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WO2012008013A1 - Installation de concentration, installation pour la production d'eau douce par concentration et pour la production d'énergie électrique, procédé de concentration et procédé de fonctionnement d'une installation pour la production d'eau douce par concentration et de production d'énergie électrique - Google Patents

Installation de concentration, installation pour la production d'eau douce par concentration et pour la production d'énergie électrique, procédé de concentration et procédé de fonctionnement d'une installation pour la production d'eau douce par concentration et de production d'énergie électrique Download PDF

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Publication number
WO2012008013A1
WO2012008013A1 PCT/JP2010/061803 JP2010061803W WO2012008013A1 WO 2012008013 A1 WO2012008013 A1 WO 2012008013A1 JP 2010061803 W JP2010061803 W JP 2010061803W WO 2012008013 A1 WO2012008013 A1 WO 2012008013A1
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WIPO (PCT)
Prior art keywords
water
concentration
concentrated
pretreatment
function
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.)
Ceased
Application number
PCT/JP2010/061803
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English (en)
Japanese (ja)
Inventor
みさき 隅倉
堀次　睦
俊一 久芳
高橋　文夫
康ニ 原田
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Hitachi Ltd
Sasakura Engineering Co Ltd
Original Assignee
Hitachi Ltd
Sasakura Engineering Co Ltd
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 Hitachi Ltd, Sasakura Engineering Co Ltd filed Critical Hitachi Ltd
Priority to AU2010357340A priority Critical patent/AU2010357340B9/en
Priority to PCT/JP2010/061803 priority patent/WO2012008013A1/fr
Priority to JP2012524356A priority patent/JP5495403B2/ja
Publication of WO2012008013A1 publication Critical patent/WO2012008013A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • B01D3/007—Energy recuperation; Heat pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/30—Adding water, steam or other fluids for influencing combustion, e.g. to obtain cleaner exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F02C6/04—Gas-turbine plants providing heated or pressurised working fluid for other apparatus, e.g. without mechanical power output
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
    • F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
    • F03G7/00—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
    • F03G7/008—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for characterised by the actuating element
    • F03G7/015—Actuators using the difference in osmotic pressure between fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/08—Specific process operations in the concentrate stream
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/10—Energy recovery
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/22—Eliminating or preventing deposits, scale removal, scale prevention
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C02F5/025—Hot-water softening devices
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • 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
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the present invention relates to a concentrating plant and a concentrating method for separating raw water such as brine and seawater, in particular accompanying water discharged from a coal seam together with coal seam gas into fresh water and salt solids, and a concentrated water production system comprising the concentrating plant.
  • the present invention relates to a plant and an operation method thereof.
  • Non-Patent Document 1 water in the coal seam (hereinafter referred to as accompanying water) is discharged with CBM collection.
  • the accompanying water is brine containing salt, and it is necessary to press into the formation again or to separate the salts by desalting and return to the soil.
  • the treatment capacity of the accompanying water is a limiting condition for increasing the amount of collected CBM.
  • the accompanying water is stored in a pond and removed by natural evaporation to remove water and concentrate and separate the salt as solid matter.
  • Non-Patent Document 2 As a main desalting method, a membrane method for separating salts with a reverse osmosis membrane or an ion exchange membrane, an evaporation method for condensing moisture evaporated by heating, and the like have been studied. According to Non-Patent Document 3, there is a case where fresh water is produced from accompanying water by a two-stage reverse osmosis membrane treatment.
  • Concentrated water separated by the reverse osmosis membrane device is discharged through a valve or supplied to a desalination device of an evaporation method together with second-stage nanofiltration water to generate fresh water.
  • Non-Patent Document 1 As a method for treating the accompanying water (brine containing salt) discharged with CBM collection, the evaporating pond system described in Non-Patent Document 1 is currently being implemented in many CBM production facilities. A vast site is required.
  • Non-Patent Document 2 As described in Patent Document 1, Non-Patent Document 2, and Non-Patent Document 3, as a treatment method that replaces the evaporating pond method, a membrane method and an evaporation method have been studied and partially implemented.
  • the accompanying water is concentrated by a two-stage reverse osmosis membrane treatment to reduce the volume.
  • the volume of the concentrated water after separating the fresh water is reduced to about 1/10 of the supplied accompanying water, and the volume of the evaporation pond for separating salt from the concentrated water can also be reduced to 1/10. It is.
  • the volume even if the volume is reduced, there is no change in the need for an evaporating pond for solidifying and separating the salts.
  • Patent Document 2 a reverse osmosis membrane and an evaporation method are combined in order to improve water production efficiency.
  • a part of pretreatment wastewater second-stage filtration membrane unit concentrated water
  • a reverse osmosis membrane device When the concentrated water separated in (1) is discarded to the outside, and this is applied to the treatment of accompanying water, an evaporation pond for solidifying and separating the salts is also required.
  • the object of the present invention is to solve the above-mentioned conventional problems, and by concentrating water containing salts such as associated water stably at low equipment cost by combining a demineralizer by a membrane method and a concentrator by an evaporation method. And providing a concentration plant and a concentration method for separating into fresh water and salts.
  • the present invention provides a concentrating device, a reverse osmosis membrane device for separating accompanying water discharged from a coal bed together with coal bed gas into permeated water and non-permeated water, and concentrating the non-permeated water. And an evaporating and concentrating device for discharging concentrated water to the storage facility.
  • this invention for achieving the said objective is a pretreatment apparatus which pre-processes raw
  • the concentration and volume reduction of the raw water (associated water) can be achieved by combining the previous stage and the latter stage.
  • the concentrated water can be evaporated to dryness.
  • the evaporation pond is unnecessary and the installation cost of the evaporation pond becomes zero. .
  • the present invention provides a gas turbine power generator equipped with a gas turbine using hydrocarbon as a main fuel, an exhaust heat recovery boiler that generates steam by exhaust heat of the gas turbine, and concentrates raw water.
  • a concentrated desalination power plant comprising a concentrating device, the concentrating device separates raw water after pretreatment through the pretreatment device into permeated water and non-permeated water.
  • the energy cost for generating steam in the evaporative concentrator is no longer required. Resources can be used efficiently throughout the facility, and operating costs can be reduced.
  • the concentration device preferably includes a precipitation device for precipitating inorganic components in the non-permeate water in a flow path through which the non-permeate water flows into the evaporative concentration device.
  • the precipitation apparatus may have one or more of a function of increasing the pH of the non-permeate water, a function of increasing carbonate ions, a function of heating, a function of injecting fine bubbles, and a function of injecting calcium ions. preferable.
  • the precipitation apparatus is a heater for heating the non-permeated water using the generated steam of the exhaust heat recovery boiler as a heat source, or an apparatus for injecting the exhaust gas discharged from the gas turbine into the non-permeate water. Is provided.
  • the concentrated water production power plant further includes a steam supply system for injecting the generated steam of the exhaust heat recovery boiler into a combustor of the gas turbine, and in this case, the steam supply system includes the exhaust heat recovery It is preferable to have a valve that adjusts the supply amount of steam generated by the boiler to the combustor.
  • the concentrated desalination power plant further includes an indirect heat exchanger that generates steam to be supplied to the evaporative concentrator with the steam generated by the exhaust heat recovery boiler.
  • the present invention for achieving the above object is a concentration method, wherein the accompanying water discharged together with the coal bed gas from the coal bed is separated into permeated water and non-permeated water using a reverse osmosis membrane, A step of concentrating non-permeated water by an evaporation concentration method and discharging the concentrated water to a storage facility.
  • the present invention for achieving the above object includes a step of pretreating raw water in the concentration method, and a step of separating the pretreated water into permeated water and non-permeated water using a reverse osmosis membrane. And a step of producing concentrated water by concentrating the pretreated waste water generated as a result of the pretreatment and the non-permeated water produced in the separation step by an evaporation concentration method.
  • the present invention provides an operation of a concentrated freshwater power plant having a gas turbine power generation device, an exhaust heat recovery boiler, a pretreatment device, a reverse osmosis membrane device, and an evaporative concentration device.
  • the step of generating electric power and exhaust heat by the gas turbine power generation device, the step of generating steam by the exhaust heat of the gas turbine power generation device by the exhaust heat recovery boiler, and the raw water using the pretreatment device A step of pre-treatment, a step of separating water after pre-treatment via the pre-treatment device into permeated water and non-permeated water using the reverse osmosis membrane device, and steam generated in the exhaust heat recovery boiler
  • a heat source it has the process of producing
  • the site for the associated water treatment facility in the CBM production facility can be reduced, and the facility cost can be greatly reduced.
  • waste can be reduced and stable operation can be realized.
  • the site for the associated water treatment facility in the CBM production facility be reduced and the operation with reduced waste can be realized, but also the entire facility can be utilized by using the exhaust heat of the power generation facility. This makes it possible to efficiently use resources and reduce operating costs.
  • FIG. 1 is a schematic diagram showing a configuration of a concentration plant according to a first embodiment of the present invention.
  • the present embodiment is an example in the case where the accompanying water of a CBM production plant is targeted as raw water.
  • the raw water may be water other than the accompanying water (for example, industrial wastewater, groundwater, salt lake water, etc.), or seawater.
  • a brine concentrating plant denoted as a whole by reference numeral 100 includes a pretreatment facility 3, a reverse osmosis membrane concentration facility 4 (reverse osmosis membrane device), a storage tank 5, and an evaporation concentration facility 6 (evaporation concentration device). And the concentrated water tank 7 and the precipitation part 10 (precipitation apparatus).
  • the accompanying water 20 is pretreated water 21 from which the solid and soluble substances are removed or the water temperature and pH are adjusted.
  • the purpose of the pretreatment is to prevent concentration / precipitation of calcium carbonate or the like on the membrane surface of the reverse osmosis membrane concentration equipment 4.
  • the pH of the accompanying water 20 is usually 7 to less than 10, and when the pH is adjusted in the pretreatment, it is generally adjusted to about 6 to 7, although it varies depending on the membrane used, the water temperature, and the like.
  • the pretreated water 21 flows into the reverse osmosis membrane concentration equipment 4 and is separated into permeated water 22 and membrane concentrated water 24.
  • the permeated water 22 is used as fresh water.
  • the membrane concentrated water 24 contains calcium carbonate, silica, and the like, which are components of the accompanying water 20.
  • All of the evaporated and concentrated feed water 25 flows into the evaporated and concentrated equipment 6 and is separated into condensed water 26 and evaporated and concentrated water 27.
  • the condensed water 26 is used as fresh water.
  • the evaporated concentrated water 27 is stored in the concentrated water tank 7.
  • the evaporated concentrated water 27 stored in the concentrated water tank 7 is preferably evaporated to dryness at an appropriate timing thereafter.
  • the evaporative concentration facility 6 is, for example, a multi-effect evaporator having a plurality of evaporators.
  • the multi-effect evaporator for example, the one described in Patent Document 1 (Japanese Patent Application Laid-Open No. 2004-41850) can be used.
  • Patent Document 1 Japanese Patent Application Laid-Open No. 2004-41850
  • the evaporative concentration facility 6 includes a plurality of evaporators, there is a problem that insoluble salts adhere as scales to the inner wall surface of each evaporator.
  • the insoluble salt is precipitated as fine crystals floating in water in the precipitation unit 10 in advance, so that the insoluble salt is grown as a nucleus in the evaporator.
  • scale deposition / growth on the wall surface of the subsequent evaporator can be avoided, stable operation can be realized, and the amount of chemical used and labor for cleaning the inside of the can can be reduced.
  • FIGS. 2A to 2D Examples of the apparatus configuration of the precipitation unit 10 are shown in FIGS. 2A to 2D.
  • the membrane concentrated water 24 flows into the mixing water tank 40 and is mixed with the alkaline agent added from the chemical injection equipment 41 to precipitate an insoluble salt such as calcium carbonate.
  • an insoluble salt such as calcium carbonate.
  • caustic soda or slaked lime can be used as the alkaline agent.
  • the mixing water tank 40 is not provided, and mixing can be performed by a pipe line. In this case, a line mixer may be installed.
  • a line mixer may be installed.
  • calcium carbonate can be easily deposited.
  • the silica solubility increases and the silica scale generation potential can be reduced.
  • calcium ions may be injected.
  • a heating tank 42 (heater) may be provided in the previous stage of mixing the alkaline agent, and the membrane concentrated water 24 may be heated.
  • the solubility of calcium carbonate decreases and precipitation is promoted.
  • You may provide only the heating tank 42, without providing the mixing water tank 40 and a line mixer.
  • a gas 35 containing CO 2 may be injected into the mixing water tank 40a before the addition of the alkaline agent.
  • the pH is adjusted to be slightly acidic by dissolving CO2
  • the solubility of slaked lime is increased and the amount of calcium ions can be increased, so that precipitation of calcium carbonate can be promoted.
  • the membrane concentrated water 24 that has flowed into the mixing water tank 40 b is taken into the fine bubble generating device 43, and the gas 36 containing air or CO 2 is added to the membrane concentrated water 24 in the fine bubble generating device 43.
  • fine bubbles having a diameter of about 50 micrometers or less may be generated, and the fine bubbles may be returned to the mixing water tank 40b. In this case, fine crystal nuclei are generated with rapid dissolution of fine bubbles, and precipitation of insoluble salt can be promoted.
  • the accompanying water 20, the permeated water 22, and the condensed water 26 before flowing into the pretreatment facility 3 may be used as the cooling water 28.
  • the salt permeability in the reverse osmosis membrane concentration facility 4 increases as the water temperature increases when the pretreatment facility 3 is supplied and processed by the reverse osmosis membrane concentration facility 4. Therefore, it is desirable that the permeated water 22 be maintained within a range where the water quality can be maintained at a necessary level.
  • the former has a higher salt content than the latter, and therefore may be mixed and used according to the purpose of use.
  • the permeated water 22 as a raw material for drinking water and the condensed water 26 as industrial water that requires a low salt content.
  • the accompanying water 20 is used as the cooling water 28 as mentioned above, the accompanying water 20 is heated and the salt content of the permeated water 22 may increase by the heating. In this case, the quality of the water can be adjusted by mixing the accompanying water 20 after heating with the condensed water 26.
  • FIG. 3A is a conceptual diagram of the effect of the present embodiment.
  • the vertical axis is the expected value of the ratio when the installation cost of the evaporation pond is compared with the conventional evaporation pond method and the reverse osmosis membrane concentration method.
  • the water to be treated in the evaporating pond is reduced to about 1/10 compared to the evaporating basin method without concentration. Installation costs will be reduced accordingly.
  • the evaporating concentrated water 27 stored in the concentrated water tank 7 is evaporated to dryness, the evaporating pond is unnecessary and the evaporating pond installation cost is zero.
  • an evaporating pond may be provided, and also in this case, the installation area of an evaporating pond can be reduced significantly and the installation cost of an evaporating pond can be reduced.
  • the site for the associated water treatment facility in the CBM production facility can be reduced, and the equipment cost can be greatly reduced.
  • waste can be reduced and stable operation can be realized.
  • FIG. 4 is a schematic diagram showing a configuration of a concentrated desalination power plant according to the second embodiment of the present invention.
  • a gas turbine power generation facility is additionally provided in the concentration plant in the first embodiment.
  • the concentrated desalination power plant includes a gas turbine power generation device 200 including a gas turbine 1 that uses hydrocarbon, for example, LNG as a main fuel, and an exhaust heat recovery boiler 2 that generates steam by the exhaust heat of the power generation device 200. And a concentrating device 300.
  • the concentration apparatus 300 for example, the concentration plant 100 of the first embodiment is used.
  • the gas turbine 1 includes a compressor 1a, a turbine 1b, a combustor 8, a generator 9, and an exhaust gas treatment tower 12.
  • the air 30 is compressed by the compressor 1 a to become compressed air 30 a, flows into the combustor 8, and is mixed with the fuel gas 33.
  • the fuel gas 33 is combusted in the combustor 8 to become combustion gas, and flows out as exhaust gas 31 after rotating the turbine 1b.
  • the generator 9 receives electricity from the turbine 1b and generates electricity.
  • the exhaust gas 31 flows into the exhaust heat recovery boiler 2, generates steam by exhaust heat, is sent to the exhaust gas treatment tower 12, is processed by the exhaust gas treatment tower 12, and is diffused into the atmosphere.
  • the heat exchanger 2a of the first steam supply system 32A is arranged. Circulating water flows through the first steam supply system 32 ⁇ / b> A, and the exhaust gas 31 that has flowed into the exhaust heat recovery boiler 2 supplies heat to the circulating water through the heat exchanger 2 a to change the phase to the steam 32.
  • the steam 32 flows into the evaporative concentration facility 6 and heats the evaporative concentrated feed water 25 to change the phase to steam.
  • the generated steam is cooled by cooling water 28 to become condensed water 26.
  • the steam 32 is deprived of heat and returns to the circulating water.
  • the configuration of the concentration apparatus 300 (concentration plant 100) is the same as that of the first embodiment. That is, the accompanying water 20 is subjected to removal of solid / soluble substances by the pretreatment facility 3 or the water temperature / pH and the like are adjusted to become pretreated water 21.
  • the pretreated water 21 flows into the reverse osmosis membrane concentration equipment 4 and is separated into permeated water 22 and membrane concentrated water 24.
  • the permeated water 22 is used as fresh water.
  • the membrane concentrated water 24 flows into the precipitation part 10 and is mixed with an alkaline agent to precipitate insoluble components, and then flows into the storage tank 5.
  • Pretreatment wastewater 23 containing solid and soluble substances removed from the accompanying water 20 by the pretreatment device 3 also flows into the storage tank 5 and is mixed with the membrane concentrated water 24 to become the evaporated concentrated supply water 25.
  • the evaporated concentrated feed water 25 flows into the evaporated concentration facility 6 and is separated into condensed water 26 and evaporated concentrated water 27.
  • the condensed water 26 is used as fresh water.
  • the evaporated concentrated water 27 is stored in the concentrated water tank 7.
  • the exhaust gas 31 of the gas turbine 1 may be used as the heat source of the heating tank 42. Moreover, you may utilize the waste gas 31 of the gas turbine 1 as the gas 33 containing CO2 in the example of FIG. 2C and FIG. 2D.
  • the exhaust gas 31 may be after heat exchange in the exhaust heat recovery boiler 2.
  • FIG. 4 is an example in which the exhaust gas 31 after heat exchange in the exhaust heat recovery boiler 2 is supplied to the precipitation unit 10.
  • the power generated by the generator 9 can be used as a power source for the pretreatment facility 3 and the reverse osmosis membrane concentration facility 4.
  • LNG produced from CBM can be used.
  • FIG. 5 shows an example (third embodiment) in which the amount of heat of the steam 32 is supplied to the evaporative concentration facility 6 through the indirect heat exchanger 13.
  • the first steam supply system includes a primary steam supply system 32B including a heat exchanger 2a, a secondary evaporator supply system 32C that supplies steam to the evaporation concentration facility 6, and a primary steam supply system 32B.
  • an indirect heat exchanger 13 that generates steam by supplying heat to the circulating water of the secondary evaporator supply system 32C. Since the system 32B of the steam 32 and the system 32C flowing into and out of the evaporative concentration facility 6 are separated, salt is not mixed into the steam 32, and corrosion of the exhaust heat recovery boiler 2 can be avoided.
  • FIG. 6 shows an example (fourth embodiment) when the steam generated in the exhaust heat recovery boiler 2 is injected into the combustor 8.
  • the heat source generated by the exhaust heat recovery boiler 2 is also used as the heat source of the heating tank 42 (FIG. 2B) of the precipitation unit 10.
  • FIG. 6 in the exhaust heat recovery boiler 2, there are a heat exchanger 2a of the first steam supply system 32A, a heat exchanger 2b of the heat source supply system 202A, and a heat exchanger 2c of the second steam supply system 34A.
  • the steam 32 to the evaporative concentration facility 6 the heat source 210 to the heating tank 42 of the precipitation unit 10, and the steam 34 to the combustor 8 are generated separately.
  • the heat source 210 to the heating tank 42 of the precipitation unit 10 may be steam-water or hot water-cold water. Moreover, substances other than water can also be used.
  • a normally closed valve 11 is provided in a pipeline through which the steam 34 of the second steam supply system 34 ⁇ / b> A flows, and the valve 11 is opened to supply the steam 34 to the combustor 8.
  • the steam 34 is supplied to the combustor 8
  • the mass flow rate of the combustion gas flowing into the turbine 1b increases, and the power generation amount of the generator 9 can be increased.
  • the consumption amount of the fuel gas 33 can be reduced.
  • the steam 34 is mixed into the exhaust gas 31 and is released to the atmosphere via the exhaust heat recovery boiler 2 and the exhaust gas treatment tower 12.
  • the permeated water 22 and the condensed water 26 are generated as fresh water, and water is supplied to the heat exchanger 2 c in the exhaust heat recovery boiler 2 using these.
  • FIG. 6 shows an example in which a part of the condensed water 26 is taken out and supplied to the heat exchanger 2c.
  • This embodiment is extremely effective for treatment of accompanying water from CBM.
  • Hydrocarbons such as methane produced from CBM can be used as fuel for the gas turbine 1.
  • the electric power generated by the gas turbine 1 can be used in the concentrator 100. Surplus power can be supplied to the outside.
  • the associated water concentration from CBM is as small as about 1/5 of the seawater concentration, and the osmotic pressure is small. Therefore, the power consumption of the reverse osmosis membrane concentration equipment 4 can be kept small in the present invention in which the reverse osmosis membrane concentration equipment 4 is placed in the front stage and the evaporation concentration equipment 6 is placed in the rear stage.
  • Steam 32 to be supplied to the evaporative concentration facility 6 can be generated by exhaust heat of the gas turbine 1.
  • the pre-stage and the post-stage can be combined to greatly reduce the volume, and the electric power and exhaust heat from the gas turbine 1 can be used.
  • the accompanying water from CBM contains more carbonate, which is an underground rock component, than seawater.
  • the carbonate precipitates when the temperature is raised, causing contamination of the heat transfer surface of the evaporative concentration facility 6.
  • the heating tank 42 is provided in the precipitation unit 10 and heated by the heat source 210, the carbonate is precipitated and separated, and the concentrated water is sent to the evaporation concentration facility 6.
  • the exhaust heat of the gas turbine 1 is also used as the heat source of the heat source 210.
  • the opening degree of the valve 11 is adjusted in accordance with fluctuations in the accompanying water treatment amount and power supply amount. For example, when the accompanying water treatment amount is small and the power supply amount is large, the valve 34 is opened and the steam 34 sent to the combustor 8 is increased. In this case, the amount of heat recovered by the exhaust heat recovery boiler 2 is often used to generate the steam 34, and the heating amount of the steam 32 and the heat source 210 is reduced.
  • FIG. 3B is a conceptual diagram of the effect of the present embodiment.
  • the vertical axis is the expected value of the ratio when the operation cost of the concentration plant is compared with the conventional evaporating basin method and the reverse osmosis membrane concentration method.
  • the conventional evaporating basin method uses solar concentration, so the operating cost is 0.
  • the conventional reverse osmosis membrane concentration method requires operating costs such as power and membrane replacement for reverse osmosis membrane concentration equipment. Is required.
  • Pretreatment drainage 24 Membrane concentrated water 25 ... Evaporated concentrated feed water 26 ... Condensed water 27 ... Evaporated concentrated water 28 ... Cooling water 30 ... Air 30a ... Compressed air 31 ... Exhaust gas 32 ... Steam 32A ... first steam supply system 33 ... fuel gas 34 ... steam 34A ... second steam supply system 35 ... CO2-containing gas 40 ... mixed water tank 41 ... chemical injection equipment 42 ... Heating tank (heater) 43 ... Microbubble generator 100 ... Concentration plant (concentrator) 200 ... Gas turbine power generation device 210 ... Heat source 210A ... Heat source supply system 300 ... Concentration device

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Hydrology & Water Resources (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Nanotechnology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Removal Of Specific Substances (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention consiste à utiliser un dispositif de dessalement fonctionnant par un procédé à membrane et un dispositif de concentration fonctionnant par un procédé de vaporisation en combinaison pour de cette manière concentrer de façon stable de l'eau contenant un sel, tel que de l'eau d'accompagnement, à un faible coût d'équipement et séparer l'eau en eau douce et en sel. L'eau d'accompagnement (20) est traitée dans un équipement de prétraitement (3) pour enlever les substances solides et les substances dissoutes de celle-ci, pour produire de cette manière de l'eau prétraitée (21). L'eau prétraitée (21) s'écoule dans un équipement de concentration à membrane d'osmose inverse (4) et est séparée en eau de filtrat (22) et eau concentrée sur membrane (24). L'eau de filtrat (22) est utilisée comme eau douce. L'eau concentrée sur membrane (24) s'écoule dans une partie de précipitation (10), dans laquelle un alcali est mélangé avec celle-ci pour faire précipiter la matière insoluble. Après cela, cette eau concentrée sur membrane s'écoule dans une cuve de stockage (5) conjointement avec de l'eau rejetée (23) provenant du prétraitement et envoyée à partir du dispositif de prétraitement (3), ce qui donne de l'eau d'alimentation (25) pour la concentration par vaporisation. L'eau d'alimentation (25) s'écoule dans l'équipement de concentration par vaporisation (6) et est séparée en eau condensée (26) et eau concentrée par vaporisation (27). L'eau condensée (26) est utilisée comme eau douce. L'eau concentrée par vaporisation (27) est stockée dans une cuve d'eau concentrée (7). Dans l'équipement de concentration par vaporisation (6), la concentration est effectuée à l'aide, comme source de chaleur, de la vapeur d'eau produite dans une chaudière de récupération de chaleur (2).
PCT/JP2010/061803 2010-07-12 2010-07-12 Installation de concentration, installation pour la production d'eau douce par concentration et pour la production d'énergie électrique, procédé de concentration et procédé de fonctionnement d'une installation pour la production d'eau douce par concentration et de production d'énergie électrique Ceased WO2012008013A1 (fr)

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AU2010357340A AU2010357340B9 (en) 2010-07-12 2010-07-12 Concentration plant, plant for producing fresh water by concentration and for generating electric power, concentration method, and method for operating plant for producing fresh water by concentration and for generating electric power
PCT/JP2010/061803 WO2012008013A1 (fr) 2010-07-12 2010-07-12 Installation de concentration, installation pour la production d'eau douce par concentration et pour la production d'énergie électrique, procédé de concentration et procédé de fonctionnement d'une installation pour la production d'eau douce par concentration et de production d'énergie électrique
JP2012524356A JP5495403B2 (ja) 2010-07-12 2010-07-12 濃縮プラント、濃縮造水発電プラント、濃縮方法及び濃縮造水発電プラントの運転方法

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