CN219526435U - Zero-emission high-concentration brine resource utilization treatment system for coal chemical industry - Google Patents

Abstract

The utility model discloses a zero-emission high-concentration brine recycling treatment system in coal chemical industry, wherein a decarburization tower of a decarburization working section of the system is used for removing free carbon dioxide; the advanced catalytic oxidation tower of the advanced catalytic oxidation section is used for removing COD; the silicon removal high-efficiency coagulating sedimentation tank of the silicon removal working section is used for removing silicon; the ultrafiltration chelation bed working section comprises ultrafiltration and chelation beds, wherein the ultrafiltration is used for removing suspended matters, and the chelation beds are used for selectively adsorbing divalent metal ions; the nanofiltration device of the nanofiltration salt separation section is used for separating high-concentration salt water into two parts of sodium chloride-containing brine and sodium sulfate-containing brine; the evaporating and crystallizing section carries out evaporating and crystallizing on the sodium sulfate-containing brine, the drying and packaging section further removes water from the crystallized sodium sulfate slurry and realizes purification and recycling of sodium sulfate, and the dust removing section treats dust generated by the drying and packaging section. The utility model solves the problem that the high-concentration brine recycling treatment system in the prior art has low sodium sulfate recycling utilization rate.

Description

Zero-emission high-concentration brine resource utilization treatment system for coal chemical industry

Technical Field

The utility model belongs to the technical field of wastewater treatment, and particularly relates to a zero-emission high-concentration brine recycling treatment system for coal chemical industry.

Background

Along with the change of national environmental protection policy, the national requirements on chemical wastewater treatment standards are higher and higher, the zero discharge of chemical wastewater in the present stage not only requires the complete recovery of wastewater, but also puts forward higher requirements on the treatment of waste salt, namely, the requirements on resource utilization. The ratio of sodium chloride to sodium sulfate in the high-concentration brine of the current zero-emission system is subverted, and the utilization rate of the current treatment system for sodium sulfate is not high. Meanwhile, the existing treatment system also has the problems of high labor intensity of carbon replacement and influence of components such as COD, metal ions, alkalinity, silicon and the like on evaporation and salt separation.

Disclosure of Invention

The embodiment of the utility model solves the problem that the high-concentration brine recycling treatment system in the prior art has low sodium sulfate recycling utilization rate by providing the high-concentration brine recycling treatment system with zero emission in the coal chemical industry.

In order to achieve the aim, the embodiment of the utility model provides a zero-emission high-concentration brine recycling treatment system for coal chemical industry, which comprises a decarburization working section, a high-grade catalytic oxidation working section, a desilication working section, an ultrafiltration chelating bed working section, a nanofiltration salt separation working section, an evaporation crystallization working section, a drying packaging working section and a dust removal working section which are sequentially arranged according to a treatment flow;

the decarbonization section comprises a decarbonization tower for removing free carbon dioxide in the high-concentration brine;

the advanced catalytic oxidation working section comprises an advanced catalytic oxidation tower, wherein the advanced catalytic oxidation tower is used for removing COD in high-concentration brine;

the silicon removal working section comprises a silicon removal high-efficiency coagulating sedimentation tank, and the silicon removal high-efficiency coagulating sedimentation tank is used for removing silicon in high-concentration brine;

the ultrafiltration chelation bed working section comprises ultrafiltration and chelation beds, wherein the ultrafiltration is used for removing suspended matters in the high-concentration brine, and the chelation beds are used for selectively adsorbing divalent metal ions in the high-concentration brine;

the nanofiltration and salt separation working section comprises a nanofiltration device, wherein the nanofiltration device is used for dividing high-concentration salt water into two parts of sodium chloride-containing brine and sodium sulfate-containing brine;

the evaporation and crystallization working section performs evaporation and crystallization on sodium sulfate-containing brine, the drying and packaging working section further removes water from the crystallized sodium sulfate slurry and realizes purification and recycling of sodium sulfate, and the dust removal working section treats dust generated by the drying and packaging working section.

In one possible implementation, the decarbonization section further includes a decarbonization tower blower, an intermediate basin, and an intermediate basin lift pump;

the liquid outlet of the high-concentration brine conveying pipe is connected with the liquid inlet of the decarburization tower, and the air outlet of the decarburization tower fan is connected with the air inlet of the decarburization tower;

the liquid outlet of the decarburization tower is connected with the liquid inlet of the middle water tank, the liquid outlet of the middle water tank is connected with the liquid inlet of the middle water tank lifting pump, and the liquid outlet of the middle water tank lifting pump is connected with the liquid inlet of the advanced catalytic oxidation tower.

In one possible implementation, the advanced catalytic oxidation section further includes an ozone catalytic water producing tank, an ozone catalytic water producing lift pump, an activated carbon adsorption tower, an activated carbon adsorption water producing tank, and an activated carbon adsorption water producing tank lift pump;

the liquid outlet of the advanced catalytic oxidation tower is connected to the liquid inlet of the ozone catalytic water producing tank, the liquid outlet of the ozone catalytic water producing tank is connected to the liquid inlet of the ozone catalytic water producing lifting pump, the liquid outlet of the ozone catalytic water producing lifting pump is connected to the liquid inlet of the activated carbon adsorption tower, the liquid outlet of the activated carbon adsorption tower is connected to the liquid inlet of the activated carbon adsorption water producing tank, the liquid outlet of the activated carbon adsorption water producing tank is connected to the liquid inlet of the activated carbon adsorption water producing tank lifting pump, and the liquid outlet of the activated carbon adsorption water producing tank lifting pump is connected to the liquid inlet of the silicon-removing high-efficiency coagulation sedimentation tank.

In one possible implementation manner, an ozone circulating pump and an ozone conveying port are arranged on an ozone circulating pipeline of the advanced catalytic oxidation tower, an air outlet of an ozone generator is connected to the ozone conveying port, and an exhaust gas outlet of the advanced catalytic oxidation tower is connected to an ozone tail gas damage system.

In one possible implementation, the silicon removal section further comprises a silicon removal production water tank;

the liquid outlet of the silicon-removing high-efficiency coagulating sedimentation tank is connected with the liquid inlet of the silicon-removing water-producing tank;

the dosing ports of the silicon removal water producing pool are respectively connected with a PFS dosing device, a sodium metaaluminate dosing device, a liquid alkali dosing device, a PAM dosing device and a sulfuric acid dosing device.

In one possible implementation, the ultrafiltration chelation bed section further comprises an ultrafiltration water producing tank, an ultrafiltration water producing lift pump, and a nanofiltration buffer water tank;

the liquid outlet of the desilication water producing pond is connected with the liquid inlet of the ultrafiltration, the liquid outlet of the ultrafiltration is connected with the liquid inlet of the ultrafiltration water producing pond, the liquid outlet of the ultrafiltration water producing pond is connected with the liquid inlet of the ultrafiltration water producing lifting pump, the liquid outlet of the ultrafiltration water producing lifting pump is connected with the liquid inlet of the chelating bed, and the liquid outlet of the chelating bed is connected with the liquid inlet of the nanofiltration buffer water tank.

In one possible implementation manner, the nanofiltration salt separation section further comprises a nanofiltration water feed pump, a cartridge filter, a nanofiltration high pressure water feed pump, a nanofiltration water production pool and a nanofiltration concentrated water pool;

the liquid outlet of the nanofiltration buffer water tank is connected with the liquid inlet of the nanofiltration water supply pump, the liquid outlet of the nanofiltration water supply pump is connected with the liquid inlet of the security filter, the liquid outlet of the security filter is connected with the liquid inlet of the nanofiltration high-pressure water supply pump, the liquid outlet of the nanofiltration high-pressure water supply pump is connected with the liquid inlet of the nanofiltration device, the water outlet of the nanofiltration device is connected with the liquid inlet of the nanofiltration water supply tank, and the liquid outlet of the nanofiltration water supply tank is connected with the sodium chloride evaporation crystallization system;

the concentrated water outlet of the nanofiltration device is connected with the liquid inlet of the nanofiltration concentrated water tank.

In one possible implementation manner, the evaporation crystallization section comprises a nanofiltration concentrated water delivery pump, a sodium sulfate crystallizer, a crystallization heating chamber, a sodium sulfate crystallization tank, a freezing crystallizer, a hot melt crystallizer and a hot melt crystal slurry tank;

the circulating liquid outlet of the sodium sulfate crystallizer is connected with the liquid inlet of the crystallization heating chamber through a sodium sulfate circulating pipeline, and a sodium sulfate crystallization circulating pump is arranged on the sodium sulfate circulating pipeline;

the liquid outlet of the nanofiltration concentrated water tank is connected with the liquid inlet of the sodium sulfate circulating pipeline through a nanofiltration concentrated water pipeline, and a nanofiltration concentrated water pump is arranged on the nanofiltration concentrated water pipeline;

the liquid outlet of the crystallization heating chamber is connected with the circulating liquid inlet of the sodium sulfate crystallizer;

the liquid outlet of the sodium sulfate crystallizer is connected with the liquid inlet of the sodium sulfate crystallization tank, the liquid outlet of the sodium sulfate crystallization tank is connected with the liquid inlet of the freezing crystallizer, the liquid outlet of the freezing crystallizer is connected with the liquid inlet of the hot melt crystallizer, and the liquid outlet of the hot melt crystallizer is connected with the liquid inlet of the hot melt crystal slurry tank;

an external cooler and a freezing crystallization circulating pump are arranged on an evaporation mother liquor circulating pipe of the freezing crystallizer.

In one possible implementation, the dry packaging section includes a hot melt magma transfer pump, a sodium sulfate cyclone, a sodium sulfate separator, a vibrating fluidized bed, a sodium sulfate packing machine, a cyclone, and a sodium sulfate silo;

the liquid outlet of the hot melt crystal slurry tank is connected with the liquid inlet of the hot melt crystal slurry conveying pump, and the liquid outlet of the hot melt crystal slurry conveying pump is connected with the liquid inlet of the sodium sulfate cyclone;

the concentrated solution outlet of the sodium sulfate cyclone is connected with the liquid inlet of the sodium sulfate separator, the discharge port of the sodium sulfate separator is connected with the feed inlet of the vibrating fluidized bed, and the discharge port of the vibrating fluidized bed is connected with the feed inlet of the sodium sulfate bin;

the clear liquid outlet of the sodium sulfate cyclone is connected with the liquid inlet of the sodium sulfate crystallizer, and the liquid outlet of the sodium sulfate separator is connected with the liquid inlet of the sodium sulfate crystallizer;

the air outlet of the vibrating fluidized bed is connected with the air inlet of the cyclone separator, the dust outlet at the bottom of the cyclone separator is connected with the feed inlet of the sodium sulfate bin, and the discharge outlet of the sodium sulfate bin is connected with the feed inlet of the sodium sulfate packaging machine.

In one possible implementation, the dry packaging section includes an induced draft fan, a water scrubber, a mist eliminator, and a dust discharge drum;

the gas outlet at cyclone top connect in the air inlet of draught fan, the gas outlet of draught fan connect in the air inlet of washing tower, the gas outlet of washing tower connect in the air inlet of defroster, the gas outlet of defroster connect in the air inlet of dirt discharge tube.

One or more technical solutions provided in the embodiments of the present utility model at least have the following technical effects or advantages:

the embodiment of the utility model provides a coal chemical industry zero-emission high-concentration brine recycling treatment system, which solves the problems of low salt recycling utilization rate, unstable device operation, large impurity salt yield and the like in the concentrated brine in the prior art, realizes the recycling utilization of sodium sulfate in the coal chemical industry zero-emission high-concentration brine nanofiltration concentrated water, solves the problems of COD, silicon, carbonate and the like affecting the salt production quality, reduces the carbon-changing frequency of activated carbon, eliminates the restriction factors affecting the nanofiltration salt-separating operation, ensures the long-period stable operation of nanofiltration salt-separating, meets the requirements of sodium sulfate production industrial salt, and finally produces qualified sodium sulfate. Simultaneously, the corrosion of the slurry to the evaporation and crystallization working section is effectively reduced, and the daily maintenance cost of equipment and facilities is effectively reduced.

Drawings

In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the drawings that are required to be used in the description of the embodiments will be briefly described below. It is obvious that the drawings in the following description are only some embodiments of the present utility model, and that other drawings may be obtained from these drawings without inventive effort for a person of ordinary skill in the art.

Fig. 1 is a schematic structural diagram of a system for recycling and treating high-concentration brine in coal chemical industry.

Reference numerals: 1-a decarburization tower; 2-advanced catalytic oxidation tower; 3-a desilication high-efficiency coagulating sedimentation tank; 4-ultrafiltration; 5-chelation bed; 6-nanofiltration device; 7-a decarbonization tower fan; 8-an intermediate pool; 9-an ozone catalytic water producing pool; 10-an activated carbon adsorption tower; 11-an activated carbon adsorption water producing tank; 12-an ozone circulation pipeline; 13-a silicon removal water producing pool; 14-ultra-filtering a water producing tank; 15-nanofiltration buffer water tank; 16-a cartridge filter; 17-nanofiltration water producing pool; 18-nanofiltration concentrated water tank; a 19-sodium sulfate crystallizer; 20-a crystallization heating chamber; a 21-sodium sulfate crystallization tank; 22-freezing crystallizer; 23-a hot melt crystallizer; 24-a hot melt crystal slurry pool; 25-sodium sulfate cyclone; a 26-sodium sulfate separator; 27-vibrating a fluidized bed; 28-sodium sulfate packing machine; 29-cyclone separator; 30-sodium sulfate bin; 31-induced draft fan; 32-a water washing tower; 33-demister; 34-a dust discharge cartridge; 35-an external cooler;

Detailed Description

The following description of the embodiments of the present utility model will be made clearly and fully with reference to the accompanying drawings, in which it is evident that the embodiments described are some, but not all embodiments of the utility model. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.

In the description of the embodiments of the present utility model, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," "outer," and the like indicate or are based on the orientation or positional relationship shown in the drawings, merely to facilitate description of the embodiments of the present utility model and simplify description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model. The terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. Furthermore, the terms "mounted," "connected," "coupled," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the embodiments of the present utility model will be understood by those of ordinary skill in the art according to specific circumstances.

As shown in fig. 1, the system for recycling and treating the high-concentration brine with zero emission in the coal chemical industry provided by the embodiment of the utility model comprises a decarburization working section, a high-grade catalytic oxidation working section, a desilication working section, an ultrafiltration chelating bed working section, a nanofiltration salt separation working section, an evaporation crystallization working section, a drying packaging working section and a dust removal working section which are sequentially arranged according to a treatment flow.

The decarbonization section comprises a decarbonization tower 1, wherein the decarbonization tower 1 is used for removing free carbon dioxide in high-concentration brine.

The advanced catalytic oxidation section comprises an advanced catalytic oxidation tower 2, and the advanced catalytic oxidation tower 2 is used for removing COD in the high-concentration brine.

The silicon removal section comprises a silicon removal high-efficiency coagulating sedimentation tank 3, and the silicon removal high-efficiency coagulating sedimentation tank 3 is used for removing silicon in high-concentration brine.

The ultrafiltration chelation bed section comprises ultrafiltration 4 and chelation bed 5, wherein the ultrafiltration 4 is used for removing suspended matters in the high-concentration brine, and the chelation bed 5 is used for selectively adsorbing divalent metal ions in the high-concentration brine.

The nanofiltration salt separation section comprises a nanofiltration device 6, wherein the nanofiltration device 6 is used for separating high-concentration salt water into two parts of sodium chloride-containing brine and sodium sulfate-containing brine.

The evaporating and crystallizing section carries out evaporating and crystallizing on the sodium sulfate-containing brine, the drying and packaging section further removes water from the crystallized sodium sulfate slurry and realizes purification and recycling of sodium sulfate, and the dust removing section treats dust generated by the drying and packaging section.

The decarbonization tower 1 removes carbon dioxide contained in the gas with a liquid absorbent.

The advanced catalytic oxidation tower 2 uses ozone as an oxidant, and hydroxyl radicals generated on the surface of a special catalyst are utilized to oxidize and remove organic matters in water. When hydroxyl free radicals react with organic matters, the organic matters which are difficult to degrade in water can be decomposed in a non-selective, thorough and rapid way, and the organic free radicals generated in the reaction process can continuously participate in a chain reaction, so that the oxidation reaction process is accelerated, and finally, the organic matters which are difficult to degrade are mineralized into water and carbon dioxide.

The desilication high-efficiency coagulating sedimentation tank 3 comprehensively adopts a mode of desilication by sodium metaaluminate medicament, and is matched with a reaction tank, a flocculation tank, a clarification tank and the like. Silicon in sewage mainly exists in two forms of suspended silicon dioxide and soluble silicate ions, and coagulation silicon removal is realized by utilizing the adsorption or agglomeration of oxides or hydroxides of certain metals on silicic acid. Although the amount of silicon element in the high-concentration brine is small, the influence on the system is large, and particularly for salt recycling, it is necessary to remove silicon before evaporation. The silicon removal high-efficiency coagulating sedimentation tank 3 removes the silicon before evaporation to below 20mg/L, thereby greatly reducing the risk of silicon scaling and ensuring the long-period stable operation of the evaporating crystallization device.

The ultrafiltration 4 is a screening process related to the pore size of the membrane, uses the pressure difference at two sides of the membrane as a driving force, uses an ultrafiltration membrane as a filtering medium, and under a certain pressure, when the stock solution flows through the surface of the membrane, a plurality of tiny micropores densely distributed on the surface of the ultrafiltration membrane only allow water and small molecular substances to pass through to become permeate, and substances with the volume larger than the micro pore size of the surface of the membrane in the stock solution are trapped at the liquid inlet side of the membrane to become concentrate, so that the purposes of purifying, separating and concentrating the stock solution are realized.

The mechanism of the chelate resin in the chelate bed 5 for adsorbing metal ions is that functional atoms on the resin and the metal ions undergo coordination reaction to form a stable structure similar to a micromolecular chelate, so that the purpose of adsorbing divalent metal ions in high-concentration brine is realized.

The nanofiltration membrane of the nanofiltration device 6 and electrolyte ions form an electrostatic effect, the charge intensity of electrolyte salt ions is different, so that the rejection rate of the membrane to the ions is different, in a multi-element system containing ions in different valence states, the selectivity of the membrane to the ions is different due to the southwest effect, and the proportion of the ions passing through the membrane is different, so that sodium chloride in a concentrated salt solution is separated from mixed salt.

The evaporating and crystallizing section carries out evaporating and crystallizing on the sodium sulfate-containing brine, the drying and packaging section further removes water from the crystallized sodium sulfate slurry and realizes purification and recycling of sodium sulfate, and the dust removing section treats dust generated by the drying and packaging section. The system can realize the recycling utilization of the high-concentration brine with zero emission in the coal chemical industry, improve the recycling utilization rate of sodium sulfate, and solve the problems that the existing treatment system has high labor intensity for changing carbon and the components such as COD, metal ions, alkalinity, silicon and the like affect evaporation and salt separation. Realizing the high-efficiency and low-cost recycling utilization of sodium sulfate in the high-concentration brine.

In this embodiment, the decarbonization section further includes a decarbonization tower blower 7, an intermediate basin 8, and an intermediate basin lift pump.

The liquid outlet of the high-concentration brine conveying pipe is connected with the liquid inlet of the decarburization tower 1, and the air outlet of the decarburization tower fan 7 is connected with the air inlet of the decarburization tower 1.

The liquid outlet of decarbonization tower 1 is connected in the inlet of middle pond 8, and the liquid outlet of middle pond 8 is connected in the inlet of middle pond elevator pump, and the liquid outlet of middle pond elevator pump is connected in the inlet of advanced catalytic oxidation tower 2.

The decarburization section may be provided with a multistage decarburization tower 1 according to the specific water quality.

The decarburization tower fan 3 is used for providing air, brine is uniformly sprayed to the packing layer through a spraying device at the upper part of the decarburization tower 1, the lower part is purged by the input air, and the air is in countercurrent contact with the brine to blow out carbon dioxide in the brine, so that the carbon dioxide in the gas is removed.

In this embodiment, the advanced catalytic oxidation section further includes an ozone catalytic water producing tank 9, an ozone catalytic water producing lift pump, an activated carbon adsorption tower 10, an activated carbon adsorption water producing tank 11, and an activated carbon adsorption water producing tank lift pump.

The liquid outlet of advanced catalytic oxidation tower 2 is connected in the inlet of ozone catalysis and produces pond 9, the liquid outlet of ozone catalysis and produce pond 9 is connected in the inlet of ozone catalysis and produce the water elevator pump, the liquid outlet of ozone catalysis and produce the water elevator pump is connected in the inlet of active carbon adsorption tower 10, the liquid outlet of active carbon adsorption tower 10 is connected in the inlet of active carbon adsorption and produce pond 11, the liquid outlet of active carbon adsorption and produce pond 11 is connected in the inlet of active carbon adsorption and produce pond elevator pump, the liquid outlet of active carbon adsorption and produce pond elevator pump is connected in the inlet of desilication high-efficient coagulating sedimentation tank 3.

In this embodiment, an ozone circulation pump and an ozone delivery port are arranged on the ozone circulation pipeline 12 of the advanced catalytic oxidation tower 2, an air outlet of an ozone generator is connected to the ozone delivery port, and an exhaust gas outlet of the advanced catalytic oxidation tower 2 is connected to an ozone tail gas destruction system.

The ozone catalytic water producing tank 9 adopts a high-efficiency oxidant catalytic oxidation process to treat the wastewater. The catalyst loaded with the transition metal ions is added into the oxidation system, so that an obvious catalytic effect can be generated on the oxidation of the oxidant, and the self-decomposition of the oxidant in water can be catalyzed, thereby improving the oxidation effect of the oxidant, effectively reducing organic pollutants in water, reducing the use amount of subsequent activated carbon, improving the operation period of the evaporation device and ensuring the standard rate of product salt.

The activated carbon adsorption tower 10 removes the chromaticity of the high-concentration brine, and the working section can be provided with a plurality of stages of activated carbon adsorption towers 10 according to specific water quality conditions.

The activated carbon adsorption water producing tank 11 is a collecting buffer tank and plays a role in regulating the water quality and quantity.

The ozone circulating pump is used for taking water from the upper part of the reaction tank of the advanced catalytic oxidation tower 2, feeding water from the bottom, the ozone circulating pump is matched with the water outlet pipeline of the water ejector, ozone gas is efficiently dissolved into sewage through the water ejector, and when the process is operated, residual ozone gas in the reactor is completely collected and enters the ozone tail gas damage system, so that no ozone leakage is ensured.

In this embodiment, the silicon removal section further comprises a silicon removal water producing pool 13.

The liquid outlet of the silicon-removing high-efficiency coagulating sedimentation tank 3 is connected with the liquid inlet of the silicon-removing water producing tank 13.

The dosing ports of the silicon removal water producing pool 13 are respectively connected with a PFS dosing device, a sodium metaaluminate dosing device, a liquid alkali dosing device, a PAM dosing device and a sulfuric acid dosing device.

The high-efficiency coagulation sedimentation tank 3 for removing silicon removes silicon in the high-concentration brine before evaporation to below 20mg/L, thereby greatly reducing the risk of silicon scaling and ensuring the long-period stable operation of the evaporation crystallization section. The material treated by the silicon-removing high-efficiency coagulating sedimentation tank 3 enters a silicon-removing water-producing tank 13, and the silicon-removing water-producing tank 13 plays a role in adjusting the water quality and the water quantity.

PFS dosing device: the polymeric ferric sulfate PFS is a novel high-efficiency inorganic polymeric flocculant, and has the advantages of good polymeric property, stable chemical property and high sedimentation speed. The suspended solids and the organic substances are coagulated with the added polymeric iron to produce micro-flocculated particles. The concentration of the added polymeric iron is manually set by an operator in the DCS, and the polymeric iron is kept unchanged for a long time, so that the water quality is changed strongly.

Sodium metaaluminate dosing device: sodium metaaluminate is added to settle the generated aluminum silicate.

Liquid alkali dosing device: to ensure pH, sodium hydroxide is added to the treatment system. Sodium hydroxide has not only a function of adjusting pH but also a part of silica, carbon dioxide, etc. can be removed.

PAM dosing device: polyacrylamide PAM converts the micro-flocculated particles into large, dense particles, which facilitate sedimentation.

Sulfuric acid dosing device: and (3) adjusting the pH value of the discharged material of the desilication high-efficiency coagulating sedimentation tank 3.

In this embodiment, the ultrafiltration chelation bed section further comprises an ultrafiltration water producing tank 14, an ultrafiltration water producing lift pump, and a nanofiltration buffer water tank 15.

The liquid outlet of the desilication water producing pond 13 is connected with the liquid inlet of the ultrafiltration 4, the liquid outlet of the ultrafiltration 4 is connected with the liquid inlet of the ultrafiltration water producing pond 14, the liquid outlet of the ultrafiltration water producing pond 14 is connected with the liquid inlet of the ultrafiltration water producing lift pump, the liquid outlet of the ultrafiltration water producing lift pump is connected with the liquid inlet of the chelation bed 5, and the liquid outlet of the chelation bed 5 is connected with the liquid inlet of the nanofiltration buffer water tank 15.

It should be noted that the ultrafiltration water producing tank 14 is a collection buffer tank for the material.

In this embodiment, the nanofiltration salt separation section further comprises a nanofiltration water feed pump, a cartridge filter 16, a nanofiltration high pressure water feed pump, a nanofiltration water production pool 17 and a nanofiltration concentrated water pool 18.

The liquid outlet of nanofiltration buffer tank 15 is connected in the inlet of nanofiltration feed water pump, and the liquid outlet of nanofiltration feed water pump is connected in the inlet of cartridge filter 16, and the liquid outlet of cartridge filter 16 is connected in the inlet of nanofiltration high pressure feed water pump, and the liquid outlet of nanofiltration high pressure feed water pump is connected in the inlet of nanofiltration device 6, and the water outlet of nanofiltration device 6 is connected in the inlet of nanofiltration water yield pond 17, and the liquid outlet of nanofiltration water yield pond 17 is connected in sodium chloride evaporation crystallization system.

The concentrated water outlet of the nanofiltration device 6 is connected with the liquid inlet of the nanofiltration concentrated water tank 18.

The trace suspended particles, colloids, microorganisms, etc. remaining in the water are trapped or adsorbed on the surface and pores of the filter element in the safety filter 16. The cartridge filter 16 adopts a formed filter material, and the stock solution passes through the filter material under the action of pressure, filter residues are remained on the pipe wall, and the filtrate flows out through the filter material, so that the purpose of filtration is achieved. The water discharged from the nanofiltration device 6 enters a nanofiltration water production pool 17 for caching.

The nanofiltration device 6 of the nanofiltration salt separation section is provided with two stages to ensure the content of sodium chloride in the nanofiltration water producing pool 17, ensure the proportion of sodium chloride to be stably maintained above 92%, the nanofiltration water producing pool 17 is connected with an independent sodium chloride evaporation crystallization system, and the nanofiltration concentrated water pool 18 is connected with an independent sodium sulfate evaporation crystallization unit.

The independent sodium chloride evaporation crystallization system adopts a six-effect evaporation system, 1 to 4 effects adopt falling film evaporation, 5 to 6 effects adopt forced circulation evaporation, negative pressure of 1 to 6 effects is increased by vacuum pump evacuation, evaporation temperature is decreased to form secondary steam for front effect evaporation, the secondary steam becomes a heat source for heating and evaporating rear effect feed liquid, waste heat steam and condensate after evaporation are used as a heat source of a feed liquid preheater, the falling film evaporation and the forced circulation evaporation are reasonably combined, and the unit feed liquid evaporation of the whole system is greatly reduced in evaporation consumption by fully utilizing waste heat. After six-effect evaporation crystallization process treatment, the final-effect concentrated solution is suspension with mixed salt solid crystallization content of 10-15% by mass. The suspension is pumped to an evaporative crystallization system by a thickener to be evaporated and crystallized, enters a vibrating fluidized bed and is then dried and packaged, so that the requirements of industrial salt national standard GB-T5462-2016 for sun-curing industrial salt secondary products are met.

In this embodiment, the evaporation crystallization section includes a nanofiltration concentrated water transfer pump, a sodium sulfate crystallizer 19, a crystallization heating chamber 20, a sodium sulfate crystallization tank 21, a freezing crystallizer 22, a hot melt crystallizer 23, and a hot melt slurry tank 24.

The circulating liquid outlet of the sodium sulfate crystallizer 19 is connected with the liquid inlet of the crystallization heating chamber 20 through a sodium sulfate circulating pipeline, and a sodium sulfate crystallization circulating pump is arranged on the sodium sulfate circulating pipeline.

The liquid outlet of the nanofiltration concentrated water tank 18 is connected with the liquid inlet of the sodium sulfate circulating pipeline through a nanofiltration concentrated water pipeline, and a nanofiltration concentrated water pump is arranged on the nanofiltration concentrated water pipeline.

The liquid outlet of the crystallization heating chamber 20 is connected with the circulating liquid inlet of the sodium sulfate crystallizer 19.

The liquid outlet of the sodium sulfate crystallizer 19 is connected with the liquid inlet of the sodium sulfate crystallization tank 21, the liquid outlet of the sodium sulfate crystallization tank 21 is connected with the liquid inlet of the freezing crystallizer 22, the liquid outlet of the freezing crystallizer 22 is connected with the liquid inlet of the hot melt crystallizer 23, and the liquid outlet of the hot melt crystallizer 23 is connected with the liquid inlet of the hot melt crystal slurry tank 24.

An external cooler 35 and a freezing and crystallizing circulating pump are arranged on the evaporation mother liquor circulating pipe of the freezing crystallizer 22.

The sodium sulfate-containing brine in the nanofiltration concentrated water tank 18 is conveyed to the crystallization heating chamber 20 through a nanofiltration concentrated water pipeline and a sodium sulfate circulating pipeline, the crystallization heating chamber 20 crystallizes the sodium sulfate-containing brine through the input steam, the crystallization heating chamber 20 inputs the steam through a steam pipe network, and the crystallization heating chamber 20 discharges the steam condensate for recovery.

The crystallization heating chamber 20 conveys the crystallized sodium sulfate-containing brine into the sodium sulfate crystallizer 19 for further crystallization, the circulating water output by the circulating liquid outlet of the sodium sulfate crystallizer 19 is conveyed to the crystallization heating chamber 20 for recrystallization through a sodium sulfate circulating pipeline, and the part of the sodium sulfate circulating pipeline, which is close to the liquid inlet, is obliquely arranged at 45 degrees, so that the material output is facilitated, and the pipeline blockage frequency is reduced.

The sodium sulfate crystallizer 19 conveys the crystallized sodium sulfate-containing brine to the sodium sulfate crystallization tank 21 for buffering through a liquid outlet of the sodium sulfate crystallizer, and after the sodium sulfate-containing brine in the sodium sulfate crystallization tank 21 is conveyed to the freezing crystallizer 22, the solubility of the sodium sulfate-containing brine is rapidly reduced under the influence of temperature, and finally the sodium sulfate-containing brine is separated out in the form of sodium sulfate decahydrate. The external cooler 35 and the freezing and crystallizing circulating pump form an independent refrigerating unit so as to ensure that sodium sulfate decahydrate is separated out after the temperature of the sodium sulfate-containing brine is reduced.

The precipitated sodium sulfate decahydrate is conveyed to a hot melt crystallizer 23 to be crystallized by hot melt evaporation, and finally the precipitated anhydrous sodium sulfate enters a hot melt crystal slurry tank 24. The steam condensate of the hot melt crystallizer 23 is the steam after heat exchange in the crystallization heating chamber 20, and the steam from the steam pipe network is used for heating the materials in the hot melt crystallizer 23, and evaporating and crystallizing to remove crystallization water after further melting.

In this embodiment, the dry packing section includes a hot melt magma transfer pump, a sodium sulfate cyclone 25, a sodium sulfate separator 26, a vibrating fluidized bed 27, a sodium sulfate packing machine 28, a cyclone 29, and a sodium sulfate silo 30.

The liquid outlet of the hot melt crystal slurry tank 24 is connected with the liquid inlet of a hot melt crystal slurry conveying pump, and the liquid outlet of the hot melt crystal slurry conveying pump is connected with the liquid inlet of a sodium sulfate cyclone 25.

The concentrated solution outlet of the sodium sulfate cyclone 25 is connected with the liquid inlet of the sodium sulfate separator 26, the discharge outlet of the sodium sulfate separator 26 is connected with the feed inlet of the vibrating fluidized bed 27, and the discharge outlet of the vibrating fluidized bed 27 is connected with the feed inlet of the sodium sulfate silo 30.

The clear liquid outlet of the sodium sulfate cyclone 25 is connected with the liquid inlet of the sodium sulfate crystallizer 19, and the liquid outlet of the sodium sulfate separator 26 is connected with the liquid inlet of the sodium sulfate crystallizer 19.

The gas outlet of the vibrating fluidized bed 27 is connected with the gas inlet of the cyclone 29, the dust outlet at the bottom of the cyclone 29 is connected with the feed inlet of the sodium sulfate bin 30, and the discharge outlet of the sodium sulfate bin 30 is connected with the feed inlet of the sodium sulfate packing machine 28.

The sodium sulfate cyclone 25 separates the sodium sulfate-containing brine output from the hot melt slurry tank 24 into a clear solution with a smaller density and a concentrated solution with a larger density under the action of centrifugal force, the concentrated solution is conveyed to the sodium sulfate separator 26, the sodium sulfate separator 26 separates solid particles in the concentrated solution from the liquid, the separated solid particles enter the vibrating fluidized bed 27 and are dried, sodium sulfate output from the vibrating fluidized bed 27 enters the sodium sulfate bin 30 for storage, and sodium sulfate output from the sodium sulfate bin 30 enters the sodium sulfate packing machine 28 for packing.

The clear liquid separated by the sodium sulfate cyclone 25 and the liquid separated by the sodium sulfate separator 26 are both conveyed to the sodium sulfate crystallizer 19 of the evaporative crystallization section for re-evaporative crystallization.

The cyclone 29 removes dust from the dust-laden air stream produced by the vibrating fluidized bed 27, and dust particles enter the sodium sulfate silo 30 through a dust outlet at the bottom of the cyclone 29 for recovery.

In this embodiment, the dry packaging section includes an induced draft fan 31, a water scrubber 32, a mist eliminator 33, and a dust discharge drum 34.

The gas outlet at cyclone 29 top is connected in the air inlet of draught fan 31, and the air outlet of draught fan 31 is connected in the air inlet of washing tower 32, and the air outlet of washing tower 32 is connected in the air inlet of defroster 33, and the air outlet of defroster 33 is connected in the air inlet of dirt discharge tube 34.

The waste gas at the top of the cyclone 29 enters the water scrubber 32 to be washed and dedusted under the action of the induced draft fan 31, then enters the demister 33 to filter out water mist, sodium sulfate and other components exist in the water mist, and the gas after reaching the standard is processed and enters the dust discharge barrel 34 to be discharged.

The treatment system solves the problems of low utilization rate of salt in strong brine, unstable device operation, large impurity salt yield and the like in the prior art, realizes the utilization of sodium sulfate in the strong brine nanofiltration device 6 with zero emission in coal chemical industry, solves the problems of COD, silicon, carbonate and the like affecting the quality of produced salt, reduces the carbon-changing frequency of activated carbon, eliminates the restriction factors affecting the salt separation operation of the nanofiltration device 6, ensures the stable operation of the nanofiltration device 6 in a long salt separation period, meets the requirements of industrial salt production of sodium sulfate, and finally produces sodium sulfate as an acceptable product. Simultaneously, the corrosion of the slurry to the evaporation and crystallization working section is effectively reduced, and the daily maintenance cost of equipment and facilities is effectively reduced.

In the present embodiment, it will be apparent to those skilled in the art that the present utility model is not limited to the details of the above-described exemplary embodiments, but that the present utility model may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. The present embodiments are, therefore, to be considered in all respects as illustrative and not restrictive, the scope of the utility model being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.

Claims (10)

1. A coal chemical industry zero release high strength brine resource utilization processing system, its characterized in that: comprises a decarburization working section, an advanced catalytic oxidation working section, a desilication working section, an ultrafiltration chelating bed working section, a nanofiltration salt separation working section, an evaporation crystallization working section, a drying packaging working section and a dedusting working section which are sequentially arranged according to a treatment flow;

the decarbonization section comprises a decarbonization tower (1), wherein the decarbonization tower (1) is used for removing free carbon dioxide in high-concentration brine;

the advanced catalytic oxidation section comprises an advanced catalytic oxidation tower (2), wherein the advanced catalytic oxidation tower (2) is used for removing COD in high-concentration brine;

the silicon removal working section comprises a silicon removal high-efficiency coagulating sedimentation tank (3), and the silicon removal high-efficiency coagulating sedimentation tank (3) is used for removing silicon in high-concentration brine;

the ultrafiltration chelation bed working section comprises an ultrafiltration (4) and a chelation bed (5), wherein the ultrafiltration (4) is used for removing suspended matters in the high-concentration brine, and the chelation bed (5) is used for selectively adsorbing divalent metal ions in the high-concentration brine;

the nanofiltration and salt separation working section comprises a nanofiltration device (6), wherein the nanofiltration device (6) is used for dividing high-concentration salt water into two parts, namely sodium chloride-containing salt water and sodium sulfate-containing salt water;

the evaporation and crystallization working section performs evaporation and crystallization on sodium sulfate-containing brine, the drying and packaging working section further removes water from the crystallized sodium sulfate slurry and realizes purification and recycling of sodium sulfate, and the dust removal working section treats dust generated by the drying and packaging working section.

2. The coal chemical industry zero release high-concentration brine recycling treatment system according to claim 1, which is characterized in that: the decarburization working section also comprises a decarburization tower fan (7), an intermediate water tank (8) and an intermediate water tank lifting pump;

the liquid outlet of the high-concentration brine conveying pipe is connected with the liquid inlet of the decarburization tower (1), and the air outlet of the decarburization tower fan (7) is connected with the air inlet of the decarburization tower (1);

the liquid outlet of decarburization tower (1) connect in the liquid inlet of middle pond (8), the liquid outlet of middle pond (8) connect in the liquid inlet of middle pond elevator pump, the liquid outlet of middle pond elevator pump connect in the liquid inlet of senior catalytic oxidation tower (2).

3. The coal chemical industry zero release high-concentration brine recycling treatment system according to claim 2, which is characterized in that: the advanced catalytic oxidation working section also comprises an ozone catalytic water producing tank (9), an ozone catalytic water producing lifting pump, an activated carbon adsorption tower (10), an activated carbon adsorption water producing tank (11) and an activated carbon adsorption water producing tank lifting pump;

the liquid outlet of advanced catalytic oxidation tower (2) connect in the inlet of ozone catalysis product pond (9), the liquid outlet of ozone catalysis product pond (9) connect in the inlet of ozone catalysis product water elevator pump, the liquid outlet of ozone catalysis product water elevator pump connect in the inlet of active carbon adsorption tower (10), the liquid outlet of active carbon adsorption tower (10) connect in the inlet of active carbon adsorption product pond (11), the liquid outlet of active carbon adsorption product pond (11) connect in the inlet of active carbon adsorption product pond elevator pump, the liquid outlet of active carbon adsorption product pond elevator pump connect in the inlet of desilication high-efficient coagulation sedimentation tank (3).

4. The coal chemical industry zero release high-concentration brine recycling treatment system according to claim 3, which is characterized in that: an ozone circulating pump and an ozone conveying port are arranged on an ozone circulating pipeline (12) of the advanced catalytic oxidation tower (2), an air outlet of an ozone generator is connected to the ozone conveying port, and an exhaust outlet of the advanced catalytic oxidation tower (2) is connected to an ozone tail gas damage system.

5. The coal chemical industry zero release high-concentration brine recycling treatment system according to claim 3, which is characterized in that: the silicon removal working section also comprises a silicon removal water producing pool (13);

the liquid outlet of the silicon-removing high-efficiency coagulating sedimentation tank (3) is connected with the liquid inlet of the silicon-removing water producing tank (13);

the dosing opening of the silicon removal water producing pool (13) is respectively connected with the PFS dosing device, the sodium metaaluminate dosing device, the liquid alkali dosing device, the PAM dosing device and the sulfuric acid dosing device.

6. The coal chemical industry zero release high strength brine recycling treatment system according to claim 5, which is characterized in that: the ultrafiltration chelating bed working section also comprises an ultrafiltration water producing tank (14), an ultrafiltration water producing lifting pump and a nanofiltration buffer water tank (15);

the liquid outlet of the desilication water producing pond (13) is connected to the liquid inlet of the ultrafiltration (4), the liquid outlet of the ultrafiltration (4) is connected to the liquid inlet of the ultrafiltration water producing pond (14), the liquid outlet of the ultrafiltration water producing pond (14) is connected to the liquid inlet of the ultrafiltration water producing lifting pump, the liquid outlet of the ultrafiltration water producing lifting pump is connected to the liquid inlet of the chelation bed (5), and the liquid outlet of the chelation bed (5) is connected to the liquid inlet of the nanofiltration buffer water tank (15).

7. The coal chemical industry zero release high-concentration brine recycling treatment system according to claim 6, which is characterized in that: the nanofiltration salt separation working section also comprises a nanofiltration water supply pump, a security filter (16), a nanofiltration high-pressure water supply pump, a nanofiltration water production pool (17) and a nanofiltration concentrated water pool (18);

the liquid outlet of the nanofiltration buffer water tank (15) is connected with the liquid inlet of the nanofiltration water supply pump, the liquid outlet of the nanofiltration water supply pump is connected with the liquid inlet of the security filter (16), the liquid outlet of the security filter (16) is connected with the liquid inlet of the nanofiltration high-pressure water supply pump, the liquid outlet of the nanofiltration high-pressure water supply pump is connected with the liquid inlet of the nanofiltration device (6), the water outlet of the nanofiltration device (6) is connected with the liquid inlet of the nanofiltration water production tank (17), and the liquid outlet of the nanofiltration water production tank (17) is connected with the sodium chloride evaporation crystallization system;

the concentrated water outlet of the nanofiltration device (6) is connected with the liquid inlet of the nanofiltration concentrated water tank (18).

8. The coal chemical industry zero release high strength brine recycling treatment system according to claim 7, which is characterized in that: the evaporation crystallization section comprises a nanofiltration concentrated water delivery pump, a sodium sulfate crystallizer (19), a crystallization heating chamber (20), a sodium sulfate crystallization tank (21), a freezing crystallizer (22), a hot melt crystallizer (23) and a hot melt crystal slurry tank (24);

the circulating liquid outlet of the sodium sulfate crystallizer (19) is connected with the liquid inlet of the crystallization heating chamber (20) through a sodium sulfate circulating pipeline, and a sodium sulfate crystallization circulating pump is arranged on the sodium sulfate circulating pipeline;

the liquid outlet of the nanofiltration concentrated water tank (18) is connected with the liquid inlet of the sodium sulfate circulating pipeline through a nanofiltration concentrated water pipeline, and a nanofiltration concentrated water pump is arranged on the nanofiltration concentrated water pipeline;

the liquid outlet of the crystallization heating chamber (20) is connected with the circulating liquid inlet of the sodium sulfate crystallizer (19);

the liquid outlet of the sodium sulfate crystallizer (19) is connected with the liquid inlet of the sodium sulfate crystallization tank (21), the liquid outlet of the sodium sulfate crystallization tank (21) is connected with the liquid inlet of the freezing crystallizer (22), the liquid outlet of the freezing crystallizer (22) is connected with the liquid inlet of the hot melt crystallizer (23), and the liquid outlet of the hot melt crystallizer (23) is connected with the liquid inlet of the hot melt crystal slurry tank (24);

an external cooler (35) and a freezing crystallization circulating pump are arranged on the evaporation mother liquor circulating pipe of the freezing crystallizer (22).

9. The coal chemical industry zero release high strength brine recycling treatment system according to claim 8, which is characterized in that: the drying and packaging working section comprises a hot melt crystal slurry conveying pump, a sodium sulfate cyclone (25), a sodium sulfate separator (26), a vibrating fluidized bed (27), a sodium sulfate packaging machine (28), a cyclone separator (29) and a sodium sulfate bin (30);

the liquid outlet of the hot melt crystal slurry tank (24) is connected with the liquid inlet of the hot melt crystal slurry conveying pump, and the liquid outlet of the hot melt crystal slurry conveying pump is connected with the liquid inlet of the sodium sulfate cyclone (25);

the concentrated solution outlet of the sodium sulfate cyclone (25) is connected with the liquid inlet of the sodium sulfate separator (26), the discharge port of the sodium sulfate separator (26) is connected with the feed inlet of the vibrating fluidized bed (27), and the discharge port of the vibrating fluidized bed (27) is connected with the feed inlet of the sodium sulfate bin (30);

the clear liquid outlet of the sodium sulfate cyclone (25) is connected with the liquid inlet of the sodium sulfate crystallizer (19), and the liquid outlet of the sodium sulfate separator (26) is connected with the liquid inlet of the sodium sulfate crystallizer (19);

the air outlet of the vibrating fluidized bed (27) is connected with the air inlet of the cyclone separator (29), the dust outlet at the bottom of the cyclone separator (29) is connected with the feeding port of the sodium sulfate bin (30), and the discharging port of the sodium sulfate bin (30) is connected with the feeding port of the sodium sulfate packaging machine (28).

10. The coal chemical industry zero release high strength brine recycling treatment system according to claim 9, which is characterized in that: the drying and packaging working section comprises an induced draft fan (31), a water washing tower (32), a demister (33) and a dust discharge barrel (34);

the gas outlet at cyclone (29) top is connected in the air inlet of draught fan (31), the gas outlet of draught fan (31) connect in the air inlet of washing tower (32), the gas outlet of washing tower (32) connect in the air inlet of defroster (33), the gas outlet of defroster (33) connect in the air inlet of dirt emission section of thick bamboo (34).