CN113979507A - Harmless recycling treatment process and system for high-salt and high-concentration organic wastewater - Google Patents
Harmless recycling treatment process and system for high-salt and high-concentration organic wastewater Download PDFInfo
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- CN113979507A CN113979507A CN202111384937.XA CN202111384937A CN113979507A CN 113979507 A CN113979507 A CN 113979507A CN 202111384937 A CN202111384937 A CN 202111384937A CN 113979507 A CN113979507 A CN 113979507A
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Images
Classifications
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/54—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms
- B01D46/543—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms using membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- 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
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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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
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Engineering & Computer Science (AREA)
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- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Materials Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Treating Waste Gases (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
A harmless recycling treatment process and a system for high-salt and high-concentration organic wastewater are characterized in that after moisture in the high-salt and high-concentration organic wastewater is removed through a flue gas evaporator, crystalline salt wrapping organic dirt is separated out, and partial organic dirt is subjected to a pyrolysis reaction under the action of high-temperature flue gas. The salt particles are intercepted along with the ascending flue gas under the action of a high-temperature demineralizer, and the material is distributed and enters a high-temperature melting furnace for further heating and temperature rise to generate high-temperature oxidation reaction, so that organic dirt components are removed. The flue gas generated by the high-temperature melting furnace and the flue gas discharged by the high-temperature desalter enter a secondary combustion chamber for treatment, one part of the flue gas discharged by the secondary combustion chamber is required by a flue gas evaporator, and the other part of the flue gas discharged by the secondary combustion chamber is treated by a waste heat boiler, a quench tower, an SCR (selective catalytic reduction), a dust remover, a washing tower and other sections and then becomes clean flue gas to be discharged. The invention has the advantages of low investment, low energy consumption, stable operation and high efficiency.
Description
Technical Field
The invention relates to an environment-friendly technology, in particular to a wastewater treatment technology, and specifically relates to a harmless recycling treatment process and system for high-salt and high-concentration organic wastewater.
Background
The high-salt and high-concentration organic wastewater mainly comes from the processing and production processes in the fields of coal chemical industry, petrochemical industry, fine chemical industry, medicine and pesticide and the like, and also comprises concentrated mother liquor obtained by carrying out multiple reduction treatment on salt-containing wastewater in other fields, for example, the wastewater generates concentrated liquor after membrane treatment, and the wastewater discharges the concentrated mother liquor after evaporation and crystallization. It is characterized in that the salt content of the wastewater is higher, and the general concentration is more than 3.5 percent. Meanwhile, the waste water has high organic content, COD concentration is usually more than 50g/L, and B/C value is low, biodegradability is poor, and the waste water contains harmful substances which are toxic to organisms. Such waste water cannot be directly treated by a biochemical method. The conventional evaporative crystallization process which is adopted only comprises multi-effect evaporative crystallization and MVR evaporative crystallization, and the problems of scaling, corrosion and the like of the device caused by high-concentration organic matter enrichment exist, and the stable operation and the salt discharge quality of the device are seriously influenced.
Aiming at the wastewater, various process coupling treatment modes including an evaporative crystallization technology, a pyrolysis carbonization technology, a wastewater incineration technology, an advanced oxidation technology, a physical and chemical separation technology and a salt separation technology are conventionally adopted at present. For example, the processes of incineration and salt separation coupling, advanced oxidation, evaporative crystallization and salt separation coupling and the processes of evaporative crystallization, pyrolysis carbonization and salt separation coupling can basically realize zero discharge of wastewater and resource of waste salt after wastewater is treated by the processes. But still has the problems of large equipment investment, high process energy consumption, high operating cost, low quality of resource byproduct salt and the like, and the maximum environmental protection treatment benefit is difficult to achieve.
Specifically, if waste water incineration is adopted, when the water content of the feed waste water is high, a large amount of heat is needed to evaporate the water, and the energy consumption in the incineration process is large. Meanwhile, molten salt easily causes severe corrosion of high-temperature refractory materials, and the generated smoke is large in amount and serious in salt particle entrainment. The equipment and the pipeline can not be normally used easily due to cooling and crystallization in subsequent treatment equipment, and the resource rate is reduced. If advanced oxidation methods such as ozone, UV/H are used2O2Fenton handles, and when feeding waste water organic matter concentration was too big, need drop into a large amount of chemical agent, increase device running cost. Meanwhile, the advanced oxidation method is mostly used as a pretreatment section for removing organic matters, and the influence of high salinity on the organic matter degradation efficiency still needs to be solved when the wastewater at the later stage enters a biochemical link. If an advanced oxidation method such as wet oxidation and supercritical water oxidation treatment is adopted, the reaction conditions are harsh, the treatment needs to be carried out at high temperature and high pressure, the requirement on equipment manufacturing is high, and the investment and the operation cost are high. If the pyrolysis carbonization treatment is adopted, the decomposition and the damage of organic matters are not thorough due to low reaction temperature, so that the byproduct salt is difficult to reach the recycling standard, and the resource recycling route is hindered. If the salt separation process is adopted for treatment, the recovery rate and purity of byproduct salt are limited by the content of organic matters in the wastewater. When the concentration of organic matters is high, the recovery rate can only be sacrificed for ensuring the purity of the recovered salt, so that the resource rate is reduced; to ensure high recovery of the salt, the purity of the recovered salt is affected and the resource approach is hindered.
The current market urgently needs the process and equipment for harmlessly and resourcefully treating the organic wastewater with high salt content and high concentration, and can meet the multiple requirements of investment saving, low energy consumption, stable operation, high efficiency and the like, and realize the maximization of the environmental protection treatment benefit.
Disclosure of Invention
The invention aims to provide a novel harmless recycling treatment process and equipment for high-salt-content and high-concentration organic wastewater, which are low in investment, low in energy consumption, stable in operation and high in efficiency, aiming at the problems of high equipment investment, high process energy consumption, high operation cost, low resource byproduct salt quality, environment-friendly treatment benefit maximization and the like in the conventional high-salt-content and high-concentration organic wastewater treatment.
One of the technical schemes of the invention is as follows:
a harmless and resource treatment process for high-salt and high-concentration organic wastewater is characterized by comprising the following steps: it comprises the following steps:
firstly, removing water from high-salt and high-concentration organic wastewater under the action of a flue gas evaporator;
secondly, enabling the flue gas with the water removed to carry crystallized polluted salt to enter a high-temperature desalter for drying and crystallization;
thirdly, intercepting the dried crystallized polluted salt, distributing the intercepted salt into a high-temperature melting furnace, performing high-temperature oxidation treatment, decomposing and destroying organic pollutants wrapping the inside and outside of the high-temperature melting furnace to form molten clean salt, cooling the molten clean salt, adding water to prepare refined salt water, and performing quality-based crystallization process to obtain a byproduct refined salt which reaches the standard and is sold;
fourthly, combining the flue gas at the outlet of the high-temperature demineralizer and the high-temperature melting furnace, and treating the combined flue gas in a second combustion chamber, wherein the organic waste gas and pollutants are thoroughly destroyed and decomposed;
fifthly, one part of high-temperature flue gas discharged from the second combustion chamber flows back to enter a flue gas evaporator, and the other part of high-temperature flue gas is treated by a waste heat boiler, a quench tower, an SCR (selective catalytic reduction), a dust remover and a washing tower to become clean flue gas to be discharged outside, and finally zero discharge of wastewater and resource utilization of salt are realized.
The high-salt and high-concentration organic wastewater source related by the invention comprises but is not limited to industries such as coal chemical industry, petrochemical industry, printing and dyeing, pesticide and medicine, new materials and the like, and also comprises high-salt and high-concentration organic wastewater such as concentrated mother liquor and distillation raffinate which are generated after the original wastewater is concentrated and distilled, for example, concentrated liquor which is generated after garbage percolate passes through a membrane treatment system, concentrated mother liquor which is generated after the coal chemical wastewater passes through an MVR evaporation system, kettle bottom raffinate which is generated after the pesticide wastewater passes through a distillation system and the like. The wastewater is characterized by salt concentration not less than 3.5% and COD concentration not less than 50 g/L.
The wastewater can be treated by the process provided by the invention after being provided with necessary pretreatment units, the pretreatment is mainly used for reducing the content of suspended solids in the feed wastewater, and the temperature of the feed wastewater is controlled to be 20-80 ℃.
The high-salt and high-concentration organic wastewater enters the spraying annular pipeline through the wastewater inlet pipeline on the upper side of the flue gas evaporator, the spraying annular pipeline is provided with regularly distributed atomizing nozzles, the nozzles are made of stainless steel or ceramic and other wear-resistant and high-temperature-resistant materials, and the forms of a spiral-flow type mechanical atomizing nozzle, a steam atomizing nozzle, a compressed air atomizing nozzle or a combined nozzle and the like can be adopted according to the water quality characteristics of the wastewater. Under the action of the nozzle, the wastewater is atomized into fine droplets with micro-nano particle size and dispersed in the evaporator cavity. High-temperature flue gas is input to the side of evaporator bottom by flue gas import pipe to get into from four directions along cyclic annular gas distribution pipe, atomizing liquid drop direct contact carries out strong heat exchange and chemical reaction in the same cavity, and atomizing liquid drop is desiccated rapidly, and the crystallization salt of parcel organic filth is appeared, and in high temperature flue gas environment, lasts the drying. The dirty salt granule is at the in-process that rises along with the flue gas, and the continuous heat absorption intensifies, and the organic filth that contains takes place the pyrolytic reaction in step, has a small amount of the great dirty salt granule of proportion because of atomization effect is not good or gas-liquid contact reaction is bad, can sink to the evaporimeter bottom by the action of gravity, collects the back through the toper bottom surface and discharges the evaporimeter by bottom dirty salt collecting pipe. The residence time of the wastewater fog drops in the cavity of the flue gas evaporator is controlled to be 0.5 s-2 s.
The temperature of the flue gas discharged by the flue gas evaporator is controlled to be 300-450 ℃, and the flue gas enters the high-temperature demineralizer through a flue gas pipeline. The high-temperature demineralizer is internally provided with a plurality of ceramic membrane tubes which are arranged in a tubular or multi-channel shape, the polluted salt particles carried in the flue gas are intercepted on the outer surface of the tubes by the ceramic membrane tubes, the salt particles deposited on the surfaces of the tubes are removed by the periodic purging system, and the salt particles are further collected at the conical bottom of the high-temperature demineralizer and are discharged to a polluted salt feeding port at the top of the high-temperature melting furnace.
The high-temperature melting furnace is in a tower shape, the side surface of the high-temperature melting furnace is provided with another dirty salt feeding hole which is connected with a salt discharging hole at the bottom of the flue gas evaporator through a pipeline, and a distributing device is arranged below the feeding hole at the top of the high-temperature melting furnace, so that salt particles are uniformly distributed and fall into a melting furnace cavity. The side surface of the lower part of the melting furnace body is provided with a combustion-supporting device which provides a heat source for the high-temperature melting treatment of the polluted salt and comprises a fuel inlet pipe, an air inlet pipe, an ignition device, a fuel nozzle, a controller, a regulating valve, a fan and other auxiliary equipment. Liquid or gaseous fuels may be selected, with gaseous fuels, such as natural gas, being preferred. When using liquid fuel, the fuel nozzle is internally provided with a stainless steel nozzle core guide vane, and the spray shape is annular fog. When the fuel oil with high viscosity is selected, a steam atomizing nozzle is adopted. The polluted salt entering the high-temperature melting furnace absorbs heat, the temperature is further raised, the polluted salt undergoes the processes of drying, pyrolysis, melting and the like, and the organic pollutants are gradually oxidized and decomposed until the polluted salt is completely removed. At the moment, the temperature of the molten salt area in the furnace reaches 1100-1200 ℃, organic matters in molten liquid salt and oxygen are subjected to gas-liquid mixing reaction, compared with gas-solid reaction in the pyrolysis carbonization process, the gas-solid reaction is more thorough, and the problem that organic matters wrapped by waste salt are not completely removed can be effectively solved.
The molten clean salt without organic dirt is discharged through a bottom pipeline of a high-temperature melting furnace, the molten clean salt enters a salt melting pool after being cooled, process water is added to prepare a clean salt water solution with the concentration of 20-40% and the temperature of 40-80 ℃, the salt water solution is subjected to a quality-grading crystallization process to obtain by-product refined salt, including inorganic salts such as sodium sulfate, sodium chloride and the like, the quality of the salt water solution reaches the industrial salt standards of class II class I of Industrial anhydrous sodium sulfate (GB/T6009-. The TOC content of the by-product refined salt can be controlled to be less than 10ppm, for example, the by-product refined salt of sodium chloride can be directly used as the raw material salt for producing the ionic membrane chlor-alkali. The quality-separating crystallization process can adopt a thermal method, a membrane method or a coupling method. The hot salt separation process mainly relates to an evaporative crystallization technology, and comprises multiple-effect evaporative crystallization, MVR evaporative crystallization and other forms.
And (3) discharging flue gas containing a small amount of organic waste gas generated in the high-temperature melting furnace through a side smoke outlet of the furnace, controlling the temperature of the flue gas to be 900-1100 ℃, and enabling the flue gas and the flue gas discharged by the high-temperature desalter to enter a secondary combustion chamber through a flue gas pipeline, wherein the secondary combustion chamber is provided with a combustion-supporting device, so that the organic waste gas in the flue gas is further subjected to high-temperature oxidative decomposition and removal. The temperature of the flue gas in the secondary combustion chamber is controlled to be 1000-1200 ℃, the residence time of the flue gas is not less than 2s, the high-temperature flue gas after incineration is discharged through a pipeline, one part of the high-temperature flue gas is input into a flue gas evaporator, and the other part of the high-temperature flue gas is changed into clean flue gas to be discharged outside after being sequentially treated by a waste heat boiler, a quench tower, an SCR (selective catalytic reduction), a dust remover, a washing tower and other processes.
The waste heat boiler is used for recovering heat of high-temperature flue gas, the temperature of a flue gas outlet of the waste heat boiler is controlled to be 500-600 ℃, a fire tube or water tube furnace mode can be adopted, generated steam can be used for a hot salt separation process, and steam condensate water can be used as partial salt separation process water. The quenching tower is used for rapidly cooling the flue gas from 500-600 ℃ to below 200 ℃, the retention time is less than 1s, and dioxin is prevented from being formed in the system; the SCR is used for reducing the concentration of nitrogen oxides in the flue gas to reach the emission standard limit value; the dust remover is used for cooling the flue gas and removing a small amount of smoke dust substances, and can adopt a Venturi type, a cloth bag type, an electrostatic dust removal type and the like; the washing tower is used for removing acid gases in the flue gas, such as HCl, HF and the like, and the used washing liquid can be process water or alkali liquor according to specific wastewater components.
The second technical scheme of the invention is as follows:
the utility model provides a high innoxious resourceful treatment system of containing salt high concentration organic waste water which characterized in that: it includes:
the flue gas evaporator is used for removing moisture of the high-salt and high-concentration organic wastewater;
the high-temperature desalter is used for drying and crystallizing crystallized polluted salt carried by the flue gas subjected to moisture removal by the flue gas evaporator;
the high-temperature melting furnace is used for carrying out high-temperature oxidation treatment on the dried and crystallized polluted salt so that organic dirt wrapped inside and outside the polluted salt is decomposed and destroyed to form molten clean salt;
a salt dissolving pool, which is used for cooling the molten clean salt and adding water to prepare refined salt water;
a quality-divided crystallization device, which is used for treating the refined brine to obtain a byproduct of refining;
the second combustion chamber is used for combining the high-temperature desalter and the outlet flue gas of the high-temperature melting furnace for secondary combustion treatment, so that organic waste gas and pollutants are thoroughly destroyed and decomposed; one part of high-temperature flue gas discharged from the secondary combustion chamber flows back to enter a flue gas evaporator, and the other part of high-temperature flue gas enters a flue gas advanced treatment device for purification treatment;
the flue gas advanced treatment device comprises a waste heat boiler, a quench tower, an SCR, a dust remover and a washing tower, wherein the flue gas is treated by the flue gas advanced treatment device and then becomes clean flue gas to be discharged;
after the high-salt and high-concentration organic wastewater is treated by the treatment device, zero emission and salt resource utilization are realized.
The invention has the beneficial effects that:
the invention has the advantages of low investment, low energy consumption, stable operation and high efficiency.
Drawings
FIG. 1 is a block diagram of the process flow and the system composition of the harmless resource treatment of the high-salt and high-concentration organic wastewater.
FIG. 2 is a schematic view of a flue gas evaporator apparatus of the present invention.
FIG. 3 is a schematic view of a flue gas distribution system and a waste water spray system in the flue gas evaporator of the present invention.
FIG. 4 is a schematic view of a high temperature melting furnace apparatus according to the present invention.
In the figure: 1-smoke gas distribution pipe; 2-a waste water spray pipe; 3-an atomizing nozzle; 4-a smoke exhaust outlet pipe; 5-a salt grain collecting pipe; 6-a flue gas inlet pipe; 7-gas distribution ring pipe; 8-a smoke dispersion port; 9-a waste water inlet pipe; 10-spraying ring pipe; 11-an atomizing nozzle; 12-a combustion-supporting device; 13, 14-dirty salt inlet; 15-a distributor; 16-a smoke exhaust outlet pipe; 17-furnace bottom molten salt discharge pipe.
Detailed Description
The invention is further described below with reference to the figures and examples.
As shown in fig. 1.
A harmless resource treatment process and a system for high-salt and high-concentration organic wastewater are characterized in that the high-salt and high-concentration organic wastewater is subjected to the action of a flue gas evaporator, after moisture is removed, flue gas carrying crystallized dirt salt enters a high-temperature desalter, the dried crystallized dirt salt is intercepted and distributed to enter a high-temperature melting furnace, the high-temperature oxidation treatment is carried out, organic dirt wrapping the inside and the outside of the flue gas is decomposed and destroyed to form molten state clean salt, the molten state clean salt is cooled and added with water to prepare refined salt water, and the refined salt water is subjected to quality-based crystallization process treatment to obtain a byproduct refined salt which reaches the standard and is sold. The high-temperature desalter and the outlet flue gas of the high-temperature melting furnace are combined and enter a second combustion chamber for treatment, and pollutants such as organic waste gas and the like are thoroughly destroyed and decomposed. One part of high-temperature flue gas discharged from the secondary combustion chamber enters a flue gas evaporator, and the other part of high-temperature flue gas is treated by processes of a waste heat boiler, a quench tower, an SCR (selective catalytic reduction), a dust remover, a washing tower and the like in sequence and then becomes clean flue gas to be discharged outside, and finally zero discharge of waste water and resource utilization of salt are realized.
The following will further describe the present invention in detail by taking the treatment of the salt-containing wastewater generated in the washing process of certain epoxy resin manufacturing enterprises as an example:
as shown in figure 2, salt-containing wastewater generated in a washing process of an epoxy resin production enterprise is treated by an evaporation concentration process to obtain high-salt and high-concentration organic wastewater, wherein the temperature is 60-80 ℃, the salt concentration is 20-25%, the COD concentration is 55-60 g/L, and the main components comprise sodium chloride, bisphenol A, epichlorohydrin, toluene and the like.
The salt-containing organic wastewater enters the side wastewater inlet pipe 9 on the flue gas evaporator, is pumped into the system through the wastewater spray pipe 2, and is cut into micro-nano-scale fog drops through the spray ring pipe 10 and the high-temperature-resistant and wear-resistant stainless steel steam atomizing nozzles 3 arranged at the tail ends, and the fog drops are scattered in the cavity of the evaporator. Flue gas with the temperature of 1000-1100 ℃ coming from the back-end process enters through a flue gas inlet pipe 6 on the side face of the bottom of the evaporator and is blown into the system through a flue gas distribution pipe 1 and is discharged from flue gas spreading openings 8 in four directions along a gas distribution ring pipe 7, high-temperature flue gas is in direct contact with micro mist drops to generate strong heat exchange and chemical reaction, the mist drops lose water, organic dirt is wrapped by the high-temperature flue gas, crystallized salt is separated out, and the high-temperature flue gas is discharged from a smoke exhaust outlet pipe 4 along with the rising of the flue gas. And (3) continuously dehydrating and drying the precipitated salt under the surrounding of high-temperature flue gas, further absorbing heat and raising the temperature to 300-400 ℃, and thermally cracking the contained organic dirt to generate light hydrocarbon and other small molecular gases which are discharged along with the flue gas. In the process, the polluted salt crystal grains with larger specific gravity are deposited at the bottom of the flue gas evaporator under the action of gravity. The residence time of the flue gas in the evaporator is 1 s-2 s.
The method comprises the following steps of discharging flue gas outside an evaporator, blowing the flue gas into a high-temperature demineralizer, arranging a ceramic membrane tube bundle in the high-temperature demineralizer in a multi-channel shape, intercepting dirt salt particles in the flue gas on the outer surface by the ceramic membrane tube bundle, and stripping and collecting the dirt salt particles on the conical bottom surface of the demineralizer through periodic gas back-flushing operation. And the waste salt is conveyed to a waste salt feeding port 14 at the top of the high-temperature melting furnace through a pipeline, and simultaneously, the waste salt at the bottom of the flue gas evaporator is conveyed to a waste salt feeding port 13 at the side surface of the high-temperature melting furnace through a salt particle collecting pipe 5. The dirty salt particles are uniformly distributed and fall into the melting furnace cavity through a distributor 15 below a dirty salt feeding hole 14 at the top. A combustion-supporting device 12 is arranged in the furnace, natural gas is combusted to generate heat, dirt salt particles absorb the heat, the temperature is further increased to 1100-1200 ℃, the solid state is changed into a molten state, organic dirt is subjected to high-temperature oxidation reaction under the action of oxygen, organic matters are gradually destroyed and decomposed into carbon dioxide and water, in addition, part of small molecules of organic gas which are not completely reacted and flue gas generated by combustion are discharged from a flue gas outlet pipe 16, and the small molecules of organic gas and the flue gas generated by combustion are blown into a secondary combustion chamber together with the flue gas from a high-temperature desalter. The second combustion chamber is provided with a burner, natural gas is combusted to generate heat, and organic gas molecules which are not completely reacted further undergo high-temperature oxidation reaction to generate carbon dioxide and water. The residence time of the flue gas in the secondary combustion chamber is 2 s-3 s, so that the organic dirt is completely oxidized and decomposed as far as possible. The temperature of the flue gas discharged from the secondary combustion chamber is 1000-1100 ℃, and a part of the flue gas is blown into the flue gas evaporator through a pipeline. The other part of high-temperature flue gas passes through a fire tube type waste heat boiler to recover the heat of the flue gas, and the temperature of the outlet flue gas is reduced to 500-600 ℃. Then the flue gas temperature is reduced to below 200 ℃ within 1s through a quench tower, so that the generation of dioxin is effectively avoided. The flue gas is heated and enters SCR to remove nitrogen oxides generated in the burning process, fly ash in the flue gas is removed through a Venturi dust collector, the temperature of the flue gas is reduced to be below 100 ℃, the flue gas is washed through alkali liquor in a washing tower, acid gases such as HCl in the flue gas are removed, and finally the requirement of standard discharge of clean flue gas is met.
The clean molten salt in the high-temperature melting furnace is discharged to a salt melting pool through a furnace bottom molten salt discharge pipe 17, is cooled and then dissolved in process water to prepare brine with the temperature of 70-80 ℃ and the concentration of 30-40%, the COD content of the brine is less than 20mg/L, and the brine enters an MVR evaporation crystallizer to obtain refined sodium chloride salt, wherein the recovery rate of the salt is more than 90%, the purity is more than 98%, and the TOC is less than 10ppm, so that the refined sodium chloride salt can be used as a raw material salt for the ionic membrane chlor-alkali industry for export sales. The steam required by MVR evaporation crystallization is provided by a waste heat boiler, and the steam condensate can be used as partial salt process water. The MVR evaporative crystallization mother liquor reenters the treatment system through a circulating pipeline.
The present invention is not concerned with parts which are the same as or can be implemented using prior art techniques.
Claims (10)
1. A harmless and resource treatment process for high-salt and high-concentration organic wastewater is characterized by comprising the following steps: it comprises the following steps:
firstly, removing water from high-salt and high-concentration organic wastewater under the action of a flue gas evaporator;
secondly, enabling the flue gas with the water removed to carry crystallized polluted salt to enter a high-temperature desalter for drying and crystallization;
thirdly, intercepting the dried crystallized polluted salt, distributing the intercepted salt into a high-temperature melting furnace, performing high-temperature oxidation treatment, decomposing and destroying organic pollutants wrapping the inside and outside of the high-temperature melting furnace to form molten clean salt, cooling the molten clean salt, adding water to prepare refined salt water, and performing quality-based crystallization process to obtain a byproduct refined salt which reaches the standard and is sold;
fourthly, combining the flue gas at the outlet of the high-temperature demineralizer and the high-temperature melting furnace, and treating the combined flue gas in a second combustion chamber, wherein the organic waste gas and pollutants are thoroughly destroyed and decomposed;
fifthly, one part of high-temperature flue gas discharged from the second combustion chamber flows back to enter a flue gas evaporator, and the other part of high-temperature flue gas is treated by a waste heat boiler, a quench tower, an SCR (selective catalytic reduction), a dust remover and a washing tower to become clean flue gas to be discharged outside, and finally zero discharge of wastewater and resource utilization of salt are realized.
2. The process according to claim 1, characterized in that: the concentration of the high-salt and high-concentration organic wastewater is not less than 3.5%, the COD concentration is not less than 50g/L, and the high-salt and high-concentration organic wastewater comprises but not limited to high-salt and high-concentration organic wastewater generated in coal chemical industry, petrochemical industry, printing and dyeing, pesticide and medicine industry and new material industry, and also comprises concentrated mother liquor and high-salt and high-concentration organic wastewater generated after the original wastewater is concentrated and distilled.
3. The process according to claim 1, characterized in that: the main structure of the flue gas evaporator is an evaporation chamber cavity, and is provided with a waste water feeding spraying system, a flue gas blowing system and a salt particle collecting auxiliary system at the bottom of the evaporator; high-salt and high-concentration organic wastewater enters a spraying annular pipeline through a wastewater inlet pipeline on the upper side of a flue gas evaporator, atomizing nozzles are distributed on the annular pipeline according to a high-efficiency scattering principle, and the wastewater is atomized into fine droplets with micro-nano particle sizes to be scattered in a cavity of the evaporator; high-temperature flue gas is input from a flue gas inlet pipe on the side surface of the bottom of the evaporator, enters the flue gas evaporator from four directions along an annular gas distribution pipe, and performs strong heat exchange and chemical reaction with atomized liquid drops in the cavity; the atomized liquid drops are quickly dehydrated, and the crystal salt wrapping the organic dirt is separated out and is carried by the ascending flue gas to be discharged from the flue gas outlet pipeline, so that the pyrolysis reaction of partial organic dirt is synchronously carried out; the dirty salt particles with poor atomization effect and large specific gravity sink to the bottom of the evaporator under the action of gravity, are collected through the conical bottom surface and are discharged out of the evaporator through the bottom salt particle collecting pipe.
4. The process according to claim 3, characterized in that: the atomizing nozzle of the flue gas evaporator is made of stainless steel or ceramic which is wear-resistant and high-temperature-resistant, and adopts the form of a rotational flow type mechanical atomizing nozzle, a steam atomizing nozzle, a compressed air atomizing nozzle or a combined nozzle; the residence time of the wastewater fog drops in the cavity of the flue gas evaporator is controlled to be 0.5-2 s, and the temperature of the feed wastewater is controlled to be 20-80 ℃.
5. The process according to claim 1, characterized in that: the flue gas temperature from a flue gas outlet of a flue gas evaporator in the high-temperature demineralizer is 300-450 ℃, the flue gas enters the high-temperature demineralizer through a flue gas pipeline, a plurality of ceramic membrane tubes are arranged in the high-temperature demineralizer and are arranged in a tubular or multi-channel shape, crystalline salt containing organic dirt carried in the flue gas is intercepted on the outer surface of the tube by the ceramic membrane tubes, and the flue gas enters the ceramic membrane tubes and is discharged out of the high-temperature demineralizer after being converged; crystallized salt particles outside the ceramic membrane pipe are collected at the bottom of the high-temperature desalter and discharged through a pipeline; the high-temperature demineralizer is designed to be a conical bottom surface and is provided with a gas back-blowing device for cleaning salt particle deposition on the outer surface of the ceramic membrane pipe.
6. The process according to claim 1, characterized in that: the high-temperature melting furnace body is in a tower shape, the top of the high-temperature melting furnace body is provided with a dirty salt feeding hole, and the dirty salt feeding hole is connected with a salt discharging hole at the bottom of the high-temperature desalter through a pipeline; a distributing device is arranged below the dirty salt feeding hole, so that salt particles are uniformly distributed and fall into the cavity of the melting furnace; a dirty salt feeding port is arranged on the side surface of the furnace body and is connected with a salt discharging port at the bottom of the flue gas evaporator through a pipeline; a combustion-supporting device is arranged on the side surface of the lower part of the furnace body, and provides a heat source for the high-temperature melting treatment of the polluted salt; the polluted salt entering the high-temperature melting furnace absorbs heat, is dried, pyrolyzed and melted while being heated, and the organic pollutants are gradually oxidized and decomposed until being completely removed; the flue gas and a small amount of organic waste gas generated in the process are discharged through a flue gas outlet pipeline at the side of the melting furnace; discharging the molten state crystallized salt without the organic dirt through a furnace bottom pipeline; the temperature of a molten salt area in the furnace is controlled to be 1100-1200 ℃; the temperature of the discharged flue gas is controlled to be 900-1100 ℃.
7. The process according to claim 1, wherein the second combustion chamber is provided with two flue gas inlets, one inlet is connected with the flue gas outlet of the high-temperature demineralizer through a pipeline, and the other inlet is connected with the flue gas outlet of the high-temperature melting furnace through a pipeline; the second combustion chamber is provided with a combustion-supporting device, so that organic waste gas in the flue gas is further subjected to high-temperature oxidative decomposition and removal; the temperature of the flue gas in the secondary combustion chamber is controlled to be 1000-1200 ℃, the retention time is not less than 2s, and the flue gas after incineration is discharged from an outlet pipeline; one part of high-temperature flue gas is input into a flue gas evaporator through a pipeline, and the other part of the high-temperature flue gas is sequentially treated by a waste heat boiler, a quench tower, an SCR (selective catalytic reduction), a dust remover, a washing tower and the like to become clean flue gas to be discharged; the temperature of a flue gas outlet of the waste heat boiler is controlled to be 500-600 ℃, and a water pipe or fire pipe furnace form can be adopted; the temperature of the flue gas outlet of the quenching tower is controlled below 200 ℃, the residence time of the flue gas is less than 1s, and dioxin is prevented from being formed in the system; the dust remover can adopt a Venturi type, a cloth bag type, an electrostatic dust removing type and other forms; the washing liquid used by the washing tower can select process water or alkali liquor according to specific wastewater components.
8. The process according to claim 6 or 7; it is characterized in that the combustion-supporting device comprises a fuel inlet pipe, an air inlet pipe, an ignition device, a fuel nozzle, a controller, an adjusting valve and a fan; selecting a liquid or gaseous fuel; when the liquid fuel is used, a stainless steel nozzle core guide vane is arranged in the fuel nozzle, and the spray shape is annular fog; when the fuel oil viscosity is high, a steam atomizing nozzle is adopted.
9. The process of claim 1, wherein the clean salt in molten state discharged from the bottom of the high-temperature melting furnace through the pipeline enters a salt melting tank after being cooled, is dissolved by adding process water to prepare a clean salt solution with the concentration of 20-40%, the temperature of the salt solution in the salt melting tank is controlled at 40-80 ℃, and is subjected to a fractional crystallization process to obtain a byproduct of refined salt for sale; the quality-divided crystallization process comprises a thermal method, a membrane method and a coupling method; the thermal method salt separation mainly relates to an evaporative crystallization technology, and comprises the forms of multi-effect evaporative crystallization, MVR evaporative crystallization and the like; when the hot method salt separation process is adopted, the required steam can be provided by a waste heat boiler; the steam condensate can be used as partial salt process water; the crystallization mother liquor enters the treatment system again through a circulating pipeline; (ii) a The byproduct refined salt can be used for obtaining inorganic salt such as sodium sulfate, sodium chloride and the like, meets the relevant industrial salt standard and can be sold outside the mouth.
10. The utility model provides a high innoxious resourceful treatment system of containing salt high concentration organic waste water which characterized in that: it includes:
the flue gas evaporator is used for removing moisture of the high-salt and high-concentration organic wastewater;
the high-temperature desalter is used for drying and crystallizing crystallized polluted salt carried by the flue gas subjected to moisture removal by the flue gas evaporator;
the high-temperature melting furnace is used for carrying out high-temperature oxidation treatment on the dried and crystallized polluted salt so that organic dirt wrapped inside and outside the polluted salt is decomposed and destroyed to form molten clean salt;
a salt dissolving pool, which is used for cooling the molten clean salt and adding water to prepare refined salt water;
a quality-divided crystallization device, which is used for treating the refined brine to obtain a byproduct of refining;
the second combustion chamber is used for combining the high-temperature desalter and the outlet flue gas of the high-temperature melting furnace for secondary combustion treatment, so that organic waste gas and pollutants are thoroughly destroyed and decomposed; one part of high-temperature flue gas discharged from the secondary combustion chamber flows back to enter a flue gas evaporator, and the other part of high-temperature flue gas enters a flue gas advanced treatment device for purification treatment;
the flue gas advanced treatment device comprises a waste heat boiler, a quench tower, an SCR, a dust remover and a washing tower, wherein the flue gas is treated by the flue gas advanced treatment device and then becomes clean flue gas to be discharged;
after the high-salt and high-concentration organic wastewater is treated by the treatment device, zero emission and salt resource utilization are realized.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114873884A (en) * | 2022-06-02 | 2022-08-09 | 中车山东机车车辆有限公司济南低碳科技分公司 | Method for obtaining molten salt and byproduct carbon material by comprehensively treating high-salt-content chemical sludge |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH078750A (en) * | 1993-06-14 | 1995-01-13 | Chubu Electric Power Co Inc | Treatment of drainage after desulfurization |
| KR20040031917A (en) * | 2002-10-07 | 2004-04-14 | 에틴시스템 주식회사 | Complete Renewal pollution-free process of various kind of wastes, and major equipments required |
| WO2012063137A2 (en) * | 2010-11-08 | 2012-05-18 | Key Group Holding S.R.O. | Method of organic waste processing, processing equipment and utilization of processed products |
| CN203264529U (en) * | 2013-04-22 | 2013-11-06 | 西安西热锅炉环保工程有限公司 | Cross flow-convection flue gas purification and adsorption tower |
| CN207121514U (en) * | 2017-06-07 | 2018-03-20 | 北京清新环境技术股份有限公司 | A kind of SO3 removings and the charging integrated device of desulfurization wastewater zero-emission |
| CN109775785A (en) * | 2017-11-15 | 2019-05-21 | 江苏金牛环保工程设备有限公司 | A kind of high-salt wastewater burns desalting system and its processing method |
| CN110642271A (en) * | 2019-10-31 | 2020-01-03 | 江苏省环境科学研究院 | Device and method for melting treatment and refining of industrial waste salt |
| CN113146834A (en) * | 2021-03-08 | 2021-07-23 | 广东家美陶瓷有限公司 | Ceramic spray tower discharging device and control method thereof |
| CN113184932A (en) * | 2021-04-26 | 2021-07-30 | 武汉天空蓝环保科技有限公司 | Utilize flue gas evaporative concentration device and desulfurization effluent disposal system |
| CN216472341U (en) * | 2021-11-22 | 2022-05-10 | 江苏中圣高科技产业有限公司 | Harmless resourceful processing apparatus of high salt high concentration organic waste water that contains |
-
2021
- 2021-11-22 CN CN202111384937.XA patent/CN113979507B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH078750A (en) * | 1993-06-14 | 1995-01-13 | Chubu Electric Power Co Inc | Treatment of drainage after desulfurization |
| KR20040031917A (en) * | 2002-10-07 | 2004-04-14 | 에틴시스템 주식회사 | Complete Renewal pollution-free process of various kind of wastes, and major equipments required |
| WO2012063137A2 (en) * | 2010-11-08 | 2012-05-18 | Key Group Holding S.R.O. | Method of organic waste processing, processing equipment and utilization of processed products |
| CN203264529U (en) * | 2013-04-22 | 2013-11-06 | 西安西热锅炉环保工程有限公司 | Cross flow-convection flue gas purification and adsorption tower |
| CN207121514U (en) * | 2017-06-07 | 2018-03-20 | 北京清新环境技术股份有限公司 | A kind of SO3 removings and the charging integrated device of desulfurization wastewater zero-emission |
| CN109775785A (en) * | 2017-11-15 | 2019-05-21 | 江苏金牛环保工程设备有限公司 | A kind of high-salt wastewater burns desalting system and its processing method |
| CN110642271A (en) * | 2019-10-31 | 2020-01-03 | 江苏省环境科学研究院 | Device and method for melting treatment and refining of industrial waste salt |
| CN113146834A (en) * | 2021-03-08 | 2021-07-23 | 广东家美陶瓷有限公司 | Ceramic spray tower discharging device and control method thereof |
| CN113184932A (en) * | 2021-04-26 | 2021-07-30 | 武汉天空蓝环保科技有限公司 | Utilize flue gas evaporative concentration device and desulfurization effluent disposal system |
| CN216472341U (en) * | 2021-11-22 | 2022-05-10 | 江苏中圣高科技产业有限公司 | Harmless resourceful processing apparatus of high salt high concentration organic waste water that contains |
Non-Patent Citations (1)
| Title |
|---|
| 时钧，袁权，高从阶 主编: "《工业固体废物处理及回收利用》", 中国环境科学出版社, pages: 116 - 187 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114873884A (en) * | 2022-06-02 | 2022-08-09 | 中车山东机车车辆有限公司济南低碳科技分公司 | Method for obtaining molten salt and byproduct carbon material by comprehensively treating high-salt-content chemical sludge |
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