through a mixed steam outlet; on the mixed steam output pipeline 50, the mixed steam enters the reboiler 52 after being subjected to the temperature and pressure increasing treatment by the compressor 51; at the reboiler 52, the mixed steam warms up the lean liquor of the lean liquor reboiling pipeline 40 while the mixed steam itself is condensed into a target gas and a condensate; then, the target gas and the condensate flow into the gas-liquid separator 53 to be subjected to gas-liquid separation, wherein the condensate flows into the condensate return line 60 via the liquid outlet end of the gas-liquid separator 53; at the first heat exchanger 61, the condensate heats up the rich liquid in the rich liquid input pipeline 20, and simultaneously the condensate itself further cools down; finally, the condensate flows back into the desorption tower 10 through the condensate reflux inlet.

Compared with the prior art, the desorption system 1 of the application utilizes the compressor 51 to increase the temperature grade of the mixed steam, so that the mixed steam can replace the original fresh steam as the heat source of the reboiler 52 to heat the lean solution in the lean solution reboiling pipeline 40, and the lean solution in the desorption tower 10 meets the temperature requirement of the desorption reaction, i.e. no additional fresh steam heat supply is needed; meanwhile, the mixed steam is condensed into condensate and low-temperature target gas by the lean solution, and the low-temperature target gas can directly flow into a subsequent sulfur product-related process, namely, an additional cooling process is not required. Furthermore, the condensate is further cooled by the rich liquid in the rich liquid input pipeline 20 through the first heat exchanger 61, so that the temperature of the condensate meets the temperature requirement of returning to the desorption tower 10, and the purpose of recycling the condensate is achieved without additional cooling water; meanwhile, the temperature of the rich liquid in the rich liquid input pipeline 20 is increased primarily, so that the energy consumption required for resolving the target gas in the rich liquid input pipeline 20 is reduced. Therefore, in the normal operation process of the whole analysis system 1, fresh steam or extra circulating cooling water does not need to be additionally provided, the heat balance of the analysis tower 10 is optimized, the analysis energy consumption is greatly reduced, and the economic benefit and the environmental benefit of energy conservation and emission reduction are obviously improved. Furthermore, the condensing agent of the whole analysis system 1 is also recycled, reducing the material loss of the analysis system 1.

It should be noted that: as shown in fig. 1, the arrows on the rich liquid input line 20 indicate the flow direction of the rich liquid in the rich liquid input line 20; the arrows on the above-mentioned lean liquid reboiling line 40 indicate the flow direction of the lean liquid in the lean liquid reboiling line 40; the arrows on the mixed steam output pipeline 50 indicate the flowing direction of the mixed steam in the mixed steam output pipeline 50; the arrows on the condensate return line 60 indicate the direction of flow of condensate in the condensate return line 60.

In one embodiment, the analytical tower 10 includes a housing having a generally oblong container in the up-down direction, defining an interior cavity therein. Wherein the lean reboil inlet and the lean reboil outlet are formed at a bottom of the housing, the rich inlet is formed at a middle of the housing, and the condensate return inlet and the mixed vapor outlet are formed at a top of the housing. Due to the arrangement, the distribution rule of the tower top product and the tower bottom product in the desorption tower 10 is better met, and the mixed steam and the barren solution are conveniently led out.

Wherein the inlet end of the rich liquid input line 20 can be connected to an external rich liquid source to deliver the rich liquid to be subjected to the desorption reaction to the desorption tower 10. In one embodiment, the inlet end of the rich liquid input line 20 is connected to the outlet end of an absorption tower, so as to provide the rich liquid generated in the absorption tower to the desorption tower 10.

Referring to fig. 1, the compressor 51, the reboiler 52 and the gas-liquid separator 53 are sequentially arranged in the mixed steam output line 50 along the flow direction of the mixed steam.

Wherein the inlet end of the compressor 51 is used as the inlet end of the mixed vapor output pipeline 50 and is communicated with the mixed vapor outlet. The compressor 51 is used as a temperature increasing and pressure increasing device for increasing the heat source grade of the mixed steam, so that the mixed steam replaces the original fresh steam to be used as the heating medium of the reboiler 52. In particular implementations, the compressor 51 may be one of a screw compressor, a roots compressor, or a centrifugal compressor. Preferably, the compressor 51 is a screw compressor.

In one embodiment, the reboiler 52 has a heating medium circuit and a cooling medium circuit that exchange heat with each other. The refrigerant pipeline of the reboiler 52 is disposed on the lean liquid reboiling pipeline 40, so that the refrigerant pipeline, the lean liquid reboiling pipeline 40, and the desorption tower 10 form a lean liquid reboiling circulation loop. And the heat medium line is disposed on the mixed vapor output line 50 between the compressor 51 and the gas-liquid separator 53. In a specific implementation, the reboiler 52 may be a plate heat exchanger, a tube heat exchanger, or a falling film heat exchanger.

In this application, wherein a cooling medium pipeline or a heating medium pipeline is disposed on a pipeline, it may be understood that the cooling medium pipeline or the heating medium pipeline is configured as a part of the pipeline, or the cooling medium pipeline or the heating medium pipeline is connected to the pipeline.

With reference to FIG. 1, the lean liquid reboiling circuit 40 has a first reboiling branch 401 and a second reboiling branch 402. Wherein the inlet end of the first reboiling branch 401 is connected to the lean liquid reboiling outlet of the desorption tower 10, and the outlet end thereof is connected to the inlet end of the refrigerant pipeline of the reboiler 52. The inlet end of the second reboiling branch 402 is communicated with the outlet end of the refrigerant pipeline of the reboiler 52, and the outlet end thereof is connected to the lean liquid reboiling inlet of the desorption tower 10. In short, the first reboiling branch 401, the refrigerant line of the reboiler 52, and the second reboiling branch 402 are connected in series in this order.

In some of these embodiments, a reboiler pump 41 is provided in the lean liquid reboiler line 40 to drive the circulating flow of lean liquid in the lean liquid reboiler cycle. The circulation flow speed of the lean liquid in the lean liquid reboiling circulation loop can be controlled by arranging the reboiling pump 41, and the heat exchange working condition of the reboiler 52 can also be controlled. In this embodiment, the reboiling pump 41 may be located on the first reboiling branch 401. In yet other embodiments, the reboiling pump 41 is located on the second reboiling branch 402.

Wherein the gas-liquid separator 53 receives the condensate and the target gas flowing out from the reboiler 52 and performs gas-liquid separation of the condensate and the target gas. Illustratively, the top of the gas-liquid separator 53 is provided with a gas-liquid inlet and a gas outlet, and the bottom is provided with a liquid outlet, wherein the gas-liquid inlet, the gas outlet and the liquid outlet are respectively configured as a gas-liquid inlet end, a gas outlet end and a liquid outlet end of the gas-liquid separator 53. Specifically, the gas-liquid inlet of the gas-liquid separator 53 communicates with the outlet end of the heating medium line of the reboiler 52, and the liquid outlet communicates with the inlet end of the condensate return line 60.

Further, in order to lead out the target gas separated by the gas-liquid separator 53, the analysis system 1 further includes a target gas output line 70, and an inlet of the target gas output line 70 is connected to a gas outlet of the gas-liquid separator 53. The arrows on the above-mentioned target gas output line 70 indicate the flow direction of the target gas in the target gas output line 70.

As can be seen, the gas-liquid separator 53 is disposed on the mixed vapor output line 50, the condensate return line 60, and the target gas output line 70 at the same time to achieve separation and diversion of the target gas and the condensate.

In one embodiment, the output end of the target gas output line 70 is communicated with a sulfur product related device to deliver the low-temperature target gas to the sulfur product related device. Wherein the sulfur product-related plant may be a plant for producing liquid sulfur dioxide, sulfuric acid, sulfur, and other chemical products.

Referring to fig. 1, the inlet end of the condensate return line 60 is connected to the liquid outlet of the gas-liquid separator 53, and the outlet end of the condensate return line 60 is connected to the condensate return inlet of the desorption tower 10, so as to return the condensate into the desorption tower 10. The condensate is refluxed to the desorption tower 10 through the condensate reflux pipeline 60, so that the total amount of the condensing agent in the whole desorption system 1 is continuously maintained in a stable range, and the consumption of the condensing agent is reduced.

As previously described, the condensate reflux inlet is located at the top of the stripper column 10. That is, the condensate is sprayed downwards from the top of the desorption tower 10, and the mixed vapor flows upwards in the desorption tower 10 from the bottom, so that the mixed vapor is more fully contacted with the condensate to wash away the absorbent vapor included in the mixed vapor, and the absorbent loss is reduced.

Specifically, the first heat exchanger 61 has a heat medium pipeline and a refrigerant pipeline which exchange heat with each other. The heat medium pipeline of the first heat exchanger 61 is arranged on the condensate return pipeline 60, and the refrigerant pipeline thereof is arranged on the rich liquid input pipeline 20. More specifically, the heat medium line of the first heat exchanger 61 is connected between the gas-liquid separator 53 and the condensate return inlet of the desorption tower 10, and the refrigerant line of the first heat exchanger 61 is configured as a partial section of the rich liquid input line 20.

Further, a return pump 62 is provided on the condensate return line 60. Along the condensate return line 60, the return pump 61 is located between the gas-liquid separator 53 and the first heat exchanger 61, and is configured to provide a driving force for the condensate in the condensate return line 60, so as to drive the condensate flowing out from the gas-liquid separator 53 to flow to the first heat exchanger 61. Therefore, the flow or the flow speed in the condensate return pipeline 60 can be adjusted through adjusting the rotating speed of the return pump 62, and the heat exchange working condition of the first heat exchanger 61 can be adjusted and controlled.

With continued reference to fig. 1, the analysis system 1 further includes a compensation pipeline 80, and the compensation pipeline 80 is used for performing liquid compensation (i.e. liquid replenishment) on the compressor 51. Wherein the arrows on the compensation line 80 indicate the flow direction of the compensation liquid in the compensation line 80.

In particular, the compensation liquid may be the condensate in the condensate return line 60.

Based on the above embodiment, the inlet end of the compensation pipeline 80 is connected to the outlet end of the reflux pump 62, and the outlet end of the compensation pipeline 80 is connected to the inlet end of the compressor 51. At this time, the compensation line 80 may compensate the inlet end of the compressor 51 with the condensate.

It will be appreciated that the position at which the compressor 51 is liquid compensated may be adjusted depending on the arrangement of the compressor 51 or superheat requirements. That is, the position of the outlet end of the compensating pipe 80 can be adjusted. For example, condensate compensation may also be performed on the outlet side of the compressor 51. In this case, the outlet end of the compensation pipe 80 is connected to the outlet end of the compressor 51.

In a specific implementation, a compensation adjusting valve may be disposed on the compensation pipeline 80 to control whether the compensation pipeline 80 performs fluid compensation on the compressor 51, and to control a fluid compensation mode or a fluid compensation amount of the compensation pipeline 80.

The above schematically provides the case where the compensation line 80 is replenished with condensate from the condensate return line 60. However, it should be noted that the embodiment of the compensating pipe 80 described in the present application is not limited thereto. In other embodiments, the compensation pipe 80 is configured to reserve an external compensation pipe, i.e. the inlet end of the compensation pipe 80 is connected to an external condensate source. In this case, the liquid may be replenished by directly using the condensate of the external condensate source.

Referring to fig. 1, the desorption tower 10 further has a barren solution outlet communicated with an inner cavity thereof, and the desorption system 1 further includes a barren solution output pipeline 30, an inlet end of the barren solution output pipeline 30 is connected to the barren solution outlet for guiding out barren solution of the desorption tower 10. Wherein the above-mentioned arrow on the lean liquid output pipe 30 indicates the flow direction of the lean liquid in the lean liquid output pipe 30.

In specific implementation, the desorption tower 10 further includes a lean liquid tank, and an output end of the lean liquid output pipeline 30 is connected to the lean liquid tank, so as to input and temporarily store the lean liquid in the lean liquid tank. The lean solution tank is also communicated with the absorption tower and is used for supplementing lean solution into the absorption tower.

Based on the above embodiment, the desorption system 1 further includes the second heat exchanger 31, and the second heat exchanger 31 is disposed on the rich liquid input pipeline 20 and the lean liquid output pipeline 30 at the same time, so that the lean liquid output pipeline 30 and the rich liquid input pipeline 20 exchange heat with each other. Through the heat exchange at the second heat exchanger 31, the temperature of the high-temperature lean solution flowing out of the desorption tower 10 in the lean solution output pipeline 30 is reduced, so that the lean solution enters the previous process stage of absorbing the target gas, and meanwhile, the temperature of the low-temperature rich solution in the rich solution input pipeline 20 is initially increased, thereby reducing the heat requirement for desorption of the rich solution in the desorption tower 10.

Specifically, the second heat exchanger 31 includes a heat medium pipeline and a cooling medium pipeline, which exchange heat with each other. The heat medium pipeline of the second heat exchanger 31 is arranged on the lean liquid output pipeline 30, and the refrigerant pipeline is arranged on the rich liquid input pipeline 20.

In the present embodiment, the first heat exchanger 61 is connected in series downstream of the second heat exchanger 31 on the rich liquid input line 20. More specifically, the refrigerant line of the first heat exchanger 61 is connected in series with the refrigerant line of the second heat exchanger 31 downstream of the rich liquid input line 20.

Further, a lean liquid pump 32 is provided on the lean liquid output line 30. Along the lean liquid output line 30, the lean liquid pump 32 is located between the second heat exchanger 31 and the desorption tower 10. The flow speed of the lean solution can be controlled by the lean solution pump 32, and the heat exchange condition of the second heat exchanger 31 can be adjusted.

With continued reference to fig. 1, in some embodiments, the desorption system 1 further includes at least one reboiled vapor input line 90. Wherein the reboiled vapor input line 90 represents the direction of flow of vapor within the reboiled vapor input line 90.

Specifically, the inlet end of the reboiled steam input line 90 is connected to an external steam source, the outlet end of the reboiled steam input line 90 is connected to the inlet end of the heating medium line of the reboiler 52, and the reboiled steam input line 90 is used to selectively provide steam from the external steam heat source to the reboiler 52.

In the present embodiment, the reboiled steam input line 90 is configured with a start-up mode of operation, i.e., a start-up phase steam supply mode. I.e., the reboil steam input 90 is used to provide startup phase steam to the reboiler 52, and the reboil steam input 90 is closed during normal operation of the desorption system. In this case, the entire desorption system 1 does not need an additional fresh steam supply, and the heat energy required by the reboiler 52 is provided by the mixed steam after being warmed and pressurized by the compressor 51.

In still other embodiments, the reboiled steam input 90 is configured with a back-up mode of operation, i.e., a failed stage steam supply mode. More specifically, the reboiled steam input line 90 serves as a backup heat source, and when the condensate return line 60 or the mixed steam output line 50 fails, fresh steam can be provided to the reboiler 52 to meet the requirement of raising the temperature of the lean solution of the desorption tower 10 again, so that the reliability and stability of the operation of the desorption system 1 are improved.

Alternatively, the reboiled steam input 90 is configured with a supplemental mode of operation. More specifically, the reboiling steam input line 90 may provide heat source steam to the desorption system 1 when the operating condition of the desorption system 1 changes, so as to ensure that the reboiler 52 stably re-heats the lean solution of the desorption tower 10. It should be noted that the above is only an exemplary embodiment of the reboiled steam input line 90, and the specific embodiment of the reboiled steam input line 90 in the present application is not limited thereto.

In some of the embodiments, the desorption system 1 further comprises a condenser connected between the mixed vapor outlet of the desorption tower 10 and the gas-liquid inlet of the gas-liquid separator 53 to condense the mixed vapor from the desorption tower 10. When the condensate return pipeline 60 or the gas-liquid output pipeline 50 fails, the condenser is used as a backup cooling pipeline to ensure the condensation effect on the mixed steam and prevent the influence on the separation and purification of the target gas.

In one embodiment, the target gas may be SO ₂ . In this case, the absorbent may be an organic amine type desulfurizing agent. The organic amine desulfurizer absorbs sulfur dioxide at a lower temperature, and decomposes sulfur dioxide at a higher temperature. Further, the organic amine desulfurizing agent may be dimethylaniline, monoethanolamine or diethanolamine. However, it should be noted that the absorbent of the present application is not limited to the above desulfurizing agent as long as the absorbent used can absorb and resolve SO at different temperatures, respectively ₂ It is sufficient.

In still other embodiments, the target gas may also be carbon dioxide (CO) ₂ ) Or nitrogen dioxide (NO) ₂ ) One kind of (1). It will be appreciated that the adsorbent is adapted according to the type of target gas. When the target gas is CO ₂ In this case, the absorbent may be alcohol amine. The alcohol amine includes alkyl alcohol amine and alkylene alcohol amine, and the alkyl alcohol amine includes primary amine (represented by ethanolamine MEA), secondary amine (represented by DEA), and tertiary amine (represented by MDEA).

Referring to fig. 2, the present application further provides a second embodiment of the parsing system 1. Compared to the analysis system 1 in fig. 1, the main difference of the analysis system 1 in fig. 2 is that: the first heat exchanger 61 and the second heat exchanger 31 are arranged in parallel with each other. In particular, the rich liquid inlet line 20 has a first rich liquid inlet branch 201 and a second rich liquid inlet branch 202 connected in parallel to the rich liquid inlet of the stripping column. Wherein the first heat exchanger 61 is arranged on the condensate return line 60 and the first rich liquid inlet branch 201, and the second heat exchanger 31 is arranged on the lean liquid outlet line 30 and the second rich liquid inlet branch 202.

In other embodiments, the first heat exchanger 61 is disposed on the condensate return line 60 and the second rich liquid input branch 202, and the second heat exchanger 31 is disposed on the lean liquid output line 30 and the first rich liquid input branch 201.

In the description herein, particular features, structures, materials, or characteristics may be combined in any suitable manner in any one or more embodiments or examples.

The above description is only for the specific embodiments of the present application, but the scope of the present application is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present application, and shall be covered by the scope of the present application. Therefore, the protection scope of the present application shall be subject to the protection scope of the claims. In addition, the principle and the implementation of the present application are illustrated by applying specific examples in the specification, the above description of the embodiments is only for assisting understanding of the method and the core idea of the present application, and the content of the present application should not be construed as limiting the present application.

Claims

1. A parsing system, comprising:

a lean liquid reboiling line connected between the liquid reboiling outlet and the lean liquid reboiling inlet;

2. The resolving system of claim 1 wherein the compressor is a screw compressor, roots compressor, or centrifugal compressor.

3. The desorption system of claim 1 wherein a reboiler pump is provided in the lean reboil line and the reboiler pump is located in the lean reboil line between the lean reboil outlet and the lean reboil inlet.

4. The analytic system of claim 1, further comprising a target gas output line, an inlet end of the target gas output line connected to a gas outlet end of the gas-liquid separator.

5. The resolution system of claim 1, wherein a reflux pump is disposed on the condensate return line, the reflux pump being positioned between the gas-liquid separator and the first heat exchanger along the condensate return line.

6. The desorption system of claim 1, wherein the desorption tower further has a lean liquid outlet;

7. The desorption system of claim 6, further comprising a second heat exchanger disposed on the rich liquid input line and the lean liquid output line to exchange heat between the lean liquid output line and the rich liquid input line.

8. The resolution system of claim 7, wherein the first heat exchanger is in series downstream of the second heat exchanger on the rich liquid input line; or,

9. The desorption system of claim 7 wherein a lean liquid pump is disposed on the lean liquid output line, the lean liquid pump being positioned between the second heat exchanger and the desorption tower along the lean liquid output line.

10. The resolving system of claim 1 further comprising a compensating line having an inlet end connected to an external source of condensate or to a portion of the condensate return line between the gas-liquid separator and the first heat exchanger, and an outlet end connected to the mixed vapor output line upstream of the reboiler.

11. The desorption system of claim 1 further comprising a reboil vapor input line having an inlet end connected to an external source of vapor and an outlet end connected to the vapor output line and positioned between the compressor and the reboiler to selectively provide vapor from the external source of vapor to the reboiler.

12. The desorption system of claim 1, further comprising a condenser connected between the mixed vapor outlet of the desorption column and the gas-liquid inlet end of the gas-liquid separator to condense the mixed vapor flowing out of the desorption column.