WO2000029333A1 - Clavier et procede de saisie correspondant - Google Patents

Clavier et procede de saisie correspondant Download PDF

Info

Publication number
WO2000029333A1
WO2000029333A1 PCT/CN1999/000185 CN9900185W WO0029333A1 WO 2000029333 A1 WO2000029333 A1 WO 2000029333A1 CN 9900185 W CN9900185 W CN 9900185W WO 0029333 A1 WO0029333 A1 WO 0029333A1
Authority
WO
WIPO (PCT)
Prior art keywords
stage
seawater
evaporator
pressure vessel
refrigeration
Prior art date
Application number
PCT/CN1999/000185
Other languages
English (en)
Chinese (zh)
Inventor
Yuanming Yi
Original Assignee
Yuanming Yi
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Yuanming Yi filed Critical Yuanming Yi
Priority to AU11469/00A priority Critical patent/AU1146900A/en
Publication of WO2000029333A1 publication Critical patent/WO2000029333A1/fr

Links

Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/008—Liquid distribution
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
    • 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

Definitions

  • the present invention relates to seawater desalination technology, and in particular to a negative temperature difference seawater desalination device that uses the energy possessed by the negative temperature difference between the amount of cold provided by artificial refrigeration and the natural normal temperature seawater itself. Description of the prior art
  • the object of the present invention is to provide a new negative temperature difference seawater desalination device, which utilizes a large amount of cooling capacity provided by a pure phase-change athermal refrigerating device to efficiently refrigerate, and forms a low-temperature negative pressure condensation space. Temperature difference, under the state of negative pressure, it is vaporized into water vapor, so that the water vapor is condensed and liquefied into fresh water in the low-temperature negative pressure condensing space, and at the same time external cooling is provided.
  • a negative temperature difference seawater desalination device includes an evaporator that absorbs heat and vaporizes seawater, a condenser that condenses water vapor into liquid freshwater, and collects freshwater droplets and currents. Devices and pipelines, thereby forming a thermal phase change cycle of seawater desalination;
  • a multi-stage refrigeration cycle using pure phase-change athermal refrigeration technology which includes a first-stage vapor compression refrigeration cycle consisting of a refrigeration compressor, a condenser, a throttle, and an evaporator to provide the original refrigeration capacity.
  • a terminal heat-insulating pressure vessel connected with a working fluid infusion pipe and a heat-insulating return pipe behind the middle N-stage heat-insulating pressure vessel, together with seawater and freshwater drainage pumps and connecting pipes, said end heat-insulating pressure vessel is equipped with more than one tubular tubular middle N-stage Refrigeration evaporator, a seawater evaporator provided on the periphery of the middle N-stage refrigeration evaporator, a fresh water condensation plate installed on the top of the middle N-stage refrigeration evaporator, a fresh water
  • the siphon suction height is determined by the pressure and flow rate of the siphon outlet water required by the seawater evaporator inlet.
  • the seawater flows through the seawater evaporator to Seawater trough, which is connected by a water pipe to a water pump, and drains the cooled seawater to a cold user for external cooling, or re-drains deep into the sea;
  • the intermediate N-stage refrigeration evaporator is fitted with a fresh water condensation plate, and the intermediate N-stage refrigeration liquid working medium with an evaporation temperature of about 0 ° C absorbs heat and vaporizes from the fresh water condensation plate, and then returns to the previous stage heat preservation pressure through the heat insulation return pipe.
  • the condensing space in the container condenses and liquefies.
  • Negative pressure condensation space is formed in the terminal heat insulation pressure vessel.
  • the seawater flows from top to bottom in the seawater evaporator with a heat insulation layer.
  • the surface seawater in the seawater evaporator absorbs heat from itself and the inner seawater and vaporizes into water vapor.
  • the pipes are concentrated into the fresh water reservoir, and the fresh water reservoir is connected to the water pump.
  • Fresh water is pressurized and delivered to fresh water users by a pump.
  • the bottom condensing space in the end heat-preserving pressure vessel is connected to a moisture absorption drying box located in the middle-stage heat-preserving pressure vessel via a gas pipe. A small amount of air dissolved in seawater passes through The gas pipe enters the heat insulation pressure vessel at the middle level from the end of the heat insulation pressure vessel. After the water vapor is absorbed by the moisture absorption drying box, the temperature of the dry air entering the evaporator and the supercooled liquid working fluid condensation plate is
  • the low-temperature condensing space at about 200 ° C is continuously condensed and liquefied, and is accumulated in the liquid air tank for regular discharge, thereby effectively ensuring that a negative-pressure condensing space is formed stably in the terminal insulated pressure vessel;
  • the liquid refrigerant in the middle-stage attached evaporator absorbs heat and vaporizes from the dry air introduced from the end heat-retaining pressure vessel, and condenses through the heat-recovery return pipe to the condensation space in the first heat-retaining pressure vessel, and then liquefies it again;
  • the evaporation temperature of the first-stage refrigerant is the lowest, and then the evaporation temperature of each stage of the refrigerant is increased in stages.
  • the invention adopts a pure phase change heatless refrigeration technology, implements a multi-stage phase change to cool the refrigeration cycle, and reuses the amount of cooling provided by the previous stage refrigeration cycle to condense and liquefy the phase change of the working medium vapor in the refrigeration cycle of this stage to cool
  • the refrigeration cycle multiplies the original cooling capacity provided by the first-stage vapor compression refrigeration cycle, and takes out a large amount of cooling with a temperature of about O'C and a small amount of low-temperature deep cooling cooling with a high cooling efficiency;
  • Negative pressure condensing space condenses the water vapor formed by the evaporation of seawater's own heat under negative pressure conditions, realizes the desalination of negative temperature difference seawater, and can simultaneously provide external cooling.
  • Figure 1 is the first thermal insulation pressure vessel and the intermediate first-level protection in a negative temperature difference seawater desalination equipment. Schematic diagram of the structure of a warm pressure vessel, a middle-stage thermal insulation pressure vessel and a middle N-stage thermal insulation pressure vessel.
  • FIG. 2 is a schematic structural diagram of a terminal thermal insulation pressure vessel in the above seawater desalination equipment. Description of the embodiments
  • a refrigeration compressor 1, a condenser 2, a throttle 4, and an evaporator 6 are installed in a first heat-preserving pressure vessel 8 to form a first-stage vapor compression cold cycle to provide an original refrigeration capacity.
  • the lower part of the first temperature-keeping pressure vessel 8 is filled with a liquid refrigerant working medium 14, and the refrigeration compressor 1 and the condenser 2 in the above-mentioned first-stage vapor compression refrigeration cycle are immersed in the liquid refrigerant working medium 14.
  • a subcooled liquid working medium condensing plate 17 is provided in the middle of the first heat preservation pressure container 8.
  • the working fluid pump 9 is connected to the first heat-preserving pressure vessel 8 through a suction pipe 18, and the other end of the working fluid pump 9 is connected to the working fluid infusion pipe 10.
  • the working fluid infusion pipe 10 is connected to the intermediate-stage refrigeration evaporator 19 and the intermediate-stage refrigeration evaporator 28 respectively.
  • the bottom of the intermediate-stage thermal insulation pressure vessel 20 is filled with a liquid refrigerant working medium 21, the intermediate-stage refrigeration evaporator 19 and the subcooled liquid refrigerant cooling plate 17 are installed in the intermediate-stage thermal insulation pressure vessel 20.
  • the intermediate stage refrigeration evaporator 19 is composed of a working fluid infusion pipe 10, a working fluid pump 9, a liquid suction pipe 18, and a temperature-retaining air return pipe 11 which communicates with the condensing space in the first heat-preserving pressure vessel 8 to form a phase change for a cold refrigeration cycle.
  • a moisture absorption and drying box 47 and a liquid air tank 50 are installed at the lower part of the middle-stage heat insulation pressure container 24, and a baffle 53 is installed above the moisture absorption and drying box 47.
  • An intermediate stage primary evaporator 28 is installed on the upper part of the middle-stage heat insulation pressure vessel 24, and a subcooled liquid working medium condensation plate 17 is installed in the middle.
  • the middle-stage auxiliary evaporator 28 is composed of a working fluid infusion pipe 10, a working fluid pump 9, a liquid suction pipe 18, and a heat preservation return pipe 11 which communicates with the condensing space in the first heat preservation pressure vessel 8 to form a phase change for a cold refrigeration cycle.
  • One end of the mass pump 9 is connected to the intermediate-stage thermal insulation pressure vessel 20 through a suction pipe 18, and the working fluid pump 9 is connected to the intermediate-stage refrigeration evaporator 12 through the working fluid transfer pipe 10.
  • an intermediate-stage refrigeration evaporator 12 In the intermediate N-stage heat-retaining and pressure vessel 13, an intermediate-stage refrigeration evaporator 12, a subcooled liquid working medium condensing plate 17, and a liquid cooling working medium 22 are installed.
  • the intermediate-stage refrigeration evaporator 12 is composed of a working fluid infusion pipe 10, a working fluid pump 9, a suction pipe 18, and an insulation return pipe 11, which communicates with the condensing space in the intermediate-stage insulation pressure vessel 20 to form a phase change for cold refrigeration. cycle. Referring to FIG.
  • one end of the working fluid pump is connected to the intermediate N-level thermal insulation pressure vessel 13 through a suction pipe 18, and the other end of the working fluid pump is connected to the middle N-level refrigeration evaporator in the end thermal insulation container 30 through the working fluid infusion pipe 25.
  • a seawater evaporator 34 is installed in the terminal heat-preserving pressure vessel 30.
  • a cover plate 54 is provided on the seawater evaporator 34, and a large number of ventilation holes 37 are provided on the cover plate 54.
  • a blocking plate 33 is provided above the ventilation holes 37.
  • the middle N-stage refrigeration evaporator 35 is affixed under the bottom plate of the fresh water condensing plate 31, and the fresh water collection tank 36 is connected to the fresh water condensing plate 31.
  • the middle N-stage refrigeration evaporator 35 is connected through the suction pipe 18 ", working medium pump",
  • the mass infusion pipe 25 and the heat preservation air return pipe 26 communicate with the condensing space in the intermediate N-stage heat preservation pressure vessel 13 to form a phase change for a cold refrigeration cycle.
  • the middle N-stage refrigeration evaporator 35 installed in the terminal heat-preserving pressure vessel 30 is connected with N units from bottom to top, and each unit includes an intermediate N-stage refrigeration evaporator 35, a seawater evaporator 34, a fresh water condensation plate 31, and fresh water. Collection tank 36 and connecting pipe.
  • a gas-conducting pipe 46 is provided in the lower-layer negative-pressure condensing space in the terminal heat-preserving pressure vessel 30, and the gas-conveying pipe 46 is connected to a moisture absorption drying box 47 located at the lower part of the middle-stage heat-preserving pressure vessel 24.
  • a small amount of air existing in the terminal insulated pressure vessel 30 enters the moisture absorption drying box 47 through the air pipe 46, and the dry air enters the middle-stage condensing space to condense into liquid air, falls back into the liquid air tank 50, and then is intermittently driven by the industrial shield pump 9, "through the suction pipe 18", sucked out from the liquid air tank 50, and after being pressurized, is discharged into the space through the working fluid infusion pipe 29.
  • the normal temperature seawater in the natural sea area 48 is sucked in from the surface of the natural sea area through the siphon 38, rises along the siphon 38, and enters the seawater evaporator 34 from the seawater inlet 52 above the seawater evaporator 34 in the end thermal insulation pressure vessel 30, and the normal temperature seawater absorbs heat from itself Under the negative pressure, it vaporizes into water vapor.
  • the water vapor enters the negative pressure condensing space in the terminal insulation pressure vessel 30 from the vent hole 37 on the seawater evaporator cover plate 54 and condenses into fresh water, thereby forming the final phase change for cold refrigeration. Cycle and desalination phase change thermodynamic cycle.
  • the fresh water droplets are collected by the fresh water collection tank 36, flow into the fresh water reservoir 41 through the water pipe 42 and the water pipe 40, and the fresh water liquid 39 is delivered to the fresh water user through the water pump 51, the suction pipe 55 and the water delivery pipe 49.
  • the cold seawater that has been cooled down in the seawater evaporator 34 and can no longer be evaporated flows into the seawater tank 32 located at the bottom of the end heat insulation pressure vessel 30 through the water channel in the seawater evaporator 34, and is pressurized by the suction pipe 44 and the water pump 43. 45 is discharged into the deep sea area, or the cooled seawater is sent as a refrigerant through the water pipe 45 to the cold user for external cooling.
  • the working process of the present invention is as follows:
  • the refrigeration compressor 1 is started to cool, and its heat is dissipated by the latent heat of vaporization of the liquid refrigerant working medium 14, and its vapor enters the condensing space composed of the supercooled liquid working medium condensation plate 17 and the evaporator 6 from the vent pipe 16; At the same time, the liquid level regulator 23 automatically replenishes the upper liquid refrigerant working medium 14 of the first heat-preserving pressure vessel 8 to the lower layer through the liquid supply pipe 15.
  • the working medium vapor absorbs heat and vaporizes and refrigerates, and returns to the condensing space inside the first heat-preserving pressure vessel 8 through the heat-returning gas return pipe 11 to liquefy.
  • the middle-stage evaporator 28 absorbs heat and vaporizes from the dry air introduced from the end heat-preserving pressure vessel 30. And refrigerate, and return to the condensing space liquid in the first heat-preserving pressure vessel 8 through the heat-returning air return pipe 1 1.
  • the middle N-stage refrigeration evaporator 35 absorbs heat from the water vapor, vaporizes and refrigerates, and returns to the The gas pipe 26 returns to the intermediate N-stage heat-preserving pressure vessel 13 to condense and liquefy.
  • the seawater When negative pressure occurs in the terminal insulated pressure vessel 30, the seawater automatically enters the seawater evaporator 34 along the siphon 38, and at this time, the water pump 43 is started to discharge the seawater in the seawater tank 32.
  • the water pump 51 When the fresh water level in the fresh water reservoir 41 reaches or exceeds the storage limit, the water pump 51 is started to supply fresh water to water users.
  • a large or extra large desalination base can be built, and a wastewater treatment base for purifying industrial waste water or similar to industrial waste water can be built, which can provide pure fresh water to industrial and agricultural production and residents' life on a large scale and cheaply.

Abstract

L'invention porte sur un clavier permettant d'introduire des mots anglais en continu au moyen d'un petit nombre de touches et sur son procédé de saisie. Ce type de clavier peut être un clavier d'ordinateur déjà disponible ou spécifique, un clavier de téléphone, etc. Un plan codé de mots anglais dont la vitesse de codage de répétition des mots anglais est minimale a été sélectionné en fonction d'un grand nombre de résultats comparatifs et de statistiques de code de répétition de mots anglais, ce qui simplifie la règle du procédé de saisie et génère une bande de données codées de mots anglais. Les mots anglais peuvent donc être introduits en continu au moyen de 2 à 13 touches seulement du clavier en fonction de leur orthographe correcte selon la règle de simplification des racines de mots.
PCT/CN1999/000185 1998-11-12 1999-11-12 Clavier et procede de saisie correspondant WO2000029333A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU11469/00A AU1146900A (en) 1998-11-12 1999-11-12 A device for desalinizing sea water

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN98121993A CN1223234A (zh) 1998-11-12 1998-11-12 负温差海水淡化设备
CN98121993.4 1998-11-12

Publications (1)

Publication Number Publication Date
WO2000029333A1 true WO2000029333A1 (fr) 2000-05-25

Family

ID=5227481

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN1999/000185 WO2000029333A1 (fr) 1998-11-12 1999-11-12 Clavier et procede de saisie correspondant

Country Status (3)

Country Link
CN (1) CN1223234A (fr)
AU (1) AU1146900A (fr)
WO (1) WO2000029333A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10246345B2 (en) 2015-12-30 2019-04-02 General Electric Company Water desalination system and method for fast cooling saline water using turbines

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101109536B1 (ko) * 2009-07-06 2012-01-31 한국에너지기술연구원 상변화 매체를 이용한 증발식 해수 담수화 장치
AU2009357310A1 (en) * 2009-12-25 2012-07-19 Chen, Jian-An Easing pressure oxygen-dissolving device
CN105540709B (zh) * 2015-12-23 2018-05-04 中置新能源科技发展(上海)有限公司 一种海水淡化装置及海水淡化系统

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3492205A (en) * 1967-11-17 1970-01-27 Robert C Webber Distillation system and method
US3675436A (en) * 1970-02-25 1972-07-11 Struthers Scient And Intern Co Desalination process
US3714791A (en) * 1971-02-25 1973-02-06 Pacific Lighting Service Co Vapor freezing type desalination method and apparatus
US3892103A (en) * 1972-06-13 1975-07-01 Nuovo Pignone Spa Liquefying refrigerant for water desalination with liquefied natural gas and an intermediate energy cycle
WO1991013300A1 (fr) * 1990-02-27 1991-09-05 Cheng Chen Yen Procedes de transformation a phases multiples solide-liquide-vapeur par des operations d'absorption-fusion couplees
CN2194903Y (zh) * 1994-07-02 1995-04-19 王燕华 低温海水淡化装置
CN1117562A (zh) * 1994-08-24 1996-02-28 张庆玉 真空海浪发电和海水淡化装置
US5729987A (en) * 1996-02-27 1998-03-24 Miller; Joel V. Desalinization method and apparatus

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3492205A (en) * 1967-11-17 1970-01-27 Robert C Webber Distillation system and method
US3675436A (en) * 1970-02-25 1972-07-11 Struthers Scient And Intern Co Desalination process
US3714791A (en) * 1971-02-25 1973-02-06 Pacific Lighting Service Co Vapor freezing type desalination method and apparatus
US3892103A (en) * 1972-06-13 1975-07-01 Nuovo Pignone Spa Liquefying refrigerant for water desalination with liquefied natural gas and an intermediate energy cycle
WO1991013300A1 (fr) * 1990-02-27 1991-09-05 Cheng Chen Yen Procedes de transformation a phases multiples solide-liquide-vapeur par des operations d'absorption-fusion couplees
CN2194903Y (zh) * 1994-07-02 1995-04-19 王燕华 低温海水淡化装置
CN1117562A (zh) * 1994-08-24 1996-02-28 张庆玉 真空海浪发电和海水淡化装置
US5729987A (en) * 1996-02-27 1998-03-24 Miller; Joel V. Desalinization method and apparatus

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10246345B2 (en) 2015-12-30 2019-04-02 General Electric Company Water desalination system and method for fast cooling saline water using turbines

Also Published As

Publication number Publication date
CN1223234A (zh) 1999-07-21
AU1146900A (en) 2000-06-05

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