CN114890604B - System and method for treating salt-containing waste liquid based on in-liquid incineration technology - Google Patents

System and method for treating salt-containing waste liquid based on in-liquid incineration technology Download PDF

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CN114890604B
CN114890604B CN202210705370.XA CN202210705370A CN114890604B CN 114890604 B CN114890604 B CN 114890604B CN 202210705370 A CN202210705370 A CN 202210705370A CN 114890604 B CN114890604 B CN 114890604B
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steam
outlet
waste liquid
liquid
water
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CN114890604A (en
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马贵林
左武
崔灵丰
周海云
封凯
刘浩
周尤超
宋涛
涂勇
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Jiangsu Environmental Engineering Technology Co Ltd
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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
    • 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
    • B01D53/14—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 by absorption
    • B01D53/1456—Removing acid components
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • 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
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • 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
    • 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
    • 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
    • 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
    • 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
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
    • 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
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
    • 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
    • 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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Abstract

The invention relates to a saline waste liquid treatment system and method based on a submerged incineration technology. The method is characterized in that the dilute low-calorific-value salt-containing waste liquid is concentrated by a concentration system and then is sent to a liquid incinerator, the high-calorific-value waste liquid is used as a substitute fuel and is sent to the incinerator from the top of the incinerator together with natural gas, and harmful components in the waste liquid are thoroughly incinerated and removed in a high-temperature section of the incinerator. The method can simultaneously carry out harmless treatment on the low-calorific-value salt-containing waste liquid and the high-calorific-value salt-containing waste liquid to obtain the dry solid miscellaneous salt, has the advantages of low energy consumption, less wastewater discharge, low wastewater treatment unit price and the like, and has wide application prospect in the field of salt-containing waste liquid treatment.

Description

System and method for treating salt-containing waste liquid based on in-liquid incineration technology
Technical Field
The invention relates to the field of treatment of salt-containing waste liquid, in particular to a system and a method for treating salt-containing waste liquid based on a submerged incineration technology.
Background
According to the statistics of the China chemical industry environmental protection Association, the production amount of waste salt in the chemical industry is more than 1000 million tons every year, the storage amount of industrial waste salt in China is large, and the main disposal mode is landfill at present. However, most domestic landfill sites belong to flexible landfill sites, and according to the hazardous waste landfill pollution control standard GB 18598-2019, the flexible landfill sites can be fed with waste which satisfies the condition that the total amount of water-soluble salt is less than 10%, so industrial waste salt cannot enter the flexible landfill sites without pretreatment. The prior industrial waste salt which mainly comprises NaCl and Na2SO4 generally cannot meet the requirements after pretreatment, and only can enter a rigid landfill or be comprehensively utilized. The rigid landfill site has small storage capacity and high construction cost, and the rigid landfill disposal and comprehensive utilization cost is as high as 4000-6000 yuan/ton, and the disposal cost is expensive.
At present, common treatment technologies for waste salt comprise a physical chemical method and a thermochemical method, and toxic and harmful substances in the waste salt are removed, so that the conditions of subsequent harmless treatment or resource recycling of the waste salt are met.
1 physicochemical method. The physical and chemical method for treating industrial waste salt is mainly characterized in that chemical agents are added to the salt to generate neutralization, precipitation or oxidation reaction with toxic and harmful substances in the salt, so that the conversion and migration of the toxic and harmful substances are realized. At present, the method is mainly divided into a recrystallization method, a salt washing method, an advanced oxidation method and the like. (1) The recrystallization method is a treatment method in which crystals dissolved in a solvent or melted are recrystallized from a solution or a melt according to the difference in solubility of a solute. The method is easy to operate and low in cost, but has low organic matter removing efficiency, and is mainly used for refining and separating the waste salt after detoxification and harm removal. (2) The salt washing method is to wash the waste salt with saturated salt water to dissolve organic matters, heavy metals and other matters in the waste salt into the washing liquid, so as to purify the salt. The method is simple to operate, low in treatment cost, narrow in application range, low in treatment efficiency, and difficult to treat high-salinity wastewater, and is only suitable for treating waste salt with simple components and low impurity content, and multi-stage washing is often required. (3) The advanced oxidation method is to oxidize toxic and harmful organic pollutants by means of the strong oxidizing property of a chemical oxidant on the basis of cleaning saturated salt water, thereby realizing the harmlessness of waste salt and obtaining clean byproduct salt. The treatment effect of the advanced oxidation method is usually determined by the properties of organic pollutants, the application range is small, the consumed oxidant amount is large, and the treatment cost is high; in addition, the dosage of the oxidant is not easy to control, and the problems of waste of excessive oxidant, incomplete removal of organic matters and the like are easily caused.
2 thermochemical process. The thermochemical method mainly utilizes the characteristic that organic impurities in salt residues are easy to decompose and volatilize under the high-temperature condition, decomposes the organic impurities into volatile gas through high-temperature treatment, and realizes effective separation from solid salt residues, thereby achieving the purpose of removing the organic impurities. The thermochemical method has obvious reduction effect and high organic matter removal rate, is considered to be the most effective and feasible method for harmless treatment of hazardous solid waste containing salt as a byproduct, and the conventional thermochemical method treatment technology comprises a thermal incinerator, a flap incinerator, a pyrolysis furnace, a rotary kiln incinerator and the like. In the treatment process, inorganic salt is softened in a high-temperature environment, so that the problems of equipment blockage, corrosion and the like caused by the fact that the salt is adhered to the wall of a heating surface at the tail part of an incinerator and scales are caused. Meanwhile, the conventional thermochemical method usually needs to consume a large amount of natural or diesel fuel and other fuels, the energy consumption of the system is high, and the unit disposal cost is high, so that the large-scale utilization of the thermochemical method is limited. If a waste salt thermochemical treatment system which has low energy consumption, large waste liquid treatment scale and no risk of molten salt particle blockage can be developed, the application prospect of the thermochemical method can be greatly improved.
The invention provides a sodium salt-containing organic waste liquid incinerator and an incineration process method thereof, wherein the invention is CN106989405A in China through retrieval. The system comprises an incineration chamber, a combustor is arranged at the top of the incineration chamber, the combustor is provided with an organic waste liquid inlet and an auxiliary fuel inlet which are communicated with the incineration chamber, and the bottom of the side wall of the incineration chamber is provided with a molten state slag discharge port and an excessive settling chamber. The excessive settling chamber comprises an excessive inlet and an excessive outlet, the excessive inlet is arranged along the horizontal direction and is connected with the incineration chamber, and a steam tube bank is arranged in the excessive settling chamber and used for recovering system waste heat. This system sets up the heat transfer bank of tubes in excessive settling chamber top, can utilize the heat of combustion of organic waste liquid, improves the economic nature of system. By analyzing the system, a large number of heating surfaces are arranged on the upper side of the excessive settling chamber arranged at the outlet of the incinerator, and high-temperature semi-molten ash particles are cooled on the heating surfaces during normal operation, so that large-area blockage is formed.
The invention also discloses CN112225275A in China, and provides a device and a system for efficiently evaporating salt-containing organic wastewater. The system comprises a high-efficiency evaporation device, a gas-liquid heat exchange device and a depth treatment device, wherein the high-efficiency evaporation device is an immersed combustion evaporator, the top of the evaporator is provided with a burner, a demister and a smoke outlet, the side surface of the evaporator is provided with a manhole, a liquid level meter, a valve pipeline and the like, the bottom of the evaporator is provided with an emptying valve, a salt mud well, a hand hole and a screw pump, and the inside of the evaporator is provided with a combustion chamber, a baffle plate and the like. The invention adopts the injection type nozzle for gas distribution, improves the heat transfer efficiency between the flue gas and the evaporated liquid, strengthens the internal circulation of the evaporator, has the advantages of high capacity utilization efficiency, low pollutant discharge and the like in a complete system, and has certain applicability to the quantitative reduction treatment of part of salt-containing waste liquid. However, the system cannot fully treat and remove toxic and harmful components in the salt-containing waste liquid, only can play a role in reduction, and only has applicability to a part of the waste liquid. Meanwhile, the salt-containing wastewater is concentrated by an RO membrane, the waste heat of the system is not fully utilized, and the operation cost is high.
Disclosure of Invention
In order to solve the problems discussed above, the invention discloses a saline waste liquid treatment system and method based on a submerged incineration technology, which solve the problems that the waste heat of the saline waste liquid is difficult to recover in the treatment process, the heating surface is easy to block, the overhaul and maintenance are frequent, the discharge amount of the waste water of the treatment system is large, the treatment scale is limited, and the like.
In order to achieve the purpose, the technical scheme of the invention is as follows:
a saline waste liquid treatment system based on a submerged incineration technology comprises a submerged incinerator body, a positive pressure steam generator, a quench tank, a low-calorific-value waste liquid concentration system, an integrated absorption tower, a disturbance pump, a saturated liquid discharge pump, a crystallized salt recovery system, a bypass regulating valve, a first water supply regulating valve, a fresh water discharge pump, a fresh water control valve and a fresh water bypass valve;
the liquid incinerator body is sequentially provided with a combustion section, a high-temperature section, a low-temperature section and a liquid salt discharge section from top to bottom;
wherein the combustion section is internally provided with a multifunctional burner which is used for spraying high-calorific-value salt-containing waste liquid and auxiliary fuel into the combustion section for full combustion, so that the temperature of the flue gas is more than 1100 ℃ in the high-temperature section after the flue gas enters the high-temperature section,
a special spray gun is arranged in the high-temperature section and is used for spraying the concentrated low-calorific-value salt-containing waste liquid into the high-temperature section, the volume of the high-temperature section ensures that the flue gas stays in the high-temperature section for more than 2s,
a positive pressure steam generator is arranged in the low temperature section, the positive pressure steam generator is a heat exchanger, one side of the positive pressure steam generator is introduced with feed water, the other side of the positive pressure steam generator is introduced with flue gas, the positive pressure steam generator is used for absorbing partial heat of the flue gas to heat the feed water and generate positive pressure steam, the temperature of the flue gas is still kept above 850 ℃ after the flue gas is absorbed by the positive pressure steam generator, the low temperature section is also provided with an SNCR urea spray gun for denitration,
the liquid salt discharging section is in a cone shape with a hole at the bottom and gradually necking down along the smoke direction;
the quenching tank is provided with a flue gas inlet, a flue gas outlet, a starting water replenishing port, a water inlet and a liquid outlet, the bottom of the quenching tank is provided with a jet nozzle,
the flue gas inlet of the quenching tank is connected with the bottom outlet of the liquid salt discharge section, the flue gas outlet of the quenching tank is connected with the integrated absorption tower, the integrated absorption tower is used for deacidifying the entering flue gas and discharging the deacidified flue gas, and the high-salt-content wastewater generated by the deacidification and discharge of the deacidified flue gas is periodically discharged,
the high-salt-content wastewater discharged by the integrated absorption tower is connected to a water inlet of the quenching tank,
a liquid outlet pipeline of the quenching tank is connected with a saturated liquid discharge pump, the saturated liquid discharge pump is connected to a crystallization salt recovery system, the crystallization salt recovery system is provided with a saturated liquid reflux main pipe, the saturated liquid reflux main pipe is connected into the quenching tank, the crystallization salt recovery system is used for separating crystallization salt and sending the separated liquid back to the quenching tank,
the quenching tank is also provided with an outlet connected with a disturbance pump, the outlet of the disturbance pump is provided with two paths, one path is connected with a jet nozzle at the bottom of the quenching tank, the other path is connected with the quenching tank through a bypass adjusting valve,
the low heat value waste liquid concentration system has the functions of concentrating the dilute low heat value waste liquid into concentrated low heat value waste liquid by using steam as a heat source,
the low heat value waste liquid concentration system is provided with a waste liquid inlet which is used as an inlet of the dilute low heat value waste liquid,
the low heat value waste liquid concentration system is provided with a waste liquid outlet which is connected to a special spray gun in the high temperature section and is used for spraying concentrated low heat value waste liquid into the high temperature section,
the low-heat value waste liquid concentration system is provided with a fresh water outlet for discharging fresh water separated during concentration of the dilute low-heat value waste liquid, the fresh water outlet is connected to a fresh water discharge pump, the outlet of the fresh water discharge pump is divided into two paths, one path is connected to the quenching tank through a fresh water control valve, the other path is connected to the waste water treatment system through a fresh water bypass valve,
the low-heat value waste liquid concentration system is provided with a positive pressure steam inlet, positive pressure steam discharged by a positive pressure steam generator is connected to the positive pressure steam inlet,
the low-heat-value waste liquid concentration system is provided with a steam drain port, is connected into the positive-pressure steam generator through a first water supply regulating valve, and is used for absorbing smoke heat by taking the drained water of the steam drain port as the water supply of the positive-pressure steam generator.
Further comprises a second water supply regulating valve and a negative pressure steam generator,
the low-calorific-value waste liquid concentration system comprises an evaporator, a first steam-water separator, a second steam-water separator, a two-section steam-supplementing type evaporator, a dead steam cooler, a condensed water tank, a first circulating pump, a second circulating pump, a transfer pump, a concentrated low-calorific-value waste liquid conveying pump, a drain tank, a vacuum pump and a water feeding pump;
the steam inlet of the evaporator is connected with the steam outlet of the positive pressure steam generator,
the drain outlet of the evaporator is connected with the drain tank,
the waste liquid inlet of the evaporator is connected with the first circulating pump,
the waste liquid inlet of the evaporator is also connected with a concentrated low-heat value waste liquid delivery pump,
the vapor-liquid outlet of the evaporator is connected with the first vapor-water separator,
the secondary steam outlet of the first steam-water separator is connected with the two-section steam-supplementing evaporator,
the separation liquid outlet of the first steam-water separator is connected with the inlet of the first circulating pump,
the liquid supplementing port of the first steam-water separator is connected with the outlet of the transfer pump,
two steam inlets of the two-section steam-supplementing type evaporator are respectively connected with a steam outlet of the negative pressure steam generator and a secondary steam outlet of the first steam-water separator, two drain outlets of the two-section steam-supplementing type evaporator are respectively connected with a drain tank and a condensate water tank,
the vapor-liquid outlet of the two-section steam-supplementing evaporator is connected with the second vapor-water separator,
the waste liquid inlet of the two-section steam-supplementing evaporator is connected with the outlet of the second circulating pump,
the waste liquid inlet of the two-section steam-supplementing evaporator is also connected with the inlet of the transfer pump,
the waste liquid inlet of the second steam-water separator is used for introducing dilute low-heat-value waste liquid,
the secondary steam outlet of the second steam-water separator is connected with the dead steam cooler,
the separation liquid outlet of the second steam-water separator is connected with a second circulating pump,
the vapor-liquid inlet of the second vapor-water separator is connected with the two sections of steam-supplementing evaporators,
the negative pressure steam area and the condensed water tank of the two sections of steam compensating evaporators are provided with pumping ports which are connected with the pumping port of the vacuum pump,
the drainage outlet of the dead steam cooler is connected with a condensed water tank,
the outlet of the condensed water tank is connected with the inlet of the fresh water discharge pump,
the drain tank is provided with a water replenishing port,
the drain outlet of the drain tank is connected with a water supply pump,
the outlet of the feed water pump is connected with the first feed water regulating valve and the second feed water regulating valve to respectively feed water to the positive pressure steam generator and the negative pressure steam generator,
and an outlet of the concentrated low-calorific-value waste liquid conveying pump is connected with a high-temperature section of the submerged incinerator.
Wherein the negative pressure steam generator is used for further absorbing the heat in the flue gas and generating negative pressure steam,
before the exhanst gas outlet of quench jar was connected to the integration absorption tower, it had earlier passed through negative pressure steam generator for further absorb the heat in the flue gas, the exhanst gas temperature that the exhanst gas outlet of quench jar got into negative pressure steam generator is 80-90 ℃, negative pressure steam generator also has water seal for collect the comdenstion water in the flue gas, and carry out the water seal to the flue, water seal outlet connection to the water inlet of quench jar.
Furthermore, the internal structure of the two sections of steam supplementing evaporators is in an inner-outer sleeve form and comprises a waste liquid inlet, a waste liquid outlet, an inlet pipe plate, an outlet pipe plate, a negative pressure steam inlet, a secondary steam inlet, a drain outlet, a condensed water outlet, a non-condensable gas outlet, a first heat exchange pipe bundle, a steam partition plate, a spiral partition plate, an arch partition plate, a second heat exchange pipe bundle and a shell, the two sections of steam supplementing evaporators adopt the steam partition plate to partition two kinds of quality steam, the second heat exchange pipe bundle on the inner side is used for removing the secondary steam, the first heat exchange pipe bundle on the outer side is used for removing the negative pressure steam,
the arched clapboard is arranged at the inner side of the steam clapboard and is used for disturbing flow of secondary steam,
the spiral clapboard is arranged at the outer side of the steam clapboard and is used for disturbing negative pressure steam,
the waste liquid inlet and the waste liquid outlet are connected with the shell,
the first heat exchange tube bundle and the second heat exchange tube bundle are in expanded joint with the inlet tube plate and the outlet tube plate,
the drainage of the secondary steam on the inner side is discharged from a condensed water outlet, the drainage of the negative pressure steam on the outer side is discharged from a drainage outlet, and the non-condensed gas of the negative pressure steam on the outer side is extracted from a non-condensed gas outlet. .
Further, the crystallized salt recovery system comprises a heat exchanger, a bubbling bed dryer, a centrifuge, a cyclone and a dust remover,
the outlet of the saturated liquid discharge pump is connected with the saturated liquid inlet of the heat exchanger,
the saturated liquid outlet of the heat exchanger is connected with a cyclone, the overflow outlet of the cyclone is connected with a saturated liquid reflux main pipe,
the underflow outlet of the cyclone is connected with a centrifuge,
the outlet of the centrifugal machine separation liquid is connected back to the saturated liquid reflux main pipe,
the outlet of the centrifuge is connected with the material inlet of the bubbling bed dryer,
the outlet of the bubbling bed dryer is used for outputting the finished product miscellaneous salt,
the air side outlet of the heat exchanger is connected with a bubbling bed dryer,
the exhaust gas outlet of the bubbling bed is connected with a dust remover,
the exhaust gas outlet of the dust remover is connected to the combustion section of the incinerator in the liquid to be used as air supplement.
And a bottom ash outlet of the dust remover is used for outputting finished product miscellaneous salt.
A method for treating salt-containing waste liquid based on a liquid incineration technology comprises the following steps:
step 1: spraying the high-calorific-value salt-containing waste liquid and natural gas into a furnace from a combustion section for combustion, and forming high temperature of over 1100 ℃ in a high-temperature section;
and 2, step: the flue gas flows through a high-temperature section, a low-temperature section and a liquid salt removal section in sequence and then enters a quenching tank, water is added into the quenching tank from a starting water replenishing port during initial starting, and the flue gas is rapidly cooled after contacting with liquid in the quenching tank and then discharged into an integrated absorption tower for deacidification;
and step 3: the integrated absorption tower discharges the high-salt-content wastewater generated by deacidification into a quenching tank;
and 4, step 4: absorbing heat of flue gas by feed water provided by a low-calorific-value waste liquid concentration system through a positive pressure steam generator to heat the feed water into positive pressure steam, keeping the outlet temperature of a low-temperature section to be higher than 850 ℃, adding dilute low-calorific-value salt-containing waste liquid into the low-calorific-value waste liquid concentration system, concentrating the dilute low-calorific-value salt-containing waste liquid into concentrated low-calorific-value salt-containing waste liquid by using the positive pressure steam, discharging fresh water separated from the dilute low-calorific-value salt-containing waste liquid into a quench tank or a wastewater treatment system, recycling drainage of the positive pressure steam as the feed water, and spraying the concentrated low-calorific-value salt-containing waste liquid into a hearth from a high-temperature section through a special spray gun;
and 5: sending the liquid containing the crystallized salt in the quenching tank into a crystallized salt recovery system by using a saturated liquid discharge pump, discharging the crystallized salt, and sending the separated liquid back to the quenching tank;
and 6: the liquid in the quenching tank is pumped out by using a disturbance pump and then is sprayed from a jet nozzle at the bottom of the quenching tank.
Further, step 6 includes adjusting the flow rate of the jet nozzle at the bottom of the quench tank using a bypass regulator valve.
A concentration method of a saline waste liquid treatment system based on an in-liquid incineration technology comprises the following steps:
step 1: when the system is started for the first time, the dilute low-calorific-value salt-containing waste liquid enters from a waste liquid inlet of the second steam-water separator,
and passes through the second circulating pump, the transfer pump and the first circulating pump,
adding a certain amount of dilute low-heat-value waste liquid into an evaporator and a two-section steam-supplementing evaporator;
step 2: starting a vacuum pump to establish and maintain a certain vacuum degree in a negative pressure steam area and a condensation water tank of the two-section steam supplementing type evaporator;
and step 3: supplementing water in the drainage tank, maintaining a certain water level, and sending the feed water to the positive pressure steam generator through a feed water pump;
and 4, step 4: introducing the positive pressure steam from the positive pressure steam generator into the evaporator,
the drainage of the positive pressure steam is discharged into a drainage tank,
the low heat value waste liquid at the bottom of the evaporator is conveyed to a high temperature section by a concentrated low heat value waste liquid conveying pump at regular intervals,
the vapor and the liquid of the evaporator are sent into a first vapor-water separator,
the separated liquid separated by the first steam-water separator is sent back to the evaporator by the first circulating pump,
the secondary steam separated by the first steam-water separator is sent to the two-section steam-supplementing type evaporator;
and 5: respectively introducing the secondary steam of the first steam-water separator and the steam of the negative pressure steam generator into two sections of steam-supplementing evaporators,
the drained water of the secondary steam of the first steam-water separator is discharged into a condensed water tank,
the drainage of the steam of the negative pressure steam generator is discharged into a drainage tank,
the low heat value liquid at the bottom of the two-section steam-supplementing evaporator is periodically sent into the first steam-water separator through a transfer pump,
the vapor and liquid of the two-section steam-supplementing evaporator are sent into a second vapor-water separator,
the separated liquid from the second steam-water separator is sent back to the two-section steam-supplementing evaporator through a second circulating pump,
the waste liquid inlet of the second steam-water separator is supplemented with dilute low-heat value salt-containing waste liquid,
the secondary steam of the second steam-water separator is discharged into a condensate water tank after being cooled by a dead steam cooler,
and (4) periodically discharging the fresh water in the condensed water tank into a quenching tank or a wastewater treatment system.
A method for recovering crystallized salt of a salt-containing waste liquid treatment system based on a submerged incineration technology comprises the following steps:
step 1: saturated liquid in the quenching tank is sent into a heat exchanger through a saturated liquid discharge pump at regular intervals, the heat exchanger cools the saturated liquid through air, and the obtained hot air enters a bubbling bed dryer;
and 2, step: the cooled saturated liquid enters a cyclone for solid-liquid separation, the separated liquid returns to a quenching tank, and the separated crystal salt enters a centrifugal machine for deep dehydration;
and 3, step 3: returning the separated liquid of the centrifuge to the quenching tank, and allowing the crystallized salt separated by the centrifuge to enter a bubbling bed dryer;
and 4, step 4: hot air in the bubbling bed dryer directly contacts with crystallized salt from a centrifuge, the dried crystallized salt is finished product miscellaneous salt, and waste gas at the outlet of the bubbling bed dryer enters a dust remover;
and 5: the fine crystal salt particles collected by the dust remover are the finished product miscellaneous salt, and the wet tail gas of the dust remover is sent to the combustion section of the liquid incinerator for burning as the supplementary air.
The beneficial effects of the invention are:
the complete system developed by 1 can realize harmless, reduction and resource treatment of high-calorific-value and low-calorific-value salt-containing waste liquid. The high-calorific-value salt-containing waste liquid is sprayed out from a burner of a special burner at the top of the furnace and sent into the furnace for burning and heat supplementing to replace part of fuel required by burning, and the low-calorific-value waste liquid is concentrated by waste heat recovered by the system, sent to a low-calorific-value waste liquid spray gun of the incinerator and treated by the incinerator system to obtain harmless industrial miscellaneous salt.
2, deep recovery of waste heat. Burn burning furnace low temperature section in novel liquid and set up positive pressure steam generator for retrieve partial high temperature flue gas waste heat, the flue sets up negative pressure steam generator and retrieves the low temperature saturated flue gas heat behind the stove simultaneously, high-temperature steam and low temperature negative pressure steam that positive pressure steam generator and negative pressure steam generator produced respectively are used for low heat value waste liquid evaporative concentration, the system make full use of development fuel and the heat that high heat value waste liquid burning was emitted have fine energy saving and emission reduction effect.
3, the discharge amount of waste water is small. The saturated liquid containing salt discharged from the bottom of the quenching tank is sent to a crystallized salt separation system to obtain dry finished salt, the mother liquid flows back to the quenching tank for recycling, and no wastewater is discharged out of the incinerator body. Meanwhile, salt-containing wastewater generated by the integrated absorption tower, fresh water generated by the low-calorific-value waste liquid concentration system and flue gas condensate water generated by the negative pressure steam generator are used as water supplement of the quenching tank, zero water supplement and zero water drainage can be realized during normal operation of the system, and when the low-calorific-value waste liquid is operated at a high concentration rate, generated redundant fresh water can be sent to a factory wastewater treatment system and a miscellaneous water section.
4, an anti-blocking high-rate concentration quenching tank and a miscellaneous salt drying system are developed. Novel burning furnace exhaust high temperature flue gas and liquid miscellaneous salt get into the concentrated rapid cooling jar of high multiplying power through the honeycomb duct in the liquid, salt solution and high temperature flue gas and fuse salt contact in the concentrated rapid cooling jar of high multiplying power, with the high temperature flue gas and the liquid miscellaneous salt that burning furnace produced in the novel liquid cool down to 90 ℃ in the twinkling of an eye, the steam that evaporates in the flue gas and the jar then discharges through the rapid cooling tank deck, through the water supplementation volume in the control rapid cooling jar, can realize that the salt solution is direct concentrated in the rapid cooling jar, and then reduce the concentrated equipment investment cost outside the tower. And (4) sending the saturated salt solution obtained by concentrating the salt solution in the tank at a high rate to a crystallized salt separation system to obtain dry finished product miscellaneous salt.
5a negative pressure steam generator was developed. The negative pressure steam generator is used for recovering the saturated flue gas waste heat at the low temperature of about 90 ℃ after the quenching tank, and generating saturated steam at the temperature of about 70 ℃ for concentrating the low-calorific-value salt-containing waste liquid.
6A two-stage steam-supplying type steaming device is developed. The developed two-section steam-supplementing type evaporator is a vertical evaporator and adopts a sleeve structure, a steam source on the outer side of the sleeve is negative pressure steam generated by a negative pressure steam generator, and a steam source on the inner side of the sleeve is secondary steam generated by a preceding-stage evaporator. Because the sleeve is adopted to isolate the steam with two qualities, the two-section steam-supplementing type evaporator can realize the combined heating of saturated waste liquid by the steam with two qualities, and simultaneously avoid the increase of the water discharge amount of the system and the overhigh operation cost of a softened water system caused by the mixing of the drainage with two qualities.
7 a novel four-stage type liquid medium incinerator is developed. The novel liquid medium incinerator is divided into a combustion section, a high-temperature section, a low-temperature section and a molten salt discharge section, wherein the combustion section, the high-temperature section and the molten salt discharge section are all heat insulation wall surfaces except for the fact that the low-temperature section is a water cooling wall heating surface. The high-heat value waste liquid and the natural gas are combusted in the combustion section, the high temperature of over 1100 ℃ is formed in the high-temperature section, and meanwhile, the high-temperature section of the incinerator in the liquid can ensure that the flue gas stays for over 2s at the temperature of over 1100 ℃, so that the harmful substances in the waste liquid are completely incinerated. A positive pressure steam generator is arranged at the low temperature section of the in-liquid incinerator and used for recovering waste heat of high-temperature flue gas to generate high-parameter steam, the temperature of the flue gas is maintained to be above 850 ℃, molten salt is guaranteed to be in a liquid state, and an optimal working temperature section is created for liquid discharge of waste salt generated at the bottom of the in-liquid incinerator and SNCR denitration. The molten salt discharge section is conical, and the outlet is connected with the quenching tank.
Drawings
The drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component that is illustrated in various figures may be represented by a like numeral. For purposes of clarity, not every component may be labeled in every drawing. Embodiments of various aspects of the present invention will now be described, by way of example, with reference to the accompanying drawings, in which:
FIG. 1 is a flow chart of the entire system;
FIG. 2 is a flow diagram of a low heating value waste liquid concentration 5 system;
fig. 3 is a schematic view of the positive pressure steam generator 2;
FIG. 4 is a schematic view of the negative pressure steam generator 4;
FIG. 5 is a schematic structural view of a two-stage steam-make-up evaporator 504;
the system comprises a submerged incinerator body 1, a positive pressure steam generator 2, a quenching tank 3, a negative pressure steam generator 4, a low-calorific-value waste liquid concentration system 5, an integrated absorption tower 6, a disturbance pump 7, a saturated liquid discharge pump 8, a heat exchanger 9, a bubbling bed dryer 10, a centrifuge 11, a cyclone 12, a dust remover 13, a bypass adjusting valve 14, a first water supply adjusting valve 15, a second water supply adjusting valve 16, a fresh water discharge pump 17, a fresh water control valve 18, a fresh water bypass valve 19, an absorption tower waste water discharge pump 20, a combustion section 101, a high-temperature section 102, a low-temperature section 103, a liquid salt discharge section 104 and a jet nozzle 301.
The system comprises an evaporator 501, a first steam-water separator 502, a second steam-water separator 503, a two-stage steam-supplementing type evaporator 504, a dead steam cooler 505, a condensed water tank 506, a first circulating pump 507, a second circulating pump 508, a transfer pump 509, a concentrated low-heating-value waste liquid conveying pump 510, a drain tank 511, a vacuum pump 512 and a water feeding pump 513.
The system comprises a steam outlet annular mother pipe 201, a feed water inlet annular mother pipe 202, a downcomer 203, a water wall tube bundle 204, a high temperature flue gas inlet 205, a high temperature flue gas outlet 206, a steam outlet 207 and a feed water inlet 208.
The negative pressure steam generator comprises a negative pressure steam generator body 401, an air inlet pipe box end plate 402, an air outlet pipe box end plate 403, an air inlet bell mouth 404, an air outlet bell mouth 405, a heat exchange pipe bundle 406, a water distribution pipe 407, a water sealing device 408, a discharge port 409, a negative pressure steam outlet 410, a condensed water inlet 408-1, a condensed water baffle 408-2, an inner sleeve 408-3 and a condensed water outlet 408-4.
The system comprises a waste liquid inlet 504-1, a waste liquid outlet 504-2, an inlet tube plate 504-3, an outlet tube plate 504-4, a negative pressure steam inlet 504-5, a secondary steam inlet 504-6, a drainage outlet 504-7, a condensed water outlet 504-8, a non-condensable gas outlet 504-9, a first heat exchange tube bundle 504-10, a steam separation plate 504-11, a spiral separation plate 504-12, an arch separation plate 504-13 and a second heat exchange tube bundle 504-14.
Detailed Description
The present invention will be further illustrated with reference to the accompanying drawings and specific embodiments, which are to be understood as merely illustrative of the invention and not as limiting the scope of the invention. It will be appreciated by those skilled in the art that changes may be made to the embodiments described below, or equivalents may be substituted for elements thereof, and any changes, equivalents, improvements, system omissions, and the like that fall within the spirit and scope of the present invention are intended to be embraced therein. It should be noted that the terms "front," "back," "left," "right," "upper" and "lower" used in the following description refer to directions in the drawings, and the terms "inner" and "outer" refer to directions toward and away from, respectively, the geometric center of a particular component.
The flow chart and the related structure schematic diagram provided by the invention are shown in fig. 1-5, and the specific implementation mode is as follows:
specifically, the saline waste liquid treatment system based on the submerged incineration technology comprises a submerged incinerator body 1, a positive pressure steam generator 2, a quenching tank 3, a negative pressure steam generator 4, a low calorific value waste liquid concentration system 5, an integrated absorption tower 6, a disturbance pump 7, a saturated liquid discharge pump 8, a heat exchanger 9, a bubbling bed dryer 10, a centrifuge 11, a cyclone 12, a dust remover 13, a bypass adjusting valve 14, a first water supply adjusting valve 15, a second water supply adjusting valve 16, a fresh water discharge pump 17, a fresh water control valve 18, a fresh water bypass valve 19 and an absorption tower waste water discharge pump 20.
Specifically, the dilute low calorific value salt-containing waste liquid firstly enters a low calorific value waste liquid concentration system 5, and concentrated low calorific value salt-containing waste liquid is formed after concentration. The waste liquid outlet of the low-heat value waste liquid concentration system 5 is connected with a high-temperature section 102 concentrated low-heat value salt-containing waste liquid interface of the liquid middle incinerator body 1, and the liquid middle incinerator body 1 comprises a combustion section 101, a high-temperature section 102, a low-temperature section 103 and a liquid salt discharge section 104.
Specifically, high-calorific-value salt-containing waste liquid and natural gas are sprayed into the furnace from the combustion section 101 to be combusted, the high-calorific-value salt-containing waste liquid and the natural gas are fully combusted in the combustion section 101, high temperature higher than 1100 ℃ is formed in the high-temperature section 102, an outlet of the high-temperature section 102 enters the low-temperature section 103, the low-temperature section 103 is provided with the positive-pressure steam generator 2, then the flue gas passes through the liquid salt discharge section 104, an outlet of the liquid salt discharge section 104 is connected with a flue gas inlet of the quenching tank 3, a flue gas outlet of the quenching tank 3 is connected with a flue gas inlet of the negative-pressure steam generator 4, a flue gas outlet of the negative-pressure steam generator 4 is connected with the integrated absorption tower 6, and finally the flue gas is discharged from the top of the integrated absorption tower 6.
Specifically, be equipped with the start-up moisturizing mouth on rapid cooling jar 3 for moisturizing when starting, 3 flue gas inlets of rapid cooling jar are provided with saturated liquid and insert the mouth, and 3 jar bodies of rapid cooling jar are provided with disturbance pump 7 and saturated liquid discharge pump 8 interfaces, 3 end fluidic nozzle 301 link to each other at the bottom of disturbance pump 7 export all the way and rapid cooling jar, and another way links to each other with bypass control valve 14, and 14 exports of bypass control valve link to each other with the main pipe of saturated liquid backward flow.
Specifically, the outlet of the saturated liquid discharge pump 8 is connected with the saturated liquid inlet of the heat exchanger 9, the outlet of the saturated liquid of the heat exchanger 9 is connected with the cyclone 12, the overflow outlet of the cyclone 12 is connected with the saturated liquid reflux main pipe, and finally the saturated liquid reflux main pipe is connected to the flue gas inlet saturated liquid reflux interface of the quenching tank 3.
Specifically, the underflow outlet of the cyclone 12 is connected with a centrifuge 11, the separation liquid of the centrifuge 11 is connected back to the saturated liquid reflux main pipe, the outlet of the centrifuge 11 is connected with the material inlet of the bubbling bed dryer 10, and the outlet of the bubbling bed dryer 10 is the finished product miscellaneous salt.
Specifically, an air side outlet of the heat exchanger 9 is connected with a bubbling bed dryer 10, an exhaust gas outlet of the bubbling bed is connected with a dust remover 13, bottom ash of the dust remover 13 is a finished product of miscellaneous salt, and the exhaust gas of the dust remover 13 is sent to a combustion section 101 of the novel liquid medium incinerator 1 to be used as air supplement.
Specifically, a fresh water outlet of the low-calorific-value waste liquid concentration system 5 is connected with a fresh water discharge pump 17, an outlet of the fresh water discharge pump 17 is connected with a fresh water return valve 18, an outlet of the fresh water control valve 18 is connected with a fresh water return main pipe, and the other path of the outlet of the fresh water discharge pump 17 is connected with a fresh water bypass valve 19.
Specifically, one path of a water supply outlet of the low-calorific-value waste liquid concentration system 5 is connected with a first water supply regulating valve 15, the other path of the water supply outlet is connected with a second water supply regulating valve 16, an outlet of the first water supply regulating valve 15 is connected with a water supply inlet of the positive pressure steam generator 2, and an outlet of the second water supply regulating valve 16 is connected with a water supply inlet of the negative pressure steam generator 4.
Specifically, the steam outlets of the positive pressure steam generator 2 and the negative pressure steam generator 4 are connected with the steam inlet of the low heating value waste liquid concentration system 5.
Specifically, the waste water discharge port of the integrated absorption tower 6 is connected with an absorption tower discharge pump 20, and the outlet of the absorption tower waste water discharge pump 20 is connected with a fresh water reflux main pipe.
Specifically, the low calorific value waste liquid concentration system 5 comprises an evaporator 501, a first steam-water separator 502, a second steam-water separator 503, a two-stage steam-supplementing type evaporator 504, a dead steam cooler 505, a condensed water tank 506, a first circulating pump 507, a second circulating pump 508, a transfer pump 509, a concentrated low calorific value waste liquid conveying pump 510, a drain tank 511, a vacuum pump 512 and a water feeding pump 513.
Specifically, the steam inlet of the evaporator 501 is connected with the steam outlet of the positive pressure steam generator 2, the drain outlet thereof is connected with the drain tank 511, the vapor-liquid outlet thereof is connected with the first vapor-water separator 502, and the waste liquid inlet thereof is connected with the first circulating pump 507.
Specifically, the secondary steam outlet of the first steam-water separator 502 is connected with the two-stage steam-supplementing evaporator 504, the separated liquid outlet thereof is connected with the inlet of the first circulating pump 507, the liquid supplementing port thereof is connected with the outlet of the transfer pump 509, and the inlet of the transfer pump 509 is connected with the outlet of the second circulating pump 508.
Specifically, two steam inlets of the two-stage steam supply evaporator 504 are respectively connected with a steam outlet of the negative pressure steam generator 4 and a secondary steam outlet of the first steam-water separator 502, two drain outlets thereof are respectively connected with the drain tank 511 and the condensed water tank 506, a steam-liquid outlet is connected with the second steam-water separator 503, and a waste liquid inlet is connected with the second circulating pump 508.
Specifically, the waste liquid inlet of the second steam-water separator 503 is connected to the incoming dilute low-calorific-value salt-containing waste liquid inlet, the secondary steam outlet thereof is connected to the exhaust steam cooler 505, the separation liquid outlet thereof is connected to the second circulation pump 508, and the steam-liquid inlet thereof is connected to the two-stage steam-supplementing evaporator 504. The negative pressure steam area of the two sections of steam compensating evaporators 504 and the condensed water tank 506 are provided with pumping ports, and the pumping ports are connected with the pumping port of the vacuum pump 512.
Specifically, the hydrophobic outlet of the dead steam cooler 505 is connected with a condensed water tank 506, and the outlet of the condensed water tank 506 is connected with the inlet of the fresh water discharge pump 17. The drain outlet of the drain tank 511 is connected with a feed pump 513. The outlet of the concentrated low-heat value waste liquid delivery pump 510 is connected with the high-temperature section 102 of the novel liquid medium incinerator 1.
Specifically, the positive pressure steam generator 2 is characterized in that the positive pressure steam generator 2 is installed in a low temperature section 103 of a novel liquid middle incinerator 1, the working temperature is 850-1100 ℃, the positive pressure steam generator is of a membrane wall cavity structure, and the positive pressure steam generator is characterized by mainly comprising: the system comprises a steam outlet annular mother pipe 201, a feed water inlet annular mother pipe 202, a downcomer 203, a water wall tube bundle 204, a high temperature flue gas inlet 205, a high temperature flue gas outlet 206, a steam outlet 207 and a feed water inlet 208.
Specifically, the high-temperature flue gas inlet 205 and the high-temperature flue gas outlet 206 are of a steel plate lining castable structure, and an inlet steel plate is welded to a steel plate of the high-temperature section 102 of the novel submerged combustion furnace 1.
Specifically, the water wall tube bundle 204 is a steel tube with diameter of 38-45mm, and the tube spacing is 55mm. The steam outlet annular main pipe 201 is a steel pipe with the diameter of 108-219mm, and the water supply inlet annular main pipe 202 is a steel pipe with the diameter of 76-108 mm.
Specifically, the negative pressure steam generator 4 is characterized in that the negative pressure steam generator 4 is installed at an outlet of a quenching tank, and mainly comprises: the negative pressure steam generator comprises a negative pressure steam generator body 401, an air inlet channel box end plate 402, an air outlet channel box end plate 403, an air inlet bell mouth 404, an air outlet bell mouth 405, a heat exchange tube bundle 406, a water distribution pipe 407, a water sealing device 408, a discharge port 409 and a negative pressure steam outlet 410.
Specifically, the negative pressure steam generator 4 is characterized in that the saturated flue gas flows through the heat exchange tube bundle 406, and the saturated water is located in the cabin of the negative pressure steam generator body 401. The heat exchange tube bundle 406 is installed in a slightly inclined manner, the recovered saturated flue gas condensate water flows into a flue gas outlet water seal device 408, and a water discharge port of the water seal device is connected with the quenching tank 3.
The water sealing device 408 is of a sleeve type structure and comprises a condensed water inlet 408-1, a condensed water baffle 408-2, an inner sleeve 408-3 and a condensed water outlet 408-4. The condensed water baffle 408-2 is of an annular structure, is arranged above the inner sleeve 408-3 and is welded with the inner sleeve 408-3, and a turned-out skirt edge of a straight cylinder section at the upper part of the condensed water baffle 408-2 is fixed between two connecting flanges of the condensed water inlet 408-1 to play a role in fixing and sealing. And the condensed water outlet 408-4 is arranged at the upper part of the shell of the water seal device.
Specifically, the two-section steam-supplementing evaporator 504 is characterized in that the internal structure is in the form of an inner sleeve and an outer sleeve, and mainly comprises a waste liquid inlet 504-1, a waste liquid outlet 504-2, an inlet tube plate 504-3, an outlet tube plate 504-4, a negative pressure steam inlet 504-5, a secondary steam inlet 504-6, a drainage outlet 504-7, a condensed water outlet 504-8, a noncondensable gas outlet 504-9, a first heat exchange tube bundle 504-10, a steam partition plate 504-11, a spiral partition plate 504-12, an arched partition plate 504-13 and a second heat exchange tube bundle 504-14.
Specifically, the two-stage steam compensating evaporator 504 adopts a steam separation plate 504-11 to separate two quality steam, secondary steam flows through an inner second heat exchange tube bundle 504-14, and negative pressure steam flows through an outer first heat exchange tube bundle 504-10. The arched partition plates 504-13 are installed on the inner sides of the steam partition plates 504-11 and used for disturbing secondary steam, and the spiral partition plates 504-12 are installed on the outer sides of the steam partition plates 504-11 and used for disturbing negative-pressure steam. The waste liquid inlet 504-1 and the waste liquid outlet 504-2 are connected with the shell, and the first heat exchange tube bundle 504-10 and the second heat exchange tube bundle 504-14 are in expanded joint with the inlet tube plate 504-3 and the outlet tube plate 504-4. The drainage of the inner secondary steam is discharged from a condensed water outlet 504-8, the drainage of the outer negative pressure steam is discharged from a drainage outlet 504-7, and the non-condensable gas of the outer negative pressure steam is pumped out from a non-condensable gas outlet 504-9.
Specifically, the system can be used for simultaneously treating the low-calorific-value salt-containing waste liquid and the high-calorific-value salt-containing waste liquid, the calorific value of the low-calorific-value salt-containing waste liquid can be-600-200 kcal/kg, the calorific value of the high-calorific-value salt-containing waste liquid can be 4000-10000 kcal/kg, and the salt content of the two waste liquids is about 5-20%. The high-low salt-containing waste liquid is treated by the system to obtain harmless solid crystal salt, the system can fully realize zero discharge of system waste water when the concentration multiplying power of the low-calorific value salt-containing waste liquid is 2.5-3, and when the concentration multiplying power is higher than 3, the low-calorific value waste liquid system can generate certain fresh water which can be used for other process water in a plant area and can also enter a sewage treatment plant for comprehensive treatment.
Specifically, the dilute low heat value of incoming flow contains salt waste liquid and at first gets into low heat value waste liquid concentration system 5, carries out the concentrated processing, and the waste heat that burns burning furnace system production in the heat that low heat value waste liquid concentration system 5 adopted is novel liquid can reduce by a wide margin the natural gas consumption volume that burns burning furnace in novel liquid after retrieving its a large amount of used heat, saves system cost to improve system's productivity. The use method of the low-calorific-value waste liquid concentration system 5 comprises the following steps that incoming dilute low-calorific-value salt-containing waste liquid enters the concentration system from a waste liquid inlet of the second steam-water separator 503, fresh dilute waste liquid is mixed with liquid separated from the second steam-water separator 503 and then flows downwards from a separated liquid outlet of the second steam-water separator 503 to enter the second circulating pump 508, the mixture is pushed to the two-section steam-supplementing type evaporator 504 through the second circulating pump 508 to be evaporated, a generated steam-water mixture enters the second steam-water separator 503 to be separated, secondary steam is led out from a secondary steam outlet of the second steam-water separator 503 to be sent to the dead steam cooler 505 to be condensed, the condensed water enters the condensed water tank 506 to be stored, and the quality of the condensed water is clean and can be sent to the main system flash tank 3 to be used as process water supplement or used for other purposes. The low-calorific-value salt-containing waste liquid preliminarily concentrated at the outlet of the second circulating pump 508 is periodically sent to the waste liquid inlet of the first steam-water separator 502 through the transfer pump 509, the newly added waste liquid is mixed with the liquid separated from the first steam-water separator 502 and then flows downwards from the separating liquid outlet of the first steam-water separator 502 to enter the first circulating pump 507, the mixture is pushed to the evaporator 501 through the first circulating pump 507 to be evaporated, the generated steam-water mixture enters the first steam-water separator 502 to be separated, and secondary steam is led out from the secondary steam outlet of the first steam-water separator 502 and sent to the two-section steam-supplementing type evaporator 504 to serve as a heating heat source. And the concentrated low-heat-value salt-containing waste liquid at the outlet of the first circulating pump 507 is sent to the novel liquid medium incinerator 1 for treatment by a concentrated low-heat-value waste liquid conveying pump 510 at regular intervals. The heat source of the evaporator 501 is high-parameter steam from the evaporation steam generator 2, and the heat sources of the two-stage steam-supplementing evaporator 504 are low-parameter steam generated by the negative pressure steam generator 4 and secondary steam separated by the first steam-water separator 503. Because the steam entering the two sections of steam-supplementing evaporators 504 has different qualities, the designed steam of the two sections of steam-supplementing evaporators 504 is arranged in different jackets, the negative pressure steam with higher quality enters the annular heating surface at the outer side of the two sections of steam-supplementing evaporators 504, the secondary steam with lower quality enters the heating surface at the inner side, and the internal heat exchange surface can be integrally extracted, so that the cleaning and the maintenance are convenient. The condensed hydrophobic water on the outer annular heating surface of the two sections of steam-supplementing evaporators 504 and the condensed hydrophobic water on the heat source of the evaporator 501 enter a hydrophobic tank 511 together, and are finally respectively sent to the positive-pressure steam generator 2 and the negative-pressure steam generator 4 through a water feeding pump 513 to be used as the water supplementing of the heat exchange system. In order to maintain the normal and continuous operation of the low-heating-value waste liquid concentration system 5, the non-condensable gas generated by the system needs to be continuously discharged out of the system, and in addition, in order to maintain the negative pressure steam generator 4 to generate saturated steam in a negative pressure state, a vacuum pump 512 is arranged in the system and is used for continuously extracting the non-condensable gas in the annular outer space of the two-section steam-supplementing type evaporator 504 and the non-condensable gas in the condensed water tank 506.
Specifically, the core component of the system is a novel liquid medium incinerator 1, and the developed novel liquid medium incinerator is a four-section incinerator, and comprises a combustion section 101, a high-temperature section 102, a low-temperature section 103 and a liquid salt discharge section 104. The natural gas and the high-calorific-value salt-containing waste liquid are sprayed out, evaporated and combusted from the combustion section 101 through the multifunctional combustor, and the high temperature of over 1100 ℃ is formed in the high-temperature section 102. The concentrated low-calorific-value salt-containing waste liquid after concentration is sprayed into a hearth from an expanded port of the high-temperature section 102 through a special spray gun, and toxic and harmful substances in the waste liquid are thoroughly incinerated and removed. The high-temperature section 102 is of an empty tower structure, the design volume meets the requirement that the flue gas stays for more than 2s, the outlet of the high-temperature section 102 is the low-temperature section 103, the low-temperature section is provided with the positive-pressure steam generator 2, and the positive-pressure steam generator 2 recovers part of waste heat in the flue gas, so that the temperature of the flue gas is reduced, and finally, the outlet temperature of the low-temperature section 103 is ensured to be higher than 850 ℃ and higher than the melting temperature of salt. The low temperature section 103 is provided with an SNCR urea spray gun, and meets the requirement of an optimal temperature window for SNCR denitration. Low temperature section 103 exit linkage liquid row salt section 104, liquid row salt section 104 is the adiabatic wall, the fused salt flows to the rapid cooling jar along the inner wall face, 850 ℃ flue gas also discharges to the rapid cooling jar 3 in through low temperature section 103, the contact of the saturated salt solution in high temperature flue gas and the rapid cooling jar 3 (during the initial start, directly carry out the moisturizing from the start-up moisturizing mouth), by cooling to 90 ℃ rapidly, a large amount of moisture are taken out by the evaporation in the rapid cooling jar 3, saturated salt solution begins the crystallization in the rapid cooling jar 3, produce solid crystalline salt gradually.
Specifically, the flue gas flows out of the quenching tank and then enters the negative pressure steam generator 4 to deeply recover waste heat and generate negative pressure saturated steam. Because the flue gas entering the negative pressure steam generator 4 is 90 ℃ wet saturated flue gas, the volume fraction of the steam in the flue gas is about 70 percent, and the water content is huge. When the flue gas is cooled in the negative pressure steam generator 4, a large amount of moisture in the flue gas is condensed and separated out, condensed water is discharged from a water seal device 408 of the negative pressure steam generator 4 and then sent into the quenching tank 3 to be used as water supplement, the temperature of the cooled flue gas is about 75 ℃, and then the flue gas enters the integrated absorption tower 6 to be deacidified and then is discharged from the top of the tower.
Specifically, the concentrated liquid in the quenching tank 3 is a saturated salt solution and contains more solid crystalline salt particles, a disturbance pump 7 is connected to a liquid outlet of the quenching tank 3, the disturbance pump 7 pumps out the liquid and then returns to a jet nozzle 301 at the bottom of the quenching tank 3, after the saturated salt solution is sprayed out through the jet nozzle 301 at a high speed, severe disturbance is formed at the bottom of the quenching tank 3, so that a solid-liquid mixture in the quenching tank 3 can be mixed more sufficiently, and the blockage of crystalline salt discharged from the inner wall, the tank bottom and a feed inlet of the quenching tank 3 can be reduced. The other path of the outlet of the disturbance pump 7 is connected to a bypass adjusting valve 14, the outlet of the bypass adjusting valve 14 is connected to a saturated liquid return main pipe, and the bypass adjusting valve is used for constantly controlling the flow of the bypassed saturated liquid so as to ensure the stable flow of the control jet nozzle 301. The outlet of the quenching tank 3 is also provided with a saturated liquid discharge pump 8, the saturated liquid discharge pump 8 periodically discharges the saturated liquid in the quenching tank 8 to a crystallized salt recovery system, the saturated liquid is discharged by the saturated liquid discharge pump 8 and then enters a heat exchanger 9 to transfer part of heat to fluidized air of a bubbling bed dryer 10, the temperature of the cooled saturated liquid is about 50 ℃, and then the cooled saturated liquid enters a cyclone 12 for cyclone solid-liquid separation, the crystallized salt enters a centrifuge 11 for deep dehydration, and the cyclone 12 overflow and the centrifuge 11 separation liquid enter a saturated liquid reflux mother pipe and then return to the inlet of the quenching tank 3. The crystallized salt at the outlet of the centrifuge 11 enters a bubbling bed dryer 10 and is directly contacted and dried with the dry hot air at the outlet of the heat exchanger 9, the waste gas at the outlet of the bubbling bed dryer 10 enters a dust remover 13 to recover fine crystallized salt particles escaping from the bubbling bed dryer 10, and the wet tail gas is sent to the combustion section 103 of the novel liquid middle incinerator 1 to be burnt as air supplement.
Specifically, the steam-water sides of the positive pressure steam generator 2, the negative pressure steam generator 4 and the low-calorific-value waste liquid concentration system 5 adopt a closed circulation system, and the use method comprises the following steps: the feedwater that the concentrated system 5 of low heat value waste liquid sent the water pump 513 sends into first feedwater governing valve 15 and second feedwater governing valve 16 respectively, two governing valves are used for controlling the feedwater flow that gets into positive pressure steam generator 2 and negative pressure steam generator 4, in order to maintain the female pipe 201 of annular steam and negative pressure steam generator body 401 liquid level stability, the concentrated system 5 of low heat value waste liquid is then sent back to high parameter steam and low parameter steam of production, be used for the concentrated salt waste liquid of rare low heat value, the drainage is beaten back two steam generator again and is realized cyclic utilization.
Specifically, in order to reduce the consumption of process water and the discharge amount of system wastewater to the maximum extent, the quenching tank 3 system adopts the following three water sources as water supplement, 1 is condensed water generated by the negative pressure steam generator 4, 2 is integrated with the absorption tower 6 to discharge high-salt-content wastewater, and 3 is fresh water generated by the low-calorific-value waste liquid concentration system 5. When the low-calorific-value waste liquid concentration system 5 operates at a high concentration rate, the fresh water generation amount of the system is very large, and the quenching tank 3 cannot be completely consumed. Therefore, a fresh water bypass valve 19 is provided at the outlet of the fresh water discharge pump 17 to control the liquid level in the quench tank 3 to be stable.
Example one
The analysis operation parameters are combined with the analysis operation parameters of a 4.4-million-ton salt-containing waste liquid treatment production line every year, and the specific operation parameters are as follows:
high-calorific-value salt-containing waste liquid treatment capacity: 8t/d;
high calorific value salt-containing waste liquid calorific value: 3200kcal/kg;
treating amount of concentrated low-calorific-value salt-containing waste liquid: 33.3t/d;
concentrated low calorific value salt-containing waste liquid calorific value: -598kcal/kg;
consumption of natural gas: 174.5Nm3/h;
natural gas calorific value: 8500kcal/Nm3;
outlet temperature of high-temperature section of incinerator in liquid: 1155 deg.C;
flue gas amount at the outlet of the high-temperature section of the incinerator in liquid: 5109Nm3/h;
flue gas components at the outlet of the high-temperature section of the submerged incinerator:
CO2：301Nm3/h；
H2O：2332Nm3/h；
N2：2409Nm3/h；
O2：67Nm3/h；
outlet temperature of low-temperature section of incinerator in liquid: 850 ℃;
steam yield of a positive pressure steam generator of the liquid medium incinerator: 0.9t/h;
temperature of flue gas at outlet of quenching tank: 89 ℃;
flue gas composition at the outlet of the quenching tank:
CO2：301Nm3/h；
H2O：5758Nm3/h；
N2：2409Nm3/h；
O2：67Nm3/h；
temperature of flue gas at outlet of negative pressure steam generator: 75 ℃;
steam amount of flue gas at outlet of negative pressure steam generator: 1745Nm3/h;
the amount of condensed water of the negative pressure steam generator is as follows: 3.2t/h;
steam yield of the negative pressure steam generator: 3.25t/h;
total steam production: 4.15t/h;
treating capacity of dilute low-calorific-value salt-containing waste liquid: 138.7t/d;
concentration ratio of the low-calorific-value waste liquid concentration system: 4.16;
the salt content of the low-calorific-value salt-containing waste liquid is as follows: 4 percent;
high-calorific-value salt-containing waste liquid contains salt: 6 percent;
amount of crystalline salt produced: 8.7t/d;
the system discharges fresh water: 100t/d.
The technical means disclosed in the scheme of the invention are not limited to the technical means disclosed in the above embodiments, but also include the technical means formed by any combination of the above technical features.

Claims (7)

1. A saline waste liquid treatment system based on a submerged incineration technology is characterized by comprising a submerged incinerator body (1), a positive pressure steam generator (2), a quenching tank (3), a low-calorific-value waste liquid concentration system (5), an integrated absorption tower (6), a disturbance pump (7), a saturated liquid discharge pump (8), a crystallized salt recovery system, a bypass regulating valve (14), a first water supply regulating valve (15), a fresh water discharge pump (17), a fresh water control valve (18) and a fresh water bypass valve (19);
the liquid incinerator body (1) is sequentially provided with a combustion section (101), a high-temperature section (102), a low-temperature section (103) and a liquid salt discharge section (104) from top to bottom;
wherein a multifunctional burner is arranged in the combustion section (101) and is used for spraying high-heat-value salt-containing waste liquid and auxiliary fuel into the combustion section (101) for full combustion, so that the temperature in the high-temperature section (102) is more than 1100 ℃ after the flue gas enters the high-temperature section (102),
a special spray gun is arranged in the high-temperature section (102) and is used for spraying the concentrated low-calorific-value salt-containing waste liquid into the high-temperature section (102), the volume of the high-temperature section (102) enables the flue gas to stay in the high-temperature section for more than 2s,
the low-temperature section (103) is internally provided with a positive pressure steam generator (2), the positive pressure steam generator (2) is a heat exchanger, one side of the heat exchanger is introduced with feed water, the other side of the heat exchanger is introduced with flue gas for absorbing partial heat of the flue gas to heat the feed water to generate positive pressure steam, the temperature of the flue gas is still kept above 850 ℃ after the flue gas is absorbed by the positive pressure steam generator (2), the low-temperature section (103) is also provided with an SNCR urea spray gun for denitration,
the liquid salt discharging section (104) is a cone with a hole at the bottom and gradually necking along the smoke direction;
the quenching tank (3) is provided with a flue gas inlet, a flue gas outlet, a starting water replenishing port, a water inlet and a liquid outlet, the bottom of the quenching tank (3) is provided with a jet nozzle (301),
a flue gas inlet of the quenching tank (3) is connected with a bottom outlet of the liquid salt discharging section (104), a flue gas outlet of the quenching tank (3) is connected with the integrated absorption tower (6),
the integrated absorption tower (6) is used for deacidifying the entering flue gas and discharging the deacidified flue gas, and periodically discharging the high-salt-content waste water generated by the deacidification and discharge,
the high-salt-content wastewater discharged by the integrated absorption tower (6) is connected to a water inlet of the quenching tank (3),
a liquid outlet pipeline of the quenching tank (3) is connected with a saturated liquid discharge pump (8), an outlet of the saturated liquid discharge pump (8) is connected to a crystallization salt recovery system, the crystallization salt recovery system is provided with a saturated liquid reflux main pipe, a cyclone and a centrifuge, the saturated liquid reflux main pipe is connected to the quenching tank (3), the crystallization salt recovery system is used for separating crystallization salt and sending the overflow of the cyclone and the separation liquid of the centrifuge back to the quenching tank (3),
the quenching tank (3) is also provided with an outlet connected with a disturbance pump (7), the outlet of the disturbance pump (7) is provided with two paths, one path is connected to a jet nozzle (301) at the bottom of the quenching tank (3), and the other path is connected to the quenching tank (3) through a bypass regulating valve (14),
the low heat value waste liquid concentration system (5) is used for concentrating the dilute low heat value waste liquid into concentrated low heat value waste liquid by using steam as a heat source,
the low heat value waste liquid concentration system (5) is provided with a waste liquid inlet which is used as an inlet of the dilute low heat value waste liquid,
the low-heat value waste liquid concentration system (5) is provided with a waste liquid outlet, is connected to a special spray gun in the high-temperature section (102) and is used for spraying concentrated low-heat value waste liquid into the high-temperature section (102),
the low-heat-value waste liquid concentration system (5) is provided with a fresh water outlet for discharging fresh water separated during concentration of the dilute low-heat-value waste liquid, the fresh water outlet is connected to a fresh water discharge pump (17), the outlet of the fresh water discharge pump (17) is divided into two paths, one path is connected to the quenching tank (3) through a fresh water control valve (18), the other path is connected to a waste water treatment system through a fresh water bypass valve (19),
the low-heat value waste liquid concentration system (5) is provided with a positive pressure steam inlet, positive pressure steam discharged by the positive pressure steam generator (2) is connected to the positive pressure steam inlet,
the low-calorific-value waste liquid concentration system (5) is provided with a steam drain port, is connected to the positive pressure steam generator (2) through a first water supply and adjustment valve (15) and is used for taking drain water discharged from the steam drain port as water supply of the positive pressure steam generator (2) to absorb heat of flue gas,
the saline waste liquid treatment system based on the in-liquid incineration technology also comprises a second water supply regulating valve (16) and a negative pressure steam generator (4),
the low-calorific-value waste liquid concentrating system (5) comprises an evaporator (501), a first steam-water separator (502), a second steam-water separator (503), two sections of steam-supplementing evaporators (504), a dead steam cooler (505), a condensed water tank (506), a first circulating pump (507), a second circulating pump (508), a transfer pump (509), a concentrated low-calorific-value waste liquid conveying pump (510), a drain tank (511), a vacuum pump (512) and a water feeding pump (513);
the steam inlet of the evaporator (501) is connected with the steam outlet of the positive pressure steam generator (2),
the hydrophobic outlet of the evaporator (501) is connected with a hydrophobic tank (511),
the waste liquid inlet of the evaporator (501) is connected with a first circulating pump (507),
the waste liquid inlet of the evaporator (501) is also connected with a concentrated low-heat value waste liquid conveying pump (510),
the vapor-liquid outlet of the evaporator (501) is connected with the first vapor-water separator (502),
the secondary steam outlet of the first steam-water separator (502) is connected with the two sections of steam-supplementing evaporators (504),
the separated liquid outlet of the first steam-water separator (502) is connected with the inlet of a first circulating pump (507),
the liquid supplementing port of the first steam-water separator (502) is connected with the outlet of the transfer pump (509),
two steam inlets of the two-section steam-supplementing type evaporator (504) are respectively connected with a steam outlet of the negative pressure steam generator (4) and a secondary steam outlet of the first steam-water separator (502), two drain outlets thereof are respectively connected with a drain tank (511) and a condensed water tank (506),
the vapor-liquid outlet of the two-section vapor-supplementing evaporator (504) is connected with the second vapor-water separator (503),
the waste liquid inlet of the two-section steam-supplementing evaporator (504) is connected with the outlet of a second circulating pump (508),
the waste liquid inlet of the two-section steam-supplementing evaporator (504) is also connected with the inlet of a transfer pump (509),
the waste liquid inlet of the second steam-water separator (503) is used for introducing dilute low-heat value waste liquid,
the secondary steam outlet of the second steam-water separator (503) is connected with a dead steam cooler (505),
the separated liquid outlet of the second steam-water separator (503) is connected with a second circulating pump (508),
the vapor-liquid inlet of the second vapor-water separator (503) is connected with the two sections of vapor-supplementing evaporators (504),
the negative pressure steam area of the two sections of steam supplementing type evaporators (504) and the condensed water tank (506) are provided with pumping ports which are connected with the pumping port of the vacuum pump (512),
the hydrophobic outlet of the dead steam cooler (505) is connected with a condensed water tank (506),
the outlet of the condensed water tank (506) is connected with the inlet of the fresh water discharge pump (17),
the drain tank (511) is provided with a water replenishing port,
the drainage outlet of the drainage tank (511) is connected with a water feeding pump (513),
the outlet of the water feeding pump (513) is connected with a first water feeding regulating valve (15) and a second water feeding regulating valve (16) to respectively feed water to the positive pressure steam generator (2) and the negative pressure steam generator (4),
the outlet of the concentrated low-heat value waste liquid delivery pump (510) is connected with the high-temperature section (102) of the incinerator body (1) in liquid,
wherein the negative pressure steam generator (4) is used for further absorbing the heat in the flue gas and generating negative pressure steam,
before the flue gas outlet of the quenching tank (3) is connected to the integrated absorption tower (6), the flue gas passes through the negative pressure steam generator (4) for further absorbing heat in the flue gas, the temperature of the flue gas entering the negative pressure steam generator (4) from the flue gas outlet of the quenching tank (3) is 80-90 ℃,
the negative pressure steam generator (4) is also provided with a water seal device (408) which is used for collecting condensed water in the flue gas and sealing the flue,
the outlet of the water seal device (408) is connected to the water inlet of the quenching tank (3).
2. The saline waste liquid treatment system based on submerged incineration technology as claimed in claim 1, wherein the internal structure of the two-stage steam-supplementing evaporator (504) is in the form of an inner sleeve and an outer sleeve, and comprises a waste liquid inlet (504-1), a waste liquid outlet (504-2), an inlet tube plate (504-3), an outlet tube plate (504-4), a negative pressure steam inlet (504-5), a secondary steam inlet (504-6), a hydrophobic outlet (504-7), a condensed water outlet (504-8), a non-condensable gas outlet (504-9), a first heat exchange tube bundle (504-10), a steam separation plate (504-11), a spiral partition plate (504-12), an arched partition plate (504-13), a second heat exchange tube bundle (504-14) and a shell,
the two-section steam-supplementing type evaporator (504) adopts a steam separation plate (504-11) to separate two types of quality steam, the second heat exchange tube bundle (504-14) at the inner side is used for feeding secondary steam, the first heat exchange tube bundle (504-10) at the outer side is used for feeding negative pressure steam,
the arched clapboard (504-13) is arranged at the inner side of the steam separation plate (504-11) and is used for disturbing flow of secondary steam,
the spiral clapboard (504-12) is arranged at the outer side of the steam clapboard (504-11) and is used for disturbing negative pressure steam,
the waste liquid inlet (504-1) and the waste liquid outlet (504-2) are connected with the shell,
the first heat exchange tube bundle (504-10) and the second heat exchange tube bundle (504-14) are expanded with an inlet tube plate (504-3) and an outlet tube plate (504-4),
the drainage of the inner secondary steam is discharged from a condensed water outlet (504-8), the drainage of the outer negative pressure steam is discharged from a drainage outlet (504-7), and the non-condensable gas of the outer negative pressure steam is pumped out from a non-condensable gas outlet (504-9).
3. A saline waste treatment system based on submerged incineration technology according to claim 2, characterized in that the crystallized salt recovery system comprises a heat exchanger (9), a bubbling bed dryer (10), a centrifuge (11), a cyclone (12), a dust remover (13),
the outlet of the saturated liquid discharge pump (8) is connected with the saturated liquid inlet of the heat exchanger (9),
a saturated liquid outlet of the heat exchanger (9) is connected with a cyclone (12), an overflow outlet of the cyclone (12) is connected with a saturated liquid reflux main pipe,
the underflow outlet of the cyclone (12) is connected with a centrifugal machine (11),
the outlet of the separation liquid of the centrifuge (11) is connected back to the saturated liquid reflux main pipe,
the outlet of the centrifuge (11) is connected with the material inlet of the bubbling bed dryer (10),
the outlet of the bubbling bed dryer (10) is used for outputting the finished product miscellaneous salt,
the air side outlet of the heat exchanger (9) is connected with a bubbling bed dryer (10),
the exhaust gas outlet of the bubbling bed is connected with a dust remover (13),
the exhaust gas outlet of the dust remover (13) is connected with the combustion section (101) of the incinerator body (1) in the liquid as air supplement,
the bottom ash outlet of the dust remover (13) is used for outputting finished product miscellaneous salt.
4. A method for treating salt-containing waste liquid based on a submerged incineration technology, which is characterized in that the system for treating salt-containing waste liquid based on the submerged incineration technology of claim 1 is adopted, and comprises the following steps:
step 1: the high-calorific-value salt-containing waste liquid and natural gas are sprayed into the furnace from the combustion section (101) to be combusted, and high temperature of over 1100 ℃ is formed in the high-temperature section (102);
step 2: the flue gas flows through a high-temperature section (102), a low-temperature section (103) and a liquid salt discharge section (104) in sequence and then enters a quenching tank (3), water is added into the quenching tank (3) from a starting water replenishing port during initial starting, and the flue gas is rapidly cooled after contacting with liquid in the quenching tank (3) and then discharged into an integrated absorption tower (6) for deacidification;
and 3, step 3: the integrated absorption tower (6) discharges the high-salt-content wastewater generated by deacidification into the quenching tank (3);
and 4, step 4: the feed water provided by the low-heat-value waste liquid concentration system (5) absorbs the heat of the flue gas through the positive pressure steam generator (2) to heat the feed water into positive pressure steam, and simultaneously the outlet temperature of the low-temperature section (103) is kept higher than 850 ℃,
dilute low-calorific-value salt-containing waste liquid is added into a low-calorific-value waste liquid concentration system (5), the dilute low-calorific-value salt-containing waste liquid is concentrated into concentrated low-calorific-value salt-containing waste liquid by using the positive pressure steam,
fresh water separated from the dilute low-calorific-value salt-containing waste liquid is discharged into a quenching tank (3) or a wastewater treatment system, the drainage of positive pressure steam is recycled as feed water, and the concentrated low-calorific-value salt-containing waste liquid is sprayed into a hearth from a high-temperature section (102) through a special spray gun;
and 5: sending the liquid containing the crystallized salt in the quenching tank (3) into a crystallized salt recovery system by using a saturated liquid discharge pump (8), discharging the crystallized salt, and sending the separated liquid back to the quenching tank (3);
step 6: the liquid in the quenching tank (3) is pumped out by using a disturbance pump (7) and then is sprayed from a jet nozzle (301) at the bottom of the quenching tank (3).
5. The method for treating waste liquid containing salt by using submerged incineration technology according to claim 4, characterized in that the step 6 further comprises adjusting the flow rate of the jet nozzle (301) at the bottom of the quench tank (3) by using a bypass adjusting valve (14).
6. The concentration method of the saline waste liquid treatment system based on the submerged incineration technology, which is characterized by comprising the following steps:
step 1: when the system is started for the first time, the dilute low-calorific-value salt-containing waste liquid enters from a waste liquid inlet of a second steam-water separator (503),
and passes through a second circulating pump (508), a transfer pump (509) and a first circulating pump (507),
adding a certain amount of dilute low-heat-value waste liquid into an evaporator (501) and a two-stage steam-supplementing evaporator (504);
step 2: starting a vacuum pump (512) to establish and maintain a certain vacuum degree in a negative pressure steam area of the two-section steam supplementing type evaporator (504) and a condensed water tank (506);
and step 3: replenishing water in the steam trap (511), maintaining a certain water level, and sending the water to the positive pressure steam generator (2) through a water feeding pump (513);
and 4, step 4: introducing positive pressure steam from a positive pressure steam generator (2) into an evaporator (501),
the drainage of the positive pressure steam is discharged into a drainage tank (511),
the low heat value waste liquid at the bottom of the evaporator (501) is sent to the high temperature section (102) by a concentrated low heat value waste liquid delivery pump (510) at regular intervals,
the vapor and the liquid of the evaporator (501) are sent to a first vapor-water separator (502),
the separated liquid from the first steam-water separator (502) is sent back to the evaporator (501) through a first circulating pump (507),
the secondary steam separated by the first steam-water separator (502) is sent to a two-section steam-supplementing type evaporator (504);
and 5: the secondary steam of the first steam-water separator (502) and the steam of the negative pressure steam generator (4) are respectively led into two sections of steam supplementing evaporators (504),
the drained water of the secondary steam of the first steam-water separator (502) is discharged into a condensed water tank (506),
the drainage of the steam of the negative pressure steam generator (4) is discharged into a drainage tank (511),
the low heat value liquid at the bottom of the two sections of steam-supplementing evaporators (504) is sent into the first steam-water separator (502) periodically through a transfer pump (509),
the vapor and liquid of the two sections of vapor-supplementing evaporators (504) are sent to a second vapor-water separator (503),
the separated liquid from the second steam-water separator (503) is sent back to the two-stage steam-supplementing evaporator (504) through a second circulating pump (508),
the waste liquid inlet of the second steam-water separator (503) is supplemented with the dilute low heat value salt-containing waste liquid,
the secondary steam of the second steam-water separator (503) is discharged into a condensate water tank (506) after being cooled by a dead steam cooler (505),
the fresh water in the condensed water tank (506) is periodically discharged into the quenching tank (3) or a wastewater treatment system.
7. A method for recovering crystallized salt of a saline waste liquid treatment system based on a submerged incineration technology, which is characterized by comprising the following steps of:
step 1: saturated liquid in the quenching tank (3) is sent into a heat exchanger (9) through a saturated liquid discharge pump (8) at regular intervals, the heat exchanger (9) cools the saturated liquid through air, and the obtained hot air enters a bubbling bed dryer (10);
step 2: the cooled saturated liquid enters a cyclone (12) for solid-liquid separation, the separated liquid returns to a quenching tank (3), and the separated crystal salt enters a centrifuge (11) for deep dehydration;
and step 3: the separated liquid of the centrifuge (11) returns to the quenching tank (3), and the crystallized salt separated by the centrifuge (11) enters a bubbling bed dryer (10);
and 4, step 4: hot air in the bubbling bed dryer (10) directly contacts with crystallized salt from a centrifuge (11), the dried crystallized salt is finished miscellaneous salt, and waste gas at the outlet of the bubbling bed dryer (10) enters a dust remover (13);
and 5: the fine crystal salt particles collected by the dust remover (13) are finished product miscellaneous salt, and the wet tail gas of the dust remover (13) is sent to the combustion section (101) of the incinerator body (1) in the liquid to be burnt as air supplement.
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