WO2022116633A1 - 一种有机固废湿式氧化处理系统及其处理工艺 - Google Patents

一种有机固废湿式氧化处理系统及其处理工艺 Download PDF

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Publication number
WO2022116633A1
WO2022116633A1 PCT/CN2021/117727 CN2021117727W WO2022116633A1 WO 2022116633 A1 WO2022116633 A1 WO 2022116633A1 CN 2021117727 W CN2021117727 W CN 2021117727W WO 2022116633 A1 WO2022116633 A1 WO 2022116633A1
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sludge
reaction
pipeline
wet oxidation
mud
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PCT/CN2021/117727
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English (en)
French (fr)
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孟继安
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清华大学
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C02F11/08—Wet air oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/06—Treatment of sludge; Devices therefor by oxidation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/20—Sludge processing

Definitions

  • the invention relates to the technical field of organic solid waste treatment, in particular to an organic solid waste wet oxidation treatment system and a treatment process thereof.
  • Organic solid waste refers to solid and semi-solid organic wastes that pollute the environment generated by human beings in production and living activities.
  • Organic solid waste generally includes municipal sludge, industrial sludge, kitchen waste, domestic waste, especially wet waste, River bottom sludge, high-concentration organic waste liquid, feces, etc., the sludge made from organic solid waste has similar chemical and physical properties to municipal sludge, and similar treatment processes and technologies for municipal sludge can be used.
  • organic solid waste mud for short.
  • the sludge wet oxidation treatment process has the advantages of no three wastes (gas-liquid-solid) discharge and easy resource utilization, and may become the mainstream treatment technology in the future, but this process technology also has the following problems or deficiencies Need to further improve and develop:
  • the wet oxidation reaction needs to be carried out in a high temperature and high pressure liquid phase.
  • the temperature of the sludge in the reactor is 160-370 °C and the pressure is 1.8-5.4MPa.
  • the gas After the gas is exhausted, it enters the heat exchanger to transfer the heat to the low-temperature sludge before wet oxidation, and the sludge after the cooling reaction enters the flash tank for flash cooling. Therefore, there are two problems or deficiencies in the process: first, the energy of the discharged high-temperature and high-pressure gas cannot be recovered with high quality; second, the sludge pressure at the outlet of the heat exchanger is still high, and it is necessary to adjust the valve opening on the pipeline connected to the flash tank.
  • reaction gas can be retained in the high-temperature reacted sludge and flow through the heat exchanger, on the one hand, the heat energy of the reaction gas can be recovered, and on the other hand, the pressure drop of the reacted sludge in the heat exchanger can be appropriately increased , greatly reduce the pressure of the reacted sludge discharged from the heat exchanger, so that the life of its control valve can be greatly extended, and on the other hand, the reaction gas can be used to strengthen the sludge heat exchange, which can serve multiple purposes.
  • the current wet oxidation process technology discharges the wet oxidation sludge into the flash tank for cooling and pressure relief, and after cooling with cooling water, all of it is sent to dehydration.
  • the initial precipitation sewage (supernatant liquid, containing a small amount of solid phase) is returned to the sludge before the reaction to improve the fluidity of the sludge before the reaction, instead of the conventional use of the sewage to dehydrate the reaction sludge.
  • the fluidity can be called "raw mud water injection conditioning process", which can greatly reduce the dewatering amount and dewatering energy consumption of the sludge after the reaction.
  • the initial precipitation of the mud can also reduce the water injection energy consumption of the raw mud water injection conditioning process.
  • the post-reaction sludge storage tank can be used to store pressure energy and post-reaction sludge pre-precipitation, and the pre-precipitated supernatant can be reinjected for the raw mud water injection conditioning process, which can not only greatly reduce the post-reaction sludge It can reduce the amount of dehydration and energy consumption of dehydration, and can also reduce the energy consumption of water injection in the water injection conditioning process of raw mud.
  • the current wet oxidation process technology mainly adopts the intermediate medium (water or oil) circulating heat exchange technology to recover the heat of the high-temperature sludge, that is, the heat of the high-temperature sludge is transferred to the low-temperature sludge through the medium water or oil in the intermediate circuit.
  • the heat transfer increases the heat transfer resistance, resulting in poor heat transfer effect and relatively high process energy consumption. If the sludge-sludge direct and efficient heat exchange can be achieved, significant energy-saving effects will be obtained.
  • the present invention provides a wet oxidation treatment system for organic solid waste.
  • a large amount of process water injection, the sludge and process water injection are initially mixed and then enter the pipeline sludge heat exchanger and the subsequent pipeline reactor, which saves the process and phase of the current conventional process of setting a conditioning tank for full stirring and conditioning.
  • Corresponding energy consumption control the pressure drop of the reaction sludge in the pipeline sludge heat exchanger by controlling the proportion of the reaction gas retained in the pipeline sludge heat exchanger, so as to realize the sludge in the reaction process in the pipeline reactor.
  • the pressure energy of the reaction mud in the mud pressure storage tank, and the reaction mud pressure storage tank is used to carry out preliminary sedimentation and stratification of the reacted sludge, so that the heavy components in the reacted sludge settle at the bottom of the reaction mud pressure storage tank and the light components
  • the sewage (supernatant) is in the upper part of the reaction mud pressure storage tank, on the one hand, it can reduce the pressure adjustment range and amplitude of the pressure regulating valve of the reaction mud entering the reaction mud pressure storage tank, and improve the life of the regulating valve and the process stability and reliability.
  • the pressure energy can be used in the subsequent reaction sludge dehydration process (as the follow-up reaction sludge dehydration transmission power), and the sewage at the upper part of the reaction sludge pressure storage tank, that is, the supernatant, can be added to the original sludge as process water injection , that is, using the pressure energy of the reaction mud pressure storage tank and the primary sedimentation effect of the reacted sludge to realize the raw mud water injection conditioning process, which can greatly reduce the energy consumption of the reaction mud dehydration and save the pump power consumption of the raw mud water injection process;
  • the present invention also provides a treatment process using the above-mentioned organic solid waste wet oxidation treatment system, which has all the characteristics of the treatment system.
  • the present invention provides a wet oxidation treatment system for organic solid waste, including a sludge storage tank, a pipeline type self-heat exchange and reaction assembly, a reaction sludge pressure storage tank, a mechanical dehydration unit, a sewage tank and a sludge pump ;
  • the sludge storage tank is used to store the organic solid waste sludge to be treated
  • the sludge pump is arranged on the conveying pipeline between the sludge storage tank and the pipeline type self-heat exchange and reaction assembly, and the sludge pump is used for pumping the organic solid waste sludge in the sludge storage tank to the pipeline type.
  • Self-heat exchange and reaction assembly components and preliminarily mix organic solid waste sludge with process water injection by mixing water to form mud-water mixed sludge;
  • the pipeline type self-heat exchange and reaction collection assembly includes pipeline type sludge heat exchanger for mud-sludge heat exchange, pipeline type sludge reactor for wet oxidation reaction, gas-liquid separator and mud gas static mixing device;
  • the pipeline type sludge heat exchanger includes a first heat exchange pipeline for the flow of mixed sludge with mud and water, and a second heat exchange pipeline for the flow of high-temperature sludge after wet oxidation of part of the exhaust gas.
  • Heat exchange is performed between the heat exchange pipeline and the second heat exchange pipeline to convert the mud-water mixed sludge and the high-temperature sludge after partial exhaust wet oxidation into high-temperature sludge before wet oxidation and low-temperature sludge under pressure after wet oxidation, respectively.
  • the pipeline sludge reactor includes a reaction pipeline, the reaction pipeline is connected in series between the outlet of the first heat exchange pipeline and the inlet of the second heat exchange pipeline, and the mud gas static mixer is arranged in the first heat exchange pipeline.
  • a pipeline between the heat exchange pipeline and the reaction pipeline is used to add the oxidant required for the wet oxidation reaction in the high temperature sludge before the wet oxidation reaction to obtain the high temperature sludge before the wet oxidation with the oxidant added;
  • the reaction pipeline is used for receiving the high temperature sludge before wet oxidation with oxidant added and through wet oxidation reaction to obtain the high temperature sludge after wet oxidation;
  • the gas-liquid separator is arranged on the pipeline between the reaction pipeline and the second heat exchange pipeline, and is used for controllable separation and discharge of the reaction gas in the high-temperature sludge after wet oxidation, so as to form a partial exhaust wet type.
  • the reaction sludge pressure storage tank is used for receiving the wet-oxidized low-temperature sludge under pressure generated by the second heat exchange pipeline, and performing exhaust and depressurization to obtain the wet-oxidized sludge;
  • the mechanical dewatering unit is used to receive and dewater the wet oxidized sludge
  • the sewage tank is used for receiving and storing sewage discharged from the mechanical unit.
  • reaction gas absorption tank is further included, and the reaction gas absorption tank is used for receiving the reaction gas separated by the gas-liquid separator and the reaction gas discharged from the reaction mud pressure storage tank.
  • the muddy water static mixer is arranged on the conveying pipeline between the sludge pump and the pipeline type self-heat exchange and reaction assembly, and is used to realize the mixing between the organic solid waste mud and the process water injection. Mix again.
  • It is further arranged as follows: it also includes an oxygen-enriched air unit, which prepares oxygen-enriched air, is connected with the mud gas static mixer, and injects the oxygen-enriched air into the mud gas static mixer and passes through the mud gas static mixer. After mixing, it is injected into the pipeline sludge reactor to participate in the wet oxidation reaction.
  • an oxygen-enriched air unit which prepares oxygen-enriched air, is connected with the mud gas static mixer, and injects the oxygen-enriched air into the mud gas static mixer and passes through the mud gas static mixer. After mixing, it is injected into the pipeline sludge reactor to participate in the wet oxidation reaction.
  • a pulverizer is further included, and the pulverizer is arranged on the conveying pipeline between the sludge pump and the pipeline-type self-heat exchange and reaction assembly, and is used for shearing and crushing the mud-water mixed sludge.
  • the reaction mud pressure storage tank is provided with a floating suction unit, the floating suction unit floats on the upper part of the supernatant liquid layered above the reaction mud pressure storage tank and discharges the supernatant liquid through the connecting pipeline.
  • the pipeline type self-heat exchange and reaction assembly assembly further comprises a heater, and the heater is used for heating the pipeline type sludge reactor to control the temperature of the wet oxidation reaction.
  • a plurality of mixed swirl structures are arranged in the first heat exchange pipeline and/or the second heat exchange pipeline and/or the reaction pipeline.
  • first heat exchange pipeline and the second heat exchange pipeline of the pipeline sludge heat exchanger are arranged in a serpentine structure
  • reaction pipelines of the pipeline sludge reactor are arranged in a meandering structure.
  • the process water injection modified by mixing water with the organic solid waste mud includes at least the supernatant liquid in the reaction mud pressure storage tank and/or the reinjection sewage from the sewage tank.
  • process water injection is injected into the organic solid waste sludge through the pipeline and equipment between the sludge storage tank and the pipeline type self-heat exchange and reaction aggregate assembly.
  • the present invention also provides a process for wet oxidation treatment of organic solid waste, comprising the following steps:
  • Step 1 The organic solid waste sludge is mixed with process water injection to form a mud-water mixed sludge
  • the organic solid waste sludge from the sludge storage tank is initially mixed with the process water injection to prepare the first mud-water mixed sludge;
  • Step 2 Sludge heats up in the pipeline sludge heat exchanger
  • the low-temperature mud-water mixed sludge and the high-temperature sludge after wet oxidation of part of the exhaust gas flowing out of the pipeline sludge reactor are exchanged for heat, so that the low-temperature mud-water mixed sludge is heated to form It is high temperature sludge before wet oxidation, and part of exhaust gas is cooled down after wet oxidation to form low temperature sludge under pressure after wet oxidation;
  • Step 3 Add wet oxidation oxidant
  • the high temperature sludge before wet oxidation is mixed with the oxidant through a mud gas static mixer to form the high temperature sludge before wet oxidation with oxidant added;
  • Step 4 Sludge is reacted in the pipeline sludge reactor
  • the high temperature sludge before wet oxidation with oxidant added is subjected to wet oxidation reaction in a pipeline sludge reactor to obtain high temperature sludge after wet oxidation;
  • Step 5 Partial exhaust of reactive gas and system pressure regulation
  • the high temperature sludge is separated from gas and liquid by a gas-liquid separator, and part of the reaction gas is controlled and discharged, so as to obtain part of the exhaust high temperature sludge after wet oxidation;
  • Step 6 Cool the reaction mud
  • the high-temperature sludge flows into the second heat exchange pipeline of the pipeline sludge heat exchanger, and exchanges heat with the low-temperature sewage mixed sludge in the first heat exchange pipeline to cool down, so as to convert into wet type sludge.
  • Step 7 Sludge storage in reaction mud pressure storage tank, pressure energy storage and system pressure regulation
  • the low-temperature sludge under pressure enters the reaction sludge pressure storage tank for storage to obtain wet oxidation sludge, and the reaction gas is precipitated in the reaction sludge pressure storage tank, and the pressure energy is stored;
  • Step 8 Sludge Dewatering
  • the sludge After wet oxidation, the sludge is subjected to solid-liquid separation and dehydration through a mechanical dehydration unit.
  • the process water injected by the sludge pump in step 1 comes at least partially from the reinjected sewage from the sewage tank and/or the supernatant of the reaction sludge pressure storage tank.
  • step 1 the method further includes mixing the first mud-water mixed sludge with water again through a mud-water static mixer to obtain a second mud-water mixed sludge.
  • step 1 also includes shearing and crushing the first mud-water mixed sludge by a pulverizer.
  • step 4 it also includes heating the pipeline sludge reactor through a heater to control the temperature of the wet oxidation reaction.
  • step 5 the proportion of reaction gas separated and discharged by the gas-liquid separator is 0-50%.
  • step 7 the method further includes pumping the supernatant liquid layered above the reaction sludge pressure storage tank through the flotation suction unit and supplying at least part of the supernatant to the sludge pump.
  • step 8 the method further includes receiving and storing the sewage discharged from the mechanical dewatering unit through the sewage tank and supplying at least part of the sewage to the sludge pump through the injection pump.
  • the present invention has the following advantages:
  • the sludge to be treated is organic solid waste sludge with high solid content.
  • a certain proportion of sewage is mixed with the sludge-water static mixer and/or the pre-stage sludge pump and/or the pre-stage conveying pipeline, and the sludge is passed through the sludge-water static mixer. After preliminary mixing by the mixer or the pre-stage sludge pump, it enters the serpentine pipeline channel of the pipeline sludge heat exchanger and the subsequent pipeline sludge reactor for full mixing again (a large number of pipeline channels are arranged in the pipeline channel).
  • the swirling mixing structure the fluid mixing can be realized when the sludge and water flow in it, and the meandering pipeline channel can reach hundreds of meters or even kilometers, so the flowing sludge and water can be fully mixed. ), which simplifies the need to set up the conditioning process of stirring and mixing before the sludge with high solid content enters the pipeline sludge heat exchanger (set conditioning tank, inject water into the sludge and fully stir to achieve sufficient sludge and water injection) Mixing), which not only simplifies the process equipment but also saves the energy of sludge conditioning.
  • the oxygen-enriched air enters the pipeline sludge reactor through the mud gas static mixer. Under the condition of high temperature and high pressure, the oxygen in it reacts with some organic substances in the sludge, and the reaction gas generated by the reaction can be adjusted by the gas-liquid separator.
  • reaction gas is discharged into the reaction sludge pressure storage tank through the self heat exchanger with the reaction sludge, so that the heat exchanger exists in the solid-liquid gas (solid phase in the sludge + sewage liquid phase + reaction Gas-phase) three-phase flow can control the pressure drop of the reaction high-temperature sludge in the heat exchanger, while using the pressure drop to the greatest extent to strengthen the heat exchange, it can slow down the wear of the subsequent control valves, and also improve the stability and controllability of the process. (Increasing the reaction gas will increase the flow resistance correspondingly, and also strengthen the heat exchange; the pressure drop of the control valve can be significantly reduced, and its life can be significantly improved).
  • the pressure of the reaction sludge in the reactor is generally about 1.8-5.4MPa, and the pressure of the material needs to be lowered before being discharged into the reaction sludge pressure storage tank.
  • the reaction gas) in the heat exchanger can achieve the above-mentioned control purpose, and also recover the heat energy of the reaction gas, so as to achieve the effect of energy saving and consumption reduction.
  • the conventional technology is to discharge the overflowable reaction gas at the outlet of the reactor, and the pressure of the reaction sludge is regulated by the control valve in the subsequent sequence, which is easy to cause damage to the valve, and the valve is usually replaced in a few days; and the reaction gas needs to be cooled in the subsequent sequence. Thermal energy is wasted.
  • the conventional heat exchanger is a three-phase material, it is prone to plug flow, stratified flow, local deposition and large pressure fluctuations, etc.
  • the meandering pipeline self-heat exchange and reaction collection components used in this patent the reaction gas It flows in a long pipeline of equal or close to equal diameter, and it is meandering and gradually flows from bottom to top, and a large number of swirl mixing structures are set in the pipeline to ensure that the three-phase materials will not appear plug flow, separation phenomena such as laminar flow, local deposition and large pressure fluctuations.
  • reaction sludge pressure storage tank Set up a reaction sludge pressure storage tank to store a part of the pressure energy of the reaction sludge discharged from the reactor into the reaction sludge pressure storage tank.
  • the pressure energy can be used in the subsequent reaction sludge dewatering process (as the follow-up reaction sludge dewatering and conveying power), and can also be used in the sludge water injection conditioning process (as the supernatant in the reaction sludge pressure storage tank) It can greatly reduce the energy consumption of the reaction mud dehydration and the power consumption of the injection pump.
  • Fig. 1 is the principle structure schematic diagram one of a kind of organic solid waste wet oxidation treatment system of the present invention
  • Fig. 2 is a kind of pipeline self-heat exchange and wet oxidation reaction assembly assembly structure schematic diagram of the present invention
  • Fig. 3 is the principle structure schematic diagram II of a kind of organic solid waste wet oxidation treatment system of the present invention
  • Fig. 4 is the principle structure schematic diagram 3 of a kind of organic solid waste wet oxidation treatment system of the present invention.
  • Fig. 5 is the principle structure schematic diagram 4 of a kind of organic solid waste wet oxidation treatment system of the present invention.
  • Fig. 6 is the principle structure schematic diagram five of a kind of organic solid waste wet oxidation treatment system of the present invention.
  • Fig. 7 is the principle structure schematic diagram VI of a kind of organic solid waste wet oxidation treatment system of the present invention.
  • Fig. 8 is a frame flow schematic diagram 1 of a kind of organic solid waste wet oxidation treatment process of the present invention.
  • Fig. 9 is a frame flow schematic diagram 2 of a kind of organic solid waste wet oxidation treatment process of the present invention.
  • FIG. 10 is a schematic diagram 3 of a frame-shaped flow diagram of a wet oxidation treatment process for organic solid waste according to the present invention.
  • OSW organic solid waste sludge
  • OSP organic solid product after wet oxidation.
  • S1 first mud-water mixed sludge; S2, second mud-water mixed sludge; S3, high temperature sludge before wet oxidation; S4, high temperature sludge before wet oxidation with oxygen-enriched air; S5, high temperature sludge after wet oxidation; S6, high temperature sludge after partial exhaust wet oxidation; S7, low temperature sludge under pressure after wet oxidation; S8, sludge after wet oxidation;
  • W0 process water injection; W1, supernatant; W2, mechanical dewatering sewage; W3, reinjection sewage; W4, external sewage; W5, discharge water up to standard; W6, absorption waste water; W7, gas absorption waste water; W8, sewage removal
  • the treatment plant is used as a carbon source to discharge water;
  • G1 oxygen-enriched compressed air
  • G2 generated gas from the reactor part
  • G3 generated gas from the reaction mud pressure storage tank
  • G4 mixed reaction gas
  • the main equipment includes a sludge storage tank 1, a pipeline self-heat exchange and reaction assembly assembly 2, a reaction sludge pressure storage tank 3, and an oxygen-enriched air unit 4. , a reaction gas absorption tank 5, a mechanical dehydration unit 6, a sewage tank 7 and a number of pumping equipment, the pumping equipment includes a sludge pump 9, a dewatering water pump 10, a water injection pump 11, and a spray water pump 12, and can be selectively set according to needs.
  • the heat pipe 212, the pipeline sludge reactor 23 includes a serpentinely arranged reaction pipe 231.
  • the organic solid waste sludge OSW with high solid content is stored in the sludge storage tank 1 , and the organic solid waste sludge OSW and the process water injection W0 are injected by the sludge pump 9 according to a certain proportion.
  • a first mud-water mixed sludge S1 is prepared, and the fluidity of the first mud-water mixed sludge S1 is significantly improved compared with OSW.
  • Reasonable choice to inject a certain proportion of process water injection W0 into the organic solid waste sludge OSW can reduce the power consumption of the sludge pump 9 and the energy consumption of the subsequent sludge wet oxidation treatment.
  • the organic solid waste sludge OSW contains The solid content is relatively high.
  • the solid content of the foreign mud is about 20% (the moisture content is about 80%).
  • This kind of sludge with high solid content has poor fluidity and is difficult to pump. It needs to add a certain amount of water. Reducing the solid content also reduces the viscosity of the sludge, but it is not advisable to add too much water. If the moisture content of the sludge to be treated is too high, although the viscosity can be greatly reduced, the energy consumption of transportation will also increase, especially the sludge will be significantly increased.
  • the heating energy consumption and dewatering energy consumption of sludge treatment, etc. generally, the solid content of the sludge entering the pipeline self-heat exchange and reaction assembly 2 should be controlled between 15% and 5%, and the preferred range is 12% to 8%.
  • the proportion of water injection W0 injected into the organic solid waste sludge OSW is related to the original solid content and organic matter content in OSW. If the organic solid waste sludge OSW is directly adjacent to the sewage treatment plant and does not need to be transported, the solid content of the organic solid waste sludge OSW can be appropriately reduced, such as the solid content of 8% to 2%, which can greatly save the previous process.
  • the above-mentioned water injection into raw sludge with high solid content to improve its fluidity is called sludge water injection conditioning process.
  • the process water injection W0 in this embodiment is the reinjection sewage W3 from the sewage tank 7 .
  • the first mud-water mixed sludge S1 can selectively pass through the pulverizer 13 to refine and homogenize the large-particle materials and long-fiber materials in the sludge.
  • the pulverizer 13 may not be provided.
  • the refined and homogenized sludge is beneficial to subsequent treatment and resource utilization.
  • the first mud-water mixed sludge S1 will flow into the pipeline-type self-heat exchange and reaction assembly 2 for self-heat exchange and wet oxidation reaction, thereby completing the process of degrading the organic matter in the sludge.
  • the mud-water static mixer 24 pre-mixes the first mud-water mixed sludge S1 optionally with the process water injection W0 (in this embodiment, the reinjection sewage W3 from the sewage tank 7 ), Thereby, the second mud-water mixed sludge S2 which is convenient to transport and has a suitable solid content is prepared.
  • a certain amount of process water injection W0 can be injected from the muddy water static mixer 24 as required, or only a certain amount of process water injection W0 can be injected from the sludge pump 9 without injecting the process water injection W0 from the muddy water static mixer 24 .
  • Process water injection W0 can be injected from the pipelines and equipment between the sludge storage tank 1 and the pipeline self-heat exchange and reaction aggregate assembly 2, including through the sludge pump 9 and the sludge-water static mixer 24, from the convenience of implementation and effect. It is considered that it is better to inject the process water W0 from the sludge pump 9, which can reduce the conveying power consumption of the sludge pump 9, which is a preferred process solution.
  • the second mud-water mixed sludge S2 enters into the serpentine pipe-type channel in the pipe-type self-heat exchange and reaction aggregate assembly 2 and in the pipe-type sludge heat exchanger 21 and the subsequent pipe-type sludge reactor 23 to be fully mixed again.
  • a large number of swirl mixing structures are arranged in the meandering pipeline channel, and the fluid can be mixed when the sludge and water flow in it.
  • the meandering pipeline channel reaches hundreds of meters or even kilometers, so The flowing sludge and water can be fully mixed), which simplifies the quenching and tempering process that requires stirring and mixing before the sludge with high solid content enters the heat exchanger (conventional technology sets a quenching and tempering tank, and in the high solid content sludge
  • the rate of water injection in the original mud is fully stirred to achieve full mixing of the original mud and water injection), which not only simplifies the process equipment, but also saves the energy consumption of sludge conditioning.
  • the low-temperature second mud-water mixed sludge S2 flows into the first heat exchange pipeline 211 and the second heat exchange pipeline 212 in the pipeline sludge heat exchanger 21 from the pipeline sludge reactor 23 Part of the exhaust gas flowing into the middle-temperature sludge S6 is subjected to heat exchange after wet oxidation.
  • the mud-water mixed sludge S2 is heated up to form high-temperature sludge S3 before wet oxidation, and part of the exhaust air is cooled to high-temperature sludge S6 after wet oxidation to become pressurized low-temperature sludge S7 after wet oxidation.
  • the pipeline-type sludge heat exchanger 21 can realize automatic The thermal process is sludge-sludge heat exchange, so that the process heat can be recovered to the maximum extent, and even in some cases, the process can be self-sustained, which significantly reduces the energy consumption of the organic solid waste sludge wet oxidation treatment system, and also significantly improves. It has energy saving and economic benefits, and the operating cost of organic solid waste wet oxidation treatment is extremely low.
  • Several mixed swirling structures are arranged in the first heat exchange pipeline 211 of the pipeline sludge heat exchanger 21, so as to facilitate the sufficient mixing and conditioning of the mud-water mixed sludge to improve its fluidity, strengthen the heat exchange process, and enhance the heat exchange process in the pipeline.
  • the oxygen-enriched air G1 is mixed with the high-temperature sludge S3 before wet oxidation through the mud gas static mixer 26 to form the high-temperature sludge S4 before wet oxidation with oxygen-enriched air added, and then enters the pipeline sludge reactor. twenty three.
  • Several mixing and swirling structures are arranged in the reaction pipeline 231 of the pipeline sludge reactor 23 to facilitate the sufficient mixing and conditioning of the sludge and the oxidant (oxygen-enriched air) to strengthen the reaction process.
  • a heater 22 is arranged in the pipeline sludge reactor 23 to further increase the temperature of the sludge, thereby regulating the temperature of the wet oxidation reaction.
  • part of the organic matter in the reaction sludge reacts with oxygen under high temperature and high pressure conditions to degrade the macromolecular organic matter into small molecular organic acids, and the reaction gas generated by the reaction is partially or not discharged through the gas-liquid separator 25.
  • the discharge ratio is 0-50%)
  • part of the generated gas G2 from the reactor part is discharged into the reaction gas absorption tank 5, and most or all of the reaction gas is discharged into the pipeline sludge heat exchanger 21 along with the reaction sludge
  • the reaction gas and the mud water are separated and stratified in the reaction mud pressure storage tank 3 under the action of gravity.
  • the three-phase flow of solid-liquid gas (solid phase in mud + sewage liquid phase + reaction gas phase) in the pipeline sludge heat exchanger 21 can be controlled by the gas-liquid separator 25 to control the reaction of high-temperature sludge in the pipeline sludge heat exchange.
  • the pressure drop in the device 21 can reduce the wear of the subsequent control valve while maximizing the use of the pressure drop (pressure energy) of the sludge after the reaction and strengthen the heat exchange, and also improve the stability and controllability of the process (increase the The reaction gas increases the flow resistance correspondingly, and also strengthens the heat exchange; the pressure drop of the control valve can be significantly reduced, and its life can be significantly improved).
  • the pressure of the reacted sludge in the pipeline sludge heat exchanger 21 is generally 1.8-5.4MPa. Before discharging into the reaction sludge pressure storage tank 3, the pressure of the material needs to be lowered. The range of 50%-100% of the reaction gas is retained in the pipeline sludge heat exchanger 21, which can achieve the above-mentioned control purpose, and also recover the heat energy of the reaction gas to achieve the effect of energy saving and consumption reduction.
  • the conventional technology is to discharge the reaction gas at the outlet of the reactor, and the pressure of the reaction sludge is regulated by the valve in the subsequent sequence, which can easily cause valve damage, and the valve is usually replaced within a few days; and the reaction gas needs to be cooled in the subsequent sequence, which also wastes heat energy.
  • the internal fluid of a conventional heat exchanger is a three-phase material, plug flow, stratified flow, local deposition and large pressure fluctuations are prone to occur, while this patent uses a meandering pipe-type organic solid waste self-heat exchange and reaction.
  • the reaction gas flows in a long pipeline of equal or nearly equal diameter, and it is meandering and gradually flows from bottom to top, and a large number of swirl mixing structures are set in the pipeline, which can ensure the three-phase material and reactant gas.
  • the mixing is relatively uniform without the phenomenon of plug flow, stratified flow, local deposition and large pressure fluctuations.
  • the pipe-type self-heat exchange and reaction aggregate assembly 2 includes a pipe-type sludge heat exchanger 21 for self-heat exchange and a pipe-type sludge reactor 23 for wet oxidation reaction.
  • the pipeline-type sludge heat exchanger 21 and the pipeline-type sludge reactor 23 in the embodiment shown in FIG. 1 are connected as a whole, and the formed pipeline-type self-heat exchange and reaction assembly 2 have an integrated structure, which can also be Separate structure, choose according to need.
  • the high temperature sludge S6 is exchanged and cooled with the low temperature second mud-water mixed sludge S2 in the pipeline sludge heat exchanger 21 to obtain the wet oxidation low temperature sludge S7 under pressure. , and then flow into the reaction mud pressure storage tank 3.
  • the residual pressure energy is stored in the reaction sludge pressure storage tank 3 by receiving the low temperature sludge S7 under pressure after wet oxidation.
  • the pressure in the storage tank can be regulated, on the one hand, it can reduce the pressure in the storage tank.
  • the sludge S8 after wet oxidation can directly enter the mechanical dehydration unit 6 for dehydration under pressure conveying. 10 into the mechanical dehydration unit 6 , the dehydrated solid product OSP forms a product that can be recycled, and the mechanically dehydrated sewage W2 separated by the dehydration process flows into the sewage tank 7 .
  • the solid-phase product of the wet oxidation process of the present invention meets the standard specification requirements of paper packaging materials, and can be used as packaging (corrugated) paper and wood substitute raw materials. Generally, 30%- 50%, which not only saves wood raw material resources and raw material costs, but also improves the strength and thermal insulation performance of packaging cardboard and substitute wood after adding organic solid waste treatment products of this process. It is a high-quality packaging cardboard and substitute wood.
  • the solid-phase products of this process, the organic solid products after wet oxidation meet the requirements of garden, land restoration, and even agricultural standards, and can also be used as organic fertilizer resources.
  • the excess reaction sludge pressure storage tank generated gas G3 is mixed with the reactor part generated gas G2 discharged from the gas-liquid separator to form a mixed reaction gas G4 and enters the reaction gas absorption tank 5 .
  • the absorption wastewater W6 from the sewage tank 7 is sprayed down in the upper part of the reaction gas absorption tank 5, and exchanges heat and mass with the mixed reaction gas G4 in the reaction gas absorption tank, and part of the condensable gas is dissolved in the water body to form absorption gas
  • the waste water W7 is returned to the sewage tank 7, and the non-condensable gas G5 is discharged into the atmosphere after reaching the standard.
  • FIG. 3 also provides a reaction sludge pressure storage tank 3 with a built-in floating suction unit 31.
  • the lower part of the floating suction unit 31 is connected with a hose, and then communicates with the sludge through the pipeline.
  • the water injection port of the pump 9 is connected.
  • the floating suction unit 31 is provided to inject the supernatant of the reaction sludge pressure storage tank 3 into the sludge pump 9 under the drive of the pressure in the reaction sludge pressure storage tank 3 to be conditioned and mixed with the sludge, which can be adjusted by adjusting the electric valve.
  • the size of the injection flow The arrangement of this component not only eliminates the need to install the water injection pump 11 and saves the power consumption of the water injection pump for extracting and re-injected sewage W3 from the sewage tank 7, but also greatly reduces the amount of sludge that needs to be processed by the mechanical dewatering unit 6 and other processes, and significantly improves the process. economy.
  • an injection pump 11 can be set at the same time to extract process water from the sewage tank 7 and inject it into the sludge pump 9 for conditioning and mixing with the sludge, and a floating suction unit can be set in the reaction sludge pressure storage tank 3 at the same time. 31
  • the supernatant in the reaction sludge pressure storage tank 3 is injected into the sludge pump 9 for conditioning and mixing with the sludge, as shown in FIG. 4 . That is, the raw mud water injection process with high solid content in the embodiments shown in Fig. 1, Fig. 3 and Fig.
  • the reinjection sewage W3 in the sewage tank 7 is preliminarily mixed, and/or the supernatant liquid W1 in the upper layer of the storage tank is injected into the sludge pump 9 by using the pressure energy in the reaction sludge pressure storage tank 3, and is mixed with the organic solid waste sludge.
  • the OSWs are mixed to obtain the first mud-water mixed sludge S1.
  • the process water injection W0 at least partially comes from the reinjection sewage of the sewage tank and/or the supernatant of the reaction sludge pressure storage tank.
  • Fig. 3 the sewage W4 discharged from the sewage tank 7 needs to be treated
  • the discharge that meets the standard is mainly suitable for the situation far away from the sewage treatment plant. Since the mechanically dewatered sewage W2 in the sewage tank 7 contains a large amount of small molecular acids such as acetic acid, it can be used as a carbon source for the sewage denitrification process of the sewage treatment plant, so it can be directly sent to the sewage treatment plant.
  • the difference between the embodiments of Figure 3 and Figure 5 is that the mechanically dewatered sewage in Figure 3 needs to be treated and discharged up to the standard, which is mainly suitable for the situation far away from the sewage treatment plant; while the mechanically dehydrated sewage in Figure 5 is sent to the sewage treatment plant as a sewage countermeasure.
  • the carbon source of the nitrification process is mainly suitable for the construction near the sewage treatment plant or in the sewage treatment plant.
  • An organic solid waste wet oxidation treatment device exemplified in FIG. 3 and FIG. 5 of the present invention can be selected according to specific conditions.
  • the reinjection sewage W3 of the sewage tank 7 is injected into the sludge pump 9 through the interface of the sewage pump 9 , and is pre-treated with the external sludge OSP inside the sludge pump 9 .
  • the reinjection sewage W3 of the sewage tank 7 is connected on the connecting pipe between the sludge pump 9 and the pipeline sludge heat exchanger 21 or on the muddy water static mixer 24 (in the muddy water static state
  • the mixer 24 is provided with an interface (not shown in the embodiment), and the OSP and the process water injection W0 are mixed during the flow in the pipeline.
  • the process water injection from the pipeline and the muddy water static mixer 24 in FIG. 6 is an option, the process water injection from the interface of the sewage pump 9 shown in FIG. 1 is more reasonable and can be selected according to specific circumstances.
  • a gas-liquid separator 25 is provided, and the high-temperature sludge S5 after wet oxidation is partially separated and discharged from the gas-liquid through the gas-liquid separator 25 (the discharge ratio is about 0-50%).
  • the reactor part generated gas G2 enters the reaction gas absorption tank 3 and absorbs the waste water W6 for condensation and heat exchange, and after the non-condensable gas reaches the standard It is discharged into the atmosphere; the condensed liquid forms the absorption gas waste water W7 and returns to the sewage tank 7 .
  • the present invention also provides an organic solid waste wet oxidation treatment process. processing, including the following steps:
  • Process step 1 organic solid waste sludge is mixed with water to form mud-water mixed sludge (optional)
  • the organic solid waste sludge OSW from the sludge storage tank 1 and the process water injection W0 are preliminarily mixed by the sludge pump 9, Thereby, the first mud-water mixed sludge S1 is prepared, and/or, the supernatant of the upper layer of the storage tank is injected into the sludge pump 9 by using the pressure energy in the reaction sludge pressure storage tank 3, and mixed with the organic solid waste sludge OSW to make the sludge. A first mud-water mixed sludge S1 is obtained.
  • the fluidity of the mixed sludge with increased water content has been significantly improved, especially the general process water injection is to wrap the sludge, that is, water-in-sludge, which can significantly reduce the energy consumption of sludge transportation; (Note: if it is close to a sewage treatment plant, it can be Properly reducing the solid content of the sludge to be treated can save the energy consumption of the sludge dewatering in the previous stage, so the fluidity of the sludge to be treated is better, so that there is no need to inject water into the sludge to be treated.)
  • the large particulate matter and long-fiber matter in the first mud-water mixed sludge S1 can be selectively sheared and crushed by the crusher 13, and the sludge crushing process step can usually be omitted if the sludge is relatively fine;
  • the first mud-water mixed sludge S1 and the process water injection W0 are mixed by the mud-water static mixer 24 to obtain the second mud-water mixed sludge S2.
  • the first step of the process is to inject water into the foreign high-solid-content raw mud to obtain a mud-water mixed sludge with good fluidity, which is convenient for pumping and can be selected according to needs.
  • the low-temperature second mud-water mixed sludge S2 and part of the exhaust gas flowing out from the pipe-type sludge reactor part 23 are passed through the meandering pipeline-type sludge heater part 21 .
  • the high-temperature sludge S6 performs heat exchange, so that the low-temperature second mud-water mixed sludge S2 is heated to form a high-temperature sludge S3 before wet-oxidation, and the high-temperature partial exhaust gas after wet oxidation is cooled to form a wet-type high-temperature sludge S6.
  • Low temperature sludge S7 under pressure after oxidation.
  • Process step 3 adding wet oxidation oxidant (oxygen-enriched air)
  • the high temperature sludge S3 before wet oxidation is mixed with the oxygen-enriched air G1 obtained from the oxygen-enriched air machine unit 4 through the mud gas static mixer 26 to obtain the addition of oxygen-enriched air.
  • High temperature sludge S4 before wet oxidation of air If the economy is reasonable, hydrogen peroxide and pure oxygen can also be used instead of oxygen-enriched air.
  • the oxidant (oxygen-enriched air) added in the wet oxidation should be appropriate. If it is too much, it will be useless and consume more energy. If it is less, the wet oxidation product cannot meet the standard.
  • the high temperature sludge S4 before the wet oxidation with oxygen-enriched air flows into the meandering pipeline reactor 23, and the wet oxidation reaction occurs in the pipeline reactor to obtain the wet oxidation High temperature sludge S5;
  • the heater 22 is turned on for heating, so as to control the reaction temperature of the wet oxidation.
  • the oxidizing reactant added in this embodiment is oxygen-enriched air, which is relatively safe, stable and economical. Hydrogen peroxide, pure oxygen can also be selected according to the actual situation, and even a certain amount of oxidation reaction catalyst can be added when necessary.
  • the high temperature sludge S5 after wet oxidation is partially separated and discharged from the gas and liquid through the gas-liquid separator 25 (the discharge ratio is about 0-50%) to form the generated gas in the reactor part G2 and high temperature sludge S6 after wet oxidation of partial exhaust gas;
  • the generated gas G2 of the reactor part enters the reaction gas absorption tank 3 and the absorption waste water W6 for condensation and heat exchange, and the non-condensable gas is discharged into the atmosphere after reaching the standard; the condensed liquid forms the absorption gas waste water W7 and returns to the sewage tank 7.
  • the prior art is to discharge the non-condensable gas (mainly oxygen and nitrogen) that can overflow in the reactor to avoid entering subsequent process equipment and pipelines such as heat exchangers to generate plug flow, stratified flow, partial flow, etc. Sedimentation and large pressure fluctuations (a phenomenon that gas-liquid-solid three-phase flow is particularly prone to), while the pipeline-type organic solid waste self-heat exchange and reaction unit components used in this patent, the reaction gas is in the same diameter or close to the same diameter. Flow in long pipelines, and gradually meander from bottom to top, and set up a large number of swirl mixing structures in the pipeline to ensure that three-phase materials will not appear plug flow, stratified flow, local deposition and large pressure.
  • non-condensable gas mainly oxygen and nitrogen
  • the patent scheme is to control the discharge ratio of non-condensable gas that can overflow in the high-temperature sludge S5 after wet oxidation, and the discharge ratio range is 0-50%, which can appropriately increase the subsequent flow pressure drop to obtain enhanced heat exchange. , Improve the control valve life of the sludge after the reaction and the effect of recovering the heat energy of the reaction gas.
  • Process step 6 cooling the reaction sludge
  • the high-temperature sludge S6 flows into the second heat exchange pipeline 212 of the pipeline sludge heat exchanger 21 and the low-temperature second sludge-water mixed sewage in the first heat exchange pipeline 211.
  • Sludge S2 is cooled by heat exchange to obtain low-temperature sludge S7 under pressure after wet oxidation.
  • the heat energy in the process can be recovered to the maximum extent through the mud-sludge heat exchange;
  • the fluid in the second heat exchange pipeline 212 of the pipeline sludge heat exchanger 21 is a gas-liquid-solid three-phase flow, and the first heat exchange pipeline 211 and the second heat exchange pipeline 212 are provided with several mixed swirling structures, which can prevent stratification, deposition and even plug flow, etc., and can achieve relatively homogeneous gas-liquid-solid flow and enhance the heat transfer process and other excellent effects.
  • Process Step 7 Sludge storage in the reaction sludge pressure storage tank, storage of pressure energy and regulation of system pressure
  • the low temperature sludge S7 under pressure enters the reaction sludge pressure storage tank 3 for storage to obtain wet oxidation sludge S8, and the reaction gas is precipitated in the reaction sludge pressure storage tank 3 to store pressure energy.
  • part or the generated gas G2 in the reactor part is discharged into the reaction gas absorption tank 5, and most or all of the reaction gas (generally controlled ratio is 50%-100%) passes through the pipeline sludge heat exchanger 21 along with the reaction sewage.
  • the mud is discharged into the reaction mud pressure storage tank 3, the reaction gas and the muddy water are separated in the reaction mud pressure storage tank 3 under the action of gravity and stored in the upper part of the reaction mud pressure storage tank 3, and the pressure of the reaction mud pressure storage tank 3 is regulated.
  • An exhaust pressure regulating valve is arranged on the upper part of the reaction mud pressure storage tank 3)
  • the pre-stage system pressure (mainly regulating the pressure in the reactor) can be regulated.
  • the low-temperature sludge S7 under pressure enters the reaction sludge pressure storage tank 3 and is stored for a certain period of time. After the reaction, the sludge will be layered, and the upper part of the liquid phase is the supernatant (sewage containing a small amount of solid phase) and the lower part.
  • the flotation suction supernatant unit 31 set in the reaction sludge pressure storage tank 3 can float on the upper part of the reacted sludge stored in the reaction sludge pressure storage tank 3, and the floating suction supernatant
  • the supernatant liquid suction unit 31 is connected with a hose, which is connected with the injection pipe of the sludge pump 9 through the pipe, and the upper supernatant liquid is injected into the sludge pump 9 under the pressure of the reaction sludge pressure storage tank 3, so that the The sludge treatment volume of the mechanical dewatering unit is reduced, and the power consumption of the injection pump 11 for injecting water from the sewage tank to the sludge pump 9 is also saved.
  • this process step is to store the reacted sludge for subsequent intermittent dehydration, and to store the excess residual pressure energy in the system to reduce the energy consumption of the subsequent dehydration process.
  • the primary settling of the tank injects water into the sludge pump to reduce the energy consumption of the injection pump, that is, the energy consumption of the sludge water injection conditioning process.
  • the pressure drop range of the control valve of the sludge after the post-reaction of the heat exchanger is smaller, which can greatly extend the life of the control valve and improve the stability of the system, and can also strengthen the heat exchange.
  • the reactor sludge wet oxidation reaction process is carried out under a certain pressure and temperature, the pressure is generally above 2.0MPa, and the subsequent process pressure such as heat exchange is usually not enough to consume the pressure energy, which causes the subsequent control valve. There are problems such as short life and poor reliability. Therefore, using the reaction mud pressure storage tank 3 to store a part of the pressure energy can achieve multiple positive benefits at one stroke.
  • the wet-oxidized sludge S8 is subjected to solid-liquid separation through the mechanical dewatering unit 6 to obtain the mud cake OSP and the separated liquid-mechanical dewatering sewage W2.
  • the mud cake OSP after wet oxidation treatment can be used as a blending raw material for packaging (corrugated) paper.
  • the optimum ratio can be added up to 30-50%, which can not only obtain good social benefits, that is, realize the utilization of organic solid waste resources, but also It also significantly improves its economy due to resource utilization; in addition, it can also be used as nutrient soil for landscaping.
  • the mechanically dewatered sewage W2 flows into the sewage tank 7 as the process water injection W0 (re-injection sewage W3) required by other components of the system.
  • the excess sewage can be treated by the sewage treatment unit 8 and then discharged up to the standard, or it can be selected as a sewage treatment plant. carbon source for denitrification.
  • the specific design of the wet oxidation process and parameters are as follows: for the municipal sludge with a moisture content of 80% in organic solid waste (assuming that the solid organic matter content is about 35%-65%), the moisture content of the first mud-water mixed sludge S1 The rate is about 90% (generally 87%-93% is more suitable for fluidity, and the optimum moisture content is related to the mud quality) and the temperature is 30 ° C. Under the pumping of the sludge pump 9, the pressure is about 2.4MPa to 3.5MPa , after preliminary mixing and tempering by the mud-water static mixer, the second mud-water mixed sludge S2 is obtained.
  • the second mud-water mixed sludge S2 flows through the pipeline sludge heat exchanger and is heated to a temperature of 170-190°C, and flows through the heater to heat the sludge to reach a temperature of 200°C (the reaction temperature is related to the mud quality and the resource utilization of the sludge after the reaction). Relevant, generally 180-230°C), if the sludge flowing through the pipeline sludge heat exchanger 21 reaches 180-190°C, the heater basically does not need to work.
  • the reaction sludge enters the pipeline sludge reactor at a pressure of about 2.0MPa to 3.2MPa and a temperature of 200°C for wet oxidation reaction.
  • oxygen-enriched air is added (generally, the oxygen concentration is about 60%), The oxygen-enriched air is provided by the oxygen-enriched air unit.
  • the sludge continues to heat up by about 10-30 °C due to the exothermic oxidation reaction. Therefore, the high temperature sludge temperature after wet oxidation of the sludge is 200 °C.
  • the pressure is about 2.0-3.2MPa, then it is cooled to about 40-50°C through the pipeline sludge heat exchanger, the pressure is about 0.5-2.0MPa, and then flows into the reaction mud pressure storage tank, under the design conditions , try to make the pressure in the reaction sludge pressure storage tank 1.0-1.2MPa.
  • the reaction mud pressure storage tank stores a part of the pressure energy, which can be used in the subsequent reaction mud dehydration process (as the transmission power for the subsequent reaction mud dehydration), which can greatly reduce the energy consumption of the reaction mud dehydration, and can also be used for raw mud water injection In the quenching and tempering process, the energy consumption of the injection pump is reduced.
  • the heater needs to be properly supplemented; During the start-up process of the system, a heater is required to provide start-up heat energy for the sludge. In addition, under the design working conditions, a reasonable total can ensure that the heating process of the heater is basically unnecessary.
  • the wet oxidation process of the present invention can be self-sustaining under the design process parameters, that is, it can be self-sustaining most of the time, so the process energy consumption extremely low.
  • the reduction, stabilization, harmlessness and resource utilization of organic solid waste can be completely achieved.
  • the perishable and easily degradable organic matter protein, fat, sugar, antibiotics, etc.
  • the small molecular organic acids of the ion enter the liquid phase and the gas CO 2 is discharged into the atmosphere, the pathogenic bacteria are completely inactivated, and the heavy metal part is eliminated, which meets the requirements of stabilization and harmlessness;
  • the solid product after mechanical dehydration the moisture content It is less than 40%, the weight is only less than 25% of the original, and the weight is reduced by more than 75%; in the solid-phase product of the wet oxidation process of the present invention, lignin, cellulose and insoluble humic acid are retained in the solid-phase product
  • the particle size can also meet the requirements of relevant standards and specifications for raw materials
  • the present invention has a simple and reasonable structure, realizes high-efficiency heat exchange between low-temperature sludge and high-temperature sludge through meandering pipeline self-heat exchange and reaction assembly components, recovers most of the process heat, and greatly improves the efficiency of the process.
  • Reduce process energy consumption at the same time realize the mixing of sludge and process water injection (plate and frame filtrate and/or supernatant in the reaction mud pressure storage tank) through the sludge-water static mixer and sewage pump or pipeline, reducing the need for conditioning tanks and other components and
  • the process link simplifies the process flow.
  • the gas-liquid separator can release the reaction gas generated by the reactor to adjust the pressure drop of the high-temperature sludge flowing into the second heat exchange pipeline of the pipeline sludge heat exchanger, so as to maximize the use of the pressure drop to strengthen the exchange. At the same time, it can slow down the wear of the subsequent control valve, and also improve the stability and controllability of the process.
  • the reaction sludge pressure storage tank stores a part of the pressure energy of the reaction sludge discharged from the reactor into the reaction sludge pressure storage tank, which can be used in the subsequent reaction sludge dehydration process (as the transmission power for the subsequent reaction sludge dehydration, the insufficient part can be supplemented by pumping) , it can also be used in the raw mud water injection conditioning process (as the conveying power for the supernatant liquid of the reaction mud pressure storage tank), so that the energy consumption of the reaction mud dehydration and the energy consumption of the raw mud water injection conditioning process can be greatly reduced.

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Abstract

本发明公开了一种有机固废湿式氧化处理系统及其处理工艺，包括污泥储罐、管道式自换热和反应集合组件、反应泥压力储罐、机械脱水单元、污水箱、污泥泵和注水泵；通过污泥泵能够实现污泥与工艺注水的混合，省去了传统工艺中的调质罐调质；通过管道式自换热和反应集合组件的泥-泥换热和湿式氧化反应，同时通过控制保留在管道式自换热和反应集合组件中反应气的比例能够调控压力降；采用反应泥压力储罐储存一部分反应泥的压力能并将反应泥初沉，不仅可减少调节阀的调节范围、延长阀门寿命，而且可将压力能用于反应泥脱水和上清液回注调质，如此充分回收工艺过程绝大部分热量，大幅降低工艺能耗，且产物可资源化利用，获得显著的环保和经济效益。

Description

一种有机固废湿式氧化处理系统及其处理工艺 技术领域
本发明涉及有机固废处理技术领域，特别涉及一种有机固废湿式氧化处理系统及其处理工艺。
背景技术
随着我国城镇化的不断推进和环境保护要求的不断提高，有机固废特别是大量的市政污泥、生活垃圾和和餐厨餐余垃圾的处理越来越受到重视。有机固废是指人类在生产生活等活动中产生的污染环境的固态、半固态有机废物，有机固废一般包括市政污泥、工业污泥、餐厨餐余垃圾、生活垃圾特别是湿垃圾、江河底泥、高浓度有机废液、粪便等，将有机固废制成的泥浆，与城市污泥具有类似的化学物理性质，可以采用城市污泥相类似的处理工艺和技术。为了便于叙述，后续将有机固废制成的泥浆(包括市政污泥)，简称有机固废泥或者污泥。在众多的污泥处理技术中，污泥湿式氧化处置工艺具有无三废(气液固)排放和便于资源化利用等优点，可能成为未来的主流处理技术，但该工艺技术也存在以下问题或者不足需要进一步完善和发展：
(1)由于污泥具有高粘性不便于泵送，目前的湿式氧化工艺技术将高含固率污泥在进入换热器前设置搅拌混合的调质罐，在调质罐内将污泥与水充分搅拌混合，通过调质处理改善污泥的流动性。如果能利用污泥换热器和反应器同步进行调质，则可简化工艺环节，减少调质工艺设备，减少建造成本和运行费用。
(2)湿式氧化反应需要在高温高压液相中进行，一般反应器中的污泥温度为160-370℃和压力为1.8-5.4MPa，湿式氧化反应后的高温污泥一般先将反应可溢出气体排净后再进入换热器将热量传递给湿式氧化前的低温污泥，降温后的反应后污泥进入闪蒸罐内进行闪蒸冷却。因此工艺存在两个问题或者不足：第一，不能高品位回收排出的高温高压气体的能量，第二，换热器出口的污泥压力依旧较高，需要通过调节连接闪蒸罐管路上阀门开度进一步降低污泥压力，然而目前市场上的换热器换热效果差，经常导致换热器出口污泥温度高于110℃，有些甚至高于140℃，压力大于1.0MPa，因此，控制阀门在如此恶劣的工艺环境(高温高压)很容易造成损坏，需要经常更换阀门，同时也降低了系统的可靠性和稳定性。如果能将部分或者全部反应气保留在高温的反应后污泥中并流经换热器，一方面可以回收反应气热能，另一方面可适当增加反应后污泥在换热器中的压力降，大幅降低换热器排出的反应后污泥的压力，从而可以大幅延长其调控阀门的寿命，再一方面还可利用反应气强化污泥 换热，可一举多得。
(3)目前的湿式氧化工艺技术将湿式氧化后污泥排入闪蒸罐内进行降温和卸压，再通过污泥泵输送至机械脱水单元进行固液分离，未能很好的利用污泥和反应气所携带的压力能。如果将其压力能利用用于后续脱水工艺将获得明显的节能效果。
(4)目前的湿式氧化工艺技术将湿式氧化后污泥排入闪蒸罐内进行降温和卸压并经冷却水冷却后全部送至脱水，如果在氧化后污泥脱水之前进行初沉淀并将初沉淀污水(上清液，含有少量的固相)返回反应前污泥中用于改善反应前污泥的流动性而不是常规采用反应泥脱水的污水调质原泥(在原泥中注水改善其流动性可称为“原泥注水调质工艺”)，则可以大幅减少反应后污泥的脱水量和脱水能耗，如果再利用反应后污泥压力储罐储存的压力能以及对反应后污泥进行初沉淀，则还可以减免原泥注水调质工艺的注水能耗。也就是说，可以利用反应后污泥储罐进行储存压力能和进行反应后污泥初沉淀，将初沉淀的上清液回注进行原泥注水调质工艺，不仅可以大幅降低反应后污泥脱水量和脱水能耗，而且还可以减免原泥注水调质工艺的注水能耗，一举多得。
(5)目前的湿式氧化工艺技术主要是采用中间介质(水或油)循环换热技术回收高温污泥热量，即高温污泥的热量传递给低温污泥需要通过中间回路的介质水或油进行传递，增加了传热热阻，导致传热效果差，工艺能耗比较高。如果能实现污泥-污泥直接高效换热，将可获得显著的节能效果。
发明内容
本发明是为了克服上述现有技术中缺陷，提供一种有机固废湿式氧化处理系统，通过在管道式污泥换热器污泥进口前的污泥泵和/或污泥输送管线中加入一定量的工艺注水，污泥和工艺注水进行初步混合后进入管道式污泥换热器和后序的管道式反应器，节省了目前常规工艺的设置调质罐进行充分搅拌调质的工艺和相对应的能耗；通过控制保留在管道式污泥换热器中的反应气的比例来调控管道式污泥换热器中反应泥的压力降，以实现管道式反应器中反应过程中污泥反应压力的调控和强化管道式污泥换热器的换热，同时可大幅延长调控阀门的寿命和提高工艺过程的稳定可控性；设置反应泥压力储罐，储存一部分从反应器排入反应泥压力储罐中的反应泥的压力能，并利用反应泥压力储罐将反应后污泥进行初步沉降分层使得反应后污泥中的重组分沉降在反应泥压力储罐底部而轻组分的污水(上清液)在反应泥压力储罐的上部，一方面可减少反应泥进入反应泥压力储罐的压力调节阀的压力调节范围和幅度，提高该调节阀的寿命和工艺稳定可靠性，另一方面可将该压力能用于后续的反应泥脱水工艺中(作为后续反应泥脱水输送动力)，还可将该反应泥压力储罐上部的污水即上清液 作为工艺注水加入原泥中，即利用反应泥压力储罐的压力能和对反应后污泥的初沉功效实现原泥注水调质工艺，从而可以大幅减少反应泥脱水能耗以及节省原泥注水工艺的泵功耗；本发明还提供了运用上述有机固废湿式氧化处理系统的处理工艺，其具有处理系统的所有特点。
为实现上述目的，本发明提供一种有机固废湿式氧化处理系统，包括污泥储罐、管道式自换热和反应集合组件、反应泥压力储罐、机械脱水单元、污水箱和污泥泵；
所述污泥储罐用于储存待处理的有机固废泥；
所述污泥泵设置在污泥储罐与管道式自换热和反应集合组件之间的输送管路上，该污泥泵用于将污泥储罐内的有机固废泥泵送给管道式自换热和反应集合组件并通过掺水将有机固废泥与工艺注水初步混合以形成泥水混合污泥；
所述管道式自换热和反应集合组件包括用于泥-泥换热的管道式污泥换热器、用于湿式氧化反应的管道式污泥反应器、气液分离器和泥气静态混合器；
其中，所述管道式污泥换热器包括供泥水混合污泥流动的第一换热管路、以及供部分排气湿式氧化后高温污泥流动的第二换热管路，所述第一换热管路与第二换热管路之间进行换热以将泥水混合污泥和部分排气湿式氧化后高温污泥分别转化为湿式氧化前高温污泥和湿式氧化后带压低温污泥；
所述管道式污泥反应器包括反应管路，该反应管路串接于第一换热管路的出口与第二换热管路的进口之间，所述泥气静态混合器设置在第一换热管路与反应管路之间管路上，用于在湿式氧化反应前高温污泥内添加湿式氧化反应所需的氧化剂以制得添加氧化剂的湿式氧化前高温污泥；
所述反应管路用于接收添加氧化剂的湿式氧化前高温污泥并通过湿式氧化反应以制得湿式氧化后高温污泥；
所述气液分离器设置在反应管路与第二换热管路之间的管路上，其用于可操控的将湿式氧化后高温污泥中的反应气分离排出，以形成部分排气湿式氧化后高温污泥；
所述反应泥压力储罐用于接收第二换热管路生成的湿式氧化后带压低温污泥并进行排气降压以制得湿式氧化后污泥；
所述机械脱水单元用于接收湿式氧化后污泥并对其进行脱水；
所述污水箱用于接收、存储机械单元脱出的污水。
进一步设置为：还包括反应气吸收罐，该反应气吸收罐用于接收气液分离器分离出的反应气、以及反应泥压力储罐排出的反应气。
进一步设置为：还包括泥水静态混合器，所述泥水静态混合器设置在污泥泵与管道 式自换热和反应集合组件之间的输送管路上，用于实现有机固废泥与工艺注水的再次混合。
进一步设置为：还包括富氧空气机单元，所述富氧空气机单元制备富氧空气，并与所述泥气静态混合器连接，将富氧空气注入所述泥气静态混合器中并经混合后注入所述管道式污泥反应器中参与湿式氧化反应。
进一步设置为：还包括粉碎机，所述粉碎机设置在污泥泵与管道式自换热和反应集合组件之间的输送管路上，用于对泥水混合污泥进行剪切破碎。
进一步设置为：所述反应泥压力储罐内设置有漂浮抽吸单元，该漂浮抽吸单元漂浮于反应泥压力储罐上方分层的上清液上部并通过连接管道将其上清液排出。
进一步设置为：所述管道式自换热和反应集合组件还包括加热器，所述加热器用于加热管道式污泥反应器以控制湿式氧化反应温度。
进一步设置为：所述第一换热管路和/或第二换热管路和/或反应管路内设置有若干混合旋流结构。
进一步设置为：所述管道式污泥换热器的第一换热管路和第二换热管路为蜿蜒结构布置；
和/或管道式污泥反应器的反应管路为蜿蜒结构布置。
进一步设置为：所述有机固废泥掺水改性的所述工艺注水至少包括所述反应泥压力储罐内的上清液和/或来自所述污水箱的回注污水。
进一步设置为：所述工艺注水通过污泥储罐至管道式自换热和反应集合组件之间的管路和设备注入有机固废泥中。
本发明还提供了一种有机固废湿式氧化处理工艺，包括以下步骤：
步骤一：有机固废泥与工艺注水混合以形成泥水混合污泥
至少通过污泥泵将来自污泥储罐的有机固废泥与工艺注水进行初次混合以制的第一泥水混合污泥；
步骤二：污泥在管道式污泥换热器中换热升温
通过管道式污泥换热器将低温的泥水混合污泥和从管道式污泥反应器中流出的部分排气湿式氧化后高温污泥进行换热，以使得低温的泥水混合污泥被加热形成为湿式氧化前高温污泥，部分排气湿式氧化后高温被降温以形成为湿式氧化后带压低温污泥；
步骤三：添加湿式氧化的氧化剂
湿式氧化前高温污泥通过泥气静态混合器与氧化剂混合以形成添加氧化剂的湿式氧化前高温污泥；
步骤四：污泥在管道式污泥反应器中反应
添加氧化剂的湿式氧化前高温污泥在管道式污泥反应器中进行湿式氧化反应以制得湿式氧化后高温污泥；
步骤五：反应气部分排气与系统压力调控
湿式氧化后高温污泥通过气液分离器进行气液分离将部分反应气控制排出，以制得部分排气湿式氧化后高温污泥；
步骤六：反应泥降温
部分排气湿式氧化后高温污泥流入管道式污泥换热器的第二换热管路并与第一换热管路内的低温的污水混合污泥进行换热而降温，以转化为湿式氧化后带压低温污泥；
步骤七：反应泥压力储罐储泥、储压力能和调控系统压力
湿式氧化后带压低温污泥进入反应泥压力储罐进行存储以制得湿式氧化后污泥，反应气在反应泥压力储罐析出，并储存压力能；
步骤八：污泥脱水
湿式氧化后污泥通过机械脱水单元进行固液分离脱水。
进一步设置为：在步骤一中的污泥泵掺混的工艺注水至少部分来自污水箱的回注污水和/或反应泥压力储罐的上清液。
进一步设置为：在步骤一中还包括通过泥水静态混合器对第一泥水混合污泥与水进行再次混合以制得第二泥水混合污泥。
进一步设置为：在步骤一中还包括通过粉碎机对第一泥水混合污泥进行剪切破碎。
进一步设置为：在步骤四中还包括通过加热器加热管道式污泥反应器以控制湿式氧化反应的温度。
进一步设置为：在步骤五中气液分器分离排出的反应气比例为0～50％。
进一步设置为：在步骤七中还包括通过漂浮抽吸单元抽离反应泥压力储罐上方分层的上清液并至少部分供应给污泥泵。
进一步设置为：在步骤八还包括通过污水箱接收、储存机械脱水单元脱出的污水并通过注水泵至少将部分污水供应给污泥泵。
与现有技术相比，本发明具有以下优点：
1)待处理污泥为高含固率的有机固废污泥，经泥水静态混合器和/或前序污泥泵和/或前序输送管路上掺混一定比例的污水，并经泥水静态混合器或者前序污泥泵进行初步混合后进入管道式污泥换热器和后序的管道式污泥反应器的蜿蜒管道式通道中进行再次充分混合(在管道 式通道中设置有大量的旋流混合结构，污泥和水在其中流动时就可以实现流体的混合，再加上蜿蜒管道式通道达数百米甚至千米，因而其中流动的污泥和水可以实现充分的混合)，简化了常规技术在高含固率污泥进入管道式污泥换热器前需要设置搅拌混合的调质工艺(设置调质罐，在污泥中注水充分搅拌实现污泥和注水的充分混合)，既简化了工艺设备又节省了污泥调质能源。
2)富氧空气经泥气静态混合器进入管道式污泥反应器，在高温高压湿态条件下其中的氧气与污泥中的部分有机物反应，反应产生的反应气经气液分离器可调控的排出一部分，其大部分或者全部反应气经自换热器随反应污泥排入反应泥压力储罐中，这样换热器存在中固液气(泥中的固相+污水液相+反应气气相)三相流动可以调控反应高温污泥在换热器中的压力降，在最大程度利用压力降强化换热的同时可减缓后序调控阀门的磨损，也提高了工艺过程的稳定可控性(增加了反应气，则相应增加了流动阻力，也强化了换热；调控阀门的压力降显著降低可以显著提高其寿命)。反应器中反应污泥的压力一般大约在1.8-5.4MPa，在排入反应泥压力储罐前需要将物料的压力降下来，通过保留部分或者全部反应气(一般调控范围保留50％-100％反应气)在换热器中，可以实现上述调控目的，还回收了反应气的热能，达到节能降耗的效果。常规技术是在反应器出口排出可溢出的反应气，反应污泥的压力靠后序的调控阀门调控，很容易造成阀门损坏，通常几天就更换阀门；而且反应气后序还需要冷却，也浪费了热能。常规的换热器如果为三相物料，很容易出现柱塞流、分层流、局部沉积和较大压力波动等，而本专利采用的蜿蜒管道式自换热和反应集合组件，反应气是在等径或者接近等径的长管道中流动，而且是蜿蜒逐渐由下往上流，以及在管道中设置了大量的旋流混合结构，可保证三相物料不会出现柱塞流、分层流、局部沉积和较大压力波动等现象。
3)设置反应泥压力储罐，储存一部分从反应器排入反应泥压力储罐中的反应泥的压力能，一方面可减少反应泥进入反应泥压力储罐的压力调节阀的压力调节范围和幅度，另一方面可将该压力能用于后续的反应泥脱水工艺中(作为后续反应泥脱水输送动力)，也可以用于污泥注水调质工艺中(作为反应泥压力储罐中上清液的输送动力)，从而可以大幅减少反应泥脱水能耗和注水泵功耗。
附图说明
图1是本发明一种有机固废湿式氧化处理系统的原理结构示意图一；
图2是本发明一种管道式自换热和湿式氧化反应集合组件结构原理示意图；
图3是本发明一种有机固废湿式氧化处理系统的原理结构示意图二；
图4是本发明一种有机固废湿式氧化处理系统的原理结构示意图三；
图5是本发明一种有机固废湿式氧化处理系统的原理结构示意图四；
图6是本发明一种有机固废湿式氧化处理系统的原理结构示意图五；
图7是本发明一种有机固废湿式氧化处理系统的原理结构示意图六；
图8是本发明一种有机固废湿式氧化处理工艺的框形流程示意图一；
图9是本发明一种有机固废湿式氧化处理工艺的框形流程示意图二；
图10是本发明一种有机固废湿式氧化处理工艺的框形流程示意图三。
结合附图在其上标记以下附图标记：
1、污泥储罐；2、管道式自换热和反应集合组件；21、管道式污泥换热器；211、第一换热管路；212、第二换热管路；22、加热器；23、管道式污泥反应器；231、反应管路；24、泥水静态预混合器；25、气液分离器；26、泥气静态混合器；3、反应泥压力储罐；31、漂浮抽吸单元；4、富氧空气机单元；5、反应气吸收罐；6、机械脱水单元；7、污水箱；8、污水处理单元；9、污泥泵；10、脱水水泵；11、注水泵；12、喷淋水泵；13、粉碎机；
OSW、有机固废泥；OSP、湿式氧化后有机固体产物。
S1、第一泥水混合污泥；S2、第二泥水混合污泥；S3、湿式氧化前高温污泥；S4、添加富氧空气的湿式氧化前高温污泥；S5、湿式氧化后高温污泥；S6、部分排气湿式氧化后高温污泥；S7、湿式氧化后带压低温污泥；S8、湿式氧化后污泥；
W0、工艺注水；W1、上清液；W2、机械脱水污水；W3、回注污水；W4、外排污水；W5、达标排放水；W6、吸收废水；W7、吸收气废水；W8、去污水处理厂做碳源排放水；
G1、富氧压缩空气；G2、反应器部生成气；G3、反应泥压力储罐生成气；G4、混合反应气；G5、达标外排气。
具体实施方式
下面结合附图，对本发明的一个具体实施方式进行详细描述，但应当理解本发明的保护范围并不受具体实施方式的限制。
本发明一种有机固废湿式氧化处理系统如图1所示，主要设备包括污泥储罐1、管道式自换热和反应集合组件2、反应泥压力储罐3、富氧空气机单元4、反应气吸收罐5、机械脱水单元6、污水箱7和以及若干泵送设备，泵送设备包括污泥泵9、脱水水泵10、注水泵11、喷淋水泵12，此外根据需要选择性设置粉碎机13和污水处理单元8；其中，该管道式自换热和反应集合组件2包括用于自换热的管道式污泥换热器21、用于湿式氧化反应的管道式污泥反应器23、气液分离器25、泥气静态混合器26、泥水静态混合器24和加热器22，该管道式污泥换热器21包括蜿蜒布置的第一换热管路211和第二换热管路212，管道式污 泥反应器23包括蜿蜒布置的反应管路231。
具体的，如图1所示，外来高含固率的有机固废污泥OSW存储于污泥储罐1中，通过污泥泵9将有机固废污泥OSW和工艺注水W0按照一定比例进行初步混合，制得第一泥水混合污泥S1，第一泥水混合污泥S1的流动性相比OSW有明显的提高。合理选择在有机固废污泥OSW中注入一定比例的工艺注水W0，可减少污泥泵9的功耗和后续污泥湿式氧化处理的能耗，这是因为如果有机固废污泥OSW的含固率比较高，如外来泥的含固率在20％左右(含水率在80％左右)，这种高含固率的污泥流动性太差泵送很困难，需要加入一定量的水来降低含固率，也降低了污泥粘度，但加入的水也不宜过多，待处理污泥含水率过高虽然粘度可以大幅降低，但输送能耗也会增加，特别是还会显著增加污泥处理的加热能耗和脱水能耗等，一般进入管道式自换热和反应集合组件2的污泥的含固率应控制在15％至5％之间，优选范围12％至8％。在有机固废污泥OSW中注入工艺注水W0的比例，与OSW中原有含固率和含有机质比例有关。如果有机固废污泥OSW直接临近来自污水处理厂而无需外运，则有机固废污泥OSW的含固率可以适当降低，如含固率在8％至2％，这样可以大幅节省前序工艺污泥脱水的能耗，此时有机固废污泥OSW的流动性比较好，则无需在有机固废污泥OSW中加入工艺注水W0。上述向高含固率的原泥中注水以改善其流动性称为污泥注水调质工艺。本实施例的工艺注水W0为来自于污水箱7中的回注污水W3。
如图1所示，第一泥水混合污泥S1可选择地经过粉碎机13对污泥中大颗粒物料和长纤维物料进行细化和均质，若来料均匀、粒径细小，如临近直接来自污水处理厂的污泥，则可不设置粉碎机13。细化和均质的污泥有利于后续的处理以及资源化利用。第一泥水混合污泥S1将流入管道式自换热和反应集合组件2中进行自换热和湿式氧化反应，从而完成污泥中有机物降解的过程。
如图1和图2所示，首先，泥水静态混合器24将第一泥水混合污泥S1可选择地和工艺注水W0(本实施例为来自污水箱7的回注污水W3)进行预混合，从而制得便于输送、含固率合适的第二泥水混合污泥S2。可根据需要从泥水静态混合器24注入一定量的工艺注水W0，或者不从泥水静态混合器24注入工艺注水W0而只从污泥泵9中注入一定量的工艺注水W0。工艺注水W0可以从污泥储罐1至管道式自换热和反应集合组件2之间的管路和设备上注入，包括通过污泥泵9和泥水静态混合器24，从实施方便性和效果考虑，工艺注水W0从污泥泵9注入更佳，可以减少污泥泵9的输送功耗，为优选工艺方案。第二泥水混合污泥S2进入管道式自换热和反应集合组件2的管道式污泥换热器21和后序的管道式污泥反应器23中的蜿蜒管道式通道中进行再次充分混合(在蜿蜒管道式通道中设置有大量的旋 流混合结构，污泥和水在其中流动时就可以实现流体的混合，再加上蜿蜒管道式通道达数百米甚至千米级，因而其中流动的污泥和水可以实现充分的混合)，简化了常规技术在高含固率污泥进入换热器前需要设置搅拌混合的调质工艺(常规技术设置调质罐，在高含固率原泥中注水充分搅拌实现原泥和注水的充分混合)，既简化了工艺设备又节省了污泥调质能耗。
如图1所示，低温的第二泥水混合污泥S2流入管道式污泥换热器21中的第一换热管路211和第二换热管路212中从管道式污泥反应器23中流入的部分排气湿式氧化后高温污泥S6进行换热，高、低温污泥的换热设置为逆流换热，对数换热温差更小、换热效果高效，因而，低温的第二泥水混合污泥S2升温后形成湿式氧化前高温污泥S3，部分排气湿式氧化后高温污泥S6降温为湿式氧化后带压低温污泥S7，该管道式污泥换热器21可实现自热工艺即污泥-污泥换热，从而可以最大限度回收工艺热能，甚至在某些情况下可以实现工艺过程自持，显著降低了有机固废污泥湿式氧化处理系统的能耗，也显著提高其节能经济效益，有机固废湿式氧化处理运营成本极低。在管道式污泥换热器21的第一换热管路211内设置若干混合旋流结构，以利于泥水混合污泥充分混合调质而改善其流动性，以及强化换热过程，以及在管道式污泥换热器21的第二换热管路212内设置若干混合旋流结构，以利于反应后泥与反应生成气充分混合均质化，可避免产生气液固三相流动的柱塞流、分层流、局部沉积和较大压力波动等问题。
如图1所示，富氧空气G1经泥气静态混合器26与湿式氧化前高温污泥S3进行混合，形成添加富氧空气的湿式氧化前高温污泥S4，而后进入管道式污泥反应器23。在管道式污泥反应器23的反应管路231内设置若干混合旋流结构，以利于污泥与氧化剂(富氧空气)的充分混合调质而强化反应过程。管道式污泥反应器23内设置有加热器22用于进一步提高污泥温度，从而调控湿式氧化反应的温度。
如图1所示，反应污泥中的部分有机物在高温高压条件下和氧气进行反应，将大分子有机物降解为小分子有机酸，反应生成的反应气经气液分离器25排出一部分或者不排(排放比例为0-50％)，排出的部分反应器部生成气G2排入反应气吸收罐5中，其大部分或者全部反应气经管道式污泥换热器21随反应污泥排入反应泥压力储罐3中，反应气与泥水在重力的作用下在反应泥压力储罐3中分离分层。这样管道式污泥换热器21中固液气(泥中的固相+污水液相+反应气气相)三相流动可以通过气液分离器25调控反应高温污泥在管道式污泥换热器21中的压力降，在最大程度利用反应后污泥的压力降(压力能)和强化换热的同时可减缓后序调控阀门的磨损，也提高了工艺过程的稳定可控性(增加了反应气，则相应增加了流动阻力，也强化了换热；调控阀门的压力降显著降低可以显著提高其寿命)。管 道式污泥换热器21中反应后污泥的压力一般在1.8-5.4MPa，在排入反应泥压力储罐3前需要将物料的压力降下来，通过保留部分或者全部反应气(一般调控范围保留50％-100％反应气)在管道式污泥换热器21中，可以实现上述调控目的，还回收了反应气的热能，达到节能降耗的效果。常规技术是在反应器出口排出反应气，反应污泥的压力靠后序的阀门调控，很容易造成阀门损坏，通常几天就更换阀门；而且反应气后序还需要冷却，也浪费了热能。常规的换热器内部流体如果为三相物料，很容易出现柱塞流、分层流、局部沉积和较大压力波动等，而本专利采用蜿蜒的管道式有机固废自换热和反应集合组件，反应气是在等径或者接近等径的长管道中流动，而且是蜿蜒逐渐由下往上流，以及在管道中设置了大量的旋流混合结构，可保证三相物料与反应气混合比较均匀而不会出现柱塞流、分层流、局部沉积和较大压力波动等现象。
如图1所示，管道式自换热和反应集合组件2包括用于自换热的管道式污泥换热器21和用于湿式氧化反应的管道式污泥反应器23。如图1所示的实施例的管道式污泥换热器21和管道式污泥反应器23连接为一体，所组成的管道式自换热和反应集合组件2为一体式结构，也可以为分离式结构，根据需要选择。
如图1所示，湿式氧化后高温污泥S6在管道式污泥换热器21中与低温的第二泥水混合污泥S2进行换热冷却后，制得湿式氧化后带压低温污泥S7，而后流入反应泥压力储罐3中。反应泥压力储罐3中通过接收湿式氧化后带压低温污泥S7将剩余压力能进行了储存，通过在反应泥压力储罐3中设置安全阀可调控储罐中的压力，一方面可减少反应泥进入反应泥压力储罐3的压力调节阀的压力调节范围和幅度，提高该调节阀的寿命和工艺稳定可靠性，另一方面可将该压力能用于后续的反应泥脱水工艺中(作为后续反应泥脱水输送动力)，从而可以大幅减少反应泥脱水能耗。具体的，如图1所示，湿式氧化后污泥S8可在压力输送下直接进入机械脱水单元6进行脱水，如果反应泥压力储罐3中压力不够用于污泥脱水，则可在脱水水泵10的输送下进入机械脱水单元6，脱水后的固体产物OSP形成可资源化的产品，而脱水工艺分离出的机械脱水污水W2流入污水箱7。本发明湿式氧化工艺的固相产品一一湿式氧化后有机固体产物OSP，满足纸包装材料原料的标准规范要求，可以作为包装用(瓦楞)纸和代木的添加原料，一般可添加30％-50％，不仅可省木材原料资源和节省原材料成本，而且还提高了添加本工艺有机固废处理产物后的包装类纸板和代木的强度和隔热性能，是优质的包装类纸板和代木原料，而且需求量巨大；另外，该工艺的固相产品一一湿式氧化后有机固体产物，符合园林、土地修复、甚至农用等标准的要求，也可以作为有机肥土资源化利用。
如图1所示，多余的反应泥压力储罐生成气G3与气液分离器中排出的反应器部生成气G2混合形成混合反应气G4进入反应气吸收罐5中。来自污水箱7中的吸收废水W6在反应气吸收罐5中上部喷淋而下，与混合反应气G4在反应气吸收罐中进行热质交换，部分凝结性气体溶解在水体中，形成吸收气废水W7回流至污水箱7，不凝结性气体G5达标后排放至大气中。
由图1和图3对比可知：图3中的实施例还提供了一种内置漂浮抽吸单元31的反应泥压力储罐3，漂浮抽吸单元31下部连接软管，再通过管道与污泥泵9的注水口相连。经过湿式氧化处理的污泥在反应泥压力储罐3内静置一段时间后，泥水分层明显，上层液体中含泥量明显降低，漂浮抽吸单元31漂浮在反应泥压力储罐3的上清液上部。设置漂浮抽吸单元31可将反应泥压力储罐3的上清液在反应泥压力储罐3内压力的驱动下注入污泥泵9内与污泥进行调质混合，通过调节电动阀可以调节注入流量大小。该部件的设置不仅可以不需要设置注水泵11，节省从污水箱7中抽取回注污水W3的注水泵功耗，而且大幅减少机械脱水单元6等工艺所需要处理的污泥量，显著提高工艺的经济性。为了提高运行操作的灵活性，可以同时设置注水泵11从污水箱7中抽取工艺注水注入污泥泵9内与污泥进行调质混合，和在反应泥压力储罐3内设置漂浮抽吸单元31将反应泥压力储罐3内的上清液注入污泥泵9内与污泥进行调质混合，如图4所示。也就是，图1、图3和图4所示的实施例中的高含固率的原泥注水工艺，是通过污泥泵9将来自污泥储罐1中的有机固废泥OSW和来自污水箱7中的回注污水W3进行初步的混合，和/或，利用反应泥压力储罐3中的压力能将储罐上层的上清液W1注入污泥泵9中，与有机固废泥OSW进行混合，制得第一泥水混合污泥S1。工艺注水W0至少部分来自污水箱的回注污水和/或反应泥压力储罐的上清液由图3和图5对比可知：在图3中，污水箱7的外排污水W4需要经处理后达标排放，主要适合于远离污水处理厂的情况。污水箱7的机械脱水污水W2由于含有大量的乙酸等小分子酸，可以作为污水处理厂污水反硝化工艺的碳源，因此就可以直接送至污水处理厂。图3和图5的实施例差异，图3的机械脱水污水需要经处理后达标排放，主要适合于远离污水处理厂的情况；而图5中的机械脱水污水被送至污水处理厂作为污水反硝化工艺的碳源，主要适合于临近污水处理厂建设的或者建设在污水处理厂内。本发明的图3和图5示例的一种有机固废湿式氧化处理装置，可视具体情况选择。
由图1和图6对比可知：在图1中，污水箱7的回注污水W3通过污水泵9的接口注入污泥泵9内，并在污泥泵9内部与外料污泥OSP进行预混合；而图6中，污水箱7的回注污水W3则在污泥泵9与管道式污泥换热器21之间的连接管道上或者在泥水静态混合器 24上接入(在泥水静态混合器24上设置接口，实施例未标出)，OSP和工艺注水W0在管道内流动过程中进行混合处理。尽管图6的从管道和泥水静态混合器24上注入工艺注水是一种可选项，但图1所示的从污水泵9的接口注入工艺注水更为合理，可视具体情况选择。
由图5和图7对比可知：在图5中，设置气液分离器25，湿式氧化后高温污泥S5通过气液分离器25将气液进行部分分离和排出(排出比例范围大约0-50％)，形成反应器部生成气G2和部分排气湿式氧化后高温污泥S6；以及，反应器部生成气G2进入反应气吸收罐3和吸收废水W6进行冷凝换热，不凝气体达标后排入大气；冷凝后的液体形成吸收气废水W7回流至污水箱7。但在某些情况下，允许湿式氧化后高温污泥S5中的全部气相进入管道式污泥换热器21中的第二换热管路212中而无需向反应气吸收罐3排出部分反应器部生成气G2，这样整个污泥处理工艺只是反应泥压力储罐3上部排出气相，而反应泥压力储罐3上部排出气相基本满足达标要求，无需通过反应气吸收罐5二次吸收污染气相，因此，在该情况下则可以不设置反应气吸收罐5和喷淋管路系统(包括喷淋水泵12和相应连接管道)，即如图7所示。但从便于运行调控的角度出发，优选图5所示的设置气液分离器25和反应气吸收罐3以及喷淋管路系统。
如图1、图3、图4和图8、图9、图10所示，本发明还提供了一种有机固废湿式氧化处理工艺，通过上述有机固废湿式氧化处理系统对有机固废进行处理，包括如下步骤：
工艺步骤一：有机固废泥与水混合以形成泥水混合污泥(可选择)
如图1、图3、图4和图8、图9、图10所示，通过污泥泵9将来自污泥储罐1中的有机固废泥OSW和工艺注水W0进行初步的混合处理，从而制得第一泥水混合污泥S1，和/或，利用反应泥压力储罐3中的压力能将储罐上层的上清液注入污泥泵9中，与有机固废泥OSW进行混合制得第一泥水混合污泥S1。含水率增加的混合污泥流动性得到明显改善，特别是一般加入的工艺注水是将污泥包裹即水包泥，可以明显降低污泥输送能耗；(说明：如果临近污水处理厂，则可以将待处理污泥的含固率适当降低，可以节省前序污泥脱水能耗，因而其待处理污泥的流动性比较好，这样就无需向待处理污泥中注水。)
进一步的，可选择地通过粉碎机13对第一泥水混合污泥S1中的大颗粒物质和长纤维物质进行剪切破碎，如果来泥比较均细则通常可以省略该污泥粉碎工艺步骤；
进一步的，可选择地通过泥水静态混合器24对第一泥水混合污泥S 1和工艺注水W0进行混合制得第二泥水混合污泥S2。
本工艺步骤一是将外来高含固率原泥注水制得流动性好的泥水混合污泥物便于泵送，可根据需要选择。
工艺步骤二：污泥在管道式污泥换热器中换热升温
如图2、图3和图9所示，通过蜿蜒的管道式污泥热器部21将低温的第二泥水混合污泥S2和从管道式污泥反应器部23中流出的部分排气湿式氧化后高温污泥S6进行换热，以使得低温的第二泥水混合污泥S2被加热形成湿式氧化前高温污泥S3，高温的部分排气湿式氧化后高温污泥S6被降温以形成湿式氧化后带压低温污泥S7。
工艺步骤三：添加湿式氧化的氧化剂(富氧空气)
如图2、图3和图9所示，湿式氧化前高温污泥S3通过泥气静态混合器26和来自富氧空气机单元4制得的富氧空气G1进行混合，以制得添加富氧空气的湿式氧化前高温污泥S4。如果经济性合理，还可选择双氧水、纯氧替代富氧空气。添加的湿式氧化的氧化剂(富氧空气)应该适量，多则无益而且需多消耗能源，少则湿式氧化产物不能达标。
工艺步骤四：污泥在管道式污泥反应器中反应
如图2、图3和图9所示，添加富氧空气的湿式氧化前高温污泥S4流入蜿蜒管道式反应器23，在管道式反应器内发生湿式氧化反应，以制得湿式氧化后高温污泥S5；
进一步的，添加富氧空气的湿式氧化前高温污泥根据反应的需要，开启加热器22进行加热，以控制湿式氧化的反应温度。
需要说明的是，本实施例添加的氧化反应物为富氧空气，比较安全、稳定和经济，也可根据实际情况选择双氧水、纯氧气，甚至必要时还可以添加一定量的氧化反应催化剂。
工艺步骤五：反应气部分排气与系统压力调控
如图2、图3和图9所示，湿式氧化后高温污泥S5通过气液分离器25将气液进行部分分离和排出(排出比例范围大约0-50％)，形成反应器部生成气G2和部分排气湿式氧化后高温污泥S6；
进一步的，反应器部生成气G2进入反应气吸收罐3和吸收废水W6进行冷凝换热，不凝气体达标后排入大气；冷凝后的液体形成吸收气废水W7回流至污水箱7。
需要说明的是，现有技术是将反应器中可溢出的不凝气体(主要为氧气和氮气)排出以免进入后续的工艺设备和管路如换热器产生柱塞流、分层流、局部沉积和较大压力波动等(气液固三相流动特别容易出现的现象)，而本专利采用的管道式有机固废自换热和反应单元组件，反应气是在等径或者接近等径的长管道中流动，而且是蜿蜒逐渐由下往上流，以及在管道中设置了大量的旋流混合结构，可保证三相物料不会出现柱塞流、分层流、局部沉积和较大压力波动等现象，因此本专利方案是控制湿式氧化后高温污泥S5中可溢出不凝性气体的排出比例，排出比例范围为0-50％，可以实现适当提高后续流动压力降以获得强化换 热、提高反应后泥的控制阀门寿命以及回收反应气的热能的效果。
工艺步骤六：反应泥降温
部分排气(包含不排气)湿式氧化后高温污泥S6流入管道式污泥换热器21的第二换热管路212与第一换热管路211中的低温的第二泥水混合污泥S2进行换热而降温，以制得湿式氧化后带压低温污泥S7。说明：通过泥泥换热，可最大限度回收工艺过程中的热能；管道式污泥热器21的第二换热管路212中流体为气液固三相流，在第一换热管路211和第二换热管路212内均设置若干混合旋流结构，可以防止出现分层、沉积甚至柱塞流等，可以实现气液固比较均质的流动和强化传热过程等优良效果。
工艺步骤七：反应泥压力储罐储泥、储压力能和调控系统压力
湿式氧化后带压低温污泥S7进入反应泥压力储罐3进行存储以制得湿式氧化后污泥S8，反应气在反应泥压力储罐3析出，并储存压力能。具体的，部分或反应器部生成气G2排入反应气吸收罐5中，其大部分或者全部反应气(一般调控比例为50％-100％)经管道式污泥换热器21随反应污泥排入反应泥压力储罐3中，反应气与泥水在重力的作用下在反应泥压力储罐3中分离而存储在反应泥压力储罐3的上部，调控反应泥压力储罐3的压力(在反应泥压力储罐3上部设置有排气压力调控阀门)可以调控前序系统压力(主要是调控反应器中压力)。
另外，湿式氧化后带压低温污泥S7进入反应泥压力储罐3存储静置一定时间后，反应后污泥会出现分层，液相上部为上清液(含少量固相的污水)下部为高含固率的污泥，在反应泥压力储罐3内设置的漂浮抽吸上清液单元31，可漂浮在反应泥压力储罐3内储存的反应后污泥的上部，与漂浮抽吸上清液单元31连接有软管，通过管道与污泥泵9的注入管道相连接，上部的上清液在反应泥压力储罐3的压力作用下注入污泥泵9中，即可大幅减少机械脱水单元的污泥处理量，同时还节省了从污水箱向污泥泵9注水的注水泵11功耗。
说明：本工艺步骤一方面是将反应后污泥储存起来以便后序间歇式脱水，将系统中多余剩余压力能储存起来以降低后序脱水工艺能耗，另一方面可利用该压力能和储罐初沉作用向污泥泵中注水以降低注水泵的能耗即污泥注水调质工艺能耗，再一方面系统压力是通过可控排气阀门的调节来实现，因而比现有技术的换热器后反应后污泥的调控阀门压力降的范围更小，可以大大延长调控阀门的寿命和提高系统的稳定性，而且还可以强化换热。反应器污泥湿式氧化反应过程是在一定的压力和温度下进行的，压力一般在2.0MPa以上，而后续的换热等工艺过程压力通常不足以消耗掉该压力能，这就造成后续控制阀门寿命短、可靠性差等问题，因此，利用反应泥压力储罐3储存一部分压力能可一举多得获得多项正收益。
工艺步骤八：污泥脱水
湿式氧化后污泥S8通过机械脱水单元6进行固液分离制得泥饼OSP和分离液-机械脱水污水W2。
说明：经过湿式氧化处理的泥饼OSP可作为包装用(瓦楞)纸的掺混原料一般可添加最佳比例达30-50％，不仅可以获得良好社会效益即实现有机固废资源化利用，而且还由于资源化利用而显著提高了其经济性；另外也可以作为园林绿化用地的营养土。
另外，机械脱水污水W2流入污水箱7作为系统其他部件所需的工艺注水W0(回注污水W3)，多余的污水可选择经过污水处理单元8进行处理后达标排放，也可以选择作为污水处理厂反硝化的碳源。
如图1所示，具体设计湿式氧化工艺及参数如下：对于有机固废为含水率80％的市政污泥(假设固体有机质含量大约35％-65％)，第一泥水混合污泥S1的含水率为90％左右(一般为87％-93％流动性比较合适，最佳含水率与泥质有关)和温度为30℃，在污泥泵9泵送下，压力大约为2.4MPa至3.5MPa，经过泥水静态混合器初步混合调质后为第二泥水混合污泥S2。第二泥水混合污泥S2流经管道式污泥换热器加热至温度170-190℃，流经加热器加热使得污泥温度达到200℃(反应温度与泥质和反应后污泥的资源化有关，一般为180-230℃)，如果流经管道式污泥换热器21后的污泥达到180-190℃，则加热器基本无需工作。反应污泥在压力大约为2.0MPa至3.2MPa、温度200℃状态下进入管道式污泥反应器中进行湿式氧化反应，在发生湿式氧化过程前加入富氧空气(一般氧浓度大约60％)，富氧空气由富氧空气机单元提供，在湿式氧化反应过程中由于氧化反应放热污泥继续升温大约10-30℃，因此，污泥经湿式氧化后的湿式氧化后高温污泥温度为200℃、压力为大约2.0-3.2MPa，然后经管道式污泥换热器换热降温至大约40-50℃，压力为大约0.5-2.0MPa，而后流入反应泥压力储罐，在设计工况下，尽量使得反应泥压力储罐内的压力为1.0-1.2MPa，如此，不仅可以最大程度利用压力降强化换热，而且可减缓管道式污泥换热器出口管道上调控阀门的磨损，同时提高了工艺过程的稳定可控性(增加了反应气，则相应增加了流动阻力，也强化了换热；换热器后的污泥调控阀门的压力降显著降低可以显著提高其寿命)；另外，反应泥压力储罐储存一部分压力能，可将该压力能用于后续的反应泥脱水工艺中(作为后续反应泥脱水输送动力)，从而可以大幅减少反应泥脱水能耗，也可用于原泥注水调质工艺中，减少注水泵能耗。需要说明的是，在某些条件下，如有机固废污泥中的有机质偏低、环境温度偏低、换热器结垢导致换热效能下降等，需要加热器适当补热；以及，在系统启动过程中，需要加热器为污泥提供启动热能。另外，在设计工况条件下，合理合计可以保证基本无需加热器加热工 艺过程，本发明的湿式氧化工艺在设计工艺参数条件下可以自持，也就是大部分时候可以实现自持，因而工艺过程能耗极低。
通过上述湿式氧化工艺，完全可以实现有机固废的减量化、稳定化、无害化和资源化等处理目标。对于含水率大约80％的市政污泥，采用本发明的湿式氧化工艺，易腐易降解有机质(蛋白质、脂肪、糖类、抗生素等)被氧化变为稳定的、无污染的主要以乙酸为主的小分子有机酸进入液相中和气体CO 2排入大气中，病原菌完全灭活，而且重金属部分被剔除，达到了稳定化和无害化的要求；其机械脱水后的固体产物，含水率为40％以下，重量只剩下原来的25％以下，减量化75％以上；采用本发明的湿式氧化工艺的固相产品，木质素、纤维素和不溶腐植酸在固相产品中被保留下来，粒径也可满足包装类纸板或者包装用复合木板生产的原料的相关标准规范的要求，可以添加在原有原料中，试验表明添加比例最佳范围为30-50％，以及除作为包装类纸板生产原料和代木外，还用作农林用肥基，符合园林、土地修复、甚至农用等标准，从而不仅实现全资源化而且还可以获得显著的资源化经济效益。
与现有技术相比，本发明结构简单、合理，通过蜿蜒的管道式自换热和反应集合组件实现了低温污泥和高温污泥的高效换热，回收了绝大部分工艺热量，大幅降低工艺能耗；同时通过泥水静态混合器和污水泵或管道内实现污泥和工艺注水(板框滤液和/或反应泥压力储罐内上清液)的混合，减少调质罐等部件和工艺环节，简化了工艺流程，同时通过在管道式自换热和反应集合组件内的管道式通道中设置有大量的旋流混合结构，使得污泥和水在流动过程中就可以实现流体的混合，再加上蜿蜒管道式通道达数百米甚至千米，因而其中流动的污泥和水可以实现充分的混合。可选择的通过气液分离器能够释放反应器产生的反应气，以调节流入管道式污泥换热器的第二换热管路的高温污泥的压力降，在最大程度利用压力降强化换热的同时可减缓后序调控阀门的磨损，也提高了工艺过程的稳定可控性。反应泥压力储罐储存一部分从反应器排入反应泥压力储罐中的反应泥的压力能可用于后续的反应泥脱水工艺中(作为后续反应泥脱水输送动力，不足部分可以采用泵送补充)，也可作为原泥注水调质工艺中(作为反应泥压力储罐上清液的输送动力)，从而可以大幅减少反应泥脱水能耗和原泥注水调质工艺能耗。
以上公开的仅为本发明的实施例，但是，本发明并非局限于此，任何本领域的技术人员能思之的变化都应落入本发明的保护范围。

Claims (19)

  1. 一种有机固废湿式氧化处理系统，其特征在于，包括污泥储罐、管道式自换热和反应集合组件、反应泥压力储罐、机械脱水单元、污水箱和污泥泵；
    所述污泥储罐用于储存待处理的有机固废泥；
    所述污泥泵设置在污泥储罐与管道式自换热和反应集合组件之间的输送管路上，该污泥泵用于将污泥储罐内的有机固废泥泵送给管道式自换热和反应集合组件并通过掺水将有机固废泥与工艺注水初步混合以形成泥水混合污泥；
    所述管道式自换热和反应集合组件包括用于泥-泥换热的管道式污泥换热器、用于湿式氧化反应的管道式污泥反应器、气液分离器和泥气静态混合器；
    其中，所述管道式污泥换热器包括供泥水混合污泥流动的第一换热管路、以及供部分排气湿式氧化后高温污泥流动的第二换热管路，所述第一换热管路与第二换热管路之间进行换热以将泥水混合污泥和部分排气湿式氧化后高温污泥分别转化为湿式氧化前高温污泥和湿式氧化后带压低温污泥；
    所述管道式污泥反应器包括反应管路，该反应管路串接于第一换热管路的出口与第二换热管路的进口之间，所述泥气静态混合器设置在第一换热管路与反应管路之间管路上，用于在湿式氧化反应前高温污泥内添加湿式氧化反应所需的氧化剂以制得添加氧化剂的湿式氧化前高温污泥；
    所述反应管路用于接收添加氧化剂的湿式氧化前高温污泥并通过湿式氧化反应以制得湿式氧化后高温污泥；
    所述气液分离器设置在反应管路与第二换热管路之间的管路上，其用于可操控的将湿式氧化后高温污泥中的反应气分离排出，以形成部分排气湿式氧化后高温污泥；
    所述反应泥压力储罐用于接收第二换热管路生成的湿式氧化后带压低温污泥并进行排气降压以制得湿式氧化后污泥；
    所述机械脱水单元用于接收湿式氧化后污泥并对其进行脱水；
    所述污水箱用于接收、存储机械单元脱出的污水。
  2. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，还包括反应气吸收罐，该反应气吸收罐用于接收气液分离器分离出的反应气、以及反应泥压力储罐排出的反应气。
  3. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，还包括泥水静态混合器，所述泥水静态混合器设置在污泥泵与管道式自换热和反应集合组件之间的输送管路上，用于实现有机固废泥与工艺注水的再次混合。
  4. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，还包括富氧空气机单元，所述富氧空气机单元制备富氧空气，并与所述泥气静态混合器连接，将富氧空气注入所述泥气静态混合器中并经混合后注入所述管道式污泥反应器中参与湿式氧化反应。
  5. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，还包括粉碎机，所述粉碎机设置在污泥泵与管道式自换热和反应集合组件之间的输送管路上，用于对泥水混合污泥进行剪切破碎。
  6. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，所述反应泥压力储罐内设置有漂浮抽吸单元，该漂浮抽吸单元漂浮于反应泥压力储罐上方分层的上清液上部并通过连接管道将其上清液排出。
  7. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，所述管道式自换热和反应集合组件还包括加热器，所述加热器用于加热管道式污泥反应器以控制湿式氧化反应温度。
  8. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，所述第一换热管路和/或第二换热管路和/或反应管路内设置有若干混合旋流结构。
  9. 根据权利要求1所述的一种有机固废湿式氧化处理系统，其特征在于，所述管道式污泥换热器的第一换热管路和第二换热管路为蜿蜒结构布置；
    和/或管道式污泥反应器的反应管路为蜿蜒结构布置。
  10. 根据权利要求6所述的一种有机固废热水解处理系统，其特征在于，所述有机固废泥掺水改性的所述工艺注水至少包括所述反应泥压力储罐内的上清液和/或来自所述污水箱的回注污水。
  11. 根据权利要求1、3和10所述的一种有机固废热水解处理系统，其特征在于，所述工艺注水通过污泥储罐至管道式自换热和反应集合组件之间的管路和设备注入有机固废泥中。
  12. 一种有机固废湿式氧化处理工艺，其特征在于，包括以下步骤：
    步骤一：有机固废泥与工艺注水混合以形成泥水混合污泥
    至少通过污泥泵将来自污泥储罐的有机固废泥与工艺注水进行初次混合以制的第一泥水混合污泥；
    步骤二：污泥在管道式污泥换热器中换热升温
    通过管道式污泥换热器将低温的泥水混合污泥和从管道式污泥反应器中流出的部分排气湿式氧化后高温污泥进行换热，以使得低温的泥水混合污泥被加热形成为湿式氧化前高温污泥，部分排气湿式氧化后高温被降温以形成为湿式氧化后带压低温污泥；
    步骤三：添加湿式氧化的氧化剂
    湿式氧化前高温污泥通过泥气静态混合器与氧化剂混合以形成添加氧化剂的湿式氧化前高温污泥；
    步骤四：污泥在管道式污泥反应器中反应
    添加氧化剂的湿式氧化前高温污泥在管道式污泥反应器中进行湿式氧化反应以制得湿式氧化后高温污泥；
    步骤五：反应气部分排气与系统压力调控
    湿式氧化后高温污泥通过气液分离器进行气液分离将部分反应气控制排出，以制得部分排气湿式氧化后高温污泥；
    步骤六：反应泥降温
    部分排气湿式氧化后高温污泥流入管道式污泥换热器的第二换热管路并与第一换热管路内的低温的污水混合污泥进行换热而降温，以转化为湿式氧化后带压低温污泥；
    步骤七：反应泥压力储罐储泥、储压力能和调控系统压力
    湿式氧化后带压低温污泥进入反应泥压力储罐进行存储以制得湿式氧化后污泥，反应气在反应泥压力储罐析出，并储存压力能；
    步骤八：污泥脱水
    湿式氧化后污泥通过机械脱水单元进行固液分离脱水。
  13. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤一中的污泥泵掺混的工艺注水至少部分来自污水箱的回注污水和/或反应泥压力储罐的上清液。
  14. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤一中还包括通过泥水静态混合器对第一泥水混合污泥与水进行再次混合以制得第二泥水混合污泥。
  15. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤一中还包括通过粉碎机对第一泥水混合污泥进行剪切破碎。
  16. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤四中还包括通过加热器加热管道式污泥反应器以控制湿式氧化反应的温度。
  17. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤五中气液分器分离排出的反应气比例为0～50％。
  18. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤七中还包括通过漂浮抽吸单元抽离反应泥压力储罐上方分层的上清液并至少部分供应给污泥泵。
  19. 根据权利要求12所述的一种有机固废湿式氧化处理工艺，其特征在于，在步骤八还包 括通过污水箱接收、储存机械脱水单元脱出的污水并通过注水泵至少将部分污水供应给污泥泵。
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