CN211445200U - Supercritical water oxidation system - Google Patents
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- CN211445200U CN211445200U CN201922386175.1U CN201922386175U CN211445200U CN 211445200 U CN211445200 U CN 211445200U CN 201922386175 U CN201922386175 U CN 201922386175U CN 211445200 U CN211445200 U CN 211445200U
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Abstract
The supercritical water oxidation system comprises an oxidant source, an organic waste liquid source, an auxiliary fuel source, a softened water source, a pressure reduction device, a gas-liquid separator and a controller which are connected with a reactor. The oxidant source is air, the air compressor and the air preheater are sequentially connected on a pipeline between the oxidant source and the oxidant inlet of the reactor, and the controller is electrically connected with each feeding source adjusting device and each detecting device; the oxidant inlet and the material inlet of the reactor are respectively provided with one, and the material inlet is connected with a material main inlet pipe. When the reactor is started, air enters the reactor after being preheated to a set temperature by the air preheater outside the reactor; when the reactor is in normal operation, the oxidant source, the organic waste liquid source, the auxiliary fuel source and the softened water source all enter the reactor in a cold state. The method has the advantages of safety, reliability, continuous and stable operation, low cost, easy operation, no problem of generating coke, tar and salt by heating organic waste liquid outside the reactor, and is particularly suitable for an industrial device for continuous and stable production.
Description
Technical Field
The utility model belongs to the technical field of chemical machinery, especially, relate to supercritical water oxidation system handles organic waste liquid.
Background
The supercritical water oxidation technology has the advantages of multiple types of treatable organic wastes, high decomposition efficiency, no secondary pollution, quick reaction, high efficiency, energy conservation and the like, and has wide application prospect in the field of treatment of refractory organic wastes.
Among the prior art, supercritical water oxidation system includes that the material is sent into structure, reactor, step-down structure, vapour and liquid separator and control system, and the structure is sent into to the material includes that the oxidant sends into the pipeline, organic waste material send into the pipeline, auxiliary fuel sends into the pipeline and softened water and sends into the pipeline, and each pipeline and the reactor on correspond interface connection. The reactor is a closed double-layer container, the outer layer is a shell, the inner layer is a porous lining pipe, and the outlet of the reactor is connected with a gas-liquid separator through a pressure regulating valve. In the supercritical water oxidation system in the prior art, one or two of organic waste, auxiliary fuel and softened water are heated to a set temperature before entering a reactor, and then enter the reactor, wherein in the reactor, the organic waste and an oxidant react and release heat, so that the inside of the reactor reaches a supercritical state, and the organic waste is degraded. The reaction product is discharged from the outlet of the reactor, and the reaction product is decompressed and then enters a gas-liquid separator for separation. The pressure reducing structure is a pressure regulating valve which is connected on a pipeline between the reactor and the gas-liquid separator, and the pressure regulating valve reduces the pressure and simultaneously regulates the reaction pressure in the reactor. The oxidant is generally pure oxygen or hydrogen peroxide, and the pure oxygen comprises liquid oxygen and high-purity oxygen. The defects of the prior art are as follows:
1. when liquid oxygen is used as an oxidant, equipment such as air separation and gasification needs to be added to the system, the investment cost is high, once leakage occurs, oxygen poisoning of operators is easy to occur, and the liquid oxygen is also used as a combustion improver and has the danger of forming an explosion environment. When high-purity oxygen is used as an oxidant, the number of oxygen tanks is large, the volume is large, the investment cost is high, and the corrosion rate of equipment can be accelerated in a pure oxygen environment. When hydrogen peroxide is used as an oxidant, the operation cost is high.
2. In auxiliary fuel or organic waste liquid heated to the set temperature outside the reactor and then entered into the reactor, the auxiliary fuel or organic waste liquid is easy to be degraded in the heating process to generate coke and tar, partial salinity can be crystallized and separated out due to temperature rise, the generated coke, tar and salinity can generate the phenomenon of deposition and scaling, and the heat exchange coefficient of the heater is reduced. After long-term operation, the outlet of the heat exchanger is difficult to reach the preheating temperature, so that the system is difficult to start or cannot normally operate.
3. The water flux on the surface of the porous lining pipe is greatly influenced by the static pressure difference of a water column, and the water flux at the upper end of the lining pipe is small, so that the wall is easily dried, and the service life of equipment is influenced. The increase of the water flux of the lining pipe can relieve the dry wall phenomenon, but the effective supercritical reaction temperature is difficult to ensure, so that the system treatment effect is poor.
4. The pressure is reduced by throttling through a pressure regulating valve, salt is easily deposited on a valve sealing surface, so that the reactor is difficult to seal, and the pressure cannot be maintained; in the pressure reduction process, water is in an overheated state, a large amount of water is vaporized, cavitation erosion is caused to pipelines and valves, and the service life of a pressure reduction system is influenced.
Disclosure of Invention
The utility model aims at providing a supercritical water oxidation system overcomes prior art's is not enough.
The technical scheme of the utility model is that: a supercritical water oxidation system comprises an oxidant source, an organic waste liquid source, an auxiliary fuel source, a softened water source, an oxidant feeding adjusting device, an organic waste liquid feeding adjusting device, an auxiliary fuel feeding adjusting device, a feeding softened water adjusting device, a dividing wall water feeding adjusting device, a reactor, a pressure reducing device, a gas-liquid separator and a controller, wherein the reactor consists of an outer cylinder body and a porous body lining pipe; the device comprises an oxidant source, an organic waste liquid source, an auxiliary fuel source and a softened water source, wherein the oxidant source, the organic waste liquid source, the auxiliary fuel source and the softened water source are respectively connected with inlets of an oxidant feeding adjusting device, an organic waste liquid feeding adjusting device, an auxiliary fuel feeding adjusting device and a feeding softened water adjusting device through pipelines; the pressure reduction device is respectively connected with the outlet of the reactor and the inlet of the gas-liquid separator through pipelines, and the controller is respectively electrically connected with the organic waste liquid feeding adjusting device, the auxiliary fuel feeding adjusting device, the feeding softened water adjusting device, the dividing wall water feeding adjusting device, the reactor temperature detecting device, the reactor pressure detecting device, the organic waste liquid flow detecting device, the auxiliary fuel flow detecting device, the feeding softened water flow detecting device and the dividing wall water flow detecting device; wherein the source of oxidant is air; oxidant feeding adjusting device includes air compressor and air heater, and the air compressor export is connected through the pipeline with the air heater import, and the air compressor import is connected with the air source, and the air heater export links to each other with reactor oxidant import, is equipped with air heater export temperature-detecting device on the pipeline of air heater and reactor oxidant access connection, and the controller is connected with air heater's controller and air heater export temperature-detecting device electricity.
The utility model relates to a supercritical water oxidation system, its characterized in that: the wall thickness of the lining pipe of the reactor is 2-5 mm, the holes on the wall of the lining pipe are divided into more than two layers according to the average pore diameter, the holes are distributed in a gradient manner layer by layer, the gradient distribution manner layer by layer is that the holes are distributed in a gradient manner along the radial direction of the lining pipe or are distributed in a gradient manner along the axial direction of the lining pipe, and the gradient distribution manner along the radial direction of the lining pipe is that the average pore diameter of the holes on the wall of the pipe is reduced layer by layer from the inner layer; the gradient distribution along the axial direction of the lining pipe is that the average pore diameter of the pores on the pipe wall increases layer by layer from the bottom layer to the top layer along the axial direction of the lining pipe, the average pore diameter of the inner layer or the top layer is 5-40 mu m, the average pore diameter of the outer layer or the bottom layer is 0.2-3 mu m, and the average pore diameter of the middle layer is 2-10 mu m.
The utility model relates to a supercritical water oxidation system, its characterized in that: the pressure reduction device is a microchannel pressure reduction device, the microchannel pressure reduction device comprises a multistage connecting pipeline, a microchannel heat exchanger and a microchannel pressure reducer, the microchannel heat exchanger and the microchannel pressure reducer are connected through a pipeline, an inlet of the microchannel heat exchanger is connected with an outlet of the reactor through a multistage necking pipeline, and an outlet of the microchannel pressure reducer is connected with an inlet of the gas-liquid separator through a multistage expanding pipeline; the multi-stage necking pipeline is more than two stages, wherein the pipe diameter of the first-stage pipeline connected with the outlet of the reactor corresponds to the diameter of the outlet of the reactor, the pipe diameter of the first-stage pipeline connected with the inlet of the micro-channel heat exchanger corresponds to the diameter of the inlet of the micro-channel heat exchanger, the pipe diameters of the pipelines at all stages between the first-stage pipeline and the inlet of the micro-channel heat exchanger are gradually reduced, and the pipe diameter of the inlet of the micro-channel heat exchanger is 1/5-1/100 of the; the multistage expanding pipeline is a pipeline with more than two stages, wherein the diameter of a first-stage pipeline connected with the outlet of the microchannel pressure reducer corresponds to the diameter of the outlet of the microchannel pressure reducer, the diameter of a first-stage pipeline connected with the inlet of the gas-liquid separator corresponds to the diameter of the inlet of the gas-liquid separator, the diameters of the pipelines at all stages between the first-stage pipeline and the inlet of the gas-liquid separator are gradually increased, and the diameter of the inlet of the gas-liquid separator is 5-100 times that of the outlet of the microchannel pressure reducer.
The utility model relates to a supercritical water oxidation system, its characterized in that: the organic waste liquid feeding adjusting device, the auxiliary fuel feeding adjusting device, the feeding softened water adjusting device and the dividing wall water feeding adjusting device are any one of a variable frequency pump, or a combination of a pump and an adjusting valve, or a branch adjusting combination established on an outlet pipeline of the pump and the pump.
The utility model relates to a supercritical water oxidation system, its characterized in that: the reactor is provided with one material inlet, and a material main inlet pipe is connected to the material inlet; the outlets of the organic waste liquid feeding adjusting device, the auxiliary fuel feeding adjusting device and the feeding softened water adjusting device are connected with the reactor, and the outlets of the organic waste liquid feeding adjusting device, the auxiliary fuel feeding adjusting device and the feeding softened water adjusting device are connected with the material main inlet pipe.
The utility model relates to a supercritical water oxidation system, its characterized in that: the auxiliary fuel source is a low ignition point liquid fuel.
The utility model relates to a supercritical water oxidation system, its characterized in that: the controller is a computer controller with a built-in control program.
The utility model discloses a supercritical water oxidation system's start-up method includes the intensification of reactor and steps up, and the intensification of reactor steps up including following step:
1) starting a feeding softened water adjusting device to supply softened water into the reactor, then starting a dividing wall water feeding adjusting device to supply softened water into a dividing wall of the reactor, and then starting an air compressor to supply air into the reactor until the pressure in the reactor is stable;
2) starting an air preheater to preheat air, setting the outlet temperature of the air preheater, mixing the preheated air and feed softened water in a reactor, and heating the mixed material;
3) when the temperature in the reactor rises to be higher than the ignition point temperature of the auxiliary fuel, starting the auxiliary fuel feeding adjusting device to supply the auxiliary fuel into the reactor, and enabling the auxiliary fuel to generate oxidation reaction in the reactor to enable the temperature in the reactor to rise to the set temperature;
4) stopping the air preheater from preheating air, adjusting the feeding amount of the fed softened water, the feeding amount of the dividing wall softened water and the feeding amount of the auxiliary fuel to enable the feeding amounts of all the materials to reach the set amount of the supercritical working condition, and then adjusting the feeding amounts of the fed softened water and the dividing wall softened water, so as to maintain the supercritical working condition in the reactor and stably run;
5) starting the organic waste liquid feeding adjusting device to supply organic waste liquid to the reactor, and adjusting the feeding amount of the organic waste liquid, the feeding amount of the auxiliary fuel and the feeding amount of the feeding softened water in due time according to the heat value of the organic waste liquid to keep the supercritical working condition in the reactor until the organic waste liquid feeding reaches the normal operation state of the system, and finishing the starting.
According to the calorific value of the organic waste liquid, timely adjusting comprises adjusting when the calorific value of the organic waste liquid is lower than the self-heating requirement of a system and adjusting when the calorific value of the organic waste liquid is higher than the self-heating requirement of the system, wherein the adjusting when the calorific value of the organic waste liquid is lower than the self-heating requirement of the system comprises the following steps: adjusting the feeding amount of the fed softened water to be closed, adjusting the feeding amount of the auxiliary fuel and the feeding amount of the organic waste liquid, and maintaining the supercritical working condition in the reactor; when the calorific value of the organic waste liquid is higher than the self-heating requirement of the system, the regulation is as follows: and adjusting the feeding amount of the auxiliary fuel to be closed, adjusting the feeding amount of the organic waste liquid and the feeding amount of the feeding softened water, and maintaining the supercritical working condition in the reactor.
Setting the outlet temperature of an air preheater to be 300-600 ℃; the temperature set in the reactor in the step 3) is 400-700 ℃, the supercritical working condition in the reactor comprises temperature and pressure, the temperature of the supercritical working condition is 400-700 ℃, and the pressure of the supercritical working condition is 230-250 bar.
The principle of the utility model is that: organic waste liquid, auxiliary fuel, demineralized water join a house steward entering reactor after organic waste liquid charge pump, auxiliary fuel charge pump and feeding softened water pump boost respectively, and during the start-up, the air is boosted through air compressor and is preheated the back with air heater and get into the reactor, forms supercritical water oxidation environment in the reactor, and during normal operating, the air is boosted through air compressor and is not preheated cold state and get into the reactor, makes the oxygen in the air and organic waste liquid react. The temperature and pressure in the reactor are maintained by adjusting the flow of the auxiliary fuel, the feed softened water, the organic waste liquid and the partition wall softened water, when the oxidation reaction heat value of the organic waste liquid is lower than the heat required by the supercritical water oxidation environment, the reaction temperature is maintained by adjusting the amount of the auxiliary fuel, otherwise, the reaction temperature is maintained by adjusting the amount of the organic waste liquid. Softened water of the partition walls enters a gap between the wall of the reactor and the lining pipe, and the softened water of the partition walls permeates into the inner wall of the lining pipe through holes in the pipe wall of the lining pipe to form a water film or a gas film on the inner wall of the lining pipe, so that the corrosion of equipment is slowed down, and the salt deposition is avoided.
The product of the reaction of oxygen and organic waste liquid is weakened into a subcritical state at the bottom of the reactor, enters a pressure reducing device through a pipeline at a discharge port, the material after temperature reduction and pressure reduction enters a gas-liquid separator, a liquid phase is discharged through the bottom of the gas-liquid separator, and a gas phase is discharged through the top after small liquid drops are removed through a demister.
The utility model has the advantages that:
1. air is used as an oxidant for supercritical water oxidation reaction, so that the investment cost can be reduced, oxygen poisoning of operators due to pure oxygen leakage can be avoided, the air raw material cost is zero, and the operation cost is greatly reduced.
2. The organic waste liquid enters the reactor to react at normal temperature, so that the defects of low heat transfer efficiency of a heat exchanger, difficulty in system starting and the like caused by high-temperature coking and salt scaling of organic matters in the heating process of the organic waste liquid are avoided.
3. The reactor lining pipe adopts a gradient design porous composite form, and can provide proper flux, so that the influence of static pressure difference can be reduced, the liquid distribution is more uniform, the dry wall is avoided, and the energy consumption of the system can be reduced.
4. The micro-channel structure form adopted by the pressure reduction device reduces the temperature and the pressure of the fluid in the pressure reduction device and avoids
The vaporization caused by overheating of liquid water in the pressure reduction process is avoided, so that the pressure reduction process is more stable, the sealing failure of the valve can be avoided, and the stable operation of the system is ensured.
5. The utility model provides a supercritical water oxidation device possesses safe and reliable, can continuous stable operation, running cost low, the characteristics of easily operation, the continuous stable production requirement of specially adapted industrialization device.
Drawings
Fig. 1 is a schematic structural diagram of a supercritical water oxidation system.
FIG. 2 is a schematic diagram of a reactor structure of a supercritical water oxidation system.
FIG. 3 is a schematic view of the structure of the lining pipe with radial gradient distribution of pore diameter.
Fig. 4 is a top view of fig. 3.
FIG. 5 is a schematic view of the structure of the lining tube with the axial gradient distribution of the pore diameter.
Fig. 6 is a schematic structural diagram of the pressure reduction device.
In the figure, 1, organic waste liquid source, 2, auxiliary fuel source, 3, softened water source, 4, organic waste liquid feed adjusting device, 5, auxiliary fuel feed adjusting device, 6, feed softened water adjusting device, 7, partition wall water feed adjusting device, 8, air compressor, 9, reactor, 901, high temperature bolt, 902, pressure ring, 903, gasket, 904, upper end cover, 905, reactor outer cylinder, 906, lining pipe, 907, lower end cover, 908, inner layer, 909, radial middle layer, 910, outer layer, 911, bottom layer, 912, axial middle layer, 913, top layer, 10, pressure reducing device, 10-1, microchannel heat exchanger, 10-2, microchannel pressure reducer, 11, gas-liquid separator, 12, air preheater, 13, oxidant source, 14, reactor gas outlet, 15, reactor liquid outlet, 16, reactor temperature detecting device, 17. the device comprises a reactor pressure detection device, an air preheater outlet temperature detection device, an organic waste liquid flow detection device, an auxiliary fuel flow detection device, a feeding softened water flow detection device, a partition wall water flow detection device and a controller, wherein the reactor pressure detection device 18, the air preheater outlet temperature detection device 19, the organic waste liquid flow detection device 20, the auxiliary fuel flow detection device 21, the feeding softened water flow detection device 22, the partition.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
The supercritical water oxidation system comprises an oxidant source 13, an organic waste liquid source 1, an auxiliary fuel source 2, a softened water source 3, an oxidant feeding adjusting device, an organic waste liquid feeding adjusting device 4, an auxiliary fuel feeding adjusting device 5, a feeding softened water adjusting device 6, a dividing wall water feeding adjusting device 7, a reactor 9, a pressure reduction device 10, a gas-liquid separator 11 and a controller 23, wherein the reactor 9 consists of an outer cylinder body and a porous lining pipe, the top of the reactor 9 is provided with an oxidant inlet and a material inlet, the material inlet on the reactor 9 is one, the material inlet is connected with a material main inlet pipe, the upper part or the side surface of the reactor is provided with a dividing wall softened water inlet, and the bottom of the reactor is provided with a reactor outlet; an oxidant source 13, an organic waste liquid source 1, an auxiliary fuel source 2 and a softened water source 3 are respectively connected with inlets of an oxidant feeding adjusting device, an organic waste liquid feeding adjusting device 4, an auxiliary fuel feeding adjusting device 5 and a feeding softened water adjusting device 6 through pipelines, outlets of the oxidant feeding adjusting device, the organic waste liquid feeding adjusting device 4, the auxiliary fuel feeding adjusting device 5 and the feeding softened water adjusting device 6 are connected with a material main feeding pipe of a material inlet of a reactor 9, the softened water source 3 is also connected with a partition wall softened water feeding adjusting device 7 and a partition wall softened water inlet of the reactor 9, the organic waste liquid feeding adjusting device 4, the auxiliary fuel feeding adjusting device 5, the feeding softened water adjusting device 6 and the partition wall water feeding adjusting device 7 are frequency conversion pumps, or are combined with adjusting valves, or are combined with branch adjusting devices established on outlet pipelines of the pumps and the pumps, a reactor temperature detection device 16 and a reactor pressure detection device 17 for detecting the temperature and the pressure in the reactor are arranged on the reactor 9; the pressure reduction device 10 is respectively connected with a reactor outlet and an inlet of the gas-liquid separator 11 through pipelines, and the controller 23 is respectively electrically connected with the organic waste liquid feeding adjusting device 4, the auxiliary fuel feeding adjusting device 5, the feeding softened water adjusting device 6, the dividing wall water feeding adjusting device 7, the reactor temperature detecting device 16, the reactor pressure detecting device 17, the organic waste liquid flow detecting device 19, the auxiliary fuel flow detecting device 20, the feeding softened water flow detecting device 21 and the dividing wall water flow detecting device 22; the oxidant source 13 is air; oxidant feeding adjusting device includes air compressor 8 and air heater 12, 8 exports of air compressor and air heater 12 import and is connected through the pipeline, 8 imports of air compressor are connected with the air source, 12 exports of air heater link to each other with 9 oxidant imports of reactor, be equipped with air heater export temperature-detecting device 18 on the pipeline of air heater 12 and reactor oxidant access connection, controller 23 is connected with air heater 12's controller and air heater export temperature-detecting device 18 electricity. The auxiliary fuel source 2 is a low-ignition-point liquid fuel. The controller is a computer controller with a built-in control program.
The wall thickness of the lining pipe 906 of the reactor 9 is 2-5 mm, the holes on the pipe wall of the lining pipe 906 are divided into more than two layers according to the average pore diameter, the holes are distributed in a gradient manner layer by layer, the gradient distribution manner layer by layer is that the holes are distributed in a gradient manner along the radial direction of the lining pipe or are distributed in a gradient manner along the axial direction of the lining pipe, and the gradient distribution manner along the radial direction of the lining pipe is that the average pore diameter of the holes on the pipe wall is reduced layer by layer from the inner layer 908; the gradient distribution along the axial direction of the lining pipe is that the average pore diameter of pores on the pipe wall increases from the bottom layer 911 to the top layer by layer along the axial direction of the lining pipe, the average pore diameter of the inner layer 908 or the top layer 913 is 5-40 μm, the average pore diameter of the outer layer 910 or the bottom layer 911 is 0.2-3 μm, and the average pore diameter of the middle layers 909 and 912 is 2-10 μm.
The pressure reduction device 10 is a microchannel pressure reduction device, the microchannel pressure reduction device comprises a multistage connecting pipeline, a microchannel heat exchanger 10-1 and a microchannel pressure reducer 10-2, the microchannel heat exchanger 10-1 and the microchannel pressure reducer 10-2 are connected through a pipeline, an inlet of the microchannel heat exchanger is connected with an outlet of a reactor through a multistage necking pipeline, and an outlet of the microchannel pressure reducer 10-2 is connected with an inlet of a gas-liquid separator 11 through a multistage expanding pipeline; the multi-stage necking pipeline is more than two stages, wherein the pipe diameter of the first-stage pipeline connected with the outlet of the reactor corresponds to the diameter of the outlet of the reactor, the pipe diameter of the first-stage pipeline connected with the inlet of the micro-channel heat exchanger corresponds to the diameter of the inlet of the micro-channel heat exchanger, the pipe diameters of the pipelines at all stages between the first-stage pipeline and the inlet of the micro-channel heat exchanger are gradually reduced, and the pipe diameter of the inlet of the micro-channel heat exchanger is 1/5-1/100 of; the multistage expanding pipeline is a pipeline with more than two stages, wherein the diameter of a first-stage pipeline connected with the outlet of the microchannel pressure reducer corresponds to the diameter of the outlet of the microchannel pressure reducer, the diameter of a first-stage pipeline connected with the inlet of the gas-liquid separator corresponds to the diameter of the inlet of the gas-liquid separator, the diameters of the pipelines at all stages between the first-stage pipeline and the inlet of the gas-liquid separator are gradually increased, and the diameter of the inlet of the gas-liquid separator is 5-100 times that of the outlet of the microchannel pressure.
The starting method of the supercritical water oxidation system comprises the temperature and pressure rise of the reactor 9, and the temperature and pressure rise of the reactor 9 comprises the following steps:
1) starting a feeding softened water adjusting device 6 to supply softened water into a reactor 9, then starting a dividing wall water feeding adjusting device 7 to supply softened water into a dividing wall of the reactor 9, and then starting an air compressor 8 to supply air into the reactor 9 until the pressure in the reactor is stable;
2) starting the air preheater 12, setting the outlet temperature of the air preheater to be 300-600 ℃, mixing the preheated air and the feed softened water in the reactor, and heating the mixed material;
3) when the temperature in the reactor 9 rises to be higher than the ignition temperature of the auxiliary fuel, starting the auxiliary fuel feeding adjusting device 5 to supply the auxiliary fuel into the reactor 9, and enabling the auxiliary fuel to generate oxidation reaction in the reactor 9 to enable the temperature in the reactor to rise to a set temperature, wherein the set temperature is 400-700 ℃;
4) stopping the air preheater 12 from preheating air, adjusting the feeding amount of the fed softened water, the feeding amount of the dividing wall softened water and the feeding amount of the auxiliary fuel to ensure that the feeding amount of each material reaches the maintaining amount of the supercritical working condition, and no longer adjusting the feeding amount of the fed softened water and the dividing wall softened water to maintain the supercritical working condition in the reactor and stably operate, wherein the temperature of the supercritical working condition is 400-700 ℃, and the pressure of the supercritical working condition is 230-250 bar;
5) starting the organic waste liquid feeding adjusting device 4 to supply organic waste liquid to the reactor 9, and adjusting the feeding amount of the organic waste liquid, the feeding amount of the auxiliary fuel and the feeding amount of the feeding softened water in due time according to the heat value of the organic waste liquid to keep the supercritical working condition in the reactor until the organic waste liquid feeding reaches the normal operation maintenance amount of the system, and finishing the starting. The timely regulation comprises regulation when the calorific value of the organic waste liquid is lower than the self-heating requirement of the system and regulation when the calorific value of the organic waste liquid is higher than the self-heating requirement of the system, wherein the regulation when the calorific value of the organic waste liquid is lower than the self-heating requirement of the system is as follows: adjusting the feeding amount of the fed softened water to be closed, adjusting the feeding amount of the auxiliary fuel and the feeding amount of the organic waste liquid, and maintaining the supercritical working condition in the reactor; when the calorific value of the organic waste liquid is higher than the self-heating requirement of the system, the regulation is as follows: and adjusting the feeding amount of the auxiliary fuel to be closed, adjusting the feeding amount of the organic waste liquid and the feeding amount of the feeding softened water, and maintaining the supercritical working condition in the reactor.
The normal operation of the system is carried out by the control system according to a set program.
When the machine is stopped, the organic waste liquid feeding adjusting device 4 is adjusted to slowly reduce the feeding amount of the organic waste liquid to zero, then the auxiliary fuel feeding adjusting device 5 is stopped, after 0-10min, the reactor 9 is cooled to normal temperature, the feeding softened water adjusting device 6 and the dividing wall softened water feeding adjusting device 7 are stopped, the air compressor 8 is closed, and the power supply is closed.
Example 1
The organic waste liquid adjusting device 4, the auxiliary fuel adjusting device 5, the feeding softened water adjusting device 6 and the dividing wall water feeding adjusting device 7 are in a pump and adjusting valve combined form; the porous lining pipe 906 of the reactor 9 is a lining pipe with an average pore diameter of three layers distributed in a gradient manner in the radial direction, and the length of the lining pipe is 2 meters; the multistage pipe section of the pressure reducing device 10 is a ten-stage pipe section, wherein a five-stage reducing and reducing pipeline is arranged between the outlet of the reactor and the inlet of the microchannel heat exchanger, and a five-stage reducing and enlarging pipeline is arranged between the outlet of the microchannel pressure reducer and the inlet of the gas-liquid separator; the micro-channel heat exchanger 10-1 and the micro-channel pressure reducer 10-2 are a single-channel type micro-channel heat exchanger and a single-channel type micro-channel pressure reducer.
Example 2
The organic waste liquid adjusting device 4, the auxiliary fuel adjusting device 5, the feeding softened water adjusting device 6 and the dividing wall water feeding adjusting device 7 are in the form of variable frequency pumps; the porous lining pipe 906 of the reactor 9 is a lining pipe with an average pore diameter of axial three-layer gradient distribution, and the length of the lining pipe is 2 meters; the multistage pipe section of the pressure reducing device 10 is a ten-stage pipe section, wherein a five-stage reducing and reducing pipeline is arranged between the outlet of the reactor and the inlet of the microchannel heat exchanger, and a five-stage reducing and enlarging pipeline is arranged between the outlet of the microchannel pressure reducer and the inlet of the gas-liquid separator; the micro-channel heat exchanger 10-1 and the micro-channel pressure reducer 10-2 are a multi-channel micro-channel heat exchanger and a single-channel micro-channel pressure reducer.
Claims (7)
1. A supercritical water oxidation system comprises an oxidant source (13), an organic waste liquid source (1), an auxiliary fuel source (2), a softened water source (3), an oxidant feeding adjusting device, an organic waste liquid feeding adjusting device (4), an auxiliary fuel feeding adjusting device (5), a feeding softened water adjusting device (6), a dividing wall water feeding adjusting device (7), a reactor (9), a pressure reducing device (10), a gas-liquid separator (11) and a controller (23), wherein the reactor (9) consists of an outer cylinder body and a porous body lining pipe, the top of the reactor (9) is provided with an oxidant inlet and a material inlet, the upper part or the side surface of the reactor is provided with a dividing wall softened water inlet, and the bottom of the reactor is provided with a reactor discharge port; an oxidant source (13), an organic waste liquid source (1), an auxiliary fuel source (2) and a softened water source (3) are respectively connected with inlets of an oxidant feeding adjusting device, an organic waste liquid feeding adjusting device (4), an auxiliary fuel feeding adjusting device (5) and a feeding softened water adjusting device (6) through pipelines, outlets of the oxidant feeding adjusting device, the organic waste liquid feeding adjusting device (4), the auxiliary fuel feeding adjusting device (5) and the feeding softened water adjusting device (6) are connected with a material inlet of a reactor (9), the softened water source (3) is also connected with a dividing wall softened water inlet of the reactor (9) through a dividing wall water feeding adjusting device (7), and a reactor temperature detecting device (16) and a reactor pressure detecting device (17) for detecting the temperature and the pressure in the reactor are arranged on the reactor (9); the pressure reduction device (10) is respectively connected with a reactor outlet and an inlet of a gas-liquid separator (11) through pipelines, and the controller (23) is respectively electrically connected with an organic waste liquid feeding adjusting device (4), an auxiliary fuel feeding adjusting device (5), a feeding softened water adjusting device (6), a dividing wall water feeding adjusting device (7), a reactor temperature detecting device (16), a reactor pressure detecting device (17), an organic waste liquid flow detecting device (19), an auxiliary fuel flow detecting device (20), a feeding softened water flow detecting device (21) and a dividing wall water flow detecting device (22); characterized in that the source of oxidant (13) is air; oxidant feed adjusting device includes air compressor (8) and air heater (12), and air compressor (8) export and air heater (12) import are connected through the pipeline, and air compressor (8) import is connected with the air source, and air heater (12) export links to each other with reactor (9) oxidant import, is equipped with air heater export temperature detection device (18) on air heater (12) and reactor oxidant access connection's pipeline, and controller (23) are connected with air heater (12) controller and air heater export temperature detection device (18) electricity.
2. The supercritical water oxidation system of claim 1, wherein: the wall thickness of a lining pipe (906) of the reactor (9) is 2-5 mm, holes in the wall of the lining pipe (906) are divided into more than two layers according to the average pore diameter, the holes are distributed in a gradient manner layer by layer, the gradient distribution manner layer by layer is in radial gradient distribution along the lining pipe or in axial gradient distribution along the lining pipe, and the gradient distribution manner along the radial direction of the lining pipe is that the average pore diameter of the holes in the wall of the pipe is gradually reduced layer by layer from an inner layer (908) to the outside along the radial direction of the lining pipe; the average pore diameter of the pores on the pipe wall is gradually increased from the bottom layer (911) to the top layer along the axial direction of the lining pipe, the average pore diameter of the inner layer (908) or the top layer (913) is 5-40 mu m, the average pore diameter of the outer layer (910) or the bottom layer (911) is 0.2-3 mu m, and the average pore diameter of the middle layers (909, 912) is 2-10 mu m.
3. The supercritical water oxidation system of claim 2, wherein: the pressure reduction device (10) is a microchannel pressure reduction device, the microchannel pressure reduction device comprises a multistage connecting pipeline, a microchannel heat exchanger (10-1) and a microchannel pressure reducer (10-2), the microchannel heat exchanger (10-1) is connected with the microchannel pressure reducer (10-2) through a pipeline, an inlet of the microchannel heat exchanger is connected with an outlet of a reactor through a multistage necking pipeline, and an outlet of the microchannel pressure reducer (10-2) is connected with an inlet of a gas-liquid separator (11) through a multistage expanding pipeline; the multi-stage necking pipeline is more than two stages, wherein the pipe diameter of the first-stage pipeline connected with the outlet of the reactor corresponds to the diameter of the outlet of the reactor, the pipe diameter of the first-stage pipeline connected with the inlet of the micro-channel heat exchanger corresponds to the diameter of the inlet of the micro-channel heat exchanger, the pipe diameters of the pipelines at all stages between the first-stage pipeline and the inlet of the micro-channel heat exchanger are gradually reduced, and the pipe diameter of the inlet of the micro-channel heat exchanger is 1/5-1/100 of the; the multistage expanding pipeline is a pipeline with more than two stages, wherein the diameter of a first-stage pipeline connected with the outlet of the microchannel pressure reducer corresponds to the diameter of the outlet of the microchannel pressure reducer, the diameter of a first-stage pipeline connected with the inlet of the gas-liquid separator corresponds to the diameter of the inlet of the gas-liquid separator, the diameters of the pipelines at all stages between the first-stage pipeline and the inlet of the gas-liquid separator are gradually increased, and the diameter of the inlet of the gas-liquid separator is 5-100 times that of the outlet of the microchannel pressure reducer.
4. The supercritical water oxidation system of claim 3, wherein: the reactor (9) is provided with one material inlet, and the material inlet is connected with a material main inlet pipe; the outlets of the organic waste liquid feeding adjusting device (4), the auxiliary fuel feeding adjusting device (5) and the feeding softened water adjusting device (6) are connected with the reactor (9), and the outlets of the organic waste liquid feeding adjusting device (4), the auxiliary fuel feeding adjusting device (5) and the feeding softened water adjusting device (6) are connected with a material main inlet pipe.
5. The supercritical water oxidation system of claim 4, wherein: the organic waste liquid feeding adjusting device (4), the auxiliary fuel feeding adjusting device (5), the feeding softened water adjusting device (6) and the dividing wall water feeding adjusting device (7) are any one of a variable frequency pump, or a combination of a pump and an adjusting valve, or a branch adjusting combination established on an outlet pipeline of the pump and the pump.
6. The supercritical water oxidation system of claim 5, wherein: the auxiliary fuel source (2) is a low ignition point liquid fuel.
7. The supercritical water oxidation system of claim 6, wherein: the controller is a computer controller with a built-in control program.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111003793A (en) * | 2019-12-26 | 2020-04-14 | 一重集团大连工程技术有限公司 | Supercritical water oxidation system and starting method |
| CN115501817A (en) * | 2022-09-29 | 2022-12-23 | 一重集团大连工程技术有限公司 | Supercritical water oxidation reactor control system and method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111003793A (en) * | 2019-12-26 | 2020-04-14 | 一重集团大连工程技术有限公司 | Supercritical water oxidation system and starting method |
| CN115501817A (en) * | 2022-09-29 | 2022-12-23 | 一重集团大连工程技术有限公司 | Supercritical water oxidation reactor control system and method |
| CN115501817B (en) * | 2022-09-29 | 2024-01-30 | 一重集团大连工程技术有限公司 | Supercritical water oxidation reactor control system and method |
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