CN112902196A - High-salt-content chlorine-containing organic waste liquid zero-emission resource utilization system - Google Patents

High-salt-content chlorine-containing organic waste liquid zero-emission resource utilization system Download PDF

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Publication number
CN112902196A
CN112902196A CN201911217670.8A CN201911217670A CN112902196A CN 112902196 A CN112902196 A CN 112902196A CN 201911217670 A CN201911217670 A CN 201911217670A CN 112902196 A CN112902196 A CN 112902196A
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pipeline
water
tower
denitration
module
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Inventor
余传林
关小川
宋爱军
张翔武
王祺
赵广播
孙绍增
赵洪宇
余瀚坤
程坤乾
余世玉
张�杰
李赫男
谷长智
乔忠喜
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Dalian Kelin Energysaving & Environmental Protection Co ltd
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Dalian Kelin Energysaving & Environmental Protection Co ltd
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Priority to CN201911217670.8A priority Critical patent/CN112902196A/en
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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
    • F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B01D50/10—Combinations of devices covered by groups B01D45/00, B01D46/00 and B01D47/00
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • 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
    • B01D53/75—Multi-step processes
    • 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
    • B01D53/77—Liquid phase processes
    • 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
    • B01D53/8631—Processes characterised by a specific device
    • 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
    • B01D53/90—Injecting reactants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
    • 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
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/12—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating using gaseous or liquid fuel
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    • 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
    • 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
    • F23J15/006—Layout of treatment plant
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    • 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
    • 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
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • 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
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • 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
    • 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
    • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/10—Supplementary heating arrangements using auxiliary fuel
    • F23G2204/103—Supplementary heating arrangements using auxiliary fuel gaseous or liquid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/10—Liquid waste
    • F23G2209/101—Waste liquor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
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    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F23J2215/301—Dioxins; Furans
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/10—Intercepting solids by filters
    • F23J2217/101—Baghouse type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices
    • 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

Abstract

The invention discloses a high-salt-content chlorine-containing organic waste liquid zero-emission resource utilization system, which relates to the technical field of industrial waste treatment and comprises a high-temperature incineration module, a rapid cooling dioxin suppression generation module, a gas-solid separation module, an HCl separation module, an alkali washing neutralization module, a low-temperature denitration module, a water treatment module and a molten salt cooling, conveying and packaging module, wherein the high-temperature incineration module, the rapid cooling dioxin suppression generation module, the gas-solid separation module, the HCl separation module, the alkali washing neutralization module and the low-temperature denitration module are sequentially connected through a flue. The invention has reasonable design and compact structure, melts the inorganic salt generated by waste liquid incineration into molten salt by utilizing the high-temperature incineration principle, packs the molten salt after cooling, and recovers the high-purity inorganic salt. The HCl gas in the flue gas is absorbed by adopting water spray mist in a secondary absorption tower by utilizing the principle that the HCl gas is easily dissolved in water, and dilute hydrochloric acid is recovered. And a waste heat boiler is adopted to recover heat energy in the flue gas, and byproduct steam is provided for users to use. The invention changes waste into valuable, not only meets the national requirements of environmental protection and energy conservation, but also realizes the resource utilization of the waste, meets the strategic requirements of national sustainable development, provides a scientific method for reducing burden and increasing efficiency of enterprises, and is suitable for popularization and use.

Description

High-salt-content chlorine-containing organic waste liquid zero-emission resource utilization system
Technical Field
The invention relates to the technical field of industrial waste treatment, in particular to a zero-emission resource utilization system for high-salt-content chlorine-containing organic waste liquid.
Background
The current chemical industry is more and more developed, the production amount of waste liquid and waste gas is more and more, the national requirement on environmental protection is more and more high, along with the development of production, a chemical production device is rapidly built on a large scale, the yield of harmful wastes is more and more, the technical requirement on the treatment of the harmful wastes is more and more high, the incineration technology is thorough in treatment, high efficiency, low investment, small occupied area and the like, the incineration device becomes an important technology in the chemical industry, the incineration device also becomes an important component in chemical equipment, the incineration method for treating organic wastes is an effective means for deeply oxidizing and treating organic matters in the waste liquid by utilizing air under the high-temperature condition, the wastes of organic compounds are generally incinerated at high temperature and converted into CO2And H2After O, the reaction mixture is discharged to the atmosphere. As long as the temperature in the incinerator is more than 800 ℃ and the waste has enough residence time in the high temperature zone in the incinerator, the waste can be decomposed basically and completely, thereby realizing pollution-free discharge, but for some wasteThe waste gas of chlorine-containing organic waste liquid generated in chemical production can emit HCl and free chlorine when being incinerated at high temperature. Chlorine has strong corrosivity, which not only causes high-temperature corrosion damage of a heating surface, but also causes low-temperature corrosion of a tail heating surface and a flue; more seriously, chlorine is an extremely toxic medium, and is easy to cause huge pollution to the environment, and all countries have strict regulations on the pollution. Therefore, how to achieve the standard discharge of the chlorine-containing waste is an important subject before engineering design workers.
For example, patent No. CN 101634453B can solve the problem of chlorine-containing waste, but has the disadvantages that a large amount of dilute hydrochloric acid is generated, a large amount of sodium hydroxide solution is consumed after alkali washing neutralization, a large amount of high-salinity wastewater is generated and needs to be discharged into a sewage treatment system to be treated up to the standard, HCL is removed by sacrificing alkali liquor, and the operation cost is high. Patent No. CN201520057318 proposes 'a treatment device for chlorine-containing salt-containing organic waste liquid', and the invention adopts the following process flows: the device has the advantages that an incineration treatment method is adopted, the temperature of a hearth is over 1200 ℃, the removal rate of organic matters is high, the liquid state can be used for collecting salt and recycling sewage, and the device has the defects that HCl gas and NOX generated by incineration are not subjected to special environment-friendly treatment, so that the smoke generated after incineration is difficult to achieve standard emission according to the control requirement of pollutant emission specified by the national environment-friendly standard. The ultimate goal of industrial waste treatment is to save cost in recycling and zero discharge, environmental protection equipment workers need to continuously make efforts, and a high-salt-content chlorine-containing organic waste liquid zero-discharge resource utilization system is provided for solving the problems.
Disclosure of Invention
The invention aims to provide a zero-emission resource utilization system for high-salt-content chlorine-containing organic waste liquid, which aims to solve the problems in the background art.
In order to achieve the purpose, the invention provides the following technical scheme: a zero-emission resource utilization system for chlorine-containing organic waste liquid with high salt content comprises a high-temperature incineration module, a quenching and restraining dioxin generation module, a gas-solid separation module, an HCl separation module, an alkali washing neutralization module, a low-temperature denitration module, a water treatment module and a molten salt cooling, conveying and packaging module, wherein the high-temperature incineration module, the quenching and restraining dioxin generation module, the gas-solid separation module, the HCl separation module, the alkali washing neutralization module and the low-temperature denitration module are sequentially connected through a flue, the high-temperature incineration module comprises a heat-insulation incinerator, two layers of main burners are arranged in the middle of the interior of the heat-insulation incinerator, an atomization spray gun is arranged at the upper end of the heat-insulation incinerator, a waste liquid pipeline and a compressed air pipeline are connected to the upper part of the outer side of the heat-insulation incinerator, a, the air pipeline is connected with a combustion-supporting fan, the bottom of the heat-insulation incinerator is connected with a waste heat boiler, a afterburning burner is installed inside the waste heat boiler, a soot blowing device is arranged on the right side of the waste heat boiler, a steam drum is arranged on the upper side of the heat-insulation boiler, the lower end of the steam drum is connected with a heated surface inside the waste heat boiler through a pipeline, the upper end of the steam drum is connected with a saturated steam pipeline, the right end of the steam drum is connected with a desalination and oxygen removal water pipeline, and a boiler water feeding pump is connected to;
quenching containment dioxin generates module includes quench tower, quenching spray gun, quench water pump, quench water jar, the quenching spray gun is installed to the inside top of quench tower, the upper right end of quench tower is connected with the quench water jar through pipeline and quench water pump, quench water jar right-hand member is connected with desalination deoxidization water pipeling, the quench tower lower extreme has quench tower replacement storehouse through the pipe connection, the quench tower right-hand member passes through the flue and connects gas-solid separation module.
The gas-solid separation module comprises a bag-type dust remover or a ceramic membrane gas-solid separator and a compressed air buffer tank, the left upper end of the bag-type dust remover or the ceramic membrane gas-solid separator is connected with the compressed air buffer tank through a pipeline, the right end of the compressed air buffer tank is connected with a compressed air pipeline, the lower end of the bag-type dust remover or the ceramic membrane gas-solid separator is connected with a bag replacement bin through a pipeline, the right upper end of the quenching tower replacement bin is connected in parallel with a flue between the quenching tower and the bag-type dust remover or the ceramic membrane gas-solid separator through a flue, the right upper end of the bag replacement bin is connected in parallel with a main flue at the outlet of the bag-type dust remover or the ceramic membrane gas-solid separator through;
the HCl separation module comprises a pre-cooling tower, a primary absorption tower, a circulating acid tank, a heat exchanger, an acid storage tank, a secondary absorption tower and a secondary heat exchanger, wherein a cooling spray gun is installed at the upper end inside the pre-cooling tower, the upper end of the pre-cooling tower is connected with the primary heat exchanger through a pipeline, the upper end of the heat exchanger is connected with the circulating acid tank through a pipeline and a primary circulating pump, the upper right end of the circulating acid tank is connected with the acid storage tank through a pipeline, the right end of the acid storage tank is connected with a hydrochloric acid pipeline and a hydrochloric acid delivery pump, the bottom of the right side of the pre-cooling tower is connected with a storage tank in the bottom of the primary absorption tower through a pipeline, the upper left end of the primary absorption tower is connected with a pipeline between the pre-cooling tower and the heat exchanger through a pipeline, the lower right end of the primary absorption tower is respectively connected with, the left side of the secondary absorption tower is provided with a secondary heat exchanger, the lower end of the secondary heat exchanger is connected with a storage tank at the bottom end of the secondary absorption tower through a pipeline and a secondary circulating pump, the pipeline above the secondary circulating pump is also connected with the bottom of the primary absorption tower, the upper end of the secondary heat exchanger is connected with the middle upper end of the secondary absorption tower through a pipeline, the right upper end of the secondary absorption tower is connected with a high-level water storage tank through a pipeline, and the left upper end of the high-level water storage tank is connected with a desalting and;
the alkali washing neutralization module comprises an alkali washing tower, the left upper end of the alkali washing tower is connected with an alkali washing tank through a pipeline and an alkali washing circulating pump, the right end of the alkali washing tank is connected with an alkali solution pipeline, the right upper end of the alkali washing tank is respectively connected to the high-level water storage tank and the waste liquid buffer tank through pipelines, and the left upper end of the alkali washing tank is connected with a storage tank in the alkali washing tower through a pipeline and an alkali washing extraction pump;
the low-temperature denitration module comprises a denitration device, a denitration solution preparation tank, a denitration solution buffer tank, a static mixer and a denitration solution atomizing nozzle, wherein a flue gas heater is installed at the upper end of the denitration device, a flue gas heater burner is arranged in the flue gas heater, the left end of the flue gas heater burner is connected with a natural gas pipeline and an air pipeline, the right side of the denitration device is provided with the static mixer, the right end of the static mixer is connected with a desalting and deoxidizing water pipeline, the upper end of the static mixer is connected with the denitration solution buffer tank through a pipeline and a denitration solution booster pump, the upper right end of the denitration solution buffer tank is connected with the desalting and deoxidizing water pipeline, the upper left end of the denitration solution buffer tank is connected with the denitration solution preparation tank through a pipeline and a denitration delivery pump, and the right end of the denitration solution preparation, the left lower end of the denitration device is connected to the bottom of the chimney through a flue and an induced draft fan;
the water treatment module comprises a deaerator, wherein the left side and the right side of the lower end of the deaerator are connected with a desalination deaerator pipeline, and the upper end of the deaerator is connected with a low-pressure steam pipeline;
the molten salt cooling, conveying and packaging module comprises a double-shaft cooler, a water-cooling scraper slag remover and a packaging device, wherein the upper end of the middle of the water-cooling scraper slag remover is connected with the double-shaft cooler through a pipeline, the upper end of the double-shaft cooler is connected with the bottom end of the waste heat boiler through a pipeline, the left end of the double-shaft cooler is connected with a circulating cooling water upper water pipeline and a circulating cooling water return pipeline, the lower end of the water-cooling scraper slag remover is connected with the circulating cooling water upper water pipeline and the circulating cooling water return pipeline, the upper right end of the water-cooling scraper slag remover is respectively connected with the bottoms of a quench tower replacement bin and a cloth bag replacement bin through pipelines, and the leftmost;
further: the heat-insulation incineration boiler is characterized in that the combustion temperature of the heat-insulation incineration boiler is 1200 ℃, the waste heat boiler is in a membrane wall type and comprises a salt collecting chamber, a quenching chamber and a molten salt pool, the salt collecting chamber is arranged at the lower part of the heat-insulation incineration boiler, a fireproof furnace wall is laid inside the membrane wall of the salt collecting chamber, the quenching chamber is formed by a membrane water-cooling wall and a water-cooling screen, and a steam soot blower is arranged in the quenching chamber.
Further: the absorption tower is characterized in that the primary absorption tower is made of glass fiber reinforced plastic, three absorption filler layers are arranged inside the primary absorption tower, a primary absorption nozzle layer is arranged at the upper end of each absorption filler layer, pall ring fillers are arranged in the secondary absorption tower, a secondary absorption nozzle is arranged at the upper end of each pall ring filler, and a foam cover layer is arranged at the upper end of each secondary absorption nozzle.
Further: the first-stage heat exchanger and the second-stage heat exchanger are graphite heat exchangers, and the left ends of the first-stage heat exchanger and the second-stage heat exchanger are connected with a circulating cooling water upper water pipeline and a circulating cooling water return pipeline.
Further: and an alkaline washing packing layer is arranged at the upper end in the alkaline washing tower, and an alkaline washing spray nozzle is arranged at the upper end of the alkaline washing packing layer.
Further: the denitration device adopts a low-temperature denitration mode, the middle of the denitration device is provided with a three-layer denitration packing layer, a denitration solution atomizing nozzle is arranged above the denitration packing layer, the outer end of the left side of the denitration solution atomizing nozzle is connected with a static mixer through a pipeline, an agitator is arranged in a denitration solution preparation tank, a urea solution is adopted as a denitration catalyst, and the temperature is controlled to be 180-260 ℃.
Further: the temperature of the flue gas in the quenching tower is rapidly reduced from 550 ℃ to 180 ℃ within 1 s.
Compared with the prior art, the invention has the beneficial effects that:
1. the waste heat boiler is directly arranged at the lower part of the incinerator, and molten salt generated by incineration directly falls into a molten salt pool of a salt collecting chamber of the waste heat boiler, so that the temperature of the molten salt is always kept above the salt melting point of 100 ℃, and the problem that the salt solidifies and adheres to a wall surface is avoided;
2. the refractory castable is laid on the heating surfaces of the salt collecting chambers of the waste heat boiler, so that the problem that molten salt directly contacts the membrane wall to corrode the membrane wall is solved;
3. the secondary absorption tower adopts a foam cover layer, uses clear water to absorb HCl gas carried in the flue gas, and is matched with a packing layer to use, so that the absorption efficiency is higher;
4. the chlorine-containing salt-containing organic waste liquid can be subjected to resource treatment, utilization and recovery of dilute hydrochloric acid and byproduct salt, and the national sustainable development strategy is met;
5. organic chemical energy in the waste liquid can be effectively utilized while the organic waste liquid is subjected to environment-friendly standard-reaching treatment, and the byproduct saturated steam is supplied to users after being converted into heat energy by incineration;
6. the system can realize that the saline water generated by the wastewater zero-emission alkaline washing tower can be sent back to the incinerator for incineration, the solid salt generated after incineration is collected, and part of the water carried in the flue gas is washed by the alkaline washing tower and the two-stage absorption tower and collected for recycling;
the invention has reasonable design and compact structure, completely meets the national environmental protection requirement, lightens the burden of enterprises and is suitable for popularization and use.
Drawings
FIG. 1 is a schematic general flow diagram of the present invention;
FIG. 2 is a schematic view of a high temperature incineration module according to the present invention;
fig. 3 is a schematic diagram of a rapid cooling and dioxin generation suppressing module and a gas-solid separation module according to the present invention;
FIG. 4 is a schematic diagram of an HCL separation module of the present invention;
FIG. 5 is a schematic diagram of an alkaline cleaning neutralization module according to the present invention;
FIG. 6 is a schematic view of a low temperature denitration module according to the present invention;
FIG. 7 is a schematic view of a water treatment module according to the present invention;
FIG. 8 is a schematic view of a molten salt cooling delivery bagging module of the invention;
FIG. 9 is a schematic view of the adiabatic incinerator and the exhaust-heat boiler according to the present invention.
In the figure: 1. A waste liquid buffer tank, 2, a heat insulation incinerator, 3, a waste heat boiler, 4, a steam pocket, 5, a deaerator, 6, a quench tower, 7, a quench tower replacement bin, 8, a quench water tank, 9, a compressed air buffer tank, 10, a bag-type dust remover (or a ceramic membrane gas-solid separator), 11, a bag replacement bin, 12, a pre-cooling tower, 13, a primary absorption tower, 14, a circulating acid tank, 15, a primary heat exchanger, 16, an acid storage tank, 17, a secondary absorption tower, 18, a secondary heat exchanger, 19, a high-level water tank, 20, an alkali washing tower, 21, an alkali liquor tank, 22, a flue gas heater, 23, a denitration device, 24, a denitration solution preparation tank, 25, a denitration solution buffer tank, 26, a static mixer, 27, a chimney, 28, a waste liquid booster pump, 29, a combustion fan, 30, a main combustion combustor, 31, a afterburning combustor, 32, a double-shaft cooler, 33 and a water-cooling scraper, 34. soot blower, 35, boiler feed pump, 36, quench water pump, 37, primary extraction pump, 38, primary circulation pump, 39, hydrochloric acid delivery pump, 40, secondary circulation pump, 41, alkaline washing extraction pump, 42, alkaline washing circulation pump, 43, flue gas heater burner, 44, denitration delivery pump, 45, denitration booster pump, 46, induced draft fan, 47, storage tank, 48, packing device, 201, atomizing spray gun, 301, salt collecting chamber, 302, quench chamber, 303, molten salt bath, 601, quench spray gun, 1001, waste liquid pipeline, 1002, natural gas pipeline, 1003, air pipeline, 1004, saturated steam pipeline, 1005, desalinization water pipeline, 1006, low pressure steam pipeline, 1007, recirculated cooling water upper water pipeline, 1008, recirculated cooling water return pipeline, 1009, nitrogen pipeline, 1010, hydrochloric acid pipeline, 1011, compressed air pipeline, 1012, alkaline solution pipeline, 1013, denitration feed pipeline, 1201. the device comprises a cooling spray gun, 1301, an absorption filler layer, 1302, a primary absorption nozzle, 1701, pall ring filler, 1702, a secondary absorption nozzle, 1703, a bubble cap layer, 2001, an alkaline washing filler layer, 2002, an alkaline washing spray nozzle, 2301, a denitration filler layer, 2302, a denitration nozzle, 3401 and a steam soot blower.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1 to 9, the present invention provides a technical solution: contain high temperature burn module, rapid cooling suppression dioxin generate module, gas-solid separation module, HCl separation module, alkali wash in module, low temperature denitration module and water treatment module and fused salt cooling transport packing module, high temperature burn module, rapid cooling suppression dioxin generate module, gas-solid separation module, HCl separation module, alkali wash in module, low temperature denitration module loop through the flue and connect, high temperature burn the module including adiabatic burning furnace 2, be equipped with two-layer main burner 30 in the middle of adiabatic burning furnace 2 is inside, atomizing spray gun 201 is installed to adiabatic burning furnace 2 upper end, adiabatic burning furnace 2 outside upper portion is connected with waste liquid pipeline 1001 and compressed air pipeline 1011, waste liquid pipeline 1001 front end is connected with waste liquid booster pump 28 and waste liquid buffer tank 1, adiabatic boiler 2 left side is connected with natural gas pipeline 1002 and air pipeline 1003, be connected with combustion-supporting fan 29 on the air pipeline 1003, the bottom of the heat insulation incinerator 2 is connected with a waste heat boiler 3, a afterburning burner 31 is installed inside the waste heat boiler 3, a soot blower 34 is arranged on the right side of the waste heat boiler 3, a steam drum 4 is arranged on the upper side of the heat insulation boiler 2, the lower end of the steam drum 4 is connected with a heated surface inside the waste heat boiler 3 through a pipeline, the upper end of the steam drum 4 is connected with a saturated steam pipeline 1004, the right end of the steam drum 4 is connected with a desalting and deoxidizing water pipeline 1005, and a boiler water feed pump 35 is connected to the desalting and deoxidizing water pipeline 1005;
quenching containment dioxin generates module includes quench tower 6, quenching spray gun 601, quench water pump 36, quench water tank 8, quench spray gun 601 is installed to 6 inside tops of quench tower, 6 upper right ends of quench tower are connected with quench water tank 8 through pipeline and quench water pump 36, quench water tank 8 right-hand member is connected with desalination oxygen removal water pipeline 1005, 6 lower extremes of quench tower have quench tower to replace storehouse 7 through the pipe connection, 6 right-hand members of quench tower pass through flue connection gas-solid separation module.
The gas-solid separation module comprises a bag-type dust remover or ceramic membrane gas-solid separator 10 and a compressed air buffer tank 9, the left upper end of the bag-type dust remover or ceramic membrane gas-solid separator 10 is connected with the compressed air buffer tank 9 through a pipeline, the right end of the compressed air buffer tank 9 is connected with a compressed air pipeline 1011, the lower end of the bag-type dust remover or ceramic membrane gas-solid separator 10 is connected with a bag replacement bin 11 through a pipeline, the right upper end of the quenching tower replacement bin 7 is connected in parallel with a flue between the quenching tower 6 and the bag-type dust remover or ceramic membrane gas-solid separator 10 through a flue, the right upper end of the bag replacement bin 11 is connected in parallel with a main flue at the outlet of the bag-type dust remover or ceramic membrane gas-solid separator 10 through a flue, and the left lower ends of the;
the HCl separation module comprises a pre-cooling tower 12, a primary absorption tower 13, a circulating acid tank 14, a heat exchanger 15, an acid storage tank 16, a secondary absorption tower 17 and a secondary heat exchanger 18, wherein a cooling spray gun 1201 is installed at the upper end inside the pre-cooling tower 12, the upper end of the pre-cooling tower 12 is connected with the primary heat exchanger 15 through a pipeline, the upper end of the heat exchanger 15 is connected with the circulating acid tank 14 through a pipeline and a primary circulating pump 38, the upper right end of the circulating acid tank 14 is connected with the acid storage tank 16 through a pipeline, the right end of the acid storage tank 16 is connected with a hydrochloric acid pipeline 1010 and a hydrochloric acid delivery pump 39, the bottom of the right side of the pre-cooling tower 12 is connected with a storage tank 47 in the bottom of the primary absorption tower 13 through a pipeline, the upper left end of the primary absorption tower 13 is connected with a pipeline between the pre-cooling tower 12 and the heat exchanger 15 through a pipeline, the lower right end of the primary, the right side of the primary absorption tower 13 is connected with a secondary absorption tower 17 through a flue, the left side of the secondary absorption tower 17 is provided with a secondary heat exchanger 18, the lower end of the secondary heat exchanger 18 is connected with a storage tank 47 at the bottom end of the secondary absorption tower 17 through a pipeline and a secondary circulating pump 40, the pipeline above the secondary circulating pump 40 is also connected with the bottom of the primary absorption tower 13, the upper end of the secondary heat exchanger 18 is connected with the middle upper end of the secondary absorption tower 17 through a pipeline, the right upper end of the secondary absorption tower 17 is connected with a high-level water storage tank 19 through a pipeline, and the left upper end of the high-level water storage tank 19 is;
the alkaline washing neutralization module comprises an alkaline washing tower 20, the left upper end of the alkaline washing tower 20 is connected with an alkaline washing tank 21 through a pipeline and an alkaline washing circulating pump 42, the right end of the alkaline washing tank 21 is connected with an alkaline solution pipeline 1012, the right upper end of the alkaline washing tank 21 is respectively connected to the high-level water storage tank 19 and the waste liquid buffer tank 1 through pipelines, and the left upper end of the alkaline washing tank 21 is connected with a storage tank 47 in the alkaline washing tower 20 through a pipeline and an alkaline washing extraction pump 41;
the low-temperature denitration module comprises a denitration device 23, a denitration solution preparation tank 24, a denitration solution buffer tank 25, a static mixer 26 and a denitration solution atomizing nozzle 2302, wherein a flue gas heater 22 is installed at the upper end of the denitration device 23, a flue gas heater burner 43 is arranged inside the flue gas heater 22, the left end of the flue gas heater burner 43 is connected with a natural gas pipeline 1002 and an air pipeline 1003, the static mixer 26 is arranged on the right side of the denitration device 23, a desalting and deoxidizing water pipeline 1005 is connected to the right end of the static mixer 26, the upper end of the static mixer 26 is connected with the denitration solution buffer tank 25 through a pipeline and a denitration solution booster pump 45, the right upper end of the denitration solution buffer tank 25 is connected with the desalting and deoxidizing water pipeline 1005, the left upper end of the denitration solution buffer tank 25 is connected with the denitration solution preparation tank 24 through a pipeline and a denitration delivery pump 44, and the right end of the denitration solution preparation, the left lower end of the denitration device 23 is connected to the bottom of the chimney 27 through a flue and an induced draft fan 46;
the water treatment module comprises a deaerator 5, wherein the left side and the right side of the lower end of the deaerator 5 are connected with a desalting and deaerating water pipeline 1005, and the upper end of the deaerator 5 is connected with a low-pressure steam pipeline 1006;
the molten salt cooling, conveying and packaging module comprises a double-shaft cooler 32, a water-cooling scraper slag remover 33 and a packaging device 48, the upper end of the middle of the water-cooling scraper slag remover 33 is connected with the double-shaft cooler 32 through a pipeline, the upper end of the double-shaft cooler 32 is connected with the bottom end of the waste heat boiler 3 through a pipeline, the left end of the double-shaft cooler 32 is connected with a circulating cooling water upper water pipeline 1007 and a circulating cooling water return pipeline 1008, the lower end of the water-cooling scraper slag remover 33 is connected with a circulating cooling water upper water pipeline 1007 and a circulating cooling water return pipeline 1008, the upper right end of the water-cooling scraper slag remover 33 is respectively connected with the bottoms of a quench tower replacement bin 7 and a cloth bag replacement bin 11 through pipelines, and the leftmost side;
the combustion temperature of the heat-insulation incineration boiler 2 is 1200 ℃, the waste heat boiler 3 adopts a membrane wall type and consists of a salt collecting chamber 301, a quenching chamber 302 and a molten salt pool 303, the salt collecting chamber 301 is arranged at the lower part of the heat-insulation incineration boiler 2, a refractory furnace wall is laid inside the membrane wall of the salt collecting chamber 301, the quenching chamber 302 consists of a membrane water wall and a water cooling screen, and a steam soot blower 3401 is arranged in the quenching chamber 302.
The primary absorption tower 13 is made of glass fiber reinforced plastic, three layers of absorption filler layers 1301 are arranged inside the primary absorption tower 13, a layer of primary absorption nozzles 1302 is arranged at the upper ends of the absorption filler layers 1301, pall ring fillers 1701 are arranged in the secondary absorption tower 17, secondary absorption nozzles 1702 are arranged at the upper ends of the pall ring fillers 1701, and bubble cap layers 1703 are arranged at the upper ends of the secondary absorption nozzles 1702.
The primary heat exchanger 15 and the secondary heat exchanger 18 are both graphite heat exchangers, and the left ends of the primary heat exchanger 15 and the secondary heat exchanger 18 are both connected with a circulating cooling water upper water pipeline 1007 and a circulating cooling water return pipeline 1008.
An alkaline washing filler layer 2001 is arranged at the upper end inside the alkaline washing tower 20, and an alkaline washing spray nozzle 2002 is arranged at the upper end of the alkaline washing filler layer 2001.
The denitration device 23 adopts a low-temperature denitration mode, the middle of the denitration device 23 is provided with a three-layer denitration packing layer 2301, a denitration solution atomizing nozzle 2302 is arranged above the denitration packing layer 2301, the outer end of the left side of the denitration solution atomizing nozzle 2302 is connected with the static mixer 26 through a pipeline, a stirrer is arranged in the denitration solution preparation tank 24, the denitration agent adopts urea solution as a denitration catalyst, and the temperature is controlled at 180-260 ℃.
The temperature of the flue gas in the quenching tower 6 is rapidly reduced from 550 ℃ to 180 ℃ within 1 s.
Example one: firstly, high-salt-content chlorine-containing waste liquid is sent into a high-salt-content chlorine-containing waste liquid buffer tank 1, the high-salt-content chlorine-containing waste liquid enters the top of a heat-insulating incinerator 2 after being pressurized by a waste liquid booster pump 28, the waste liquid is atomized by compressed air and is sprayed into the heat-insulating incinerator 2 by an atomization spray gun 201, two layers of natural gas main combustion burners 30 are arranged on the heat-insulating incinerator 2, the high-temperature burning of 1200 ℃ in the heat-insulating incinerator 2 is controlled by burning natural gas, chlorine in the high-salt chlorine-containing waste liquid is converted into HCL gas which enters a next device, namely a waste heat boiler 3, along with flue gas, the waste heat boiler 3 is in a membrane wall type and is divided into a salt collecting chamber 301 and a quenching chamber 302, the salt collecting chamber 301 is arranged at the lower part of the heat-insulating incinerator 2, a fireproof furnace wall is laid inside the membrane wall of the salt collecting chamber 301 to protect the membrane wall, and high-temperature molten salt from the heat-insulating incinerator 2 is cooled in the salt collecting chamber 301 and falls into a molten salt pool 303 at the lower part of the salt collecting chamber 301 to be discharged out of the waste heat boiler 3; quench chamber 302 is made up by membrane wall water cooling screen, multiple spot steam soot blower 3401 has been arranged in the quench chamber 302, sweep to quench chamber 302 inside string ash, salt in the chlorine waste liquid of high salt becomes the molten state and directly falls into the fused salt pond 303 of exhaust-heat boiler 3 of adiabatic burning furnace 2 lower part, burner 31 has been arranged to the fused salt pond 303 top, make fused salt keep good mobility in the fused salt pond 303 through the afterburning natural gas, the fused salt flows out through the salt outlet of fused salt pond 303 lower part and gets into among the biaxial cooler 32, cool off the fused salt through the recirculated cooling water and fall into in the water-cooling scraper blade removes sediment machine 33 to solid-state discharge, carry to packing apparatus 48 by water-cooling scraper blade removes sediment machine 33 and pack.
In the demineralized water got into deaerator 5, carried out the deoxidization through letting in low pressure steam to the deaerator 5 in to the demineralized water and handled, the deaerated water after the deoxidization passes through boiler feed pump 35 and sends to in the steam pocket 4, and the stove water in the steam pocket 4 gets into in the exhaust-heat boiler 3 heating surface and produces saturated steam with the heat transfer of high temperature flue gas and discharge the steam pocket and send to factory steam pipe network, and the flue gas is in rapid cooling to 550 ℃ discharge exhaust-heat boiler 3 gets into in quench chamber 302 in the quench tower 6.
The desalted water and the deoxygenated water in the rapid cooling water tank 8 are pumped by a rapid cooling water pump 36 to spray and cool the flue gas in the rapid cooling tower, so that the temperature of the flue gas is rapidly cooled from 550 ℃ to 180 ℃, the generation of dioxin harmful substances is inhibited, part of solid salt particles carried by the flue gas are thrown out under the action of inertia and enter a rapid cooling tower replacement bin 7 at the lower part of the rapid cooling tower 6, because the flue gas contains a large amount of HCL gas, the thrown solid salt particles also carry part of HCL gas, therefore in solid salt granule gets into quench tower replacement storehouse 7, gaseous the displacing of HCL that carries in to the quench tower replacement storehouse 7 through letting in nitrogen gas to solid salt granule, use nitrogen gas to carry out gaseous HCL in the flue after sending back to quench tower 6, the water-cooling scraper blade slagging-off machine 33 that falls into the lower part is regularly discharged to solid salt granule in the quench tower replacement storehouse 7, is carried to packing device 48 in by water-cooling scraper blade slagging-off machine 33 and packs.
The low-temperature flue gas at 180 ℃ from the quenching tower 6 carries partial solid salt particles, the flue gas enters a bag-type dust remover 10, the flue gas is subjected to gas-solid separation again through the bag-type dust remover 10, a bag is subjected to back blowing regularly through compressed air in a compressed air buffer tank 9, so that the solid salt particles on the bag are blown down, the solid salt particles collected by the bag-type dust remover 10 carry partial HCL gas, therefore, a bag-type dust remover replacement bin 11 is arranged at the lower part of the bag-type dust remover 10, the bag-type dust remover replacement bin 11 is similar to the quenching tower replacement bin 7, after the HCL gas is replaced through nitrogen, the HCL gas enters an outlet flue of the bag-type dust remover 10 along with the nitrogen, the collected solid salt particles are regularly discharged into a water-cooling scraper slag remover 33 at the lower part of the bag-type dust remover replacement bin 11 and are sent to a packing device 48 for packing, and the solid, therefore, the bag-type dust collector 10 can achieve high removing efficiency, and the smoke at the outlet of the bag-type dust collector 10 basically does not carry solid salt.
In consideration of the safety, durability and economy of the system, the first-stage absorption tower 13 is made of glass fiber reinforced plastic, and the temperature of the flue gas at 180 ℃ at the outlet of the bag-type dust collector 10 is higher than the long-term use temperature of the glass fiber reinforced plastic, so the pre-cooling tower 12 is arranged at the front part of the first-stage absorption tower 13, the flue gas enters the pre-cooling tower 12, the flue gas is pre-cooled to about 80 ℃ by spraying dilute acid liquid through the first-stage circulating pump 38 and enters the first-stage absorption tower 13, the bottom of the pre-cooling tower 12 is communicated with the storage tank 47 at the lower part of the first-stage absorption tower 13, and the sprayed dilute acid liquid. The three-layer packing layer 1301 and the three-layer one-level absorption nozzle 1302 are arranged in the one-level absorption tower 13, HCl gas carried in the flue gas is absorbed once through a large amount of circulating dilute acid liquid, the contact area between the flue gas and the spraying dilute acid liquid can be greatly increased by using the packing type tower, the absorption efficiency of the HCL is improved, the sprayed and absorbed dilute acid liquid falls into the storage tank 47 at the bottom of the one-level absorption tower 13 and is pumped into the circulating acid tank 14 through the one-level extraction pump 37, and the dilute acid liquid can be heated up after being absorbed and cooled by the circulating dilute acid liquid, so that the one-level heat exchanger 15 is arranged to cool the circulating dilute acid liquid, and the circulating dilute acid liquid is cooled to 60 ℃ from 80 ℃. And then the dilute acid liquid in the circulating acid tank 14 is pumped by a primary circulating pump 38 and sent to a primary heat exchanger 15 for heat exchange, one part of the dilute acid liquid after heat exchange is sent to a pre-cooling tower 12 for spraying to pre-cool the flue gas, the other part of the dilute acid liquid is sent back to a primary absorption tower 13 for circulating spraying to absorb the HCL gas, when the circulating dilute acid liquid reaches a certain concentration, an acid discharge valve is opened, one part of the dilute acid liquid is discharged by the primary circulating pump 38 to an acid storage tank 16 for storage, and the dilute acid liquid in the acid storage tank 16 is discharged outside the boundary area through a hydrochloric acid pipeline 1010 and a hydrochloric acid delivery pump 39 for recovery treatment.
The flue gas at 60 ℃ after absorbing 13 a part of HCL gas by the first-stage absorption tower enters the second-stage absorption tower 17, pall ring packing 1701 is arranged in the second-stage absorption tower 17, a layer of second-stage absorption nozzles 1702 is arranged on the upper part of the pall ring packing 1701, and the dilute acid in the storage tank 47 at the lower part of the second-stage absorption tower 17 is extracted by the second-stage circulating pump 40 and enters a spraying layer to be sprayed and absorbed in the packing absorption tower. The flue gas and the circulating absorption diluted hydrochloric acid liquid move in the same direction, the contact area of the flue gas and the diluted hydrochloric acid is increased through the pall ring packing 1701, the HCL gas in the flue gas is dissolved in the diluted hydrochloric acid liquid, and the supersaturated water vapor is condensed into water. A bubble cap layer 1703 is arranged on the upper portion of the secondary absorption nozzle 1702, a water film is formed on the bubble cap layer 1703 by supplemented 25 ℃ industrial water, a gas-raising pipe is arranged in the bubble cap, a rotary space is formed between the bubble cap and the gas-raising pipe, flue gas enters the rotary space through the gas-raising pipe, is sprayed into the rotary space from a tooth seam of the bubble cap at a certain speed, and forms a bubbling contact with the industrial water film on the tower plate to perform a mass transfer process. The temperature of the flue gas absorbed by the secondary absorption tower 17 is reduced to 50-60 ℃. The absorbed dilute acid liquid falls into a storage tank 47 at the lower part of the secondary absorption tower 17, most of the dilute acid liquid is sent back to the secondary absorption tower 17 by a secondary circulating pump 40 to be used as spraying circulating absorption liquid, and the rest part of the dilute acid liquid is conveyed to a supplement liquid level of the primary absorption tower 13. Because the temperature of the flue gas rises in the process of absorbing HCL gas, the secondary heat exchanger 18 is arranged to cool the circulating diluted acid liquid of the secondary absorption tower to 40 ℃, and the cooled diluted acid liquid is sent back to the secondary absorption tower for spraying and absorption.
The flue gas after the HCL gas is absorbed by the two-stage absorption tower enters the alkaline washing tower 20, so that the flue gas is efficiently subjected to final washing treatment by using alkaline liquor. The alkali liquor is prepared from sodium hydroxide and industrial water in an alkali liquor tank 21, and the sodium hydroxide neutralizes residual HCL in the flue gas through acid-base neutralization reaction, so that the emission of acid gas in the flue gas meets the national standard requirement. Sodium chloride salts are generated and dissolved in the circulating absorption liquid when the sodium hydroxide lye absorbs HCL gas, and the front two-stage absorption tower can achieve high absorption efficiency for HCl gas, so that the amount of brine generated in the alkaline tower per hour is greatly reduced, and a small amount of brine generated by the alkaline tower 20 can be sent to the heat-insulating incinerator 2 for incineration treatment. When the sodium chloride salts in the circulating absorption liquid reach a certain concentration, discharging a part of salt water into the high-salt chlorine-containing waste liquid buffer tank, burning the high-salt chlorine-containing waste liquid into the heat-insulating incinerator 2 along with the high-salt chlorine-containing waste liquid, collecting and packaging the generated molten salt as a byproduct, and realizing zero emission of the system.
The flue gas after deacidification enters a flue gas heater, and the flue gas is reheated to 220 ℃ by the incineration auxiliary fuel of the flue gas heater 22 and then enters an SCR denitration device 23.
The SCR denitration device 23 adopts a low-temperature denitration mode, adopts a low-temperature denitration catalyst, sprays a denitration reducing agent into the flue gas at a temperature point of 180-260 ℃ to be fully mixed with the flue gas, and the mixed flue gas enters the low-temperature denitration catalyst to carry out redox reaction, so that nitrogen oxides carried in the flue gas are oxidized and reduced into nitrogen and water.
The treated flue gas reaching the standard of 220 ℃ is extracted by an induced draft fan 46, enters a chimney 48 and is discharged into the atmosphere.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.

Claims (7)

1. The utility model provides a high contains salt chlorine organic waste liquid zero release utilization system, contains high temperature and burns the module, the quenching suppression dioxin generates the module, gas-solid separation module, the HCl separation module, alkali wash in the module, low temperature denitration module and water treatment module and fused salt cooling transport packing module, and high temperature burns the module, the quenching suppression dioxin generates the module, gas-solid separation module, the HCl separation module, alkali wash in the module, the low temperature denitration module loops through the flue and connects its characterized in that: the high-temperature incineration module comprises a heat insulation incinerator (2), two layers of main burners (30) are arranged in the middle of the inside of the heat insulation incinerator (2), an atomization spray gun (201) is installed at the upper end of the heat insulation incinerator (2), a waste liquid pipeline (1001) and a compressed air pipeline (1011) are connected to the upper portion of the outer side of the heat insulation incinerator (2), a waste liquid booster pump (28) and a waste liquid buffer tank (1) are connected to the front end of the waste liquid pipeline (1001), a natural gas pipeline (1002) and an air pipeline (1003) are connected to the left side of the heat insulation boiler (2), a combustion fan (29) is connected to the air pipeline (1003), the bottom of the heat insulation incinerator (2) is connected with a waste heat boiler (3), a supplementary combustion burner (31) is installed inside the waste heat boiler (3), a soot blower (34) is arranged on the right side of the waste, the lower end of the steam drum (4) is connected with the internal heating surface of the waste heat boiler (3) through a pipeline, the upper end of the steam drum (4) is connected with a saturated steam pipeline (1004), the right end of the steam drum (4) is connected with a desalting and oxygen removing water pipeline (1005), and a boiler feed pump (35) is connected to the desalting and oxygen removing water pipeline (1005);
the quenching and restraining dioxin generating module comprises a quenching tower (6), a quenching spray gun (601), a quenching water pump (36) and a quenching water tank (8), wherein the quenching spray gun (601) is installed above the inside of the quenching tower (6), the upper right end of the quenching tower (6) is connected with the quenching water tank (8) through a pipeline and the quenching water pump (36), the right end of the quenching water tank (8) is connected with a desalting and oxygen removing water pipeline (1005), the lower end of the quenching tower (6) is connected with a quenching tower replacement bin (7) through a pipeline, and the right end of the quenching tower (6) is connected with a gas-solid separation module through a flue;
the gas-solid separation module comprises a bag-type dust remover or a ceramic membrane gas-solid separator (10) and a compressed air buffer tank (9), the left upper end of the bag-type dust collector or the ceramic membrane gas-solid separator (10) is connected with a compressed air buffer tank (9) through a pipeline, the right end of the compressed air buffer tank (9) is connected with a compressed air pipeline (1011), the lower end of the bag-type dust collector or the ceramic membrane gas-solid separator (10) is connected with a bag replacement bin (11) through a pipeline, the right upper end of the quenching tower replacement bin (7) is connected in parallel with a flue between the quenching tower (6) and a bag-type dust remover or a ceramic membrane gas-solid separator (10) through a flue, the right upper end of the cloth bag replacement bin (11) is connected in parallel with a main flue at the outlet of the cloth bag dust remover or the ceramic membrane gas-solid separator (10) through a flue, the left lower ends of the quenching tower replacement bin (7) and the cloth bag replacement bin (11) are connected with a nitrogen pipeline (1009);
the HCl separation module comprises a pre-cooling tower (12), a primary absorption tower (13), a circulating acid tank (14), a heat exchanger (15), an acid storage tank (16), a secondary absorption tower (17) and a secondary heat exchanger (18), wherein a cooling spray gun (1201) is installed at the upper end inside the pre-cooling tower (12), the upper end of the pre-cooling tower (12) is connected with the primary heat exchanger (15) through a pipeline, the upper end of the heat exchanger (15) is connected with the circulating acid tank (14) through a pipeline and a primary circulating pump (38), the upper right end of the circulating acid tank (14) is connected with the acid storage tank (16) through a pipeline, the right end of the acid storage tank (16) is connected with a hydrochloric acid pipeline (1010) and a hydrochloric acid delivery pump (39), the bottom of the right side of the pre-cooling tower (12) is connected with a storage tank (47) in the bottom of the primary absorption tower (13) through a pipeline, the upper left end of the primary absorption tower (13, the right lower end of the primary absorption tower (13) is respectively connected with an acid storage tank (16) and a circulating acid tank (14) through a pipeline and a primary extraction pump (37), the right side of the first-stage absorption tower (13) is connected with a second-stage absorption tower (17) through a flue, a secondary heat exchanger (18) is arranged at the left side of the secondary absorption tower (17), the lower end of the secondary heat exchanger (18) is connected with a storage tank (47) at the bottom end of the secondary absorption tower (17) through a pipeline and a secondary circulating pump (40), the pipeline above the second-stage circulating pump (40) is also connected with the bottom of the first-stage absorption tower (13), the upper end of the secondary heat exchanger (18) is connected with the middle upper end of the secondary absorption tower (17) through a pipeline, the right upper end of the secondary absorption tower (17) is connected with a high-level water storage tank (19) through a pipeline, the upper left end of the high-level water storage tank (19) is connected with a desalting and deoxidizing water pipeline (1005);
the alkali washing neutralization module comprises an alkali washing tower (20), the left upper end of the alkali washing tower (20) is connected with an alkali washing tank (21) through a pipeline and an alkali washing circulating pump (42), the right end of the alkali washing tank (21) is connected with an alkali solution pipeline (1012), the right upper end of the alkali washing tank (21) is respectively connected to the high-level water storage tank (19) and the waste liquid buffer tank (1) through pipelines, and the left upper end of the alkali washing tank (21) is connected with a storage tank (47) in the alkali washing tower (20) through a pipeline and an alkali washing extraction pump (41);
the low-temperature denitration module comprises a denitration device (23), a denitration solution preparation tank (24), a denitration solution buffer tank (25), a static mixer (26) and a denitration solution atomizing nozzle (2302), wherein a flue gas heater (22) is installed at the upper end of the denitration device (23), a flue gas heater burner (43) is arranged inside the flue gas heater (22), the left end of the flue gas heater burner (43) is connected with a natural gas pipeline (1002) and an air pipeline (1003), the static mixer (26) is arranged on the right side of the denitration device (23), the right end of the static mixer (26) is connected with a desalting and deoxidizing water pipeline (1005), the upper end of the static mixer (26) is connected with the denitration solution buffer tank (25) through a pipeline and a denitration solution booster pump (45), and the upper right end of the denitration solution buffer tank (25) is connected with a desalting and deoxidizing water pipeline (1005, the denitration solution buffer tank (25) is connected with a denitration solution preparation tank (24) at the upper left end through a pipeline and a denitration conveying pump (44), the denitration solution preparation tank (24) is connected with a desalting and oxygen removing water pipeline (1005) and a denitration feeding pipeline (1013) at the right end, and the denitration device (23) is connected to the bottom of a chimney (27) at the lower left end through a flue and an induced draft fan (46);
the water treatment module comprises a deaerator (5), wherein the left side and the right side of the lower end of the deaerator (5) are connected with desalting and deaerating water pipelines (1005), and the upper end of the deaerator (5) is connected with a low-pressure steam pipeline (1006);
the molten salt cooling, conveying and packing module comprises a double-shaft cooler (32), a water-cooling scraper slag remover (33) and a packing device (48), the upper end of the middle of the water-cooling scraper slag remover (33) is connected with a double-shaft cooler (32) through a pipeline, the upper end of the double-shaft cooler (32) is connected with the bottom end of the waste heat boiler (3) through a pipeline, the left end of the double-shaft cooler (32) is connected with a circulating cooling water upper water pipeline (1007) and a circulating cooling water return pipeline (1008), the lower end of the water-cooling scraper slag remover (33) is connected with a circulating cooling water upper water pipeline (1007) and a circulating cooling water return pipeline (1008), the right upper end of the water-cooling scraper slag remover (33) is respectively connected with the bottoms of the quenching tower replacement bin (7) and the cloth bag replacement bin (11) through pipelines, and a packing device (48) is arranged at the leftmost side of the water-cooling scraper slag remover (33).
2. The high-salt chlorine-containing organic waste liquid zero-emission resource utilization system according to claim 1, characterized in that: the heat insulation incineration boiler (2) is used for heating the waste heat boiler (3) at the combustion temperature of 1200 ℃, the waste heat boiler (3) is in a membrane wall type and comprises a salt collecting chamber (301), a quenching chamber (302) and a molten salt pool (303), the salt collecting chamber (301) is arranged at the lower part of the heat insulation incineration boiler (2), a fireproof furnace wall is laid inside the membrane wall of the salt collecting chamber (301), the quenching chamber (302) is formed by a membrane water cooling wall and a water cooling screen, and a steam soot blower (3401) is arranged in the quenching chamber (302).
3. The high-salt chlorine-containing organic waste liquid zero-emission resource utilization system according to claim 1, characterized in that: the primary absorption tower (13) is made of glass fiber reinforced plastic, three layers of absorption filler layers (1301) are arranged inside the primary absorption tower (13), a layer of primary absorption nozzles (1302) are arranged at the upper ends of the absorption filler layers (1301), pall ring packing (1701) is arranged in the secondary absorption tower (17), secondary absorption nozzles (1702) are arranged at the upper ends of the pall ring packing (1701), and a foam cover layer (1703) is arranged at the upper ends of the secondary absorption nozzles (1702).
4. The high-salt chlorine-containing organic waste liquid zero-emission resource utilization system according to claim 1, characterized in that: the primary heat exchanger (15) and the secondary heat exchanger (18) are graphite heat exchangers, and the left ends of the primary heat exchanger (15) and the secondary heat exchanger (18) are connected with a circulating cooling water upper water pipeline (1007) and a circulating cooling water return pipeline (1008).
5. The high-salt chlorine-containing organic waste liquid zero-emission resource utilization system according to claim 1, characterized in that: an alkaline washing filler layer (2001) is arranged at the upper end inside the alkaline washing tower (20), and an alkaline washing spray nozzle (2002) is arranged at the upper end of the alkaline washing filler layer (2001).
6. The high-salt chlorine-containing organic waste liquid zero-emission resource utilization system according to claim 1, characterized in that: the denitration device (23) adopts a low-temperature denitration mode, the middle of the denitration device (23) is provided with a three-layer denitration packing layer (2301), a denitration solution atomizing nozzle (2302) is arranged above the denitration packing layer (2301), the outer end of the left side of the denitration solution atomizing nozzle (2302) is connected onto a static mixer (26) through a pipeline, a stirrer is arranged in a denitration solution preparation tank (24), the denitration agent adopts urea solution as a denitration catalyst, and the temperature is controlled to be 180-260 ℃.
7. The high-salt chlorine-containing organic waste liquid zero-emission resource utilization system according to claim 1, characterized in that: the temperature of the flue gas in the quenching tower (6) is rapidly reduced from 550 ℃ to 180 ℃ within 1 s.
CN201911217670.8A 2019-12-03 2019-12-03 High-salt-content chlorine-containing organic waste liquid zero-emission resource utilization system Pending CN112902196A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113719839A (en) * 2021-07-16 2021-11-30 清远金谷智联环保产业研究院有限公司 Environment-friendly and economical treatment method for waste incineration/smelting system
EP4205833A1 (en) * 2021-12-30 2023-07-05 Indaver nv Method for processing waste comprising chlorine

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113719839A (en) * 2021-07-16 2021-11-30 清远金谷智联环保产业研究院有限公司 Environment-friendly and economical treatment method for waste incineration/smelting system
EP4205833A1 (en) * 2021-12-30 2023-07-05 Indaver nv Method for processing waste comprising chlorine
BE1030150B1 (en) * 2021-12-30 2023-07-31 Indaver Nv METHOD FOR PROCESSING CHLORINE WASTE

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