Process condensate recovery system
By designing the process condensate recovery system, using the booster pipeline and bypass pipeline combined with the booster pump and valve control, the problem of pipeline shaking and high energy consumption in the process condensate recovery system is solved, and stable operation and energy consumption savings are achieved.
Patent Information
- Application Number
- CN202422407112.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-30
- Publication Date
- 2025-07-22
- Estimated Expiration
- 2034-09-30
AI Technical Summary
There are problems in the existing process condensate recovery system with severe pipeline shaking, pipeline rupture, unstable operation and high energy consumption.
A process condensate recovery system is designed, including a process condensate input pipeline, a first heat exchanger, a stripping tower, a stripping condensate output pipeline, a stripping condensate heat exchange pipeline, a stripping condensate export pipeline and a second heat exchanger. By setting up a boosting pipeline and a bypass pipeline, the conveying path is selected according to the pressure of the downstream device, and combined with the boosting pump and valve control, stable transportation is achieved.
It saves energy consumption of the recycling system, avoids pipeline shaking, improves operating stability, and reduces the risk of pipeline rupture.
Smart Images
Figure CN223127288U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of petrochemical engineering, and particularly relates to a recovery system for process condensate. Background Art
[0002] As a by-product of the methanation reaction, process condensate has a large output. After being processed by a recovery system, it needs to be sent to the slag water unit of the downstream gasification device and / or the circulating water device for reuse to achieve the purpose of saving energy. However, in the current recovery system for process condensate, there are problems such as severe pipeline shaking, possible pipeline rupture, unstable operation, and high energy consumption. Summary of the Utility Model
[0003] The purpose of the utility model is to provide a recovery system for process condensate, which can save the energy consumption of the recovery system, avoid pipeline shaking in the recovery system, and improve the operation stability of the recovery system.
[0004] In order to achieve the above purpose and other related purposes, the utility model is realized by the following technical solutions.
[0005] The utility model provides a recovery system for process condensate, which at least includes:
[0006] A process condensate input pipeline;
[0007] A first heat exchanger, connected to the process condensate input pipeline;
[0008] A heated condensate output pipeline, connected to the process condensate input pipeline through the first heat exchanger; A stripping tower, connected to one end of the heated condensate output pipeline far from the first heat exchanger;
[0009] A stripped condensate output pipeline, connecting the stripping tower and the first heat exchanger;
[0010] A stripped condensate heat exchange pipeline, connected to the stripped condensate output pipeline through the first heat exchanger;
[0011] A stripped condensate external delivery pipeline, connected to the stripped condensate heat exchange pipeline, and the stripped condensate external delivery pipeline includes a pressurizing pipeline and a bypass pipeline arranged in parallel;
[0012] A second heat exchanger, connecting the stripped condensate heat exchange pipeline and the stripped condensate external delivery pipeline; and
[0013] At least one downstream device, connected to the stripped condensate external delivery pipeline.
[0014] In an embodiment of the present utility model, the pressurizing pipeline is at least one. When there are multiple pressurizing pipelines, after the multiple pressurizing pipelines are arranged in parallel, they are connected in parallel with the bypass pipeline to the second heat exchanger.
[0015] In an embodiment of the present utility model, a pressurizing pump is provided on the pressurizing pipeline. When there are multiple pressurizing pipelines, the pressurizing pumps are respectively provided on the multiple pressurizing pipelines.
[0016] In an embodiment of the present utility model, the recovery system further includes a reflux pipeline, and the reflux pipeline connects the outlet of the pressurizing pump and the stripping column.
[0017] In an embodiment of the present utility model, at least one valve is provided on the bypass pipeline.
[0018] In an embodiment of the present utility model, when there are multiple downstream devices, after the multiple downstream devices are arranged in parallel, they are connected to the stripping condensate outgoing pipeline.
[0019] In an embodiment of the present utility model, the recovery system further includes a cold medium input pipeline, and the cold medium input pipeline is connected to the second heat exchanger.
[0020] In an embodiment of the present utility model, the recovery system further includes a cold medium output pipeline, and the cold medium output pipeline is connected to the cold medium input pipeline through the second heat exchanger.
[0021] In an embodiment of the present utility model, a steam input pipeline is provided on the stripping column, and the steam input pipeline is connected to the stripping column.
[0022] In an embodiment of the present utility model, the recovery system further includes an output pipeline and a branch pipeline, and the output pipeline and the branch pipeline are arranged in parallel between the stripping condensate outgoing pipeline and the downstream device.
[0023] In summary, the present utility model provides a recovery system for process condensate, which can save the energy consumption of the recovery system and increase the economic benefits of the recovery system. Moreover, the recovery system for process condensate provided by the present utility model can avoid the pipelines in the recovery system from shaking, reduce the risk of pipeline rupture, and improve the operation stability of the recovery system.
[0024] Of course, it is not necessary to achieve all the above advantages simultaneously when implementing any mode of the present utility model. BRIEF DESCRIPTION OF THE DRAWINGS
[0025] To more clearly illustrate the technical solutions of the embodiments of the present invention, the following will briefly introduce the drawings required for the description of the embodiments. Obviously, the drawings in the following description are only some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.
[0026] Figure 1 It is a schematic diagram of the process condensate recovery system in an embodiment of the present invention.
[0027] Marking description:
[0028] 11. Process condensate input pipeline; 12. First heat exchanger; 13. Heated condensate output pipeline; 14. Stripping column; 15. Steam input pipeline; 16. Stripped condensate output pipeline; 17. Stripped condensate heat exchange pipeline; 18. Stripped condensate external delivery pipeline; 181. Bypass pipeline; 182. Boosting pipeline; 1821. First boosting pipeline; 1822. Second boosting pipeline; 19. First booster pump; 20. Second booster pump; 21. Return pipeline; 211. First return pipeline; 212. Second return pipeline; 22. Cold medium input pipeline; 23. Cold medium output pipeline; 24. Second heat exchanger; 25. Downstream device; 251. First device; 252. Second device; 26. Output pipeline; 27. Branch pipeline. Specific embodiments
[0029] The following illustrates the embodiments of the present invention through specific examples. Those skilled in the art can easily understand other advantages and effects of the present invention from the content disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments. Various details of the present invention can also be modified or changed based on different viewpoints and applications without departing from the spirit of the present invention. It should be noted that, without conflict, the following embodiments and the features in the embodiments can be combined with each other.
[0030] It should be noted that the drawings provided in the following embodiments only schematically illustrate the basic concept of the present invention. Therefore, only the components related to the present invention are shown in the drawings, rather than being drawn according to the number, shape, and size of the components in actual implementation. The type, quantity, and ratio of each component in actual implementation can be arbitrarily changed, and the component layout type may also be more complex.
[0031] In the present utility model, it should be noted that when terms such as "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. appear, the orientation or positional relationship indicated is based on the orientation or positional relationship shown in the drawings. This is only for the convenience of describing the present application and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation. Therefore, it should not be construed as a limitation to the present application. In addition, when terms such as "first" and "second" appear, they are only used for descriptive and distinguishing purposes and cannot be construed as indicating or implying relative importance.
[0032] Please refer to Figure 1 As shown, the present utility model provides a process condensate recovery system, for example, including a process condensate input pipeline 11, a first heat exchanger 12, a heated condensate output pipeline 13, a stripping tower 14, a stripped condensate output pipeline 16, a stripped condensate heat exchange pipeline 17, a stripped condensate external delivery pipeline 18, a second heat exchanger 24, and a downstream device 25, etc. Among them, the process condensate input pipeline 11 and the heated condensate output pipeline 13 are connected through the first heat exchanger 12. One end of the heated condensate output pipeline 13 far from the first heat exchanger 12 is connected to the stripping tower 14. The stripped condensate output pipeline 16 connects the stripping tower 14 and the first heat exchanger 12. The stripped condensate output pipeline 16 and the stripped condensate heat exchange pipeline 17 are connected through the first heat exchanger 12. The stripped condensate heat exchange pipeline 17 and the stripped condensate external delivery pipeline 18 are connected through the second heat exchanger 24. The stripped condensate external delivery pipeline 18 includes a bypass pipeline 181 and a pressurization pipeline 182 arranged in parallel and is connected to the downstream device 25. In the process condensate recovery system provided by the present utility model, according to the pressure of the downstream device 25, the bypass pipeline 181 or the pressurization pipeline 182 can be selected to transport the stripped condensate to the downstream device 25, thereby being able to save energy consumption and avoid the pipelines in the recovery system from shaking, improving the operation stability of the recovery system. The process condensate recovery system provided by the present utility model can be applied to various process condensate recovery systems. In this embodiment, taking the recovery of the process condensate generated by the methanation reaction as an example, the recovery system is described.
[0033] Please refer to Figure 1 As shown, in an embodiment of the present utility model, the process condensate input pipeline 11 is used to input process condensate. Among them, the temperature of the process condensate is, for example, 20°C - 50°C, and the main component of the process condensate is water. If the process condensate is directly discharged, it will cause waste of water resources. Therefore, the process condensate must be recovered and reused.
[0034] Please refer to Figure 1As shown, in an embodiment of the present utility model, the heated condensate output pipeline 13 is connected to the process condensate input pipeline 11, and the heated condensate output pipeline 13 and the process condensate input pipeline 11 are connected through a first heat exchanger 12. Specifically, the process condensate input pipeline 11 transports the process condensate into the first heat exchanger 12. The process condensate serves as the cold fluid and exchanges heat with the hot fluid of the first heat exchanger 12. The heated process condensate flows out of the first heat exchanger 12 through the heated condensate output pipeline 13. Among them, the temperature of the heated process condensate is, for example, 120°C - 140°C. The first heat exchanger 12 is, for example, one of the shell-and-tube heat exchangers, jacketed heat exchangers, spray heat exchangers, and plate heat exchangers and other wall-type heat exchangers to prevent the process condensate and the hot fluid in the first heat exchanger 12 from contacting and mixing and prevent the process condensate from being contaminated.
[0035] Please refer to Figure 1 As shown, in an embodiment of the present utility model, the stripping tower 14 is connected to the end of the heated condensate output pipeline 13 far from the first heat exchanger 12. Specifically, the top of the stripping tower 14 is connected to the outlet of the heated condensate output pipeline 13. The heated condensate output pipeline 13 transports the high-temperature process condensate into the stripping tower 14, and the acidic gas in the process condensate is stripped out and leaves from the top of the stripping tower 14. By setting the stripping tower 14, it is used to remove the acidic gas in the process condensate and prevent the acidic gas from contaminating the downstream device 25.
[0036] Please refer to Figure 1 As shown, in an embodiment of the present utility model, a steam input pipeline 15 is also provided on the stripping tower 14, and the steam input pipeline 15 is connected to the stripping tower 14. In this embodiment, the steam input pipeline 15 is connected to the bottom of the stripping tower 14. Specifically, in the stripping tower 14, the steam transported by the steam input pipeline 15 and the process condensate transported by the heated condensate output pipeline 13 are in countercurrent contact, and the acidic gas in the process condensate is stripped out by the steam and becomes pure stripped condensate, which leaves from the bottom of the stripping tower 14.
[0037] Please refer to Figure 1 As shown, in an embodiment of the present utility model, the stripped condensate output pipeline 16 connects the stripping tower 14 and the first heat exchanger 12. Specifically, since the steam transported by the steam input pipeline 15 enters the steam stripping tower 14 and the steam contacts and exchanges heat with the process condensate, the stripped condensate leaving from the bottom of the stripping tower 14 maintains a relatively high temperature. Therefore, by setting the stripped condensate output pipeline 16, the stripped condensate is introduced from the stripping tower 14 into the first heat exchanger 12. The stripped condensate serves as the hot fluid and heats the process condensate input into the first heat exchanger 12 by the process condensate input pipeline 11.
[0038] Please refer to Figure 1As shown, in an embodiment of the present utility model, between the stripping condensate heat exchange pipeline 17 and the stripping condensate output pipeline 16, they are connected through the first heat exchanger 12. Specifically, the stripping condensate output pipeline 16 conveys the stripping condensate into the first heat exchanger 12, heating the process condensate input pipeline 11 to input the process condensate into the first heat exchanger 12, while the stripping condensate is cooled and leaves the first heat exchanger 12 from the stripping condensate heat exchange pipeline 17. Among them, the temperature of the stripping condensate in the stripping condensate heat exchange pipeline 17 is, for example, 140°C - 150°C, and the pressure is, for example, 0.1 MPa - 0.3 MPa.
[0039] Please refer to Figure 1 As shown, in an embodiment of the present utility model, a second heat exchanger 24 is provided at the outlet of the stripping condensate heat exchange pipeline 17. Specifically, since the temperature of the stripping condensate in the stripping condensate heat exchange pipeline 17 is high, if the stripping condensate in the stripping condensate heat exchange pipeline 17 is directly sent to the downstream device 25, the heat of the stripping condensate will be wasted. Therefore, by setting the second heat exchanger 24, the stripping condensate in the stripping condensate heat exchange pipeline 17 is input into the second heat exchanger 24. The stripping condensate serves as a hot fluid and exchanges heat with the cold fluid in the second heat exchanger 24 to recover the heat of the stripping condensate in the stripping condensate heat exchange pipeline 17. Among them, the second heat exchanger 24 is, for example, one of the shell-and-tube heat exchangers, jacketed heat exchangers, spray heat exchangers, and plate heat exchangers and other wall-type heat exchangers to prevent the stripping condensate and the cold fluid in the second heat exchanger 24 from contacting and mixing and prevent the stripping condensate from being contaminated.
[0040] Please refer to Figure 1 As shown, in an embodiment of the present utility model, a cold medium input pipeline 22 and a cold medium output pipeline 23 are further provided on the second heat exchanger 24. The cold medium input pipeline 22 and the cold medium output pipeline 23 are connected through the second heat exchanger 24. Specifically, the cold medium input pipeline 22 conveys the cold medium into the second heat exchanger 24 as a cold fluid to exchange heat with the stripping condensate conveyed by the stripping condensate heat exchange pipeline 17 into the second heat exchanger 24. The cold medium is heated and leaves the second heat exchanger 24 from the cold medium output pipeline 23. Among them, the cold medium in the cold medium input pipeline 22 is, for example, a gas or a liquid. In this embodiment, the cold medium is, for example, demineralized water to prevent the cold medium from corroding the second heat exchanger 24. The temperature of the cold medium in the cold medium input pipeline 22 is, for example, 40°C - 60°C, and the temperature of the cold medium in the cold medium output pipeline 23 is, for example, 100°C - 120°C.
[0041] Please refer to Figure 1As shown, in an embodiment of the present utility model, a stripping condensate external delivery pipeline 18 is connected to a stripping condensate heat exchange pipeline 17 through a second heat exchanger 24. Specifically, the stripping condensate heat exchange pipeline 17 conveys the stripping condensate into the second heat exchanger 24. After the stripping condensate is cooled, it leaves the second heat exchanger 24 from the stripping condensate external delivery pipeline 18 and is sent to a downstream device 25. Among them, the temperature of the stripping condensate in the stripping condensate external delivery pipeline 18 is, for example, 60°C - 80°C, and the pressure is, for example, 0.1 MPa - 0.3 MPa.
[0042] Please refer to Figure 1 As shown, in an embodiment of the present utility model, the stripping condensate external delivery pipeline 18, for example, includes a bypass pipeline 181, a pressurization pipeline 182, etc. Among them, the inlet of the bypass pipeline 181 is connected to the stripping condensate heat exchange pipeline 17 through the second heat exchanger 24, and the outlet of the bypass pipeline 181 is connected to the downstream device 25. In this embodiment, when the pressure of the downstream device 25 is lower than the pressure of the stripping condensate at the outlet of the second heat exchanger 24, by setting the bypass pipeline 181, without a booster pump, relying on the self-pressure of the stripping condensate, the stripping condensate can be sent to the downstream device 25 through the bypass pipeline 181, thereby saving the energy consumption of the recovery system.
[0043] Please refer to Figure 1 As shown, in an embodiment of the present utility model, at least one valve is, for example, provided on the bypass pipeline 181 to control the flow of the stripping condensate in the bypass pipeline 181. Among them, the valve is, for example, a butterfly valve, a ball valve, a gate valve, or a diaphragm valve, etc.
[0044] Please refer to Figure 1 As shown, in an embodiment of the present utility model, the pressurization pipeline 182 is arranged in parallel with the bypass pipeline 181 between the second heat exchanger 24 and the downstream device 25. Among them, the pressurization pipeline 182 is, for example, at least one. When there are multiple pressurization pipelines 182, after the multiple pressurization pipelines 182 are connected in parallel, they are then arranged in parallel with the bypass pipeline 181 between the second heat exchanger 24 and the downstream device 25. In this embodiment, the pressurization pipeline 182 is, for example, two. The two pressurization pipelines 182, for example, include a first pressurization pipeline 1821 and a second pressurization pipeline 1822. After the first pressurization pipeline 1821 and the second pressurization pipeline 1822 are arranged in parallel, they are then arranged in parallel with the bypass pipeline 181 between the second heat exchanger 24 and the downstream device 25, and a booster pump is provided on each of the two pressurization pipelines 182, that is, a first booster pump 19 is provided on the first pressurization pipeline 1821, and a second booster pump 20 is provided on the second pressurization pipeline 1822. Specifically, when the pressure of the downstream device 25 is higher than the pressure of the stripping condensate at the outlet of the second heat exchanger 24, by setting the pressurization pipeline 182, the stripping condensate at the outlet of the second heat exchanger 24 is pressurized and then smoothly sent to the downstream device 25.
[0045] Please refer toFigure 1 As shown, in an embodiment of the present utility model, a reflux pipeline 21 is further provided at the outlet of the booster pump. The inlet of the reflux pipeline 21 is connected to the outlet of the booster pump, and the outlet of the reflux pipeline 21 is connected to the stripping column 14. In this embodiment, the reflux pipeline 21 includes, for example, a first reflux pipeline 211 and a second reflux pipeline 212. The first reflux pipeline 211 is connected to the outlet of the first booster pump 19 and the stripping column 14, and the second reflux pipeline 212 is connected to the outlet of the second booster pump 20 and the stripping column 14. The first reflux pipeline 211 and the second reflux pipeline 212 are arranged in parallel. By providing the reflux pipeline 21, on the one hand, the reflux pipeline 21 can serve as the minimum reflux line to protect the booster pump, and on the other hand, it can make the materials in the stripping column 14 flow, avoiding the stagnation of materials in the stripping column 14.
[0046] Please refer to Figure 1 As shown, in an embodiment of the present utility model, the downstream device 25 is used to receive and reuse the stripped condensate output from the stripped condensate external pipeline 18. Among them, the downstream device 25 is, for example, at least one. When there are multiple downstream devices 25, after the multiple downstream devices 25 are arranged in parallel, they are connected to the stripped condensate external pipeline 18. In this embodiment, the downstream device 25 is, for example, two. The two downstream devices 25 include, for example, a first device 251 and a second device 252, etc. Taking the first device 251 as a circulating water device and the second device 252 as a gasification device as an example, the recovery system will be described. Specifically, the pressure of the first device 251 is normal pressure, and the pressure of the second device 252 is higher than the pressure of the stripped condensate at the outlet of the second heat exchanger 24. When only the first device 251 needs the stripped condensate, through the bypass pipeline 181, relying on the self-pressure of the stripped condensate at the outlet of the second heat exchanger 24, the stripped condensate can be sent to the first device 251, thus avoiding starting the booster pump in the booster pipeline 182, which can not only save energy consumption, but also avoid the problem of pipeline shaking in the recovery system caused by the start of the booster pump, improving the operation stability of the recovery system. When the second device 252 needs the stripped condensate, through the booster pipeline 182, the stripped condensate at the outlet of the second heat exchanger 24 is pressurized and then smoothly sent to the second device 252, and the second device 252 reuses the stripped condensate.
[0047] Please refer to Figure 1 As shown, in an embodiment of the present utility model, between the stripped condensate output pipeline 16, the stripped condensate heat exchange pipeline 17, the first booster pipeline 1821, the second booster pipeline 1822, the first reflux pipeline 211, the second reflux pipeline 212, and the parallel main path of the booster pipeline 182 and the bypass pipeline 181 and the downstream device 25, at least one valve is provided respectively to control the flow of materials in the pipeline. Among them, the valve is, for example, a butterfly valve, a ball valve, a gate valve or a diaphragm valve, etc.
[0048] Please refer toFigure 1 As shown, in an embodiment of the present utility model, an output pipeline 26 is provided between the downstream device 25 and the stripping condensate external delivery pipeline 18. Specifically, after the bypass pipeline 181 and the boosting pipeline 182 are connected in parallel, they are connected to the inlet of the output pipeline 26, and the outlet of the output pipeline 26 is connected to the downstream device 25 to send the stripping condensate in the stripping condensate external delivery pipeline 18 to the downstream device 25. Among them, at least one valve is provided on the output pipeline 26, for example, to control the flow of materials in the output pipeline 26, and the valve is, for example, a butterfly valve, a ball valve, a gate valve or a diaphragm valve, etc.
[0049] Please refer to Figure 1 As shown, in an embodiment of the present utility model, a branch pipeline 27 is further provided between the downstream device 25 and the stripping condensate external delivery pipeline 18, and the branch pipeline 27 is arranged in parallel with the output pipeline 26. By providing the branch pipeline 27 as a bypass of the output pipeline 26, when the valve in the output pipeline 26 fails and the output pipeline 26 cannot transport the stripping condensate, the branch pipeline 27 can replace the output pipeline 26 to send the stripping condensate in the stripping condensate external delivery pipeline 18 to the downstream device 25. Among them, at least one valve is provided on the branch pipeline 27, for example, to control the flow of materials in the branch pipeline 27, and the valve is, for example, a butterfly valve, a ball valve, a gate valve or a diaphragm valve, etc.
[0050] In summary, the present utility model provides a recovery system for process condensate, which strips the process condensate through a stripping column to obtain stripping condensate and sends the stripping condensate to a downstream device for recycling and reuse of the stripping condensate. Moreover, the recovery system provided by the present utility model selects a bypass pipeline or a boosting pipeline according to the pressure of the downstream device to transport the stripping condensate to the downstream device, thereby being able to save energy consumption, and also being able to avoid the pipelines in the recovery system from shaking and improve the operation stability of the recovery system.
[0051] Throughout the specification, references to "one embodiment", "an embodiment", or "a specific embodiment" mean that a particular feature, structure, or characteristic described in connection with the embodiment is included in at least one embodiment of the present invention, and not necessarily in all embodiments. Thus, the appearances of the phrases "in one embodiment", "in an embodiment", or "in a specific embodiment" in various places throughout the specification are not necessarily referring to the same embodiment. In addition, the particular features, structures, or characteristics of any specific embodiment of the present invention may be combined with one or more other embodiments in any suitable manner. It should be understood that other variations and modifications of the embodiments of the invention described and shown herein may be made in accordance with the teachings herein and will be considered part of the spirit and scope of the present invention.
[0052] The above description is only a preferred embodiment of the present application and an explanation of the applied technical principles. Those skilled in the art should understand that the scope of the utility model involved in the present application is not limited to the technical solution formed by the specific combination of the above technical features. It should also cover other technical solutions formed by any combination of the above technical features or their equivalent features without departing from the inventive concept, such as the technical solution formed by mutually replacing the above features with the (but not limited to) technical features with similar functions disclosed in the present application. Except for the technical features described in the specification, the remaining technical features are known to those skilled in the art. To highlight the innovative features of the present invention, the remaining technical features are not described herein again.
Claims
1. A recovery system for process condensate, characterized in that, At least including: Process condensate input pipeline; The first heat exchanger, connected to the process condensate input pipeline; Heated condensate output pipeline, connected to the process condensate input pipeline through the first heat exchanger; Stripping column, connected to one end of the heated condensate output pipeline away from the first heat exchanger; Stripped condensate output pipeline, connecting the stripping column and the first heat exchanger; Stripped condensate heat exchange pipeline, connected to the stripped condensate output pipeline through the first heat exchanger; Stripped condensate external delivery pipeline, connected to the stripped condensate heat exchange pipeline, and the stripped condensate external delivery pipeline includes a pressurization pipeline and a bypass pipeline arranged in parallel; The second heat exchanger, connecting the stripped condensate heat exchange pipeline and the stripped condensate external delivery pipeline; And At least one downstream device, connected to the stripped condensate external delivery pipeline.
2. The recovery system according to claim 1, wherein There is at least one pressurization pipeline. When there are multiple pressurization pipelines, after the multiple pressurization pipelines are arranged in parallel, they are connected in parallel to the bypass pipeline and then to the second heat exchanger.
3. The recovery system according to claim 2, characterized in that, A booster pump is provided on the pressurization pipeline. When there are multiple pressurization pipelines, booster pumps are respectively provided on the multiple pressurization pipelines.
4. The recovery system according to claim 3, wherein The recovery system further includes a reflux pipeline, which connects the outlet of the booster pump and the stripping column.
5. The recovery system according to claim 1, wherein At least one valve is provided on the bypass pipeline.
6. The recovery system according to claim 1, wherein When there are multiple downstream devices, after the multiple downstream devices are arranged in parallel, they are connected to the stripped condensate external delivery pipeline.
7. The recovery system according to claim 1, characterized in that, The recovery system further includes a cold medium input pipeline, which is connected to the second heat exchanger.
8. The recovery system according to claim 7, wherein The recovery system further includes a cold medium output pipeline, which is connected to the cold medium input pipeline through the second heat exchanger.
9. The recovery system according to claim 1, wherein A steam input pipeline is provided on the stripping column, and the steam input pipeline is connected to the stripping column.
10. The recovery system according to claim 1, wherein The recovery system further includes an output pipeline and a branch pipeline, and the output pipeline and the branch pipeline are arranged in parallel between the stripped condensate external delivery pipeline and the downstream device.