CN111001173A - Improved generation economic benefits and social benefits cross-flow MVR system - Google Patents
Improved generation economic benefits and social benefits cross-flow MVR system Download PDFInfo
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- CN111001173A CN111001173A CN201911253207.9A CN201911253207A CN111001173A CN 111001173 A CN111001173 A CN 111001173A CN 201911253207 A CN201911253207 A CN 201911253207A CN 111001173 A CN111001173 A CN 111001173A
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- 230000008901 benefit Effects 0.000 title claims description 9
- 239000007788 liquid Substances 0.000 claims abstract description 154
- 238000004140 cleaning Methods 0.000 claims abstract description 34
- 238000007906 compression Methods 0.000 claims abstract description 20
- 230000006835 compression Effects 0.000 claims abstract description 18
- 239000002918 waste heat Substances 0.000 claims abstract description 17
- 238000011084 recovery Methods 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 12
- 238000002425 crystallisation Methods 0.000 claims description 90
- 230000008025 crystallization Effects 0.000 claims description 90
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 230000000694 effects Effects 0.000 claims description 17
- 238000011010 flushing procedure Methods 0.000 claims description 14
- 239000007789 gas Substances 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 6
- 230000009977 dual effect Effects 0.000 claims 6
- 238000001704 evaporation Methods 0.000 abstract description 29
- 230000008020 evaporation Effects 0.000 abstract description 29
- 238000007599 discharging Methods 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 239000011552 falling film Substances 0.000 description 10
- 239000013078 crystal Substances 0.000 description 9
- 238000010438 heat treatment Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 7
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 230000009291 secondary effect Effects 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 238000009434 installation Methods 0.000 description 3
- 235000011164 potassium chloride Nutrition 0.000 description 3
- 239000001103 potassium chloride Substances 0.000 description 3
- 239000012459 cleaning agent Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000009290 primary effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- -1 for example Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0094—Evaporating with forced circulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
-
- 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
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Crystallography & Structural Chemistry (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses an improved double-effect cross flow MVR system which comprises a material liquid flow subsystem, a cross flow steam compression subsystem, a waste heat recovery subsystem and a cleaning system, wherein the material liquid flow subsystem is connected with the cross flow steam compression subsystem, and the waste heat recovery subsystem is respectively connected with the cross flow steam compression subsystem and the cleaning system. The invention has low operation energy consumption, can not generate flash evaporation phenomenon during discharging, can avoid pipeline blockage and has high evaporation efficiency.
Description
Technical Field
The invention relates to the technical field of industrial evaporators, in particular to an improved double-effect cross-flow MVR system.
Background
The negative pressure ejection of compact mode of current economic benefits and social benefits cross-flow MVR system adopts the vacuum pump to take out the gas of crystallization kettle and produces the negative pressure, and is high to the sealed requirement of crystallization kettle, and difficult control vacuum moreover, because the negative pressure produces the flash distillation during the ejection of compact and separates out the crystallization and block up the ejection of compact pipeline, solution produces the crystallization easily or only produces a small amount of crystallization along with concentration improves in the evaporation process, because the scale deposit leads to heat exchanger heat exchange effect variation, the risk that evaporation efficiency reduces.
Disclosure of Invention
The invention aims to solve the technical problem of providing an improved double-effect cross-flow MVR system which is low in operation energy consumption, free of flash evaporation phenomenon during discharging, capable of avoiding pipeline blockage and high in evaporation efficiency.
In order to solve the technical problems, the technical scheme of the invention is as follows:
an improved double-effect cross-flow MVR system comprises a material liquid flow subsystem, a cross-flow steam compression subsystem, a waste heat recovery subsystem and a cleaning system, wherein the material liquid flow subsystem is connected with the cross-flow steam compression subsystem, and the waste heat recovery subsystem is respectively connected with the cross-flow steam compression subsystem and the cleaning system.
Preferably, the feed liquid flow subsystem comprises a raw material tank 1, a feed pump 2, a liquid-liquid heat exchanger 3, a vapor-liquid heat exchanger 4, a first-effect preheater 16, a first-effect heater 7, a first-effect separator 8, a first-effect circulating pump 9, a second-effect preheater 17, a second-effect heater 11, a second-effect separator 12, a second-effect circulating pump 13, a crystallization kettle 20 and a solid-liquid separator 23, wherein the raw material tank 1, the feed pump 2, the cold side of the liquid-liquid heat exchanger 3 and the cold side of the vapor-liquid heat exchanger 4 are sequentially connected in series, the outlet of the cold side of the vapor-liquid heat exchanger 4 is connected to a pipeline between the outlet of the first-effect circulating pump 9 and the inlet of the feed liquid of the first-effect separator 16, the outlet of the feed liquid of the first-effect circulating pump 9 is connected with the feed liquid inlet of the first-effect preheater 16, the feed liquid outlet of the first-effect preheater, a feed liquid outlet at the bottom of the first-effect separator 8 is connected with an inlet of a first-effect circulating pump 9, a connecting pipe between an outlet of the first-effect circulating pump 9 and a feed liquid inlet of a first-effect preheater 16 is connected with a connecting pipe between an outlet at the upper end of a solid-liquid separator 23 and a feed liquid inlet of a second-effect preheater 17, the connecting position is at the lower end of a first-effect feed port, and a valve is arranged between the first-effect feed port and the first; an outlet of the double-effect circulating pump 13 is connected with a tangential inlet of the solid-liquid separator 23, an outlet at the upper end of the solid-liquid separator 23 is connected with a feed liquid inlet of the double-effect preheater 17, a feed liquid outlet of the double-effect preheater 17 is connected with an upper pipe box of the double-effect heater 11, a feed liquid outlet at the bottom of the double-effect heater 11 is connected with an inlet of the double-effect separator 12, a feed liquid outlet at the bottom of the double-effect separator 12 is connected with an inlet of the double-effect circulating pump 13, an outlet at the lower end of the solid-liquid separator 23 is connected with an inlet of the crystallization kettle 20, and; the steam outlet of the two-effect separator 12 is connected with the inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
Preferably, the cross-flow vapor compression subsystem comprises a first-effect heater 7, a first-effect separator 8, a second-effect heater 11, a second-effect separator 12, a first-effect compressor 10 and a second-effect compressor 15, wherein a vapor outlet of the first-effect separator 8 is connected with an inlet of the first-effect compressor 10, and an outlet of the first-effect compressor 10 is connected with a vapor inlet of the second-effect heater 11; the steam outlet of the two-effect separator 12 is connected with the inlet of a two-effect compressor 15, and the outlet of the two-effect compressor 15 is connected with the steam inlet of the one-effect heater 7.
Preferably, the waste heat recovery subsystem comprises a first-effect heater 7, a second-effect heater 11, a first-effect preheater 16, a second-effect preheater 17, a condensed water collection tank 6, a liquid-liquid heat exchanger 3, a vapor-liquid heat exchanger 4 and a condensed water pump 5, condensed water outlets of the first-effect heater 7 and the second-effect heater 11 and condensed water outlets of the first-effect preheater 16 and the second-effect preheater 17 are respectively connected with the condensed water collection tank 16, and a non-condensable gas outlet of the first-effect heater 7 and the second-effect heater 11, a non-condensable gas outlet at the upper part of the condensed water collection tank 16 and a hot side of the vapor-liquid heat exchanger 4 are sequentially connected in series; and a liquid outlet at the bottom of the condensed water collecting tank 16, the hot side of the liquid-liquid heat exchanger 3 and an inlet of the condensed water pump 5 are sequentially connected in series.
Preferably, the cleaning system comprises a cleaning dosing tank 18, a cleaning pump 19, a liquid-liquid heat exchanger 3 and a vapor-liquid heat exchanger 4, wherein the cleaning dosing tank 18, the cleaning pump 19, the cold side of the liquid-liquid heat exchanger 3 and the cold side of the vapor-liquid heat exchanger 4 are sequentially connected in series, and the outlet of the cold side of the vapor-liquid heat exchanger 4 is connected to a one-effect feed port pipeline.
Preferably, the second-effect evaporator of the feed liquid flow subsystem adopts a forced circulation evaporator mode, wherein the forced circulation evaporator comprises: the system comprises a two-effect forced circulation heater 11, a two-effect separator 12, a two-effect forced circulation pump 13, a crystallization backflushing pump 14 and a crystallization kettle 20, wherein a connecting pipe between an outlet of a first-effect circulation pump 9 and a feed liquid inlet of a first-effect preheater 16 is connected with a connecting pipe between an outlet at the lower end of the two-effect separator 12 and a feed liquid inlet of the two-effect heater 11, an inlet and an outlet of the two-effect forced circulation pump 13 are connected with the two-effect heater 11, and a feed liquid outlet of the two-effect heater 11 is connected with an inlet at the upper end of; the double-effect separator 12 is connected with a crystallization back-flushing pump 14, an outlet at the bottom of the double-effect separator 12 is connected with an inlet of a crystallization kettle 20, and a steam outlet of the double-effect separator 12 is connected with an inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
Preferably, the feed liquid flow subsystem adopts a forced circulation evaporator mode, wherein the forced circulation evaporator comprises: the system comprises a first-effect forced circulation heater 7, a first-effect separator 8, a first-effect forced circulation pump 9, a second-effect forced circulation heater 11, a second-effect separator 12, a second-effect forced circulation pump 13, a crystallization recoil pump 14, a crystallization recoil pump 22, a crystallization kettle 20 and a crystallization kettle 21, wherein a cold side outlet of a gas-liquid heat exchanger 4 is connected with a connecting pipe between a lower end outlet of the first-effect separator 8 and a feed liquid inlet of the first-effect forced circulation heater 7, an inlet and an outlet of the first-effect forced circulation pump 9 are connected with the first-effect forced circulation heater 7, and a feed liquid outlet of the first-effect forced circulation heater 7 is connected with an upper end inlet of the first-effect; the first-effect separator 8 is connected with a crystallization back-flushing pump 22, an outlet at the bottom of the first-effect separator 8 is connected with an inlet of a crystallization kettle 21, and a steam outlet of the first-effect separator 8 is connected with an inlet of the crystallization kettle 21, so that the pressure in the separator is the same as that in the crystallization kettle; an outlet of the crystallization recoil pump 22 is connected with a connecting pipe between an outlet at the lower end of the double-effect separator 12 and a feed liquid inlet of the double-effect heater 11, an inlet and an outlet of the double-effect forced circulation pump 13 are connected with the double-effect heater 11, and a feed liquid outlet of the double-effect heater 11 is connected with an inlet at the upper end of the double-effect separator 12; the two-effect separator 12 is connected with a crystallization back-flushing pump 14, an outlet at the bottom of the two-effect separator 12 is connected with an inlet of a crystallization kettle 20, and a steam outlet of the two-effect separator 12 is connected with an inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
By adopting the technical scheme, the improved double-effect cross flow MVR system provided by the invention has the advantages that the feed liquid flow subsystem in the improved double-effect cross flow MVR system is connected with the cross flow steam compression subsystem, the waste heat recovery subsystem is respectively connected with the cross flow steam compression subsystem and the cleaning system, the operation energy consumption of the whole system is low, the flash evaporation phenomenon cannot be generated during discharging, the pipeline blockage can be avoided, the heat exchange effect of a heat exchanger is prevented from being deteriorated due to scaling by adding the cleaning system, and the evaporation efficiency is high.
Drawings
FIG. 1 is a system flow diagram of a first embodiment of the present invention;
FIG. 2 is a system flow diagram of a second embodiment of the present invention;
fig. 3 is a system flow chart of a third embodiment of the present invention.
Detailed Description
The following further describes embodiments of the present invention with reference to the drawings. It should be noted that the description of the embodiments is provided to help understanding of the present invention, but the present invention is not limited thereto. In addition, the technical features involved in the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the invention.
The first embodiment is as follows: the improved double-effect cross-flow MVR system can be a double-effect cross-flow MVR falling film evaporator, compared with the existing double-effect cross-flow MVR system, a lower pipe box of the falling film evaporator and a gas-liquid separator are combined, the double-effect falling film evaporator is provided with a solid-liquid separator, a discharging mode is improved, a cleaning system is added, the improved double-effect cross-flow MVR system is mainly used for treating a solution with high material solubility, such as ammonium salt and nitrate solution, and the solution cannot generate crystals or only generates a small amount of crystals along with the increase of concentration.
The specific implementation method is shown in fig. 1, and the feed liquid flow subsystem of the double-effect cross-flow MVR evaporation and concentration system comprises a raw material tank 1, a feed pump 2, a liquid-liquid heat exchanger 3, a vapor-liquid heat exchanger 4, a first-effect preheater 16, a first-effect heater 7, a first-effect separator 8, a first-effect circulating pump 9, a second-effect preheater 17, a second-effect heater 11, a second-effect separator 12, a second-effect circulating pump 13, a crystallization kettle 20 and a solid-liquid separator 23. The raw material tank 1, the feed pump 2, the cold side of the liquid-liquid heat exchanger 3 and the cold side of the vapor-liquid heat exchanger 4 are sequentially connected in series, the outlet of the cold side of the vapor-liquid heat exchanger 4 is connected to a pipeline between the outlet of the first-effect circulating pump 9 and the feed liquid inlet of the first-effect preheater 16, the outlet of the first-effect circulating pump 9 is connected with the feed liquid inlet of the first-effect preheater 16, the feed liquid outlet of the first-effect preheater 16 is connected with the upper pipe box of the first-effect heater 7, the feed liquid outlet at the bottom of the first-effect heater 7 is connected with the inlet of the first-effect separator 8, the feed liquid outlet at the bottom of the first-effect separator 8 is connected with the inlet of the first-effect circulating pump 9, a connecting pipe between the outlet of the first-effect circulating pump 9 and the feed liquid inlet of the first-effect preheater 16 is connected with a connecting pipe between the outlet at the upper end of the solid-liquid separator 23 and the feed liquid inlet of the second-effect preheater 17, the connecting; an outlet of the double-effect circulating pump 13 is connected with a tangential inlet of the solid-liquid separator 23, an outlet at the upper end of the solid-liquid separator 23 is connected with a feed liquid inlet of the double-effect preheater 17, a feed liquid outlet of the double-effect preheater 17 is connected with an upper pipe box of the double-effect heater 11, a feed liquid outlet at the bottom of the double-effect heater 11 is connected with an inlet of the double-effect separator 12, a feed liquid outlet at the bottom of the double-effect separator 12 is connected with an inlet of the double-effect circulating pump 13, an outlet at the lower end of the solid-liquid separator 23 is connected with an inlet of the crystallization kettle 20, and; the steam outlet of the two-effect separator 12 is connected with the inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
The cross-flow vapor compression subsystem includes: the system comprises a first-effect heater 7, a first-effect separator 8, a second-effect heater 11, a second-effect separator 12, a first-effect compressor 10 and a second-effect compressor 15. The steam outlet of the one-effect separator 8 is connected with the inlet of a one-effect compressor 10, and the outlet of the one-effect compressor 10 is connected with the steam inlet of a two-effect heater 11; the steam outlet of the two-effect separator 12 is connected with the inlet of a two-effect compressor 15, and the outlet of the two-effect compressor 15 is connected with the steam inlet of the one-effect heater 7; the scheme realizes that the secondary steam generated by the first-effect heating evaporation separation is compressed by the first-effect compressor and then is used as the heat source of the second-effect evaporator, and the secondary steam generated by the second-effect heating evaporation separation is compressed by the second-effect compressor and then is used as the heat source of the first-effect evaporator; the steam pressure difference between the inlet and the outlet of the first-effect compressor 10 and the outlet of the second-effect compressor 15 is effectively reduced, so that the power consumption in the compression process of the compressors is reduced, the pollution of energy consumption to the environment is reduced, and the performance and the market competitiveness of the double-effect cross-flow MVR evaporation concentration system are improved.
The waste heat recovery subsystem includes: a first-effect heater 7, a second-effect heater 11, a first-effect preheater 16, a second-effect preheater 17, a condensed water collecting tank 6, a liquid-liquid heat exchanger 3, a vapor-liquid heat exchanger 4 and a condensed water pump 5. Condensed water outlets of the first-effect heater 7 and the second-effect heater 11 and condensed water outlets of the first-effect preheater 16 and the second-effect preheater 17 are respectively connected with a condensed water collecting tank 16, and a non-condensable gas outlet of the first-effect heater 7 and the second-effect heater 11, a non-condensable gas outlet at the upper part of the condensed water collecting tank 16 and a hot side of the steam-liquid heat exchanger 4 are sequentially connected in series; the liquid outlet at the bottom of the condensed water collecting tank 16, the hot side of the liquid-liquid heat exchanger 3 and the inlet of the condensed water pump 5 are connected in series in sequence. According to the scheme, waste heat generated in the operation process of the material liquid flow subsystem and the cross-flow steam compression subsystem of the MVR evaporation concentration system is effectively utilized, the material liquid initially entering the system is heated twice, the temperature of the material liquid before entering the first-effect heater 7 is effectively improved, energy consumption during heating in the first-effect heater 7 is reduced, and energy conservation and environmental protection of the whole machine of the double-effect cross-flow MVR evaporation concentration system are effectively realized.
The cleaning system includes: a cleaning dosing tank 18, a cleaning pump 19, a liquid-liquid heat exchanger 3 and a vapor-liquid heat exchanger 4. The cleaning and dispensing box 18, the cleaning pump 19, the cold side of the liquid-liquid heat exchanger 3 and the cold side of the vapor-liquid heat exchanger 4 are sequentially connected in series, and the outlet of the cold side of the vapor-liquid heat exchanger 4 is connected to a pipeline with an effective feed port. The cleaning system effectively removes scales in the heat exchanger and the heater, and ensures the evaporation efficiency of the evaporator.
Example two: the improved double-effect cross-flow MVR system can be a double-effect cross-flow MVR falling film + forced circulation evaporator, and compared with the existing double-effect cross-flow MVR system, the improved double-effect cross-flow MVR system combines a falling film evaporator down tube box and a gas-liquid separator, improves a heating body and a discharging mode of the forced circulation evaporator, increases a crystallization anti-impact pump and a cleaning system, and is mainly used for treating a solution which generates crystallization along with concentration increase in an evaporation process.
In the specific implementation, as shown in fig. 2, the two-effect evaporator of the feed liquid flow subsystem adopts a forced circulation evaporator mode, wherein the forced circulation evaporator comprises: a double-effect forced circulation heater 11, a double-effect separator 12, a double-effect forced circulation pump 13, a crystallization back-flushing pump 14 and a crystallization kettle 20. The connection mode is as follows: a connecting pipe between an outlet of the primary-effect circulating pump 9 and a feed liquid inlet of the primary-effect preheater 16 is connected with a connecting pipe between an outlet at the lower end of the secondary-effect separator 12 and a feed liquid inlet of the secondary-effect heater 11, an inlet and an outlet of the secondary-effect forced circulating pump 13 are connected with the secondary-effect heater 11, and a feed liquid outlet of the secondary-effect heater 11 is connected with an inlet at the upper end of the secondary-effect separator 12; the two-effect separator 12 is connected with a crystallization back-flushing pump 14, an outlet at the bottom of the two-effect separator 12 is connected with an inlet of a crystallization kettle 20, and a steam outlet of the two-effect separator 12 is connected with an inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle. It is understood that the cross-flow vapor compression subsystem, the waste heat recovery subsystem, and the cleaning system are the same as the first embodiment.
Example three: the improved double-effect cross-flow MVR system can be a double-effect cross-flow MVR forced circulation evaporator, compared with the existing double-effect cross-flow MVR system, the heating body and the discharging mode of the forced circulation evaporator are improved, a crystallization anti-impact pump and a cleaning system are added, the improved double-effect cross-flow MVR system is mainly used for processing salt separating solution, salt is separated by sections by utilizing the saturation solubility difference characteristics of different materials, for example, sodium chloride and potassium chloride in the solution are separated, sodium chloride is saturated and continuously separated out of crystals in the evaporation process, the crystals are separated and led out of the evaporator through a separator, potassium chloride is saturated along with the evaporation, concentrated solution is sent to a crystallization kettle, and potassium chloride crystals are respectively obtained after cooling.
In the specific implementation, as shown in fig. 3, the feed liquid flow subsystem adopts a forced circulation evaporator mode, wherein the forced circulation evaporator includes: the system comprises a first-effect forced circulation heater 7, a first-effect separator 8, a first-effect forced circulation pump 9, a second-effect forced circulation heater 11, a second-effect separator 12, a second-effect forced circulation pump 13, a crystallization back-flushing pump 14, a crystallization back-flushing pump 22, a crystallization kettle 20 and a crystallization kettle 21. The connection mode is as follows: a cold side outlet of the vapor-liquid heat exchanger 4 is connected with a connecting pipe between a lower end outlet of the first effect separator 8 and a feed liquid inlet of the first effect forced circulation heater 7, an inlet and an outlet of the first effect forced circulation pump 9 are connected with the first effect forced circulation heater 7, and a feed liquid outlet of the first effect forced circulation heater 7 is connected with an upper end inlet of the first effect separator 8; the first-effect separator 8 is connected with a crystallization back-flushing pump 22, an outlet at the bottom of the first-effect separator 8 is connected with an inlet of a crystallization kettle 21, and a steam outlet of the first-effect separator 8 is connected with an inlet of the crystallization kettle 21, so that the pressure in the separator is the same as that in the crystallization kettle; an outlet of the crystallization recoil pump 22 is connected with a connecting pipe between an outlet at the lower end of the double-effect separator 12 and a feed liquid inlet of the double-effect heater 11, an inlet and an outlet of the double-effect forced circulation pump 13 are connected with the double-effect heater 11, and a feed liquid outlet of the double-effect heater 11 is connected with an inlet at the upper end of the double-effect separator 12; the two-effect separator 12 is connected with a crystallization back-flushing pump 14, an outlet at the bottom of the two-effect separator 12 is connected with an inlet of a crystallization kettle 20, and a steam outlet of the two-effect separator 12 is connected with an inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle. It is understood that the cross-flow vapor compression subsystem, the waste heat recovery subsystem, and the cleaning system are the same as the first embodiment.
It can be understood that the invention has reasonable design and unique structure, and compared with the prior double-effect cross-flow MVR system:
(1) the heating body of the forced circulation evaporator is changed into 2 forced circulation heating bodies. The effect is as follows: the number of the tubes in the single forced circulation heating body is reduced, and under the condition that the flow rate of the forced circulation material is not changed, the circulation flow required by the evaporator is reduced, the power of the matched forced circulation pump is reduced, and the operation energy consumption is reduced; and the installation height of the forced circulation evaporator is reduced, so that the integral installation of the evaporator is more compact.
(2) The steam outlet of the three-phase separator of the forced circulation evaporator is additionally provided with a pipeline which is connected with the crystallization kettle. The effect is as follows: the pressure in the three-phase separator is the same as that in the crystallization kettle, the concentrated feed liquid at the bottom of the three-phase separator can automatically flow and discharge through gravity, a discharge pump or negative pressure discharge equipment is not required to be added, and the operation energy consumption is reduced; the negative pressure discharging mode in the prior art adopts a vacuum pump to pump out gas of the crystallization kettle to generate negative pressure, has high requirement on the sealing of the crystallization kettle, is difficult to control the vacuum degree, and avoids the blockage of a discharging pipeline because crystals are separated out by flash evaporation generated by the negative pressure during discharging.
(3) A crystallization back-flushing pump is added at the lower end of the three-phase separator of the forced circulation evaporator. The effect is as follows: in the running process of the evaporator, the concentrated solution at the upper end of the three-phase separator is conveyed to the bottom of the three-phase separator by the crystallization back-flushing pump and is pumped in, and crystals at the lower end of the separator are back-flushed, so that the blockage of a discharge pipeline caused by crystallization deposition and agglomeration is prevented.
(4) And combining a lower pipe box of the falling film evaporator and the gas-liquid separator. The effect is as follows: the installation height of the falling film evaporator is reduced, and the manufacturing cost of the equipment is reduced.
(5) An additional pipeline of a steam outlet of a gas-liquid separator of a double-effect falling film evaporator of the double-effect cross-flow MVR falling film evaporation system is connected with the crystallization kettle. The effect is as follows: the pressure in the gas-liquid separator is the same as that of the crystallization kettle, concentrated feed liquid can be positively conveyed to the crystallization kettle through the two-effect circulating pump without adding a discharge pump or negative pressure discharge equipment, and the operation energy consumption is reduced; in the negative pressure discharging mode in the prior art, the vacuum pump is adopted to pump out gas of the crystallization kettle 20 to generate negative pressure, the sealing requirement on the crystallization kettle 20 is high, the vacuum degree is not easy to control, and flash evaporation is generated to separate out crystals and block a discharging pipeline due to the negative pressure during discharging.
(6) An evaporator cleaning system is added. The effect is as follows: the risk that the heat exchange effect of the heat exchanger is poor and the evaporation efficiency is reduced due to scaling is avoided.
(7) The double-effect falling-film evaporator is provided with a solid-liquid separator. The effect is as follows: and crystals in the concentrated solution are separated, so that pipeline blockage is avoided, and the circulating pump is protected against abrasion.
It can be understood that the feed liquid flow subsystem in the improved double-effect cross-flow MVR system refers to: the feed liquid enters the system and is preheated by the waste heat recovery subsystem, then is connected into a first-effect circulating pipeline and is mixed with the first-effect circulating feed liquid, then is continuously preheated to a bubble point by external raw steam through a preheater and enters first-effect evaporation, the feed liquid in a first-effect evaporator is evaporated and preliminarily concentrated, the produced preliminary concentrate and secondary steam are subjected to first-effect separation, part of the separated feed liquid returns to the first-effect evaporation and separation circulation, and part of the feed liquid is subjected to second-effect evaporation and second-effect separation to obtain a concentrated solution which is discharged out of the system; the cross-flow vapor compression subsystem refers to: the secondary steam generated by the first-effect evaporation separation is compressed by the first-effect compressor and then is used as a heat source for the second-effect evaporation, and the secondary steam generated by the second-effect evaporation separation is compressed by the second-effect compressor and then is used as a heat source for the first-effect evaporation; the waste heat recovery subsystem is as follows: high-temperature non-condensable gas and high-temperature condensed water discharged by the first-effect preheater 7, the first-effect evaporator and the second-effect evaporator are recovered to a condensed water collecting tank 6, then the high-temperature non-condensable gas is discharged out of the system through a gas-liquid heat exchanger 4 and a non-condensed gas separator of a waste heat recovery system, and the high-temperature condensed water is discharged out of the system through a liquid-liquid heat exchanger 3 and a condensed water pump 5 of the waste heat recovery system; the cleaning system is as follows: cleaning agent with proper concentration is prepared in the cleaning and dispensing box 18, and then the cleaning agent is sent to the liquid-liquid heat exchanger 3, the vapor-liquid heat exchanger 4 and the evaporator by the cleaning pump 19, and scales in the heat exchanger and the evaporator are removed by circulating cleaning.
The technical scheme effectively reduces the steam pressure difference between the inlet and the outlet of the first-effect compressor and the second-effect compressor, thereby reducing the power consumption in the compression process of the compressors, realizing the energy conservation and consumption reduction of the system operation, and improving the performance and market competitiveness of the improved double-effect cross-flow MVR system.
The embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited to the described embodiments. It will be apparent to those skilled in the art that various changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, and the scope of protection is still within the scope of the invention.
Claims (7)
1. An improved generation economic benefits and social benefits cross-flow MVR system which characterized in that: the system comprises a material liquid flow subsystem, a cross-flow steam compression subsystem, a waste heat recovery subsystem and a cleaning system, wherein the material liquid flow subsystem is connected with the cross-flow steam compression subsystem, and the waste heat recovery subsystem is respectively connected with the cross-flow steam compression subsystem and the cleaning system.
2. The improved dual effect cross-flow MVR system of claim 1, wherein: the feed liquid flow subsystem comprises a raw material tank 1, a feed pump 2, a liquid-liquid heat exchanger 3, a vapor-liquid heat exchanger 4, a first-effect preheater 16, a first-effect heater 7, a first-effect separator 8, a first-effect circulating pump 9, a second-effect preheater 17, a second-effect heater 11, a second-effect separator 12, a second-effect circulating pump 13, a crystallization kettle 20 and a solid-liquid separator 23, wherein the raw material tank 1, the feed pump 2, the cold side of the liquid-liquid heat exchanger 3 and the cold side of the vapor-liquid heat exchanger 4 are sequentially connected in series, the outlet of the cold side of the vapor-liquid heat exchanger 4 is connected to a pipeline between the outlet of the first-effect circulating pump 9 and the feed liquid inlet of the first-effect preheater 16, the outlet of the first-effect circulating pump 9 is connected with the feed liquid inlet of the first-effect preheater 16, the feed liquid outlet of the first-effect preheater 16 is connected with a, a feed liquid outlet at the bottom of the first-effect separator 8 is connected with an inlet of a first-effect circulating pump 9, a connecting pipe between an outlet of the first-effect circulating pump 9 and a feed liquid inlet of a first-effect preheater 16 is connected with a connecting pipe between an outlet at the upper end of a solid-liquid separator 23 and a feed liquid inlet of a second-effect preheater 17, the connecting position is at the lower end of a first-effect feed port, and a valve is arranged between the first-effect feed port and the first; an outlet of the double-effect circulating pump 13 is connected with a tangential inlet of the solid-liquid separator 23, an outlet at the upper end of the solid-liquid separator 23 is connected with a feed liquid inlet of the double-effect preheater 17, a feed liquid outlet of the double-effect preheater 17 is connected with an upper pipe box of the double-effect heater 11, a feed liquid outlet at the bottom of the double-effect heater 11 is connected with an inlet of the double-effect separator 12, a feed liquid outlet at the bottom of the double-effect separator 12 is connected with an inlet of the double-effect circulating pump 13, an outlet at the lower end of the solid-liquid separator 23 is connected with an inlet of the crystallization kettle 20, and; the steam outlet of the two-effect separator 12 is connected with the inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
3. The improved dual effect cross-flow MVR system of claim 1, wherein: the cross-flow steam compression subsystem comprises a first-effect heater 7, a first-effect separator 8, a second-effect heater 11, a second-effect separator 12, a first-effect compressor 10 and a second-effect compressor 15, wherein a steam outlet of the first-effect separator 8 is connected with an inlet of the first-effect compressor 10, and an outlet of the first-effect compressor 10 is connected with a steam inlet of the second-effect heater 11; the steam outlet of the two-effect separator 12 is connected with the inlet of a two-effect compressor 15, and the outlet of the two-effect compressor 15 is connected with the steam inlet of the one-effect heater 7.
4. The improved dual effect cross-flow MVR system of claim 1, wherein: the waste heat recovery subsystem comprises a first-effect heater 7, a second-effect heater 11, a first-effect preheater 16, a second-effect preheater 17, a condensed water collection tank 6, a liquid-liquid heat exchanger 3, a vapor-liquid heat exchanger 4 and a condensed water pump 5, condensed water outlets of the first-effect heater 7 and the second-effect heater 11 and condensed water outlets of the first-effect preheater 16 and the second-effect preheater 17 are respectively connected with the condensed water collection tank 16, and a non-condensable gas outlet of the first-effect heater 7 and the second-effect heater 11, a non-condensable gas outlet at the upper part of the condensed water collection tank 16 and a hot side of the vapor-liquid heat exchanger 4 are sequentially connected in series; and a liquid outlet at the bottom of the condensed water collecting tank 16, the hot side of the liquid-liquid heat exchanger 3 and an inlet of the condensed water pump 5 are sequentially connected in series.
5. The improved dual effect cross-flow MVR system of claim 1, wherein: the cleaning system comprises a cleaning dosing tank 18, a cleaning pump 19, a liquid-liquid heat exchanger 3 and a vapor-liquid heat exchanger 4, wherein the cleaning dosing tank 18, the cleaning pump 19, the cold side of the liquid-liquid heat exchanger 3 and the cold side of the vapor-liquid heat exchanger 4 are sequentially connected in series, and the outlet of the cold side of the vapor-liquid heat exchanger 4 is connected to a one-effect feed port pipeline.
6. The improved dual effect cross-flow MVR system of claim 1, wherein: the second effect evaporator of the feed liquid flow subsystem adopts a forced circulation evaporator mode, wherein the forced circulation evaporator comprises: the system comprises a two-effect forced circulation heater 11, a two-effect separator 12, a two-effect forced circulation pump 13, a crystallization backflushing pump 14 and a crystallization kettle 20, wherein a connecting pipe between an outlet of a first-effect circulation pump 9 and a feed liquid inlet of a first-effect preheater 16 is connected with a connecting pipe between an outlet at the lower end of the two-effect separator 12 and a feed liquid inlet of the two-effect heater 11, an inlet and an outlet of the two-effect forced circulation pump 13 are connected with the two-effect heater 11, and a feed liquid outlet of the two-effect heater 11 is connected with an inlet at the upper end of; the double-effect separator 12 is connected with a crystallization back-flushing pump 14, an outlet at the bottom of the double-effect separator 12 is connected with an inlet of a crystallization kettle 20, and a steam outlet of the double-effect separator 12 is connected with an inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
7. The improved dual effect cross-flow MVR system of claim 1, wherein: the feed liquid flow subsystem all adopts forced circulation evaporimeter mode, and wherein forced circulation evaporimeter includes: the system comprises a first-effect forced circulation heater 7, a first-effect separator 8, a first-effect forced circulation pump 9, a second-effect forced circulation heater 11, a second-effect separator 12, a second-effect forced circulation pump 13, a crystallization recoil pump 14, a crystallization recoil pump 22, a crystallization kettle 20 and a crystallization kettle 21, wherein a cold side outlet of a gas-liquid heat exchanger 4 is connected with a connecting pipe between a lower end outlet of the first-effect separator 8 and a feed liquid inlet of the first-effect forced circulation heater 7, an inlet and an outlet of the first-effect forced circulation pump 9 are connected with the first-effect forced circulation heater 7, and a feed liquid outlet of the first-effect forced circulation heater 7 is connected with an upper end inlet of the first-effect; the first-effect separator 8 is connected with a crystallization back-flushing pump 22, an outlet at the bottom of the first-effect separator 8 is connected with an inlet of a crystallization kettle 21, and a steam outlet of the first-effect separator 8 is connected with an inlet of the crystallization kettle 21, so that the pressure in the separator is the same as that in the crystallization kettle; an outlet of the crystallization recoil pump 22 is connected with a connecting pipe between an outlet at the lower end of the double-effect separator 12 and a feed liquid inlet of the double-effect heater 11, an inlet and an outlet of the double-effect forced circulation pump 13 are connected with the double-effect heater 11, and a feed liquid outlet of the double-effect heater 11 is connected with an inlet at the upper end of the double-effect separator 12; the two-effect separator 12 is connected with a crystallization back-flushing pump 14, an outlet at the bottom of the two-effect separator 12 is connected with an inlet of a crystallization kettle 20, and a steam outlet of the two-effect separator 12 is connected with an inlet of the crystallization kettle 20, so that the pressure in the separator is the same as that in the crystallization kettle.
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