CN213207823U - Multistage flash distillation of high temperature high pressure condensate is retrieved well, low pressure superheated steam system - Google Patents
Multistage flash distillation of high temperature high pressure condensate is retrieved well, low pressure superheated steam system Download PDFInfo
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- CN213207823U CN213207823U CN202020927250.0U CN202020927250U CN213207823U CN 213207823 U CN213207823 U CN 213207823U CN 202020927250 U CN202020927250 U CN 202020927250U CN 213207823 U CN213207823 U CN 213207823U
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Abstract
The utility model relates to a multistage flash distillation of high temperature high pressure lime set is retrieved in, the superheated steam system of low pressure, the preferred second grade flash distillation system of this multistage (second grade, tertiary) flash distillation system can be used to the high temperature high pressure lime set of heat energy utilization technical field to retrieve and rich product in, the superheated steam of low pressure, belong to energy-conserving technical field. The utility model provides a multistage flash distillation of high temperature high pressure condensate is retrieved production well, low pressure superheated steam system which characterized in that includes second grade flash distillation device, one-level water separator, second grade water separator, one-level steam superheater, second grade steam superheater, condensate pump and condensate heat exchanger. The utility model discloses can be used to retrieve the waste heat of the high temperature high pressure lime set of steam power plant and richly produce overheated medium and low pressure steam.
Description
Technical Field
The utility model relates to a multistage flash distillation of high temperature high pressure lime set is retrieved in, low pressure superheated steam system can be used to heat utilization technical field's high temperature high pressure lime set retrieve with rich product in, low pressure superheated steam, belong to energy-conserving technical field.
Background
The production of the polyester industry needs to consume a large amount of heat energy, the polyester process usually uses heat conduction oil to provide the heat energy, the heat energy of the heat conduction oil can be obtained through heat exchange between a large-scale steam heat exchanger and steam, high-pressure steam and the heat conduction oil are converted into high-temperature high-pressure condensate after heat exchange, and the high-temperature high-pressure condensate contains huge heat energy. A large amount of high-temperature and high-pressure condensate cannot directly enter a steam-water circulation system of the thermal power plant, and how to return the part of high-temperature and high-pressure condensate to the steam-water circulation system of the thermal power plant becomes a key for judging whether the steam heating heat-conducting oil process can normally run. Meanwhile, the heat and the quality of the high-temperature and high-pressure condensate are recovered, and the method has great significance for improving the energy utilization efficiency, saving the fuel and reducing the treatment cost of desalted water.
At present, the scheme among utility model CN 210069822U utilizes the middling pressure condensate after the one-level flash distillation to heat the secondary steam in order to obtain overheated low pressure steam, and the weak point of this method is that can not be at any time according to the production change adjustment technology of owner in order to satisfy the operating mode requirement, can not produce overheated middling pressure steam simultaneously.
Disclosure of Invention
An object of the utility model is to provide a middle and low pressure superheated steam system is retrieved to multistage flash distillation of high temperature high pressure lime set can be used to retrieve the waste heat of the high temperature high pressure lime set of steam power plant and rich production, middle and low pressure steam.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a high-temperature high-pressure condensate multistage flash evaporation recovery production medium-pressure and low-pressure superheated steam system is characterized by comprising a primary flash evaporation device, a secondary flash evaporation device, a primary steam-water separation device, a secondary steam-water separation device, a primary steam superheater, a secondary steam superheater, a condensate pump and a condensate heat exchanger;
the working condition I is as follows: the high-temperature high-pressure condensate firstly enters a primary steam superheater for heat exchange as a heat source, then enters a primary flash evaporation device to generate secondary steam, and then enters a primary steam-water separation device through a pressure regulating control valve (the primary steam-water separation device is required to be put into use when the steam superheat degree requirement is high, and the primary steam-water separation device is optionally not required when the steam superheat degree requirement is low), the secondary steam is divided into two paths after entrained water mist is removed, one path of secondary steam is subjected to heat exchange through the primary steam superheater to generate superheated medium-pressure steam to supply a medium-pressure steam main pipe, the other path of secondary steam is subjected to heat exchange through the pressure regulating control valve to enter a secondary. After high-temperature high-pressure condensate enters a primary flash device, medium-pressure condensate is generated and used as a heat source to exchange heat through a secondary steam superheater, secondary steam which is fed into a secondary flash device to generate enters a secondary steam-water separation device through a pressure regulating control valve (the secondary steam-water separation device is required to be used when the steam superheat degree requirement is high, and the secondary steam-water separation device is not required when the steam superheat degree requirement is low), saturated secondary steam with entrained water mist is removed, and the saturated secondary steam is subjected to heat exchange through the secondary steam superheater after passing through the pressure regulating control valve to generate superheated low-pressure steam to be supplied to a low-pressure steam. The low-pressure condensate generated after the medium-pressure condensate enters the secondary flash evaporation device can be directly subjected to heat exchange through the condensate heat exchanger by utilizing potential energy according to actual requirements, the condensate temperature is reduced to be supercooled water, and the supercooled water is sent to a deaerator or is pressurized by a condensate pump and sent to the deaerator;
working conditions are as follows: high-temperature high-pressure condensate firstly serves as a heat source to enter a primary steam superheater for heat exchange, then secondary steam generated by a primary flash device enters a primary steam-water separation device through a pressure regulating control valve (the primary steam-water separation device is required to be put into use when the steam superheat degree requirement is high, and the primary steam-water separation device is not required when the steam superheat degree requirement is low), and the secondary steam is subjected to heat exchange through a primary steam heater after entrained water mist is removed to generate superheated medium-pressure steam to be supplied to a medium-pressure steam main pipe; according to actual requirements, the high-temperature and high-pressure condensate can be directly subjected to heat exchange through a condensate heat exchanger by using potential energy, then the condensate temperature is reduced to be subcooled water, and the subcooled water is sent to a deaerator or is pressurized by using a condensate pump;
working conditions are as follows: the high-temperature high-pressure condensate enters a primary flash evaporation device to generate secondary steam, the secondary steam enters a primary steam-water separation device through a pressure regulating control valve (the primary steam-water separation device is required to be used when the steam superheat degree requirement is high, and the primary steam-water separation device can be selected not to be used when the steam superheat degree requirement is low), and the secondary steam after water mist is removed is subjected to heat exchange through a secondary steam superheater to generate superheated low-pressure steam to supply a low-pressure steam main pipe. After entering a primary flash evaporation device, high-temperature and high-pressure condensate generates medium-pressure condensate as a heat source and exchanges heat with a secondary steam superheater, then secondary steam as feed enters a secondary flash evaporation device and enters a secondary steam-water separation device through a pressure regulating control valve (the secondary steam-water separation device is required when the steam superheat degree requirement is high, and the secondary steam-water separation device is not required when the steam superheat degree requirement is low), and saturated secondary steam with water mist removed passes through the pressure regulating control valve and then exchanges heat with the secondary steam superheater to generate superheated low-pressure steam to be supplied to a low-pressure steam main pipe; the low-pressure condensate generated after the medium-pressure condensate enters the secondary flash evaporation device can be directly subjected to heat exchange through the condensate heat exchanger by utilizing potential energy according to actual requirements, the condensate temperature is reduced to be supercooled water, and the supercooled water is sent to a deaerator or is pressurized by a condensate pump and sent to the deaerator;
preferably, the multi-stage (two-stage, three-stage) flash system, preferably a two-stage flash system.
Preferably, when the primary steam superheater is put into use, medium-pressure steam and superheated low-pressure steam are produced by means of simultaneous superheating, and the yield of the two kinds of steam can be adjusted according to actual requirements; and only low-pressure superheated steam is produced when the primary steam superheater is switched out of the system.
Preferably, only the superheated medium-pressure steam is produced when the secondary steam superheater, the secondary steam-water separation device and the secondary flash device are switched out of the system.
Preferably, the top of the first-stage flash evaporation device is provided with a wire mesh defoaming part, the first-stage steam-water separation device is required to be used when the steam superheat degree requirement is high, and the first-stage steam-water separation device can be selected not to be used when the steam superheat degree requirement is low.
Preferably, the top of the secondary flash evaporation device is provided with a wire mesh defoaming part, the secondary steam-water separation device is required to be used when the steam superheat degree requirement is high, and the secondary steam-water separation device can be selected not to be used when the steam superheat degree requirement is low.
Preferably, the secondary steam superheater is a shell-and-tube heat exchanger, medium-pressure condensate flows from the primary side, and secondary steam flows from the secondary side.
Preferably, the medium-pressure condensate at the bottom of the primary flash evaporation device is divided into two paths, one path of the medium-pressure condensate is connected to the secondary steam superheater as a heat source, and the other path of the medium-pressure condensate after heat exchange with the secondary steam superheater is converged and then is connected to the secondary flash evaporation device as a feed for flash evaporation to produce secondary steam.
Preferably, the low-pressure condensate discharged from the bottom of the secondary flash evaporation device can be directly conveyed to the deaerator through heat exchange of the condensate heat exchanger or pressurization of the condensate pump by using potential energy according to actual requirements.
Preferably, the primary flash tank and the secondary flash tank can be horizontal or vertical, and the type of flash tank is selected according to actual working conditions.
Preferably, the primary steam superheater and the secondary steam superheater can adopt floating head heat exchangers and U-shaped tube plate heat exchangers, and which structural type heat exchanger is selected according to actual working conditions.
Preferably, the superheated medium-pressure steam on the secondary side of the primary steam superheater is merged into a medium-pressure steam supply pipe network, an electric isolation valve and an external steam exhaust pipeline are arranged in front of the medium-pressure steam supply pipe network, and when the superheated medium-pressure steam pressure does not reach the pipe network pressure, the steam is exhausted outwards.
Preferably, the first-stage flash evaporation device is provided with a safety valve and a liquid level meter, the high-temperature and high-pressure condensate is connected to the side wall of the first-stage flash evaporation device after heat exchange, the secondary steam is connected out from the top, and the medium-pressure condensate is connected out from the bottom.
Preferably, a pressure regulating control valve is arranged on a secondary steam pipeline connected to the top of the primary flash evaporation device, and the opening of the valve is regulated according to the pressure in the primary flash evaporation device, so that the primary flash evaporation device maintains stable set pressure.
Preferably, the secondary flash evaporation device is provided with a safety valve and a liquid level meter, medium-pressure condensate is used as a heat source and is connected to the side wall of the secondary flash evaporation device after heat exchange through the secondary steam superheater, generated secondary steam is connected out from the top, and low-pressure condensate is connected out from the bottom.
Preferably, a pressure regulating control valve is arranged on a secondary steam pipeline connected to the top of the secondary flash evaporation device, and the opening of the valve is regulated according to the pressure in the secondary flash evaporation device, so that the secondary flash evaporation device maintains stable set pressure.
Preferably, the primary steam-water separation device is provided with a safety valve and a liquid level meter, secondary steam is connected from the side wall of the primary steam-water separation device and is discharged from the top, and drainage water is discharged from the bottom. When the requirement of the steam superheat degree is high, a first-stage steam-water separation device is required to be used, and when the requirement of the steam superheat degree is low, the first-stage steam-water separation device can be selected not to be used.
Preferably, a pressure regulating control valve is arranged on a saturated secondary steam pipeline connected to the top of the primary steam-water separation device, so that the steam pressure after pressure reduction meets the use requirements of low-pressure steam users in a park.
Preferably, the secondary steam-water separation device is provided with a safety valve and a liquid level meter, secondary steam is connected from the side wall of the secondary steam-water separation device and is connected out from the top, and drainage water is connected out from the bottom. When the requirement of the steam superheat degree is high, a secondary steam-water separation device is required to be used, and when the requirement of the steam superheat degree is low, the secondary steam-water separation device can be selected not to be used.
Preferably, the secondary side superheated low-pressure steam of the secondary steam heater is merged into a low-pressure steam supply pipe network, and a check valve is arranged on the superheated low-pressure steam pipeline.
Preferably, the superheated low-pressure steam at the secondary side of the secondary steam heater is merged into a low-pressure steam supply pipe network, an electric isolating valve and an outward steam exhaust pipeline are arranged in front of the low-pressure steam supply pipe network, and when the superheated low-pressure steam pressure does not reach the pipe network pressure, the steam is exhausted outwards.
Preferably, the medium-pressure condensate discharged from the bottom of the primary flash evaporation device is divided into two paths, one path is used as a heat source and connected to the primary steam heater, and the other path is combined with the medium-pressure condensate subjected to heat exchange with the secondary steam superheater and then connected to the secondary flash evaporation device as a feed for flash evaporation to produce secondary steam.
Preferably, the heat exchange control valve on the medium-pressure condensate pipeline controls the opening of the valve according to the temperature of the superheated low-pressure steam, and the medium-pressure condensate flow to the secondary steam heater is adjusted.
Preferably, the medium-pressure condensate control valve controls the valve opening according to the liquid level of the primary flash device to adjust the medium-pressure condensate flow directly going to the secondary steam superheater and the secondary flash device.
A high-temperature high-pressure condensate multistage flash evaporation system for recovering medium-pressure and low-pressure superheated steam is characterized by comprising a primary steam-water separation device, a primary flash evaporation device, a condensate pump and a condensate heat exchanger; the output end of the high-temperature high-pressure condensate pipe is communicated with the input port of the first-stage flash evaporation device, a secondary steam outlet of the first-stage flash evaporation device enters the input port of the first-stage steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the first-stage steam-water separation device is respectively communicated with the input ends of a ninth pipeline and an eleventh pipeline through a second pipeline, and the output end of the eleventh pipeline is connected with a deaerator; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; a first output port of the primary steam-water separation device is communicated with a medium-pressure steam pipe network; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; and a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline.
According to above-mentioned technical scheme, a high temperature high pressure condensate multistage flash distillation is retrieved well, low pressure superheated steam system still includes second grade steam superheater, second grade steam-water separation device, second grade flash distillation plant { promptly: a secondary steam superheater, a secondary steam-water separation device and a secondary flash device are connected in series between the primary steam-water separation device and the primary flash device and between the condensate pump and the condensate heat exchanger; i.e., the contents of example 3 }; the output end of the high-temperature high-pressure condensate pipe is communicated with the input port of the primary flash device, a secondary steam outlet of the primary flash device enters the input port of the primary steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the primary steam-water separation device is respectively communicated with the input ends of a fourth pipeline and a sixth pipeline through a second pipeline, the output end of the fourth pipeline is communicated with a first medium input port of the secondary steam superheater, and a first medium output port of the secondary steam superheater is communicated with the sixth pipeline through a fifth pipeline; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; a second medium input port of the secondary steam superheater is communicated with a first output port of the primary steam-water separation device through a seventeenth pipeline, and a second medium output port of the secondary steam superheater is communicated with a low-pressure steam pipe network through a nineteenth pipeline; the output end of the sixth pipeline is communicated with the input port of the secondary flash evaporation device, a secondary steam outlet of the secondary flash evaporation device is communicated with the input port of the secondary steam-water separation device through a twenty-first pipeline, and a condensate outlet of the secondary flash evaporation device is communicated with the third pipeline through an eighth pipeline; a first output port of the secondary steam-water separation device is communicated with a second medium input port of the secondary steam superheater through a twentieth pipeline, a second output port of the secondary steam-water separation device is respectively communicated with input ends of a ninth pipeline and an eleventh pipeline through a seventh pipeline, and an output end of the eleventh pipeline is connected with a deaerator; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; and a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline.
According to the technical scheme, the system for recovering the medium-pressure superheated steam and the low-pressure superheated steam by the multistage flash evaporation of the high-temperature high-pressure condensate further comprises a first-stage steam superheater (namely the content of the embodiment 2); the output end of the high-temperature high-pressure condensate pipe is respectively communicated with the input ends of a fourteenth pipeline and a first pipeline, the output end of the fourteenth pipeline is communicated with a first medium input port of a first-stage steam superheater, a first medium output port of the first-stage steam superheater is communicated with the first pipeline through a thirteenth pipeline, the output end of the first pipeline is communicated with an input port of a first-stage flash evaporation device, a second medium input port of the first-stage steam superheater is communicated with a first output port of the first-stage steam-water separation device through a fifteenth pipeline, and a second medium output port of the first-stage steam superheater is communicated with a medium-pressure steam pipe network through a sixteenth pipeline; a secondary steam outlet of the first-stage flash evaporation device enters an input port of the first-stage steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the first-stage steam-water separation device is respectively communicated with input ends of a ninth pipeline and an eleventh pipeline through a second pipeline, and an output end of the eleventh pipeline is connected with a deaerator; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; and a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline.
According to the technical scheme, the system for recovering the medium-pressure superheated steam and the low-pressure superheated steam by the multistage flash evaporation of the high-temperature high-pressure condensate further comprises a primary steam superheater, a secondary steam-water separation device and a secondary flash evaporation device (namely the content of the embodiment 1); the output end of the high-temperature high-pressure condensate pipe is respectively communicated with the input ends of a fourteenth pipeline and a first pipeline, the output end of the fourteenth pipeline is communicated with a first medium input port of a first-stage steam superheater, a first medium output port of the first-stage steam superheater is communicated with the first pipeline through a thirteenth pipeline, the output end of the first pipeline is communicated with an input port of a first-stage flash evaporation device, a second medium input port of the first-stage steam superheater is communicated with a first output port of the first-stage steam-water separation device through a fifteenth pipeline, and a second medium output port of the first-stage steam superheater is communicated with a medium-pressure steam pipe network through a sixteenth pipeline; a secondary steam outlet of the primary flash evaporation device enters an input port of the primary steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the primary steam-water separation device is respectively communicated with input ends of a fourth pipeline and a sixth pipeline through a second pipeline, an output end of the fourth pipeline is communicated with a first medium input port of the secondary steam superheater, and a first medium output port of the secondary steam superheater is communicated with the sixth pipeline through a fifth pipeline; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; a second medium input port of the secondary steam superheater is communicated with a first output port of the primary steam-water separation device through a seventeenth pipeline, and a second medium output port of the secondary steam superheater is communicated with a low-pressure steam pipe network through a nineteenth pipeline; the output end of the sixth pipeline is communicated with the input port of the secondary flash evaporation device, a secondary steam outlet of the secondary flash evaporation device is communicated with the input port of the secondary steam-water separation device through a twenty-first pipeline, and a condensate outlet of the secondary flash evaporation device is communicated with the third pipeline through an eighth pipeline; a first output port of the secondary steam-water separation device is communicated with a second medium input port of the secondary steam superheater through a twentieth pipeline, a second output port of the secondary steam-water separation device is respectively communicated with input ends of a ninth pipeline and an eleventh pipeline through a seventh pipeline, and an output end of the eleventh pipeline is connected with a deaerator; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; and a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline.
According to the technical scheme, the eighteenth pipeline is communicated with the fifteenth pipeline through a twenty-sixth pipeline, and a valve is arranged on the twenty-sixth pipeline.
According to the technical scheme, the twenty-first pipeline is communicated with the twentieth pipeline through a twenty-seventh pipeline, and a valve is arranged on the twenty-seventh pipe.
The utility model has the advantages that: the method can be used for recovering the waste heat of high-temperature and high-pressure condensate of the thermal power plant and producing superheated medium-pressure steam and superheated low-pressure steam.
The utility model discloses utilize the flash distillation to retrieve high temperature high pressure lime set, rich product accords with the user's demand and is applicable to the overheated middling pressure steam and the overheated low-pressure steam of long-range transportation, has reduced the temperature and the pressure that the lime set was retrieved to the steam power plant, makes it satisfy the requirement of intaking of other workshop sections, can directly recycle, has fully retrieved the heat and the quality of high temperature high pressure lime set. During actual operation of the system, the flow rate of the generated superheated medium-pressure steam and the yield of the superheated low-pressure steam can be adjusted through operation according to actual needs.
Drawings
Fig. 1 is the structure schematic diagram of the middle and low pressure superheated steam in the production of the high temperature and high pressure condensate multistage flash distillation recovery system.
Fig. 2 is the utility model discloses a multistage flash distillation of high temperature high pressure condensate is retrieved, low pressure superheated steam system production middling pressure superheated steam's schematic structure drawing.
Fig. 3 is the utility model discloses a multistage flash distillation of high temperature high pressure condensate is retrieved, low pressure superheated steam system produces the schematic structure drawing of low pressure superheated steam.
Description of reference numerals: 1 is a first-stage steam superheater, 2 is a first-stage steam-water separation device, 3 is a first-stage flash evaporation device, 4 is a second-stage steam superheater, 5 is a second-stage steam-water separation device, 6 is a second-stage flash evaporation device, 7 is a condensate pump, 8 is a condensate heat exchanger, 9-a high-temperature high-pressure condensate pipe, 10-a valve, 11-a first pipeline, 12-a second pipeline, 13-a third pipeline, 14-a fourth pipeline, 15-a fifth pipeline, 16-a sixth pipeline, 17-a seventh pipeline, 18-an eighth pipeline, 19-a ninth pipeline, 20-a tenth pipeline, 21-an eleventh pipeline, 22-a twelfth pipeline, 23-a thirteenth pipeline, 24-a fourteenth pipeline, 25-a fifteenth pipeline, 26-a sixteenth pipeline, 27-a seventeenth pipeline, 28-an eighteenth pipeline, 29-nineteenth, 30-twentieth, 31-twenty-first, 32-twenty-second, 33-twenty-third, 34-twenty-fourth, 35-twenty-fifth.
Detailed Description
In order to make the present invention more comprehensible, preferred embodiments are described in detail below with reference to the accompanying drawings.
The utility model relates to a high-temperature high-pressure condensate multistage flash recovery medium and low-pressure superheated steam system, which comprises a primary flash device 3, a secondary flash device 6, a primary steam-water separation device 2, a secondary steam-water separation device 5, a primary steam superheater 1, a secondary steam superheater 4, a condensate pump 7 and a condensate heat exchanger 8;
the working condition I is as follows: as shown in fig. 1, high-temperature and high-pressure condensate firstly enters a primary steam superheater 1 as a heat source for heat exchange, then enters a primary flash evaporation device 3 to generate secondary steam, and then enters a primary steam-water separation device 2 through a pressure regulating control valve (the primary steam-water separation device is required to be used when the steam superheat degree requirement is high, and the primary steam-water separation device is not required when the steam superheat degree requirement is low), the secondary steam is divided into two paths after entrained water mist is removed, one path of secondary steam is subjected to heat exchange through the primary steam superheater 1 to generate superheated medium-pressure steam to supply a medium-pressure steam main pipe, the other path of secondary steam is subjected to heat exchange through the pressure regulating control valve to enter a secondary steam superheater. After high-temperature high-pressure condensate enters the primary flash device 3, medium-pressure condensate is generated and used as a heat source to exchange heat through the secondary steam superheater 4, secondary steam which is used as feed and enters the secondary flash device 6 enters the secondary steam-water separation device 5 through the pressure regulating control valve (the secondary steam-water separation device is required when the steam superheat degree requirement is high, and the secondary steam-water separation device is not required when the steam superheat degree requirement is low), and the entrained water mist saturated secondary steam is removed, passes through the pressure regulating control valve and then is subjected to heat exchange through the secondary steam superheater 4 to generate superheated low-pressure steam to be supplied to the low-pressure steam main pipe. The low-pressure condensate generated after the medium-pressure condensate enters the secondary flash evaporation device can be directly subjected to heat exchange through a condensate heat exchanger 8 by utilizing potential energy according to actual requirements, the condensate temperature is reduced to be subcooled water, and the subcooled water is sent to a deaerator or is pressurized and sent to the deaerator by a condensate pump 7;
working conditions are as follows: as shown in fig. 2, after entering a primary steam superheater for heat exchange 1 as a heat source, the high-temperature and high-pressure condensate enters a primary steam separator 2 through a pressure regulating control valve (the primary steam separator is required to be used when the steam superheat degree requirement is high, and the primary steam separator is not required when the steam superheat degree requirement is low), and after entrained water mist is removed, the secondary steam is subjected to heat exchange through the primary steam heater 1 to generate superheated medium-pressure steam to be supplied to a medium-pressure steam main pipe. The medium-pressure condensate generated after the high-temperature and high-pressure condensate enters the primary flash evaporation device 3 can be directly subjected to heat exchange through the condensate heat exchanger 8 by utilizing potential energy according to actual requirements, the condensate temperature is reduced to be subcooled water, and the subcooled water is sent to a deaerator or is pressurized by the condensate pump 7 and sent to the deaerator;
working conditions are as follows: as shown in fig. 3, the secondary steam generated by the high-temperature and high-pressure condensate entering the primary flash evaporation device 3 enters the primary steam-water separation device 2 through the pressure regulating control valve (the primary steam-water separation device is required to be used when the steam superheat degree requirement is high, and the primary steam-water separation device is not required when the steam superheat degree requirement is low), and the secondary steam after entrained water mist is removed is subjected to heat exchange through the secondary steam superheater 4 to generate superheated low-pressure steam to be supplied to the low-pressure steam main pipe. After high-temperature high-pressure condensate enters the primary flash device 3, medium-pressure condensate is generated and used as a heat source to exchange heat through the secondary steam superheater 4, secondary steam which is used as feed and enters the secondary flash device 6 enters the secondary steam-water separation device 5 through the pressure regulating control valve (the secondary steam-water separation device is required when the steam superheat degree requirement is high, and the secondary steam-water separation device is not required when the steam superheat degree requirement is low), and the entrained water mist saturated secondary steam is removed, passes through the pressure regulating control valve and then is subjected to heat exchange through the secondary steam superheater 4 to generate superheated low-pressure steam to be supplied to the low-pressure steam main pipe. The low-pressure condensate generated after the medium-pressure condensate enters the secondary flash evaporation device 6 can be directly subjected to heat exchange through the condensate heat exchanger 8 by utilizing potential energy according to actual requirements, the condensate temperature is reduced to be subcooled water, and the subcooled water is sent to a deaerator or is pressurized by the condensate pump 7 and sent to the deaerator.
Example 1:
as shown in fig. 1, a high-temperature high-pressure condensate multistage flash evaporation system for recovering medium-pressure and low-pressure superheated steam comprises a primary steam superheater 1, a primary steam-water separation device 2, a primary flash evaporation device 3, a secondary steam superheater 4, a secondary steam-water separation device 5, a secondary flash evaporation device 6, a condensate pump 7 and a condensate heat exchanger 8; the output ends of the high-temperature and high-pressure condensate pipes 9 are respectively connected with a fourteenth pipeline 24, the input end of the first pipeline 11 is communicated (can be communicated by a three-way pipe or a three-way valve; high-temperature high-pressure condensate enters from a high-temperature high-pressure condensate pipe 9. the system of the utility model has the advantages that the output end of the fourteenth pipeline 24 is communicated with the first medium input port of the first-stage steam superheater 1, the first medium output port of the first-stage steam superheater 1 is communicated with the first pipeline 11 (can be communicated by a three-way pipe or a three-way valve) by a thirteenth pipeline 23, the output end of the first pipeline 11 is communicated with the input port of the first-stage flash evaporation device 3, the second medium input port of the first-stage steam superheater 1 is communicated with the first output port of the first-stage steam-water separation device 2 by a fifteenth pipeline 25, and the second medium output port;
a secondary steam outlet of the primary flash device 3 enters an input port of the primary steam-water separation device 2 through a pressure regulating control valve and an eighteenth pipeline 28, a second output port of the primary steam-water separation device 2 is respectively communicated with input ends of a fourth pipeline 14 and a sixth pipeline 16 through a second pipeline 12, an output end of the fourth pipeline 14 is communicated with a first medium input port of the secondary steam superheater 4, and a first medium output port of the secondary steam superheater 4 is communicated with the sixth pipeline 16 through a fifth pipeline 15; a medium-pressure condensate outlet of the primary flash device 3 is connected with a condensate drainage system through a third pipeline 13;
a second medium input port of the secondary steam superheater 4 is communicated with a first output port of the primary steam-water separation device 2 through a seventeenth pipeline 27, and a second medium output port of the secondary steam superheater 4 is communicated with a low-pressure steam pipe network through a nineteenth pipeline 29;
the output end of the sixth pipeline 16 is communicated with the input port of the secondary flash evaporation device 6, the secondary steam outlet of the secondary flash evaporation device 6 is communicated with the input port of the secondary steam-water separation device 5 through a twenty-first pipeline 31, and the condensate outlet of the secondary flash evaporation device 6 is communicated with the third pipeline 13 through an eighth pipeline 18; a first output port of the secondary steam-water separation device 5 is communicated with a second medium input port of the secondary steam superheater 4 through a twentieth pipeline 30, a second output port of the secondary steam-water separation device 5 is respectively communicated with input ends of a ninth pipeline 19 and an eleventh pipeline 21 through a seventh pipeline 17, and an output end of the eleventh pipeline 21 is connected with a deaerator;
the output end of the ninth pipeline 19 is respectively communicated with the input ends of a tenth pipeline 20 and a twenty-second pipeline 32, the output end of the tenth pipeline 20 is communicated with the input end of the condensate pump 7, and the output end of the condensate pump 7 is connected with a deaerator through a twelfth pipeline 22; the output end of the twenty-second pipeline 32 is communicated with the first medium input port of the condensate heat exchanger 8, and the first medium output port of the condensate heat exchanger 8 is connected with a deaerator through a twenty-fifth pipeline 35; a second medium inlet of the condensate heat exchanger 8 is communicated with a twenty-third pipeline 33 (the twenty-third pipeline is connected with heat exchange water), and a second medium outlet of the condensate heat exchanger 8 is communicated with a twenty-fourth pipeline 34.
The eighteenth pipeline 28 is communicated with the fifteenth pipeline 25 through a twenty-sixth pipeline, and a valve is arranged on the twenty-sixth pipeline.
The twenty-first pipeline 31 is communicated with the twentieth pipeline 30 through a twenty-seventh pipeline, and a valve is arranged on the twenty-seventh pipeline.
Any one of the first pipeline to the twenty-seventh pipeline can be provided with a valve.
The working process is shown in the working condition I.
Example 2:
as shown in fig. 2, a high-temperature high-pressure condensate multistage flash evaporation system for recovering medium-pressure and low-pressure superheated steam comprises a primary steam superheater 1, a primary steam-water separation device 2, a primary flash evaporation device 3, a condensate pump 7 and a condensate heat exchanger 8; the output ends of the high-temperature and high-pressure condensate pipes 9 are respectively connected with a fourteenth pipeline 24, the input end of the first pipeline 11 is communicated (can be communicated by a three-way pipe or a three-way valve; high-temperature high-pressure condensate enters from a high-temperature high-pressure condensate pipe 9. the system of the utility model has the advantages that the output end of the fourteenth pipeline 24 is communicated with the first medium input port of the first-stage steam superheater 1, the first medium output port of the first-stage steam superheater 1 is communicated with the first pipeline 11 (can be communicated by a three-way pipe or a three-way valve) by a thirteenth pipeline 23, the output end of the first pipeline 11 is communicated with the input port of the first-stage flash evaporation device 3, the second medium input port of the first-stage steam superheater 1 is communicated with the first output port of the first-stage steam-water separation device 2 by a fifteenth pipeline 25, and the second medium output port;
a secondary steam outlet of the first-stage flash evaporation device 3 enters an input port of the first-stage steam-water separation device 2 through a pressure regulating control valve and an eighteenth pipeline 28, a second output port of the first-stage steam-water separation device 2 is respectively communicated with input ends of a ninth pipeline 19 and an eleventh pipeline 21 through a second pipeline 12, and an output end of the eleventh pipeline 21 is connected with a deaerator; a medium-pressure condensate outlet of the primary flash device 3 is connected with a condensate drainage system through a third pipeline 13;
the output end of the ninth pipeline 19 is respectively communicated with the input ends of a tenth pipeline 20 and a twenty-second pipeline 32, the output end of the tenth pipeline 20 is communicated with the input end of the condensate pump 7, and the output end of the condensate pump 7 is connected with a deaerator through a twelfth pipeline 22; the output end of the twenty-second pipeline 32 is communicated with the first medium input port of the condensate heat exchanger 8, and the first medium output port of the condensate heat exchanger 8 is connected with a deaerator through a twenty-fifth pipeline 35; a second medium inlet of the condensate heat exchanger 8 is communicated with a twenty-third pipeline 33 (the twenty-third pipeline is connected with heat exchange water), and a second medium outlet of the condensate heat exchanger 8 is communicated with a twenty-fourth pipeline 34.
The eighteenth pipeline 28 is communicated with the fifteenth pipeline 25 through a twenty-sixth pipeline, and a valve is arranged on the twenty-sixth pipeline.
The working process is shown in the working condition II.
Example 3:
as shown in fig. 3, a high-temperature high-pressure condensate multistage flash evaporation system for recovering medium-pressure and low-pressure superheated steam comprises a primary steam-water separation device 2, a primary flash evaporation device 3, a secondary steam superheater 4, a secondary steam-water separation device 5, a secondary flash evaporation device 6, a condensate pump 7 and a condensate heat exchanger 8; the output end of the high-temperature high-pressure condensate pipe 9 is communicated with the input port of the primary flash device 3, a secondary steam outlet of the primary flash device 3 enters the input port of the primary steam-water separation device 2 through a pressure regulating control valve and an eighteenth pipeline 28, a second output port of the primary steam-water separation device 2 is respectively communicated with the input ends of a fourth pipeline 14 and a sixth pipeline 16 through a second pipeline 12, the output end of the fourth pipeline 14 is communicated with a first medium input port of the secondary steam superheater 4, and a first medium output port of the secondary steam superheater 4 is communicated with the sixth pipeline 16 through a fifth pipeline 15; a medium-pressure condensate outlet of the primary flash device 3 is connected with a condensate drainage system through a third pipeline 13;
a second medium input port of the secondary steam superheater 4 is communicated with a first output port of the primary steam-water separation device 2 through a seventeenth pipeline 27, and a second medium output port of the secondary steam superheater 4 is communicated with a low-pressure steam pipe network through a nineteenth pipeline 29;
the output end of the sixth pipeline 16 is communicated with the input port of the secondary flash evaporation device 6, the secondary steam outlet of the secondary flash evaporation device 6 is communicated with the input port of the secondary steam-water separation device 5 through a twenty-first pipeline 31, and the condensate outlet of the secondary flash evaporation device 6 is communicated with the third pipeline 13 through an eighth pipeline 18; a first output port of the secondary steam-water separation device 5 is communicated with a second medium input port of the secondary steam superheater 4 through a twentieth pipeline 30, a second output port of the secondary steam-water separation device 5 is respectively communicated with input ends of a ninth pipeline 19 and an eleventh pipeline 21 through a seventh pipeline 17, and an output end of the eleventh pipeline 21 is connected with a deaerator;
the output end of the ninth pipeline 19 is respectively communicated with the input ends of a tenth pipeline 20 and a twenty-second pipeline 32, the output end of the tenth pipeline 20 is communicated with the input end of the condensate pump 7, and the output end of the condensate pump 7 is connected with a deaerator through a twelfth pipeline 22; the output end of the twenty-second pipeline 32 is communicated with the first medium input port of the condensate heat exchanger 8, and the first medium output port of the condensate heat exchanger 8 is connected with a deaerator through a twenty-fifth pipeline 35; a second medium inlet of the condensate heat exchanger 8 is communicated with a twenty-third pipeline 33 (the twenty-third pipeline is connected with heat exchange water), and a second medium outlet of the condensate heat exchanger 8 is communicated with a twenty-fourth pipeline 34.
The eighteenth pipeline 28 is communicated with the fifteenth pipeline 25 through a twenty-sixth pipeline, and a valve is arranged on the twenty-sixth pipeline.
The twenty-first pipeline 31 is communicated with the twentieth pipeline 30 through a twenty-seventh pipeline, and a valve is arranged on the twenty-seventh pipeline.
The working process is shown in the working condition three.
Example 4:
a high-temperature high-pressure condensate multistage flash evaporation system for recovering medium-pressure and low-pressure superheated steam comprises a primary steam-water separation device 2, a primary flash evaporation device 3, a condensate pump 7 and a condensate heat exchanger 8; the output end of the high-temperature high-pressure condensate pipe 9 is communicated with the input port of the first-stage flash evaporation device 3, a secondary steam outlet of the first-stage flash evaporation device 3 enters the input port of the first-stage steam-water separation device 2 through a pressure regulating control valve and an eighteenth pipeline 28, a second output port of the first-stage steam-water separation device 2 is respectively communicated with the input ends of a ninth pipeline 19 and an eleventh pipeline 21 through a second pipeline 12, and the output end of the eleventh pipeline 21 is connected with a deaerator; a medium-pressure condensate outlet of the primary flash device 3 is connected with a condensate drainage system through a third pipeline 13; a first output port of the primary steam-water separation device 2 is communicated with a medium-pressure steam pipe network; the output end of the ninth pipeline 19 is respectively communicated with the input ends of a tenth pipeline 20 and a twenty-second pipeline 32, the output end of the tenth pipeline 20 is communicated with the input end of the condensate pump 7, and the output end of the condensate pump 7 is connected with a deaerator through a twelfth pipeline 22; the output end of the twenty-second pipeline 32 is communicated with the first medium input port of the condensate heat exchanger 8, and the first medium output port of the condensate heat exchanger 8 is connected with a deaerator through a twenty-fifth pipeline 35; a second medium inlet of the condensate heat exchanger 8 is communicated with a twenty-third pipeline 33, and a second medium outlet of the condensate heat exchanger 8 is communicated with a twenty-fourth pipeline 34.
Example 5:
substantially the same as in example 1 or example 3, except that: and a third-stage steam-water separation device and a third-stage flash evaporation device are connected in series between the second-stage steam-water separation device 5 and the second-stage flash evaporation device 6 and the condensate pump 7 and the condensate heat exchanger 8.
Claims (1)
1. A high-temperature high-pressure condensate multistage flash evaporation system for recovering medium-pressure and low-pressure superheated steam is characterized by comprising a primary steam-water separation device, a primary flash evaporation device, a condensate pump and a condensate heat exchanger; the output end of the high-temperature high-pressure condensate pipe is communicated with the input port of the first-stage flash evaporation device, a secondary steam outlet of the first-stage flash evaporation device enters the input port of the first-stage steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the first-stage steam-water separation device is respectively communicated with the input ends of a ninth pipeline and an eleventh pipeline through a second pipeline, and the output end of the eleventh pipeline is connected with a deaerator; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; a first output port of the primary steam-water separation device is communicated with a medium-pressure steam pipe network; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline;
also includes one of the following 3 types:
1) the system also comprises a secondary steam superheater, a secondary steam-water separation device and a secondary flash evaporation device; the output end of the high-temperature high-pressure condensate pipe is communicated with the input port of the primary flash device, a secondary steam outlet of the primary flash device enters the input port of the primary steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the primary steam-water separation device is respectively communicated with the input ends of a fourth pipeline and a sixth pipeline through a second pipeline, the output end of the fourth pipeline is communicated with a first medium input port of the secondary steam superheater, and a first medium output port of the secondary steam superheater is communicated with the sixth pipeline through a fifth pipeline; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; a second medium input port of the secondary steam superheater is communicated with a first output port of the primary steam-water separation device through a seventeenth pipeline, and a second medium output port of the secondary steam superheater is communicated with a low-pressure steam pipe network through a nineteenth pipeline; the output end of the sixth pipeline is communicated with the input port of the secondary flash evaporation device, a secondary steam outlet of the secondary flash evaporation device is communicated with the input port of the secondary steam-water separation device through a twenty-first pipeline, and a condensate outlet of the secondary flash evaporation device is communicated with the third pipeline through an eighth pipeline; a first output port of the secondary steam-water separation device is communicated with a second medium input port of the secondary steam superheater through a twentieth pipeline, a second output port of the secondary steam-water separation device is respectively communicated with input ends of a ninth pipeline and an eleventh pipeline through a seventh pipeline, and an output end of the eleventh pipeline is connected with a deaerator; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline;
2) the system also comprises a primary steam superheater; the output end of the high-temperature high-pressure condensate pipe is respectively communicated with the input ends of a fourteenth pipeline and a first pipeline, the output end of the fourteenth pipeline is communicated with a first medium input port of a first-stage steam superheater, a first medium output port of the first-stage steam superheater is communicated with the first pipeline through a thirteenth pipeline, the output end of the first pipeline is communicated with an input port of a first-stage flash evaporation device, a second medium input port of the first-stage steam superheater is communicated with a first output port of the first-stage steam-water separation device through a fifteenth pipeline, and a second medium output port of the first-stage steam superheater is communicated with a medium-pressure steam pipe network through a sixteenth pipeline; a secondary steam outlet of the first-stage flash evaporation device enters an input port of the first-stage steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the first-stage steam-water separation device is respectively communicated with input ends of a ninth pipeline and an eleventh pipeline through a second pipeline, and an output end of the eleventh pipeline is connected with a deaerator; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline;
3) the system also comprises a primary steam superheater, a secondary steam-water separation device and a secondary flash device; the output end of the high-temperature high-pressure condensate pipe is respectively communicated with the input ends of a fourteenth pipeline and a first pipeline, the output end of the fourteenth pipeline is communicated with a first medium input port of a first-stage steam superheater, a first medium output port of the first-stage steam superheater is communicated with the first pipeline through a thirteenth pipeline, the output end of the first pipeline is communicated with an input port of a first-stage flash evaporation device, a second medium input port of the first-stage steam superheater is communicated with a first output port of the first-stage steam-water separation device through a fifteenth pipeline, and a second medium output port of the first-stage steam superheater is communicated with a medium-pressure steam pipe network through a sixteenth pipeline; a secondary steam outlet of the primary flash evaporation device enters an input port of the primary steam-water separation device through a pressure regulating control valve and an eighteenth pipeline, a second output port of the primary steam-water separation device is respectively communicated with input ends of a fourth pipeline and a sixth pipeline through a second pipeline, an output end of the fourth pipeline is communicated with a first medium input port of the secondary steam superheater, and a first medium output port of the secondary steam superheater is communicated with the sixth pipeline through a fifth pipeline; a medium-pressure condensate outlet of the primary flash device is connected with a condensate drainage system through a third pipeline; a second medium input port of the secondary steam superheater is communicated with a first output port of the primary steam-water separation device through a seventeenth pipeline, and a second medium output port of the secondary steam superheater is communicated with a low-pressure steam pipe network through a nineteenth pipeline; the output end of the sixth pipeline is communicated with the input port of the secondary flash evaporation device, a secondary steam outlet of the secondary flash evaporation device is communicated with the input port of the secondary steam-water separation device through a twenty-first pipeline, and a condensate outlet of the secondary flash evaporation device is communicated with the third pipeline through an eighth pipeline; a first output port of the secondary steam-water separation device is communicated with a second medium input port of the secondary steam superheater through a twentieth pipeline, a second output port of the secondary steam-water separation device is respectively communicated with input ends of a ninth pipeline and an eleventh pipeline through a seventh pipeline, and an output end of the eleventh pipeline is connected with a deaerator; the output end of the ninth pipeline is respectively communicated with the input ends of a tenth pipeline and a twenty-second pipeline, the output end of the tenth pipeline is communicated with the input end of a condensate pump, and the output end of the condensate pump is connected with a deaerator through a twelfth pipeline; the output end of the twenty-second pipeline is communicated with the first medium input port of the condensate heat exchanger, and the first medium output port of the condensate heat exchanger is connected with the deaerator through a twenty-fifth pipeline; and a second medium input port of the condensate heat exchanger is communicated with a twenty-third pipeline, and a second medium output port of the condensate heat exchanger is communicated with a twenty-fourth pipeline.
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