CN112755566A - Flash evaporation coupling cyclone vapor-liquid separation device and waste heat recovery process thereof - Google Patents
Flash evaporation coupling cyclone vapor-liquid separation device and waste heat recovery process thereof Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/16—Evaporating by spraying
- B01D1/20—Sprayers
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
- B01D1/305—Demister (vapour-liquid separation)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
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Abstract
The system comprises an inner core pipe and an outer straight cylinder which are coaxial and vertically arranged, wherein the length of the inner core pipe is smaller than that of the outer straight cylinder, the bottom of the outer straight cylinder is connected with a cone hopper, and an annular channel is formed between the inner core pipe and the outer straight cylinder; the top of annular channel seals, and the top is equipped with the passageway pipe of slope, is equipped with the contained angle between the axis of passageway pipe and the axis of the straight barrel in outside, and is the acute angle, and the inside of passageway pipe is equipped with the atomizer, and the top of inside core pipe is linked together through pipeline and condensation heat exchanger, be equipped with the heat exchange tube in the condensation heat exchanger.
Description
Technical Field
The disclosure belongs to the field of waste heat recovery and environmental protection, and particularly relates to a flash evaporation coupling cyclone gas-liquid separation device and a waste heat recovery process thereof.
Background
The statements herein merely provide background related to the present disclosure and may not necessarily constitute prior art.
At present, a large amount of waste water or sewage with higher temperature is generated in the production processes of the coal-fired power generation industry, the printing and dyeing industry, the slaughtering industry, the ferrous metallurgy industry, the chemical industry and the like. The traditional method is that the waste water is directly discharged after simple treatment (such as sedimentation in a sedimentation tank and open-air cooling). This not only pollutes the environment, but also wastefully wastes the heat energy in the waste water with higher temperature, wastes a large amount of water resources. The method is especially unfortunately in the present day when the energy and fresh water resources are increasingly tense. In order to reduce energy consumption and production cost, a small part of production enterprises directly utilize the heat exchanger to exchange cold energy and hot energy so as to recycle waste heat of the waste sewage. Although the process has simple principle, short process flow and less investment, the process is difficult to popularize because of the defects of serious scaling and corrosion of a heat exchanger, short service life of a system, low heat recovery rate, no water resource recovery and the like.
Inspired by seawater evaporation desalination technology developed in the fifties of the twentieth century, some waste sewage waste heat utilization projects adopt a vacuum evaporation heat removal process, and the process flow is as follows: the process is that industrial waste water with certain temperature is sprayed into the middle part of an evaporation tower with certain vacuum degree through a spraying device to evaporate rapidly, liquid drops carried in steam are removed through a demister on the upper part of a spraying layer, and clean steam is converted into high-quality available heat energy through a heat pump. The process method is characterized in that under the high vacuum condition, the boiling point of the waste water is lower than the temperature of the waste water by about 15 ℃, under the working condition, the waste water is evaporated violently, liquid drops sprayed by a nozzle are rapidly formed and enlarged due to internal steam bubbles to cause explosion and cracking of the liquid drops, and accordingly tiny micron-sized fog drops are formed, and the tiny fog drops are easily taken away by water vapor with high rising speed due to large surface coefficient and small free suspension speed. Because of the waste water composition is complicated, viscidity is big, and is strong at solid surface adhesion, in case adhere to on the defroster blade, hardly removes, and operating duration is long slightly, just can agglomerate, solidification, scale deposit, and light then defroster running resistance increases, and serious can arouse the defroster to block up, leads to the unable operation of whole system.
Disclosure of Invention
The flash evaporation coupling rotational flow vapor-liquid separation device and the waste heat recovery process thereof avoid direct contact of a heat exchanger with waste water and sewage, avoid scaling and corrosion of a heat exchange surface, and simultaneously achieve the purpose of waste water and waste heat recovery.
The device comprises an inner core pipe and an outer straight cylinder which are coaxial and vertically arranged, wherein the length of the inner core pipe is smaller than that of the outer straight cylinder, the bottom of the outer straight cylinder is connected with a lower cone hopper, and an annular channel is formed between the inner core pipe and the outer straight cylinder; the top of annular channel is sealed, and the top is equipped with the rectangle passageway of downward sloping, is equipped with the contained angle between the axis of rectangle passageway and the axis of the straight barrel of outside, and is the acute angle, and the inside of passageway is equipped with sprays atomizing device.
Furthermore, the top of the inner core tube is communicated with a condensation heat exchanger through a pipeline, and a heat exchange tube is arranged in the condensation heat exchanger.
Furthermore, the top of the condensing heat exchanger is communicated with a condensed water storage tank, and the bottom of the condensing heat exchanger is communicated with the condensed water storage tank through a pipeline.
Further, the condensation heat exchange system is connected with a noncondensable gas discharge vacuum pump.
Further, the width of the rectangular channel is equal to the width of the annular channel.
Further, a rectangular channel is tangentially connected to the annular channel.
Furthermore, the spraying and atomizing device is a pipeline network consisting of a plurality of nozzles, and the direction of the spray droplets sprayed by the nozzles is parallel to the axial direction of the rectangular channel.
At least one embodiment of the present disclosure further provides a desulfurization absorption tower, which includes the above-mentioned flash evaporation coupling cyclone vapor-liquid separation device.
Furthermore, the spraying and atomizing device is connected with a slurry pool at the bottom of the desulfurization absorption tower through a pipeline, and the bottom of the lower cone body is connected with the uppermost spraying layer in the desulfurization tower through an external discharge pump.
At least one embodiment of the present disclosure further provides a waste heat recovery process based on the above flash evaporation coupling cyclone vapor-liquid separation device, and the method includes the following steps:
vacuumizing the interiors of the flash evaporation coupling cyclone vapor-liquid separation device and the condensation heat exchanger; communicating a high-temperature waste sewage pipeline with an atomizer in a vapor-liquid separation device, and evaporating the high-temperature waste sewage under a vacuum working condition to form low-temperature saturated water vapor and low-temperature saturated liquid;
the low-temperature saturated steam forms high-speed spirally descending outer rotational flow airflow under the flow guiding action of an annular channel formed by the external straight cylinder body and the internal core pipe, the outer rotational flow airflow reversely and upwards continuously performs spirally ascending inner rotational flow movement when moving downwards to the lower conical hopper on the external straight cylinder body, and flows into the condensation heat exchanger through the top of the internal core pipe to perform cold and heat exchange with a medium in the heat exchange pipe.
Further, the bottom of the condensing heat exchanger is connected with a noncondensable gas discharge vacuum pump.
The beneficial effects of this disclosure are as follows:
the flash evaporation coupling cyclone vapor-liquid separation device has the dual functions of flash evaporation and vapor-liquid separation, and avoids the defects of difficult scale cleaning of demister blades and large running resistance in the traditional flash evaporation process. Because of centrifugal force get rid of to the liquid drop of this device tower wall along the wallboard downward flow and be collected under the dead weight effect, even the scale deposit also clears up easily, more can not cause the rise of running resistance, reduces system operation energy consumption, reduces system maintenance.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure and are not to limit the disclosure.
FIG. 1 is a diagram of a system for recovering waste heat from wastewater based on a flash evaporation coupled cyclone vapor-liquid separation device according to an embodiment of the present disclosure;
FIG. 2 is a front view of a flash coupled cyclonic vapor-liquid separation device provided in an embodiment of the present disclosure;
FIG. 3 is a top view of a flash coupled cyclonic vapor-liquid separation device provided in accordance with an embodiment of the present disclosure;
FIG. 4 is a diagram of a system for recovering waste heat from wastewater with multiple flash evaporation coupled cyclone vapor-liquid separation devices connected in parallel according to an embodiment of the disclosure;
in the figure: 1. the device comprises a flash evaporation coupling rotational flow vapor-liquid separation device, a slurry spraying atomization device, a flash evaporation and vapor flow forming channel, an internal core pipe, a straight cylinder body, a conical hopper, a condensation heat exchange system, a condensation water collecting system, a non-condensable gas discharging vacuum pump system, a low-temperature waste water discharging system, a desulfurization absorption tower and a flash evaporation and vapor flow forming channel, wherein the internal core pipe is 13, the straight cylinder body is 14, the conical hopper is 15, the condensation.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs.
As shown in fig. 1, an embodiment of the present disclosure provides a slurry waste heat recovery system for a desulfurization absorption tower, which mainly includes a flash evaporation coupling cyclone vapor-liquid separation device 1, a condensation heat exchange system 2, a condensed water collection system 3, a noncondensable gas discharge vacuum pump system 4, and a low-temperature slurry discharge system 5.
The slurry pool of the desulfurization absorption tower is connected with a flash evaporation coupling cyclone vapor-liquid separation device 1 through a pipeline, the separation of slurry fog drops and steam is realized through the double centrifugal action of the outer cyclone steam flow and the inner cyclone steam flow in the device, then clean steam flowing out from the top of the device enters a condensation heat exchange system 2 for condensation, a condensed water collection system 3 is connected with the condensation heat exchange system 2, and condensed water after condensation is recycled. And the low-temperature waste slurry discharge system 5 is connected with the bottom of the flash evaporation coupling cyclone gas-liquid separation device 1, and conveys the low-temperature slurry generated by the device to the uppermost spraying mother layer of the desulfurization absorption tower 6.
Wherein flash distillation coupling whirl vapour-liquid separator 1, condensation heat transfer system 2 in this embodiment are linked together, and these two parts keep vacuum state all the time, wherein noncondensable gas is arranged vacuum pump system 4 and is connected with condensation heat transfer system 2 outward, before using this set of waste heat recovery system, closes all valves in this system in advance, keeps the enclosed state, then arranges vacuum pump system 4 through noncondensable gas and takes out the vacuum with whole waste water treatment system evacuation, just so can make the high temperature thick liquid that gets into in flash distillation coupling whirl vapour-liquid separator 1 partly evaporate in the twinkling of an eye, forms microthermal saturated steam and microthermal saturated thick liquid.
The flash evaporation coupling cyclone vapor-liquid separation device for slurry of a desulfurization absorption tower and the waste heat recovery system thereof provided in this embodiment take a vacuum working condition of-91.5 kPa as an example, wherein the slurry of 51 ℃ coming out of the desulfurization tower is partially evaporated instantaneously under the vacuum working condition of-91.5 kPa to form saturated water vapor of 45 ℃ and saturated slurry of 45 ℃.
Specifically, as shown in fig. 2, the flash evaporation coupling cyclone gas-liquid separation device 1 of the present embodiment mainly includes two coaxial and vertically disposed inner core tubes 13 and a straight cylinder 14, wherein the inner core tube 13 is a large-caliber short tube disposed at the center of the top of the straight cylinder 14, the lower end of the inner core tube is inserted into the straight cylinder 14 for a certain depth, the length of the inner core tube 13 is smaller than that of the straight cylinder 14, and the upper end of the inner core tube 13 is used as a clean steam outlet; an annular channel is formed between the inner core tube 13 and the straight cylinder body 14, and the bottom of the straight cylinder body 14 is connected with a cone hopper 15.
In this embodiment the top of the annular channel is closed and connected to a downwardly inclined flash and steam flow forming channel 12, which channel 12 is also closed, but the channel 12 is connected to the annular channel, the axis of the flash and steam flow forming channel 12 is at an acute angle to the axis of the straight barrel 14, and the channel is connected tangentially to the annular channel. The width of the channel is equal to the width of the annular channel formed between the inner core tube and the straight cylinder, it being understood that the flash evaporation and steam flow forming channel 12 is a rectangular channel in this embodiment.
Further, in the present embodiment, a slurry spray atomizer 11 is disposed inside the top of the flash evaporation and steam flow forming channel 12, and the slurry spray atomizer 11 is a pipe network with a plurality of nozzles, and the direction of mist spray from each nozzle on the pipe network is parallel to the axis of the flash evaporation and steam flow forming channel 12.
The working principle of the flash evaporation coupling cyclone vapor-liquid separation device is as follows: when the flash evaporation coupling rotational flow steam-liquid separation device reaches a set negative pressure working condition, the slurry is sprayed into a flash evaporation and steam flow forming channel 12 through the slurry spraying and atomizing device 11 to be partially evaporated instantly, part of liquid drops carried by flash evaporation steam tangentially enter the upper part of the flash evaporation coupling rotational flow steam-liquid separation device at a speed of 50-60 m/s, under the flow guide effect that the straight cylinder body 11 and the inner core pipe 13 form an annular channel, high-speed spirally descending outer rotational flow airflow is formed, when the outer rotational flow airflow moves downwards to the middle lower part of the conical hopper 15, the outer rotational flow airflow is inverted upwards to continue to perform spirally ascending inner rotational flow movement, and finally the ascending inner rotational flow airflow flows out of the tower body through the top of the inner. The vapor-liquid separation device in this embodiment operates under the working condition of high vacuum degree (-91.5kPa, approximately), the density difference between liquid drops and water vapor is large (the density of the liquid drops is 16000 times of the vapor density), and the liquid drops carried in the water vapor are almost completely removed under the centrifugal action of the high-speed rotating outer rotational flow and inner rotational flow airflow, so that the outlet of the inner core tube 13 of the flash evaporation coupling rotational flow vapor-liquid separation device is extremely clean water vapor. So far the flash distillation coupling whirl vapour-liquid separation device has just realized the quadruple function that thick liquid sprays atomizing, flash distillation steam defogging purified and concentrated cooling thick liquid is kept in.
It should be noted that the conical hopper at the bottom of the straight cylinder in this embodiment has a dual function, and this partial structure is a place where the spirally descending outer swirling steam flow is reversed to form the spirally ascending inner swirling steam flow, and is a temporary storage container for non-evaporated, concentrated and cooled slurry and liquid separated by the inner and outer swirling flows, the bottom of the conical hopper in this embodiment is also connected with the spray layer 7 at the topmost layer of the desulfurization tower through the low-temperature slurry discharge system 5, and the low-temperature slurry discharge system 5 mainly comprises a slurry discharge pump, a valve and a pipeline, and has a function of discharging the concentrated slurry collected by the conical hopper of the flash evaporation coupling swirling steam-liquid separation device to the outside of the system.
Further, the top of the inner core tube of the flash evaporation coupling cyclone vapor-liquid separation device 1 in the embodiment is communicated with the condensation heat exchange system 2 through a pipeline, clean vapor generated by the vapor-liquid separation device enters the condensation heat exchange system 2, and is subjected to waste heat recovery through a vapor-liquid heat exchange mode with the inner heat exchange tube, and the high-temperature clean vapor is condensed into clean water in the case of meeting cold to realize the purpose of waste water recovery.
Further, in the embodiment, the top of the condensation heat exchange system 2 is communicated with the top of the condensed water storage tank 3 through a pipeline, so that the pressure balance between the condensation heat exchange system 2 and the condensed water storage tank 3 is realized, meanwhile, the bottom of the condensation heat exchange system 2 is communicated with the condensed water storage tank 3 through a pipeline, so that clean steam from the vapor-liquid separation device is condensed into condensed water in the condensation heat exchange system 2, the condensed water flows into the condensed water storage tank 3 along the pipeline under the action of self weight and is stored, and the purpose of waste sewage recovery is achieved,
of course, the condensed water storage tank 3 may also be provided with a condensed water discharge delivery pump, and the condensed water in the condensed water storage tank is delivered to the required equipment or production process by the delivery pump, so as to achieve the purpose of recycling the waste water.
Preferably, in order to ensure a vacuum environment inside the flash evaporation coupling cyclone vapor-liquid separation device 1 and the condensation heat exchange system 2 in this embodiment, the condensation heat exchange system in this embodiment is further connected to a noncondensable gas discharge vacuum pump system 4, and the system discharges noncondensable gas that cannot be absorbed by the condensation heat exchange system 2 in time to maintain a negative pressure condition of the whole system, specifically, the noncondensable gas discharge vacuum pump 4 in this embodiment includes a water ring vacuum pump, a vapor-water separator, a pipeline, a valve, and the like. This noncondensable gas outer discharge vacuum pump system 4 is the key system who guarantees that the whole set of waste heat recovery system forms the design vacuum, and when the whole set of waste heat recovery system starts, at first start noncondensable gas outer discharge vacuum pump system 4 so that with all gas emissions in the whole waste heat recovery system, provide the negative pressure condition for the flash distillation, guarantee the normal operating of whole set of system.
Therefore, the embodiment of the present disclosure provides a slurry waste heat recovery system for desulfurization absorption tower, carry the thick liquid drop in detaching steam in advance through flash distillation coupling whirl vapour-liquid separator 1, avoided condensation heat exchanger direct and desulfurization thick liquid direct contact, no heat transfer surface scale deposit, the emergence of corrosion phenomena, the efficiency of getting heat of thick liquid has been improved, the life of heat exchanger has been prolonged, connect simultaneously condensation heat transfer system 2 and condensate water collecting system outside having realized the purpose of thick liquid waste heat recovery utilization, realize simultaneously that partial waste water turns into clean water, compromise waste water recovery and utilize, the purpose of water economy resource. Simultaneously flash distillation coupling whirl vapour-liquid separation device 1 in this embodiment has the flash distillation, vapour-liquid separation's dual function, has avoided defroster blade scale deposit clearance difficulty in the traditional flash distillation technology, and the drawback that the running resistance is big gets rid of the liquid drop of getting rid of to this device tower wall and is collected along the wallboard downcast under the dead weight effect because of centrifugal force, even the scale deposit also clears up easily, more can not arouse the rise of running resistance, reduction system operation energy consumption, reduction system maintenance.
In addition, the waste heat recovery system for the desulfurization absorption tower provided by the embodiment has the advantages of reducing the temperature of the desulfurization slurry and increasing SO2Thereby improving the desulfurization efficiency. The low-temperature desulfurization slurry discharged by the flash evaporation coupling cyclone vapor-liquid separation device is conveyed to the uppermost spraying layer of the desulfurization tower, so that the smoke discharge temperature at the outlet of the absorption tower is reduced, and the water carrying amount of saturated wet flue gas is reduced. The water can be saved by 60-80 t/h by the accounting of a 300MW unit.
It should be noted that the waste heat recovery system composed of the flash evaporation coupling cyclone gas-liquid separation device 1 and the condensation heat exchange system 2 in this embodiment may not only be used in the separation absorption tower in fig. 1, but also be used in other fields of discharging high-temperature wastewater, such as waste heat recovery of wastewater discharged from some slaughterhouses. The process flow and the system configuration of the waste heat recovery system are basically the same as those of the waste heat recovery system in the figure 1. The difference lies in that the waste water generated in the slaughtering production process at 48 ℃ is sprayed into the waste water spraying and atomizing device 1 shown in the attached figure 1. The same as the embodiment 1 is that the purposes of waste heat recovery and waste water recovery are realized after the flash evaporation coupling cyclone gas-liquid separation device 1 and condensation heat exchange. The concentrated cooling wastewater collected by the cone hopper 5 at the lower part of the attached drawing 1 is conveyed to a wastewater treatment tank through the low-temperature wastewater discharge system 5 of the attached drawing 2.
Some other embodiments of this disclosure still provide with the waste water waste heat recovery system application example that constitutes of flash evaporation coupling whirl vapour-liquid separation device 1 and condensation heat transfer system 2, as shown in fig. 4, set up a plurality of flash evaporation coupling whirl vapour-liquid separation devices 1 parallelly connected, waste water in these flash evaporation coupling whirl vapour-liquid separation devices 1 sprays atomizing device 11 and is connected to same waste water pipeline 11, and the inside core pipe top of these flash evaporation coupling whirl vapour-liquid separation devices 1 is connected to same condensate system simultaneously, can handle a large amount of waste water through a plurality of separation devices 1 simultaneously like this, improve treatment effeciency.
The following waste heat recovery process for the desulfurization absorption tower slurry is based on the above process:
except opening a vacuum pump inlet valve of a noncondensable gas exhaust vacuum pump system 4, closing all external interface valves of the whole system to enable the whole system to be a closed system, starting the noncondensable gas exhaust vacuum pump system 4, starting an inlet adjusting valve of a spray device of a flash evaporation coupling cyclone vapor-liquid separation device 1 when the vacuum degree of the whole desulfurization slurry waste heat recovery system reaches-91.5 kPa, spraying slurry in the uppermost layer spray mother pipe of a desulfurization absorption tower 6 into the flash evaporation coupling cyclone vapor-liquid separation device 1 through a spray atomization device 11 shown in the attached drawing 1 under the action of the negative pressure of the system, and instantly and partially evaporating the slurry at 51 ℃ under the vacuum working condition of the pressure of-91.5 kPa to form saturated vapor at 45 ℃ and saturated slurry at 45 ℃; and (3) forming an external swirling steam flow and an internal swirling steam flow of 45-50 m/s in the special structure of the flash evaporation coupling swirling steam-liquid separation device 1 by carrying partial slurry fog drops with steam, and throwing the slurry fog drops carried with the steam flow to a tower body wall plate to be separated from the steam under the dual centrifugal force action of the spirally descending external swirling flow and the spirally ascending internal swirling flow. The purified steam reaches the condensation heat exchange system 2 under the suction action of lower negative pressure, and the steam releases latent heat in the condensation heat exchange system 2 to the working medium so as to achieve the purpose of waste heat recovery; meanwhile, the steam is condensed into clean water, and the clean water is collected by the condensed water collecting system 3 to achieve the purpose of recycling the waste water. In order to keep the negative pressure working condition of-91.5 kPa of the whole system, the non-condensable gas which is not condensed in the condensation heat exchange system 2 is discharged out of the system by the non-condensable gas discharge vacuum pump system 4. The non-evaporated and concentrated 45 ℃ saturated slurry is collected by a lower cone hopper of the flash evaporation coupling rotational flow vapor-liquid separation device 1 and is conveyed to the spraying mother pipe at the uppermost layer of the desulfurization absorption tower 6 by the low-temperature waste sewage discharge system 5.
Finally, the above embodiments are only intended to illustrate the technical solutions of the present disclosure and not to limit, although the present disclosure has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions may be made to the technical solutions of the present disclosure without departing from the spirit and scope of the technical solutions, and all of them should be covered in the claims of the present disclosure.
Although the present disclosure has been described with reference to specific embodiments, it should be understood that the scope of the present disclosure is not limited thereto, and those skilled in the art will appreciate that various modifications and changes can be made without departing from the spirit and scope of the present disclosure.
Claims (10)
1. A flash evaporation coupling rotational flow steam-liquid separation device is characterized by comprising an inner core pipe and an outer straight cylinder which are coaxial and vertically arranged, wherein the length of the inner core pipe is smaller than that of the outer straight cylinder, the bottom of the outer straight cylinder is connected with a lower conical hopper, and an annular channel is formed between the inner core pipe and the outer straight cylinder; the top of annular channel is sealed, and the top is equipped with the passageway pipe of slope, is equipped with the contained angle between the axis of passageway pipe and the axis of the straight barrel of outside, and is the acute angle, and the inside of passageway pipe is equipped with the atomizer.
2. A flash coupled cyclone gas-liquid separator as claimed in claim 1, wherein the top of the inner core tube is connected to the condensing heat exchanger through a pipeline, and the condensing heat exchanger is provided with a heat exchange tube.
3. The flash coupled cyclonic vapor-liquid separation device of claim 2 wherein the top of the condensing heat exchanger is in communication with the condensate storage tank and the bottom of the condensing heat exchanger is in communication with the condensate storage tank via a conduit.
4. The flash coupled cyclone vapor-liquid separation device according to claim 2, wherein the condensation heat exchange system is connected with a noncondensable gas discharge vacuum pump.
5. The flash coupled cyclonic vapor-liquid separation device of claim 1, wherein the width of the passage tube is equal to the width of the annular passage, and the passage tube is tangentially connected to the annular passage.
6. The flash-coupled cyclonic vapor-liquid separation apparatus of claim 1, wherein said atomizer is a piping network comprising a plurality of nozzles, and the direction of the spray droplets from said nozzles is parallel to the axial direction of said passage tube.
7. A desulfurization absorption tower comprising a flash coupled cyclonic vapor-liquid separation apparatus as claimed in any one of claims 1 to 6.
8. The desulfurization absorption tower as recited in claim 1, wherein the high temperature waste water pipe of the desulfurization absorption tower is connected with the atomizer in the channel pipe, and the bottom of the outer straight cylinder body is connected with the uppermost spray layer in the desulfurization tower through an external discharge pump.
9. A waste heat recovery process of a flash evaporation coupling cyclone gas-liquid separation device based on any one of claims 3-6 is characterized by comprising the following steps:
vacuumizing the interiors of the flash evaporation coupling cyclone vapor-liquid separation device and the condensation heat exchanger; communicating a high-temperature waste sewage pipeline with an atomizer in a vapor-liquid separation device, and evaporating the high-temperature waste sewage under a vacuum working condition to form low-temperature saturated water vapor and low-temperature saturated liquid;
the low-temperature saturated steam forms high-speed spirally descending outer rotational flow airflow under the flow guiding action of an annular channel formed by the external straight cylinder body and the internal core pipe, the outer rotational flow airflow reversely and upwards continuously performs spirally ascending inner rotational flow movement when moving downwards to the lower conical hopper on the external straight cylinder body, and flows into the condensation heat exchanger through the top of the internal core pipe to perform cold and heat exchange with a medium in the heat exchange pipe.
10. The waste heat recovery process of claim 9, wherein a noncondensable gas emission vacuum pump is connected to the bottom of the condensing heat exchanger.
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