CN212741101U

CN212741101U - Continuous supercritical water oxidation system for treating oily sludge

Info

Publication number: CN212741101U
Application number: CN202022035518.2U
Authority: CN
Inventors: 胡德栋; 杨桑宇; 韩俊杰; 谭富庭
Original assignee: Qingdao University of Science and Technology
Current assignee: Qingdao University of Science and Technology
Priority date: 2020-09-17
Filing date: 2020-09-17
Publication date: 2021-03-19
Anticipated expiration: 2030-09-17

Abstract

The utility model provides a continuous supercritical water oxidation system for handling oily sludge, including muddy water mixed feed system, supercritical oxidation system, energy recuperation system. When the whole system is initially started, the heat of the glow plug is utilized to ignite the fuel in the reaction inclined tube, a fuel preheater is not needed, the organic waste liquid is quickly preheated and efficiently degraded, and the investment and the energy consumption of equipment are reduced. And the mixing of the oil sludge and the clean water/organic wastewater and the continuous feeding of the sludge water are realized by adjusting the switches of the first electric ball valve and the second electric ball valve. Muddy water reacts with the non-preheated high-pressure oxidant in the reaction inclined tube, and automatic salt discharge can be realized by adjusting the switches of the third electric ball valve and the fourth electric ball valve, so that salt-containing sewage is avoided, continuous operation and zero emission of the reactor are facilitated, and the requirement of industrial treatment is met.

Description

Continuous supercritical water oxidation system for treating oily sludge

Technical Field

The invention relates to the field of supercritical water oxidation, in particular to a continuous supercritical water oxidation system for treating oily sludge.

Background

The oily sludge is mainly produced in oil fields and oil refineries, and the production amount of the oily sludge is 0.5 to 1 percent of the crude oil yield by taking the petroleum exploration and development industry as an example. According to the current estimation of crude oil yield in China, nearly millions of tons of oil sludge and oil sand are generated every year, and if three kinds of sludge generated by petrochemical industry are added, the total amount is much larger. The oily sludge entering surface soil and water will cause serious pollution problems and therefore needs to be effectively treated before being discharged.

At present, the treatment of the oil sludge has few literature reports, the method mainly adopted is still an incineration method, but a dust removal and gas recovery device is required to be arranged during incineration, otherwise serious air pollution is generated. In addition, a low-temperature pyrolysis method, a dissolving and washing method and a microbial treatment method are also provided, but the two methods are complex in process and generate secondary pollution to the environment, and the microbes have certain selectivity to oil products, are harsh in application conditions and are not mature at present.

The supercritical water oxidation (SCWO) technology is characterized in that supercritical water is used as a reaction medium, and air and O are used at the temperature of 400-600 ℃ under the pressure of 23-30 MPa₂Or H₂O₂As an oxidant, degrading organic matter to harmless CO₂、N₂And H₂The SCWO technology is recognized in the united states as the most promising key technology for waste treatment in the energy and environmental fields, and although the application base has been established, some SCWO industrial plants are already available at home and abroad, but the problems of corrosion of the reactor, salt deposition and high operation cost hinder the industrial popularization of the technology.

Patent number is CN 104291546A's supercritical water oxidation unit, can be used to municipal sludge's processing, the main part comprises the inclined tube reactor that the slope was placed and the straight tube separator of perpendicular placement, it mixes back with oxidant and 500 ~ 600 ℃ supercritical water to preheat to 200 ℃ waste material and gets into the pipe chute reaction, be equipped with porous interior bushing pipe in the pipe chute, boundary fluid forms the protection film at the inside surface of lining pipe, avoid solid particle at reactor inner wall deposit, reduce the corruption and the salt deposit of reaction product to the pipe chute, and reduce reaction pipe chute 10-4 inner wall temperature, ensure the safe operation of equipment, reduce the material requirement of equipment. The product is subjected to solid-liquid separation in a separator through gravity settling, and is neutralized and cooled by cooling water, and solid particles at the bottom of the separator are dissolved and discharged. But along with the going on of reaction, the device need constantly let in 500 ~ 600 ℃ supercritical water, has high running cost problem, can produce secondary pollution after solid particle dissolves the discharge moreover, can't realize the zero release, is unfavorable for the continuous operation of device.

At present, in order to solve the problem of preheating materials, a supercritical water oxidation reactor with patent number CN102190363A for supplying heat by using auxiliary fuel is provided with a fuel heating method, wherein the heat required by the reaction is supplied by using the auxiliary fuel, and materials, fuel and an oxidant (air or oxygen) are efficiently mixed by jet flows in different directions so as to improve the oxidation efficiency. However, this device has the problems of difficult ignition of the fuel, the use of a preheater before entering the reactor together with the oxidant, and high running cost.

Disclosure of Invention

Aiming at the problems, the invention provides a continuous supercritical water oxidation system for treating oily sludge, which solves the problems of high operation cost during system material preheating and secondary pollution generated during reactor salt elimination.

The technical scheme of the invention is as follows:

a continuous supercritical water oxidation system for treating oily sludge comprises a sludge-water mixing feeding system, a supercritical oxidation system and an energy recovery system,

the mud-water mixing and feeding system comprises a first booster pump 1, a first one-way valve 2, an injection mixer 3, an oil sludge tank 4, a first electric ball valve 5, a mixing pipe 6, a second electric ball valve 7, a mixing tank 8 and a second one-way valve 9, wherein the oil sludge tank 4 comprises an oil sludge tank body 4-1 and a mud discharge port 4-2, the mixing tank 8 comprises a mixing tank body 8-1, a water inlet 8-2, a water discharge port 8-3 and a mud-water discharge port 8-4,

the inlet of the first booster pump 1 is the inlet of clear water or organic wastewater, the outlet of the first booster pump 1 is connected with the inlet of the first one-way valve 2 through a pipeline, the outlet of the first one-way valve 2 is connected with the working fluid inlet at the left end of the pipeline jet mixer 3, the mixed fluid outlet at the right end of the jet mixer 3 is connected with the water inlet 8-2 of the mixing tank 8 through a pipeline, a sludge discharge port 4-2 of the sludge tank 4 is connected with an inlet of a first electric ball valve 5 through a flange, the outlet of the first electric ball valve 5 is connected with the inlet of a mixing pipe 6 through a flange, the outlet of the mixing pipe 6 is connected with the inlet of a second electric ball valve 7 through a flange, the outlet of the second electric ball valve 7 is connected with a water outlet 8-3 of a mixing tank 8 through a flange, a muddy water discharge port 8-4 of the mixing tank 8 is connected with an inlet of a second one-way valve 9 through a pipeline;

the supercritical water oxidation system consists of an ignition region, a reaction region and a separation region, the core device of the supercritical water oxidation system is a supercritical water oxidation reactor 10, the supercritical water oxidation reactor 10 consists of an inclined tube end cover 10-1, a feed inlet 10-2, a first oxidant inlet 10-3, a reaction inclined tube 10-4, a T-shaped porous lining tube 10-5, an inclined tube boss 10-6, a second oxidant inlet 10-7, a separation straight tube 10-8, a straight tube end cover 10-9, an exhaust port 10-10, a third electric ball valve 10-11, a sludge discharge tube 10-12 and a fourth electric ball valve 10-13,

wherein the ignition region consists of a second booster pump 11, a first stop valve 12, a third one-way valve 13, an inclined tube end cover 10-1, a feed inlet 10-2, an oxidant supercharging device 14, a second stop valve 15, a first oxidant inlet 10-3 and a glow plug 16,

the inlet of the second booster pump 11 is a fuel inlet, the outlet of the second booster pump 11 is connected with the inlet of a first stop valve 12 through a pipeline, the outlet of the first stop valve 12 is connected with the inlet of a third one-way valve 13 through a pipeline, the upper end of an inclined tube end cover 10-1 is provided with a feed inlet 10-2 and a first oxidant inlet 10-3, the outlet of the third one-way valve 13 is connected with the feed inlet 10-2 through a pipeline, the inlet of an oxidant supercharging device 14 is an oxidant inlet, the outlet of the oxidant supercharging device 14 is connected with the inlet of a second stop valve 15, the outlet of the second stop valve 15 is connected with the first oxidant inlet 10-3 through a pipeline, and the glow plug 16 is connected with the center of the inclined tube end cover 10-1 through threads,

the reaction zone consists of a second one-way valve 9, a third one-way valve 13, an inclined tube end cover 10-1, a feed inlet 10-2, an oxidant supercharging device 14, a second stop valve 15, a first oxidant inlet 10-3, a reaction inclined tube 10-4, a T-shaped porous lining tube 10-5, an inclined tube boss 10-6, a third stop valve 17 and a second oxidant inlet 10-7,

the outlet of the second check valve 9 is connected with the outlet of a third check valve 13 in parallel through a pipeline and then is connected with a feed inlet 10-2, the inclined tube end cover 10-1 is arranged at the upper end of a reaction inclined tube 10-4, a T-shaped porous lining tube 10-5 is arranged in the reaction inclined tube 10-4, the upper end of the T-shaped porous lining tube 10-5 is a convex end, an inclined tube boss 10-6 is arranged at the inner side of the reaction inclined tube 10-4 and used for fixing the T-shaped porous lining tube 10-5, the inlet of a third stop valve 17 is connected with the inlet of a second stop valve 15 in parallel through a pipeline and then is connected with an oxidant pressurizing device 14, the outlet of the third stop valve 17 is connected with the inlet of a second oxidant 10-7 through a pipeline,

the separation area consists of a separation straight pipe 10-8, a straight pipe end cover 10-9, an exhaust port 10-10, a third electric ball valve 10-11, a sludge discharge pipe 10-12, a fourth electric ball valve 10-13, a back pressure valve 18 and a flash tank 19,

a straight pipe end cover 10-9 is arranged at the upper end of the separation straight pipe 10-8, an exhaust port 10-10 is arranged at the center of the straight pipe end cover 10-9, the lower end of the separation straight pipe 10-8 is connected with an inlet of a third electric ball valve 10-11 through a flange, an outlet of the third electric ball valve 10-11 is connected with an inlet of a sludge discharge pipe 10-12 through a flange, an outlet of the sludge discharge pipe 10-12 is connected with an inlet of a fourth electric ball valve 10-13 through a flange, an outlet of the fourth electric ball valve 10-13 is connected with an inlet of a back pressure valve 18 through a pipeline, an outlet of the back pressure valve 18 is connected with an inlet of a flash tank 19 through a pipeline, a gas-phase discharge port is arranged at the top;

the reaction inclined tube 10-4 and the separation straight tube 10-8 are welded at a certain inclination angle, the middle part of the separation straight tube 10-8 is provided with an opening for inserting the T-shaped porous lining tube 10-5, and the product in the reaction inclined tube 10-4 is ensured to flow into the separation straight tube 10-8;

the energy recovery system consists of a heat exchanger 20, a gas-liquid separator 21, a buffer tank 22, an expander 23, a generator 24, a fourth one-way valve 25 and an injection mixer 3, the tube side inlet of the heat exchanger 20 is connected with an exhaust port 10-10 of the supercritical water oxidation system through a pipeline, the tube side outlet of the heat exchanger 20 is connected with the inlet of the gas-liquid separator 21 through a pipeline, the shell side fluid of the heat exchanger 20 is cooling water, for producing high-temperature steam, the gas-phase outlet of the gas-liquid separator 21 is connected with the inlet of the buffer tank 22 through a pipeline, the outlet of the buffer tank 22 is connected with the inlet of an expander 23 through a pipeline, the expander 23 is connected with a generator 24 through a transmission shaft, the outlet of the expansion machine 23 is a steam exhaust outlet, the liquid phase outlet of the gas-liquid separator 21 is connected with the inlet of a fourth one-way valve 25 through a pipeline, the outlet of the fourth one-way valve 25 is connected with the injection fluid inlet at the lower end of the injection mixer 3 through a pipeline.

The highest working pressure of each component in an ignition region, a reaction region and a separation region of the supercritical water oxidation system is 30MPa, wherein the highest working temperature of a T-shaped porous lining pipe 10-5 in the reaction region is 1200 ℃, and the highest working temperature of the rest components in the reaction region and the separation region is 700 ℃.

The oxidant pressurizing device 14 is a plunger pump or a compressor.

The T-shaped porous lining pipe 10-5 is made of one of zirconia, alumina and silicon carbide.

The oxidant is selected from air, oxygen, hydrogen peroxide and KClO₃Solution, KMnO₄One of the solutions.

The fuel is selected from one of gasoline, kerosene, methanol and ethanol.

The invention has the advantages that:

1. according to the invention, the fuel in the reaction inclined tube is ignited by using the heat of the heating core of the electric heating plug, so that the temperature in the reaction area quickly meets the reaction requirement, and the quick preheating of the muddy water and the efficient degradation of organic matters in the muddy water are realized;

2. the fuel does not need to be preheated at high temperature in the whole heating process, so that the investment and the energy consumption of equipment are reduced;

3. the continuous mixing of the oil sludge and the clear water/organic wastewater is realized by adjusting the switches of the first electric ball valve and the second electric ball valve at the lower end of the oil sludge tank, and the material requirement of the oil sludge tank is reduced;

4. the automatic muddy water of the reactor can be realized by adjusting the switches of the third electric ball valve and the fourth electric ball valve at the lower end of the separation straight pipe, the sewage generated when cooling by adopting cooling water is avoided, zero emission is realized, the continuous operation of the reactor is facilitated, and the requirement of industrial treatment is met;

5. the energy of the reaction product is fully utilized, the heat energy of the reaction product is used for preheating muddy water, the pressure energy is used for the work of the expansion machine for power generation, the generated electric quantity can be supplied for the operation of the first booster pump, the second booster pump and the oxidant booster device, and the operation cost of the system is reduced.

Drawings

FIG. 1 is a schematic structural diagram of the continuous supercritical water oxidation system for treating oily sludge.

FIG. 2 is a schematic diagram showing the structure of a muddy water feeding process in the muddy water mixing and feeding system.

FIG. 3 is a schematic structural view of a sludge-water sedimentation process in the sludge-water mixing and feeding system.

FIG. 4 is a schematic view showing the structure of a sludge water deposition process in the reactor.

FIG. 5 is a schematic view showing the structure of a sludge water discharge process in the reactor.

In the figure: 1. a first booster pump; 2. a first check valve; 3. a jet mixer; 4. a sludge tank; 4-1, an oil sludge tank body; 4-2, a sludge discharge port; 5. a first electrically powered ball valve; 6. a mixing tube; 7. a second electrically operated ball valve; 8. a mixing tank; 8-1, mixing tank body; 8-2 parts of a water inlet; 8-3, a water outlet; 8-4, a muddy water discharge port; 9. a second one-way valve; 10. a supercritical water oxidation reactor; 10-1, an inclined tube end cover; 10-2, a feed inlet; 10-3, a first oxidant inlet; 10-4, a reaction inclined tube; 10-5, a T-shaped porous lining pipe; 10-6, inclined tube bosses; 10-7, a second oxidant inlet; 10-8, separating a straight pipe; 10-9, straight pipe end cover; 10-10 parts of an exhaust port; 10-11, a third electric ball valve; 10-12, a sludge discharge pipe; 10-13, a fourth electric ball valve; 11. a second booster pump; 12. a first shut-off valve; 13. a third check valve; 14. an oxidant pressurizing device; 15. a second stop valve; 16. a glow plug; 17. a third stop valve; 18. a back pressure valve; 19. a flash tank; 20. a heat exchanger; 21. a gas-liquid separator; 22. a buffer tank; 23. an expander; 24. a generator; 25. and a fourth check valve.

Detailed Description

The present invention will be described in further detail below by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and are not to be construed as limiting the present invention.

As shown in FIG. 1, the present invention provides a continuous supercritical water oxidation system for treating oily sludge, comprising: a mud-water mixing feeding system, a supercritical water oxidation system and an energy utilization system.

Example 1:

in the embodiment, the oxidant is air, the fuel is gasoline, and the T-shaped porous lining pipe 10-5 is made of zirconia.

In this embodiment, the pressure in the sludge tank 4 is local atmospheric pressure.

In this example, the muddy water was a mixture of oily sludge and organic wastewater, and the content of organic matter was 4%.

In this example, the amount of the oxidant used was 2 times the theoretical oxygen demand when the organic matter in the wastewater was completely oxidized.

The specific flow of this embodiment is as follows:

1. ignition heating process: when ignition is started, the first stop valve 12, the second stop valve 15 and the third stop valve 17 are opened, gasoline is pressurized to 1MPa in the second booster pump 11 and then enters the reaction inclined tube 10-4 through the third one-way valve 13 from the feeding hole 10-2, meanwhile, air is pressurized to 1MPa in the compressor 14 and then is divided into two paths, one path enters the reaction inclined tube 10-4 through the first oxidant inlet 10-3 and is combusted after being contacted with the gasoline at the heating core of the glow plug 16, the temperature in the reaction inclined tube 10-4 is rapidly increased, and the other path enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to prevent the inner wall surface of the inclined tube from being overheated.

2. The mud-water mixing and feeding process comprises the following steps: when mixing begins, the first electric ball valve 5 is opened, the second electric ball valve 7 is closed, oil sludge in the oil sludge tank 4 enters the mixing pipe 6, organic wastewater is pressurized to 23MPa in the first booster pump 1 and enters the mixing tank 8 from the water inlet 8-2 through the first one-way valve 2, then the first electric ball valve 5 is closed, the second electric ball valve 7 is opened, and high-pressure wastewater rushes into the mixing pipe 6 to be mixed with the oil sludge into muddy water. The muddy water is mixed with the high-temperature water separated by the gas-liquid separator 21 and preheated to 200 ℃.

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 600 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 23MPa and the air which is not preheated and with the pressure of 30MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the temperature required by the reaction can be maintained by means of self-oxidation heat release in the reaction process because the content of organic matters in the muddy water reaches more than 2 percent. Meanwhile, air which is not preheated and has the pressure of 23MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

4. And (3) a separation process: when the reaction product reaches the end of the T-shaped porous lining tube 10-5, it flows into the straight separation tube 10-8. Under the action of gravity, the reaction products separate into clean, upflowing supercritical fluid (water and gas free of solid particles) and downflowing muddy water (mud, sand and water). In the separation process, the third electric ball valve 10-11 is opened, the fourth electric ball valve 10-13 is closed, the supercritical fluid is discharged from the exhaust port 10-10 at the top end of the separation straight pipe 10-8, the muddy water flows into the mud pipe 10-12 after passing through the third electric ball valve 10-11 and is deposited at the inlet of the fourth electric ball valve 10-13, the liquid level of the muddy water in the mud pipe 10-12 continuously rises along with the reaction, when the liquid level reaches a certain height, the third electric ball valve 10-11 is closed, the fourth electric ball valve 10-13 is opened, the muddy water is discharged from the outlet of the fourth electric ball valve 10-13 and is reduced to 0.1MPa through the back pressure valve 18, the supercritical water in the muddy water is evaporated, the separation of silt and water is realized in the flash tank 19, the supercritical water pressure reduction is high-temperature steam and is discharged from the gas phase outlet at the top, silt is discharged from a solids outlet at the bottom of the flash tank 19.

5. The energy utilization process comprises the following steps: supercritical fluid enters a heat exchanger 20, cooling water in the supercritical fluid is heated into high-temperature steam, the temperature of the fluid is reduced to 300 ℃, then the fluid is separated in a gas-liquid separator 21, the high-temperature gas is dried in a buffer tank and then enters an expansion machine 22 to do work and generate power, exhaust steam is directly exhausted, and the high-temperature water flows into a mixing tank 8 from an injection fluid inlet at the lower end of an injection mixer 3 through a third one-way valve 25 to preheat mud water in the tank to 200 ℃.

In this embodiment, the oil content of the silt discharged from the bottom of the flash tank 19 is less than 2 wt%.

Example 2:

The specific flow of this embodiment is as follows:

2. The mud-water mixing and feeding process comprises the following steps: when mixing begins, the first electric ball valve 5 is opened, the second electric ball valve 7 is closed, oil sludge in the oil sludge tank 4 enters the mixing pipe 6, organic wastewater is pressurized to 30MPa in the first booster pump 1 and enters the mixing tank 8 from the water inlet 8-2 through the first one-way valve 2, then the first electric ball valve 5 is closed, the second electric ball valve 7 is opened, and high-pressure wastewater rushes into the mixing pipe 6 to be mixed with the oil sludge into muddy water. The muddy water is mixed with the high-temperature water separated by the gas-liquid separator 21 and preheated to 200 ℃.

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 600 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 30MPa and the air which is not preheated and with the pressure of 30MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the temperature required by the reaction can be maintained by self-oxidation heat release in the reaction process because the content of organic matters in the muddy water reaches more than 2 percent. Meanwhile, air which is not preheated and has the pressure of 30MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

4. And (3) a separation process: when the reaction product reaches the end of the T-shaped porous lining tube 10-5, it flows into the straight separation tube 10-8. Under the action of gravity, the reaction products separate into clean upflowing supercritical fluid (water and gas without solid particles) and downflowing muddy water (mud, sand, inorganic salts and water). In the separation process, the third electric ball valve 10-11 is opened, the fourth electric ball valve 10-13 is closed, the supercritical fluid is discharged from the exhaust port 10-10 at the top end of the separation straight pipe 10-8, the muddy water flows into the mud pipe 10-12 after passing through the third electric ball valve 10-11 and is deposited at the inlet of the fourth electric ball valve 10-13, the liquid level of the muddy water in the mud pipe 10-12 rises continuously along with the reaction, when the liquid level reaches a certain height, the third electric ball valve 10-11 is closed, the fourth electric ball valve 10-13 is opened, muddy water is discharged from the outlet of the fourth electric ball valve 10-13 and is reduced to 0.1MPa through the back pressure valve 18, supercritical water in the muddy water is evaporated, the silt and water are separated in the flash tank 19, the high-temperature steam is discharged from a gas-phase outlet at the top end of the flash tank 19, and the silt is discharged from a solid outlet at the bottom of the flash tank 19.

Example 3:

The specific flow of this embodiment is as follows:

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 550 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 23MPa and the air which is not preheated and with the pressure of 30MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the temperature required by the reaction can be maintained by means of self-oxidation heat release in the reaction process because the content of organic matters in the muddy water reaches more than 2 percent. Meanwhile, air which is not preheated and has the pressure of 23MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

Example 4

The specific flow of this embodiment is as follows:

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 550 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 30MPa and the air which is not preheated and with the pressure of 30MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the temperature required by the reaction can be maintained by self-oxidation heat release in the reaction process because the content of organic matters in the muddy water reaches more than 2 percent. Meanwhile, air which is not preheated and has the pressure of 30MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

Example 5:

In this example, the muddy water is a mixture of oily sludge and clear water, and the content of organic matter is 1%.

The specific flow of this embodiment is as follows:

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 600 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 23MPa and the air which is not preheated and with the pressure of 23MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the organic matter content is below 2 percent, and the temperature required by the reaction cannot be maintained only by self-oxidation heat release in the reaction process, so that the organic wastewater needs to be mixed with certain fuel before entering the reaction inclined tube 10-4. Meanwhile, air which is not preheated and has the pressure of 23MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

4. And (3) a separation process: when the reaction product reaches the end of the T-shaped porous lining tube 10-5, it flows into the straight separation tube 10-8. Under the action of gravity, the reaction products separate into clean upflowing supercritical fluid (water and gas without solid particles) and downflowing muddy water (mud, sand, inorganic salts and water). In the separation process, the third electric ball valve 10-11 is opened, the fourth electric ball valve 10-13 is closed, the supercritical fluid is discharged from the exhaust port 10-10 at the top end of the separation straight pipe 10-8, the muddy water flows into the mud pipe 10-12 after passing through the third electric ball valve 10-11 and is deposited at the inlet of the fourth electric ball valve 10-13, the liquid level of the muddy water in the mud pipe 10-12 rises continuously along with the reaction, when the liquid level reaches a certain height, the third electric ball valve 10-11 is closed, the fourth electric ball valve 10-13 is opened, muddy water is discharged from the outlet of the fourth electric ball valve 10-13 and is reduced to 0.1MPa through the back pressure valve 18, supercritical water in the muddy water is evaporated, the silt and water are separated in the flash tank 19, the high-temperature steam is discharged from a gas-phase outlet at the top end of the flash tank 19, and the silt is discharged from a solid-phase outlet at the bottom of the flash tank 19.

Example 6:

The specific flow of this embodiment is as follows:

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 600 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 30MPa and the air which is not preheated and with the pressure of 30MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the organic matter content is below 2 percent, and the temperature required by the reaction cannot be maintained only by self-oxidation heat release in the reaction process, so that the organic wastewater needs to be mixed with certain fuel before entering the reaction inclined tube 10-4. Meanwhile, air which is not preheated and has the pressure of 30MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

Example 7:

The specific flow of this embodiment is as follows:

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 550 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 23MPa and the air which is not preheated and with the pressure of 23MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the organic matter content is below 2 percent, and the temperature required by the reaction cannot be maintained only by self-oxidation heat release in the reaction process, so that the organic wastewater needs to be mixed with certain fuel before entering the reaction inclined tube 10-4. Meanwhile, air which is not preheated and has the pressure of 23MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

Example 8:

The specific flow of this embodiment is as follows:

SCWO reaction procedure: when the temperature in the reaction inclined tube 10-4 rises to 550 ℃, the power supply is cut off by the glow plug 16, the first stop valve 12 is closed, the second one-way valve 9 is opened, the muddy water preheated to 200 ℃ and with the pressure of 30MPa and the air which is not preheated and with the pressure of 30MPa enter the reaction inclined tube 10-4 through the feed inlet 10-2 and the first oxidant inlet 10-3 respectively for SCWO reaction, wherein the organic matter content is below 2 percent, and the temperature required by the reaction cannot be maintained only by self-oxidation heat release in the reaction process, so that the organic wastewater needs to be mixed with certain fuel before entering the reaction inclined tube 10-4. Meanwhile, air which is not preheated and has the pressure of 30MPa enters the reaction inclined tube 10-4 through the second oxidant inlet 10-7 to serve as a penetrating fluid, a protective gas film is formed on the inner surface of the T-shaped porous lining tube 10-5, the corrosion and salt deposition problems caused by the reaction are reduced to the maximum extent, and meanwhile, the air serves as an oxidant of the SCWO. After entering the reaction inclined tube 10-4, the material flows downwards along the T-shaped porous lining tube 10-5, and SCWO reaction occurs in the way.

Claims

1. A continuous supercritical water oxidation system for treating oily sludge, comprising: a mud-water mixing and feeding system, a supercritical oxidation system and an energy recovery system,

the mud-water mixing and feeding system comprises a first booster pump (1), a first one-way valve (2), an injection mixer (3), a mud tank (4), a first electric ball valve (5), a mixing pipe (6), a second electric ball valve (7), a mixing tank (8) and a second one-way valve (9), wherein the mud tank (4) comprises a mud tank body (4-1) and a mud discharge port (4-2), the mixing tank (8) comprises a mixing tank body (8-1), a water inlet (8-2), a water discharge port (8-3) and a mud-water discharge port (8-4),

the entry of first booster pump (1) is the entry of clear water or organic waste water, first booster pump (1) export through pipeline and first check valve (2) access connection, the export of first check valve (2) is through the working fluid access connection of pipeline injection blender (3) left end, the mixed fluid export of injection blender (3) right-hand member is through water inlet (8-2) of pipeline and blending tank (8) being connected, mud discharging port (4-2) of sludge tank (4) are through flange and first electric ball valve (5) access connection, first electric ball valve (5) export through flange and blending pipe (6) access connection, blending pipe (6) export through flange and second electric ball valve (7) access connection, second electric ball valve (7) export through flange and the outlet (8-3) of blending tank (8) are connected, a muddy water discharge port (8-4) of the mixing tank (8) is connected with an inlet of a second one-way valve (9) through a pipeline;

the supercritical water oxidation system consists of an ignition region, a reaction region and a separation region, the core device of the supercritical water oxidation system is a supercritical water oxidation reactor (10), the supercritical water oxidation reactor (10) consists of an inclined tube end cover (10-1), a feed inlet (10-2), a first oxidant inlet (10-3), a reaction inclined tube (10-4), a T-shaped porous lining tube (10-5), an inclined tube boss (10-6), a second oxidant inlet (10-7), a separation straight tube (10-8), a straight tube end cover (10-9), an exhaust port (10-10), a third electric ball valve (10-11), a sludge discharge tube (10-12) and a fourth electric ball valve (10-13),

wherein the ignition region consists of a second booster pump (11), a first stop valve (12), a third one-way valve (13), an inclined tube end cover (10-1), a feed inlet (10-2), an oxidant booster device (14), a second stop valve (15), a first oxidant inlet (10-3) and a glow plug (16),

the inlet of the second booster pump (11) is a fuel inlet, the outlet of the second booster pump (11) is connected with the inlet of the first check valve (12) through a pipeline, the outlet of the first check valve (12) is connected with the inlet of the third check valve (13) through a pipeline, the upper end of the inclined tube end cover (10-1) is provided with a feed inlet (10-2) and a first oxidant inlet (10-3), the outlet of the third check valve (13) is connected with the feed inlet (10-2) through a pipeline, the inlet of the oxidant supercharging device (14) is an oxidant inlet, the outlet of the oxidant supercharging device (14) is connected with the inlet of the second check valve (15), the outlet of the second check valve (15) is connected with the first oxidant inlet (10-3) through a pipeline, and the electric heating plug (16) is connected at the center of the inclined tube end cover (10-1) through threads,

the reaction zone consists of a second one-way valve (9), a third one-way valve (13), an inclined tube end cover (10-1), a feed inlet (10-2), an oxidant supercharging device (14), a second stop valve (15), a first oxidant inlet (10-3), a reaction inclined tube (10-4), a T-shaped porous lining tube (10-5), an inclined tube boss (10-6), a third stop valve (17) and a second oxidant inlet (10-7),

the outlet of the second check valve (9) is connected with the outlet of a third check valve (13) in parallel through a pipeline and then is connected with a feed inlet (10-2), the inclined tube end cover (10-1) is arranged at the upper end of a reaction inclined tube (10-4), a T-shaped porous lining tube (10-5) is arranged in the reaction inclined tube (10-4), the upper end of the T-shaped porous lining tube (10-5) is a convex end, an inclined tube boss (10-6) is arranged on the inner side of the reaction inclined tube (10-4) and used for fixing the T-shaped porous lining tube (10-5), the inlet of a third stop valve (17) is connected with the inlet of a second stop valve (15) in parallel through a pipeline and then is connected with an oxidant supercharging device (14), the outlet of the third stop valve (17) is connected with the inlet of a second oxidant (10-7) through a pipeline,

the separation area consists of a separation straight pipe (10-8), a straight pipe end cover (10-9), an exhaust port (10-10), a third electric ball valve (10-11), a sludge discharge pipe (10-12), a fourth electric ball valve (10-13), a back pressure valve (18) and a flash tank (19),

a straight pipe end cover (10-9) is arranged at the upper end of the separation straight pipe (10-8), an exhaust port (10-10) is arranged at the center of the straight pipe end cover (10-9), the lower end of the separation straight pipe (10-8) is connected with the inlet of a third electric ball valve (10-11) through a flange, the outlet of the third electric ball valve (10-11) is connected with the inlet of the sludge discharge pipe (10-12) through a flange, the outlet of the sludge discharge pipe (10-12) is connected with the inlet of a fourth electric ball valve (10-13) through a flange, the outlet of the fourth electric ball valve (10-13) is connected with the inlet of a back pressure valve (18) through a pipeline, the outlet of the back pressure valve (18) is connected with the inlet of a flash tank (19) through a pipeline, the top end of the flash tank (19) is a gas-phase discharge port, and the bottom of the flash tank (19) is a solid-phase discharge port;

the reaction inclined tube (10-4) and the separation straight tube (10-8) are welded at a certain inclination angle, the middle part of the separation straight tube (10-8) is provided with an opening for inserting the T-shaped porous lining tube (10-5), and the product in the reaction inclined tube (10-4) is ensured to flow into the separation straight tube (10-8);

the energy recovery system comprises a heat exchanger (20), a gas-liquid separator (21), a buffer tank (22), an expansion machine (23), a generator (24), a fourth one-way valve (25) and an injection mixer (3), wherein a tube pass inlet of the heat exchanger (20) is connected with an exhaust port (10-10) of a supercritical water oxidation system through a pipeline, a tube pass outlet of the heat exchanger (20) is connected with an inlet of the gas-liquid separator (21) through a pipeline, a shell pass fluid of the heat exchanger (20) is cooling water and is used for generating high-temperature steam, a gas phase outlet of the gas-liquid separator (21) is connected with an inlet of the buffer tank (22) through a pipeline, an outlet of the buffer tank (22) is connected with an inlet of the expansion machine (23) through a pipeline, the expansion machine (23) is connected with the generator (24) through a shaft, and an outlet of the expansion machine (23) is a steam, and a liquid phase outlet of the gas-liquid separator (21) is connected with an inlet of a fourth one-way valve (25) through a pipeline, and an outlet of the fourth one-way valve (25) is connected with an injection fluid inlet at the lower end of the injection mixer (3) through a pipeline.

2. The continuous supercritical water oxidation system for treating oily sludge according to claim 1, characterized in that:

the highest working pressure of each component in an ignition region, a reaction region and a separation region of the supercritical water oxidation system is 30MPa, wherein the highest working temperature of a T-shaped porous lining pipe (10-5) in the reaction region is 1200 ℃, and the highest working temperature of the rest components in the reaction region and the separation region is 700 ℃.

3. The continuous supercritical water oxidation system for treating oily sludge according to claim 1, characterized in that: the oxidant booster (14) is a plunger pump or a compressor.

4. The continuous supercritical water oxidation system for treating oily sludge according to claim 1, characterized in that: the T-shaped porous lining pipe (10-5) is made of one of zirconia, alumina and silicon carbide.

5. The continuous supercritical water oxidation system for treating oily sludge according to claim 1, characterized in that: the oxidant is selected from air, oxygen, hydrogen peroxide and KClO₃Solution, KMnO₄One of the solutions.

6. The continuous supercritical water oxidation system for treating oily sludge according to claim 1, characterized in that: the fuel is selected from one of gasoline, kerosene, methanol and ethanol.