• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The invention relates to the treatment of wastewater by spraying and evaporation in a carrier gas stream and allows for an increase in the degree of purification due to the release of contaminants in the form of salt crystals or hydrates. Wastewater is sprayed and evaporated in a stream of inert carrier gas. The resulting water is superheated in the heat exchanger of the purified and compressed vapor-gas mixture by cooling it below the dew point temperature, as a result of which the impurities fall out as a solid residue and are separated. With a ratio of the partial pressure of the carrier gas and the total pressure of the mixture of 0.2-0.8 and at a total pressure of the purified mixture of 3-20 bar, the optimum area for the implementation of the method is established. Preferably, before separating the solid residue, the solid particles are coagulated, and the mixture to be purified is heated to a temperature above the decomposition temperature of at least one hydrate contained in the mixture. 3 з.п f-ly. 2 Il (L S
    公开号:SU1743352A3
    申请号:SU843805259
    申请日:1984-10-12
    公开日:1992-06-23
    发明作者:Иниотакис Николас；Фрелинг Вернер；Калавритинос Георг；Бенедикт Фон Дер Декен Клаус
    申请人:Форшунгсцентрум Юлих Гмбх (Фирма)；Др.Георг Калавритинос (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to wastewater treatment by evaporating a carrier gas in a stream and removing the residue that is formed.
    The purpose of the invention is to increase the degree of purification due to the release of contaminants in the form of salt crystals or hydrates.
    Fig. 1 is a flow chart of a plant for wastewater treatment according to the proposed method; 2 shows graphs of the saturation temperature as a function of the total pressure Pf and the ratio of the partial pressure of the carrier gas P5Cc to the total pressure Pf.
    The water to be purified is pumped through the pressure pipe 2 to the installation 3 for preheating by means of a pump 1. Installation 3 preheating is performed in
    as a counter-flow heat exchanger. The condensate flowing through pipeline 4 serves as a heating body in unit 3. Condensate is pumped through unit 3 by means of a condensate pump 5.
    The water to be cleaned after the initial heating in the installation 3 through the pipeline 6 is supplied to the evaporator 7 and there by means of the device 8 is sprayed into the flow of carrier gas and injected directly into the gas flow by means of a nozzle. The flow of carrier gas is directed through line 9 to the evaporator 7. The location of the nozzle at the inlet 10 of the evaporator 7 is shown schematically. It is necessary to ensure that water with a flow of carrier gas enters the evaporator 7 only in a finely atomized form. Instead of a spray nozzle,
    other means of liquid spraying may be used. A very uniform distribution is achieved with the formation of fog.
    In the evaporator 7, the mixture of carrier gas and water entering inlet 10 is heated to a temperature that lies above the saturation point of water vapor in the mixture of gas-carrier vapor. The saturation temperature depends on the total pressure Pf in the gas-water vapor mixture. and also on the ratio between the partial pressure of the carrier gas Psch and the total pressure Pf. The dependence of the saturation temperature (corresponding to the dew point temperature) on the total pressure Pf and on the ratio Psch / Pf is shown in FIG. 2. The higher the total pressure Pf selected and the smaller the Psch / Pf ratio, the more water at the same total pressure Pf is injected into the carrier gas stream and the higher the saturation temperature.
    To create a water-free state, the mixture of gas and water vapor is superheated at least 15-20 ° C above the saturation temperature. If there is not enough heat available for this in the evaporator 7, then the mixture can be heated to the required temperature in the superheater 11 connected in series with the evaporator 7.
    The operation of the superheater 11 is provided by means of a by-pass line 12 parallel to the pipeline 14, running from the outlet 13 of the evaporator 7 to the separator 15.
    Overheated mixture consisting of a carrier gas and water vapor, through line 14 is fed to the separator 15. The latter is suitable for working with substances that remain when the water component evaporates in the carrier gas stream and is contained in a mixture of carrier gas and water vapor in the form of solid particles. Thus, the separator is selected in accordance with the desired degree of purification and has a filtering quality that satisfies the requirements. Impurities remaining in the form of solid particles can be removed, depending on the filtering applied, with a very high degree of purification.
    In parallel with the pipeline 14, there is a different bypass line 16. associated with the pressure reducer 17. The operation of the bypass line 16 is provided for the cases when the overheating of the mixture consisting of the carrier gas and water vapor is insufficient to obtain a state free from water droplets and there is no cheap heat source providing its additional supply to the superheater 11. This allows implement cost-effective process management.
    As the separator 15 serves as a chamber in which the flow of the carrier gas is deflected. The solids released from the mixture are collected at the bottom 18 of the separator 15 and are continuously removed from there by the suction device 19.
    The purified mixture of gas and water vapor, discharged from outlet 20 of the separator 15, is returned as a heat carrier to the evaporator 7 for heat recovery. The gas-water mixture is taken through the suction pipe 21 from the separator and compressed by the compressor 22, so that when the gas-vapor mixture is to be purified and heat is condensed, the water vapor condenses at the dew point temperature that lies above the saturation temperature of the water vapor in the mixture being cleaned.
    The heat generated by the condensation of the purified water component passes in this way to the gas-water mixture to be purified, respectively, the gas-water vapor.
    If the difference obtained by compression between the dew point temperature on the one hand and the saturation temperature on the other hand is not sufficient to obtain a state of the gas-water mixture to be cleaned of water droplets, the gas-vapor system can be heated to a mixture in an additional preheater 23. The latter is connected via a by-pass line 24 to the pressure pipe 25 of the compressor 22. As a heat source for the preheater 23, as well as for the superheater 11, waste heat or heat can be used Obtained by converting solar energy. The stronger the compressed mixture is compressed, the less additional heating of the mixture is required in the heater 23 in order to obtain the state of the mixture being cleaned free from water droplets. From the heater 23, the connecting pipe 26 leads to the evaporator 7, which is made in the form of a tubular boiler with pipes through which the gas – carrier – water vapor mixture is cooled in the evaporator. The compressed gas-water vapor mixture is cooled below the dew point temperature of the water vapor in the mixture. The condensate formed through the pipeline 4 is discharged to the preheating unit 3, while the remaining carrier gas is directed through the outlet 27 to the circuit to the inlet 10 of the evaporator 7. The pressure in the carrier gas is adjusted by the pressure in the pipeline for carrier gas 9. At the inlet 10 of the evaporator 7, water to be cleaned is re-introduced into the carrier gas stream. If, for example, in the installation described above, wastewater containing NJS04 is treated, then N1S04 can be recovered either as dry salt or as a hydrate + 6Н20. For the hydrate, the free enthalpy of the DN reaction and the entropy L S of the reaction are:
    NIS04 + 6H20; l N -85.80 cal / mol; d 5 213.23 cal / mol.
    From this, the required partial pressure of water vapor o to form a hydrate is determined from the relation:
    1 As 1 AH
    . | 6 RT
    PH20 I 6
    (bar)
    long
    PH2O 2.42 bar at 150 ° C;
     5.17 bar spins 170 ° C.
    If in a carrier gas-water vapor mixture, the total pressure is PbB bar and wastewater is supplied to the carrier gas, containing NiS04 at fine spraying until the ratio Psch / Pf reaches 0.5. then the partial pressure of the Pn2o wastewater will be 4 bar. In view of the above values, the formation pressure for NIS04 6H20 corresponds to this partial pressure equal to 165 ° C. At temperatures in the carrier gas-water vapor mixture above this temperature, solid particles remain in the mixture, consisting of dry salt.
    N1S04.
    If wastewater containing NiCI is treated. It is also possible to extract the dry salt of NiCI2 or NiCI2-2H20 hydrate. To form a hydrate, a partial pressure of water vapor is required.
    - 6958 5
    PH20 518061971 t (bar).
    this implies
     3.716 bar at T 150 ° СР Н20 6,529 bar at 165 ° С.
    If the total pressure in the mixture consisting of carrier gas and water vapor is set at 8 bar and the Psch / Pf ratio is 0.5, the formation temperature of the NiCI2 2H20 hydrate will be more than 153 ° C. At higher temperatures, according to this calculation, it is possible to separate out dry NiCI2 particles from the mixture.
    The preheating unit 3 can be regulated so that the amount of wastewater to be treated is fed into the carrier gas stream at a temperature of 60 ° C and above. Carrier gas flow and the amount of waste
    water is consistent with each other in such a way that in a mixture consisting of a carrier gas and water vapor, the ratio of the partial pressure of the carrier gas Psch to the total pressure Pg in the range of 0.2-0.8 is observed. With a pressure ratio of Psch / Pf of 0.4 and a total pressure of Pf of 5 bar, the saturation temperature of the water vapor is 130 ° C. To achieve a state free from water droplets,
    overheating of the mixture is at least 15-20 ° C above the saturation temperature. If we go from the fact that for this overheating in the evaporator 7, a temperature difference of 20 ° C between the compressed and purified
    With a carrier gas-water vapor mixture used as a heating body and the mixture to be cleaned, the purified mixture should be compressed at an equal pressure ratio Psch / Pf without additional overheating in the heater 23 to a total pressure of 14 bar. Taking into account the heat transfer in the evaporator as a whole, the total pressure is set within 3-20 bar. With low compression to achieve
    water-free mixture state; additional heating of the compressed mixture is necessary in a piezo-heater 23. An alternative could be any combination of all the other measures mentioned above.
    in order to reliably achieve a state that is free from water droplets, or it is possible to reduce the total pressure in a gas-water vapor mixture even before the separation of solid particles in the pressure reducer 17. The latter is made in the form of a vortex chamber in order to coagulate particles of a solid substance using adhesion. From the superheated gas-water vapor mixture, solid particles contained in the mixture are precipitated in the separator 15. The purified mixture is withdrawn from the separator.
    Helium, argon, nitrogen, air and other gases that do not react with water are used as carrier gas.
    nor with the substances to be removed in the wastewater.
    To reduce energy consumption for compression and heating of the purified mixture, it is necessary to optimize the range of operating parameters. With a Psch / Pf ratio in the range of 0.2-0.8 at a total pressure of 3-20 bar and temperatures below 220 ° C, an optimal region can be established for the implementation of the proposed method.
    权利要求:
    Claims (4)
    [1]
    Claims 1. Wastewater treatment method. including thin spraying of water in a carrier gas stream, its evaporation followed by overheating in the heat exchanger due to the supply of heat from the exhaust, purified and compressed vapor-gas mixture, removal of the formed solid sediment, characterized in that in order to increase the degree of purification due to separation of pollution in the form of salt crystals or hydrates, water is introduced into the carrier gas stream in an amount at which the ratio of the partial pressure of the carrier gas and the total pressure of the mixture at the outlet of the heat exchanger is 0.2-0.8, at th overheating
    0
    five
    the mixture is carried out by cooling the exhaust, purified and compressed gas-vapor mixture below the dew point, and an inert gas is used as the carrier gas.
    [2]
    2. A method according to claim 1, characterized in that the purified gas-vapor mixture is compressed to a pressure in the range of 3-20 bar.
    [3]
    3. A method according to claim 1, characterized in that before separating the solid residue, the solid particles coagulate.
    [4]
    4. A method according to claim 1, characterized in that the purified mixture of carrier gas and steam is heated to a temperature above the decomposition temperature of at least one hydrate contained in the mixture.
    /9
    about
    I
    eight"
    0
    /and
    five
    8 10 12 H 15
    FIG. 2
    Bobo
    Vx /
    ixlS
     - gz -
    R; о.б5
    2) TS "- 0.50 k
    3) JttJJ- 0.338
    g
    4) 0.15
    5) 0.00 p
    18
    Yavlenie bog
    类似技术:
    公开号 | 公开日 | 专利标题
    SU1743352A3|1992-06-23|Sewage treatment method
    US7357849B2|2008-04-15|Method and system for separating solids from liquids
    CA2692821C|2012-11-27|Method and system for treating feedwater
    US4698136A|1987-10-06|Process for the continuous production of boiler feed water
    US6699369B1|2004-03-02|Apparatus and method for thermal desalination based on pressurized formation and evaporation of droplets
    EP0933331B1|2005-03-23|Evaporative concentration apparatus for waste water
    JP2011140021A|2011-07-21|System and process for salt water desalination using energy from gasification process
    US5405503A|1995-04-11|Process for desalinating water while producing power
    US20150232348A1|2015-08-20|Water desalination and brine volume reduction process
    JP4688842B2|2011-05-25|Wastewater treatment method
    US4213830A|1980-07-22|Method for the transfer of heat
    US4427495A|1984-01-24|Apparatus and method for upgrading low pressure steam brines and the like
    US5512142A|1996-04-30|Process and device for purifying organically polluted waste water
    KR101860295B1|2018-05-23|Treatment Apparatus of FGD Wastewater by using Vacuum Evaporation and Method Thereof
    RU1783987C|1992-12-23|Process for producing purified water and substances dissolved in it
    JPH05104076A|1993-04-27|Method and device for treating waste liquid
    US20070045099A1|2007-03-01|Method and system for seaparating solids from liquids
    GB2088406A|1982-06-09|Process and apparatus for cooling and separating chlorides and fluorides from mixtures of gases
    JPH1047015A|1998-02-17|Generation and sea water desalting combined device
    CN108622969A|2018-10-09|The high-salt wastewater spray evaporation brine of low-quality waste heat driving detaches full reclaimer and method
    US5429667A|1995-07-04|Process for the recovery of carbon disulfide from a steam/carbon disulfide mixture
    JP3646131B2|2005-05-11|Treatment method of organic sludge
    CN212050614U|2020-12-01|Contain concentrated system of salt sewage
    JPH11244843A|1999-09-14|Steam compression type pure water producing device
    SU1405790A1|1988-06-30|Apparatus for making nicotine
    同族专利:
    公开号 | 公开日
    IL73202D0|1985-01-31|
    CA1225611A|1987-08-18|
    GR80493B|1985-02-11|
    DE3337360A1|1985-05-02|
    IL73202A|1987-09-16|
    EP0142018A1|1985-05-22|
    JPS6097086A|1985-05-30|
    AT26820T|1987-05-15|
    DK485084A|1985-04-15|
    DK485084D0|1984-10-10|
    DE3463365D1|1987-06-04|
    US4767527A|1988-08-30|
    DK160084C|1991-06-10|
    DK160084B|1991-01-28|
    EP0142018B1|1987-04-29|
    DE3337360C2|1989-10-26|
    US4643832A|1987-02-17|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    EA015066B1|2010-04-05|2011-04-29|Владимир Борисович ДУДИН|Plant for water treatment|
    RU2470869C2|2005-11-22|2012-12-27|Острейлиан Криэйтив Текнолоджиз Пти Лтд|System of pipelines|DE377747C|1921-04-21|1923-06-26|Otto Gutzwiller|Method and device for drying solid bodies in solution or in suspension within a liquid|
    US3306236A|1964-09-11|1967-02-28|Exxon Research Engineering Co|Burner for waste materials and method of burning waste materials|
    US3305091A|1965-04-20|1967-02-21|George A Brady|Method of separating liquid-solid suspensions into individual phases|
    CH493435A|1969-01-13|1970-07-15|Sutter Ernst|Process for the odor-free removal of waste water and / or sludge, installation for carrying out the process and application of the process|
    US4097378A|1975-09-30|1978-06-27|St Clair John Craig|Multiple effect evaporation of water from water containing combustible sludges|
    CH605428A5|1976-05-17|1978-09-29|Von Roll Ag|
    JPS601077B2|1981-03-28|1985-01-11|Nippon Furnace Kogyo Kk|DE3627477A1|1986-08-13|1988-02-25|Extraktionstechnik Gmbh|METHOD FOR SEPARATING WATER-INSOLUBLE DISTILLATES FROM WATER STEAM|
    DE3834319C2|1988-10-08|1991-08-01|Forschungszentrum Juelich Gmbh, 5170 Juelich, De|
    US5376262A|1993-06-08|1994-12-27|Exxon Research And Engineering Company|Concentration and/disposal of non-volatile inorganic contaminants from refinery waste water streams|
    KR0119766B1|1993-11-23|1997-10-29|신호근|Vaporizing and concentration drying apparatus and method|
    US5810977A|1994-11-21|1998-09-22|Aqua Health International Ltd.|Purifying water by superheated steam|
    DE19741806A1|1997-09-22|1999-03-25|Nicolaos Dipl Phys Iniotakis|Purifying hot waste water containing a high organic or inorganic load of impurities by evaporation and compressing vapor|
    DE19833739C1|1998-07-27|2000-03-30|Siemens Ag|Method and device for separating a neutron absorbing absorber from a coolant|
    US6565715B1|1999-07-12|2003-05-20|Marine Desalination Systems Llc|Land-based desalination using buoyant hydrate|
    US6969467B1|1999-07-12|2005-11-29|Marine Desalination Systems, L.L.C.|Hydrate-based desalination with hydrate-elevating density-driven circulation|
    US6767471B2|1999-07-12|2004-07-27|Marine Desalination Systems, L.L.C.|Hydrate desalination or water purification|
    US6475460B1|1999-07-12|2002-11-05|Marine Desalination Systems Llc|Desalination and concomitant carbon dioxide capture yielding liquid carbon dioxide|
    US6497794B1|1999-07-12|2002-12-24|Marine Desalination Systems L.L.C.|Desalination using positively buoyant or negatively buoyant/assisted buoyancy hydrate|
    US20040195160A1|1999-07-12|2004-10-07|Marine Desalination Systems, L.L.C.|Hydrate-based reduction of fluid inventories and concentration of aqueous and other water-containing products|
    JP2004501748A|2000-06-26|2004-01-22|マリーン・ディサリネーション・システムズ・リミテッド・ライアビリティ・カンパニー|Desalination fractionator using artificial pressurized assist device where input water cooling is controlled by hydrate dissociation|
    US6635149B1|2000-10-26|2003-10-21|Norman Campbell|Water purification system|
    US6673249B2|2000-11-22|2004-01-06|Marine Desalination Systems, L.L.C.|Efficiency water desalination/purification|
    DE10108528C1|2001-02-22|2002-06-13|Neubert Susanne|Process for treating liquids e.g. seawater, brackish water, wastewater and effluent comprises using preheating/removal unit for preheating and pre-cleaning the liquid|
    US7008544B2|2002-05-08|2006-03-07|Marine Desalination Systems, L.L.C.|Hydrate-based desalination/purification using permeable support member|
    US6890444B1|2003-04-01|2005-05-10|Marine Desalination Systems, L.L.C.|Hydrate formation and growth for hydrate-based desalination by means of enriching water to be treated|
    JP2005270888A|2004-03-25|2005-10-06|Choonpa Jozosho Kk|Solution concentration method and concentrator to be used therein|
    DE102006042501B4|2006-09-07|2010-11-25|Eisenmann Anlagenbau Gmbh & Co. Kg|Method and installation for drying objects|
    WO2009132327A1|2008-04-25|2009-10-29|Jepson W Paul|Desalination method and apparatus|
    US8709257B2|2010-04-20|2014-04-29|King Abdulaziz City for Science and Technology |Method and system for purifying liquid using waste heat|
    CN102887557B|2011-07-18|2015-04-15|赵凤宇|Equipment for desalination by glass ceramics dilutor and direct salt manufacturing and technology thereof|
    DE102013223837A1|2013-11-21|2015-05-21|Siemens Aktiengesellschaft|Process for dewatering a suspension-like substance mixture|
    US9783431B2|2014-05-28|2017-10-10|Katz Water Tech, Llc|Apparatus and method to remove contaminates from a fluid|
    RU2673841C2|2014-11-11|2018-11-30|Юрий Михайлович Примазон|Cleaning device for draining of waste liquid|
    JP6566876B2|2016-01-26|2019-08-28|東洋エンジニアリング株式会社|Heat exchange amount adjustment method for internal heat exchange distillation column|
    RU2642560C2|2016-04-26|2018-01-25|Общество с ограниченной ответственностью "НПО Пылеочистка"|Method of distilling liquids in inert gas environment|
    US10864482B2|2017-08-24|2020-12-15|Katz Water Tech, Llc|Apparatus system and method to separate brine from water|
    US11034605B2|2018-03-29|2021-06-15|Katz Water Tech, Llc|Apparatus system and method to extract minerals and metals from water|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19833337360|DE3337360C2|1983-10-14|1983-10-14|
    [返回顶部]