CN104379512A - Ammonia treatment system - Google Patents
Ammonia treatment system Download PDFInfo
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- CN104379512A CN104379512A CN201380025991.2A CN201380025991A CN104379512A CN 104379512 A CN104379512 A CN 104379512A CN 201380025991 A CN201380025991 A CN 201380025991A CN 104379512 A CN104379512 A CN 104379512A
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- water
- ammonia
- chloride ion
- electrolysis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
- C02F1/4674—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation with halogen or compound of halogens, e.g. chlorine, bromine
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4612—Controlling or monitoring
- C02F2201/46125—Electrical variables
- C02F2201/4614—Current
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/29—Chlorine compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/40—Liquid flow rate
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/08—Corrosion inhibition
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
An ammonia treatment system comprises: a boiler facility for collecting heat; an ammonia injection means for injecting ammonia into a water supply system arranged in the boiler facility; an ammonia concentration measurement means for measuring the concentration of ammonia in blow water coming from the water supply system or the boiler facility; a flow volume measurement means for measuring the volume of the blow water; a receiving vessel for receiving the blow water therein; a chloride ion supply means for introducing an aqueous sodium chloride solution as a chloride ion source into the receiving vessel; an electrolysis vessel for electrolyzing a treated aqueous solution comprising the blow water and the aqueous sodium chloride solution; and a control device for controlling an electric current to be applied in the electrolysis and a treatment time period. In the control device, the necessary chloride amount is calculated on the basis of the concentration of ammonia and the volume of the blow water to control the amount of an electric current to be applied in the electrolysis.
Description
Technical field
The present invention relates to ammonia treatment system, particularly to blowing as the draining from boiler plant the ammonia treatment system that the ammonia contained in water carries out electrolysis treatment.
The application advocates the right of priority of No. 2013-010251st, the Japanese patent application of No. 2012-119933rd, Japanese patent application and the submission on January 23rd, 2013 submitted on May 25th, 2012, and their content is quoted in the application.
Background technology
Such as in fuel-burning power plant, in order to remove the oxygen of the major cause becoming corrosion and the hydrazine used is be evaluated as " chemical substance observing mutagenicity ", therefore adopting safer reductor in recent years, not using the water treatment of reductor.
As the reductor not using hydrazine, there will be a known (such as pH7 ~ pH9) ammonia that the value of hydrogen ion exponent (pH) is increased, but can envision, owing to using ammonia as reductor, the ammonia density from now on from the draining in power station can increase (such as with reference to non-patent literature 1).On the other hand, according to draining regulation, also require to reduce nitrogen, thus expect to tackle as early as possible.
Describe following ammonia treatment system in patent documentation 1: by carrying out electrolysis to the draining of discharging from power station, thus by ammonolysis craft, and determine the terminal of electrolysis by concentration of residual chlorine.
In addition, also the reagent such as known use clorox carrys out the ammonia treatment system of cracked ammonium by chlorine process.
Prior art document
Patent documentation
Patent documentation 1: Japanese Patent No. 4518826 publication
Non-patent literature
Non-patent literature 1: " the de-ヒ De ラ ジ Application へ in firepower プ ラ Application ト water treatment gets Group body ", [online], Mitsubishi Heavy Industries Ltd's skill report Vol.46No.2 (2009), [Heisei retrieval on March 30th, 24], website <
uRL:http: //www.mhi.co.jp/technology/review/pdf/462/462055.pdf>
Summary of the invention
The problem that invention will solve
Such as, but when such as processing the draining from boiler plant, greatly, when the startup that the water yield of blowing water is many, there is electrolysis treatment problem not in time in the water yield of draining, the variation of ammonia density.
In addition, when utilizing the reagent such as clorox to carry out ammonolysis craft, need the space of the clorox tank being provided as strong basicity oxygenant etc., and be difficult to be assembled in existing equipment.
The invention provides a kind of ammonia treatment system being arranged at boiler plant, even if described ammonia treatment system is when the variation of blow down is large, also suitably can carry out the electrolysis treatment of ammonia.
For solving the means of problem
According to the 1st aspect of the present invention, ammonia treatment system has: boiler plant, for carrying out recovery of heat; Ammonia injection unit, injects ammonia to the water feeding system in described boiler plant; Ammonia concentration determination unit, measures the ammonia density blowing water from described water feeding system or described boiler plant; Flow measurement unit, blows the water yield of water described in mensuration; Receiver, blows water described in acceptance; Chloride ion feed unit, imports the sodium chloride aqueous solution as chloride ion source to described receiver; Electrolyzer, carries out electrolysis to the process water blowing water and described sodium chloride aqueous solution described in comprising; And control device, electric current when controlling described electrolysis and treatment time.Described control device calculates required chlorine dose based on described ammonia density and the described water meter blowing water, and magnitude of current when controlling electrolysis.
According to above-mentioned formation, control electrolysis based on the water feeding system of boiler plant or the ammonia density blowing water and the water yield of blowing water.Therefore, even if when the variation of blow down is large, the draining benchmark of ammonia density also can be met.
In above-mentioned ammonia treatment system, have the residual chlorine determination unit of the concentration of residual chlorine measuring described process water in electrolysis, above-mentioned control device can decide the terminal of electrolysis according to described concentration of residual chlorine.
According to above-mentioned formation, by the index terminated as electrolysis by concentration of residual chlorine, the draining benchmark of the ammonia density of discharging can be controlled thus more accurately.
In above-mentioned ammonia treatment system, have the chloride ion concentration determination unit of the chloride ion concentration measuring described process water, above-mentioned control device can control the import volume of described sodium chloride aqueous solution in the mode making described chloride ion concentration reach more than normality.
According to above-mentioned formation, the chloride ion required for electrolysis stably can be guaranteed.
In above-mentioned ammonia treatment system, can arrange between described receiver and electrolyzer to process water at least partially in the concentrating unit that concentrates of the ammonia that contains.
According to above-mentioned formation, the ammonia importing to electrolyzer utilizes concentrating unit to concentrate, and can reduce the chlorine of needs thus, therefore, it is possible to reduce the feed rate as the chloride ion of raw material.
According to the 2nd aspect of the present invention, ammonia treatment system possesses: boiler plant, for carrying out recovery of heat; Ammonia injection unit, injects ammonia to the water feeding system in described boiler plant; Ammonia concentration determination unit, measures the ammonia density blowing water from described water feeding system or described boiler plant; Flow measurement unit, blows the water yield of water described in mensuration; Electrolyzer, possesses the chloride ion feed unit imported as the sodium chloride aqueous solution in chloride ion source, and carries out electrolysis to described sodium chloride aqueous solution; Tempering tank, blows water described in acceptance and accepts the process water from described electrolyzer; And control device, electric current when controlling described electrolysis and treatment time.Described control device calculates required chlorine dose based on described ammonia density and the described water meter blowing water, and magnitude of current when controlling electrolysis.
According to above-mentioned formation, control electrolysis based on the water feeding system of boiler plant or the ammonia density blowing water and the water yield of blowing water.Therefore, even if when the variation of blow down is large, the draining benchmark of ammonia density also can be met.
In addition, owing to sodium chloride aqueous solution being imported to electrolyzer under the state that chloride ion concentration is high, therefore, it is possible to increase current density.
In above-mentioned ammonia treatment system, have the residual chlorine determination unit of the concentration of residual chlorine measuring described process water in electrolysis, above-mentioned control device can decide the terminal of electrolysis according to described concentration of residual chlorine.
In above-mentioned ammonia treatment system, can possess: the desalting plant being arranged on the downstream side of described tempering tank; With a condensed water recycling pipe arrangement part for the condensed water utilizing described desalting plant to concentrate being supplied to electrolyzer as chloride ion source.
According to above-mentioned formation, by carrying out the formation supplied after being set as the chloride ion being supplied to electrolyzer to reclaim from desalting plant, the supply cost of chloride ion can be reduced thus.
Invention effect
According to above-mentioned ammonia treatment system, control electrolysis based on the water feeding system of boiler plant or the ammonia density blowing water and the water yield of blowing water.Therefore, even if when the variation of blow down is large, the draining benchmark of ammonia density also can be met.
Accompanying drawing explanation
Fig. 1 is the overall system view of the combined cycle power stations of the ammonia treatment system possessed involved by the first embodiment of the present invention.
Fig. 2 is the detailed system figure of the ammonia treatment system involved by the first embodiment of the present invention.
Fig. 3 is the detailed system figure of the ammonia treatment system involved by the second embodiment of the present invention.
Fig. 4 is the detailed system figure of the ammonia treatment system involved by the 3rd embodiment of the present invention.
Fig. 5 is the detailed system figure of the ammonia treatment system involved by the 4th embodiment of the present invention.
Fig. 6 is the detailed system figure of the ammonia treatment system involved by the 5th embodiment of the present invention.
Fig. 7 is the detailed system figure of the ammonia treatment system involved by the 6th embodiment of the present invention.
Fig. 8 is the detailed system figure of the ammonia treatment system involved by the 7th embodiment of the present invention.
Fig. 9 is the detailed system figure of the ammonia treatment system involved by the 8th embodiment of the present invention.
Figure 10 is the detailed system figure of the ammonia treatment system involved by the 9th embodiment of the present invention.
Figure 11 is the detailed system figure of the ammonia treatment system involved by the tenth embodiment of the present invention.
Embodiment
(the first embodiment)
Referring to accompanying drawing, the first embodiment of the present invention is described in detail.
As shown in Figure 1, the ammonia treatment system 1 of present embodiment is arranged at the combined cycle power stations 2 possessing heat recovery boiler 3.Combined cycle power stations 2 has: internal combustion turbine 4, the heat recovery boiler 3 be sent to from the waste gas of internal combustion turbine 4, steam turbine 5, driven and carry out the generator (not shown) that generates electricity and blow to what discharge from heat recovery boiler 3 the ammonia treatment system 1 that water processes by the rotary driving force of internal combustion turbine 4 and steam turbine 5.
Heat recovery boiler 3 possesses: hyperbaric heating unit 6, middle pressure heating unit 7 and low-pressure heating unit 8.In heat recovery boiler 3, produce steam by hyperbaric heating unit 6, middle pressure heating unit 7 and low-pressure heating unit 8, the steam of generation is delivered to steam turbine 5 and is done work by steam turbine 5.The exhaust of steam turbine 5 device 9 that is condensed condenses and condensation, and utilizes condensation pump 10 to import heat recovery boiler 3.The water of condensation utilizing condenser 9 to condense delivers to heat recovery boiler 3 via giving waterline 11.
Hyperbaric heating unit 6 has: high-pressure superheater 13, high pressure cylinder 14, high pressure evaporator 15 and high pressure joint carbon device 16.The water of high pressure cylinder 14 crosses thermal cycling at the high pressure evaporator 15 be configured in heat recovery boiler 3, in high pressure cylinder 14, produce high pressure steam.The high pressure steam produced at high pressure cylinder 14 undertaken by the high-pressure superheater 13 be configured in heat recovery boiler 3 overheated after be directed to steam turbine 5.
Middle pressure heating unit 7 has: middle pressure superheater 17, middle pressure cylinder 18, middle pressure vaporizer 19 and middle pressure joint carbon device 20.The water of middle pressure cylinder 18 presses vaporizer 19 to cross thermal cycling being configured in heat recovery boiler 3, generation middle pressure steam middle pressure cylinder 18 in.The middle pressure steam produced at middle pressure cylinder 18 is directed to reheater 21 by middle pressure superheater 17, after reheater 21 carries out reheating, be directed to steam turbine 5.Steam from middle pressure superheater 17 is directed to internal combustion turbine 4 side as the cooling purposes of the high-temperature portion (burner, blade etc.) of internal combustion turbine 4.
Low-pressure heating unit 8 has: low-pressure superheater 23, low pressure cylinder 24, low pressure evaporator 25 and low pressure joint carbon device 26.The water of low pressure cylinder 24 crosses thermal cycling at the low pressure evaporator 25 be configured in heat recovery boiler 3, in low pressure cylinder 24, produce low-pressure steam.The low-pressure steam produced at low pressure cylinder 24 imports to steam turbine 5 by low-pressure superheater 23.
The water of condensation 27 carrying out condenser 9 is fed into low pressure cylinder 24 by degasser 28 and low pressure joint carbon device 26.The outlet side of low pressure joint carbon device 26 be provided with is connected with high pressure cylinder 14 and middle pressure cylinder 18 to waterline 29.By giving waterline 29, feeding water to high pressure cylinder 14 via high pressure water pump 30, feeding water to middle pressure cylinder 18 via middle pressure service pump 31.That is, feed water to low pressure cylinder 24 and middle pressure cylinder 18 and high pressure cylinder 14 concurrently.Low pressure cylinder 24 is regarded as the cylinder of low-tension side unit.Middle pressure cylinder 18 and high pressure cylinder 14 are regarded as the cylinder of high-tension side unit.
It should be noted that, save the recycle pump 32 of the feedwater of carbon device 26 from low pressure giving waterline 11 and be provided with to circulate to the streamline between waterline 29.
In addition, at the inlet side of degasser 28, a part for water of condensation 27 gets back to condenser 9, and after giving waterline 11 branch, a part of water gets back to degasser 28 side.Each machine in heat recovery boiler 3 be configured to an example, number of units, the configuration of joint carbon device, superheater suitably can be changed according to the performance etc. of internal combustion turbine 4.
As the ammonia injection unit 34 giving in waterline 11 ammonia being provided with injection pH adjusting agent of water feeding system.Injected the ammonia of specified amount by ammonia injection unit 34 as pH regulator purposes to feedwater, make the pH of the feedwater in low pressure cylinder 24 reach more than 9.0, and make ammonia density reach more than 0.5ppm.
Generally speaking, the pH of feedwater lower than 9.0 time, likely there is burn into due to flowing and corrode.Therefore, the pH of the feedwater in low pressure cylinder 24 is made to be more than 9.0.The pressure of the feedwater in low pressure cylinder 24 is lower than the pressure of the feedwater of high pressure cylinder 14 and middle pressure cylinder 18, ammonia is easy to evaporate and the more low gas phase side (being difficult to be mixed in liquid phase) that is more easily mixed in of pressure, therefore, namely the value of the partition ratio of gas phase and liquid phase is high, therefore by making the pH of the feedwater in low pressure cylinder 24 be more than 9.0, the pH of the feedwater of high pressure cylinder 14 and middle pressure cylinder 18 can be made thus to be value higher than 9.0.
In addition, condenser 9 outlet side give the multiple ammonia concentration determination devices 47,48,49 waterline 11 being provided with the ammonia density for measuring feedwater.Specifically, ammonia concentration determination device 47 is being given on waterline 11, and is arranged between condensation pump 10 and ammonia injection unit 34.Ammonia concentration determination device 48 is arranged between ammonia injection unit 34 and degasser 28.Ammonia concentration determination device 49 is arranged at degasser 28 and low pressure saves between carbon device 26.
Giving on waterline 11, and branching out between condenser 9 and condensation pump 10 and blow line 35.Blow line 35 be for discharge produce in the combined cycle power stations 2 comprising heat recovery boiler 3 as containing the circuit blowing water of ammonia draining.
In addition, the flow rate-measuring device 53 being provided with and measuring and blow the water yield of water is blowed in line 35.The water yield of blowing water measured by flow rate-measuring device 53 is sent to control device 41.
Ammonia treatment system 1 with blow line 35 and be connected.Ammonia treatment system 1 blow water by storage and be imported with the receiver 36 of seawater, electrolytic processing apparatus 37, control device 41 form.
Electrolytic processing apparatus 37 possesses: be imported with by the circulation adjustment tank 38 of blowing the process water that water and seawater are formed flowed out from receiver 36, be imported with the electrolyzer 39 of the adjustment liquid of self-circulation adjustment tank 38 and the recycle pump 40 for cyclic electrolysis treatment solution, electrolytic processing apparatus 37 is the formations making the electrolysis treatment liquid in electrolyzer 39 after process be recycled to circulation adjustment tank 38.
As shown in Figure 2, receiver 36 is connected with the seawater lead-in wire 42 (chloride ion feed unit) for importing the seawater (chloride ion concentration: about 18,000mg/ liters) as chloride ion source.Seawater lead-in wire 42 is provided with sea-water pump 46.This sea-water pump 46 formed can controlled device 41 control formation.
It should be noted that, as long as comprise the liquid of chloride ion by the liquid of seawater lead-in wire 42 importing, be not limited to seawater.Such as can for importing the formation of sodium chloride aqueous solution from seawater lead-in wire 42.Like this, by importing sodium chloride aqueous solution, also can be corresponding with the facility being difficult to obtain seawater.
In addition, circulation adjustment tank 38 is provided with: measure the pH determinator 43 of the pH of process water, measure the chloride ion concentration determinator 44 of the chloride ion concentration of the temperature measuring apparatus 51 of the temperature of process water and mensuration process water.
Electrolyzer 39 has: be immersed at least one pair of electrode in the treatment solution in electrolyzer 39 and the continuous-current plant 45 with this Electrode connection.Between these electrodes, utilize continuous-current plant 45 to apply volts DS, carry out the electrolysis of the treatment solution in groove thus.
In addition, electrolyzer 39 is provided with the residual chlorine determinator 52 of the concentration of the residual chlorine measured in electrolyzer 39.Residual chlorine determinator 52 is connected with control device 41.
Then, the effect of the ammonia treatment system 1 of present embodiment is described.
First, import in receiver 36 and blow water containing ammonia, and imported containing the seawater of sodium-chlor by the water that blows of seawater lead-in wire 42 to storage.
Then, to form and process water containing chloride ion is supplied to electrolytic processing apparatus 37 with fixing speed by blowing water and seawater.
At this, process water is fed into the circulation adjustment tank 38 of electrolytic processing apparatus 37, is then fed into electrolyzer 39.In electrolyzer 39, apply assigned voltage between the electrode in electrolyzer 39, supply electric current in the mode of the current density reaching regulation, at anode, the electrode reaction of through type (1) produces chlorine (Cl
2).
Cl
-→Cl
2+2e
-…(1)
Then, the Cl produced in the treatment solution in groove
2the solution reaction of through type (2) and generate hypochlorous acid (HClO).
Cl
2+H
2O→HClO+H
++Cl
-…(2)
When there is ammonia in process water, with hypochlorous acid generation solution reaction, through type (3), formula (4) generate chloramines (NH
2cl, NHCl
2).
NH
3+HClO→NH
2Cl+H
2O…(3)
NH
2Cl+HClO→NHCl
2+H
2O…(4)
Then, the solution reaction of the chloramines through type (5) generated in above-mentioned formula (3) and formula (4) decomposes to nitrogen (N
2).
NH
2Cl+NHCl
2→N
2+3H
++3Cl
-…(5)
Control device 41 controls continuous-current plant 45 based on the ammonia density measured by ammonia concentration determination device 47,48,49 and the water yield of blowing water that measured by flow rate-measuring device 53, thus controls current value and the treatment time of electrolytic processing apparatus 37.That is, control device 41 can control the electric current of supply unit by the mode of the hypochlorous acid concentration adapted with the water yield and ammonia density that reach with blow water, carries out the ammonia treatment in ammonia treatment system 1 thus accurately.
It should be noted that, ammonia concentration determination device can for being arranged at the formation at 1 place, now, preferentially closer to condenser 9 ammonia concentration determination device 47 position is set.
Utilize the treatment time of the electrolysis treatment of electrolytic processing apparatus 37, except ammonia density, the concentration controlled device 41 also based on the residual chlorine measured by residual chlorine determinator 52 controls, and at the end of process, process water is suitably gathered rear releasing.
Specifically, whether the concentration of control device 41 pairs of residual chlorines reaches more than set(ting)value and judges.Then, can judging that ammonia density reaches the concentration of the residual chlorine of below prescribed value based on the testing setup carried out in advance, stopping electrolysis when reaching the set(ting)value of concentration of this residual chlorine.Process water is released by not shown residual chlorine treater.
That is, for the treatment time of the electrolysis set according to ammonia density, even if when ammonia density does not suitably reduce, also the treatment time can be extended until ammonia density reaches below prescribed value.
In addition, the amount of seawater controls according to the measured value of pH determinator 43.That is, control device 41 is based on the input from pH determinator 43, controls sea-water pump 46 in the mode making the pH of the process water in circulation adjustment tank 38 reach pH7 ~ pH9, the amount of adjustment seawater.
Similarly, the amount of seawater controls according to the measured value of temperature measuring apparatus 51.That is, control device 41 controls sea-water pump 46 in the mode making the temperature of process water and reach 20 DEG C ~ 50 DEG C, the amount of adjustment seawater.
Similarly, the amount of seawater controls based on the measured value of chloride ion concentration determinator 44.
That is, control device 41 rises above mode control sea-water pump 46 to make the chloride ion concentration of process water reach 2,000mg/, the amount of adjustment seawater.
According to above-mentioned embodiment, control electrolysis based on the water feeding system of heat recovery boiler 3 or the ammonia density blowing water and the water yield of blowing water.Thus, even if when the variation of blow down is large, the draining benchmark of ammonia density also can be met.
In addition, by the index concentration of residual chlorine terminated as electrolysis, the ammonia density of discharging can be controlled more accurately.
In addition, owing to rising the import volume that above mode adjusts seawater, therefore, it is possible to stably guarantee the chloride ion required for electrolysis to make the chloride ion concentration of process water reach 2,000mg/.
In addition, owing to adjusting the import volume of seawater in the mode making the pH of the process water in electrolytic processing apparatus 37 reach pH7 ~ pH9, therefore, it is possible to suppress the generation of chlorine, three chloramines, thus carry out the decomposition of ammonia efficiently.
In addition, when the temperature of process water reaches a high temperature, the chlorine of generation becomes easy volatilization, but owing to adjusting the import volume of seawater in the mode making the temperature of process water reach 20 DEG C ~ 50 DEG C, therefore, it is possible to prevent the decline of the ammonia removing performance caused by volatilization of chlorine.
In addition, owing to not needing the space arranging clorox tank etc., be therefore easy to be assembled in existing device.
(the second embodiment)
Referring to accompanying drawing, the second embodiment of the present invention is described in detail.
Fig. 3 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the first above-mentioned embodiment centered by carry out describe, its explanation is eliminated for identical part.
As shown in Figure 3, present embodiment ammonia treatment system 1B by electrolytic processing apparatus 37B, with blow line 35 be connected and preserve blow water receiver 36, be imported with the process water that flows out from receiver 36 and form from the tempering tank 55 of the process water of electrolytic processing apparatus 37B and control device 41.
Receiver 36 is connected with the seawater lead-in wire 70 for importing the seawater as chloride ion source.Seawater lead-in wire 70 is provided with sea-water pump 71.This sea-water pump 71 formed can controlled device 41 control formation.In addition, receiver 36 is provided with the temperature measuring apparatus 72 measuring and blow the temperature of water.
Electrolytic processing apparatus 37B possesses: the circulation adjustment tank 38B being imported with seawater, the electrolyzer 39 of adjustment liquid being imported with self-circulation adjustment tank 38B and the recycle pump 40 for cyclic electrolysis treatment solution.Electrolytic processing apparatus 37B is the formation making the electrolysis treatment liquid in electrolyzer 39 after process be recycled to circulation adjustment tank 38B.
Circulation adjustment tank 38B is connected with the seawater lead-in wire 42B for importing the seawater as chloride ion source.Seawater lead-in wire 42B is provided with sea-water pump 46, and this sea-water pump 46 can control by controlled device 41.
In addition, circulation adjustment tank 38B is provided with: measure the pH determinator 43 of the pH of process water, measure the chloride ion concentration determinator 44 of the chloride ion concentration of the temperature measuring apparatus 51 of the temperature of process water and mensuration process water.
Then, the effect of the ammonia treatment system 1B of present embodiment is described.
Seawater containing sodium-chlor is imported directly into the circulation adjustment tank 38B of electrolytic processing apparatus 37B, generates hypochlorous acid (HClO).Being imported into the tempering tank 55 stored with blowing water containing hypochlorous process water, blowing the ammonia and hypochlorous acid generation solution reaction that exist in water, decomposing to nitrogen (N
2).
In addition, the amount importing to the seawater of receiver 36 controls according to the measured value of temperature measuring apparatus 72.Control device 41 controls sea-water pump 71 in the mode making the temperature of the process water in receiver 36 and reach less than 50 DEG C, the amount of adjustment seawater.
According to above-mentioned embodiment, except the effect of the first embodiment, owing to importing the high seawater of chloride ion concentration to electrolyzer, therefore, it is possible to increase current density, the densification of electrolytic processing apparatus 37B can be realized.
(the 3rd embodiment)
Referring to accompanying drawing, the 3rd embodiment of the present invention is described in detail.
Fig. 4 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the first above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 4, in the ammonia treatment system 1C of present embodiment, be provided with between receiver 36 and electrolytic processing apparatus 37 by process water part or all in the ammonia that contains carry out the concentrating unit 60 that concentrates.That is, from the process water that receiver 36 is discharged the ammonia that contains be concentrated device 60 concentrated after, import to electrolytic processing apparatus 37.As concentrating unit 60, can adopt and employ the inverse device soaking into film, electrodialysis, electrical condenser desalination, ion exchange resin, water softener.
According to above-mentioned embodiment, by utilizing concentrating unit 60 to concentrate the ammonia importing to electrolytic processing apparatus 37, required chlorine (with reference to formula (2)) can be reduced thus, therefore, it is possible to reduce the feed rate as the chloride ion of raw material.That is, in electrolyzer 39, chloride ion can be utilized efficiently, the feed rate from outside can be reduced.
(the 4th embodiment)
Referring to accompanying drawing, the 4th embodiment of the present invention is described in detail.
Fig. 5 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the 3rd above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 5, in the ammonia treatment system 1D of present embodiment, the draining that the ammonia density generated when being concentrated by the ammonia in concentrating unit 60 is low mixes with the process water of releasing from electrolytic processing apparatus 37.That is, the water shoot 61 of discharging the low draining of ammonia density is provided with in the concentrating unit 60 of present embodiment.The draining should discharged from water shoot 61 mixes with the process water of releasing from electrolytic processing apparatus 37.
According to above-mentioned embodiment, by making the low draining of the ammonia density of generation in concentrating unit 60 mix with the process water of releasing from electrolytic processing apparatus 37, the ammonia density of the process water of releasing can be remained below normality thus.
(the 5th embodiment)
Referring to accompanying drawing, the 5th embodiment of the present invention is described in detail.
Fig. 6 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the 3rd above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 6, in the ammonia treatment system 1E of present embodiment, the process water of electrolytic processing apparatus 37 is circulated between receiver 36 and concentrating unit 60.That is, in the ammonia treatment system 1E of present embodiment, the process water after electrolysis, ammonia treatment is turned back to before concentrating unit 60, by sodium-chlor recycle via process water cycle pipe arrangement 62.
According to above-mentioned embodiment, the recycling of chloride ion can be realized, not need the supply from outside.
(the 6th embodiment)
Referring to accompanying drawing, the 6th embodiment of the present invention is described in detail.
Fig. 7 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the second above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 7, in the ammonia treatment system 1F of present embodiment, be provided with the desalting plant 63 of concentrated salinity in the downstream side of tempering tank 55, be desalted device 63 concentrated after the part of condensed water be supplied to electrolytic processing apparatus 37B as chloride ion source.Desalting plant 63 recycles pipe arrangement 64 with electrolytic processing apparatus 37B by condensed water and is connected.
In addition, the process water of discharging from desalting plant 63 or conduct are released water and are discharged, or as oiler feed, process water, miscellaneous water recycling.
As desalting plant 63, can adopt and employ the inverse device soaking into film, electrodialysis, electrical condenser desalination, ion exchange resin, water softener etc.
According to above-mentioned embodiment, by being set as the chloride ion being supplied to electrolytic processing apparatus 37B, from the formation of carrying out after desalting plant 63 reclaims supplying, the supply cost of chloride ion can being reduced.
(the 7th embodiment)
Referring to accompanying drawing, the 7th embodiment of the present invention is described in detail.
Fig. 8 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the 6th above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 8, in the ammonia treatment system 1G of present embodiment, be provided with the SS tripping device 65 that the SS (suspended solid) of process water is separated at the upstream side of the tempering tank 55 blowed on line 35.That is, the ammonia treatment system 1G of present embodiment imports to via blowing line 35 formation being supplied to tempering tank 55 after the process water containing ammonia carries out SS separation.
As SS tripping device 65, the device employing filter screen, secondary filter film (MF) module, ultra-filtration membrane (UF) module, sand filtration, settling tank, wet cyclone etc. can be adopted.
According to above-mentioned embodiment, be separated by SS, the inflow of SS composition to electrolytic processing apparatus 37B, desalting plant 63 can be reduced, the risk of damage of electrolytic processing apparatus 37B, desalting plant 63 can be reduced.
(the 8th embodiment)
Referring to accompanying drawing, the 8th embodiment of the present invention is described in detail.
Fig. 9 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the 6th above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 9, in the ammonia treatment system 1H of present embodiment, be provided with the water cooler 66 of cooling process water at the upstream side of the tempering tank 55 blowed on line 35.
According to above-mentioned embodiment, by the process water utilizing water cooler 66 to cool (such as 50 DEG C) high temperature (such as 80 DEG C), the damage risk of electrolytic processing apparatus 37B, desalting plant 63 can be reduced.
(the 9th embodiment)
Referring to accompanying drawing, the 9th embodiment of the present invention is described in detail.
Figure 10 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the 6th above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in Figure 10, in the ammonia treatment system 1J of present embodiment, be provided with between tempering tank 55 and desalting plant 63 and remove residual chlorine (Cl
2, ClO
-) Cl remove device 67.
Remove device 67 as Cl, the device that make use of activated carbon, air aeration, reductive agent supply etc. can be adopted.As reductive agent, Sulfothiorine (Na can be adopted
2s
2o
3), sodium bisulfite (NaHSO
3), S-WAT (Na
2sO
3) etc.
According to above-mentioned embodiment, by utilizing Cl to remove device 67, residual chlorine is reduced and is decomposed into chloride ion, can stop the residual chlorine of the process water flowing into desalting plant 63 thus, therefore, it is possible to prevent the damage of desalting plant 63.
(the tenth embodiment)
Referring to accompanying drawing, the tenth embodiment of the present invention is described in detail.
Figure 11 is the detailed system figure of the ammonia treatment system involved by present embodiment.It should be noted that, in present embodiment, by with the difference of the 9th above-mentioned embodiment centered by record, its explanation is eliminated for identical part.
As shown in figure 11, in the ammonia treatment system 1K of present embodiment, the downstream side (upstream side of desalting plant 63) removing device 67 at the Cl of the ammonia treatment system 1J of the 9th embodiment is provided with residual chlorine determinator 68, removes device 67 according to the concentration of residual chlorine control Cl measured by this residual chlorine determinator 68.
In addition, remove the downstream side (upstream side of desalting plant 63) of device 67 at Cl to be provided with and will to remove process water branch that device 67 the discharges bypass pipe arrangement 69 to the condensed water recycling pipe arrangement 64 in the downstream side of desalting plant 63 from Cl.From Cl remove process water that device 67 discharges based on the instruction of control device 41 be directed to desalting plant 63 and bypass pipe arrangement 69 any one.Its switching is undertaken by not shown valve.
The concrete control method of the ammonia treatment system 1J of present embodiment is described.Control device 41 is monitored by the concentration of residual chlorine of residual chlorine determinator 68 to the process water of discharging from tempering tank 55, and the Cl that operates removes device 67 until can't detect concentration of residual chlorine.Specifically, reductive agent, the addition of activated carbon, air aeration amount is controlled.
When concentration of residual chlorine being detected, stop the stream leading to desalting plant 63 with valve, water will be processed and import bypass stream 69, be branched off into condensed water recycling pipe arrangement 64.
According to above-mentioned embodiment, the removal rate utilizing Cl to remove the residual chlorine of device 67 can be improved.
It should be noted that, technical scope of the present invention is not limited to above-mentioned embodiment, can carry out various change without departing from the spirit and scope of the invention.Such as, each embodiment described above is ammonia density by being arranged at forming of carrying out measuring to the ammonia concentration determination device of waterline 11, but also can for blowing the formation measuring in line 35 and blow the ammonia density of water.
In addition, as the method for the concentration of mensuration ammonia, be not limited to the mensuration based on ammonia concentration determination device, also can for always carrying out the formation inferred from the injection rate of the ammonia of ammonia injection unit and the water yield of blowing water of water feeding system.
Utilizability in industry
By above-mentioned ammonia treatment system, electrolysis can be controlled based on the water feeding system of boiler plant or the ammonia density blowing water and the water yield of blowing water.Therefore, even if when the variation of blow down is large, the draining benchmark of ammonia density also can be met.
Label declaration
1 ammonia treatment system
2 combined cycle power stations
3 heat recovery boilers (boiler plant)
11 give waterline (water feeding system)
34 ammonia injection units
35 blow line
36 receivers
37 electrolytic processing apparatus
38 circulation adjustment tanks
39 electrolyzers
41 control device
42,42B seawater lead-in wire (chloride ion feed unit)
44 chloride ion concentration determinators (chloride ion concentration determination unit)
45 continuous-current plants
46 sea-water pumps
47 ammonia concentration determination devices (ammonia concentration determination unit)
48 ammonia concentration determination devices (ammonia concentration determination unit)
49 ammonia concentration determination devices (ammonia concentration determination unit)
52 residual chlorine determinators (residual chlorine determination unit)
53 flow rate-measuring devices (flow measurement unit)
55 tempering tanks
60 concentrating uniies
63 desalting plants
64 condensed water recycling pipe arrangements
Claims (8)
1. an ammonia treatment system, it possesses:
Boiler plant, for carrying out recovery of heat,
Ammonia injection unit, injects ammonia to the water feeding system in described boiler plant,
Ammonia concentration determination unit, measures the ammonia density blowing water from described water feeding system or described boiler plant,
Flow measurement unit, blows the water yield of water described in mensuration,
Receiver, blows water described in acceptance,
Chloride ion feed unit, imports the sodium chloride aqueous solution as chloride ion source to described receiver,
Electrolyzer, carries out electrolysis to the process water blowing water and described sodium chloride aqueous solution described in comprising, and
Control device, electric current when controlling described electrolysis and treatment time,
Described control device calculates required chlorine dose based on described ammonia density and the described water meter blowing water, and magnitude of current when controlling electrolysis.
2. ammonia treatment system as claimed in claim 1, it has residual chlorine determination unit, and described residual chlorine determination unit measures the concentration of residual chlorine of described process water in electrolysis,
Described control device decides the terminal of electrolysis according to described concentration of residual chlorine.
3. ammonia treatment system as claimed in claim 1 or 2, it has chloride ion concentration determination unit, and described chloride ion concentration determination unit measures the chloride ion concentration of described process water,
Described control device controls the import volume of described sodium chloride aqueous solution in the mode making described chloride ion concentration and reach more than normality.
4. as claimed any one in claims 1 to 3 ammonia treatment system, its be provided with between described receiver and electrolyzer to process water at least partially in the concentrating unit that concentrates of the ammonia that contains.
5. an ammonia treatment system, it possesses:
Boiler plant, for carrying out recovery of heat,
Ammonia injection unit, injects ammonia to the water feeding system in described boiler plant,
Ammonia concentration determination unit, measures the ammonia density blowing water from described water feeding system or described boiler plant,
Flow measurement unit, blows the water yield of water described in mensuration,
Electrolyzer, possesses the chloride ion feed unit imported as the sodium chloride aqueous solution in chloride ion source, and carries out electrolysis to described sodium chloride aqueous solution,
Tempering tank, blows water described in acceptance and accepts the process water from described electrolyzer, and
Control device, electric current when controlling described electrolysis and treatment time,
Described control device calculates required chlorine dose based on described ammonia density and the described water meter blowing water, and magnitude of current when controlling electrolysis.
6. ammonia treatment system as claimed in claim 5, it has residual chlorine determination unit, and described residual chlorine determination unit measures the concentration of residual chlorine of described process water in electrolysis,
Described control device decides the terminal of electrolysis according to described concentration of residual chlorine.
7. the ammonia treatment system as described in claim 5 or 6, it has chloride ion concentration determination unit, and described chloride ion concentration determination unit measures the chloride ion concentration of described process water,
Described control device controls the import volume of described sodium chloride aqueous solution in the mode making described chloride ion concentration and reach more than normality.
8. the ammonia treatment system according to any one of claim 5 to 7, it possesses:
Desalting plant, is arranged on the downstream side of described tempering tank, and
Condensed water recycling pipe arrangement, is supplied to electrolyzer using a part for the condensed water utilizing described desalting plant to concentrate as chloride ion source.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2012-119933 | 2012-05-25 | ||
| JP2012119933 | 2012-05-25 | ||
| JP2013-010251 | 2013-01-23 | ||
| JP2013010251A JP6191070B2 (en) | 2012-05-25 | 2013-01-23 | Ammonia treatment system |
| PCT/JP2013/063663 WO2013176032A1 (en) | 2012-05-25 | 2013-05-16 | Ammonia treatment system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104379512A true CN104379512A (en) | 2015-02-25 |
| CN104379512B CN104379512B (en) | 2017-06-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201380025991.2A Active CN104379512B (en) | 2012-05-25 | 2013-05-16 | ammonia treatment system |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JP6191070B2 (en) |
| KR (1) | KR101757525B1 (en) |
| CN (1) | CN104379512B (en) |
| SG (1) | SG11201407526RA (en) |
| WO (1) | WO2013176032A1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107531518A (en) * | 2015-04-17 | 2018-01-02 | 三菱重工环境·化学工程株式会社 | The processing method of hypochlorous acid feedway and discharging of boiler |
| CN110078178A (en) * | 2019-05-10 | 2019-08-02 | 浙江浙能嘉华发电有限公司 | A kind of strong ammonia wastewater cyclic electrolysis treatment process and equipment |
| CN110204017A (en) * | 2019-05-16 | 2019-09-06 | 浙江浙能技术研究院有限公司 | A kind of electrolytic treatment system and method adjusting ammonia-containing water pH value |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5700735B1 (en) * | 2014-08-28 | 2015-04-15 | 株式会社日立パワーソリューションズ | Water treatment apparatus and control method for water treatment apparatus |
| MX2017004514A (en) | 2014-10-10 | 2017-10-12 | Xogen Tech Inc | System and method for oxidation of ammonia. |
| JP6388124B2 (en) | 2014-11-10 | 2018-09-12 | 三菱重工環境・化学エンジニアリング株式会社 | Electrolysis system |
| JP6331145B2 (en) * | 2014-11-26 | 2018-05-30 | 三菱重工環境・化学エンジニアリング株式会社 | Ammonia treatment system |
| WO2016116216A1 (en) * | 2015-01-23 | 2016-07-28 | Siemens Aktiengesellschaft | Pre-heating of untreated water in power plants |
| WO2016167271A1 (en) * | 2015-04-17 | 2016-10-20 | 三菱重工環境・化学エンジニアリング株式会社 | Hypochlorous acid supply device and boiler waste-water treatment method |
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| CN113003786B (en) * | 2021-03-26 | 2022-04-01 | 马鞍山钢铁股份有限公司 | Combined treatment process for industrial gas dust removal water of CCPP unit |
| JP6940713B1 (en) * | 2021-05-18 | 2021-09-29 | 三菱重工環境・化学エンジニアリング株式会社 | Hydrogen production system |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0852478A (en) * | 1994-08-11 | 1996-02-27 | Mitsubishi Heavy Ind Ltd | Treatment of waste water |
| JP2004122032A (en) * | 2002-10-03 | 2004-04-22 | Bio Carrier Technology:Kk | Water purifying treatment system |
| CN1603246A (en) * | 2003-09-29 | 2005-04-06 | 三洋电机株式会社 | Water treatment apparatus that can reduce water treatment time |
| JP2005218904A (en) * | 2004-02-03 | 2005-08-18 | Sanyo Electric Co Ltd | Water treatment apparatus |
| JP2005288358A (en) * | 2004-03-31 | 2005-10-20 | Chugoku Electric Power Co Inc:The | Electrolytic wastewater treatment system, electrolytic control device, electrolytic wastewater treatment method, program and storage medium |
| JP2007160230A (en) * | 2005-12-14 | 2007-06-28 | Mitsubishi Heavy Ind Ltd | Water treatment system |
| JP2007252965A (en) * | 2006-03-20 | 2007-10-04 | Sanyo Electric Co Ltd | Apparatus for treating waste water |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5153980B2 (en) | 2001-09-27 | 2013-02-27 | パナソニック環境エンジニアリング株式会社 | Ammonia recovery equipment |
| JP2004267967A (en) * | 2003-03-11 | 2004-09-30 | Sanyo Electric Co Ltd | Water treatment apparatus |
| JP4671743B2 (en) * | 2005-04-15 | 2011-04-20 | 三菱重工環境・化学エンジニアリング株式会社 | Electrolytic treatment method and apparatus for wastewater containing ammonia nitrogen |
| JP2006326423A (en) * | 2005-05-24 | 2006-12-07 | Sanyo Electric Co Ltd | Water treatment method and water treatment apparatus |
| JP2008105012A (en) | 2006-09-27 | 2008-05-08 | Kobelco Eco-Solutions Co Ltd | Treatment method and treatment apparatus of ammonia nitrogen-containing drainage |
| JP4982425B2 (en) | 2008-05-09 | 2012-07-25 | 株式会社東芝 | Water treatment method and water treatment apparatus |
-
2013
- 2013-01-23 JP JP2013010251A patent/JP6191070B2/en active Active
- 2013-05-16 SG SG11201407526RA patent/SG11201407526RA/en unknown
- 2013-05-16 KR KR1020147032409A patent/KR101757525B1/en active IP Right Grant
- 2013-05-16 CN CN201380025991.2A patent/CN104379512B/en active Active
- 2013-05-16 WO PCT/JP2013/063663 patent/WO2013176032A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0852478A (en) * | 1994-08-11 | 1996-02-27 | Mitsubishi Heavy Ind Ltd | Treatment of waste water |
| JP2004122032A (en) * | 2002-10-03 | 2004-04-22 | Bio Carrier Technology:Kk | Water purifying treatment system |
| CN1603246A (en) * | 2003-09-29 | 2005-04-06 | 三洋电机株式会社 | Water treatment apparatus that can reduce water treatment time |
| JP2005218904A (en) * | 2004-02-03 | 2005-08-18 | Sanyo Electric Co Ltd | Water treatment apparatus |
| JP2005288358A (en) * | 2004-03-31 | 2005-10-20 | Chugoku Electric Power Co Inc:The | Electrolytic wastewater treatment system, electrolytic control device, electrolytic wastewater treatment method, program and storage medium |
| JP2007160230A (en) * | 2005-12-14 | 2007-06-28 | Mitsubishi Heavy Ind Ltd | Water treatment system |
| JP2007252965A (en) * | 2006-03-20 | 2007-10-04 | Sanyo Electric Co Ltd | Apparatus for treating waste water |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107531518A (en) * | 2015-04-17 | 2018-01-02 | 三菱重工环境·化学工程株式会社 | The processing method of hypochlorous acid feedway and discharging of boiler |
| TWI612012B (en) * | 2015-04-17 | 2018-01-21 | 三菱重工環境 化學工程股份有限公司 | Hypochlorous acid supply device and treatment method of boiler discharged water |
| CN110078178A (en) * | 2019-05-10 | 2019-08-02 | 浙江浙能嘉华发电有限公司 | A kind of strong ammonia wastewater cyclic electrolysis treatment process and equipment |
| CN110204017A (en) * | 2019-05-16 | 2019-09-06 | 浙江浙能技术研究院有限公司 | A kind of electrolytic treatment system and method adjusting ammonia-containing water pH value |
| CN110204017B (en) * | 2019-05-16 | 2023-08-22 | 浙江浙能技术研究院有限公司 | Electrolytic treatment system and method for adjusting pH value of ammonia-containing wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| JP6191070B2 (en) | 2017-09-06 |
| WO2013176032A1 (en) | 2013-11-28 |
| JP2014000563A (en) | 2014-01-09 |
| KR101757525B1 (en) | 2017-07-12 |
| SG11201407526RA (en) | 2015-03-30 |
| CN104379512B (en) | 2017-06-13 |
| KR20150013551A (en) | 2015-02-05 |
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