WO2023207098A1 - Système et procédé de traitement de distillation-oxydation pour déchets liquides à partir d'un nettoyage chimique à l'acide organique d'une chaudière de centrale électrique - Google Patents

Système et procédé de traitement de distillation-oxydation pour déchets liquides à partir d'un nettoyage chimique à l'acide organique d'une chaudière de centrale électrique Download PDF

Info

Publication number
WO2023207098A1
WO2023207098A1 PCT/CN2022/136157 CN2022136157W WO2023207098A1 WO 2023207098 A1 WO2023207098 A1 WO 2023207098A1 CN 2022136157 W CN2022136157 W CN 2022136157W WO 2023207098 A1 WO2023207098 A1 WO 2023207098A1
Authority
WO
WIPO (PCT)
Prior art keywords
liquid
waste liquid
distillate
distillation
organic acid
Prior art date
Application number
PCT/CN2022/136157
Other languages
English (en)
Chinese (zh)
Inventor
张恒
文慧峰
位承君
龙国军
朱涛
刘永兵
党志军
Original Assignee
西安热工研究院有限公司
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 西安热工研究院有限公司 filed Critical 西安热工研究院有限公司
Publication of WO2023207098A1 publication Critical patent/WO2023207098A1/fr

Links

Images

Classifications

    • 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
    • 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
    • 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
    • C02F1/043—Details
    • 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
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen

Definitions

  • This application relates to the technical field of chemical cleaning waste liquid treatment for power station boilers, and in particular to a distillation-advanced oxidation treatment system and method for organic acid chemical cleaning waste liquid of power station boilers.
  • Organic acid cleaning waste liquid has the characteristics of high COD (30000 ⁇ 80000mg/L), high iron ion content (5000 ⁇ 10000mg/L), high color, high short-term emission (1000 ⁇ 2000t/time), and non-recurring characteristics. Power plants Existing wastewater treatment equipment and technology are difficult to meet the requirements for treatment and reuse.
  • distillation is often used to reduce wastewater.
  • the distillate usually contains low-boiling organic matter, and its COD is still high, making it difficult to meet emission standards and requiring advanced treatment.
  • the purpose of this application is to provide a power station boiler organic acid chemical cleaning waste liquid distillation-advanced oxidation treatment system and method, changing the way of solely relying on chemical methods to treat cleaning waste liquid, combining distillation and
  • the advantages of advanced oxidation technology can solve the problems of traditional treatment methods such as large dosage of chemicals, large amounts of solid waste, high cost, and unqualified effluent quality.
  • a power station boiler organic acid chemical cleaning waste liquid distillation-oxidation treatment system including: a distillation system, an oxidation system, and a crystallization system;
  • the distillation system includes a waste liquid transfer pump, a heater and a flash tank.
  • the outlet of the waste liquid transfer pump is connected to the flash tank after passing through the heater;
  • the vapor phase outlet of the flash tank is connected to the distillate collection tank after passing through a condenser.
  • the liquid phase outlet of the flash tank is connected to the heater inlet through the concentrate delivery pump;
  • the oxidation system includes: an aeration device, an advanced oxidation reactor and an effluent collection tank; the liquid outlet of the distillate collection tank is connected to the aeration device through a distillate delivery pump, and the liquid outlet of the aeration device is connected to the advanced oxidation reactor.
  • the liquid outlet of the advanced oxidation reactor is connected to the water collection tank;
  • the crystallization system includes: a crystallization separator, a salt precipitator and dehydration equipment; the concentrated liquid delivery pump is connected to the crystallization separator. After solid-liquid separation is performed by the crystallization separator, the supernatant liquid is connected to the flash tank through a supernatant liquid pipeline. ; The solid-liquid mixture enters the salt precipitator, and the outlet of the salt precipitator is connected to the dehydration equipment.
  • the flash tank is connected to a dosing pump for adding defoaming agent; the gas outlet of the distillate collection tank is connected to a vacuum pump.
  • the aeration device is connected to the aeration gas source through an aeration gas source pipe, and the aeration device is connected to a first exhaust pipe.
  • the advanced oxidation reactor is connected to a liquid oxidant dosing pump, and the advanced oxidation reactor is connected to a gas oxidant source through a gas pipeline; a second exhaust pipe is provided on the top of the advanced oxidation reactor; and the water effluent collection tank Connect the effluent transfer pump to discharge the distillate out of the system.
  • the waste liquid includes: chemical cleaning waste liquid of citric acid, formic acid, glycolic acid, EDTA or EDTA salt.
  • the heater is an electric heater or a dividing wall heat exchanger, and the heat source is electric heating or high-temperature steam; a gas-liquid separation accessory is provided inside the flash tank; the condenser is a water-cooled or air-cooled condenser.
  • the air source of the aeration device is compressed air; the air source of the aeration device is compressed air with a pressure of 0.1 to 0.2MPa; the advanced oxidation device is a bubble tower reactor, a plate tower reactor, Falling film reactor or packed tower reactor; an ultraviolet device is installed inside the advanced oxidation device; the oxidant used in the advanced oxidation reactor is a gas oxidant, a liquid oxidant, or both, the gas oxidant is ozone, and the liquid oxidant is hydrogen peroxide. solution or ammonium persulfate solution.
  • the crystallizer is a cyclone separator
  • the dehydration equipment is a centrifuge or a filter press.
  • a method for chemically cleaning a waste liquid distillation-oxidation treatment system with organic acid in a power station boiler which is characterized by including the following steps:
  • the organic acid chemical cleaning waste liquid of the power station boiler is transported to the distillation system through the waste liquid transfer pump; after being heated by the heater, the vapor and liquid are separated in the flash tank, and a defoaming agent is added through the dosing pump to control the foam; the vapor phase is condensed
  • the distillate is obtained by condensation in the device, and the distillate is stored in the distillate collection tank; the liquid phase is re-transported to the heater through the concentrate delivery pump for cyclic evaporation;
  • the distillate entering the distillate collection tank is transported to the oxidation system through the distillate transfer pump; the distillate first enters the aeration device for aeration, and the aeration gas source enters the aeration device, and the low boiling point components in the distillate After aeration, it is discharged out of the system; the aerated distillate enters the advanced oxidation reactor, the liquid oxidant is added to the advanced oxidation reactor through the liquid oxidant dosing pump, and the gas oxidant is introduced; the distillate is decomposed after advanced oxidation The product and excess gaseous oxidant are discharged from the system, and the distillate after advanced oxidation enters the effluent collection tank and is discharged from the system by the effluent delivery pump;
  • the concentrated liquid When the liquid phase in the evaporation system is concentrated to the set index, the concentrated liquid is discharged out of the system or enters the crystallization system; after the concentrated liquid entering the crystallization system is separated from solid and liquid by the crystallization separator, the supernatant liquid returns to the flash tank; the solid liquid is returned to the flash tank; The liquid mixture enters the salt precipitator, and the solid-liquid mixture that passes through the salt precipitator enters the dehydration equipment to obtain organic acid salt crystals and organic acid waste liquid saturated liquid.
  • the working pressure of the evaporation system is -0.1 ⁇ 0.1MPa
  • the waste liquid temperature is 5°C ⁇ 95°C
  • the liquid temperature entering the flash tank is 30°C ⁇ 110°C
  • the condensate temperature is 5°C ⁇ 60°C.
  • this application changes the way of treating cleaning waste liquid solely by chemical methods, and has the following advantages:
  • This system includes a distillation system, an oxidation system, and a crystallization system; through the distillation system, the organic acid chemical cleaning waste liquid of the power station boiler is flashed after heating, the vapor-liquid separation, the distillate is stored, and the liquid phase is circulated and evaporated; the distillate is then exposed Gas, low boiling point components in the distillate are discharged after aeration; the aerated distillate undergoes an oxidation reaction; decomposition products and excess gas oxidants are discharged; the concentrated liquid entering the crystallization system is separated from solid and liquid through the crystallization separator Afterwards, the supernatant liquid returns to the flash tank; the solid-liquid mixture enters the salt precipitator, and the solid-liquid mixture that passes through the salt precipitator enters the dehydration equipment to obtain organic acid salt crystals and organic acid waste liquid saturated liquid.
  • Figure 1 is a schematic diagram of a distillation-oxidation treatment system for organic acid chemical cleaning waste liquid of a power station boiler according to the present application.
  • This application provides a distillation-oxidation treatment system for organic acid chemical cleaning waste liquid of a power station boiler, which includes: a distillation system, an oxidation system, and a crystallization system.
  • the distillation system includes: waste liquid transfer pump 1, heater 2, flash tank 3, dosing pump 4, condenser 5, distillate collection tank 6, vacuum pump 7, distillate transfer pump 8, concentrate transfer pump 14 and the connecting pipes between each equipment (18, 19, 20, 21, 22, 23, 24, 25, 26, 27, 37, 38, 39, 40, 41);
  • the oxidation system includes: aeration device 9, advanced Oxidation reactor 10, liquid oxidant dosing pump 11, effluent collection tank 12, effluent transfer pump 13 and connecting pipes (28, 29, 30, 31, 32, 33, 34, 35, 36) between each equipment; among them, the crystallization system It includes: crystallization separator 15, salt precipitator 16, dehydration equipment 17 and connecting pipes (42, 43, 44, 45, 46, 47) between each equipment.
  • the heater 2 is an electric heater or a dividing wall heat exchanger, and the heat source is electric heating or high-temperature steam; defoaming agent is added through the dosing pump 4 to control foaming in the flash tank; inside the flash tank 3 Baffles, demisters, cyclone separators and other gas-liquid separation accessories are provided; the condenser 5 is a water-cooled or air-cooled condenser.
  • the gas source of the aeration device 9 is compressed air;
  • the advanced oxidation device 10 is a bubble tower reactor, plate tower reactor, falling film reactor or packed tower reactor; the advanced oxidation device 10 is equipped with a UV device inside .
  • the crystallizer 15 is a cyclone separator, and the dehydration equipment 17 is a centrifuge or a filter press.
  • the system working pressure is -0.1 ⁇ 0.1MPa
  • the waste liquid temperature is 5°C ⁇ 95°C.
  • the liquid temperature entering the flash tank 3 is 30°C ⁇ 110°C
  • the condensate temperature is 5°C ⁇ 60°C.
  • the gas source of the aeration device 9 is compressed air with a pressure of 0.1 to 0.2MPa
  • the oxidant used in the advanced oxidation reactor 10 is a gas oxidant, a liquid oxidant, or both.
  • the gas oxidant is ozone
  • the liquid oxidant is hydrogen peroxide solution or ammonium persulfate solution.
  • the organic acid chemical cleaning waste liquid of the power station boiler is heated after entering the distillation system.
  • the low-boiling point chemicals and most of the water are evaporated by heat and condensed into a distillate.
  • the distillate contains some chemicals, and its COD and ammonia are relatively high.
  • the COD is reduced to less than 50 mg/L
  • the ammonia hydrogen is reduced to less than 15 mg/L, reaching emission standards.
  • the high-boiling point pharmaceuticals that have not been evaporated in the distillation system are directly discharged from the distillation system in the form of concentrated liquid or are processed by the crystallization system and then discharged from the crystallization system in the form of crystals.
  • the concentrated liquid or crystal has low water content and high calorific value, and can be burned with coal in the furnace.
  • This application solves the problems of traditional distillation method distillate water quality COD and ammonia exceeding the standard; solves the problems of low treatment efficiency, harsh treatment conditions, and long treatment cycle of a single advanced oxidation method; solves the problem of traditional flocculation and sedimentation method with large dosage of chemicals and solid solids.
  • the problem is that the amount of waste is large and solid waste is difficult to process and recycle.
  • the organic acid chemical cleaning waste liquid in the embodiment of the present application includes: citric acid, formic acid, glycolic acid, EDTA, and EDTA salt chemical cleaning waste liquid. We will not explain them one by one here. Only Examples 1 and 2 will be described as representative examples.
  • a power plant boiler organic acid chemical cleaning waste liquid distillation-oxidation treatment system includes: a distillation system, an oxidation system, and a crystallization system.
  • the distillation system includes: waste liquid transfer pump 1, heater 2, flash tank 3, dosing pump 4, condenser 5, distillate collection tank 6, vacuum pump 7, distillate transfer pump 8, concentrate transfer pump 14 and connecting pipes 18, 19, 20, 21, 22, 23, 24, 25, 26, 27, 37, 38, 39, 40, 41 between equipment; waste liquid transfer pump 1, heater 2, flash tank 3 are connected in sequence, the flash tank 3 is connected to the dosing pump 4 for dosing; the gas pipe of the flash tank 3 is connected to the condenser 5, the distillate collection tank 6, and the gas outlet of the distillate collection tank 6.
  • the vacuum pump 7 is used to exhaust the gas, and the liquid pipeline is connected to the oxidation system through the distillate delivery pump 8 .
  • the liquid pipeline of the flash tank 3 is respectively connected to the outlet of the waste liquid transfer pump 1 and the inlet of the crystallization system through the concentrated liquid transfer pump 14.
  • the oxidation system includes: aeration device 9, advanced oxidation reactor 10, liquid oxidant dosing pump 11, effluent collection tank 12, effluent transfer pump 13 and connecting pipes 28, 29, 30, 31, 32, 33 between each equipment. 34, 35, 36.
  • the distillate transfer pump 8 is connected to the aeration device 9, the advanced oxidation reactor 10, the effluent collection tank 12, and the liquid inlet of the effluent transfer pump 13 in sequence; the advanced oxidation reactor 10 is connected to the liquid oxidant dosing pump 11 for dosing. medicine.
  • the crystallization system includes: crystallization separator 15, salt precipitator 16, dehydration equipment 17 and connecting pipes 42, 43, 44, 45, 46, 47 between each equipment.
  • the concentrated liquid delivery pump 14 is connected to the crystallization separator 15, the salt precipitator 16, and the dehydration equipment 17 in sequence. After solid-liquid separation in the crystallizer separator 15, the supernatant liquid returns to the flash tank 3 through the pipeline 43.
  • the organic acid chemical cleaning waste liquid used in this embodiment is citric acid chemical cleaning waste liquid.
  • the working pressure of the distillation system is 0.03MPa
  • the temperature of the citric acid chemical cleaning waste liquid is 25°C
  • the density is 1.020g/cm 3 .
  • the heater 2 is a dividing wall heat exchanger, and the heat source is high-temperature steam (150°C ⁇ 200°C).
  • the temperature of the liquid entering the flash tank 3 is 99.7°C, and the flash evaporation
  • the internal liquid level of tank 3 is controlled at 30% to 50%, and a baffle, demister, and cyclone separator are installed on the top; the amount of defoaming agent is 0.05 ⁇ (mass fraction) of the waste liquid; condenser 5 is water-cooled condensation device, the condensate temperature after vapor phase condensation is 40°C.
  • the gas source of the aeration device 9 is compressed air, the pressure is 0.1MPa, and the dosage is 20 times the waste liquid volume (volume);
  • the advanced oxidation device 10 is a bubble tower reactor, and the gas oxidant used is ozone, and the dosage is The amount of liquid waste is 2 ⁇ (mass fraction), the liquid oxidant is 30% hydrogen peroxide solution, and the dosage is 1 ⁇ (mass fraction) of the waste liquid;
  • the advanced oxidation device 10 is equipped with a UV device (UV intensity 0.01 W/cm 2 ).
  • the crystallizer 15 is a cyclone separator, and the dehydration equipment 17 is a centrifuge.
  • Step 1 The citric acid chemical cleaning waste liquid of the power station boiler is transported to the distillation system through the waste liquid transfer pump 1. After being heated by the heater 2, the vapor and liquid are separated in the flash tank 3, and a defoaming agent is added through the dosing pump 4 to control the foam.
  • the vapor phase is condensed through the condenser 5 to obtain a distillate, which is stored in the distillate collection tank 6; the liquid phase is re-transported to the heater 2 through the concentrate delivery pump 14 for cyclic evaporation.
  • the upper part of the distillate collection tank 6 is connected to a vacuum pump 7 to adjust the distillation system pressure to 0.03MPa and discharge non-condensable gas.
  • Step 2 The distillate entering the distillate collection tank 6 is transported to the oxidation system through the distillate transfer pump 8 .
  • the distillate first enters the aeration device 9 for aeration.
  • the aeration gas source enters the aeration device 9 through the pipeline 29.
  • the low boiling point components in the distillate are aerated and discharged from the system through the pipeline 28; the distillate after aeration
  • the effluent enters the advanced oxidation reactor 10, the hydrogen peroxide solution is added to the advanced oxidation reactor 10 through the liquid oxidant dosing pump 11, and the ozone is introduced through the pipeline 31.
  • the decomposition products and excess ozone are discharged from the system through pipeline 33.
  • the distillate after advanced oxidation enters the effluent collection tank 12 and is discharged from the system by the effluent delivery pump 13.
  • Table 1 shows this implementation An example of distillate water quality after advanced oxidation.
  • Step 3 When the liquid phase in the evaporation system is concentrated to the set index [density greater than 1.266g/cm 3 ], the concentrated liquid enters the crystallization system through pipeline 41; the concentrated liquid entering the crystallization system is separated from solid and liquid by the crystallization separator 15 , the supernatant liquid returns to the flash tank 3 through the pipeline 43; the solid-liquid mixture enters the salt precipitator 16, and the solid-liquid mixture after settling the salt enters the dehydration equipment 17 to obtain ferrous citrate, ferric citrate, and ferrous citrate.
  • Ferrous ammonium, ferric ammonium citrate solid mixture and a small amount of citric acid waste liquid saturated liquid, ferrous citrate, ferric citrate, ferrous ammonium citrate, ferric ammonium citrate solid mixture have the characteristics of high calorific value and low water content. Coal is fed into the furnace and burned.
  • a power plant boiler organic acid chemical cleaning waste liquid distillation-advanced oxidation treatment system includes: a distillation system, an advanced oxidation system, and a crystallization system.
  • the distillation system includes: waste liquid transfer pump 1, heater 2, flash tank 3, dosing pump 4, condenser 5, distillate collection tank 6, vacuum pump 7, distillate transfer pump 8, concentrate transfer pump 14 and connecting pipes 18, 19, 20, 21, 22, 23, 24, 25, 26, 27, 37, 38, 39, 40, 41;
  • the oxidation system includes: aeration device 9, advanced oxidation reaction 10, liquid oxidant dosing pump 11, effluent collection tank 12, effluent transfer pump 13 and connecting pipes 28, 29, 30, 31, 32, 33, 34, 35, 36 between each equipment;
  • the crystallization system includes: crystallization separation 15, salt precipitator 16, dehydration equipment 17 and connecting pipes 42, 43, 44, 45, 46, 47 between each equipment; the specific structural connection relationships are the same as those in the embodiment, and the same system is used.
  • the organic acid chemical cleaning waste liquid used in this embodiment is formic acid-glycolic acid chemical cleaning waste liquid.
  • the working pressure of the distillation system is 0.03MPa, and the temperature of the formic acid-glycolic acid chemical cleaning waste liquid is 25°C.
  • Heater 2 is a dividing wall heat exchanger, and the heat source is high-temperature steam (150°C ⁇ 200°C). After the waste liquid is heated by heater 2, the temperature of the liquid entering flash tank 3 is 98.7°C.
  • the liquid inside flash tank 3 The position is controlled at 30% to 50%, and a baffle, demister, and cyclone separator are installed on the top; the amount of defoaming agent is 0.05 ⁇ (mass fraction) of the waste liquid amount; condenser 5 is a water-cooled condenser, vapor phase After condensation, the condensate temperature is 40°C.
  • the gas source of the aeration device 9 is compressed air, the pressure is 0.1MPa, and the dosage is 20 times the waste liquid volume (volume);
  • the advanced oxidation device 10 is a bubble tower reactor, and the gas oxidant used is ozone, and the dosage is The liquid oxidant is 30% hydrogen peroxide solution, and the dosage is 0.5 ⁇ (mass fraction) of the waste liquid volume;
  • the advanced oxidation device 10 is equipped with an ultraviolet light device (ultraviolet light intensity 0.01 W/cm 2 ).
  • the crystallizer 15 is a cyclone separator, and the dehydration equipment 17 is a centrifuge.
  • the treatment method based on the above distillation-oxidation treatment system for organic acid chemical cleaning waste liquid of power station boilers includes the following steps:
  • Step 1 The formic acid-glycolic acid chemical cleaning waste liquid of the power station boiler is transported to the distillation system through the waste liquid transfer pump 1. After being heated by the heater 2, the vapor and liquid are separated in the flash tank 3, and a defoaming agent is added through the dosing pump 4 to control the foam.
  • the vapor phase is condensed through the condenser 5 to obtain a distillate, which is stored in the distillate collection tank 6; the liquid phase is re-transported to the heater 2 through the concentrate delivery pump 14 for cyclic evaporation.
  • the upper part of the distillate collection tank 6 is connected to a vacuum pump 7 to adjust the distillation system pressure to 0.03MPa and discharge non-condensable gas.
  • Step 2 The distillate entering the distillate collection tank 6 is transported to the oxidation system through the distillate transfer pump 8 .
  • the distillate first enters the aeration device 9 for aeration.
  • the aeration gas source enters the aeration device 9 through the pipeline 29.
  • the low boiling point components in the distillate are aerated and discharged from the system through the pipeline 28; the distillate after aeration
  • the effluent enters the advanced oxidation reactor 10, the hydrogen peroxide solution is added to the advanced oxidation reactor 10 through the liquid oxidant dosing pump 11, and the ozone is introduced through the pipeline 31.
  • the decomposition products and excess ozone are discharged from the system through pipeline 33.
  • the distillate after advanced oxidation enters the effluent collection tank 12 and is discharged from the system by the effluent delivery pump 13. Table 2 shows this implementation An example of distillate water quality after advanced oxidation.
  • Step 3 The liquid phase in the evaporation system is concentrated to the set index (when the distillate volume reaches more than 95% of the waste liquid volume), the concentrated liquid enters the crystallization system through pipeline 41, and the concentrated liquid entering the crystallization system passes through the crystallization separator 15. After the solid-liquid separation, the supernatant liquid returns to the flash tank 3 through the pipeline 43; the solid-liquid mixture enters the salt precipitator 16, and the solid-liquid mixture after settling the salt enters the dehydration equipment 17 to obtain ferrous formate and ferrous glycolate. , solid mixture of iron formate, iron glycolate and a small amount of saturated liquid of formic acid glycolate. The solid mixture of ferrous formate, ferrous glycolate, iron formate and iron glycolate has the characteristics of high calorific value and low water content, and is burned with the coal in the furnace.

Abstract

Sont divulgués dans la présente demande un système et un procédé de traitement de distillation-oxydation pour déchets liquides à partir d'un nettoyage chimique à l'acide organique d'une chaudière de centrale électrique. Le système comprend un système de distillation, un système de cristallisation et un système d'oxydation, le système de distillation comprenant une pompe de transport de déchets liquides, les déchets liquides entrant dans un réservoir de détente par l'intermédiaire de la pompe de transport de déchets liquides et d'un dispositif de chauffage, une sortie de phase vapeur du réservoir de détente étant reliée à un réservoir de collecte de distillat par l'intermédiaire d'un condenseur, et une sortie de phase liquide étant reliée à une entrée du dispositif de chauffage par l'intermédiaire d'une pompe de transport de solution concentrée; le système d'oxydation comprend un dispositif d'aération, une sortie de liquide du dispositif d'aération est reliée à un réacteur d'oxydation avancée, et une sortie de liquide du réacteur d'oxydation avancée est reliée à un réservoir de collecte d'effluent; et le système de cristallisation comprend un séparateur de cristallisation, la pompe de transport de solution concentrée est reliée au séparateur de cristallisation, un surnageant, résultant d'une séparation solide-liquide par le séparateur de cristallisation, est relié au réservoir de détente par l'intermédiaire d'une conduite, un mélange solide-liquide entre dans un dispositif de précipitation de sel, et une sortie du dispositif de précipitation de sel est reliée à un appareil de déshydratation. La présente demande résout les problèmes dans un procédé de sédimentation par floculation classique d'une grande quantité de réactifs utilisés, d'une grande quantité de déchets solides produits et d'une difficulté de traitement et de recyclage de déchets solides.
PCT/CN2022/136157 2022-04-28 2022-12-02 Système et procédé de traitement de distillation-oxydation pour déchets liquides à partir d'un nettoyage chimique à l'acide organique d'une chaudière de centrale électrique WO2023207098A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202210462733.1 2022-04-28
CN202210462733.1A CN114772829A (zh) 2022-04-28 2022-04-28 电站锅炉有机酸化学清洗废液蒸馏-氧化处理系统及方法

Publications (1)

Publication Number Publication Date
WO2023207098A1 true WO2023207098A1 (fr) 2023-11-02

Family

ID=82434151

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2022/136157 WO2023207098A1 (fr) 2022-04-28 2022-12-02 Système et procédé de traitement de distillation-oxydation pour déchets liquides à partir d'un nettoyage chimique à l'acide organique d'une chaudière de centrale électrique

Country Status (2)

Country Link
CN (1) CN114772829A (fr)
WO (1) WO2023207098A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114772829A (zh) * 2022-04-28 2022-07-22 西安热工研究院有限公司 电站锅炉有机酸化学清洗废液蒸馏-氧化处理系统及方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH11226560A (ja) * 1998-02-13 1999-08-24 Hitachi Ltd 廃液または廃水の処理方法及び装置
CN104671607A (zh) * 2015-02-09 2015-06-03 西安热工研究院有限公司 一种稠油废水处理回用电站锅炉的系统及方法
CN204529600U (zh) * 2015-02-09 2015-08-05 西安热工研究院有限公司 一种稠油废水处理回用电站锅炉的系统
CN205773863U (zh) * 2016-06-08 2016-12-07 广州汉泰环境技术有限公司 一种用于处理垃圾渗滤液的结晶系统
CN112279761A (zh) * 2020-10-30 2021-01-29 西安热工研究院有限公司 由电站锅炉柠檬酸化学清洗废液制备柠檬酸铁铵的方法
CN114772829A (zh) * 2022-04-28 2022-07-22 西安热工研究院有限公司 电站锅炉有机酸化学清洗废液蒸馏-氧化处理系统及方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH11226560A (ja) * 1998-02-13 1999-08-24 Hitachi Ltd 廃液または廃水の処理方法及び装置
CN104671607A (zh) * 2015-02-09 2015-06-03 西安热工研究院有限公司 一种稠油废水处理回用电站锅炉的系统及方法
CN204529600U (zh) * 2015-02-09 2015-08-05 西安热工研究院有限公司 一种稠油废水处理回用电站锅炉的系统
CN205773863U (zh) * 2016-06-08 2016-12-07 广州汉泰环境技术有限公司 一种用于处理垃圾渗滤液的结晶系统
CN112279761A (zh) * 2020-10-30 2021-01-29 西安热工研究院有限公司 由电站锅炉柠檬酸化学清洗废液制备柠檬酸铁铵的方法
CN114772829A (zh) * 2022-04-28 2022-07-22 西安热工研究院有限公司 电站锅炉有机酸化学清洗废液蒸馏-氧化处理系统及方法

Also Published As

Publication number Publication date
CN114772829A (zh) 2022-07-22

Similar Documents

Publication Publication Date Title
CN107399876B (zh) 一种高氨氮废水的处理方法
CN102190341B (zh) 热泵闪蒸汽提脱氨法
CN102234170B (zh) 一种快速降低污泥含水率的处理方法及其装置
CN104058538B (zh) 一种废水汽提脱酸脱氨的工艺方法
CN104843813A (zh) 一种煤气化高氨氮污水处理工艺
WO2023207098A1 (fr) Système et procédé de traitement de distillation-oxydation pour déchets liquides à partir d'un nettoyage chimique à l'acide organique d'une chaudière de centrale électrique
CN111847744B (zh) 离子交换树脂生产中高盐有机废水的处理系统及方法
CN103964631A (zh) 一种高效水煤浆气化灰水处理方法
CN108609787A (zh) 一种垃圾渗滤液浸没式燃烧处理系统
CN109626684B (zh) 高硝酸盐废水的处理装置及其工艺
CN113292187A (zh) 一种高浓度氨氮废水的资源化处理方法及装置
CN104030514A (zh) 一种双效节能废水汽提脱酸脱氨的工艺方法
CN104843816A (zh) 一种热泵闪蒸汽提脱氨联产硫酸铵及氨水的方法
CN212222702U (zh) 一种高效低温负压氨氮废水汽提系统
CN104860465B (zh) 一种双塔催化热耦合逆流脱氨方法及其脱氨装置
CN208087255U (zh) 一种氨氮废水高效脱氨装置
CN206407915U (zh) 从氨氮废水中生产高纯度氨水的装置
CN206033465U (zh) 一种煤化工废水预处理脱氨系统
CN101734813A (zh) 一种利用氰尿酸生产过程中的废酸液回收硫酸铵的工艺及其使用的设备
CN110772962A (zh) 一种利用垃圾渗滤液中的氨进行垃圾焚烧烟气脱硝的方法
TWI532681B (zh) A method for recovering ethylene glycol and acetaldehyde from polyester wastewater
CN107129087B (zh) 一种垃圾渗透液脱氨除铬工艺方法
CN212315829U (zh) 离子交换树脂生产中高盐有机废水的处理系统
CN210085221U (zh) 生化污泥处理系统
CN109650646B (zh) 一种甘氨酸生产废水的处理方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 22939912

Country of ref document: EP

Kind code of ref document: A1