CN112320920A - Supercritical water oxidation treatment system for organic waste liquid - Google Patents
Supercritical water oxidation treatment system for organic waste liquid Download PDFInfo
- Publication number
- CN112320920A CN112320920A CN202011136317.XA CN202011136317A CN112320920A CN 112320920 A CN112320920 A CN 112320920A CN 202011136317 A CN202011136317 A CN 202011136317A CN 112320920 A CN112320920 A CN 112320920A
- Authority
- CN
- China
- Prior art keywords
- organic waste
- waste liquid
- reactor
- tank
- hydrogen peroxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/21—Dissolved organic carbon [DOC]
Abstract
The invention provides a supercritical water oxidation treatment system for organic waste liquid, which comprises an organic waste liquid tank, an organic waste liquid pump, a primary hydrogen peroxide tank, a primary hydrogen peroxide pump and a preheater which are sequentially connected, wherein the organic waste liquid pump and the preheater are connected with a kettle-type reactor through a first three-way valve; the material of the kettle type reactor is stainless steel, and the material of the coil of the tubular reactor is 625 alloy, Hastelloy C276 or noble metal platinum. The invention not only solves the problem of high cost of the kettle type reactor used independently, but also solves the problem of easy blockage caused by the use of the tubular reactor used independently.
Description
Technical Field
The invention relates to the technical field of high-concentration organic waste liquid treatment, in particular to a supercritical water oxidation treatment system for organic waste liquid.
Background
Supercritical water (SCW) refers to water in a particular state at a temperature and pressure above the thermodynamic critical point of water (374.3 ℃ and 22.1 MPa). In this state, liquid and gas coexist, and water becomes an excellent nonpolar solvent for the organic molecule and the oxidizing agent.
Supercritical water oxidation technology (SCWO) takes advantage of the unique physicochemical properties of supercritical water, such as high diffusivity, low viscosity, zero surface tension, controllable dielectric constant, low hydrogen bonding effect and excellent miscibility with organic waste and oxygen. When the water temperature and the pressure are higher than the critical point, even the long carbon chains and the aromatic rings can be rapidly degraded, organic matters can be effectively degraded, secondary pollution can not be generated, and the removal rate of the organic matters by the supercritical water oxidation method reaches more than 99%.
SCWO has the advantages of high treatment efficiency, thorough degradation of organic matters and the like, and belongs to the development direction of green chemistry. However, the industrial application thereof has many difficulties, and thus the organic wastewater treatment technology has not become the mainstream. The main problems are shown in that:
(1) at normal temperature, water is an excellent solvent for most salts, and the solubility can reach 100 g/L. Most of the salts have low solubility in supercritical water of low density. During the reaction, the salt tends to adhere to the inner wall of the reactor and gradually forms a salt layer there, reducing the heat transfer capacity of the entire reactor wall. Secondly, a micro-electrolysis environment is easily formed between the salt layer and the inner wall of the reactor, so that severe corrosion occurs. Third, the accumulation of precipitated salts can also lead to increased system pressure and plugging of reactors, piping.
(2) The problem of equipment corrosion exists in the operation process of the supercritical water oxidation system, and the popularization and the application of the technology are seriously restricted. Since conventional stainless steel materials are severely corroded in supercritical water, alloy 625, hastelloy C276, noble metal platinum and the like are generally used as materials of a reactor in the industry, and the materials have good corrosion resistance in supercritical water, but the price of the materials is high.
In summary, for a supercritical water oxidation reaction (SCWO) system, a single reactor is generally adopted, the maximum operating temperature of the tank reactor is about 600 ℃, the material is 625 alloy, the manufacturing cost of the reactor is high, the inner diameter of the tubular reactor is small, and inorganic salt blockage is easily caused. The problems of salt deposition and material corrosion during supercritical water oxidation significantly reduce the reliability and economics of SCWO plants.
Therefore, in the research and development of a supercritical water oxidation treatment system for organic waste liquid, the problems of high system cost caused by material corrosion and blockage caused by salt deposition need to be solved.
Disclosure of Invention
The invention aims to provide a supercritical water oxidation treatment system for organic waste liquid, thereby solving the problem of blockage and reducing the investment cost.
In order to achieve the purpose, the invention provides a supercritical water oxidation treatment system for organic waste liquid, which comprises an organic waste liquid tank and an organic waste liquid pump which are sequentially connected along the direction of a pipeline, and a primary hydrogen peroxide tank, a primary hydrogen peroxide pump and a preheater which are sequentially connected along the direction of the pipeline, wherein the organic waste liquid pump and the preheater are connected with a kettle-type reactor through a first three-way valve; the material of the kettle type reactor is stainless steel, and the material of the coil of the tubular reactor is 625 alloy, Hastelloy C276 or noble metal platinum.
The organic waste liquid tank is internally stored with organic waste liquid, the first-stage hydrogen peroxide tank and the second-stage hydrogen peroxide tank are internally provided with oxidants, the organic waste liquid tank is connected with an inlet of the organic waste liquid pump through a Y-shaped filter, a first one-way valve and a first manual valve are arranged between the organic waste liquid pump and the first three-way valve, a second one-way valve and a second manual valve are arranged between the first-stage hydrogen peroxide tank and the inlet of the first-stage hydrogen peroxide pump, and a third one-way valve and a fourth manual valve are arranged between an outlet of the second-stage hydrogen peroxide pump and the three-way valve.
A first online mixer is arranged between the first three-way valve and the kettle type reactor, and the first online mixer is made of stainless steel; and a second online mixer is arranged between the second three-way valve and the tubular reactor, and the material of the second online mixer is 625 alloy, Hastelloy C276 or noble metal platinum.
And a pressure safety valve is arranged between the first online mixer and the kettle type reactor, and an outlet of the pressure safety valve is connected with the organic waste liquid tank.
A preheater heating module is arranged around the preheater, temperature detectors are arranged inside the preheater and inside the preheater heating module, and a pressure detector is arranged inside the preheater; the device comprises a kettle type reactor, and is characterized in that kettle type reactor heating modules are arranged on the periphery of the upper middle part of the kettle type reactor, a temperature detector and a pressure detector are arranged in the kettle type reactor, the temperature detector in the kettle type reactor is a multi-point temperature detector, the kettle type reactor heating modules are provided with a temperature detector, and the bottom of the kettle type reactor is connected with a salt discharge tank.
The inner wall of the kettle type reactor is coated with a layer of corrosion-resistant nickel-based alloy through laser cladding.
The supercritical water oxidation treatment system of the organic waste liquid also comprises a primary heat exchanger and a secondary heat exchanger, wherein the shell side of the primary heat exchanger is connected between the primary hydrogen peroxide pump and the preheater, and the tube side of the primary heat exchanger and the tube side of the secondary heat exchanger are sequentially connected between the tube reactor and the gas-liquid separator from the tube reactor; the material of the internal heat transfer pipe of the primary heat exchanger is 625 alloy, Hastelloy C276 or noble metal platinum, the material of the shell is stainless steel, and the material of the internal heat transfer pipe of the secondary heat exchanger and the material of the shell are both stainless steel.
And the outlet of the tube side of the secondary heat exchanger is connected with the inlet of the gas-liquid separator through a back pressure valve, the back pressure valve is connected with a gas cylinder, and the size of the opening of the back pressure valve is adjusted through compressed air in the gas cylinder.
And a temperature detector and a pressure detector are respectively arranged at the upstream and downstream of the back pressure valve.
The temperature in the preheater is 250-350 ℃, the internal temperature of the middle upper part of the kettle reactor is about 400-500 ℃, a coil of the tubular reactor is arranged in a high-temperature box type resistance furnace, and the temperature of the high-temperature box type resistance furnace is 500-700 ℃ during normal work; the temperature of the shell side outlet of the primary heat exchanger is 180-220 ℃, and the temperature of the tube side outlet of the primary heat exchanger is 280-320 ℃.
The supercritical water oxidation treatment system of the organic waste liquid combines the kettle reactor and the tubular reactor together, adopts stainless steel materials to reduce the cost of the kettle reactor, and adopts the tubular reactor made of 625 alloy or Ha's C276 or noble metal platinum materials to ensure that the total manufacturing cost is far lower than that of the kettle reactor made of 625 alloy or Ha's C276 or noble metal platinum materials; in addition, the circulating coolers are arranged around the bottom of the kettle type reactor, so that the temperature of the bottom of the reactor can be reduced to 300 ℃ to dissolve inorganic salt separated out in the reaction process, and the organic matters which are subjected to salt removal and incomplete oxidation by the kettle type reactor are further subjected to thorough oxidation treatment by the tubular reactor. Therefore, the problem of high cost of the independent kettle type reactor is solved, and the problem of easy blockage caused by the independent tubular reactor is also solved. In addition, the oxidant is injected in two steps, so that the removal rate of organic matters can be improved, and the consumption of the oxidant can be reduced.
Drawings
Fig. 1 is a connection structure diagram of a supercritical water oxidation treatment system of an organic waste liquid according to an embodiment of the present invention;
in the figure, 1-organic waste liquid tank, 2-organic waste liquid pump, 3-primary hydrogen peroxide tank, 4-primary hydrogen peroxide pump, 5-primary heat exchanger, 6-preheater, 61-preheater heating module, 7-kettle reactor, 71-kettle reactor heating module, 72-circulating cooler, 8-primary water cooler, 9-salt discharging tank, 10-secondary hydrogen peroxide tank, 11-secondary hydrogen peroxide pump, 12-tubular reactor, 121-high temperature box-type resistance furnace, 122-coil, 13-secondary heat exchanger, 14-secondary water cooler, 15-gas cylinder, 16-gas-liquid separator, 17-liquid collecting tank, 18-tail gas absorber; Y1-Y type filter; d1 — first check valve; d2 — a second one-way valve; d3-a third one-way valve; s1-first manual valve; s2-a second manual valve; s3-a third manual valve; s4-a fourth manual valve; f1 — first three-way valve; f2 — a second three-way valve; h1 — first in-line mixer; h2 — second in-line mixer; a1-pressure safety valve; b1-backpressure valve; a PI-pressure detector; TI-temperature probe; VOC-volatile organic concentration detector.
Detailed Description
The present invention will be further described with reference to the following specific examples. It should be understood that the following examples are illustrative only and are not intended to limit the scope of the present invention.
Fig. 1 shows a supercritical water oxidation treatment system for organic waste liquid according to one embodiment of the present invention, which comprises an organic waste liquid tank 1 and an organic waste liquid pump 2 connected in sequence along the direction of a pipeline, and a primary hydrogen peroxide tank 3, a primary hydrogen peroxide pump 4, the shell side of a primary heat exchanger 5 and a preheater 6 connected in sequence along the direction of a pipeline, wherein the organic waste liquid pump 2 and the preheater 6 are connected to a tank reactor 7 through the same first three-way valve F1. The bottom of the kettle type reactor 7 is connected with a salt discharge tank 9, the top of the kettle type reactor 7, a secondary hydrogen peroxide tank 10 and a secondary hydrogen peroxide pump 11 which are sequentially connected are connected with an inlet of a tubular reactor 12 through a same second three-way valve F2, the tubular reactor 12, the pipe side of the primary heat exchanger 5, the pipe side of the secondary heat exchanger 13 and a gas-liquid separator 16 are sequentially connected, and a liquid phase outlet of the gas-liquid separator 16 is connected with a liquid collection tank 17 and used for discharging oxidized liquid; the gas-phase outlet of the gas-liquid separator 16 is connected to a tail gas adsorber 18, and the purified gas is discharged to the atmosphere.
Wherein, organic waste liquid has been stored in organic waste liquid jar 1, organic waste liquid jar 1 links to each other through the import of a Y type filter Y1 with organic waste liquid pump 2 to make pending organic waste liquid by organic waste liquid jar 1 through Y type filter Y1 entering organic waste liquid pump 2, Y type filter Y1 is arranged in driving away the particulate matter impurity in the organic waste liquid, organic waste liquid pump 2 is the high pressure plunger metering pump, can provide flow and pressure for follow-up supercritical water oxidation reaction, and can show in real time and adjust the flow.
Because the first-stage hydrogen peroxide tank 3 is connected with the inlet of the first-stage hydrogen peroxide pump 4, the first-stage hydrogen peroxide tank 3 and the second-stage hydrogen peroxide tank 10 are internally provided with an oxidant, the preferred mass fraction of the oxidant is 30% hydrogen peroxide, and therefore the oxidant enters the inlet of the first-stage hydrogen peroxide pump 4 from the first-stage hydrogen peroxide tank 3. A second one-way valve D2 and a second manual valve S2 are arranged between the primary hydrogen peroxide tank 3 and the inlet of the primary hydrogen peroxide pump 4. The primary hydrogen peroxide pump 4 is preferably a high-pressure plunger metering pump, can provide flow and pressure for subsequent supercritical water oxidation reaction, and can display and adjust the flow in real time. The outlet of the primary hydrogen peroxide pump 4 is connected with the inlet of the shell side of the primary heat exchanger 5, the outlet of the shell side of the primary heat exchanger 5 is communicated with the inlet of the preheater 6, therefore, the oxidant absorbs the heat of the fluid at the outlet of the tubular reactor 12 through the primary heat exchanger 5, the temperature of the outlet of the shell side of the primary heat exchanger 5 reaches about 200 ℃ (180 ℃ -220 ℃), and the energy consumption of the subsequent preheater 6 can be reduced.
A preheater heating module 61 is arranged on the periphery of the preheater 6, temperature detectors TI are arranged inside the preheater 6 and inside the preheater heating module 61, and the temperature detectors inside the preheater 6 are used for monitoring the temperature inside the preheater 6; the temperature detector inside the preheater heating module 61 is provided outside the preheater 6 for monitoring the temperature of the preheater heating module 61, and the temperature detector needs to be set respectively because the wall of the preheater 6 is thick and the heat transfer time is different. In addition, a pressure detector PI is arranged in the preheater 6 and used for monitoring the pressure in the preheater 6, the pressure in normal operation is 25Mpa, a preheater heating module 61 temperature detector is used for measuring the temperature of a heating module and controlling the heating power, a preheater 6 internal temperature detector is used for monitoring the internal temperature, the temperature in the preheater 6 in normal operation is 250-350 ℃, namely about 300 ℃, and therefore the temperature of hydrogen peroxide heated by the preheater is 250-350 ℃.
The outlet of the organic waste liquid pump 2 and the outlet of the preheater 6 are connected with the inlet of the tank reactor 7 through the same first three-way valve F1, a first online mixer H1 is arranged between the first three-way valve F1 and the tank reactor 7, and the first online mixer H1 is made of stainless steel, so that the organic waste liquid and the preheated oxidant are mixed into liquid with uniform components and temperature after passing through the first online mixer H1, and the organic waste liquid does not need to be preheated. In this example, the inlet of the tank reactor 7 was disposed at the top center of the tank reactor 7, and the first three-way valve F1 was disposed so that the flow ratio of the organic waste liquid from the organic waste liquid pump 2 to the oxidizer from the preheater 6 was about 1:8 to 1: 15. A pressure safety valve A1 is arranged between the first online mixer H1 and the kettle reactor 7, the outlet of the pressure safety valve A1 is connected with the organic waste liquid tank 1, and the pressure safety valve A1 plays a role in protecting equipment and personal safety. Further, a first check valve D1 and a first manual valve S1 are provided between the organic waste liquid pump 2 and the first three-way valve F1.
The material of the tank reactor 7 is stainless steel, preferably 316 stainless steel, and 306 stainless steel and 304 stainless steel can also be used for replacement; the invention is designed to resist corrosion by adopting a laser cladding method, and the inner wall of the kettle-type reactor 7 is clad with a layer of corrosion-resistant nickel-based alloy by laser. The effective volume is 60-300L, and the method is mainly used for pre-oxidation treatment and desalination. And a kettle type reactor heating module 71 is arranged around the middle upper part of the kettle type reactor 7. A temperature detector TI and a pressure detector PI are arranged inside the kettle reactor 7, wherein the probe of the pressure detector PI is arranged inside the reactor, the temperature detector TI inside the kettle reactor 7 is a multi-point temperature detector, and the temperature of 3 positions of the upper part, the middle part and the lower part inside the kettle reactor 7 can be measured; the kettle-type reactor heating module 71 is provided with a temperature detector TI, and the temperature detector TI of the kettle-type reactor heating module 71 is arranged outside the kettle-type reactor 7 and inside the kettle-type reactor heating module 71 and used for displaying the temperature of the heating module. The pressure in the tank reactor is the organic waste liquid pump 2 described above, the primary hydrogen peroxide pump 4, and the back pressure valve described belowTo be controlled. When the tank reactor 7 is normally operated, the internal temperature of the middle upper part of the tank reactor 7 is about 400 to 500 ℃ and the pressure is about 22 to 30 MPa. At the moment, the fluid in the reaction kettle is in a supercritical state, supercritical water is used as a reaction medium, hydrogen peroxide is used as an oxidant, and the characteristics of the supercritical water enable organic matters, the oxidant and water to form a uniform phase, so that the mass transfer resistance among phases is overcome, the oxidation rate of the organic matters is greatly improved at high temperature and high pressure, and the hydrocarbon in the organic waste liquid can be oxidized into CO within seconds2And H2O, conversion of hetero atoms to inorganic compounds, e.g. P to phosphate, S to sulfate, N to N2Or N2And O. The overall oxidation of organic waste water containing heteroatoms such as S, P and Cl results in acidic solutions or the production of some inorganic salts in the presence of basic compounds. In order to reduce the corrosion of the reactor caused by the contact with the acidic solution to the maximum extent, the alkaline solution can be manually added into the hydrogen peroxide tank, so that the alkaline solution is conveyed to the kettle-type reactor through the hydrogen peroxide pump, and then the acidic solution is neutralized by the alkaline solution, so that a large amount of salts are generated, and the solubility of the salts in supercritical water is extremely low. The bottom of the kettle-type reactor 7 is provided with a circulating cooler 72 all around, the inlet of the circulating cooler 72 is connected with the outlet of the primary water cooler 8, the outlet of the circulating cooler 72 is connected with the inlet of the primary water cooler 8, so that a first cooling loop is formed, and a manual valve can be arranged in the first cooling loop. Thus, under the action of the first cooling loop formed by the circulation cooler 72 and the primary water cooler 8, the temperature of the bottom of the tank reactor 7 is 250-350 ℃, the temperature is in a subcritical state, and the inorganic salt is dissolved in subcritical water again. The bottom of the kettle type reactor 7 is provided with a third manual valve S3 and is connected with the salt discharge tank 9 through a third manual valve S3 and a discharge pipeline for discharging inorganic salt dissolved in subcritical water.
The second-stage hydrogen peroxide tank 10 is directly connected with the inlet of the second-stage hydrogen peroxide pump 11, and the outlet of the second-stage hydrogen peroxide pump 11 and the outlet of the top edge of the kettle reactor 7 are connected with the inlet of the tubular reactor 12 through the same second three-way valve F2. Wherein, a third one-way valve D3 and a fourth manual valve S4 are arranged between the outlet of the second-stage hydrogen peroxide pump 11 and the three-way valve.
A second online mixer H2 is arranged between the second three-way valve F2 and the tubular reactor 12, so that the pre-oxidized fluid and hydrogen peroxide are mixed and then enter the tubular reactor 12, and the material of the second online mixer H2 is 625 alloy, Hastelloy C276 or noble metal platinum. The second-stage hydrogen peroxide pump 11 is a high-pressure plunger metering pump, can provide flow and pressure for subsequent supercritical water oxidation reaction, and can display and adjust the flow in real time.
The tubular reactor 12 comprises a high-temperature box-type resistance furnace 121 and coils 122 arranged inside the high-temperature box-type resistance furnace 121, wherein the coils 122 are made of 625 alloy, Hastelloy C276 or noble metal platinum. The temperature of the high-temperature box-type resistance furnace 121 during normal operation is set to 500 to 700 ℃, in this embodiment, 600 ℃, so that the incompletely oxidized organic substances further undergo supercritical water oxidation reaction in the coil 122. The tube side inlet of the primary heat exchanger 5 is connected with the outlet of the tubular reactor 12, and the tube side outlet of the primary heat exchanger is connected with the tube side inlet of the secondary heat exchanger 13; the shell side inlet of the secondary heat exchanger 13 is connected with the outlet of the secondary water cooler 14, and the shell side outlet thereof is connected with the inlet of the secondary water cooler 14. The shell side inlet of the secondary heat exchanger 13 is connected with the outlet of the secondary water cooler 14, and the shell side outlet of the secondary heat exchanger is connected with the inlet of the secondary water cooler 14. The material of the internal heat transfer pipe of the primary heat exchanger 5 is 625 alloy, hastelloy C276 or noble metal platinum, the material of the shell is 304 stainless steel, 306 stainless steel or 316 stainless steel, and the material of the internal heat transfer pipe of the secondary heat exchanger 13 and the material of the shell are 304 stainless steel, 306 stainless steel or 316 stainless steel.
Therefore, the temperature of the effluent of the tubular reactor 12 is about 600 ℃, after the effluent passes through the primary heat exchanger 5, the temperature of the outlet of the tube side of the primary heat exchanger 5 is reduced to about 300 ℃ (280 ℃ -320 ℃), the secondary water cooler 14 is used for cooling the secondary heat exchanger 13, and the temperature of the effluent is reduced to 40 ℃ after the effluent passes through the secondary heat exchanger 13.
The outlet of the tube side of the secondary heat exchanger 13 is connected with the inlet of the gas-liquid separator 16 through a back pressure valve B1, a back pressure valve B1 is connected with a gas cylinder 15, the size of the opening of the back pressure valve B1 is adjusted through compressed air in the gas cylinder 15, so that the pressure at the upstream of the back pressure valve B1 is controlled, the pressure in the whole system including a sample pump, a primary heat exchanger, a preheater, a kettle reactor, a tubular reactor, a secondary heat exchanger and the like is kept at a set value of 25MPa and can be 20-30MPa in other embodiments, a temperature detector TI and a pressure detector PI are respectively arranged at the upstream and the downstream of the back pressure valve B1, and the temperature detector TI is used for monitoring the temperature of the fluid to ensure that the temperature of the fluid is within the allowable range of the back pressure valve B36; the pressure detector PI is used for monitoring the pressure at the rear end of the backpressure valve B1, and the pressure value of the fluid after being reduced through the backpressure valve B1 is obtained.
A liquid phase outlet of the gas-liquid separator 16 is connected with a liquid collecting tank 17 and used for discharging oxidized liquid; the gas-phase outlet of the gas-liquid separator 16 is connected to a tail gas adsorber 18. The outlet of the tail gas adsorber 18 is provided with a Volatile Organic Compound (VOC) concentration detector, and when the concentration is higher than the emission standard, the automatic alarm reminding is carried out. In this embodiment, the supercritical water oxidation treatment system for organic waste liquid is a pilot plant.
The above embodiments are merely preferred embodiments of the present invention, which are not intended to limit the scope of the present invention, and various changes may be made in the above embodiments of the present invention. All simple and equivalent changes and modifications made according to the claims and the content of the specification of the present application fall within the scope of the claims of the present patent application. The invention has not been described in detail in order to avoid obscuring the invention.
Claims (10)
1. A supercritical water oxidation treatment system for organic waste liquid is characterized by comprising an organic waste liquid tank (1) and an organic waste liquid pump (2) which are sequentially connected along the direction of a pipeline, and a primary hydrogen peroxide tank (3), a primary hydrogen peroxide pump (4) and a preheater (6) which are sequentially connected along the direction of the pipeline, wherein the organic waste liquid pump (2) and the preheater (6) are connected with a kettle-type reactor (7) through a first three-way valve (F1), a circulating cooler (72) is arranged around the bottom of the kettle-type reactor (7), the top of the kettle-type reactor (7) and a secondary hydrogen peroxide tank (10) and a secondary hydrogen peroxide pump (11) which are sequentially connected are connected with the inlet of a tubular reactor (12) through a second three-way valve (F2), the tubular reactor (12) is connected with a gas-liquid separator (16), the liquid phase outlet of the gas-liquid separator (16) is connected with a liquid collecting tank (17), the gas phase outlet of the tail gas adsorber is connected with a tail gas adsorber (18); the material of the tank reactor (7) is stainless steel, and the material of the coil (122) of the tubular reactor (12) is 625 alloy, Hastelloy C276 or noble metal platinum.
2. The supercritical water oxidation treatment system for organic waste liquid according to claim 1, wherein organic waste liquid is stored in the organic waste liquid tank (1), the primary hydrogen peroxide tank (3) and the secondary hydrogen peroxide tank (10) contain oxidant, the organic waste liquid tank (1) is connected with the inlet of the organic waste liquid pump (2) through a Y-type filter (Y1), a first check valve (D1) and a first manual valve (S1) are arranged between the organic waste liquid pump (2) and the first three-way valve (F1), a second check valve (D2) and a second manual valve (S2) are arranged between the primary hydrogen peroxide tank (3) and the inlet of the primary hydrogen peroxide pump (4), and a third check valve (D3) and a fourth manual valve (S4) are arranged between the outlet of the secondary hydrogen peroxide pump (11) and the three-way valve.
3. The supercritical water oxidation treatment system for organic waste liquid according to claim 1, characterized in that a first online mixer (H1) is provided between the first three-way valve (F1) and the tank reactor (7), and the first online mixer (H1) is made of stainless steel; a second on-line mixer (H2) is arranged between the second three-way valve (F2) and the tubular reactor (12), and the material of the second on-line mixer (H2) is 625 alloy, Hastelloy C276 or noble metal platinum.
4. Supercritical water oxidation treatment system for organic waste liquid according to claim 3, characterized in that a pressure relief valve (A1) is provided between the first online mixer (H1) and the tank reactor (7), and the outlet of the pressure relief valve (A1) is connected to the organic waste liquid tank (1).
5. The supercritical water oxidation treatment system for organic waste liquid according to claim 1, wherein a preheater heating module (61) is provided around the preheater (6), a temperature detector (TI) is provided inside the preheater (6) and inside the preheater heating module (61), and a pressure detector (PI) is provided inside the preheater (6);
kettle-type reactor heating module (71) is equipped with all around of upper portion in kettle-type reactor (7), and the inside of kettle-type reactor (7) is equipped with a temperature detector (TI) and a pressure detector (PI), and temperature detector (TI) of the inside of kettle-type reactor (7) is multi-point temperature detector, and kettle-type reactor heating module (71) is equipped with a temperature detector (TI), the bottom of kettle-type reactor (7) links to each other with salt discharging tank (9).
6. Supercritical water oxidation treatment system of organic waste liquid according to claim 5, characterized in that the inner wall of the tank reactor (7) is laser clad with a layer of corrosion resistant nickel based alloy.
7. The supercritical water oxidation treatment system for organic waste liquid according to claim 1, further comprising a primary heat exchanger (5) and a secondary heat exchanger (13), wherein the shell side of the primary heat exchanger (5) is connected between the primary hydrogen peroxide pump (4) and the preheater (6), and the tube side of the primary heat exchanger (5) and the tube side of the secondary heat exchanger (13) are connected between the tube reactor (12) and the gas-liquid separator (16) in this order from the tube reactor (12); the material of the internal heat transfer pipe of the primary heat exchanger (5) is 625 alloy, Hastelloy C276 or noble metal platinum, the material of the shell is stainless steel, and the material of the internal heat transfer pipe of the secondary heat exchanger (13) and the material of the shell are both stainless steel.
8. Supercritical water oxidation treatment system for organic waste liquid according to claim 7, characterized in that the tube side outlet of the secondary heat exchanger (13) is connected to the inlet of the gas-liquid separator (16) via a back pressure valve (B1), the back pressure valve (B1) is connected to a gas cylinder (15), and the size of the opening of the back pressure valve (B1) is adjusted by the compressed air in the gas cylinder (15).
9. Supercritical water oxidation treatment system of organic waste liquid according to claim 8, characterized in that upstream and downstream of the back pressure valve (B1) are provided with a temperature detector (TI) and a pressure detector (PI), respectively.
10. The supercritical water oxidation treatment system for organic waste liquid according to claim 7, wherein the temperature in the preheater (6) is 250 to 350 ℃, the internal temperature of the middle upper part of the tank reactor (7) is about 400 to 500 ℃, the coil (122) of the tubular reactor (12) is arranged in a high temperature box type resistance furnace (121), and the temperature of the high temperature box type resistance furnace (121) is 500 to 700 ℃ during normal operation; the temperature of the shell side outlet of the primary heat exchanger (5) is 180-220 ℃, and the temperature of the tube side outlet of the primary heat exchanger (5) is 280-320 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011136317.XA CN112320920A (en) | 2020-10-22 | 2020-10-22 | Supercritical water oxidation treatment system for organic waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011136317.XA CN112320920A (en) | 2020-10-22 | 2020-10-22 | Supercritical water oxidation treatment system for organic waste liquid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112320920A true CN112320920A (en) | 2021-02-05 |
Family
ID=74312041
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011136317.XA Pending CN112320920A (en) | 2020-10-22 | 2020-10-22 | Supercritical water oxidation treatment system for organic waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112320920A (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020070179A1 (en) * | 2000-12-09 | 2002-06-13 | Stephan Pilz | Process and device for supercritical wet oxidation |
| US6551517B1 (en) * | 1998-07-10 | 2003-04-22 | L'electrolyse | Method for transforming chemical structures in a fluid under pressure and in high temperature |
| CN101993143A (en) * | 2010-10-27 | 2011-03-30 | 南京工业大学 | System and method for processing alkaline residue wastewater by utilizing supercritical water oxidation method |
| CN103508605A (en) * | 2013-09-30 | 2014-01-15 | 西安交通大学 | Supercritical water oxidation treatment system of high-salt content corrosive organic wastewater |
| CN108751653A (en) * | 2018-06-19 | 2018-11-06 | 西安交通大学 | A kind of municipal sludge supercritical water oxidation staged oxidation processing system and technique |
| CN109231421A (en) * | 2018-11-09 | 2019-01-18 | 江苏省环境科学研究院 | Multifunctional continuous hydrothermal oxidization experimental system and its application method |
-
2020
- 2020-10-22 CN CN202011136317.XA patent/CN112320920A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6551517B1 (en) * | 1998-07-10 | 2003-04-22 | L'electrolyse | Method for transforming chemical structures in a fluid under pressure and in high temperature |
| US20020070179A1 (en) * | 2000-12-09 | 2002-06-13 | Stephan Pilz | Process and device for supercritical wet oxidation |
| CN101993143A (en) * | 2010-10-27 | 2011-03-30 | 南京工业大学 | System and method for processing alkaline residue wastewater by utilizing supercritical water oxidation method |
| CN103508605A (en) * | 2013-09-30 | 2014-01-15 | 西安交通大学 | Supercritical water oxidation treatment system of high-salt content corrosive organic wastewater |
| CN108751653A (en) * | 2018-06-19 | 2018-11-06 | 西安交通大学 | A kind of municipal sludge supercritical water oxidation staged oxidation processing system and technique |
| CN109231421A (en) * | 2018-11-09 | 2019-01-18 | 江苏省环境科学研究院 | Multifunctional continuous hydrothermal oxidization experimental system and its application method |
Non-Patent Citations (1)
| Title |
|---|
| 汪多仁: "《绿色净水处理剂》", 30 November 2006, 科学技术文献出版社 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102249461B (en) | Supercritical water oxidation treatment system for high-salt high-chlorine organic wastewater | |
| AU656995B2 (en) | Supercritical water oxidation process and apparatus of organics with inorganics | |
| Li et al. | Novel designs for the reliability and safety of supercritical water oxidation process for sludge treatment | |
| CN109319916A (en) | It is a kind of can long-period stable operation continuous supercritical water oxidative system | |
| CN101928080B (en) | Supercritical water oxidation treatment method for high-concentration organic wastewater | |
| Veriansyah et al. | Destruction of chemical agent simulants in a supercritical water oxidation bench-scale reactor | |
| CN103508605B (en) | Supercritical water oxidation treatment system of high-salt content corrosive organic wastewater | |
| CN102642947A (en) | Supercritical water oxidization treatment system for high-salinity organic waste water | |
| CN105601017A (en) | Near zero emission treatment system and method for high-concentration organic wastewater and sludge | |
| CN109231421B (en) | Multifunctional continuous hydrothermal oxidation experimental system and application method thereof | |
| CN109320014B (en) | Nitrogen-containing organic matter staged treatment system and method based on supercritical water oxidation reaction | |
| CN114838369B (en) | Inorganic salt online desorption system and method based on supercritical hydrothermal combustion treatment | |
| CN110642362B (en) | Supercritical water reactor integrating material preheating, pollutant multistage enhanced degradation, corrosion prevention and control functions | |
| CN204251405U (en) | A kind of Novel supercritical Water oxidize total system | |
| CN112320920A (en) | Supercritical water oxidation treatment system for organic waste liquid | |
| CN111417598B (en) | System and method for treating high-salinity high-organic wastewater and recycling energy | |
| CN201158601Y (en) | System for treating carbonized wastewater or organic waste water with supercritical water oxidization technique | |
| CN112300033A (en) | Device and method for fully and continuously synthesizing 2-nitro-4-methylsulfonylbenzoic acid from 4-methylsulfonyltoluene | |
| CN111781130B (en) | Flowing corrosion-salt deposition online test system and method used in supercritical water treatment environment | |
| CN205442756U (en) | Indirect heat exchange type supercritical water oxidation system of organic waste liquid and mud | |
| CN114890532A (en) | Spiral casing pipe reactor and micro-channel wet oxidation system | |
| CN110963557A (en) | Salt-containing wastewater treatment system and treatment method | |
| CN212864254U (en) | Organic waste water liquid phase catalytic oxidation processing system | |
| CN205442678U (en) | Inhibition type supercritical water oxidization reaction goes out water cooling deaerating plant | |
| CN2892837Y (en) | High-concentration industrial waste water processing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20210205 |
|
| WD01 | Invention patent application deemed withdrawn after publication |