CN110454760B - Fermentation tank empty waste heat recovery device and process - Google Patents
Fermentation tank empty waste heat recovery device and process Download PDFInfo
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- CN110454760B CN110454760B CN201910717302.3A CN201910717302A CN110454760B CN 110454760 B CN110454760 B CN 110454760B CN 201910717302 A CN201910717302 A CN 201910717302A CN 110454760 B CN110454760 B CN 110454760B
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- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
- A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
- A61L2/02—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor using physical phenomena
- A61L2/04—Heat
- A61L2/06—Hot gas
- A61L2/07—Steam
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- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
- A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
- A61L2/24—Apparatus using programmed or automatic operation
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- A—HUMAN NECESSITIES
- A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
- A61L—METHODS OR APPARATUS FOR STERILISING MATERIALS OR OBJECTS IN GENERAL; DISINFECTION, STERILISATION OR DEODORISATION OF AIR; CHEMICAL ASPECTS OF BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES; MATERIALS FOR BANDAGES, DRESSINGS, ABSORBENT PADS OR SURGICAL ARTICLES
- A61L2/00—Methods or apparatus for disinfecting or sterilising materials or objects other than foodstuffs or contact lenses; Accessories therefor
- A61L2/26—Accessories or devices or components used for biocidal treatment
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B37/00—Component parts or details of steam boilers
- F22B37/02—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
- F22B37/26—Steam-separating arrangements
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D11/00—Feed-water supply not provided for in other main groups
- F22D11/02—Arrangements of feed-water pumps
- F22D11/06—Arrangements of feed-water pumps for returning condensate to boiler
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Abstract
本发明属于余热回收利用技术领域，具体的涉及一种发酵罐空消余热回收装置及工艺。包括余热回收器，余热回收器的上部通过二次蒸汽出管与蒸汽压缩器相连，蒸汽压缩器通过管路与分离器相连，分离器通过管路与再利用蒸汽管道相连；余热回收器的下部管程进口与空消蒸汽进管相连；余热回收器的管程出口通过尾气连接管与尾气预热器的壳程相连，尾气预热器的壳程通过管路与尾气冷却器的壳程相连接，尾气冷却器上部设置排空口。本发明所述的发酵罐空消余热回收装置及工艺，通过对热能进行再利用，回收效率高、使用方便、节能效果好，可实现自动化控制，是一种可有效降低能源消耗的发酵罐空消余热回收装置。
The invention belongs to the technical field of waste heat recovery and utilization, and specifically relates to a fermentation tank empty waste heat recovery device and process. It includes a waste heat recovery device, the upper part of the waste heat recovery device is connected to the steam compressor through the secondary steam outlet pipe, the steam compressor is connected to the separator through the pipeline, and the separator is connected to the reuse steam pipeline through the pipeline; the lower part of the waste heat recovery device The tube side inlet is connected to the air elimination steam inlet pipe; the tube side outlet of the waste heat recovery device is connected to the shell side of the exhaust gas preheater through the exhaust gas connecting pipe, and the shell side of the exhaust gas preheater is connected to the shell side of the exhaust gas cooler through the pipeline. Connection, a drain port is provided on the upper part of the exhaust gas cooler. The fermentation tank empty waste heat recovery device and process of the present invention, by reusing heat energy, have high recovery efficiency, easy use, good energy saving effect, can realize automatic control, and are a fermentation tank emptying system that can effectively reduce energy consumption. Waste heat recovery device.
Description
Technical Field
The invention belongs to the technical field of waste heat recovery and utilization, and particularly relates to a device and a process for recovering waste heat from empty fermentation tank.
Background
Waste heat recycling refers to recycling waste heat generated in an industrial process. Mainly comprises high-temperature waste gas waste heat, waste steam waste water waste heat, cooling medium waste heat and the like.
The emptying of the fermentation tank is a method for sterilizing the whole tank body by introducing steam into the fermentation tank and simultaneously opening exhaust valves arranged on various inlet and outlet pipelines and exhausting waste heat steam. The equipment can be emptied, the utilization rate of the equipment can be improved, and continuous operation can be realized. Along with the progress of production technology, the fermentation tank gradually develops to a large-scale direction, and a large amount of consumed steam is consumed for empty consumption, and if the steam is not recycled, a large amount of energy is wasted.
Chinese patent CN204064033U discloses a device for recycling waste gas from empty fermentation tank. The gas exhausted by the empty fermentation tank is uniformly discharged into a specific pipeline and then discharged into a flexible water pipe through a recovery pipeline, so that waste gas generated by the empty fermentation tank is dissolved in water, and heat in the waste gas is used for a continuous sterilization process. The heat in the waste steam in the empty and elimination process of the fermentation tank is stored by heating water, so that the waste heat is recycled, the energy consumption is greatly reduced, and the waste steam is prevented from being discharged into the atmosphere to pollute the environment. However, the method separates out organic matters and sterilized mycelium in the waste gas without empty, which can cause pollution of heating water to affect the use.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a device and a process for recovering waste heat from empty fermentation tank. The device and the process recycle the heat energy, have the characteristics of high recovery efficiency, convenient use, good energy-saving effect and automatic control, and can recycle the heat energy by the waste heat recovery device through the energy discharged by the empty fermentation tank.
The invention relates to an empty waste heat recovery device of a fermentation tank, which comprises a waste heat recovery device, wherein the upper part of the waste heat recovery device is connected with a steam compressor through a secondary steam outlet pipe, the steam compressor is connected with a separator through a pipeline, and the separator is connected with a reuse steam pipeline through a pipeline; the inlet of the lower tube side of the waste heat recoverer is connected with an empty steam-eliminating inlet tube; the tube side outlet of the waste heat recoverer is connected with the shell side of the tail gas preheater through a tail gas connecting tube, the shell side of the tail gas preheater is connected with the shell side of the tail gas cooler through a pipeline, and the upper part of the tail gas cooler is provided with an emptying port.
Wherein:
the condensate outlet of the waste heat recoverer is connected with the condensate heat exchanger inlet through a condensate output pipe, condensate in the condensate heat exchanger exchanges heat with water in the water supplementing tank, the condensate heat exchanger outlet is connected with the condensate tank inlet through a pipeline, and the outlet at the lower part of the condensate tank is connected with the wastewater tank through a condensate outer drain pipe.
The lower part of the waste heat recoverer is connected with the inlet of a main circulating pump through a circulating inlet pipe, the outlet of the main circulating pump is connected with a circulating outlet pipe, and the circulating outlet pipe is connected with a middle ejector of the waste heat recoverer.
The upper part of the tail gas cooler is connected with a water supplementing pipeline, the outlet of the tail gas cooler is connected with the inlet of the condensate heat exchanger through a water supplementing inlet pipe, the condensate heat exchanger is connected with a water supplementing tank through a pipeline, the lower part of the water supplementing tank is connected with the inlet of the water supplementing pump through a pipeline, the outlet of the water supplementing pump is of a three-way structure, one path of the water supplementing pump is connected with the tube side inlet of the tail gas preheater through a pipeline, the water supplementing pump flows back into the water supplementing tank through a preheating circulating pipe after the heat exchange of the tail gas preheater and the tail gas, the other path of the water supplementing pump is connected with a circulating inlet pipe through another path of the water supplementing pipe, and a water supplementing valve is arranged on the water supplementing pipe.
The outlet of the lower part of the tail gas preheater is connected with the inlet of the condensate tank through a tail gas condensate discharge pipe.
A one-way valve is arranged on a pipeline connected with the separator and the reuse steam pipeline; the separator is connected with the waste heat recoverer through a liquid return pipe.
A control valve is arranged on the air-extinction steam inlet pipe.
The secondary steam generated by the waste heat recoverer is heated and boosted to a preset working condition through the steam compressor, and is reused.
The waste heat recoverer is connected with the tail gas preheater and the tail gas cooler in series, namely, a tail gas outlet of the waste heat recoverer is connected with an inlet of the tail gas preheater through a tail gas connecting pipe, and an inlet of the tail gas cooler is connected with an outlet of the tail gas preheater through a pipeline.
The tail gas preheater is connected with the water supplementing tank in series through a pipeline to recycle the waste heat of the tail gas, namely, the tail gas preheater is connected with the water supplementing tank through a preheating circulating pipe and circulates through the water supplementing pump.
The condensate outlet of the waste heat recoverer is connected with the condensate heat exchanger in series through a pipeline to recover the waste heat of the condensate.
The device adopts an automatic valve, a sensor is arranged on the equipment, and the device is connected to a controller for automatic control and can be remotely monitored.
The invention relates to a fermentation tank empty waste heat recovery process, which comprises the following steps:
(1) Waste steam at 105-125 ℃ after empty and elimination of the fermentation tank enters a tube side of the waste heat recoverer through a pipeline;
(2) The empty waste gas is circulated in a plurality of processes in a tube side of the waste heat recoverer, and fully exchanges heat with water in a shell side, the condensate at 102-112 ℃ obtained after heat exchange enters a condensate heat exchanger through a pipeline, and the obtained tail gas at 102-112 ℃ sequentially enters a tail gas preheater and a tail gas cooler through pipelines;
(3) The water in the waste heat recoverer is heated to 100 ℃ of bubble point and vaporized, secondary steam at 100 ℃ is generated, the temperature is raised and boosted by a vapor compressor, the temperature is raised to 40-45 ℃, and the vapor after the temperature is raised and boosted is discharged out of the system by a separator for reuse;
(4) The condensate of the waste heat recoverer enters a condensate heat exchanger through a pipeline to exchange heat with materials in a water supplementing tank at 102-112 ℃, and enters a condensate tank through a pipeline after the condensate is fully cooled to 35-40 ℃;
(5) The tail gas at 102-112 ℃ enters a tail gas preheater through a pipeline to exchange heat with materials in a water supplementing tank, then enters a tail gas cooler to be fully cooled to 30-35 ℃, then non-condensable gas is emptied, and condensate liquid at 35-40 ℃ enters a condensate tank through a pipeline and is discharged;
(6) The normal-temperature water at 25 ℃ sequentially enters a tail gas cooler and a condensate preheater through pipelines to be fully preheated and then enters a water supplementing tank;
(7) The water in the water supplementing tank is connected in series with the tail gas preheater through a water supplementing pump and a preheating circulating pipe and is continuously circulated for heat recovery; and is connected to the circulating inlet pipe through a water supplementing pipe to supplement water for the waste heat recoverer.
The working process of the fermentation tank empty waste heat recovery process in the waste heat recovery device is as follows:
waste steam at 105-125 ℃ after empty and elimination of the fermentation tank enters a waste heat steam pipe of the fermentation tank, enters an empty and elimination steam inlet pipe through the waste heat steam pipe of the fermentation tank, and enters a pipe side of the waste heat recoverer through the empty and elimination steam inlet pipe; the empty waste gas is circulated in a plurality of processes in a tube side of the waste heat recoverer, and fully exchanges heat with water in the shell side, the tail gas with the temperature of 102-112 ℃ obtained after heat exchange enters the shell side of the tail gas preheater through a tail gas connecting tube, exchanges heat with water in a water supplementing tank in the tail gas preheater, enters the tail gas cooler after heat exchange is finished, fully exchanges heat with water (25 ℃) in a water supplementing pipeline, and is then emptied; the condensate at 102-112 ℃ obtained after heat exchange in the waste heat recoverer enters the condensate heat exchanger through a condensate output pipe.
The water in the waste heat recoverer is heated by waste steam to 100 ℃ at bubble point and is vaporized, secondary steam at 100 ℃ is generated and enters the steam compressor through a secondary steam outlet pipe to be heated and boosted, the temperature rise is 40-45 ℃, the steam after the temperature rise and the pressure boost is discharged out of the system through a separator for reuse, and a one-way valve is arranged on a pipeline; the liquid phase separated by the separator returns to the waste heat recoverer through a liquid return pipe.
The lower water of the waste heat recoverer enters a main circulating pump through a circulating inlet pipe, and the main circulating pump is conveyed to an ejector at the middle part of the waste heat recoverer through a circulating outlet pipe to absorb heat and evaporate.
The condensate of 102-112 ℃ of the shell pass of the waste heat recoverer enters the condensate heat exchanger through a condensate output pipe to exchange heat with water in the water supplementing tank, and the condensate is fully cooled to 35-40 ℃ and then enters the condensate tank through a pipeline.
The tail gas at 102-112 ℃ enters the tail gas preheater through a tail gas connecting pipe to exchange heat with water in the water supplementing tank, after the heat exchange is finished, the tail gas enters the tail gas cooler again to be fully cooled to 30-35 ℃, the non-condensable gas is emptied, the condensate at 35-40 ℃ of the tail gas preheater enters the condensate tank through a tail gas condensate discharge pipe, and the lower part of the condensate tank is connected with a condensate discharge pipe to control the discharge treatment.
The water replenishing outside the system enters the tail gas cooler through a water replenishing pipeline, water (normal-temperature water at 25 ℃) in the water replenishing pipeline enters the condensate preheater through a water replenishing inlet pipe after being preheated through tail gas, and enters the water replenishing tank through a pipeline after being preheated again through condensate; the lower part of the water supplementing tank is connected with a water supplementing pump through a pipeline, the outlet of the water supplementing pump is of a three-way structure, water in the water supplementing tank enters the tail gas preheater through the outlet of the water supplementing pump, and after heat exchange with the tail gas, the water flows back into the water supplementing tank through the preheating circulation pipe; and the heat recovery is carried out by continuous circulation of a water supplementing pump; the outlet of the water supplementing pump is connected to the circulating inlet pipe through a water supplementing pipe to supplement water for the waste heat recoverer.
Compared with the prior art, the invention has the following beneficial effects:
according to the fermentation tank empty-elimination waste heat recovery device and process, through recycling of heat energy, the recovery efficiency is high, the use is convenient, the energy-saving effect is good, automatic control can be achieved, primary waste heat recovery and secondary tail gas waste heat recovery can be carried out on energy discharged by the fermentation tank empty-elimination through waste heat recovery equipment, the collected heat energy is converted into low-pressure steam, and then the low-pressure steam is heated and boosted to a preset working condition through the steam booster for recycling of the energy, so that the fermentation tank empty-elimination waste heat recovery device can effectively reduce energy consumption.
Drawings
FIG. 1 is a schematic structural diagram of a fermentation tank empty waste heat recovery device.
In the figure: 1. an exhaust gas cooler; 2. a tail gas preheater; 3. preheating a circulating pipe; 4. a tail gas connecting pipe; 5. a waste heat recoverer; 6. a secondary steam outlet pipe; 7. a vapor compressor; 8. a liquid return pipe; 9. a separator; 10. a one-way valve; 11. empty steam inlet pipe; 12. a control valve; 13. a circulation outlet pipe; 14. a main circulation pump; 15. circulating the pipe; 16. a water supplementing pipe; 17. a water supplementing valve; 18. a condensate output pipe; 19. a water supplementing tank; 20. a water supplementing pump; 21. a condensate heat exchanger; 22. a condensate tank; 23. a condensate discharge pipe; 24. a tail gas condensate discharge pipe; 25. supplementing water and feeding into the pipe.
Detailed Description
The invention is further described below with reference to examples.
Example 1
The invention relates to a fermentation tank empty waste heat recovery device, which comprises a waste heat recoverer 5, wherein the upper part of the waste heat recoverer 5 is connected with a steam compressor 7 through a secondary steam outlet pipe 6, the steam compressor 7 is connected with a separator 9 through a pipeline, the separator 9 is connected with a reuse steam pipeline through a pipeline, and a one-way valve 10 is arranged on the pipeline; the separator 9 is connected with the waste heat recoverer 5 through a liquid return pipe 8. The waste heat steam pipe discharged by the fermentation tank is connected with an empty steam inlet pipe 11, the empty steam inlet pipe 11 is connected with a tube side inlet of the waste heat recoverer 5, and a control valve 12 is arranged on a pipeline; the tube side outlet of the waste heat recoverer 5 is connected with the shell side of the tail gas preheater 2 through a tail gas connecting tube 4, the shell side of the tail gas preheater 2 is connected with the shell side of the tail gas cooler 1 through a pipeline, and an emptying port is arranged at the upper part of the tail gas cooler 1.
The condensate outlet of the waste heat recoverer 5 is connected with the inlet of a condensate heat exchanger 21 through a condensate output pipe 18, condensate in the condensate heat exchanger 21 exchanges heat with water in a water supplementing tank 19, the outlet of the condensate heat exchanger 21 is connected with the inlet of a condensate tank 22 through a pipeline, and the outlet of the lower part of the condensate tank 22 is connected with a wastewater tank through a condensate outer drain pipe 23.
The lower part of the waste heat recoverer 5 is connected with the inlet of a main circulating pump 14 through a circulating inlet pipe 15, the outlet of the main circulating pump 14 is connected with a circulating outlet pipe 13, and the circulating outlet pipe 13 is connected with a middle ejector of the waste heat recoverer 5.
The upper part of the tail gas cooler 1 is connected with a water supplementing pipeline, the outlet of the tail gas cooler 1 is connected with the inlet of the condensate heat exchanger 21 through a water supplementing inlet pipe 25, the condensate heat exchanger 21 is connected with a water supplementing tank 19 through a pipeline, the lower part of the water supplementing tank 19 is connected with the inlet of a water supplementing pump 20 through a pipeline, the outlet of the water supplementing pump 20 is of a three-way structure, one path is connected with the pipe side inlet of the tail gas preheater 2 through a pipeline, the preheating circulating pipe 3 flows back into the water supplementing tank 19 after the tail gas preheater 2 exchanges heat with the tail gas, and the other path is connected with the circulating inlet pipe 15 through a water supplementing pipe 16, and a water supplementing valve 17 is arranged on the water supplementing pipe 16.
The lower outlet of the tail gas preheater 2 is connected with the inlet of the condensate tank 22 through a tail gas condensate discharge pipe 24.
The lower outlet of the condensate tank 22 is connected with the wastewater pool through a condensate outlet pipe 23, two inlets are arranged at the upper part of the condensate tank 22, one inlet is the upper inlet of the condensate tank 22 and is connected with the outlet of the condensate heat exchanger 21 through a pipeline, the other inlet is the lower outlet of the condensate tank 22 and is connected with the lower outlet of the tail gas preheater 2 through a tail gas condensate discharge pipe 24, the upper outlet of the tail gas preheater 2 is connected with the lower inlet of the tail gas cooler 1 through a pipeline, and an emptying port is arranged at the upper part of the tail gas cooler 1.
The fermentation tank empty waste heat recovery process of the embodiment 1 comprises the following steps:
(1) Waste steam at 105 ℃ after the fermentation tank is empty enters a tube side of a waste heat recoverer through a pipeline;
(2) The empty waste gas is circulated in a plurality of processes in a tube side of the waste heat recoverer, and fully exchanges heat with water in a shell side, 102 ℃ condensate obtained after heat exchange enters a condensate heat exchanger through a pipeline, and the obtained 102 ℃ tail gas sequentially enters a tail gas preheater and a tail gas cooler through pipelines;
(3) The water in the waste heat recoverer is heated to 100 ℃ of bubble point and vaporized, secondary steam at 100 ℃ is generated, the temperature and the pressure are raised through a steam compressor, the temperature rise is 40 ℃, and the steam after the temperature and the pressure rise is discharged out of the system through a separator for reuse;
(4) The condensate of the waste heat recoverer enters a condensate heat exchanger through a pipeline to exchange heat with materials in the water supplementing tank, and the condensate is fully cooled to 35 ℃ and then enters the condensate tank through the pipeline;
(5) The tail gas at 102 ℃ enters a tail gas preheater through a pipeline to exchange heat with materials in a water supplementing tank, then enters a tail gas cooler to be fully cooled to 30 ℃, then non-condensable gas is emptied, and condensate liquid enters a condensate tank through a pipeline at 35 ℃ and is discharged;
(6) The normal-temperature water at 25 ℃ sequentially enters a tail gas cooler and a condensate preheater through pipelines to be fully preheated and then enters a water supplementing tank;
(7) The water in the water supplementing tank is connected in series with the tail gas preheater through a water supplementing pump and a preheating circulating pipe and is continuously circulated for heat recovery; and is connected to the circulating inlet pipe through a water supplementing pipe to supplement water for the waste heat recoverer.
The working process of the fermentation tank empty waste heat recovery process in the waste heat recovery device described in this embodiment 1 is as follows:
waste steam at 105 ℃ enters a waste heat steam pipe of the fermentation tank after the fermentation tank is empty and eliminated, enters an empty and eliminated steam inlet pipe 11 through the waste heat steam pipe of the fermentation tank, a control valve 12 is arranged on the empty and eliminated steam inlet pipe 11, and enters the pipe side of the waste heat recoverer 5 through the empty and eliminated steam inlet pipe 11; the empty waste gas circulates in a plurality of processes in the tube side of the waste heat recoverer 5, and fully exchanges heat with water in the shell side, the tail gas at 102 ℃ obtained after heat exchange enters the shell side of the tail gas preheater 2 through the tail gas connecting tube 4, the water in the water supplementing tank in the tail gas preheater exchanges heat, and the tail gas enters the tail gas cooler 1 after heat exchange is fully exchanged with water (25 ℃) in the water supplementing pipeline and then is emptied; the condensate at 102 ℃ obtained after heat exchange in the waste heat recoverer enters the condensate heat exchanger 21 through the condensate output pipe 18.
The water in the waste heat recoverer 5 is heated by waste steam to 100 ℃ at bubble point and is vaporized, secondary steam at 100 ℃ is generated and enters the steam compressor 7 through the secondary steam outlet pipe 6 to be heated and boosted, the temperature rise is 40 ℃, the steam after the temperature rise and the boosting is discharged out of the system through the separator 9 to be reused, and the pipeline is provided with the one-way valve 10; the liquid phase separated by the separator 9 is returned to the waste heat recoverer 5 through the liquid return pipe 8.
The water at the lower part of the waste heat recoverer 5 enters a main circulating pump 14 through a circulating inlet pipe 15, and is conveyed to an ejector at the middle part of the waste heat recoverer 5 through a circulating outlet pipe 13 to absorb heat and evaporate.
The condensate of 102 ℃ of the shell side of the waste heat recoverer 5 enters the condensate heat exchanger 21 through the condensate output pipe 18 to exchange heat with water in the water supplementing tank 19, and the condensate is fully cooled to 35 ℃ and then enters the condensate tank 22 through a pipeline.
The tail gas at 102 ℃ enters the tail gas preheater 2 through the tail gas connecting pipe 4 to exchange heat with water in the water supplementing tank 19, after the heat exchange is finished, the tail gas enters the tail gas cooler 1 again to be fully cooled to 30 ℃, then the non-condensable gas is emptied, the condensate at 35 ℃ of the tail gas preheater 2 enters the condensate tank 22 through the tail gas condensate discharge pipe 24, and the lower part of the condensate tank 22 is connected with the condensate discharge pipe 23 to control the discharge treatment.
The water replenishing outside the system enters the tail gas cooler 1 through a water replenishing pipeline, water (normal-temperature water at 25 ℃) in the water replenishing pipeline enters the condensate preheater 21 through a water replenishing inlet pipe 25 after being preheated by tail gas, and enters the water replenishing tank 19 through a pipeline after being preheated again by condensate; the lower part of the water supplementing tank 19 is connected with a water supplementing pump 20 through a pipeline, the outlet of the water supplementing pump 20 is of a three-way structure, water in the water supplementing tank 19 enters the tail gas preheater 2 through the outlet of the water supplementing pump 20, exchanges heat with the tail gas and then flows back into the water supplementing tank 19 through the preheating circulation pipe 3; and the heat recovery is continuously and circularly carried out by the water supplementing pump 20; the outlet of the water supplementing pump 20 is connected to the circulating inlet pipe 15 through the water supplementing pipe 16 to supplement water for the waste heat recoverer.
Example 2
The fermenter empty heat removal waste heat recovery apparatus described in example 2 is the same as that of example 1.
The fermentation tank empty waste heat recovery process of the embodiment 2 comprises the following steps:
(1) Waste steam at 115 ℃ after the empty fermentation tank is eliminated enters a tube side of a waste heat recoverer through a pipeline;
(2) The empty waste gas is circulated in a plurality of processes in a tube side of the waste heat recoverer, and fully exchanges heat with water in a shell side, the condensate at 106 ℃ obtained after heat exchange enters a condensate heat exchanger through a pipeline, and the obtained tail gas at 106 ℃ sequentially enters a tail gas preheater and a tail gas cooler through pipelines;
(3) The water in the waste heat recoverer is heated to 100 ℃ of bubble point and vaporized, secondary steam at 100 ℃ is generated, the temperature and the pressure are raised through a steam compressor, the temperature rise is 43 ℃, and the steam after the temperature and the pressure rise is discharged out of the system through a separator for reuse;
(4) The condensate of the waste heat recoverer enters a condensate heat exchanger through a pipeline to exchange heat with materials in the water supplementing tank, and the condensate is fully cooled to 37 ℃ and then enters the condensate tank through the pipeline;
(5) The tail gas at 106 ℃ enters a tail gas preheater through a pipeline to exchange heat with materials in a water supplementing tank, then enters a tail gas cooler to be fully cooled to 33 ℃, then non-condensable gas is emptied, and condensate liquid enters a condensate tank through a pipeline at 37 ℃ and is discharged;
(6) The normal-temperature water at 25 ℃ sequentially enters a tail gas cooler and a condensate preheater through pipelines to be fully preheated and then enters a water supplementing tank;
(7) The water in the water supplementing tank is connected in series with the tail gas preheater through a water supplementing pump and a preheating circulating pipe and is continuously circulated for heat recovery; and is connected to the circulating inlet pipe through a water supplementing pipe to supplement water for the waste heat recoverer.
The working process of the fermentation tank empty waste heat recovery process in the waste heat recovery device described in this embodiment 2 is as follows:
waste steam at 115 ℃ enters a waste heat steam pipe of the fermentation tank after the fermentation tank is empty and eliminated, enters an empty and eliminated steam inlet pipe 11 through the waste heat steam pipe of the fermentation tank, a control valve 12 is arranged on the empty and eliminated steam inlet pipe 11, and enters the pipe side of the waste heat recoverer 5 through the empty and eliminated steam inlet pipe 11; the empty waste gas circulates in a plurality of processes in the tube side of the waste heat recoverer 5, and fully exchanges heat with water in the shell side, the tail gas at 106 ℃ obtained after heat exchange enters the shell side of the tail gas preheater 2 through the tail gas connecting tube 4, the water in the water supplementing tank in the tail gas preheater exchanges heat, and the tail gas enters the tail gas cooler 1 after heat exchange is fully exchanged with the water (25 ℃) in the water supplementing pipeline and then is emptied; the condensate at 106 ℃ obtained after heat exchange in the waste heat recoverer enters the condensate heat exchanger 21 through the condensate output pipe 18.
The water in the waste heat recoverer 5 is heated by waste steam to 100 ℃ at bubble point and is vaporized, secondary steam at 100 ℃ is generated and enters the steam compressor 7 through the secondary steam outlet pipe 6 to be heated and boosted, the temperature rise is 43 ℃, the steam after the temperature rise and the boosting is discharged out of the system through the separator 9 to be reused, and the pipeline is provided with the one-way valve 10; the liquid phase separated by the separator 9 is returned to the waste heat recoverer 5 through the liquid return pipe 8.
The water at the lower part of the waste heat recoverer 5 enters a main circulating pump 14 through a circulating inlet pipe 15, and is conveyed to an ejector at the middle part of the waste heat recoverer 5 through a circulating outlet pipe 13 to absorb heat and evaporate.
The condensate of 106 ℃ of the shell side of the waste heat recoverer 5 enters the condensate heat exchanger 21 through the condensate output pipe 18 to exchange heat with water in the water supplementing tank 19, and the condensate is fully cooled to 37 ℃ and then enters the condensate tank 22 through a pipeline.
The tail gas at 106 ℃ enters the tail gas preheater 2 through the tail gas connecting pipe 4 to exchange heat with water in the water supplementing tank 19, after the heat exchange is finished, the tail gas enters the tail gas cooler 1 again to be fully cooled to 33 ℃, the non-condensable gas is emptied, the condensate at 37 ℃ of the tail gas preheater 2 enters the condensate tank 22 through the tail gas condensate discharge pipe 24, and the lower part of the condensate tank 22 is connected with the condensate discharge pipe 23 to control the discharge treatment.
The water replenishing outside the system enters the tail gas cooler 1 through a water replenishing pipeline, water (normal-temperature water at 25 ℃) in the water replenishing pipeline enters the condensate preheater 21 through a water replenishing inlet pipe 25 after being preheated by tail gas, and enters the water replenishing tank 19 through a pipeline after being preheated again by condensate; the lower part of the water supplementing tank 19 is connected with a water supplementing pump 20 through a pipeline, the outlet of the water supplementing pump 20 is of a three-way structure, water in the water supplementing tank 19 enters the tail gas preheater 2 through the outlet of the water supplementing pump 20, exchanges heat with the tail gas and then flows back into the water supplementing tank 19 through the preheating circulation pipe 3; and the heat recovery is continuously and circularly carried out by the water supplementing pump 20; the outlet of the water supplementing pump 20 is connected to the circulating inlet pipe 15 through the water supplementing pipe 16 to supplement water for the waste heat recoverer.
Example 3
The fermenter empty heat removal waste heat recovery apparatus described in example 3 is the same as that of example 1.
The fermentation tank empty waste heat recovery process of the embodiment 1 comprises the following steps:
(1) Waste steam at 125 ℃ after the empty and elimination of the fermentation tank enters a tube side of a waste heat recoverer through a pipeline;
(2) The empty waste gas is circulated in a plurality of processes in a tube side of the waste heat recoverer, and fully exchanges heat with water in a shell side, 112 ℃ condensate obtained after heat exchange enters a condensate heat exchanger through a pipeline, and the obtained 112 ℃ tail gas sequentially enters a tail gas preheater and a tail gas cooler through pipelines;
(3) The water in the waste heat recoverer is heated to 100 ℃ of bubble point and vaporized, secondary steam at 100 ℃ is generated, the temperature and the pressure are raised through a steam compressor, the temperature is raised to 45 ℃, and the steam after the temperature and the pressure are raised is discharged out of the system through a separator for reuse;
(4) The condensate of the waste heat recoverer enters a condensate heat exchanger through a pipeline to exchange heat with materials in a water supplementing tank, and the condensate is fully cooled to 40 ℃ and then enters the condensate tank through the pipeline;
(5) The tail gas at 112 ℃ enters a tail gas preheater through a pipeline to exchange heat with materials in a water supplementing tank, then enters a tail gas cooler to be fully cooled to 35 ℃, then non-condensable gas is emptied, and condensate liquid enters a condensate tank through a pipeline at 40 ℃ and is discharged;
(6) The normal-temperature water at 25 ℃ sequentially enters a tail gas cooler and a condensate preheater through pipelines to be fully preheated and then enters a water supplementing tank;
(7) The water in the water supplementing tank is connected in series with the tail gas preheater through a water supplementing pump and a preheating circulating pipe and is continuously circulated for heat recovery; and is connected to the circulating inlet pipe through a water supplementing pipe to supplement water for the waste heat recoverer.
The working process of the fermentation tank empty waste heat recovery process in the waste heat recovery device described in this embodiment 3 is as follows:
waste steam at 125 ℃ enters a waste heat steam pipe of the fermentation tank after the fermentation tank is empty and eliminated, and enters an empty and eliminated steam inlet pipe 11 through the waste heat steam pipe of the fermentation tank, a control valve 12 is arranged on the empty and eliminated steam inlet pipe 11, and enters the pipe side of the waste heat recoverer 5 through the empty and eliminated steam inlet pipe 11; the empty waste gas circulates in a plurality of processes in the tube side of the waste heat recoverer 5, and fully exchanges heat with water in the shell side, the 112 ℃ tail gas obtained after heat exchange enters the shell side of the tail gas preheater 2 through the tail gas connecting tube 4, the water in the water supplementing tank in the tail gas preheater exchanges heat, and the tail gas enters the tail gas cooler 1 after heat exchange is fully exchanged with water (25 ℃) in the water supplementing tube and then is emptied; the condensate at 112 ℃ obtained after heat exchange in the waste heat recoverer enters the condensate heat exchanger 21 through the condensate output pipe 18.
The water in the waste heat recoverer 5 is heated by waste steam to 100 ℃ at bubble point and is vaporized, secondary steam at 100 ℃ is generated and enters the steam compressor 7 through the secondary steam outlet pipe 6 to be heated and boosted, the temperature rise is 45 ℃, the steam after the temperature rise and the boosting is discharged out of the system through the separator 9 to be reused, and the pipeline is provided with the one-way valve 10; the liquid phase separated by the separator 9 is returned to the waste heat recoverer 5 through the liquid return pipe 8.
The water at the lower part of the waste heat recoverer 5 enters a main circulating pump 14 through a circulating inlet pipe 15, and is conveyed to an ejector at the middle part of the waste heat recoverer 5 through a circulating outlet pipe 13 to absorb heat and evaporate.
The condensate of 112 ℃ on the shell side of the waste heat recoverer 5 enters a condensate heat exchanger 21 through a condensate output pipe 18 to exchange heat with water in a water supplementing tank 19, and the condensate is fully cooled to 40 ℃ and then enters a condensate tank 22 through a pipeline.
The tail gas at 112 ℃ enters the tail gas preheater 2 through the tail gas connecting pipe 4 to exchange heat with water in the water supplementing tank 19, after the heat exchange is finished, the tail gas enters the tail gas cooler 1 again to be fully cooled to 35 ℃, the non-condensable gas is emptied, the condensate at 40 ℃ of the tail gas preheater 2 enters the condensate tank 22 through the tail gas condensate discharge pipe 24, and the lower part of the condensate tank 22 is connected with the condensate discharge pipe 23 to control the discharge treatment.
The water replenishing outside the system enters the tail gas cooler 1 through a water replenishing pipeline, water (normal-temperature water at 25 ℃) in the water replenishing pipeline enters the condensate preheater 21 through a water replenishing inlet pipe 25 after being preheated by tail gas, and enters the water replenishing tank 19 through a pipeline after being preheated again by condensate; the lower part of the water supplementing tank 19 is connected with a water supplementing pump 20 through a pipeline, the outlet of the water supplementing pump 20 is of a three-way structure, water in the water supplementing tank 19 enters the tail gas preheater 2 through the outlet of the water supplementing pump 20, exchanges heat with the tail gas and then flows back into the water supplementing tank 19 through the preheating circulation pipe 3; and the heat recovery is continuously and circularly carried out by the water supplementing pump 20; the outlet of the water supplementing pump 20 is connected to the circulating inlet pipe 15 through the water supplementing pipe 16 to supplement water for the waste heat recoverer.
The above embodiments only describe the main characteristic points and implementation methods of the present invention. It will be appreciated by those skilled in the art that the present invention is not limited to the above-described embodiments. The invention is capable of modification in various other respects, all without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (5)
1. The utility model provides a fermentation cylinder empty waste heat recovery device that disappears which characterized in that: the device comprises a waste heat recoverer (5), wherein the upper part of the waste heat recoverer (5) is connected with a steam compressor (7) through a secondary steam outlet pipe (6), the steam compressor (7) is connected with a separator (9) through a pipeline, and the separator (9) is connected with a recycling steam pipeline through a pipeline; the inlet of the lower tube side of the waste heat recoverer (5) is connected with an empty steam inlet tube (11); the tube side outlet of the waste heat recoverer (5) is connected with the shell side of the tail gas preheater (2) through a tail gas connecting tube (4), the shell side of the tail gas preheater (2) is connected with the shell side of the tail gas cooler (1) through a pipeline, and an emptying port is arranged at the upper part of the tail gas cooler (1);
the condensate outlet of the waste heat recoverer (5) is connected with the inlet of a condensate heat exchanger (21) through a condensate output pipe (18), condensate in the condensate heat exchanger (21) exchanges heat with water in a water supplementing tank (19), the outlet of the condensate heat exchanger (21) is connected with the inlet of a condensate tank (22) through a pipeline, and the outlet at the lower part of the condensate tank (22) is connected with a wastewater tank through a condensate drain pipe (23);
the lower part of the waste heat recoverer (5) is connected with the inlet of a main circulating pump (14) through a circulating inlet pipe (15), the outlet of the main circulating pump (14) is connected with a circulating outlet pipe (13), and the circulating outlet pipe (13) is connected with a middle ejector of the waste heat recoverer (5);
the upper portion of the tail gas cooler (1) is connected with a water supplementing pipeline, the outlet of the tail gas cooler (1) is connected with the inlet of the condensate heat exchanger (21) through a water supplementing inlet pipe (25), the condensate heat exchanger (21) is connected with the water supplementing tank (19) through a pipeline, the lower portion of the water supplementing tank (19) is connected with the inlet of the water supplementing pump (20) through a pipeline, the outlet of the water supplementing pump (20) is of a three-way structure, one path is connected with the pipe side inlet of the tail gas preheater (2) through a pipeline, after the tail gas preheater (2) exchanges heat with the tail gas, the tail gas flows back into the water supplementing tank (19) through the preheating circulating pipe (3), and the other path is connected with the circulating inlet pipe (15) through the water supplementing pipe (16), and the water supplementing valve (17) is arranged on the water supplementing pipe (16).
2. The fermenter empty waste heat recovery device according to claim 1, wherein: the outlet of the lower part of the tail gas preheater (2) is connected with the inlet of a condensate tank (22) through a tail gas condensate discharge pipe (24).
3. The fermenter empty waste heat recovery device according to claim 1, wherein: a one-way valve (10) is arranged on a pipeline connected with the separator (9) and the reuse steam pipeline; the separator (9) is connected with the waste heat recoverer (5) through a liquid return pipe (8).
4. The fermenter empty waste heat recovery device according to claim 1, wherein: a control valve (12) is arranged on the air-extinction steam inlet pipe (11).
5. A fermenter empty waste heat recovery process according to claim 1, wherein: the method comprises the following steps:
(1) Waste steam at 105-125 ℃ after empty and elimination of the fermentation tank enters a tube side of the waste heat recoverer through a pipeline;
(2) The empty waste gas is circulated in a plurality of processes in a tube side of the waste heat recoverer, and fully exchanges heat with water in a shell side, the condensate at 102-112 ℃ obtained after heat exchange enters a condensate heat exchanger through a pipeline, and the obtained tail gas at 102-112 ℃ sequentially enters a tail gas preheater and a tail gas cooler through pipelines;
(3) The water in the waste heat recoverer is heated to 100 ℃ of bubble point and vaporized, secondary steam at 100 ℃ is generated, the temperature is raised and boosted by a steam compressor, the temperature is raised to 40-45 ℃, and the steam after the temperature is raised and boosted is discharged out of the system by a separator for reuse;
(4) The condensate of the waste heat recoverer enters a condensate heat exchanger through a pipeline to exchange heat with materials in a water supplementing tank at 102-112 ℃, and enters a condensate tank through a pipeline after the condensate is fully cooled to 35-40 ℃;
(5) The tail gas at 102-112 ℃ enters a tail gas preheater through a pipeline to exchange heat with materials in a water supplementing tank, then enters a tail gas cooler to be fully cooled to 30-35 ℃, then non-condensable gas is emptied, and condensate liquid at 35-40 ℃ enters a condensate tank through a pipeline and is discharged;
(6) The normal-temperature water at 25 ℃ sequentially enters a tail gas cooler and a condensate preheater through pipelines to be fully preheated and then enters a water supplementing tank;
(7) The water in the water supplementing tank is connected in series with the tail gas preheater through a water supplementing pump and a preheating circulating pipe and is continuously circulated for heat recovery; and is connected to the circulating inlet pipe through a water supplementing pipe to supplement water for the waste heat recoverer.
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| CN111795503B (en) * | 2020-07-14 | 2022-05-17 | 高燕妮 | Heat energy shunting and recovering device for large-scale bathing place |
| CN113623627B (en) * | 2021-09-14 | 2023-02-07 | 西安热工研究院有限公司 | Steam generation device and method adapting to load change |
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