CN212102346U - Oil-based cutting waste liquid treatment and separation system based on supercritical water oxidation technology - Google Patents
Oil-based cutting waste liquid treatment and separation system based on supercritical water oxidation technology Download PDFInfo
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- CN212102346U CN212102346U CN202020611074.XU CN202020611074U CN212102346U CN 212102346 U CN212102346 U CN 212102346U CN 202020611074 U CN202020611074 U CN 202020611074U CN 212102346 U CN212102346 U CN 212102346U
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Abstract
The utility model discloses a processing and piece-rate system of oil base cutting waste liquid based on supercritical water oxidation technique, this system belong to supercritical water oxidation technical treatment sewage field. Processing and piece-rate system of oil base cutting waste liquid based on supercritical water oxidation technique includes oil base cutting waste liquid preliminary treatment subsystem, oil base cutting waste liquid reaction subsystem, cooling decompression subsystem, nitrous oxide purification subsystem and alkali lye preparation transport subsystem, the utility model discloses an aim at solving the problem that traditional sewage treatment system treatment effeciency is low, the utility model provides a system is fit for the processing of oil base cutting waste liquid more and has the function of high-efficient degradation organic matter, and the sewage after having handled can reach municipal sewage factory requirement of intaking to can produce nitrous oxide.
Description
Technical Field
The utility model relates to a supercritical water oxidation technology handles sewage field, especially relates to a processing and piece-rate system of oil base cutting waste liquid based on supercritical water oxidation technology.
Background
The oil-based cutting fluid has good lubricating property, cooling, cleaning, rust prevention and good stability, and is widely used for high-precision numerical control lathes, milling machines and planers. The oil-based cutting fluid is required to be replaced after the performance of the oil-based cutting fluid is reduced after being recycled for many times, so that waste cutting fluid is formed. The oil-based cutting fluid is milky white, tasteless, high in organic matter concentration (the peak value can reach 200000mg/L sometimes), good in chemical stability and complex in components, mainly contains an oily additive, an extrusion additive, an antirust additive, a mildew-proof additive, an anti-foam additive, metal powder, solid suspended matters and the like, can cause serious pollution to water resources and soil environment if not treated, and the cutting waste fluid belongs to HW09 series, can be discharged after being treated to reach the standard, or else needs to be collected and transported to a factory with dangerous waste resources for treatment.
Supercritical water oxidation is an advanced oxidation technology which takes supercritical water as a reaction medium and thoroughly decomposes organic pollutants in oil-based waste cutting fluid into inorganic micromolecular substances such as water, carbon dioxide and the like in a closed reactor under the working condition of participation of oxidant (air, oxygen, hydrogen peroxide and the like). Supercritical water has hydrogen bonds and is a double water molecular structure; the density is lower than that of normal temperature water by one order of magnitude; 1/3 with the viscosity of normal temperature water, which is equivalent to the air at normal temperature; along with the temperature rise, the surface tension of the gas-liquid interface is almost linearly reduced, and when the supercritical point is reached, the gas-liquid interface disappears and the surface tension is reduced to 0; under the supercritical condition, no matter how the temperature and the pressure are changed, water is a single-phase system all the time, and no phase interface exists; under the supercritical working condition, the dielectric constant of the supercritical water is reduced to below 2, which is equivalent to hexane at normal temperature, and the supercritical water can replace the traditional organic solvent, and has the diffusion coefficient close to 1.79 multiplied by 10 < -3 > cm2/s of superheated steam at the temperature of 450 ℃. The nonpolar of the supercritical water is mutually soluble with various organic pollutants to form a uniform single-phase reaction system, the reaction speed is high, the degradation rate of organic matters can reach more than 99 percent within 1 minute, the problem of secondary pollution caused by smoke discharged by a burning method is avoided, and the reaction mechanism belongs to free radical reaction; inorganic salts precipitate out in supercritical water. Therefore, supercritical water has solubility similar to an organic solvent and flowing and diffusing similar to gas, and ions in the supercritical water can also participate in reaction and can be used for treating oil-based cutting waste liquid.
The waste liquid containing chlorine and sulfur can generate hydrogen chloride and sulfur dioxide gas by adopting a supercritical water oxidation technology, and the gases can corrode equipment and influence the service life of the equipment; the waste liquid can produce salting out at supercritical water oxidation technique, and salt can block up equipment and pipeline, influences the long-time steady operation of system, has restricted this technique in the popularization and application of industrialization.
At present, cutting waste liquid is treated by mainly adopting a precipitation-demulsification-advanced oxidation method, wherein the advanced oxidation method mainly adopts a Fenton method (such as CN 201610503235.1), and a demulsifier and hydrochloric acid in a Fenton reaction in the technical process are easy to volatilize irritant gas, so that secondary pollution is caused to the operating environment, and the health of operators is seriously influenced; the process also comprises the steps of crushing filter residues, drying, thermal desorption, condensing oil gas, tempering oil water, centrifugally separating, treating water, purifying gas, cooling residues and solidifying the residues to treat the cutting waste liquid (such as CN201920185291.4), namely, the process adopts a distillation method to decompose organic matters in the cutting waste liquid, so that a large amount of energy is consumed, and the process flow is long; the method has the defects that the degradation efficiency of two-stage photocatalytic oxidation is low, anaerobic treatment is adopted after photocatalytic oxidation, the anaerobic retention time is long, the occupied area is large, and because the degradation of organic matters in the cutting fluid is incomplete, the pollution of an MBR membrane can be accelerated in the final MBR process, the membrane flux is reduced, and the treatment capacity of the cutting waste fluid is influenced.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model provides a be suitable for oil base cutting waste liquid, and have the ability of high-efficient degradation organic matter, reach municipal sewage factory requirement of intaking after handling to can produce nitrous oxide's processing system.
In view of the above circumstances, the utility model provides a processing and piece-rate system of oil base cutting waste liquid based on supercritical water oxidation technique, include: the oil-based cutting waste liquid pretreatment subsystem is respectively connected with the oil-based cutting waste liquid reaction subsystem and the cooling and pressure reduction subsystem, the oil-based cutting waste liquid reaction subsystem is respectively connected with the nitrous oxide purification subsystem and the alkali liquid preparation and conveying subsystem, and the cooling and pressure reduction subsystem is connected with the alkali liquid preparation and conveying subsystem.
Preferably, the oil-based cutting waste liquid pretreatment subsystem comprises a filtering and storing separation tank, a plunger pump and a preheater, the filtering and storing separation tank comprises a settling chamber and a buffer chamber, a filter screen is vertically arranged between the settling chamber and the buffer chamber, the settling chamber is used for receiving the oil-based cutting waste liquid and settling and separating impurities of the oil-based cutting waste liquid, the filter screen is used for filtering substances with density not greater than that of water, the buffer chamber is used for placing the filtered oil-based cutting waste liquid, the oil-based cutting waste liquid of the buffer chamber is pumped into the preheater connected with the plunger pump through the plunger pump connected with the buffer chamber, and the preheater is used for heating the oil-based cutting waste liquid; conveying the collected oil-based cutting waste liquid to a filtering, storing and separating tank through a pipeline or a tank car, then feeding the oil-based cutting waste liquid into a settling chamber, settling and separating impurities of the oil-based cutting waste liquid by the settling chamber, wherein the retention time of the cutting waste liquid in the settling chamber is 2-5 h, scrap iron, dust and other impurities in the cutting waste liquid are settled in a conical hopper at the bottom of the settling chamber under the action of gravity, the angle of the conical hopper is a four-sided cone, the included angle between the edge of the cone and the ground plane is 50-80 degrees, the volume of the conical hopper is 1/10-1/6 of the volume of the settling chamber, discharging the settling chamber when a certain concentration is accumulated, intercepting another part of substances with the density not greater than that of water in the oil-based cutting waste liquid in the settling chamber under the intercepting action of a filter screen, and manually removing the; pumping the oil-based cutting waste liquid subjected to gravity settling and filtering by a filter screen into a preheater for preheating by a plunger pump, wherein the preheater heats the oil-based cutting waste liquid to 380-410 ℃, the preheater adopts a U-shaped tubular heat exchanger or a floating head heat exchanger, the oil-based cutting waste liquid passes through a tube pass, and the smoke passes through a shell pass;
preferably, the oil-based cutting waste liquid reaction subsystem comprises a supercritical reactor, an air charge pump and an air purification device, wherein the air charge pump is used for sucking air and compressing the air, an air inlet of the air purification device is connected with an air outlet of the air charge pump through a first gas pipeline, an air outlet of the air purification device is connected with an air inlet of the supercritical reactor, a cutting waste liquid outlet of the preheater is connected with a cutting waste liquid inlet of the supercritical reactor, the supercritical reactor is used for performing heat and mass transfer reaction on the cutting waste liquid and the purified air, a salt discharge outlet is formed in the bottom of the supercritical reactor, and a first hydraulic salt discharge valve and a second hydraulic salt discharge valve are arranged at the salt discharge outlet; air is sucked by an air inflating pump, the air pressure is increased to be more than 23MPa through the compression action of the air inflating pump, the air tangentially enters a supercritical reactor after being subjected to oil removal and dehydration and impurity removal of air purification equipment, the air entering the supercritical reactor tangentially enters the inner wall of the reactor and performs heat and mass transfer reaction with the cutting waste liquid treated by the oil-based cutting waste liquid pretreatment subsystem through a spiral streamline, most organic matters in the cutting waste liquid are oxidized into carbon dioxide and water under the supercritical reaction condition, the rest small organic matters are oxidized into gases such as acetic acid and methane, and inorganic matters in the cutting waste liquid react to generate hydrogen sulfide, hydrogen chloride and nitrous oxide;
preferably, the cooling and pressure reducing subsystem comprises a condenser, a pressure reducing valve, a static mixer, a gas-liquid separation tank, a tap water tank and a feed water pump; a water outlet of the tap water tank is connected with a water inlet of the condenser through a water feeding pump, an air inlet of the condenser is connected with an air outlet of the supercritical reactor, and an air outlet of the condenser is connected to an air inlet of the static mixer through a pressure reducing valve; the water outlet of the condenser is connected to a gas-liquid separation tank through a first water flowing pipeline, the water outlet of the gas-liquid separation tank is connected to the water inlet of a tap water tank through a second water flowing pipeline in a return mode, and the gas outlet of the gas-liquid separation tank is used for discharging water vapor; gas generated after reaction of the supercritical reactor exchanges heat with the oil-based cutting waste liquid through a preheater in an oil-based cutting waste liquid pretreatment subsystem, the gas enters a condenser in a cooling and pressure reducing subsystem after being cooled to 120-180 ℃, the temperature is further reduced to 20-70 ℃, heat generated by cooling the gas is transferred to tap water which pumps the tap water from a tap water tank into the condenser from a water feeding pump, the tap water flows away from a tube pass, the gas flows away from a shell pass, the cooled gas is reduced to 5-8 MPa through a pressure reducing valve and then enters a static mixer, a mixture of water and steam after heat exchange from the condenser enters a gas-liquid separation tank for gas-liquid separation, the steam is discharged to a user for heat energy utilization, and a part of separated water is conveyed to the tap water tank for cyclic utilization;
preferably, the alkali liquor preparation and conveying subsystem comprises an alkali liquor tank and an alkali liquor pump, a water inlet of the alkali liquor tank is connected to the second water running pipeline, the alkali liquor tank is further provided with a lime inlet, a water outlet of the alkali liquor tank is connected to an alkali liquor inlet of the supercritical reactor through an alkali liquor pipeline, the alkali liquor pipeline is provided with the alkali liquor pump for pumping alkali liquor from the alkali liquor tank into the supercritical reactor, the alkali liquor pipeline is provided with an alkali liquor pipeline branch connected to the static mixer, the other part of water separated by the gas-liquid separation tank and the lime input from the outside are used for preparing solution in the alkali liquor tank, the alkali liquor generated after the stirring reaction of the stirrer in the alkali liquor tank is conveyed to the static mixer of the cooling and pressure reduction subsystem and the supercritical reactor in the oil-based cutting waste liquor reaction subsystem through the alkali liquor pump, and the alkali liquor enters the supercritical reactor and then undergoes neutralization reaction in the generation of acidic gases such as hydrogen chloride and hydrogen sulfide, reacting hydrogen sulfide, hydrogen chloride, acetic acid and other acidic substances to generate salt; after the alkali liquor pipeline branch is connected to the static mixer, the alkali liquor and the decompressed gas are subjected to mixing reaction in the static mixer, and the residual hydrogen sulfide, hydrogen chloride and carbon dioxide in the gas are neutralized and then enter a nitrous oxide purification subsystem;
preferably, the nitrous oxide purification subsystem comprises a high-pressure gas-liquid separator, a drying tower, an adsorption tower, a refrigerant and a low-temperature separation tank; the high-pressure gas-liquid separator is connected with the static mixer, a raffinate discharge port is formed in the high-pressure gas-liquid separator, a gas outlet in the high-pressure gas-liquid separator is connected to a gas inlet of the drying tower, a gas outlet in the drying tower is connected to a gas inlet of the adsorption tower, a gas outlet in the adsorption tower is connected to a gas inlet of the refrigerator, and the refrigerator is connected with a low-temperature separation tank; after gas discharged from a static mixer of a cooling and pressure reducing subsystem enters a high-pressure gas-liquid separator, most of moisture in the gas is separated, the separated residual liquid is discharged when the liquid level reaches a certain level, the separated gas enters a drying tower, silica gel, 13X and 3A molecular sieves are filled in the drying tower, the filling thickness of each layer of molecular sieve is 300-500 mm, the total filling height of the filling is 1500mm, the gas is separated from impurities such as moisture and carbon dioxide in the gas through the drying tower, then the gas enters an adsorption tower, activated carbon molecular sieves are filled in the adsorption tower, the filling thickness is 1200-1500 mm, the adsorption tower is used for adsorbing alkane in the gas, the gas after the alkane is removed enters a refrigerator, the gas is cooled to-70-90 ℃ through the refrigerator and then enters a low-temperature separation tank, and the air and nitrogen which are not liquefied are discharged to the outside through a gas outlet arranged on the low-temperature separation tank, liquefied nitrous oxide is bottled for use in medical anesthesia or for use as an oxidizer in rockets;
preferably, the oil-based cutting waste liquid pretreatment subsystem further comprises a heating furnace, wherein a gas outlet of the heating furnace is connected with a gas inlet of the preheater through a second gas pipeline, a valve is arranged on the second gas pipeline, and the plunger pump is an anti-corrosion plunger pump; when the temperature of the cutting waste liquid is not enough to be raised to the target temperature during start-up or when the heat provided by the reactor is insufficient, the heating furnace is started to burn natural gas, the cutting waste liquid is heated by using the heat generated by the burning of the natural gas, a burner adopted by the heating furnace is a low-nitrogen burner, when the content of organic matters in the oil-based cutting waste liquid is more than 20%, a valve arranged on the second gas pipeline is closed, and the energy generated by supercritical water oxidation of the organic matters in the oil-based cutting waste liquid maintains self reaction;
preferably, the condenser is a U-shaped tubular heat exchanger or a floating head heat exchanger;
preferably, a pipeline at an air inlet on the supercritical reactor is tangentially arranged with the supercritical reactor, a pipeline at an alkali liquor inlet is radially arranged with the supercritical reactor, an insulating layer is further arranged on the outer wall of the supercritical reactor, and a salt separation device is arranged at the lower part of the supercritical reactor; the alkali liquor inlets are symmetrically arranged in pairs on the same circumferential interface of the supercritical reactor, the number of the alkali liquor inlets is 4, 6 or 8, the alkali liquor enters the supercritical reactor in the form of impinging stream to perform heat and mass transfer reaction on acid substances, and the acid substances in the supercritical reactor are completely neutralized;
preferably, the salt separation device is in a structure of an inverted cone at the lower part of an upper cone, a salt buffer tank is arranged between the first hydraulic salt discharge valve and the second hydraulic salt discharge valve, the salt generated by neutralization reaction is carried to the salt separation device at the lower part of the supercritical reactor under the action of the tangential force of the three-dimensional spiral flow of air and the gravity of the salt separation device, in order to prevent the salt from being blocked at the outlet of the supercritical reactor, the bottom of the supercritical reactor is a cone which is firstly reduced and then enlarged, the generated salt flows to an upper cone hopper under the action of air flow and falls into an inverted cone-shaped storage chamber under the action of gravity, when the salt in the storage chamber is stored to a certain height, the first hydraulic salt discharge valve and the second hydraulic salt discharge valve are intermittently opened to discharge the residual salt, when the first hydraulic salt discharge valve is opened and the second hydraulic salt discharge valve is closed, the salt in the critical supercritical reactor is discharged to the salt buffer tank, and after the residual salt in the supercritical reactor is discharged, closing the first hydraulic salt discharge valve and opening the second hydraulic salt discharge valve to completely discharge residual salt in the salt buffer tank, wherein the salt discharge time can be determined by calculation according to the concentration of inorganic matters in the reactant.
Compared with the prior art, the utility model discloses following beneficial effect has:
(1) the utility model provides a supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system which carries out supercritical reaction on the oil-based cutting waste liquid, and can realize rapid and thorough treatment on the oil-based cutting waste liquid; (2) the oil-based cutting waste liquid generates nitrous oxide in the supercritical water oxidation treatment process, and the nitrous oxide is subjected to temperature reduction, pressure reduction, gas purification and liquefaction and then used for medical treatment and aerospace rocket launching, so that a new energy structure is developed; (3) supercritical water, oil-based cutting waste liquid and air are mutually dissolved in any proportion, and interphase mass transfer resistance is eliminated, so that the reaction rate is greatly improved; (4) organic matters in the oil-based cutting waste liquid are quickly oxidized, the reaction can be carried out under the approximate adiabatic condition, the reaction time is short, and the size of the reactor is reduced; (5) the supercritical water oxidation technology has the advantages that the oil-based cutting waste liquid is completely treated through the supercritical water oxidation technology, a large amount of heat is released through reaction, and the first heat energy can be used as a heat source in a high-temperature process in the form of supercritical water; (6) when the concentration of organic matters in the oil-based cutting waste liquid is more than 2%, natural oxidation can be realized, auxiliary combustion oil is not required to be added, energy is saved, and the operation cost is reduced.
Drawings
FIG. 1 is a schematic diagram of the system connection provided by the present invention
FIG. 2 is a connection diagram of the concrete structure of the system
FIG. 3 is a schematic structural diagram of a supercritical reactor
FIG. 4 is a schematic view of the alkali liquor inlet of the supercritical reactor
FIG. 5 is a schematic view of the supercritical reactor at the air inlet
In the figure, 1 is an air charge pump, 2 is air purification equipment, 3 is a heating furnace, 4 is a filtering storage separation tank, 5 is a plunger pump, 6 is a preheater, 7 is a supercritical reactor, 701 is an alkali liquor inlet, 702 is an air inlet, 703 is a heat preservation layer, 704 is a salt separation device, 8 is a salt buffer tank, 9 is a tap water tank, 10 is a water feed pump, 11 is a condenser, 12 is a pressure reducing valve, 13 is a high-pressure gas-liquid separator, 14 is a gas-liquid separation tank, 15 is an alkali liquor tank, 16 is an alkali liquor pump, 17 is a static mixer, 18 is a drying tower, 19 is an adsorption tower, 20 is a refrigerator, 21 is a low-temperature separation tank, 22 is an alkali liquor pipeline, 23 is a first gas pipeline, 24 is a second gas pipeline, 25 is a second water pipeline, 26 is a first water pipeline, 27 is an alkali liquor pipeline branch, 28 is a first hydraulic salt discharge valve, and 29 is a second hydraulic salt discharge valve.
Detailed Description
In order to make the technical means, creation features, achievement purposes and functions of the present invention easy to understand, the present invention will be further described with reference to the following embodiments.
Example 1: as shown in fig. 1-5, for the utility model provides a processing and separating system of oil base cutting waste liquid based on supercritical water oxidation technique, include: the system comprises an oil-based cutting waste liquid pretreatment subsystem, an oil-based cutting waste liquid reaction subsystem, a cooling and pressure reducing subsystem, a nitrous oxide purification subsystem and an alkali liquor preparation and conveying subsystem, wherein the oil-based cutting waste liquid pretreatment subsystem is respectively connected with the oil-based cutting waste liquid reaction subsystem and the cooling and pressure reducing subsystem;
the oil-based cutting waste liquid pretreatment subsystem comprises a filtering, storing and separating tank 4, a plunger pump 5 and a preheater 6, wherein the filtering, storing and separating tank 4 internally comprises a settling chamber and a buffer chamber, a filter screen is vertically arranged between the settling chamber and the buffer chamber, the settling chamber receives oil-based cutting waste liquid with COD (chemical oxygen demand) of more than 37000mg/L and settles and separates impurities of the oil-based cutting waste liquid, the filter screen is used for filtering substances with density not more than that of water, the buffer chamber is used for placing the filtered oil-based cutting waste liquid, the oil-based cutting waste liquid of the buffer chamber is pumped into the preheater 6 connected with the plunger pump 5 through the plunger pump 5 connected with the buffer chamber, and the preheater 6 is used for heating the oil-based cutting waste liquid; conveying the collected oil-based cutting waste liquid to a filtering, storing and separating tank 4 through a pipeline or a tank car, then, feeding the oil-based cutting waste liquid into a settling chamber, settling and separating impurities of the oil-based cutting waste liquid by the settling chamber, wherein the retention time of the cutting waste liquid in the settling chamber is 3 hours, scrap iron, dust and other impurities in the cutting waste liquid are settled in a conical hopper at the bottom of the settling chamber under the action of gravity, the angle of the conical hopper is a four-sided cone, the included angle between the edge of the cone and the ground plane is 60 degrees, the volume of the conical hopper is 1/10 degrees of the volume of the settling chamber, when a certain concentration is accumulated, the cutting waste liquid is discharged out of the settling chamber, and another part of substances with the density not more than that of water in the oil-based cutting waste liquid is intercepted in the settling chamber; pumping the oil-based cutting waste liquid subjected to gravity settling and filtering by a filter screen into a preheater 6 for preheating by a plunger pump 5, heating the oil-based cutting waste liquid to 400 ℃ by the preheater 6, wherein the preheater 6 adopts a floating head type heat exchanger, the oil-based cutting waste liquid passes through a tube pass, and the smoke passes through a shell pass;
the oil-based cutting waste liquid reaction subsystem comprises a supercritical reactor 7, an air inflator pump 1 and an air purification device 2, wherein the air inflator pump 1 is used for sucking air and compressing the air, an air inlet 702 of the air purification device 2 is connected with an air outlet of the air inflator pump 1 through a first gas pipeline 23, an air outlet of the air purification device 2 is connected with an air inlet 702 of the supercritical reactor 7, a cutting waste liquid outlet of a preheater 6 is connected with a cutting waste liquid inlet of the supercritical reactor 7, the supercritical reactor 7 is used for carrying out heat and mass transfer reaction on the cutting waste liquid and the purified air, a salt discharge outlet is formed in the bottom of the supercritical reactor 7, and a first hydraulic salt discharge valve 28 and a second hydraulic salt discharge valve 29 are arranged at the salt discharge outlet; air is sucked by an air inflating pump 1, the air pressure is increased to 28MPa through the compression action of the air inflating pump 1, the air is subjected to oil removal, dehydration and impurity removal by an air purifying device 2 and then tangentially enters a supercritical reactor 7, the air entering the supercritical reactor 7 is subjected to heat and mass transfer reaction with cutting waste liquid treated by an oil-based cutting waste liquid pretreatment subsystem through a spiral streamline, most organic matters in the cutting waste liquid are oxidized into carbon dioxide and water under the supercritical reaction condition, the rest small organic matters are oxidized into gases such as acetic acid and methane, and inorganic matters in the cutting waste liquid are reacted to generate hydrogen sulfide, hydrogen chloride and nitric oxide; the oil-based cutting waste liquid pretreatment subsystem further comprises a heating furnace 3, wherein a gas outlet of the heating furnace 3 is connected with a gas inlet of the preheater 6 through a second gas pipeline 24, a valve is arranged on the second gas pipeline 24, and the plunger pump 5 is an anti-corrosion plunger pump 5; when the cutting waste liquid is started or the heat provided by the reactor is not enough to raise the temperature of the cutting waste liquid to the target temperature, the heating furnace 3 is started to burn natural gas, the cutting waste liquid is heated by using the heat generated by the burning of the natural gas, and a burner adopted by the heating furnace 3 is a low-nitrogen burner; after the reaction is carried out for 5min, closing a low-nitrogen burner of the heating furnace 3 and closing a valve, wherein a pipeline at an air inlet 702 on the supercritical reactor 7 is tangentially arranged with the supercritical reactor 7, an insulating layer 703 is also arranged on the outer wall of the supercritical reactor 7, and a salt separation device 704 is arranged at the lower part of the supercritical reactor 7; the salt separation device 704 is of a structure of an inverted cone at the lower part of an upper cone, a salt buffer tank 8 is arranged between the first hydraulic salt discharge valve 28 and the second hydraulic salt discharge valve 29, the salt generated by neutralization reaction is brought to the salt separation device 704 at the lower part of the supercritical reactor 7 under the action of the tangential force of the three-dimensional spiral flow of the air and the gravity of the salt, in order to prevent the salt from being blocked at the outlet of the supercritical reactor 7, the bottom of the supercritical reactor 7 is a cone which is firstly reduced and then enlarged, the generated salt flows to an upper cone hopper under the action of air flow and falls into a storage chamber of an inverted cone under the action of gravity, when the salt in the storage chamber is stored to a certain height, the first hydraulic salt discharge valve 28 and the second hydraulic salt discharge valve 29 are intermittently opened to discharge the residual salt, and when the first hydraulic salt discharge valve 28 is opened and the second hydraulic salt discharge valve 29 is closed, the salt in the supercritical reactor 7 is discharged to the salt buffer tank 8, after the residual salt in the supercritical reactor 7 is removed, closing the first hydraulic salt discharge valve 28 and opening the second hydraulic salt discharge valve 29 to completely remove the residual salt in the salt buffer tank 8, wherein the salt discharge time can be determined by calculation according to the concentration of inorganic matters in the reactant;
the cooling and pressure reducing subsystem comprises a condenser 11, a pressure reducing valve 12, a static mixer 17, a gas-liquid separation tank 14, a tap water tank 9 and a water feeding pump 10; a water outlet in the tap water tank 9 is connected with a water inlet of a condenser 11 through a water feeding pump 10, a gas inlet of the condenser 11 is connected with a gas outlet of the supercritical reactor 7, and a gas outlet of the condenser 11 is connected to a gas inlet of a static mixer 17 through a pressure reducing valve 12; the water outlet of the condenser 11 is connected to the gas-liquid separation tank 14 through a first water flowing pipeline 26, the water outlet of the gas-liquid separation tank 14 is connected back to the water inlet of the tap water tank 9 through a second water flowing pipeline 25, and the gas outlet of the gas-liquid separation tank 14 is used for discharging water vapor; the gas generated by the reaction of the supercritical reactor 7 exchanges heat with the oil-based cutting waste liquid through a preheater 6 in an oil-based cutting waste liquid pretreatment subsystem, the gas enters a condenser 11 in a cooling and pressure reducing subsystem after being cooled to 160 ℃, the temperature is further reduced to 50 ℃, the heat generated by the cooling of the gas is transferred to tap water which pumps a tap water tank 9 into the condenser 11 from a water feeding pump 10, the tap water flows away from a tube pass, the gas flows away from a shell pass, the cooled gas is reduced to 6MPa through a pressure reducing valve 12, the pressure is then reduced to 6MPa, the gas enters a static mixer 17, the mixture of water and steam after the heat exchange of the condenser 11 enters a gas-liquid separation tank 14 for gas-liquid separation, the steam is discharged to a user for heat energy utilization, and a part of the separated water is conveyed to the tap water tank 9 for cyclic;
the alkali liquor preparation and conveying subsystem comprises an alkali liquor box 15 and an alkali liquor pump 16, a water inlet of the alkali liquor box 15 is connected to a second water flowing pipeline 25, the alkali liquor box 15 is further provided with a lime inlet, a water outlet of the alkali liquor box 15 is connected to an alkali liquor inlet 701 of the supercritical reactor 7 through an alkali liquor pipeline 22, pipelines at the alkali liquor inlet 701 and the supercritical reactor 7 are radially arranged, the alkali liquor inlets 701 are symmetrically arranged in pairs on the same circumferential interface of the supercritical reactor 7, the number of the alkali liquor inlets is 4, the alkali liquor enters the supercritical reactor 7 in an impinging stream mode to perform heat and mass transfer reaction with acid substances, and the acid substances in the supercritical reactor 7 are completely neutralized; the alkali liquor pipeline 22 is provided with an alkali liquor pump 16 for pumping alkali liquor from an alkali liquor tank 15 into the supercritical reactor 7, after air reacts with the oil-based cutting waste liquor for 10 seconds, the alkali liquor pump 16 is started, the alkali liquor pipeline 22 is provided with an alkali liquor pipeline branch 27 connected to the static mixer 17, the other part of water separated by the gas-liquid separation tank 14 and lime input from the outside are mixed into a solution in the alkali liquor tank 15, after stirring reaction of a stirrer in the alkali liquor tank 15, the generated alkali liquor is conveyed to the static mixer 17 of the cooling and pressure reducing subsystem and the supercritical reactor 7 in the oil-based cutting waste liquor reaction subsystem through the alkali liquor pump 16, and after entering the supercritical reactor 7, the alkali liquor reacts with acidic gases such as hydrogen chloride and hydrogen sulfide to react with acidic substances such as hydrogen sulfide, hydrogen chloride and acetic acid to generate salt; after the alkali liquor pipeline branch 27 is connected to the static mixer 17, the alkali liquor and the decompressed gas are subjected to mixing reaction in the static mixer 17, and the residual hydrogen sulfide, hydrogen chloride and carbon dioxide in the gas are neutralized and then enter a nitrous oxide purification subsystem;
the nitrous oxide purification subsystem comprises a high-pressure gas-liquid separator 13, a drying tower 18, an adsorption tower 19, a refrigerant and a low-temperature separation tank 21; the high-pressure gas-liquid separator 13 is connected with the static mixer 17, a raffinate discharge port is formed in the high-pressure gas-liquid separator 13, a gas outlet of the high-pressure gas-liquid separator 13 is connected to a gas inlet of a drying tower 18, a gas outlet of the drying tower 18 is connected to a gas inlet of an adsorption tower 19, a gas outlet of the adsorption tower 19 is connected to a gas inlet of a refrigerator 20, and the refrigerator 20 is connected with a low-temperature separation tank 21; after gas discharged from a static mixer 17 of a cooling and pressure reducing subsystem enters a high-pressure gas-liquid separator 13, most of moisture in the gas is separated, the separated residual liquid is discharged when the liquid level reaches a certain level, the separated gas enters a drying tower 18, silica gel, 13X and 3A molecular sieves are filled in the drying tower 18, the filling thickness of each layer of molecular sieve is 400mm, the total filling height of the filling is 1500mm, the gas is separated from impurities such as moisture and carbon dioxide in the gas through the drying tower 18, then the gas enters an adsorption tower 19, activated carbon molecular sieves are filled in the adsorption tower 19, the filling thickness is 1300mm, the adsorption tower 19 is used for adsorbing alkane in the gas, the gas after the alkane is removed enters a refrigerator 20, the gas is cooled to-80 ℃ through the refrigerator 20 and then enters a low-temperature separation tank 21, and the unliquefied air and nitrogen are discharged to the outside through a gas outlet arranged on the low-temperature separation tank 21, liquefied nitrous oxide is bottled for use in medical anesthesia or for use as an oxidizer in rockets.
Example 2: as shown in fig. 1-5, for the utility model provides a processing and separating system of oil base cutting waste liquid based on supercritical water oxidation technique, include: the system comprises an oil-based cutting waste liquid pretreatment subsystem, an oil-based cutting waste liquid reaction subsystem, a cooling and pressure reducing subsystem, a nitrous oxide purification subsystem and an alkali liquor preparation and conveying subsystem, wherein the oil-based cutting waste liquid pretreatment subsystem is respectively connected with the oil-based cutting waste liquid reaction subsystem and the cooling and pressure reducing subsystem;
the oil-based cutting waste liquid pretreatment subsystem comprises a filtering, storing and separating tank 4, a plunger pump 5 and a preheater 6, wherein the filtering, storing and separating tank 4 internally comprises a settling chamber and a buffer chamber, a filter screen is vertically arranged between the settling chamber and the buffer chamber, the settling chamber receives oil-based cutting waste liquid with COD (chemical oxygen demand) of more than 100000mg/L and performs settling separation on impurities of the oil-based cutting waste liquid, the filter screen is used for filtering substances with density not more than that of water, the buffer chamber is used for placing the filtered oil-based cutting waste liquid, the oil-based cutting waste liquid of the buffer chamber is pumped into the preheater 6 connected with the plunger pump 5 through the plunger pump 5 connected with the buffer chamber, and the preheater 6 is used for heating the oil-based cutting waste; conveying the collected oil-based cutting waste liquid to a filtering, storing and separating tank 4 through a pipeline or a tank car, then, feeding the oil-based cutting waste liquid into a settling chamber, settling and separating impurities of the oil-based cutting waste liquid by the settling chamber, wherein the retention time of the cutting waste liquid in the settling chamber is 3 hours, scrap iron, dust and other impurities in the cutting waste liquid are settled in a conical hopper at the bottom of the settling chamber under the action of gravity, the angle of the conical hopper is a four-sided cone, the included angle between the edge of the cone and the ground plane is 60 degrees, the volume of the conical hopper is 1/10 degrees of the volume of the settling chamber, when a certain concentration is accumulated, the cutting waste liquid is discharged out of the settling chamber, and another part of substances with the density not more than that of water in the oil-based cutting waste liquid is intercepted in the settling chamber; pumping the oil-based cutting waste liquid subjected to gravity settling and filtering by a filter screen into a preheater 6 for preheating by a plunger pump 5, heating the oil-based cutting waste liquid to 410 ℃ by the preheater 6, wherein the preheater 6 adopts a U-shaped tubular heat exchanger, the oil-based cutting waste liquid passes through a tube pass, and the smoke passes through a shell pass;
the oil-based cutting waste liquid reaction subsystem comprises a supercritical reactor 7, an air inflator pump 1 and an air purification device 2, wherein the air inflator pump 1 is used for sucking air and compressing the air, an air inlet 702 of the air purification device 2 is connected with an air outlet of the air inflator pump 1 through a first gas pipeline 23, an air outlet of the air purification device 2 is connected with an air inlet 702 of the supercritical reactor 7, a cutting waste liquid outlet of a preheater 6 is connected with a cutting waste liquid inlet of the supercritical reactor 7, the supercritical reactor 7 is used for carrying out heat and mass transfer reaction on the cutting waste liquid and the purified air, a salt discharge outlet is formed in the bottom of the supercritical reactor 7, and a first hydraulic salt discharge valve 28 and a second hydraulic salt discharge valve 29 are arranged at the salt discharge outlet; air is sucked by an air inflating pump 1, the air pressure is increased to 25MPa through the compression action of the air inflating pump 1, the air is subjected to oil removal, dehydration and impurity removal by an air purifying device 2 and then tangentially enters a supercritical reactor 7, the air entering the supercritical reactor 7 is subjected to heat and mass transfer reaction with the cutting waste liquid treated by an oil-based cutting waste liquid pretreatment subsystem through a spiral streamline, most organic matters in the cutting waste liquid are oxidized into carbon dioxide and water under the supercritical reaction condition, the rest small organic matters are oxidized into gases such as acetic acid and methane, and inorganic matters in the cutting waste liquid are reacted to generate hydrogen sulfide, hydrogen chloride and nitric oxide; the oil-based cutting waste liquid pretreatment subsystem further comprises a heating furnace 3, wherein a gas outlet of the heating furnace 3 is connected with a gas inlet of the preheater 6 through a second gas pipeline 24, a valve is arranged on the second gas pipeline 24, and the plunger pump 5 is an anti-corrosion plunger pump 5; when the temperature of the cutting waste liquid is not sufficiently raised to the target temperature during the start-up or the heat provided by the reactor, the heating furnace 3 is started to burn natural gas, the cutting waste liquid is heated by the heat generated by the combustion of the natural gas, and a burner adopted by the heating furnace 3 is a low-nitrogen burner; after the reaction is carried out for 10min, closing a low-nitrogen burner of the heating furnace 3 and closing a valve, wherein a pipeline at an air inlet 702 on the supercritical reactor 7 is tangentially arranged with the supercritical reactor 7, an insulating layer 703 is also arranged on the outer wall of the supercritical reactor 7, and a salt separation device 704 is arranged at the lower part of the supercritical reactor 7; the salt separation device 704 is of a structure of an inverted cone at the lower part of an upper cone, a salt buffer tank 8 is arranged between the first hydraulic salt discharge valve 28 and the second hydraulic salt discharge valve 29, the salt generated by neutralization reaction is brought to the salt separation device 704 at the lower part of the supercritical reactor 7 under the action of the tangential force of the three-dimensional spiral flow of the air and the gravity of the salt, in order to prevent the salt from being blocked at the outlet of the supercritical reactor 7, the bottom of the supercritical reactor 7 is a cone which is firstly reduced and then enlarged, the generated salt flows to an upper cone hopper under the action of air flow and falls into a storage chamber of an inverted cone under the action of gravity, when the salt in the storage chamber is stored to a certain height, the first hydraulic salt discharge valve 28 and the second hydraulic salt discharge valve 29 are intermittently opened to discharge the residual salt, and when the first hydraulic salt discharge valve 28 is opened and the second hydraulic salt discharge valve 29 is closed, the salt in the supercritical reactor 7 is discharged to the salt buffer tank 8, after the residual salt in the supercritical reactor 7 is removed, closing the first hydraulic salt discharge valve 28 and opening the second hydraulic salt discharge valve 29 to completely remove the residual salt in the salt buffer tank 8, wherein the salt discharge time can be determined by calculation according to the concentration of inorganic matters in the reactant;
the cooling and pressure reducing subsystem comprises a condenser 11, a pressure reducing valve 12, a static mixer 17, a gas-liquid separation tank 14, a tap water tank 9 and a water feeding pump 10; a water outlet in the tap water tank 9 is connected with a water inlet of a condenser 11 through a water feeding pump 10, a gas inlet of the condenser 11 is connected with a gas outlet of the supercritical reactor 7, and a gas outlet of the condenser 11 is connected to a gas inlet of a static mixer 17 through a pressure reducing valve 12; the water outlet of the condenser 11 is connected to the gas-liquid separation tank 14 through a first water flowing pipeline 26, the water outlet of the gas-liquid separation tank 14 is connected back to the water inlet of the tap water tank 9 through a second water flowing pipeline 25, and the gas outlet of the gas-liquid separation tank 14 is used for discharging water vapor; the gas generated by the reaction of the supercritical reactor 7 exchanges heat with the oil-based cutting waste liquid through a preheater 6 in an oil-based cutting waste liquid pretreatment subsystem, the gas enters a condenser 11 in a cooling and pressure reducing subsystem after being cooled to 160 ℃, the temperature is further reduced to 50 ℃, the heat generated by the cooling of the gas is transferred to tap water which pumps a tap water tank 9 into the condenser 11 from a water feeding pump 10, the tap water flows away from a tube pass, the gas flows away from a shell pass, the cooled gas is reduced to 6MPa through a pressure reducing valve 12, the pressure is then reduced to 6MPa, the gas enters a static mixer 17, the mixture of water and steam after the heat exchange of the condenser 11 enters a gas-liquid separation tank 14 for gas-liquid separation, the steam is discharged to a user for heat energy utilization, and a part of the separated water is conveyed to the tap water tank 9 for cyclic;
the alkali liquor preparation and conveying subsystem comprises an alkali liquor box 15 and an alkali liquor pump 16, a water inlet of the alkali liquor box 15 is connected to a second water flowing pipeline 25, the alkali liquor box 15 is further provided with a lime inlet, a water outlet of the alkali liquor box 15 is connected to an alkali liquor inlet 701 of the supercritical reactor 7 through an alkali liquor pipeline 22, pipelines at the alkali liquor inlet 701 and the supercritical reactor 7 are radially arranged, the alkali liquor inlets 701 are symmetrically arranged in pairs on the same circumferential interface of the supercritical reactor 7, the number of the alkali liquor inlets is 4, the alkali liquor enters the supercritical reactor 7 in an impinging stream mode to perform heat and mass transfer reaction with acid substances, and the acid substances in the supercritical reactor 7 are completely neutralized; the alkali liquor pipeline 22 is provided with an alkali liquor pump 16 for pumping alkali liquor from an alkali liquor tank 15 into the supercritical reactor 7, after air reacts with the oil-based cutting waste liquor for 5 seconds, the alkali liquor pump 16 is started, the alkali liquor pipeline 22 is provided with an alkali liquor pipeline branch 27 connected to the static mixer 17, the other part of water separated by the gas-liquid separation tank 14 and lime input from the outside are mixed into a solution in the alkali liquor tank 15, after stirring reaction of a stirrer in the alkali liquor tank 15, the generated alkali liquor is conveyed to the static mixer 17 of the cooling and pressure reducing subsystem and the supercritical reactor 7 in the oil-based cutting waste liquor reaction subsystem through the alkali liquor pump 16, and after entering the supercritical reactor 7, the alkali liquor is subjected to neutralization reaction with acidic gases such as hydrogen chloride and hydrogen sulfide, so that acidic substances such as hydrogen sulfide, hydrogen chloride and acetic acid react to form salts; after the alkali liquor pipeline branch 27 is connected to the static mixer 17, the alkali liquor and the decompressed gas are subjected to mixing reaction in the static mixer 17, and the residual hydrogen sulfide, hydrogen chloride and carbon dioxide in the gas are neutralized and then enter a nitrous oxide purification subsystem;
the nitrous oxide purification subsystem comprises a high-pressure gas-liquid separator 13, a drying tower 18, an adsorption tower 19, a refrigerant and a low-temperature separation tank 21; the high-pressure gas-liquid separator 13 is connected with the static mixer 17, a raffinate discharge port is formed in the high-pressure gas-liquid separator 13, a gas outlet of the high-pressure gas-liquid separator 13 is connected to a gas inlet of a drying tower 18, a gas outlet of the drying tower 18 is connected to a gas inlet of an adsorption tower 19, a gas outlet of the adsorption tower 19 is connected to a gas inlet of a refrigerator 20, and the refrigerator 20 is connected with a low-temperature separation tank 21; after gas discharged from a static mixer 17 of a cooling and pressure reducing subsystem enters a high-pressure gas-liquid separator 13, most of moisture in the gas is separated, the separated residual liquid is discharged when the liquid level reaches a certain level, the separated gas enters a drying tower 18, silica gel, 13X and 3A molecular sieves are filled in the drying tower 18, the filling thickness of each layer of molecular sieve is 400mm, the total filling height of the filling is 1500mm, the gas is separated from impurities such as moisture and carbon dioxide in the gas through the drying tower 18, then the gas enters an adsorption tower 19, activated carbon molecular sieves are filled in the adsorption tower 19, the filling thickness is 1300mm, the adsorption tower 19 is used for adsorbing alkane in the gas, the gas after the alkane is removed enters a refrigerator 20, the gas is cooled to-80 ℃ through the refrigerator 20 and then enters a low-temperature separation tank 21, and the unliquefied air and nitrogen are discharged to the outside through a gas outlet arranged on the low-temperature separation tank 21, liquefied nitrous oxide is bottled for use in medical anesthesia or for use as an oxidizer in rockets.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments or portions thereof without departing from the spirit and scope of the invention.
Claims (10)
1. Processing and piece-rate system of oil base cutting waste liquid based on supercritical water oxidation technique, its characterized in that includes: the oil-based cutting waste liquid pretreatment subsystem is respectively connected with the oil-based cutting waste liquid reaction subsystem and the cooling and pressure reduction subsystem, the oil-based cutting waste liquid reaction subsystem is respectively connected with the nitrous oxide purification subsystem and the alkali liquid preparation and conveying subsystem, and the cooling and pressure reduction subsystem is connected with the alkali liquid preparation and conveying subsystem.
2. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 1, wherein: oil base cutting waste liquid preliminary treatment subsystem is including filtering storage knockout drum (4), plunger pump (5) and pre-heater (6), filter storage knockout drum (4) inside settling chamber and surge chamber of including, the settling chamber with the filter screen has vertically been placed between the surge chamber, the settling chamber is used for receiving oil base cutting waste liquid and carries out the sedimentation separation with its impurity, the filter screen is used for filtering the material that density is not more than the density of water, the surge chamber is used for placing the oil base cutting waste liquid after filtering, the oil base cutting waste liquid of surge chamber is gone into in pre-heater (6) that are connected with plunger pump (5) through plunger pump (5) that are connected with the surge chamber, pre-heater (6) are used for heating oil base cutting waste liquid.
3. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 2, wherein: the oil-based cutting waste liquid reaction subsystem comprises a supercritical reactor (7), an air inflating pump (1) and air purifying equipment (2), the air inflator pump (1) is used for sucking air and compressing the air, the air inlet (702) of the air purification device (2) is connected with the air outlet of the air inflator pump (1) through a first gas pipeline (23), the air outlet of the air purification device (2) is connected with the air inlet (702) of the supercritical reactor (7), the cutting waste liquid outlet of the preheater (6) is connected with the cutting waste liquid inlet of the supercritical reactor (7), the supercritical reactor (7) is used for carrying out heat and mass transfer reaction on the cutting waste liquid and the purified air, and a salt discharge outlet is formed in the bottom of the supercritical reactor (7), and a first hydraulic salt discharge valve (28) and a second hydraulic salt discharge valve (29) are arranged at the salt discharge outlet.
4. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 3, wherein: the cooling and pressure reducing subsystem comprises a condenser (11), a pressure reducing valve (12), a static mixer (17), a gas-liquid separation tank (14), a tap water tank (9) and a water feeding pump (10); a water outlet in the tap water tank (9) is connected with a water inlet of the condenser (11) through a water feeding pump (10), a gas inlet of the condenser (11) is connected with a gas outlet of the supercritical reactor (7), and a gas outlet of the condenser (11) is connected to a gas inlet of a static mixer (17) through a reducing valve (12); the water outlet of the condenser (11) is connected to the gas-liquid separation tank (14) through a first water flowing pipeline (26), the water outlet of the gas-liquid separation tank (14) is connected to the water inlet of the tap water tank (9) through a second water flowing pipeline (25), and the air outlet of the gas-liquid separation tank (14) is used for discharging water vapor.
5. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 4, wherein: the alkali liquor preparation conveying subsystem comprises an alkali liquor box (15) and an alkali liquor pump (16), a water inlet of the alkali liquor box (15) is connected to a second water running pipeline (25), a lime inlet is further formed in the alkali liquor box (15), a water outlet of the alkali liquor box (15) is connected to an alkali liquor inlet (701) of a supercritical reactor (7) through an alkali liquor pipeline (22), the alkali liquor pipeline (22) is provided with the alkali liquor pump (16) for pumping alkali liquor into the supercritical reactor (7) from the alkali liquor box (15), and an alkali liquor pipeline branch (27) connected to a static mixer (17) is arranged on the alkali liquor pipeline (22).
6. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 5, wherein: the nitrous oxide purification subsystem comprises a high-pressure gas-liquid separator (13), a drying tower (18), an adsorption tower (19), a refrigerant and a low-temperature separation tank (21); high pressure vapour and liquid separator (13) with static mixer (17) are connected, seted up the raffinate discharge port on high pressure vapour and liquid separator (13), the gas outlet on high pressure vapour and liquid separator (13) is connected to the gas inlet of drying tower (18), the gas outlet of drying tower (18) is connected to the gas inlet of adsorption tower (19), the gas outlet of adsorption tower (19) is connected to the gas inlet of refrigerator (20), refrigerator (20) are connected with low temperature separation jar (21).
7. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 2, wherein: the oil-based cutting waste liquid pretreatment subsystem further comprises a heating furnace (3), wherein a gas outlet of the heating furnace (3) is connected with a gas inlet of the preheater (6) through a second gas pipeline (24), a valve is arranged on the second gas pipeline (24), and the plunger pump (5) is an anti-corrosion plunger pump (5).
8. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 4, wherein: the condenser (11) is a U-shaped tubular heat exchanger or a floating head heat exchanger.
9. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 3, wherein: the device is characterized in that a pipeline at an air inlet (702) on the supercritical reactor (7) is tangentially arranged with the supercritical reactor (7), a pipeline at a cutting waste liquid inlet is radially arranged with the supercritical reactor (7), an insulating layer (703) is further arranged on the outer wall of the supercritical reactor (7), and a salt separation device (704) is arranged at the lower part of the supercritical reactor (7).
10. The supercritical water oxidation technology-based oil-based cutting waste liquid treatment and separation system according to claim 9, wherein: salt separator (704) are the structure of upper portion cone lower part back taper body, first hydraulic pressure arrange salt valve (28) with be provided with salt buffer tank (8) between second hydraulic pressure arrange salt valve (29).
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