CN112010380A - Preparation device and preparation method of hot purified water - Google Patents
Preparation device and preparation method of hot purified water Download PDFInfo
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- CN112010380A CN112010380A CN202010797119.1A CN202010797119A CN112010380A CN 112010380 A CN112010380 A CN 112010380A CN 202010797119 A CN202010797119 A CN 202010797119A CN 112010380 A CN112010380 A CN 112010380A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 121
- 239000008213 purified water Substances 0.000 title claims abstract description 89
- 238000002360 preparation method Methods 0.000 title abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 122
- 239000002994 raw material Substances 0.000 claims abstract description 92
- 238000010992 reflux Methods 0.000 claims abstract description 44
- 238000001704 evaporation Methods 0.000 claims abstract description 37
- 230000008020 evaporation Effects 0.000 claims abstract description 35
- 238000010438 heat treatment Methods 0.000 claims abstract description 34
- 238000000034 method Methods 0.000 claims description 13
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 239000013535 sea water Substances 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 4
- 239000003673 groundwater Substances 0.000 claims description 3
- 239000010865 sewage Substances 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 abstract description 13
- 238000010612 desalination reaction Methods 0.000 abstract description 9
- 239000000243 solution Substances 0.000 description 59
- 239000013505 freshwater Substances 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 4
- 239000012527 feed solution Substances 0.000 description 4
- 238000007701 flash-distillation Methods 0.000 description 4
- 239000000284 extract Substances 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000004891 communication Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
-
- 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
- C02F1/06—Flash evaporation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D3/00—Hot-water central heating systems
- F24D3/10—Feed-line arrangements, e.g. providing for heat-accumulator tanks, expansion tanks ; Hydraulic components of a central heating system
- F24D3/1058—Feed-line arrangements, e.g. providing for heat-accumulator tanks, expansion tanks ; Hydraulic components of a central heating system disposition of pipes and pipe connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a preparation device and a preparation method of hot purified water, wherein the preparation device comprises the following components: an N-stage flash evaporator; a reflux liquid inlet of a J-stage reflux pipeline in the K-stage reflux pipeline is communicated with a concentrated liquid outlet of a P-stage flash evaporator in the N-stage flash evaporator, a reflux liquid outlet of the J-stage reflux pipeline is communicated with a raw material liquid inlet of a Q-stage flash evaporator in the N-stage flash evaporator, wherein N is not less than 2, K is not less than J is not less than 1, and N is not less than P is not less than Q; and the heater is used for heating the raw material liquid to the temperature required by the flash evaporation of the 1 st-stage flash evaporator, a cold medium inlet of the heater is communicated with a raw material liquid outlet of the 1 st-stage flash evaporator in the N-stage flash evaporators, and a cold medium outlet of the heater is communicated with a concentrated liquid inlet of the 1 st-stage flash evaporator in the N-stage flash evaporators. The device realizes hydrothermal coproduction on the one hand, and on the other hand makes the concentration degree of concentrate controllable, and the raw material liquid desalination degree in the hot pure water preparation process is controllable, improves the yield of hot pure water.
Description
Technical Field
The invention relates to the technical field of fresh water preparation and centralized heating, in particular to a preparation device and a preparation method of hot purified water.
Background
Due to the needs of economic development, the industrial water consumption of China is kept above 1200 billions of cubic meters all year round, and meanwhile, along with the continuous deepening of the urbanization process and the continuous improvement of the living standard of people, the domestic water consumption is increased year by year, and the problem of water resource shortage is increasingly prominent, especially in the northern area. On the premise of basically stable total water resource, fresh water preparation technologies such as seawater desalination, waste water recycling and the like are the most fundamental means for solving the problem of water resource shortage. Taking seawater desalination as an example, technologies such as a distillation method, a flash evaporation method and a reverse osmosis method are mainly adopted at present, wherein the distillation method and the flash evaporation method which depend on heat driving have the problem of low energy utilization efficiency, and the reverse osmosis method has low energy consumption per unit water production, but the reverse osmosis membrane material needs to be frequently replaced, and is finally reflected in the operation cost.
Therefore, the development of a fresh water preparation technology with high energy utilization efficiency and low operation cost has great significance for efficiently solving the problem of water resource shortage. In addition, with the improvement of living standard, the demand of people for central heating is more and more intense, and how to utilize waste heat in the traditional fresh water preparation technical process for central heating to realize hydrothermal coproduction is an important driving force for popularizing technologies such as seawater desalination and the like. The problem that attention needs to be paid in the fresh water preparation process is that the desalination degree of the fresh water and the fresh water generation rate are improved to the maximum extent in the process of preparing the fresh water while the hydrothermal coproduction is carried out.
Disclosure of Invention
The embodiment of the invention aims to provide a preparation device and a preparation method of hot purified water, which can improve the desalination degree of fresh water and the generation rate of the fresh water to the greatest extent in the preparation process of the fresh water while simultaneously carrying out hydrothermal coproduction.
In order to solve the above technical problem, an aspect of the present invention provides an apparatus for preparing hot purified water, including: each stage of flash evaporator comprises a raw material liquid heating zone and a concentrated liquid flash evaporation zone, the raw material liquid heating zone is provided with a raw material liquid inlet and a raw material liquid outlet, and the concentrated liquid flash evaporation zone is provided with a concentrated liquid inlet and a concentrated liquid outlet; k-grade return pipelines, wherein each grade of return pipeline comprises a return liquid inlet and a return liquid outlet, the return liquid inlet of the J-grade return pipeline in the K-grade return pipeline is communicated with the concentrated liquid outlet of the P-grade flash evaporator in the N-grade flash evaporator, the return liquid outlet of the J-grade return pipeline is communicated with the raw material liquid inlet of the Q-grade flash evaporator in the N-grade flash evaporator, N is more than or equal to 2, N is more than or equal to K and more than or equal to J and more than or equal to 1, and N is more than or equal to P and more than or equal to Q; and the heater comprises a cold medium inlet and a cold medium outlet, the heater is used for heating the raw material liquid to the temperature required by the flash evaporation of the 1 st-stage flash evaporator, the cold medium inlet of the heater is communicated with the raw material liquid outlet of the 1 st-stage flash evaporator in the N-stage flash evaporators, and the cold medium outlet of the heater is communicated with the concentrated liquid inlet of the 1 st-stage flash evaporator in the N-stage flash evaporators.
Further, a concentrated solution inlet of an Mth-stage flash evaporator in the N-stage flash evaporator is communicated with a concentrated solution outlet of an Mth-1-stage flash evaporator, and a raw material solution outlet of the Mth-stage flash evaporator is communicated with a raw material solution inlet of the Mth-1-stage flash evaporator; a concentrated solution outlet of an Nth-stage flash evaporator in the N-stage flash evaporator is used for discharging concentrated solution, and a raw material solution inlet of the Nth-stage flash evaporator in the N-stage flash evaporator is used for introducing raw material solution; wherein N is more than or equal to M and more than or equal to 2.
Further, a raw material liquid heating zone of each stage of the N-stage flash evaporator is of a dividing wall type structure and is positioned at the top of the flash evaporator; partial steam that the flash distillation of concentrate flash distillation district produced condenses in the raw materials liquid heating district, releases the heat of condensation, heats raw materials liquid through the heat transfer wall, and steam self condensation generates the pure water simultaneously.
Furthermore, each stage of flash evaporator in the N-stage flash evaporator also comprises a purified water generation area, and the purified water generation area comprises a purified water inlet and a purified water outlet; a purified water outlet of a G-stage flash evaporator in the N-stage flash evaporator is communicated with a purified water inlet of a G-1-stage flash evaporator; wherein N is more than or equal to G and more than or equal to 2.
Further, a purified water generation area of each stage of flash evaporator in the N-stage flash evaporator is of an open container structure, and the purified water generation area is positioned between the concentrated solution flash evaporation area and the raw material solution heating area; the purified water generation area receives purified water generated by condensation of steam flashed by the concentrated solution flash evaporation area.
Further, each of the K stages of return conduits includes: a reflux pump and a connecting pipe; and a liquid pumping port of a reflux pump of a J-th grade reflux pipeline in the K-grade reflux pipeline is communicated with a concentrated liquid outlet of a P-th grade flash evaporator in the N-grade flash evaporator through a connecting pipe, and a liquid discharging port of the reflux pump of the J-th grade reflux pipeline is communicated with a raw material liquid inlet of a Q-th grade flash evaporator in the N-grade flash evaporator through a connecting pipe.
Further, the heater also comprises a driving steam inlet and a condensed water outlet; raw material liquid enters the heater from the cold medium inlet and exchanges heat with high-temperature steam entering the heater from the driving steam inlet, condensed water generated after the high-temperature steam exchanges heat is discharged from the condensed water outlet, and the raw material liquid reaches the temperature required by the flash evaporation of the 1 st-stage flash evaporator after the heat exchange.
In another aspect of the embodiment of the present invention, there is provided a method for preparing hot purified water, which is prepared by the above-described hot purified water preparation apparatus.
Further, the raw material liquid is: sea water, river water, lake water, groundwater, sewage, wastewater or reclaimed water.
The technical scheme of the embodiment of the invention has the following beneficial technical effects:
by the device, the desalination degree of the fresh water and the generation rate of the fresh water in the fresh water preparation process are improved while the hydrothermal coproduction is realized.
Drawings
Fig. 1 is a schematic structural view of a hot purified water preparing apparatus according to an embodiment of the present invention;
fig. 2 is a schematic structural view of a hot purified water preparing apparatus according to another embodiment of the present invention.
Reference numerals:
1: a flash evaporator; 2: a reflux pump; 3: a heater; 1-A: a raw material liquid heating zone; 1-B: a concentrate flash zone; 1-C: a purified water generation zone; 1-1: a feed solution inlet; 1-2: a raw material liquid outlet; 1-3: a concentrated solution inlet; 1-4: a concentrated solution outlet; 1-5: purified water is fed; 1-6: a purified water outlet; 2-1: a reflux inlet; 2-2: a reflux liquid outlet; 3-1: a drive steam inlet; 3-2: a condensed water outlet; 3-3: a cold medium inlet; 3-4: and a cold medium outlet.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail with reference to the accompanying drawings in conjunction with the following detailed description. It should be understood that the description is intended to be exemplary only, and is not intended to limit the scope of the present invention. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present invention.
The various regions, shapes, and relative sizes and positional relationships therebetween shown in the drawings are merely exemplary, and deviations may occur in practice due to manufacturing tolerances or technical limitations, and those skilled in the art may additionally design regions/layers having different shapes, sizes, relative positions, as the actual requirements dictate.
It is to be understood that the embodiments described are only a few embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In addition, the technical features involved in the different embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
The invention will be described in more detail below with reference to the accompanying drawings. Like elements in the various figures are denoted by like reference numerals. For purposes of clarity, the various features in the drawings are not necessarily drawn to scale.
Features that are described and/or illustrated with respect to one embodiment may be used in the same way or in a similar way in one or more other embodiments, in combination with or instead of the features of the other embodiments.
Referring to fig. 1 and 2, an embodiment of the present invention provides an apparatus for preparing hot purified water, including: the flash evaporator comprises N-stage flash evaporators 1, wherein each stage of flash evaporator 1 comprises a raw material liquid heating zone 1-A and a concentrated solution flash evaporation zone 1-B, the raw material liquid heating zone 1-A is provided with a raw material liquid inlet 1-1 and a raw material liquid outlet 1-2, and the concentrated solution flash evaporation zone 1-B is provided with a concentrated solution inlet 1-3 and a concentrated solution outlet 1-4; k-grade return pipelines, wherein each grade of return pipeline comprises a return liquid inlet 2-1 and a return liquid outlet 2-2, the return liquid inlet 2-1 of the J-grade return pipeline in the K-grade return pipeline is communicated with a concentrated liquid outlet 1-4 of the P-grade flash evaporator 1 in the N-grade flash evaporator 1, the return liquid outlet 2-2 of the J-grade return pipeline is communicated with a raw material liquid inlet 1-1 of the Q-grade flash evaporator 1 in the N-grade flash evaporator 1, N is more than or equal to 2, N is more than or equal to K and more than or equal to 1, and N is more than or equal to P and more than or equal to Q; and the heater 3 comprises a cold medium inlet 3-3 and a cold medium outlet 3-4, the heater 3 is used for heating the raw material liquid to the temperature required by the flash evaporation of the 1 st-stage flash evaporator, the cold medium inlet 3-3 of the heater 3 is communicated with the raw material liquid outlet 1-2 of the 1 st-stage flash evaporator 1 in the N-stage flash evaporator 1, and the cold medium outlet 3-4 of the heater 3 is communicated with the concentrated liquid inlet 1-3 of the 1 st-stage flash evaporator 1 in the N-stage flash evaporator 1.
Referring to fig. 1, in an alternative embodiment, each flash evaporator 1 in the N-stage flash evaporators 1 is provided with a reflux pipeline, that is, N is K, and the 1 st-stage flash evaporator 1 is provided with a 1 st-stage reflux pipeline.
Referring to fig. 2, in an alternative embodiment, a first reflux pipeline is disposed in each of the N stages of flash evaporators 1, i.e., N > K.
In specific implementation mode, every grade of return line all is provided with concentrate concentration detection device in K grade return line to whether the concentration that detects the concentrate is qualified, when the concentrate concentration of a certain grade of return line department reaches the default, close this grade of return line, when the concentrate concentration of a certain grade of return line department is obviously not high, show that the raw materials liquid desalination degree before this grade of return line is lower, can open the return line according to the demand at this moment and make the concentrate flash distillation concentrate again, with the at utmost from condensing the pure water in the concentrate, improve the yield of pure water.
In some embodiments, concentrate inlet 1-3 of flash evaporator 1 of stage M in flash evaporator 1 of stage N is in communication with concentrate outlet 1-4 of flash evaporator 1 of stage M-1, and feed outlet 1-2 of flash evaporator 1 of stage M is in communication with feed inlet 1-1 of flash evaporator 1 of stage M-1; a concentrated solution outlet 1-4 of an Nth-stage flash evaporator 1 in the N-stage flash evaporator 1 is used for discharging concentrated solution, and a raw material solution inlet 1-1 of the Nth-stage flash evaporator 1 in the N-stage flash evaporator 1 is used for introducing raw material solution; wherein N is more than or equal to M and more than or equal to 2.
In some embodiments, the K stage return line is oriented from the K stage return line to the 1 st stage return line in a direction consistent with the flow of the feed solution in the feed solution heating zone 1-a.
In some embodiments, feed solution heating zone 1-a of each of N-stage flash vessel 1 is a dividing wall type structure located at the top of flash vessel 1; part of steam generated by flash evaporation in the concentrated solution flash evaporation area 1-B is condensed in the raw material solution heating area 1-A, condensation heat is released, the raw material solution is heated through the heat exchange wall, and meanwhile, the steam is condensed to generate pure water.
In some embodiments, each flash evaporator 1 of the N-stage flash evaporators 1 further comprises a purified water generation zone 1-C, and the purified water generation zone 1-C comprises a purified water inlet 1-5 and a purified water outlet 1-6; purified water outlets 1-6 of G-stage flash evaporators 1 in the N-stage flash evaporators 1 are communicated with purified water inlets 1-5 of the G-1-stage flash evaporators 1; wherein N is more than or equal to G and more than or equal to 2.
In some embodiments, purified water generation zone 1-C of each flash vessel 1 of N-stage flash vessels 1 is an open vessel configuration, with purified water generation zone 1-C located between concentrate flash distillation zone 1-B and feedstock heating zone 1-a; the purified water generation zone 1-C receives purified water generated by condensation of steam flashed in the concentrated solution flash evaporation zone 1-B.
In some embodiments, each of the K stages of return conduits includes: a reflux pump 2 and a connecting pipe; the liquid extraction port of the reflux pump 2 of the J-th stage reflux pipeline in the K-stage reflux pipeline is communicated with a concentrated liquid outlet 1-4 of the P-th stage flash evaporator 1 in the N-stage flash evaporator 1 through a connecting pipe, and the liquid discharge port of the reflux pump 2 of the J-th stage reflux pipeline is communicated with a raw material liquid inlet 1-1 of the Q-th stage flash evaporator 1 in the N-stage flash evaporator 1 through a connecting pipe.
In some embodiments, the heater 3 further comprises a drive steam inlet 3-1 and a condensate outlet 3-2; raw material liquid enters a heater 3 from a cold medium inlet 3-3 and exchanges heat with high-temperature steam entering the heater 3 from a driving steam inlet 3-1, condensed water generated after heat exchange of the high-temperature steam is discharged from a condensed water outlet 3-2, and the raw material liquid reaches the temperature required by flash evaporation of a 1 st-stage flash evaporator after heat exchange.
In another aspect of the embodiment of the present invention, there is provided a method for preparing hot purified water, which is prepared by the above-described hot purified water preparation apparatus.
In some embodiments, the feedstock solution is: sea water, river water, lake water, groundwater, sewage, wastewater or reclaimed water.
Example one
Referring to fig. 1, the present embodiment provides a flash evaporation type hydrothermal co-production hot purified water preparation apparatus, which is specifically applied to the fields of purified water preparation and central heating, so as to effectively improve the energy utilization rate and reduce the heating cost. The device comprises an N-stage flash evaporator 1(N is more than or equal to 2), an N-stage reflux pipeline, a heater 3 and a connecting pipeline.
Each stage of flash evaporator 1 comprises a raw material liquid heating zone 1-A, a concentrated solution flash evaporation zone 1-B and a purified water generation zone 1-C, the raw material liquid heating zone 1-A comprises a raw material liquid inlet 1-1 and a raw material liquid outlet 1-2, the concentrated solution flash evaporation zone 1-B comprises a concentrated solution inlet 1-3 and a concentrated solution outlet 1-4, the purified water generation zone 1-C comprises a purified water inlet 1-5 and a purified water outlet 1-6, each stage of reflux pipeline comprises a reflux pump 2, and the Nth stage of flash evaporator 1 only has a purified water outlet 1-6.
The raw material liquid heating zone 1-A is of a dividing wall type tube bundle structure and is positioned at the top of the flash evaporator 1; the concentrated solution flash evaporation area 1-B is of an open container structure and is positioned at the bottom of the flash evaporator 1; the purified water generation zone 1-C is an open container structure and is located between the raw material liquid heating zone and the concentrated liquid flash evaporation zone.
In the N-stage flash evaporator 1, a raw material liquid outlet 1-2 of an M-stage flash evaporator 1 is communicated with a raw material liquid inlet 1-1 of the M-1-stage flash evaporator 1, a concentrated liquid inlet 1-3 of the M-stage flash evaporator 1 is communicated with a concentrated liquid outlet 1-4 of the M-1-stage flash evaporator 1, a purified water outlet 1-6 of the M-stage flash evaporator 1 is communicated with a purified water inlet 1-5 of the M-1-stage flash evaporator 1, wherein N is more than or equal to M and is more than or equal to 2.
In the M-1 stage flash evaporator, the concentrated solution enters a concentrated solution flash evaporation zone 1-C from a concentrated solution inlet 1-3 for flash evaporation and concentration, and the heat required by flash evaporation is from enthalpy drop of the concentrated solution, so that the temperature of the concentrated solution is reduced; the steam generated by flash evaporation flows upwards and is divided into two parts, one part of steam enters the raw material liquid heating area 1-A, the raw material liquid flowing in from the raw material liquid inlet 1-1 is heated in a partition wall type heat exchange mode, meanwhile, the steam is condensed, the generated purified water falls into the purified water to generate 1-C, the other part of steam directly enters the purified water generating area 1-C, the steam exchanges heat with the existing lower-temperature purified water in the purified water generating area 1-C in a direct contact mode to generate new hot purified water, the condensation heat is released to heat the M-level purified water flowing in from the purified water inlet 1-5, and the two parts of purified water jointly form the purified water newly generated by the M-level flash evaporator 1 and is mixed with the M-level purified water.
Each stage of reflux pump 2 comprises a liquid pumping port and a liquid discharging port, the liquid pumping port of the Mth stage reflux pump 2 in the N stage reflux pump 2 is communicated with concentrated liquid outlets 1-4 of the Mth stage flash evaporator 1, and the liquid discharging port of the Mth stage reflux pump 2 is communicated with a raw material liquid outlet of the Mth stage flash evaporator 1.
The heater 3 comprises a driving steam inlet 3-1, a purified water outlet 3-2, a cold medium inlet 3-3 and a cold medium outlet 3-4, the driving steam inlet 3-1 is communicated with an external driving steam source, the purified water outlet 3-2 is communicated with a purified water direct discharge pipeline, the cold medium inlet 3-3 is communicated with a raw material liquid outlet 1-2 of the 1 st-stage flash evaporator, and the cold medium outlet 3-4 is communicated with a concentrated liquid inlet 1-3 of the 1 st-stage flash evaporator.
Raw material liquid enters the device from a raw material liquid inlet 1-1 of an Nth-stage flash evaporator 1, sequentially flows through a raw material liquid heating zone 1-A of a N, N-1 st-stage flash evaporator 1, … …, 2 st-stage flash evaporator 1 and a raw material liquid outlet 1-2 of the 1 st-stage flash evaporator 1, is further heated by a heater 3 and then enters a concentrated liquid flash evaporation zone 1-B of the 1 st-stage flash evaporator 1, and then sequentially flows through a concentrated liquid flash evaporation zone 1-B of the 1 st- stage flash evaporator 1, 2 nd, … …, N-1 st-stage flash evaporator 1 to be subjected to flash evaporation, is gradually cooled and concentrated, and finally flows out from a concentrated liquid outlet 1-4 of the Nth-stage flash evaporator 1 in a low-temperature and high-concentration state, part of the concentrated liquid is pumped by a multi-stage reflux pump 2, and the rest of the concentrated liquid is discharged from the device.
In the process of flowing the raw material liquid from the Nth-stage flash evaporator 1 to the heater 3, the Mth-stage reflux pump 2 pumps a part of the concentrated liquid from the concentrated liquid outlet 1-4 of the Mth-stage flash evaporator 1 to send to the raw material liquid pipeline, mixes with the raw material liquid flowing out of the raw material liquid outlet 1-2 of the Mth-stage flash evaporator 1, and enters the raw material liquid inlet 1-1 of the Mth-1-stage flash evaporator 1. The reflux pipeline has the function of improving the concentration rate of the whole device, and more purified water can be prepared under the condition of the same flow of raw material liquid; the advantage of dispersing reflux step by step is that the heat transfer temperature difference of each stage can be optimized, and finally the total heat transfer area of the whole device is reduced, so that the initial investment cost is reduced.
The purified water is sequentially heated by N, N-1, … …, 2 and 1-stage flash evaporators 1, newly generated purified water of each stage is received, and finally the purified water flows out of the device of the invention from purified water outlets 1-6 of the 1-stage flash evaporators 1.
Example two
Referring to fig. 2, in the embodiment, different from the embodiment that each flash evaporator 1 is provided with a first reflux pipeline, in the embodiment, each X stages of flash evaporators 1(N stages in total) are provided with a first reflux pipeline, so that N/X stages of reflux pipelines are totally shared, where N is a multiple of X.
An Nth/X-th stage reflux pipeline extracts partial concentrated solution from a concentrated solution outlet 1-4 of the Nth stage flash evaporator 1, mixes the partial concentrated solution with the raw material solution flowing out of a raw material solution outlet 1-2 of the Nth-X + 1-th stage flash evaporator 1, and enters a raw material solution inlet 1-1 of the Nth-X stage flash evaporator 1; and an N/X-1 stage return pipeline extracts partial concentrated solution from concentrated solution outlets 1-4 of the N-X stage flash evaporator 1, the partial concentrated solution is mixed with the raw material solution flowing out from raw material solution outlets 1-2 of the N-2X + 1 stage flash evaporator 1, the mixture enters a raw material solution inlet 1-1 … … of the N-2X stage flash evaporator 1, and the like, and finally, a 1 stage return pipeline extracts partial concentrated solution from concentrated solution outlets 1-4 of the X stage flash evaporator 1, the partial concentrated solution is mixed with the raw material solution flowing out from raw material solution outlets 1-2 of the 1 stage flash evaporator 1 and the mixture enters a cold medium inlet 3-3 of a heater 3.
The embodiment of the invention aims to protect a preparation device and a preparation method of hot purified water, and the preparation device has the following effects:
the device combines the preparation of purified water and centralized heat supply, heats the purified water while producing the purified water, conveys the hot purified water to a heat user by utilizing a heat supply pipe network, and finally conveys the cooled purified water to a tap water plant for further purification, thereby realizing the simultaneous production and the simultaneous delivery of heat and the purified water; in the process of preparing the purified water, the heat of the driving steam is fully utilized for heating the purified water and is rarely wasted as a heat source for the operation of the driving device, and compared with a common water production per unit device, the device has higher energy utilization efficiency, thereby effectively reducing the operation cost.
In addition, the device reasonably controls the concentration degree of the concentrated solution by arranging the return pipeline, and selectively returns the concentrated solution to the raw material solution for heating and flash evaporation again when the concentration of the concentrated solution is unqualified, so that the desalination degree of the raw material solution and the generation rate of hot purified water are improved.
It is to be understood that the above-described embodiments of the present invention are merely illustrative of or explaining the principles of the invention and are not to be construed as limiting the invention. Therefore, any modification, equivalent replacement, improvement and the like made without departing from the spirit and scope of the present invention should be included in the protection scope of the present invention. Further, it is intended that the appended claims cover all such variations and modifications as fall within the scope and boundaries of the appended claims or the equivalents of such scope and boundaries.
Claims (9)
1. A device for preparing hot purified water, comprising:
the device comprises N stages of flash evaporators (1), wherein each stage of flash evaporator (1) comprises a raw material liquid heating zone (1-A) and a concentrated liquid flash evaporation zone (1-B), the raw material liquid heating zone (1-A) is provided with a raw material liquid inlet (1-1) and a raw material liquid outlet (1-2), and the concentrated liquid flash evaporation zone (1-B) is provided with a concentrated liquid inlet (1-3) and a concentrated liquid outlet (1-4);
k-grade backflow pipelines, wherein each grade of backflow pipeline comprises a backflow liquid inlet (2-1) and a backflow liquid outlet (2-2), the backflow liquid inlet (2-1) of the J-grade backflow pipeline in the K-grade backflow pipeline is communicated with the concentrated liquid outlet (1-4) of the P-grade flash evaporator (1) in the N-grade flash evaporator (1), the backflow liquid outlet (2-2) of the J-grade backflow pipeline is communicated with the raw material liquid inlet (1-1) of the Q-grade flash evaporator (1) in the N-grade flash evaporator (1), N is more than or equal to 2, K is more than or equal to J is more than or equal to 1, and N is more than or equal to P is more than or equal to Q;
the heater (3) comprises a cold medium inlet (3-3) and a cold medium outlet (3-4), the heater (3) is used for heating the raw material liquid to the temperature required by the flash evaporation of the 1 st-stage flash evaporator, the cold medium inlet (3-3) of the heater (3) is communicated with the raw material liquid outlet (1-2) of the 1 st-stage flash evaporator (1) in the N-stage flash evaporators (1), and the cold medium outlet (3-4) of the heater (3) is communicated with the concentrated liquid inlet (1-3) of the 1 st-stage flash evaporator (1) in the N-stage flash evaporators (1).
2. The apparatus of claim 1,
a concentrated solution inlet (1-3) of an Mth-stage flash evaporator (1) in the N-stage flash evaporator (1) is communicated with a concentrated solution outlet (1-4) of the Mth-1-stage flash evaporator (1), and a raw material solution outlet (1-2) of the Mth-stage flash evaporator (1) is communicated with a raw material solution inlet (1-1) of the Mth-1-stage flash evaporator (1);
a concentrated solution outlet (1-4) of an Nth stage flash evaporator (1) in the N-stage flash evaporator (1) is used for discharging concentrated solution, and a raw material solution inlet (1-1) of the Nth stage flash evaporator (1) in the N-stage flash evaporator (1) is used for introducing raw material solution;
wherein N is more than or equal to M and more than or equal to 2.
3. The apparatus of claim 1,
the raw material liquid heating zone (1-A) of each stage of the N-stage flash evaporator (1) is of a dividing wall type structure and is positioned at the top of the flash evaporator (1);
part of steam generated by flash evaporation in the concentrated solution flash evaporation zone (1-B) is condensed in the raw material solution heating zone (1-A), condensation heat is released, the raw material solution is heated through the heat exchange wall, and meanwhile, the steam is condensed to generate pure water.
4. The apparatus of claim 1,
each stage of flash evaporator (1) in the N stages of flash evaporators (1) also comprises a purified water generation area (1-C), and the purified water generation area (1-C) comprises a purified water inlet (1-5) and a purified water outlet (1-6);
a purified water outlet (1-6) of a G-stage flash evaporator (1) in the N-stage flash evaporator (1) is communicated with a purified water inlet (1-5) of the G-1-stage flash evaporator (1);
wherein N is more than or equal to G and more than or equal to 2.
5. The apparatus of claim 4,
the purified water generation zone (1-C) of each stage of the N-stage flash evaporators (1) is of an open container structure, and the purified water generation zone (1-C) is positioned between the concentrated solution flash evaporation zone (1-B) and the raw material solution heating zone (1-A);
the purified water generation zone (1-C) receives purified water generated by condensation of steam flashed by the concentrated solution flash evaporation zone (1-B).
6. The apparatus of claim 1,
each stage of return pipelines in the K stages of return pipelines comprises: a reflux pump (2) and a connecting pipe;
the liquid extraction port of the reflux pump (2) of the J-level reflux pipeline in the K-level reflux pipeline is communicated with the concentrated liquid outlet (1-4) of the P-level flash evaporator (1) in the N-level flash evaporator (1) through the connecting pipe, and the liquid discharge port of the reflux pump (2) of the J-level reflux pipeline is communicated with the raw material liquid inlet (1-1) of the Q-level flash evaporator (1) in the N-level flash evaporator (1) through the connecting pipe.
7. The apparatus of claim 1,
the heater (3) further comprises a driving steam inlet (3-1) and a condensed water outlet (3-2);
raw material liquid enters the heater (3) from the cold medium inlet (3-3) and exchanges heat with high-temperature steam entering the heater (3) from the driving steam inlet (3-1), condensed water generated after heat exchange of the high-temperature steam is discharged from the condensed water outlet (3-2), and the raw material liquid reaches the temperature required by flash evaporation of the 1 st-stage flash evaporator after heat exchange.
8. A method for preparing hot purified water, characterized in that the hot purified water is prepared by the hot purified water preparing apparatus of any one of claims 1 to 8.
9. The production method according to claim 8,
the raw material liquid is as follows: sea water, river water, lake water, groundwater, sewage, wastewater or reclaimed water.
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| CN202010797119.1A Active CN112010380B (en) | 2020-06-19 | 2020-08-10 | Preparation device and preparation method of hot purified water |
| CN202010797933.3A Active CN112047432B (en) | 2020-06-19 | 2020-08-10 | Hot and fresh water preparation device and method and heat supply pipe network |
| CN202021662872.1U Active CN212269518U (en) | 2020-06-19 | 2020-08-11 | Device for preparing hot distilled water by multistage flash evaporation |
| CN202010803250.4A Pending CN112010381A (en) | 2020-06-19 | 2020-08-11 | Device and method for preparing hot distilled water through multistage flash evaporation |
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| CN113149113A (en) * | 2021-04-25 | 2021-07-23 | 清华大学 | Vertical multistage flash evaporation device for realizing hydrothermal coproduction |
| CN115507404B (en) * | 2022-09-28 | 2024-04-26 | 清华大学 | Cross-season water-saving heat-combined storage and supply system and method |
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| CN112010381A (en) | 2020-12-01 |
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| CN212269518U (en) | 2021-01-01 |
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