CN207566923U - Saline-water reclamation and the integration apparatus for preparing dry saturated steam - Google Patents
Saline-water reclamation and the integration apparatus for preparing dry saturated steam Download PDFInfo
- Publication number
- CN207566923U CN207566923U CN201721589067.9U CN201721589067U CN207566923U CN 207566923 U CN207566923 U CN 207566923U CN 201721589067 U CN201721589067 U CN 201721589067U CN 207566923 U CN207566923 U CN 207566923U
- Authority
- CN
- China
- Prior art keywords
- module
- steam
- heat
- heat storage
- enters
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 126
- 229920006395 saturated elastomer Polymers 0.000 title abstract description 7
- 230000010354 integration Effects 0.000 title abstract description 5
- 239000007788 liquid Substances 0.000 claims abstract description 60
- 239000008213 purified water Substances 0.000 claims abstract description 51
- 239000012267 brine Substances 0.000 claims abstract description 46
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 46
- 238000010612 desalination reaction Methods 0.000 claims abstract description 43
- 238000003860 storage Methods 0.000 claims abstract description 43
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000005338 heat storage Methods 0.000 claims description 114
- 238000011033 desalting Methods 0.000 claims description 15
- 239000000243 solution Substances 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 9
- 238000012546 transfer Methods 0.000 claims description 8
- 230000000694 effects Effects 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims 2
- 239000011780 sodium chloride Substances 0.000 claims 2
- 238000010521 absorption reaction Methods 0.000 abstract description 2
- 239000012141 concentrate Substances 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract 2
- 238000000034 method Methods 0.000 description 11
- 238000002360 preparation method Methods 0.000 description 10
- 239000012266 salt solution Substances 0.000 description 10
- 238000011084 recovery Methods 0.000 description 9
- 239000013505 freshwater Substances 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 6
- 239000003921 oil Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 239000002803 fossil fuel Substances 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000013535 sea water Substances 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- AZFNGPAYDKGCRB-XCPIVNJJSA-M [(1s,2s)-2-amino-1,2-diphenylethyl]-(4-methylphenyl)sulfonylazanide;chlororuthenium(1+);1-methyl-4-propan-2-ylbenzene Chemical compound [Ru+]Cl.CC(C)C1=CC=C(C)C=C1.C1=CC(C)=CC=C1S(=O)(=O)[N-][C@@H](C=1C=CC=CC=1)[C@@H](N)C1=CC=CC=C1 AZFNGPAYDKGCRB-XCPIVNJJSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000004304 potassium nitrite Substances 0.000 description 1
- 235000010289 potassium nitrite Nutrition 0.000 description 1
- 238000000079 presaturation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 235000010288 sodium nitrite Nutrition 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
-
- 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
- Y02A20/138—Water desalination using renewable energy
- Y02A20/142—Solar thermal; Photovoltaics
-
- 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
- Y02A20/20—Controlling water pollution; Waste water treatment
- Y02A20/208—Off-grid powered water treatment
- Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model provides a kind of saline-water reclamation and prepares the integration apparatus of dry saturated steam, including solar thermal collection system, heat reservoir, dry saturated steam generating system, desalination system and purification water storage systems.Solar thermal collection system is collected the thermal energy of sunlight and is stored to heat reservoir.Dry saturated steam generating system includes steam module and gas-liquid separation module；Purified water in purification water storage systems enters after steam module with heat reservoir heat exchange and being vaporizated into moist steam；Moist steam enters gas-liquid separation module and is separated into liquid water and dry saturated steam.Desalination system includes flash column, power plant module, evaporator and condenser；The liquid water that gas-liquid separation module is isolated enters flash column and generates high steam, and high steam enters power plant module；Heat absorption evaporates and isolates indirect steam and concentrate after brine enters evaporator, and a part of indirect steam enters condenser and is condensed into liquid water and stores to water storage systems are purified, and another part indirect steam enters power plant module.
Description
Technical Field
The utility model relates to a salt solution desalination field especially relates to a salt solution desalination and integrated equipment of preparation dry steam.
Background
At present, many industrial parks are opened up in deserts and gobi areas in northwest China, and a large number of high and new technology enterprises are introduced to be resident in the deserts and the gobi areas, and most of the enterprises carry out deep processing treatment on local petroleum, natural gas, coal and other petrochemical resources so as to form clean and environment-friendly products. The outstanding characteristics of such enterprises are that the process requires a large amount of fresh water and steam resources, and at the same time, a large amount of high-salinity and high-hardness industrial wastewater containing other organic impurities may be produced. Considering that most desert and gobi areas belong to arid water-deficient areas, surface water flow which flows all the year round does not exist in the areas, spring points do not appear, underground fresh water can not be collected within 200m of the surrounding shallow layer, and a large amount of high-salinity and high-hardness brackish water in the underground deep layer cannot be directly utilized. Therefore, the lack of fresh water resources becomes a bottleneck for restricting the production of enterprises. The deep impurity removal, desalination and desalination treatment of the underground brackish water or the industrial wastewater can provide partial steam for enterprises, relieve the current situation of clear water shortage, reduce public water supply pressure, solve the problem of the outgoing of the waste water rich in surplus and high salt, and ensure the clean and green sustainable development of the enterprise production.
At present, heat energy generated by burning fossil fuel or electric energy of a power grid is mostly adopted in a treatment process for realizing the reclamation of brackish water or the desalination of sea water in remote areas, but the use of the process is limited due to high fuel cost or electric power cost and the like.
In addition, the current common method for producing high pressure steam on site is to use conventional boilers based on fossil fuel combustion (coal, oil, natural gas). This not only consumes fossil fuels and incurs a certain economic cost, but also brings about serious environmental pollution hazards. Even if the electric energy is considered, the evaporation treatment is only suitable for occasions with surplus electric power resources and low electricity price, and the high electricity consumption cost is not paid for occasions with high electricity price. With the coming of the new revised national standard of emission standard of atmospheric pollutants for boilers (GB13271-2014), the direct emission of the tail gas of the coal-fired and oil-fired boilers cannot reach the standard, so that the search for low-cost and clean energy becomes an important development direction for preparing industrial steam.
SUMMERY OF THE UTILITY MODEL
In view of the problems in the prior art, the present invention is directed to an integrated apparatus for desalinating brine and preparing dry steam,
in order to achieve the above object, the present invention provides an integrated device for desalinating brine and preparing dry steam, which comprises a solar heat collecting system, a heat storage system, a dry steam generating system, a desalination system and a purified water storage system.
The solar heat collection system collects heat energy of sunlight and stores the heat energy to the heat storage system through heat exchange. The dry steam generation system comprises a steam module and a gas-liquid separation module; purified water in the purified water storage system enters the steam module and exchanges heat with the heat storage system, and is vaporized into wet steam; the wet steam enters the gas-liquid separation module and is separated into liquid water and dry steam.
The desalination system comprises a flash tower, a power module, an evaporator and a condenser; the liquid water separated by the gas-liquid separation module enters a flash tower and generates high-pressure steam, and the high-pressure steam enters a power module; the brine to be desalted enters an evaporator to absorb heat and evaporate, secondary steam and concentrated solution are separated out, a part of the secondary steam enters a condenser to be condensed into liquid water and is stored in a purified water storage system, the other part of the secondary steam enters a power module, and the concentrated solution is discharged out of the desalting system; and the high-pressure steam entering the power module heats and pressurizes the other part of secondary steam, and the heated and pressurized other part of secondary steam enters the evaporator and is heated to enter the brine of the evaporator, and then is condensed into liquid water and is stored in the purified water storage system.
The utility model has the advantages as follows:
the utility model discloses an integration equipment of salt solution desalination and preparation dry steam adopts solar energy as clean energy, and pollutant discharge is little, and the system running cost is low, has higher economic benefits and environmental protection benefit. Because the solar heat collection system and the heat storage system are independent, the heat energy collected by the solar heat collection system can be freely stored and released; at night, the heat storage system can provide heat required by equipment operation even if the solar heat collection system cannot work.
The dry steam prepared by the dry steam generating system can be directly used by users, and the separated liquid water can enter the desalting system for reuse, so that the high-efficiency utilization of energy is realized, and the energy consumption cost of steam generation and brine desalination is reduced.
Additionally, the utility model discloses an integrated equipment of salt solution desalination and preparation dry steam is integrated as an organic whole with salt solution desalination technology and steam generation technology to simplify process flow, shortened process equipment, reduce the energy consumption, whole more compact, easily control and maintenance.
In a word, the integrated equipment for desalting salt water and preparing dry steam can be suitable for treating high-salinity and high-hardness salt water such as underground brackish water desalting, seawater desalting, boiler blow-off water, oil and gas field sewage recovery and the like, and has wide adaptability; the utility model integrates the brine desalination and the high-pressure high-dryness steam preparation, and has simple and reliable process and easy realization; the utility model discloses the waste heat of the liquid water that make full use of gas-liquid separation module separates, the energy efficiency ratio is higher. Additionally, the utility model discloses make full use of clean energy realizes salt solution desalination and preparation high pressure dry steam, realizes fresh water resources regeneration, has reduced fossil fuel consumption and three wastes and has discharged, has reduced environmental pollution, has improved the energy efficiency, has reduced the running cost, has practiced thrift natural fresh water resources allocation and transportation and consumption.
Drawings
Fig. 1 is a schematic view of an embodiment of an integrated apparatus for desalinating brine and preparing dry steam according to the present invention.
Fig. 2 is a schematic view of another embodiment of an integrated brine desalination and dry steam production plant according to the present invention.
Wherein the reference numerals are as follows:
1 solar energy collection system 44 supercharger
11 solar heat collection module 5 desalination system
12 heat collection working medium 51 flash tower
13-heat-collecting working medium flow module 52 power module
14 heat collection working medium heat exchange module 521 ejector
2 heat storage system 522 steam turbine
21 heat storage medium 523 compressor
22 heat storage medium flow module 53 evaporator
23 high temperature heat storage module 54 condenser
24 low temperature heat storage module 55 blender
25 heater 56 vacuum pump
3 dry steam generating System A Dry steam
31 steam module B noncondensable gas
311 preheater C brine
312 steam generator D concentrate
32 gas-liquid separation module E pipeline
4 purified water storage system F valve
G1 working medium booster pump for 41 purified water storage tank
42 softener G2 recovery pump
43 oxygen remover G3 circulating pump
Detailed Description
The integrated equipment for desalinating brine and preparing dry steam according to the present invention will be described in detail with reference to the accompanying drawings.
Referring to fig. 1 and 2, the integrated equipment for desalinating brine and preparing dry steam according to the present invention includes a solar heat collecting system 1, a heat storage system 2, a dry steam generating system 3, a desalination system 5, and a purified water storage system 4.
The solar heat collecting system 1 collects heat energy of sunlight and stores the heat energy to the heat storage system 2 through heat exchange. The dry steam generation system 3 comprises a steam module 31 and a gas-liquid separation module 32; purified water in the purified water storage system 4 enters the steam module 31 and then exchanges heat with the heat storage system 2, and is vaporized into wet steam (the wet steam is a mixture of liquid water and gaseous water); the wet steam enters the gas-liquid separation module 32 and is separated into liquid water and dry steam a (gaseous water).
The desalination system 5 comprises a flash tower 51, a power module 52, an evaporator 53 and a condenser 54; the liquid water separated by the gas-liquid separation module 32 enters a flash tower 51 and generates high-pressure steam, and the high-pressure steam enters a power module 52; brine C (such as underground brackish water, seawater, oil and gas field sewage, boiler blow-off water and other high-salinity and high-hardness brackish water) to be desalinated enters the evaporator 53 to absorb heat and evaporate, secondary steam and concentrated solution D are separated out, a part of the secondary steam enters the condenser 54 to be condensed into liquid water and stored in the purified water storage system 4, the other part of the secondary steam enters the power module 52, and the concentrated solution D is discharged out of the desalination system 5; the high-pressure steam entering the power module 52 heats and pressurizes the other part of the secondary steam, and the heated and pressurized other part of the secondary steam enters the evaporator 53 and is heated and enters the brine C of the evaporator 53, and is further condensed into liquid water and stored in the purified water storage system 4.
The utility model discloses an integration equipment of salt solution desalination and preparation dry steam adopts solar energy as clean energy, and pollutant discharge is little, and the system running cost is low, has higher economic benefits and environmental protection benefit. Because the solar heat collection system 1 and the heat storage system 2 are independent, the heat energy collected by the solar heat collection system 1 can be freely stored and released; at night, the heat storage system 2 can provide heat required for the operation of the apparatus even if the solar heat collecting system 1 is not operated.
The dry steam A prepared by the dry steam generating system 3 can be directly used by users, and the separated liquid water can enter the desalting system 5 for reuse, so that the high-efficiency utilization of energy is realized, and the energy consumption cost of steam generation and brine desalting is reduced.
Additionally, the utility model discloses an integrated equipment of salt solution desalination and preparation dry steam is integrated as an organic whole with salt solution desalination technology and steam generation technology to simplify process flow, shortened process equipment, reduce the energy consumption, whole more compact, easily control and maintenance.
In a word, the integrated equipment for desalting salt water and preparing dry steam can be suitable for treating high-salinity and high-hardness salt water such as underground brackish water desalting, seawater desalting, boiler blow-off water, oil and gas field sewage recovery and the like, and has wide adaptability; the utility model integrates the brine desalination and the high-pressure high-dryness steam preparation, and has simple and reliable process and easy realization; the utility model discloses the waste heat of the liquid water that make full use of gas-liquid separation module 32 separated, the energy efficiency ratio is higher. Additionally, the utility model discloses make full use of clean energy realizes salt solution desalination and preparation high pressure dry steam, realizes fresh water resources regeneration, has reduced fossil fuel consumption and three wastes and has discharged, has reduced environmental pollution, has improved the energy efficiency, has reduced the running cost, has practiced thrift natural fresh water resources allocation and transportation and consumption.
The concentrated solution D separated by the evaporator 53 can be evaporated to dryness on site, thereby avoiding waste liquid discharge.
Referring to fig. 1 and 2, the solar heat collecting system 1 includes a solar heat collecting module 11, a heat collecting working medium 12, a heat collecting working medium flowing module 13, and a heat collecting working medium heat exchanging module 14. The heat collecting working medium flowing module 13 is connected with the solar heat collecting module 11 and the heat collecting working medium heat exchanging module 14, and guides the heat collecting working medium 12 to circularly flow between the solar heat collecting module 11 and the heat collecting working medium heat exchanging module 14. The solar heat collection module 11 collects heat energy of sunlight and transmits the heat energy to the heat collection working medium 12, and the heat collection working medium 12 transmits the heat energy to the heat collection working medium heat exchange module 14; the heat collection working medium heat exchange module 14 is connected with the heat storage system 2 and transfers heat energy to the heat storage system 2.
The solar heat collection module 11 may be a trough heat collection array, a tower heat collection array, or a linear fresnel heat collection array. The heat collection working medium 12 can be heat conduction oil, the heat conduction oil has good heat transfer performance, fluidity and low volatility in a wide temperature range, equipment and a pipeline system are not easy to block or corrode, high-temperature heat collected by the solar heat collection module 11 can be effectively absorbed, and the high-temperature heat is transferred to the heat storage system 2. The heat collecting working medium flow module 13 may include a working medium booster pump G1, a transmission pipeline E, a valve, and the like, and mainly aims to regulate and control the circulation flow of the heat collecting working medium 12. The heat collecting working medium heat exchange module 14 mainly comprises a heat collecting working medium heat absorbing device (such as a vacuum tube) and a heat supply heat exchanger device, and aims to realize the absorption and transmission of solar heat.
The heat collection working medium 12 pressurized by the working medium booster pump G1 enters the solar heat collection module 11, the temperature of the heat collection working medium 12 rises after absorbing solar light heat, the heat collection working medium 12 with high temperature enters the heat supply heat exchanger and transfers heat energy to the heat storage medium 21, the temperature is reduced and the heat collection working medium enters the working medium booster pump G1 again, and therefore solar light heat is continuously absorbed and transferred. The working medium booster pump G1 is preferably arranged at the downstream of the heat collection working medium heat exchange module 14, so that the pump body can be prevented from being damaged by the high-temperature heat collection working medium 12, the service life of the working medium booster pump G1 is prolonged, and the operation stability of the system is improved.
Referring to fig. 1 and 2, the heat storage system 2 includes a heat storage medium 21, a heat storage medium flow module 22, a high temperature heat storage module 23, and a low temperature heat storage module 24. The heat storage medium flowing module 22 is sequentially connected with the solar heat collection system 1, the high-temperature heat storage module 23, the steam module 31 of the dry steam generation system 3 and the low-temperature heat storage module 24, and controls the flow of the heat storage medium 21 among the solar heat collection system 1, the high-temperature heat storage module 23, the steam module 31 of the dry steam generation system 3 and the low-temperature heat storage module 24. The heat storage medium 21 is heated after passing through the solar heat collection system 1 to form a high-temperature heat storage medium 21, and the high-temperature heat storage medium 21 is stored in a high-temperature heat storage module 23; the high-temperature heat storage medium 21 in the high-temperature heat storage module 23 enters the steam module 31 of the dry steam generation system 3 to be cooled and form a low-temperature heat storage medium 21, and the low-temperature heat storage medium 21 is stored in the low-temperature heat storage module 24; the low-temperature heat storage medium 21 in the low-temperature heat storage module 24 reenters the solar heat collection system 1 to absorb heat and raise the temperature.
The heat storage medium 21 is mainly binary molten salt such as sodium nitrite and potassium nitrite, and the binary molten salt has low price, large heat capacity per unit volume, good heat conductivity, low viscosity and good flow heat transfer performance at high temperature, and is suitable for storing and releasing high-temperature heat. The heat storage medium flowing module 22 mainly includes a pipe E for transporting the heat storage medium 21, a valve F, a recovery pump G2, and a circulation pump G3, thereby ensuring that the heat storage medium 21 smoothly flows. The high temperature heat storage module 23 includes a high temperature storage tank, and traps and stores the heat storage medium 21 carrying thermal energy, and releases only a small amount of the heat storage medium 21 to maintain the normal operation of the system. The low-temperature heat storage module 24 includes a low-temperature storage tank, which can buffer the low-temperature heat storage medium 21 after releasing heat energy for recycling of the system.
The heat storage medium 21 in the low-temperature storage tank enters the heat collection working medium heat exchange module 14 after being pressurized by the circulating pump G3, the heat storage medium 21 is heated by the high-temperature heat collection working medium 12 and then is heated, and the heated high-temperature heat storage medium 21 flows into the high-temperature storage tank; most of the high-temperature heat storage medium 21 is stored in the high-temperature storage tank, only a small part of the heat storage medium 21 is output and flows through the steam module 31 (sequentially flows through a steam generator 312 and a preheater 311 which are described later), and the temperature is reduced after heat is released; the low-temperature heat storage medium 21 after the heat energy is released is pressurized by a recovery pump G2 and then flows back to the low-temperature storage tank for caching; the solar photo-thermal energy is received and released in such a continuous cycle manner. The recovery pump G2 and the circulating pump G3 are arranged at the downstream of the steam module 31, so that the heat storage medium 21 in a high-temperature state can be prevented from damaging the pump body, the service lives of the recovery pump G2 and the circulating pump G3 are prolonged, and the stability of system operation is improved.
Referring to fig. 1 and 2, a heater 25 is further disposed in the high-temperature heat storage module 23 and the low-temperature heat storage module 24. When the utility model discloses the brine desalination does not use for a long time with the integration equipment of preparation dry steam, and heat-retaining medium 21 can condense and can't flow, at this moment, heats up in order to improve mobility, improve equipment security and adaptability through heat-retaining medium 21 in heater 25 to high temperature heat-retaining module 23 and the low temperature heat-retaining module 24.
Referring to fig. 1 and 2, the steam module 31 includes a preheater 311 and a steam generator 312. The purified water in the purified water storage system 4 firstly enters the preheater 311 and then enters the steam generator 312; the heat storage medium flowing module 22 is connected to the high temperature heat storage module 23, the steam generator 312, the preheater 311, and the low temperature heat storage module 24 in sequence (that is, the heat storage medium 21 in the high temperature heat storage module 23 flows through the steam generator 312 and the preheater 311 in sequence and then enters the low temperature heat storage module 24).
The preheater 311 is capable of heating the purified water supplied from the purified water storage system 4 to a pre-saturated state and feeding it to the steam generator 312. The steam generator 312 heats and vaporizes the saturated water sent by the preheater 311, and enters the gas-liquid separation module 32 (the gas-liquid separation module 32 may be a high-pressure gas-liquid separator) after reaching a certain humidity; the gas-liquid separation module 32 performs gas-liquid separation on the high-pressure wet steam, so as to prepare high-dryness steam (namely dry steam A). The heat storage medium 21 is discharged and cooled in the steam generator 312 and then enters the preheater 311, and the purified water in the preheater 311 is heated to a pre-saturation state by using the waste heat of the heat storage medium 21; the pre-saturated purified water enters the steam generator 312, is heated and boiled highly by the high-temperature heat storage medium 21, enters the gas-liquid separation module 32 after reaching a certain humidity, is subjected to steam-water separation, and the separated dry steam A is output to the outside of the system as a product for a user to use. The remaining high pressure liquid water at the bottom of the separator is then fed to the flash column 51 of the desalination system 5.
Referring to fig. 1 and 2, the purified water storage system 4 includes a purified water storage tank 41, a softener 42, an deaerator 43, and a pressurizer 44 connected in this order, and the pressurizer 44 is connected to the steam module 31.
The softener 42 can adopt anion and cation exchange resin, and mainly aims to remove residual calcium and magnesium ions in purified water and prevent scaling of subsequent heat exchange equipment. The deaerator 43 may be deaerated by a vacuum thermal process, in order to remove residual oxygen, carbon dioxide and other gases in the water and prevent oxygen corrosion and acid corrosion in the heat exchange equipment. The pressurizer 44 mainly includes a water feed pump (not shown) and a water feed pump, wherein the water feed pump mainly takes water from the purified water storage tank 41, and the water feed pump mainly adopts a plunger pump, and aims to pressurize the purified water, overcome the pipe resistance and realize high-pressure steam generation.
The water feeding pump (not shown) pumps a certain flow of purified water from the purified water storage tank 41, and after the purified water is softened by the softener 42 and is deoxygenated by the deoxygenator 43, the purified water enters the water feeding pump of the pressurizer 44 for pressurization, so that sufficient power is provided for the flow heat exchange of the subsequent purified water.
Referring to fig. 1 and 2, the desalination system 5 further comprises a blender 55 connected to the flash tower 51 and the evaporator 53, and the brine C to be desalinated enters the blender 55; the flash column 51 produces high pressure steam leaving liquid water to enter the blender 55 and mix with the brine C entering the blender 55, and the mixed brine C enters the evaporator 53.
In addition, the desalination system 5 may further include a vacuum pump 56 connected to the condenser 54, and the vacuum pump 56 draws the non-condensable gas B (e.g., oxygen, carbon dioxide, etc.) in the condenser 54 and maintains a vacuum level in the shell side of the evaporator 53.
The flash tower 51 is used for flashing the liquid water separated by the gas-liquid separation module 32 again to generate high-pressure steam, and the high-pressure steam enters the power module 52 and serves as a power source of the power module 52. The blender 55 is used to mix the high temperature liquid water left by the flash tower 51 with the high concentration brine C sufficiently to dilute the concentration of the brine C and increase the temperature of the brine C entering the evaporator 53, reducing the consumption of heat source in the evaporator 53. The purpose of the evaporator 53 and condenser 54 is to evaporate the brine C, produce secondary steam and condense it down to form purified water. The vacuum pump 56 discharges the non-condensable gas not condensed in the condenser 54 into the atmosphere, and maintains the vacuum degree of the shell side of the evaporator 53.
The high-pressure liquid water separated by the gas-liquid separation module 32 enters a flash tower 51 for flash evaporation to generate a certain amount of steam with a certain pressure, the residual flash bottom water (namely the high-temperature liquid water left by the flash evaporation) enters a blender 55 and is mixed with the brine C, and the mixed brine C enters an evaporator 53 for evaporation and desalination; evaporating and desalting the brine C to generate secondary steam and a concentrated solution D; a part of the secondary steam enters the condenser 54 to be condensed into liquid water and is stored in the purified water storage system 4, the other part of the secondary steam enters the power module 52, and the concentrated solution D is discharged out of the desalination system 5; the flash steam entering the power module 52 heats and pressurizes the other part of the secondary steam, and the heated and pressurized other part of the secondary steam enters the evaporator 53 and is heated and enters the brine C of the evaporator 53, and is further condensed into liquid water and stored in the purified water storage system 4.
The purpose of the power module 52 is to recover the pressure energy of the secondary steam generated by the evaporator 53 using the pressure energy of the high-pressure steam generated by the flash column 51 and to generate steam having a certain temperature and pressure as a heat source for the evaporator.
The power module 52 may employ different drive configurations. For example, referring to fig. 1, the power module 52 includes an ejector 521, and the high-pressure steam generated by the flash tower 51 enters the ejector 521 to eject the other part of the secondary steam, so as to heat and pressurize the other part of the secondary steam. Alternatively, referring to fig. 2, the power module 52 includes a steam turbine 522 and a compressor 523 (e.g., mechanical compressor), the steam turbine 522 being connected to the flash column 51, the compressor 523 and the purified water storage system 4, respectively; the other part of the secondary steam enters a compressor; the high pressure steam generated by the flash column 51 pushes the steam turbine 522 and is condensed into liquid water, which is stored in the purified water storage system 4; the steam turbine 522 transfers power to the compressor, which heats and pressurizes the other portion of the secondary steam. The steam turbine 522 is a full-flow turbine, and the outlet of the full-flow turbine is connected to the inlet of the purified water storage tank 41. The steam turbine 522 is connected with the compressor 523 by a gearbox to realize power transmission. The steam turbine 522 and the compressor 523 are for directly converting kinetic energy of the flash steam into mechanical energy and mechanically compressing the secondary steam, thereby increasing pressure and temperature of the secondary steam, and further, are used as a heat source of the evaporator 53.
Referring to fig. 1 and 2, the evaporator 53 may be a multiple-effect evaporator.
The mode of operation of the preferred embodiment of the integrated brine desalination and dry steam generation apparatus of the present invention is described in detail below.
During the day, the solar energy collection system 1 operates normally. The working medium booster pump G1 boosts the low-temperature heat collection working medium 12 and then sends the boosted low-temperature heat collection working medium 12 into the solar heat collection module 11 to absorb solar energy, the temperature of the low-temperature heat collection working medium 12 rises to a certain temperature and leaves the solar heat collection module 11, then the high-temperature heat collection working medium 12 enters the heat collection working medium heat exchange module 14 to transfer heat to the low-temperature heat storage medium 21, the temperature is reduced, and the low-temperature heat collection working medium 12 flows back to the working medium booster. This cycle is repeated to transmit solar energy to the heat storage medium 21.
The heat storage medium 21 absorbing the heat of the heat collecting working medium 12 flows into the high temperature heat storage module 23 by its own excess pressure and is stored. Under the pumping action of the recovery pump G2, a certain flow rate of the high temperature heat storage medium 21 flows out of the high temperature heat storage module 23 and sequentially enters the steam generator 312 and the preheater 311, thereby releasing heat to the purified water. The temperature of the heat storage medium 21 releasing heat is reduced, the heat storage medium flows back to the low-temperature heat storage module 24 under the action of the recovery pump G2, the valve F is opened, the circulating pump G3 pumps the heat storage medium 21 with a certain flow rate and enters the heat collection working medium heat exchange module 14 to receive the heat of the heat collection working medium 12, and the process is repeated.
The purified water absorbs the heat of the heat storage medium 21 and turns into wet steam, and the wet steam is subjected to steam-water separation in the gas-liquid separation module 32, and dry steam is separated and supplied to a user. The bottom water (separated liquid water) of the gas-liquid separation module 32 is flashed by the flash tower 51 to generate steam with a certain pressure, and the steam enters the ejector 521 and ejects part of the secondary steam evaporated by the evaporator 53 to generate medium-pressure steam. The medium pressure steam, which enters the evaporator 53 and serves as a heating source of the evaporator 53, i.e., heats the brine C to evaporate, condenses itself and returns to the purified water storage tank 41.
The evaporator 53 can be set to multiple effects, the secondary steam of the previous effect and the decompressed brine C enter the next effect respectively, evaporation and concentration are carried out again, and the concentrated solution D of the tail effect is discharged out of the system. The secondary steam generated by the tail effect is divided into two streams, one stream enters the condenser 54 to be condensed into liquid water and is stored in the purified water storage tank 41, and the other stream of low-pressure secondary steam is sucked into the ejector 521 to be recycled. The condensed water in the condenser 54 and the evaporator 53 is totally returned to the purified water storage tank 41 for storage, and part of the purified water enters the preheater 311 and the steam generator 312 for heating and generating high-pressure steam after being softened by the softener 42, deoxygenated by the deoxygenator 43 and pressurized by the pressurizer 44.
At night or on a rainy day, the solar heat collecting system 1 stops operating. Closing the valve F, and cutting off the communication between the low-temperature heat storage module 24 and the heat collection working medium heat exchange module; the high temperature heat storage medium 21 stored in the high temperature heat storage module 23 continues to increase the heat required by the apparatus. The utility model discloses a valve F can realize daytime and night heat-retaining and the switching of exothermic mode, easy operation, convenient and fast.
Claims (10)
1. An integrated device for desalting brine and preparing dry steam is characterized by comprising a solar heat collection system (1), a heat storage system (2), a dry steam generation system (3), a desalting system (5) and a purified water storage system (4);
the solar heat collection system (1) collects the heat energy of the sunlight and stores the heat energy to the heat storage system (2) through heat exchange;
the dry steam generation system (3) comprises a steam module (31) and a gas-liquid separation module (32); purified water in the purified water storage system (4) enters the steam module (31) and exchanges heat with the heat storage system (2) and is vaporized into wet steam; wet steam enters a gas-liquid separation module (32) and is separated into liquid water and dry steam (A);
the desalination system (5) comprises a flash tower (51), a power module (52), an evaporator (53) and a condenser (54); the liquid water separated by the gas-liquid separation module (32) enters a flash tower (51) and generates high-pressure steam, and the high-pressure steam enters a power module (52); after entering an evaporator (53), brine (C) to be desalted absorbs heat and is evaporated, secondary steam and concentrated solution (D) are separated, a part of the secondary steam enters a condenser (54) to be condensed into liquid water and is stored in a purified water storage system (4), the other part of the secondary steam enters a power module (52), and the concentrated solution (D) is discharged out of a desalting system (5); and the high-pressure steam entering the power module (52) heats and pressurizes the other part of secondary steam, and the heated and pressurized other part of secondary steam enters the evaporator (53) and heats the saline water (C) entering the evaporator (53), so that the saline water is condensed into liquid water and stored in the purified water storage system (4).
2. The integrated brine desalination and dry steam generation plant of claim 1,
the solar heat collection system (1) comprises a solar heat collection module (11), a heat collection working medium (12), a heat collection working medium flowing module (13) and a heat collection working medium heat exchange module (14);
the heat collecting working medium flowing module (13) is connected with the solar heat collecting module (11) and the heat collecting working medium heat exchange module (14) and guides the heat collecting working medium (12) to circularly flow between the solar heat collecting module (11) and the heat collecting working medium heat exchange module (14);
the solar heat collection module (11) collects the heat energy of the sunlight and transmits the heat energy to the heat collection working medium (12), and the heat collection working medium (12) transmits the heat energy to the heat collection working medium heat exchange module (14);
the heat collection working medium heat exchange module (14) is connected with the heat storage system (2) and transfers heat energy to the heat storage system (2).
3. The integrated brine desalination and dry steam generation plant of claim 1,
the heat storage system (2) comprises a heat storage medium (21), a heat storage medium flowing module (22), a high-temperature heat storage module (23) and a low-temperature heat storage module (24);
the heat storage medium flowing module (22) is sequentially connected with the solar heat collection system (1), the high-temperature heat storage module (23), the steam module (31) of the dry steam generation system (3) and the low-temperature heat storage module (24), and controls the heat storage medium (21) to flow among the solar heat collection system (1), the high-temperature heat storage module (23), the steam module (31) of the dry steam generation system (3) and the low-temperature heat storage module (24);
the heat storage medium (21) is heated after passing through the solar heat collection system (1) to form a high-temperature heat storage medium (21), and the high-temperature heat storage medium (21) is stored in the high-temperature heat storage module (23); the high-temperature heat storage medium (21) in the high-temperature heat storage module (23) enters a steam module (31) of the dry steam generation system (3) to be cooled and form a low-temperature heat storage medium (21), and the low-temperature heat storage medium (21) is stored in the low-temperature heat storage module (24); the low-temperature heat storage medium (21) in the low-temperature heat storage module (24) reenters the solar heat collection system (1) to absorb heat and raise the temperature.
4. The integrated equipment for desalinating brine and preparing dry steam according to claim 3, wherein a heater (25) is further arranged in the high-temperature heat storage module (23) and the low-temperature heat storage module (24).
5. The integrated brine desalination and dry steam generation plant of claim 4,
the steam module (31) comprises a preheater (311) and a steam generator (312);
purified water in the purified water storage system (4) firstly enters the preheater (311) and then enters the steam generator (312);
the heat storage medium flowing module (22) is sequentially connected with the high-temperature heat storage module (23), the steam generator (312), the preheater (311) and the low-temperature heat storage module (24).
6. The integrated brine desalination and dry steam generation plant of claim 1,
the purified water storage system (4) comprises a purified water storage tank (41), a softener (42), a deaerator (43) and a supercharger (44) which are connected in sequence, and the supercharger (44) is connected with the steam module (31).
7. The integrated brine desalination and dry steam generation plant of claim 1,
the desalination system (5) also comprises a blender (55) connected with the flash tower (51) and the evaporator (53), and the brine (C) needing to be desalinated enters the blender (55);
the flash column (51) produces high pressure steam leaving liquid water to enter the blender (55) and mix with the brine (C) entering the blender (55), and the mixed brine (C) enters the evaporator (53).
8. The integrated brine desalination and dry steam generation plant of claim 1,
the desalination system (5) further comprises a vacuum pump (56) connected to the condenser (54), the vacuum pump (56) pumping the non-condensable gases (B) from the condenser (54) and maintaining a vacuum in the shell side of the evaporator (53).
9. The integrated brine desalination and dry steam generation plant of claim 1,
the power module (52) comprises an ejector (521), and the high-pressure steam generated by the flash tower (51) enters the ejector (521) to eject the other part of secondary steam so as to heat and pressurize the other part of secondary steam;
or,
the power module (52) comprises a steam turbine (522) and a compressor (523), wherein the steam turbine (522) is respectively connected with the flash tower (51), the compressor (523) and the purified water storage system (4); the other part of the secondary steam enters a compressor; the high pressure steam generated by the flash tower (51) pushes a steam turbine (522) and is condensed into liquid water, and the liquid water is stored in a purified water storage system (4); the steam turbine (522) transfers power to the compressor, which heats and pressurizes the other portion of the secondary steam.
10. The integrated brine desalination and dry steam generation plant as claimed in claim 1, wherein the evaporator (53) is a multiple effect evaporator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721589067.9U CN207566923U (en) | 2017-11-23 | 2017-11-23 | Saline-water reclamation and the integration apparatus for preparing dry saturated steam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721589067.9U CN207566923U (en) | 2017-11-23 | 2017-11-23 | Saline-water reclamation and the integration apparatus for preparing dry saturated steam |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207566923U true CN207566923U (en) | 2018-07-03 |
Family
ID=62691641
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721589067.9U Active CN207566923U (en) | 2017-11-23 | 2017-11-23 | Saline-water reclamation and the integration apparatus for preparing dry saturated steam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207566923U (en) |
-
2017
- 2017-11-23 CN CN201721589067.9U patent/CN207566923U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Kalogirou | Survey of solar desalination systems and system selection | |
| He et al. | Application of alternative energy integration technology in seawater desalination | |
| US7037430B2 (en) | System and method for desalination of brackish water from an underground water supply | |
| CN102219273B (en) | Solar and thermocompression vapor-compression distillation type water purifying device | |
| EA022856B1 (en) | OSMOTIC NETWORK STORAGE DRIVERS IN THE SCALE OF ELECTRIC POWER ENTERPRISES | |
| CN102225787A (en) | A composite solar desalination device and method | |
| CN204661346U (en) | Solar cogeneration seawater desalination system | |
| CN102329035B (en) | Fresh water collecting and supplying system | |
| CN202208652U (en) | Salt water treating system | |
| CN1323032C (en) | Apparatus of combined solar energy heat pump for desaltination of sea water | |
| Elazab et al. | A review of hybrid humidification and dehumidification desalination systems | |
| CN101130442A (en) | Method for desalinating sea water by using seawater source heat pump technology | |
| Thomas | Overview of village scale, renewable energy powered desalination | |
| CN108408804B (en) | Integrated equipment for desalting brine and preparing dry steam | |
| CN207566923U (en) | Saline-water reclamation and the integration apparatus for preparing dry saturated steam | |
| CN203177141U (en) | Four combination supply device for utilizing flue gas waste heat of gas turbine to produce cold, heat, electricity and water | |
| CN115614115B (en) | Light-nuclear complementary multi-source steam distribution sea water desalination system and operation method | |
| CN201864592U (en) | Full-automatic solar seawater desalination device | |
| CN108275738A (en) | MVR seawater desalination systems based on generation of electricity by new energy | |
| CN111620402A (en) | System and method for high-salinity wastewater through photo-thermal evaporation crystallization | |
| CN101134605A (en) | Temperature-differential sea-water distillator | |
| CN102134138A (en) | Solar multi-effect utilization seawater desalting method and device | |
| KR101489642B1 (en) | Complex fresh water production system using fuel cell apparatus | |
| CN1049643A (en) | Method and device for desalting seawater by utilizing natural energy | |
| CN212269520U (en) | High-salinity wastewater system utilizing photo-thermal evaporation crystallization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100029 Chaoyang District, Beijing Hui Xin Street six, Twelfth level. Patentee after: SINOPEC OILFIELD SERVICE Corp. Patentee after: Sinopec Jianghan Petroleum Engineering Design Co., Ltd Address before: 100029 Chaoyang District, Beijing Hui Xin Street six, Twelfth level. Patentee before: SINOPEC OILFIELD SERVICE Corp. Patentee before: Sinopec energy conservation and Environmental Protection Engineering Technology Co., Ltd |
|
| CP01 | Change in the name or title of a patent holder |