CN209906423U - Supercritical water oxidation treatment continuous experimental system for high-solid-content organic waste liquid - Google Patents
Supercritical water oxidation treatment continuous experimental system for high-solid-content organic waste liquid Download PDFInfo
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- CN209906423U CN209906423U CN201920220171.3U CN201920220171U CN209906423U CN 209906423 U CN209906423 U CN 209906423U CN 201920220171 U CN201920220171 U CN 201920220171U CN 209906423 U CN209906423 U CN 209906423U
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Abstract
The utility model belongs to the technical field of environmental protection solid waste treatment, and discloses a supercritical water oxidation treatment continuous experimental system for high solid content organic waste liquid, wherein reaction materials sequentially pass through a feeding system and a material preheater and enter a supercritical water oxidation reaction system through a material inlet, and a gas oxidant sequentially passes through an air inlet system and a gas preheater and enters the supercritical water oxidation reaction system through a gas inlet; the supercritical water oxidation reaction system is provided with a solid phase substance discharge port and a gas phase and liquid phase substance discharge port, and the gas phase and liquid phase substance discharge port is sequentially connected with a condenser, a backpressure system and a gas-liquid separator. The utility model discloses at first use feed system carry out quenching and tempering preliminary treatment to the supplied materials, then with the material that the quenching and tempering is good input supercritical water oxidation reaction system after the material preheater heating, also input supercritical water oxidation reaction system after preheating the oxidant simultaneously, can realize continuous, quick, thorough processing to high solid content organic waste liquid.
Description
Technical Field
The utility model belongs to the technical field of the solid useless processing of environmental protection, specific theory relates to a supercritical water oxidation treatment continuous experiment system suitable for high solid organic waste liquid that contains.
Background
The supercritical water oxidation technology is a novel advanced oxidation technology, when water is in a supercritical state at the temperature of 374.3 ℃ and the pressure of more than 22.05MPa, the water in the state is the supercritical water, the supercritical water is a new state different from liquid and gas, the property of the supercritical water is between that of gas and liquid, the supercritical water has the dissolution characteristic of liquid and the transmission characteristic of gas, and can be mutually dissolved with oxygen, carbon dioxide, organic matters and the like in any ratio to form a uniform phase. The supercritical water oxidation technology uses the characteristic of the supercritical water to enable organic matters and an oxidant to rapidly generate strong oxidation reaction and convert organic matters which are difficult to degrade, toxic and harmful into CO in a short time2And H2O, conversion of nitrogen to N2Or N2O and the like, and elements such as phosphorus, chlorine, sulfur and the like are oxidized and deposited from supercritical water in the form of inorganic salt, so that the harmlessness of organic toxic pollutants is realized.
However, the supercritical water oxidation technology has harsh reaction conditions, the source, composition and physical properties of the treated pollutants are complex, and particularly, solid-phase substances in reactants are extremely easy to cause hazards such as pipeline blockage and equipment abrasion, so that the long-period stable operation of the equipment is adversely affected, and the popularization and application of the technology are hindered.
SUMMERY OF THE UTILITY MODEL
The utility model discloses what solve is that technical problem such as solid phase thing deposit, equipment wearing and tearing that exist in the supercritical water oxidation technology application provides a high solid organic waste liquid supercritical water oxidation treatment continuous experiment system that contains, can ensure reaction unit's long period steady operation, has great meaning to the engineering conversion of supercritical water oxidation technology.
The utility model discloses a following technical scheme realizes:
a continuous experiment system for supercritical water oxidation treatment of high-solid-content organic waste liquid comprises a feeding system (1), a material preheater (2), a material inlet (3), an air inlet system (4), a gas preheater (5), a gas inlet (6), a supercritical water oxidation reaction system (7), a solid-phase object discharge port (8), a gas-phase and liquid-phase object discharge port (9), a condenser (10), a backpressure system (11), a gas-liquid separator (12), a gas discharge port (13) and a liquid discharge port (14);
the reaction materials enter from an inlet of the feeding system (1), an outlet of the feeding system (1) is connected with an inlet of the material preheater (2), and an outlet of the material preheater (2) is connected with the material inlet (3) of the supercritical water oxidation reaction system (7);
the gas oxidant enters from an inlet of the gas inlet system (4), an outlet of the gas inlet system (4) is connected with an inlet of the gas preheater (5), and an outlet of the gas preheater (5) is connected with the gas inlet (6) of the supercritical water oxidation reaction system (7);
the supercritical water oxidation reaction system (7) is provided with the solid phase object discharge port (8) and the gas phase and liquid phase object discharge port (9); the gas phase and liquid phase discharge port (9) is connected with an inlet of the condenser (10), an outlet of the condenser (10) is connected with an inlet of the backpressure system (11), an outlet of the backpressure system (11) is connected with an inlet of the gas-liquid separator (12), and the gas-liquid separator (12) is provided with the gas discharge port (13) and the liquid discharge port (14).
Further, the feeding system (1) comprises a homogenizing tank (101), a stirring motor (102), a stirring rod (103), a detachable wall-scraping stirring paddle (104), a shearing disc type stirring paddle (105), a wall-mounted filtering screen (106), a first stop valve (107), a grinding pump (108), a second stop valve (109), a high-pressure pump (110), a liquid flow meter (111), a first one-way valve (112), a clean water tank (113) and a third stop valve (114);
the homogenizing tank (101) is provided with the stirring motor (102) and the stirring rod (103), and the stirring rod (103) is provided with the detachable wall-scraping stirring paddle (104) and the shearing disc type stirring paddle (105);
the outlet of the unconditioned material of the homogenizing tank (101) is connected with the inlet of the grinding pump (108) through the first stop valve (107), the outlet of the grinding pump (108) is connected above the wall-mounted filter screen (106), and the wall-mounted filter screen (106) is arranged at the top of the homogenizing tank (101);
the tempered material outlet of the homogenizing tank (101) is connected with the inlet of the high-pressure pump (110) through the second stop valve (109), the outlet of the high-pressure pump (110) is connected with the inlet of the liquid flow meter (111), the outlet of the liquid flow meter (111) is connected with the inlet of the first check valve (112), and the outlet of the first check valve (112) is connected with the inlet of the material preheater (2); the outlet of the clean water tank (113) is connected with the inlet of the high-pressure pump (110) through the third stop valve (114).
Further, the gas inlet system (4) comprises a gas oxidant gas cylinder (401), a gas booster pump (402), a gas oxidant buffer tank (403), a fourth stop valve (404), a pressure reducing valve (405), a gas flow meter (406), a second one-way valve (407) and a fifth stop valve (408);
an outlet of the gas oxidant cylinder (401) is connected with an inlet of the gas booster pump (402), an outlet of the gas booster pump (402) is connected with an inlet of the gas oxidant buffer tank (403), an outlet of the gas oxidant buffer tank (403) is connected with an inlet of the pressure reducing valve (405) through the fourth stop valve (404), an outlet of the pressure reducing valve (405) is connected with an inlet of the gas flow meter (406), an outlet of the gas flow meter (406) is connected with an inlet of the second one-way valve (407), and an outlet of the second one-way valve (407) is connected with an inlet of the gas preheater (5); the bottom of the gas oxidant buffer tank (403) is connected with the fifth stop valve (408).
Further, the supercritical water oxidation reaction system (7) comprises a reactor (701), a high-pressure separator (702), a solid phase object cache tank (703), a reactor extension pipe (704), a sectional heating furnace (705), a sixth stop valve (706), a seventh stop valve (707), an eighth stop valve (708) and a ninth stop valve (709);
the reactor (701), the high-pressure separator (702) and the solid-phase buffer tank (703) are directly connected from top to bottom in sequence; the material inlet (3) and the gas inlet (6) are arranged at the top of the reactor (701), the gas-phase and liquid-phase material outlet (9) is arranged at the upper part of the high-pressure separator (702), and the solid-phase material outlet (8) is arranged at the bottom of the solid-phase material buffer tank (703);
the reactor extension pipe (704) is disposed at the bottom of the reactor (701) and extends to the middle or lower part of the high-pressure separator (702); the segmented heating furnace (705) is arranged outside the reactor (701);
the inlet at the top of the solid-phase object cache tank (703) is provided with the sixth stop valve (706), and is connected with the outlet of the high-pressure separator (702) through the sixth stop valve (706); the seventh stop valve (707) is arranged at the solid-phase material outlet (8) at the bottom of the solid-phase material buffer tank (703); the solid-phase object cache tank (703) is further provided with a pressure supplementing gas inlet and a pressure relief port, and the pressure supplementing gas inlet and the pressure relief port are respectively provided with the eighth stop valve (708) and the ninth stop valve (709).
The utility model has the advantages that:
the utility model discloses a supercritical water oxidation treatment continuous experiment system is handling the high solid organic waste liquid in-process that contains, at first uses feed system to carry out quenching and tempering preliminary treatment to the supplied materials, then with quenching and tempering the good material through the material preheater heating after input to supercritical water oxidation reaction system, also input supercritical water oxidation reaction system after preheating the oxidant simultaneously, can realize quick, thorough processing to organic waste liquid.
The material conditioning pretreatment process of the feeding system is realized at normal temperature and normal pressure by organically combining all related equipment by physical and chemical methods, is safe and reliable, has low energy consumption, is uniform and stable in conditioned reaction materials, has better fluidity, is convenient to transport and store, and can provide guarantee for continuous feeding and stable operation of the supercritical water oxidation reactor.
The gas oxidant adopted by the gas inlet system can be industrial pure oxygen, oxygen-enriched gas or air, the existing resources of the site where the equipment is located are fully utilized to develop a supercritical water oxidation treatment process, and the combined use of the gas booster pump and the gas oxidant buffer tank ensures the use of the low-pressure gas oxidant in a high-pressure environment, so that the equipment investment and the operating cost in the technical engineering application process are reduced to the maximum extent.
The reactor, the reactor extension pipe and the high-pressure separator and the solid phase object buffer tank which surround the reactor and the reactor extension pipe in the reaction system are sequentially arranged from top to bottom and are directly connected, the solid phase object with higher density in the reaction product is directly led into the bottom of the high-pressure separator through the reactor extension pipe which extends into the middle lower part of the high-pressure separator and enters the solid phase object buffer tank under the action of gravity, the blockage possibly caused by pipeline conveying is avoided, the solid phase object in the solid phase object buffer tank can be intermittently discharged in the operation process of the equipment, and the long-period uninterrupted operation of the whole system is guaranteed.
Drawings
FIG. 1 is a schematic structural view of a supercritical water oxidation treatment continuous experimental system for high solid content organic waste liquid provided by the present invention;
fig. 2 is a schematic structural diagram of a feeding system provided by the present invention;
fig. 3 is a schematic structural diagram of an air intake system provided by the present invention;
fig. 4 is a schematic structural diagram of the supercritical water oxidation reaction system provided by the present invention.
In the above figures: 1. the system comprises a feeding system, a material preheater, a material inlet, a gas inlet system, a gas preheater, a gas inlet, a supercritical water oxidation reaction system, a solid phase material outlet, a gas phase material outlet, a liquid phase material outlet, a condenser, a backpressure system, a gas-liquid separator, a gas outlet, a liquid outlet, a gas inlet, a gas preheater, a gas inlet, a supercritical water oxidation reaction system, a solid phase material outlet, a gas;
101. the device comprises a homogenizing tank, 102, a stirring motor, 103, a stirring rod, 104, a detachable wall scraping stirring paddle, 105, a shearing disc type stirring paddle, 106, a wall-mounted filtering screen, 107, a first stop valve, 108, a grinding pump, 109, a second stop valve, 110, a high-pressure pump, 111, a liquid flowmeter, 112, a first one-way valve, 113, a clear water tank, 114 and a third stop valve;
401. a gas oxidant cylinder, 402, a gas booster pump, 403, a gas oxidant buffer tank, 404, a fourth stop valve, 405, a pressure reducing valve, 406, a gas flowmeter, 407, a second check valve, 408 and a fifth stop valve;
701. the system comprises a reactor, 702, a high-pressure separator, 703, a solid-phase object buffer tank, 704, a reactor extension pipe, 705, a sectional heating furnace, 706, a sixth stop valve, 707, a seventh stop valve, 708, an eighth stop valve and 709, wherein the reactor extension pipe is connected with the reactor extension pipe through a pipeline.
Detailed Description
In order to further understand the contents, features and effects of the present invention, the following embodiments are illustrated and described in detail with reference to the accompanying drawings:
as shown in FIG. 1, an embodiment of the utility model discloses a high solid content organic waste liquid supercritical water oxidation handles continuous experiment system, mainly includes charge-in system 1, material preheater 2, material entry 3, air intake system 4, gas preheater 5, gas inlet 6, supercritical water oxidation reaction system 7, solid phase thing discharge port 8, gaseous phase and liquid phase thing discharge port 9, condenser 10, backpressure system 11, vapour and liquid separator 12, gas discharge port 13, liquid discharge port 14.
Reaction material gets into by feed system 1's entry, and feed system 1's export and material pre-heater 2's entry linkage, material pre-heater 2's export and the material entry 3 at supercritical water oxidation reaction system 7 tops are connected.
A gas oxidant (air, oxygen-enriched gas or oxygen) enters from an inlet of the gas inlet system 4, an outlet of the gas inlet system 4 is connected with an inlet of the gas preheater 5, and an outlet of the gas preheater 5 is connected with a gas inlet 6 at the top of the supercritical water oxidation reaction system 7.
The bottom of the supercritical water oxidation reaction system 7 is provided with a solid phase material outlet 8, and the middle part is provided with a gas phase material outlet 9 and a liquid phase material outlet 9. The gas phase and liquid phase material discharge port 9 is connected with the inlet of a condenser 10, the outlet of the condenser 10 is connected with the inlet of a backpressure system 11, the outlet of the backpressure system 11 is connected with the inlet of a gas-liquid separator 12, a gas discharge port 13 of the gas-liquid separator 12 discharges separated gas, and a liquid discharge port 14 of the gas-liquid separator 12 discharges separated liquid.
As shown in fig. 2, the feeding system 1 mainly comprises a homogenizing tank 101, a stirring motor 102, a stirring rod 103, a detachable wall-scraping stirring paddle 104, a shearing disk type stirring paddle 105, a wall-mounted filtering screen 106, a first stop valve 107, a grinding pump 108, a second stop valve 109, a high-pressure pump 110, a liquid flow meter 111, a first check valve 112, a clear water tank 113, and a third stop valve 114.
The reaction materials enter a homogenizing tank 101 from an inlet of a feeding system 1, a stirring motor 102 is connected with a stirring rod 103, and a detachable wall-scraping stirring paddle 104 and a shearing disc type stirring paddle 105 are arranged on the stirring rod 103. When the viscosity of the material in the homogenizing tank 11 is high and the material adherence phenomenon occurs, the detachable wall scraping stirring paddle 104 is installed on the stirring rod 103, the stirring motor 102 is started, the stirring rod 103 drives the detachable wall scraping stirring paddle 104 to rotate, and the material adhered to the inner wall of the homogenizing tank 11 is scraped; a plurality of shear disk type stirring paddles 105 are fixedly arranged on the stirring rod 103 at different heights and used for dispersing the materials gathered in the homogenizing tank 101.
An outlet of the untempered material at the bottom of the homogenizing tank 101 is connected with an inlet of a grinding pump 108 through a first stop valve 107, an outlet of the grinding pump 108 is connected above a wall-mounted filter screen 106, and the wall-mounted filter screen 106 is arranged at a feeding position at the top of the homogenizing tank 101 and used for filtering solid particles with larger particle size; the wall mounted filter screen 106 is removable for cleaning or replacement.
The outlet of the tempered material at the bottom of the homogenizing tank 101 is connected with the inlet of a high-pressure pump 110 through a second stop valve 109, the outlet of the high-pressure pump 110 is connected with the inlet of a liquid flow meter 111, the outlet of the liquid flow meter 111 is connected with the inlet of a first check valve 112, and the outlet of the first check valve 112 is connected with the inlet of a material preheater 2. Meanwhile, an outlet of the clean water tank 113 is connected to an inlet of the high pressure pump 110 through a third shut-off valve 114.
The feeding system 1 adopts the homogenizing tank 101 and the grinding pump 108 to homogenize the incoming materials, and meets the requirements of the subsequent processes. The homogenizing tank 101 is provided with a detachable wall scraping stirring paddle 104 and a shearing disc type stirring paddle 105, and the detachable wall scraping stirring paddle 104 is used for scraping the wall in the homogenizing tank 101 to prevent solid-phase substances from being adhered to the inner wall; the shear disk type stirring paddle 105 is used for dispersing large particles formed by binding solid substances. The grinding pump 108 is a fixed gap grinding pump or an adjustable gap grinding pump, and the particle size of the solid phase in the incoming material is not more than 100 μm after multi-stage grinding. The outlet pressure of the high-pressure pump 110 is not less than 22MPa so as to meet the feeding requirement of the supercritical water oxidation reaction system 7. The pressure resistance of the liquid flowmeter 111 is not less than 22MPa so as to meet the requirements of working conditions. The heating temperature of the gas preheater 5 is not less than 200 ℃ so as to meet the material preheating requirement.
As shown in fig. 3, the gas intake system 4 is mainly composed of a gas oxidant cylinder 401, a gas booster pump 402, a gas oxidant buffer tank 403, a fourth shutoff valve 404, a pressure reducing valve 405, a gas flow meter 406, a second check valve 407, and a fifth shutoff valve 408.
An outlet of the gas oxidant gas cylinder 401 is connected with an inlet of the gas booster pump 402, an outlet of the gas booster pump 402 is connected with an inlet of the gas oxidant buffer tank 403, an outlet of the gas oxidant buffer tank 403 is connected with an inlet of a pressure reducing valve 405 through a fourth stop valve 404, an outlet of the pressure reducing valve 405 is connected with an inlet of a gas flowmeter 406, an outlet of the gas flowmeter 406 is connected with an inlet of a second check valve 407, and an outlet of the second check valve 407 is connected with an inlet of the gas preheater 5. The bottom of the gas oxidizing agent buffer tank 403 is connected to a fifth stop valve 408.
The maximum allowable outlet pressure of the gas booster pump 402 is not lower than 22MPa so as to meet the requirements of subsequent processes; the pressure resistance of the gas flowmeter 406 is not less than 22MPa so as to meet the requirements of working conditions. The heating temperature of the gas preheater 5 is not less than 200 ℃ so as to meet the gas preheating requirement.
As shown in fig. 4, the supercritical water oxidation reaction system 7 includes a reactor 701, a high-pressure separator 702, a solid-phase object buffer tank 703, a reactor extension pipe 704, a step-type heating furnace 705, a sixth stop valve 706, a seventh stop valve 707, an eighth stop valve 708, and a ninth stop valve 709.
The reactor 701, the high-pressure separator 702, and the solid phase buffer tank 703 are not connected by a pipeline, but are directly connected from top to bottom, and the reactor 701, the high-pressure separator 702, and the solid phase buffer tank 703 are preferably overlapped in the vertical upper axis. The material inlet 3 and the gas inlet 6 are arranged at the top of the reactor 701, the gas phase and liquid phase discharge port 9 is arranged at the upper part of the high-pressure separator 702, and the solid phase discharge port 8 is arranged at the bottom of the solid phase buffer tank 703.
The reactor body and the top cover of the reactor 701 are made of alloy with high strength and strong corrosion resistance at high temperature, the design working pressure is not lower than 22MPa, and the working temperature is not lower than 374 ℃. The top end and the bottom end of the reactor 701 kettle body are respectively provided with an external expanding part, and the top end and the bottom end of the high-pressure separator 702 kettle body are also respectively provided with an external expanding part. The external expansion part at the top end of the reactor 701 is connected with the top cover of the reactor 701 through a bolt. The external expansion part at the bottom end of the reactor 701 and the external expansion part at the top end of the high-pressure separator 702 are connected through bolts so as to directly and hermetically connect the reactor 701 and the high-pressure separator 702 together. The external expansion part at the bottom end of the kettle body of the high-pressure separator 702 is connected with the bottom cover of the high-pressure separator 702 through a bolt, and the bottom cover of the high-pressure separator 702 is provided with an outlet which is connected with an inlet at the top of the solid-phase object cache tank 703.
The reactor 701 is also provided at the bottom with a reactor extension pipe 704, the reactor extension pipe 704 extending to the middle or lower portion of the high pressure separator 702. The reactor extension pipe 704 may be an integral extension section of the reactor 701 or may be screwed as a separate component to the bottom end of the reactor 701. The reactor extension pipe 704 is connected below the reactor 701, so that the solid matters in the reaction products can be guaranteed to be deposited at the bottom of the high-pressure separator 702, and the gas-phase and liquid-phase products are discharged from the upper part of the high-pressure separator 702.
The reactor 701, the high-pressure separator 702 and the solid phase buffer tank 703 are directly connected in sequence, the reactor extension pipe 704 extends into the middle lower part of the high-pressure separator 702 to avoid the blockage caused by pipeline transportation, and the vertical arrangement and the position layout with coincident axes of the equipment are favorable for the solid phase with higher density to smoothly enter the solid phase buffer tank 703 under the action of gravity. Thus, the reaction material and the gas oxidant enter the reactor 701 from the top of the reactor 701, and supercritical water oxidation reaction occurs; the reaction product is introduced into the high-pressure separator 702 through the reactor extension pipe 704, the undissolved inorganic salt and inorganic solid phase deposit at the bottom of the high-pressure separator 702, and enters the solid phase buffer tank 703 under the action of gravity and is discharged intermittently through the solid phase discharge port 8, and the gas phase and liquid phase product is discharged from the supercritical water oxidation reaction system 7 through the gas phase and liquid phase discharge port 9.
The sectional type heating furnace 705 is arranged outside the reactor 701, can realize sectional heating of the reactor 701, accurately control the temperature of different areas of the reactor 701, and can divide the reactor 701 into areas with different functions through temperature control, wherein the upper part of the reactor 701 is a material heating area for heating reaction materials to reach the supercritical water oxidation reaction condition; the middle part of the reactor 701 is a supercritical water oxidation reaction zone, organic pollutants in reaction materials react with oxygen to be thoroughly decomposed into inorganic small molecular substances, and inorganic salts are precipitated due to the reduction of the solubility in supercritical water; the lower part of the reactor 701 is a subcritical salt dissolution region, and inorganic salts precipitated in a supercritical state are newly dissolved into water in the region to form concentrated brine. The temperature of different areas of the reactor 701 is controlled by a sectional heating furnace 705 and thermocouples inserted into the reactor 701, so as to form a material heating area, a supercritical water oxidation reaction area and a subcritical salt solution area.
A sixth stop valve 706 is arranged at the inlet of the top of the solid phase buffer tank 703 and is connected with the outlet of the bottom cover of the high-pressure separator 702 through the sixth stop valve 706. A seventh stop valve 707 is provided at the solid matter discharge port 8 in the bottom of the solid matter buffer tank 703. The solid-phase object buffer tank 703 is further provided with a pressure-compensating gas inlet and a pressure relief port, and the pressure-compensating gas inlet and the pressure relief port are respectively provided with an eighth stop valve 708 and a ninth stop valve 709.
The utility model discloses a high solid contains organic waste liquid supercritical water oxidation and handles continuous experiment system, its working process as follows:
after coming out of the feeding system 1, the reaction materials pass through a material preheater 2 and then enter a supercritical water oxidation reaction system 7 through a material inlet 3; after coming out of the gas inlet system 4, a gas oxidant (air, oxygen-enriched gas or oxygen) passes through a gas preheater 5 and then enters a supercritical water oxidation reaction system 7 through a gas inlet 6; the material and the oxidant that enter supercritical water oxidation reaction system 7 take place supercritical water oxidation reaction, and solid phase thing discharges from supercritical water oxidation reaction system 7 bottom solid phase thing discharge port 8, and gaseous phase and liquid phase thing enter condenser 10 through gaseous phase and liquid phase thing discharge port 9, and the condensation product passes through back pressure system 11 and then gets into gas-liquid separator 12, and the gas after the separation is discharged from gas discharge port 13, and liquid is discharged from liquid discharge port 14.
When the feeding system 1 feeds materials, the second stop valve 109 is closed first, the third stop valve 114 is opened to inject the clean water in the clean water tank 113 into the supercritical water oxidation reaction system 7 through the high-pressure pump 110, the liquid flow meter 111 and the first one-way valve 112, when the temperature and the pressure of the supercritical water oxidation reaction system 7 reach the set experimental conditions, the third stop valve 114 is closed, and the second stop valve 109 is opened to inject the materials in the homogenizing tank 101 into the supercritical water oxidation reaction system 7 through the high-pressure pump 110, the liquid flow meter 111 and the first one-way valve 112. The material at the bottom of the homogenizing tank 101 enters the grinding pump 108 through the first stop valve 107, the ground material enters the homogenizing tank 101 through the pipeline, and the wall-mounted filter screen 106 is used for filtering solid particles with larger particle size.
When the gas inlet system 4 is supplying gas, the gas oxidizing agent in the gas oxidizing agent cylinder 401 is injected into the gas oxidizing agent buffer tank 403 by the gas booster pump 402, the fourth stop valve 404 is opened during the experiment, the gas oxidizing agent after pressure reduction is sent to the inlet of the gas flow meter 406 by the pressure reducing valve 405, the gas oxidizing agent after metering is sent out from the outlet of the gas flow meter 406, and the gas oxidizing agent after metering passes through the second check valve 407 and enters the next process. The fifth shutoff valve 408 is used to vent the gas oxidizer remaining in the gas oxidizer buffer tank 403 after the experiment is completed.
In the supercritical water oxidation reaction system 7, the temperature of different areas of the reactor 701 is controlled by a sectional heating furnace 705 and a thermocouple, so as to form a material heating area, a supercritical water oxidation reaction area and a subcritical salt solution area. After a reaction material and an oxidant respectively enter the reactor 701 through the material inlet 3 and the gas inlet 6, supercritical water oxidation reaction is completed at the upper part and the middle part of the reactor 701, organic pollutants in the reaction material react with oxygen to be thoroughly decomposed into inorganic small molecular substances, and inorganic salts are separated out due to the reduction of the solubility in the supercritical water; after the reaction product enters the subcritical salt dissolution zone at the lower part of the reactor 701, inorganic salts precipitated in a supercritical state are dissolved in water, the formed concentrated brine, undissolved inorganic salts and solid-phase substances which do not participate in the reaction enter the lower part of the high-pressure separator 70 through the reactor extension pipe 704, gas-phase and liquid-phase substances in the reaction product are discharged through a gas-phase and liquid-phase substance discharge port 9, and the undissolved inorganic salts and the solid-phase substances are deposited at the bottom of the high-pressure separator 702.
In the reaction process, the sixth stop valve 706 is kept in an open state, the solid matter deposited at the bottom of the high-pressure separator 702 enters the solid matter cache tank 703 under the action of gravity, the sixth stop valve 706 is closed, the ninth stop valve 709 is opened to discharge the pressure in the solid matter cache tank 703 to normal pressure, the seventh stop valve 707 is opened to discharge the solid matter in the solid matter cache tank 703 through the solid matter discharge port 8, the seventh stop valve 707 and the ninth stop valve 709 are closed, the eighth stop valve 708 is opened to balance the pressure supplemented to the solid matter cache tank 703 with the pressure in the reactor 701, the eighth stop valve 708 is closed, and the sixth stop valve 706 is opened to communicate the high-pressure separator 702 and the solid matter cache tank 703 for circularly discharging the solid matter.
The following two embodiments are combined to describe the working process of the supercritical water oxidation treatment continuous experimental system in detail:
example 1
When the system is started, clear water in a clear water tank 113 of the feeding system 1 is firstly injected into the experimental system by a high-pressure pump 110, and meanwhile, the pressure of the whole experimental system is controlled to be kept at 40MPa by a pressure control system; then starting a sectional heating furnace 705, and controlling the temperature in the reactor 701 to reach 400 ℃; starting a material preheater 2, heating to 300 ℃, simultaneously switching a clear water tank 113 of the material system 1 to a homogenizing tank 101, and injecting organic waste liquid with COD value of 100000mg/L in the homogenizing tank 101 into a reactor 701 by using a high-pressure pump 110; starting a gas preheater 5, heating to 300 ℃, and simultaneously starting a gas flowmeter 406 to inject oxidant oxygen into the reactor 701; organic waste liquid reacts with oxygen in the reactor 701, and organic pollutants in the waste liquid are thoroughly decomposed into inorganic micromolecular substances; the reaction product is discharged from the upper part of the high-pressure separator 702, passes through the condenser 10 and the backpressure system 11 and then enters the gas-liquid separator 12, the gas is discharged from the upper part of the gas-liquid separator 12, and the liquid is discharged from the lower part of the gas-liquid separator 12; the COD value of the organic waste liquid is high, so that the heat released in the reaction process is enough to maintain the reaction operation, and the material preheater 2 and the gas preheater 5 are closed when the reaction reaches a stable operation state.
Example 2
Putting the diluted viscosity-reducing liquid into a homogenizing tank 101, starting a detachable wall-scraping stirring paddle 104 and a shearing disc type stirring paddle 105, adding refined 'three-mud' (bottom mud of an oil separation tank, floating slag and residual activated sludge generated in the wastewater treatment process of refining enterprises) with the water content of 80-85% in the stirring process, and simultaneously circularly grinding the materials in the homogenizing tank 101 by using a grinding pump 108, so that the 'three-mud' and the diluted viscosity-reducing liquid are fully mixed, the water content of the 'three-mud' is increased to 90-92%, and the viscosity is reduced to be below 100 mPas; after the pressure in the reactor 701 is controlled to be 40MPa by using clean water and the temperature is 400 ℃, the hardened and tempered 'three mud' in the homogenizing tank 101 is injected into the reactor 701 by using a high-pressure pump 110, and oxidant oxygen is injected into the reactor 701 by using a gas flow meter 406; organic matters in the conditioned 'three sludge' react with oxygen in the reactor 701 to be thoroughly decomposed into inorganic micromolecular substances, solid-phase substances are settled to the bottom of the solid-phase substance cache tank 703 under the action of gravity, and are discharged from the solid-phase substance discharge port 8 by intermittently opening the sixth stop valve 706; the gas phase and liquid phase products are discharged from a gas phase and liquid phase discharge outlet 9, pass through a condenser 10 and a backpressure system 11 and then enter a gas-liquid separator 12, the gas is discharged from a gas discharge outlet 13 at the upper part of the gas-liquid separator 12, and the liquid is discharged from a liquid discharge outlet 14 at the lower part of the gas-liquid separator 12.
Although the preferred embodiments of the present invention have been described with reference to the accompanying drawings, the present invention is not limited to the above embodiments, which are only illustrative and not restrictive, and those skilled in the art can make various changes without departing from the spirit and the scope of the invention as claimed.
Claims (4)
1. A continuous experiment system for supercritical water oxidation treatment of high-solid-content organic waste liquid is characterized by comprising a feeding system (1), a material preheater (2), a material inlet (3), an air inlet system (4), a gas preheater (5), a gas inlet (6), a supercritical water oxidation reaction system (7), a solid-phase object discharge port (8), a gas-phase and liquid-phase object discharge port (9), a condenser (10), a backpressure system (11), a gas-liquid separator (12), a gas discharge port (13) and a liquid discharge port (14);
reaction materials enter from an inlet of the feeding system (1), an outlet of the feeding system (1) is connected with an inlet of the material preheater (2), and an outlet of the material preheater (2) is connected with the material inlet (3) of the supercritical water oxidation reaction system (7);
the gas oxidant enters from the inlet of the gas inlet system (4), the outlet of the gas inlet system (4) is connected with the inlet of the gas preheater (5), and the outlet of the gas preheater (5) is connected with the gas inlet (6) of the supercritical water oxidation reaction system (7);
the supercritical water oxidation reaction system (7) is provided with the solid phase object discharge port (8) and the gas phase and liquid phase object discharge port (9); the gas phase and liquid phase discharge port (9) is connected with an inlet of the condenser (10), an outlet of the condenser (10) is connected with an inlet of the backpressure system (11), an outlet of the backpressure system (11) is connected with an inlet of the gas-liquid separator (12), and the gas-liquid separator (12) is provided with the gas discharge port (13) and the liquid discharge port (14).
2. The supercritical water oxidation treatment continuous experimental system for the high-solid-content organic waste liquid as claimed in claim 1, wherein the feeding system (1) comprises a homogenizing tank (101), a stirring motor (102), a stirring rod (103), a detachable wall-scraping stirring paddle (104), a shear disk type stirring paddle (105), a wall-mounted filtering screen (106), a first stop valve (107), a grinding pump (108), a second stop valve (109), a high-pressure pump (110), a liquid flow meter (111), a first one-way valve (112), a clean water tank (113) and a third stop valve (114);
the homogenizing tank (101) is provided with the stirring motor (102) and the stirring rod (103), and the stirring rod (103) is provided with the detachable wall-scraping stirring paddle (104) and the shearing disc type stirring paddle (105);
the outlet of the unconditioned material of the homogenizing tank (101) is connected with the inlet of the grinding pump (108) through the first stop valve (107), the outlet of the grinding pump (108) is connected above the wall-mounted filter screen (106), and the wall-mounted filter screen (106) is arranged at the top of the homogenizing tank (101);
the tempered material outlet of the homogenizing tank (101) is connected with the inlet of the high-pressure pump (110) through the second stop valve (109), the outlet of the high-pressure pump (110) is connected with the inlet of the liquid flow meter (111), the outlet of the liquid flow meter (111) is connected with the inlet of the first check valve (112), and the outlet of the first check valve (112) is connected with the inlet of the material preheater (2); the outlet of the clean water tank (113) is connected with the inlet of the high-pressure pump (110) through the third stop valve (114).
3. The supercritical water oxidation treatment continuous experiment system for the high-solid-content organic waste liquid as claimed in claim 1, wherein the gas inlet system (4) comprises a gas oxidant gas cylinder (401), a gas booster pump (402), a gas oxidant buffer tank (403), a fourth stop valve (404), a pressure reducing valve (405), a gas flow meter (406), a second one-way valve (407) and a fifth stop valve (408);
an outlet of the gas oxidant cylinder (401) is connected with an inlet of the gas booster pump (402), an outlet of the gas booster pump (402) is connected with an inlet of the gas oxidant buffer tank (403), an outlet of the gas oxidant buffer tank (403) is connected with an inlet of the pressure reducing valve (405) through the fourth stop valve (404), an outlet of the pressure reducing valve (405) is connected with an inlet of the gas flow meter (406), an outlet of the gas flow meter (406) is connected with an inlet of the second one-way valve (407), and an outlet of the second one-way valve (407) is connected with an inlet of the gas preheater (5); the bottom of the gas oxidant buffer tank (403) is connected with the fifth stop valve (408).
4. The supercritical water oxidation treatment continuous experiment system for the high-solid-content organic waste liquid according to claim 1, wherein the supercritical water oxidation reaction system (7) comprises a reactor (701), a high-pressure separator (702), a solid-phase object buffer tank (703), a reactor extension pipe (704), a sectional heating furnace (705), a sixth stop valve (706), a seventh stop valve (707), an eighth stop valve (708), and a ninth stop valve (709);
the reactor (701), the high-pressure separator (702) and the solid-phase buffer tank (703) are directly connected from top to bottom in sequence; the material inlet (3) and the gas inlet (6) are arranged at the top of the reactor (701), the gas-phase and liquid-phase material outlet (9) is arranged at the upper part of the high-pressure separator (702), and the solid-phase material outlet (8) is arranged at the bottom of the solid-phase material buffer tank (703);
the reactor extension pipe (704) is disposed at the bottom of the reactor (701) and extends to the middle or lower part of the high-pressure separator (702); the segmented heating furnace (705) is arranged outside the reactor (701);
the inlet at the top of the solid-phase object cache tank (703) is provided with the sixth stop valve (706), and is connected with the outlet of the high-pressure separator (702) through the sixth stop valve (706); the seventh stop valve (707) is arranged at the solid-phase material outlet (8) at the bottom of the solid-phase material buffer tank (703); the solid-phase object cache tank (703) is further provided with a pressure supplementing gas inlet and a pressure relief port, and the pressure supplementing gas inlet and the pressure relief port are respectively provided with the eighth stop valve (708) and the ninth stop valve (709).
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109809553A (en) * | 2018-11-24 | 2019-05-28 | 中海油能源发展股份有限公司 | A kind of large arch dam organic liquid waste supercritical water oxidation processing continuous experiment system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109809553A (en) * | 2018-11-24 | 2019-05-28 | 中海油能源发展股份有限公司 | A kind of large arch dam organic liquid waste supercritical water oxidation processing continuous experiment system |
| CN109809553B (en) * | 2018-11-24 | 2024-03-15 | 中海油能源发展股份有限公司 | Supercritical water oxidation treatment continuous experimental system for high-solid organic waste liquid |
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