CN113511788A

CN113511788A - Organic solid waste wet oxidation treatment system and treatment process thereof

Info

Publication number: CN113511788A
Application number: CN202111018151.6A
Authority: CN
Inventors: 孟继安
Original assignee: Tsinghua University
Current assignee: Qingyuan Collaborative Environment Suzhou Co ltd
Priority date: 2020-12-03
Filing date: 2021-09-01
Publication date: 2021-10-19
Anticipated expiration: 2041-09-01
Also published as: WO2022116633A1; CN112679064A; CN113511788B

Abstract

The invention discloses an organic solid waste wet oxidation treatment system and a treatment process thereof, wherein the system comprises a sludge storage tank, a pipeline type self-heat exchange and reaction assembly, a reaction mud pressure storage tank, a mechanical dehydration unit, a sewage tank, a sludge pump and a water injection pump; the sludge pump can realize the mixing of the sludge and the process water injection, and the tempering of a tempering tank in the traditional process is omitted; the pressure drop can be regulated and controlled by mud-mud heat exchange and wet oxidation reaction of the pipeline type self-heat exchange and reaction assembly and by controlling the proportion of reaction gas remained in the pipeline type self-heat exchange and reaction assembly; the reaction mud pressure storage tank is used for storing the pressure energy of a part of reaction mud and primarily settling the reaction mud, so that the adjusting range of the adjusting valve can be reduced, the service life of the valve can be prolonged, and the pressure energy can be used for dehydration of the reaction mud and reinjection tempering of supernatant, so that most heat in the process can be fully recovered, the process energy consumption is greatly reduced, the product can be recycled, and remarkable environmental protection and economic benefits can be obtained.

Description

Organic solid waste wet oxidation treatment system and treatment process thereof

Technical Field

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.

Background

With the continuous promotion of urbanization in China and the continuous improvement of environmental protection requirements, the treatment of organic solid wastes, particularly a large amount of municipal sludge, household garbage and kitchen waste is more and more emphasized. The organic solid waste refers to solid and semi-solid organic waste which is produced by human beings in activities such as production and living and pollutes the environment, the organic solid waste generally comprises municipal sludge, industrial sludge, kitchen waste, household garbage, particularly wet garbage, river bottom mud, high-concentration organic waste liquid, excrement and the like, the slurry prepared from the organic solid waste has similar chemical and physical properties with the municipal sludge, and the similar treatment process and technology of the municipal sludge can be adopted. For convenience of description, the slurry (including municipal sludge) prepared from the organic solid waste is called organic solid waste sludge or sludge for short. Among a plurality of sludge treatment technologies, the wet oxidation treatment process for sludge has the advantages of no three-waste (gas, liquid and solid) discharge, convenience for resource utilization and the like, and can become a mainstream treatment technology in the future, but the process technology also has the following problems or defects and needs to be further perfected and developed:

(1) because the sludge has high viscosity and is inconvenient to pump, the prior wet oxidation process technology arranges a stirring and mixing conditioning tank for stirring and mixing the sludge with high solid content before the sludge enters a heat exchanger, fully stirs and mixes the sludge and water in the conditioning tank, and improves the fluidity of the sludge through conditioning treatment. If the sludge heat exchanger and the reactor can be used for quenching and tempering synchronously, the process link can be simplified, the quenching and tempering process equipment can be reduced, and the construction cost and the operating cost can be reduced.

(2) The wet oxidation reaction needs to be carried out in a high-temperature high-pressure liquid phase, the temperature of the sludge in a general reactor is 160-370 ℃ and the pressure is 1.8-5.4MPa, the high-temperature sludge after the wet oxidation reaction firstly discharges the gas which can overflow from the reaction, then the high-temperature sludge enters a heat exchanger to transfer the heat to the low-temperature sludge before the wet oxidation, and the sludge after the temperature reduction reaction enters a flash tank to be flash-evaporated and cooled. There are therefore two problems or disadvantages with the process: firstly, the energy of the discharged high-temperature high-pressure gas cannot be recovered at high grade, and secondly, the sludge pressure at the outlet of the heat exchanger is still high, and the sludge pressure needs to be further reduced by adjusting the opening of a valve on a pipeline connected with a flash tank, however, the heat exchanger in the current market has poor heat exchange effect, the temperature of the sludge at the outlet of the heat exchanger is often higher than 110 ℃, and is even higher than 140 ℃ and the pressure is more than 1.0MPa, so that the control valve is easy to damage in the severe process environment (high-temperature high-pressure), the valve needs to be replaced frequently, and the reliability and the stability of the system are also reduced. If part or all of the reaction gas can be retained in the high-temperature reacted sludge and flows through the heat exchanger, on one hand, the heat energy of the reaction gas can be recovered, on the other hand, the pressure drop of the reacted sludge in the heat exchanger can be properly increased, and the pressure of the reacted sludge discharged by the heat exchanger is greatly reduced, so that the service life of a regulating valve of the regulating valve can be greatly prolonged, on the other hand, the reaction gas can be used for strengthening the sludge heat exchange, and multiple purposes can be achieved.

(3) The existing wet oxidation process technology discharges sludge subjected to wet oxidation into a flash tank for cooling and pressure relief, and then conveys the sludge to a mechanical dehydration unit through a sludge pump for solid-liquid separation, so that the pressure energy carried by the sludge and reaction gas cannot be well utilized. If the pressure energy is utilized for the subsequent dehydration process, obvious energy-saving effect is obtained.

(4) The existing wet oxidation process technology discharges sludge after wet oxidation into a flash tank for cooling and pressure relief, and the sludge is completely conveyed to dehydration after being cooled by cooling water, if primary precipitation is carried out before the sludge after oxidation is dehydrated and primary precipitation sewage (supernatant containing a small amount of solid phase) is returned to the sludge before reaction for improving the fluidity of the sludge before reaction instead of modifying raw sludge by sewage dehydrated by reaction sludge conventionally (the improvement of fluidity by injecting water into the raw sludge can be called as 'raw sludge water injection modifying process'), the dehydration amount and dehydration energy consumption of the sludge after reaction can be greatly reduced, and if the pressure energy stored in a sludge pressure storage tank after reaction is reused and the primary precipitation is carried out on the sludge after reaction, the water injection energy consumption of the raw sludge water injection modifying process can be reduced. That is to say, can utilize the mud storage tank after the reaction to store the pressure energy and carry out the mud preliminary sedimentation after the reaction, carry out former mud water injection quenching and tempering technology with the supernatant reinjection of preliminary sedimentation, not only can reduce mud dehydration volume and dehydration energy consumption after the reaction by a wide margin, but also can reduce the water injection energy consumption of former mud water injection quenching and tempering technology, kill many birds with one stone.

(5) The existing wet oxidation process technology mainly adopts an intermediate medium (water or oil) circulating heat exchange technology to recover the heat of the high-temperature sludge, namely the heat of the high-temperature sludge is transferred to the low-temperature sludge and needs to be transferred through medium water or oil of an intermediate loop, so that the heat transfer resistance is increased, the heat transfer effect is poor, and the process energy consumption is high. If the direct high-efficiency sludge-sludge heat exchange can be realized, a remarkable energy-saving effect can be obtained.

Disclosure of Invention

The invention aims to overcome the defects in the prior art and provides an organic solid waste wet oxidation treatment system.A certain amount of process water injection is added into a sludge pump and/or a sludge conveying pipeline before a sludge inlet of a pipeline type sludge heat exchanger, and the sludge and the process water injection are preliminarily mixed and then enter the pipeline type sludge heat exchanger and a subsequent pipeline type reactor, so that the process of fully stirring and tempering by arranging a tempering tank and the corresponding energy consumption in the conventional process are saved; the pressure drop of the reaction mud in the pipeline type sludge heat exchanger is regulated and controlled by controlling the proportion of the reaction gas remained in the pipeline type sludge heat exchanger, so that the regulation and control of the sludge reaction pressure in the reaction process in the pipeline type reactor and the heat exchange of the pipeline type sludge heat exchanger are enhanced, the service life of a regulating and controlling valve can be greatly prolonged, and the stable controllability of the process is improved; the method is characterized in that a reaction mud pressure storage tank is arranged to store a part of pressure energy of reaction mud discharged into the reaction mud pressure storage tank from a reactor, the reaction mud pressure storage tank is utilized to carry out primary sedimentation and stratification on the reacted mud so that heavy components in the reacted mud settle at the bottom of the reaction mud pressure storage tank and light components of sewage (supernatant) are arranged at the upper part of the reaction mud pressure storage tank, on one hand, the pressure regulation range and the pressure amplitude of the reaction mud entering a pressure regulation valve of the reaction mud pressure storage tank can be reduced, the service life of the regulation valve and the process stability and reliability can be improved, on the other hand, the pressure energy can be used in a subsequent reaction mud dehydration process (as subsequent reaction mud dehydration conveying power), the sewage, namely the supernatant at the upper part of the reaction mud pressure storage tank can also be used as process water injection to be added into the raw mud, namely, the pressure energy of the reaction mud pressure storage tank and the primary tempering and sedimentation effects on the reacted mud are utilized to realize the raw mud water injection process, therefore, the energy consumption for dehydrating the reaction mud can be greatly reduced, and the pump power consumption of the original mud water injection process can be saved; the invention also provides a treatment process using the organic solid waste wet oxidation treatment system, which has all the characteristics of the treatment system.

In order to achieve the aim, the invention provides an organic solid waste wet oxidation treatment system, which comprises 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, wherein the pipeline type self-heat exchange and reaction assembly is arranged in the sludge storage tank;

the sludge storage tank is used for storing organic solid waste sludge to be treated;

the sludge pump is arranged on a conveying pipeline between the sludge storage tank and the pipeline type self-heat exchange and reaction assembly, and is used for pumping the organic solid waste sludge in the sludge storage tank to the pipeline type self-heat exchange and reaction assembly and preliminarily mixing the organic solid waste sludge with process water injection through water mixing to form sludge-water mixed sludge;

the pipeline type self-heat-exchange and reaction assembly comprises a pipeline type sludge heat exchanger for sludge-sludge heat exchange, a pipeline type sludge reactor for wet oxidation reaction, a gas-liquid separator and a sludge-gas static mixer;

the pipeline type sludge heat exchanger comprises a first heat exchange pipeline for flowing of mud-water mixed sludge and a second heat exchange pipeline for flowing of high-temperature sludge after partial exhaust wet oxidation, wherein heat exchange is carried out between the first heat exchange pipeline and the second heat exchange pipeline so as to convert the mud-water mixed sludge and partial high-temperature sludge after exhaust wet oxidation into high-temperature sludge before wet oxidation and low-temperature sludge under pressure after wet oxidation respectively;

the pipeline type sludge reactor comprises a reaction pipeline, the reaction pipeline is connected in series between an outlet of the first heat exchange pipeline and an inlet of the second heat exchange pipeline, and the sludge gas static mixer is arranged on a pipeline between the first heat exchange pipeline and the reaction pipeline and is used for adding an oxidant required by a wet oxidation reaction into high-temperature sludge before the wet oxidation reaction so as to prepare high-temperature sludge before the wet oxidation reaction with the oxidant added;

the reaction pipeline is used for receiving the high-temperature sludge before wet oxidation added with the oxidant and preparing the high-temperature sludge after wet oxidation through wet oxidation reaction;

the gas-liquid separator is arranged on a pipeline between the reaction pipeline and the second heat exchange pipeline and is used for separating and discharging reaction gas in the wet-oxidized high-temperature sludge in an operable manner so as to form part of exhausted wet-oxidized high-temperature sludge;

the reaction sludge pressure storage tank is used for receiving wet-oxidized pressurized low-temperature sludge generated by the second heat exchange pipeline and performing exhaust depressurization to prepare wet-oxidized sludge;

the mechanical dehydration unit is used for receiving the wet-oxidized sludge and dehydrating the wet-oxidized sludge;

the sewage tank is used for receiving and storing sewage discharged by the mechanical unit.

Further setting the following steps: the reaction gas absorption tank is used for receiving the reaction gas separated by the gas-liquid separator and the reaction gas discharged by the reaction mud pressure storage tank.

Further setting the following steps: still include muddy water static mixer, muddy water static mixer sets up on the pipeline between sludge pump and pipeline formula self heat transfer and reaction aggregate subassembly for realize the remixing of organic solid waste mud and technology water injection.

Further setting the following steps: the system also comprises an oxygen-enriched air machine unit, wherein the oxygen-enriched air machine unit is used for preparing oxygen-enriched air, is connected with the mud gas static mixer, and injects the oxygen-enriched air into the mud gas static mixer, mixes the oxygen-enriched air and then injects the mixed air into the pipeline type mud reactor to participate in wet oxidation reaction.

Further setting the following steps: still include the rubbing crusher, the rubbing crusher setting is on the conveyer pipe way between sludge pump and pipeline formula self heat transfer and reaction assembly subassembly for shear the breakage to muddy water mixed sludge.

Further setting the following steps: and a floating suction unit is arranged in the reaction mud pressure storage tank, floats on the upper part of the supernatant layered above the reaction mud pressure storage tank and discharges the supernatant through a connecting pipeline.

Further setting the following steps: the pipeline type self-heat-exchange and reaction 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.

Further setting the following steps: and a plurality of mixed rotational flow structures are arranged in the first heat exchange pipeline and/or the second heat exchange pipeline and/or the reaction pipeline.

Further setting the following steps: the first heat exchange pipeline and the second heat exchange pipeline of the pipeline type sludge heat exchanger are arranged in a winding structure;

and/or the reaction pipeline of the pipeline type sludge reactor is arranged in a winding structure.

Further setting the following steps: the process water injection for the organic solid waste mud water-mixing modification at least comprises supernatant in the reaction mud pressure storage tank and/or reinjection sewage from the sewage tank.

Further setting the following steps: the process water injection is injected into the organic solid waste mud through a pipeline and equipment between the sludge storage tank and the pipeline type self-heat exchange and reaction assembly.

The invention also provides an organic solid waste wet oxidation treatment process, which comprises the following steps:

the method comprises the following steps: mixing the organic solid waste sludge with process water injection to form sludge-water mixed sludge

At least mixing organic solid waste sludge from a sludge storage tank with process flooding water by a sludge pump to prepare first sludge-water mixed sludge;

step two: sludge heat exchange and temperature rise in pipeline type sludge heat exchanger

Performing heat exchange on low-temperature mud-water mixed sludge and part of exhaust gas high-temperature sludge flowing out of the pipeline type sludge reactor after wet oxidation through a pipeline type sludge heat exchanger so that the low-temperature mud-water mixed sludge is heated to form high-temperature sludge before wet oxidation, and part of exhaust gas high-temperature sludge after wet oxidation is cooled to form wet oxidation pressurized low-temperature sludge;

step three: addition of wet-oxidised oxidant

Mixing the wet pre-oxidation high-temperature sludge with an oxidant through a sludge gas static mixer to form wet pre-oxidation high-temperature sludge added with the oxidant;

step four: the sludge is reacted in a pipeline type sludge reactor

Carrying out wet oxidation reaction on the high-temperature sludge before wet oxidation added with the oxidant in a pipeline type sludge reactor to prepare high-temperature sludge after wet oxidation;

step five: partial exhaust of reaction gas and regulation of system pressure

Performing gas-liquid separation on the wet-oxidized high-temperature sludge through a gas-liquid separator to discharge part of reaction gas in a control manner so as to prepare part of exhausted wet-oxidized high-temperature sludge;

step six: cooling of reaction mud

Part of high-temperature sludge after exhaust wet oxidation flows into a second heat exchange pipeline of the pipeline type sludge heat exchanger and exchanges heat with low-temperature sewage mixed sludge in the first heat exchange pipeline to reduce the temperature so as to be converted into wet-oxidized pressurized low-temperature sludge;

step seven: reaction mud pressure storage tank stores mud, stores pressure energy and regulates and controls system pressure

After wet oxidation, the low-temperature sludge with pressure enters a reaction sludge pressure storage tank to be stored so as to prepare wet oxidized sludge, reaction gas is separated out in the reaction sludge pressure storage tank, and pressure energy is stored;

step eight: sludge dewatering

And (4) performing solid-liquid separation and dehydration on the wet-oxidized sludge through a mechanical dehydration unit.

Further setting the following steps: and injecting at least part of the return sewage from the sewage tank and/or the supernatant of the reaction mud pressure storage tank by the process water of the sludge pump blending in the step one.

Further setting the following steps: the first step further comprises the step of mixing the first muddy water mixed sludge and water again through a muddy water static mixer to prepare second muddy water mixed sludge.

Further setting the following steps: and the first step of shearing and crushing the first sludge-water mixed sludge through a crusher.

Further setting the following steps: the fourth step also comprises heating the pipeline sludge reactor by a heater to control the temperature of the wet oxidation reaction.

Further setting the following steps: in the fifth step, the proportion of the reaction gas separated and discharged by the gas-liquid separator is 0-50%.

Further setting the following steps: and the seventh step comprises the step of pumping supernatant liquid layered above the reaction sludge pressure storage tank through a floating suction unit and at least partially supplying the supernatant liquid to a sludge pump.

Further setting the following steps: step eight further comprises receiving and storing the sewage extracted by the mechanical dewatering unit through a sewage tank and supplying at least a part of the sewage to a sludge pump through a water injection pump.

Compared with the prior art, the invention has the following advantages:

1) the sludge to be treated is organic solid waste sludge with high solid content, sewage with a certain proportion is mixed in a muddy water static mixer and/or a preorder sludge pump and/or a preorder conveying pipeline, the mixture is primarily mixed by the muddy water static mixer or the preorder sludge pump and then enters a winding pipeline type channel of a pipeline type sludge heat exchanger and a subsequent pipeline type sludge reactor to be fully mixed again (a large number of rotational flow mixing structures are arranged in the pipeline type channel, the sludge and water can be mixed when flowing in the channel, and the winding pipeline type channel reaches hundreds of meters or even kilometers, so that the flowing sludge and water can be fully mixed), the conventional technology is simplified, the hardening and tempering process of stirring and mixing (a hardening and tempering tank is arranged and water is fully stirred in the sludge to fully mix the sludge and water injection) is required to be arranged before the sludge with high solid content enters the pipeline type sludge heat exchanger, not only simplifies the process equipment, but also saves the sludge conditioning energy.

2) Oxygen-enriched air enters the pipeline type sludge reactor through the sludge gas static mixer, oxygen in the oxygen-enriched air reacts with part of organic matters in the sludge under the conditions of high temperature, high pressure and wet state, reaction gas generated by the reaction is discharged partially through the gas-liquid separator in an adjustable mode, most or all of the reaction gas is discharged into a reaction sludge pressure storage tank along with the reaction sludge through a self heat exchanger, so that the pressure drop of the reaction high-temperature sludge in the heat exchanger can be regulated and controlled through the three-phase flow of solid-liquid gas (solid phase in the sludge, sewage liquid phase and reaction gas phase) in the heat exchanger, the abrasion of a subsequent regulating valve can be reduced while the heat exchange is strengthened by utilizing the pressure drop to the maximum extent, the stable controllability of the process is also improved (the reaction gas is increased, the flow resistance is correspondingly increased, and the heat exchange is strengthened; a significant reduction in the pressure drop across the regulating valve can significantly increase its life). The pressure of the reaction sludge in the reactor is generally about 1.8-5.4MPa, the pressure of the materials needs to be reduced before the materials are discharged into a reaction sludge pressure storage tank, the regulation and control purposes can be realized by retaining part or all of the reaction gas (50% -100% of the reaction gas is retained in a general regulation and control range) in a heat exchanger, the heat energy of the reaction gas is also recovered, and the effects of saving energy and reducing consumption are achieved. The conventional technology is that reaction gas which can overflow is discharged from the outlet of the reactor, the pressure of the reaction sludge is regulated and controlled by a subsequent regulating and controlling valve, the valve is easy to damage, and the valve is usually replaced for several days; moreover, the reaction gas needs to be cooled in the subsequent process, and the heat energy is also wasted. If the conventional heat exchanger is a three-phase material, plug flow, stratified flow, local deposition, large pressure fluctuation and the like can easily occur, the serpentine pipeline type self-heat exchange and reaction assembly adopted by the heat exchanger disclosed by the patent has the advantages that reaction gas flows in a long pipeline with the same diameter or close to the same diameter and gradually flows from bottom to top in a serpentine mode, and a large number of rotational flow mixing structures are arranged in the pipeline, so that the phenomena of plug flow, stratified flow, local deposition, large pressure fluctuation and the like of the three-phase material can be avoided.

3) Set up reaction mud pressure storage tank, store the partial pressure ability of discharging into the reaction mud in the reaction mud pressure storage tank from the reactor, reducible reaction mud gets into the pressure adjustment scope and the range of the pressure regulating valve of reaction mud pressure storage tank on the one hand, on the other hand can be used for this pressure ability in subsequent reaction mud dehydration technology (as follow-up reaction mud dehydration power of carrying), also can be used for among the mud water injection quenching and tempering technology (as the power of carrying of supernatant in the reaction mud pressure storage tank), thereby can reduce reaction mud dehydration energy consumption and water injection pump consumption by a wide margin.

Drawings

FIG. 1 is a schematic diagram of a wet oxidation treatment system for organic solid waste according to the present invention;

FIG. 2 is a schematic view of the structural principle of a tubular self heat exchange and wet oxidation reaction assembly of the present invention;

FIG. 3 is a schematic structural diagram of a wet oxidation treatment system for organic solid wastes according to the present invention;

FIG. 4 is a schematic structural diagram III of a wet oxidation treatment system for organic solid wastes according to the present invention;

FIG. 5 is a schematic structural diagram of a wet oxidation treatment system for organic solid wastes according to the fourth embodiment of the present invention;

FIG. 6 is a schematic structural diagram of a wet oxidation treatment system for organic solid wastes according to the present invention;

FIG. 7 is a schematic structural diagram six of a wet oxidation treatment system for organic solid wastes according to the present invention;

FIG. 8 is a first schematic diagram of a frame-shaped process of wet oxidation treatment of organic solid wastes according to the present invention;

FIG. 9 is a schematic diagram of a second frame-shaped process of wet oxidation treatment of organic solid wastes according to the present invention;

FIG. 10 is a third schematic diagram of a frame-shaped process of wet oxidation treatment of organic solid wastes according to the present invention.

The following reference numerals are marked thereon in conjunction with the accompanying drawings:

1. a sludge storage tank; 2. The pipeline type self heat exchange and reaction assembly component; 21. a pipeline type sludge heat exchanger; 211. a first heat exchange line; 212. a second heat exchange line; 22. a heater; 23. a pipeline type sludge reactor; 231. a reaction pipeline; 24. a static mud-water premixer; 25. a gas-liquid separator; 26. a mud gas static mixer; 3. a reaction mud pressure storage tank; 31. a floating suction unit; 4. an oxygen-enriched air machine unit; 5. a reaction gas absorption tank; 6. a mechanical dewatering unit; 7. a sewage tank; 8. a sewage treatment unit; 9. a sludge pump; 10. a dewatering water pump; 11. a water injection pump; 12. A spray water pump; 13. a pulverizer;

OSW, organic solid waste sludge; OSP, organic solid product after wet oxidation.

S1, first sludge-water mixed sludge; s2, mixing the second sludge and water; s3, wet pre-oxidation high-temperature sludge; s4, adding oxygen-enriched air to the wet-type pre-oxidation high-temperature sludge; s5, wet-oxidizing the high-temperature sludge; s6, partial exhaust wet oxidation high-temperature sludge; s7, wet-oxidizing the low-temperature sludge with pressure; s8, wet-oxidized sludge;

w0, process water injection; w1, supernatant; w2, mechanically dewatering sewage; w3, reinjection of sewage; w4, discharging sewage; w5, discharge water reaching the standard; w6, absorbing waste water; w7, absorption gas waste water; w8, a sewage treatment plant is used as carbon source discharge water;

g1, oxygen-enriched compressed air; g2, reactor section product gas; g3, generating gas by a reaction mud pressure storage tank; g4, mixed reaction gas; g5, exhausting gas outside the standard.

Detailed Description

An embodiment of the present invention will be described in detail below with reference to the accompanying drawings, but it should be understood that the scope of the present invention is not limited to the embodiment.

The invention discloses an organic solid waste wet oxidation treatment system, which is shown in figure 1, and mainly comprises a sludge storage tank 1, a pipeline type self-heat exchange and reaction assembly 2, a reaction sludge pressure storage tank 3, an oxygen-enriched air machine unit 4, a reaction gas absorption tank 5, a mechanical dehydration unit 6, a sewage tank 7 and a plurality of pumping devices, wherein the pumping devices comprise a sludge pump 9, a dehydration water pump 10, a water injection pump 11 and a spray water pump 12, and a crusher 13 and a sewage treatment unit 8 are selectively arranged according to requirements; wherein, the pipeline type self heat exchange and reaction assembly 2 comprises a pipeline type sludge heat exchanger 21 for self heat exchange, a pipeline type sludge reactor 23 for wet oxidation reaction, a gas-liquid separator 25, a sludge-gas static mixer 26, a sludge-water static mixer 24 and a heater 22, the pipeline type sludge heat exchanger 21 comprises a first heat exchange pipeline 211 and a second heat exchange pipeline 212 which are arranged in a winding way, and the pipeline type sludge reactor 23 comprises a reaction pipeline 231 which is arranged in a winding way.

Specifically, as shown in fig. 1, the external 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 primarily mixed according to a certain ratio by the sludge pump 9 to prepare the first sludge-water mixed sludge S1, wherein the fluidity of the first sludge-water mixed sludge S1 is obviously improved compared with the fluidity of OSW. The reasonable selection of injecting 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 wet oxidation treatment of the sludge, because if the solid content of the organic solid waste sludge OSW is relatively high, such as the solid content of external sludge is about 20% (the water content is about 80%), the high solid content sludge has poor fluidity and is difficult to pump, a certain amount of water is required to be added to reduce the solid content and also reduce the viscosity of the sludge, but the added water is not too much, the high water content of the sludge to be treated can greatly reduce the viscosity, but the energy consumption for conveying is increased, particularly the energy consumption for heating and dehydration of sludge treatment is also obviously increased, and the solid content of the sludge entering the pipeline type self-heat-exchange and reaction assembly 2 is generally controlled between 15% and 5%, and preferably between 12% and 8%. The ratio of process water injection W0 injected into the OSW is related to the original solid content and organic matter content of the OSW. If the organic solid waste sludge OSW is directly close to a sewage treatment plant without being transported outside, the solid content of the organic solid waste sludge OSW can be properly reduced, for example, the solid content is 8-2%, so that the energy consumption of preorder process sludge dewatering can be greatly saved, and at the moment, the flowability of the organic solid waste sludge OSW is good, and process water injection W0 does not need to be added into the organic solid waste sludge OSW. The above-mentioned process of injecting water into raw sludge with high solid content to improve its fluidity is called sludge water injection conditioning process. The process water injection W0 of this embodiment is the reinjection sewage W3 from the sewage tank 7.

As shown in FIG. 1, the first sludge-water mixed sludge S1 can be selectively refined and homogenized by the pulverizer 13 for large-particle materials and long-fiber materials, and if the incoming materials are uniform and have small particle size, such as sludge from sewage treatment plants directly, the pulverizer 13 is not needed. The refined and homogenized sludge is beneficial to subsequent treatment and resource utilization. The first sludge-water mixed sludge S1 flows into the pipeline type self-heat-exchange and reaction assembly component 2 to carry out self-heat-exchange and wet-type oxidation reaction, thereby completing the process of degrading organic matters in the sludge.

As shown in fig. 1 and 2, first, the static mixer 24 pre-mixes the first sludge-water mixed sludge S1 optionally with the process water injection W0 (in this example, the reinjection wastewater W3 from the wastewater tank 7) to prepare the second sludge-water mixed sludge S2 which is convenient to transport and has an appropriate solid content. The process water injection W0 may be injected in a certain amount from the static mixer 24 for muddy water as needed, or the process water injection W0 may not be injected from the static mixer 24 for muddy water but the process water injection W0 may be injected in a certain amount only from the sludge pump 9. The process water injection W0 can be injected from the pipeline and the equipment between the sludge storage tank 1 and the pipeline type self-heat exchange and reaction assembly 2, comprises the sludge pump 9 and the sludge-water static mixer 24, and is preferably injected from the sludge pump 9 in view of implementation convenience and effect, the conveying power consumption of the sludge pump 9 can be reduced, and the process water injection W0 is a preferred process scheme. The second sludge-water mixed sludge S2 enters the pipeline type sludge heat exchanger 21 of the pipeline type self-heat exchange and reaction assembly component 2 and a winding pipeline type channel in the subsequent pipeline type sludge reactor 23 to be fully mixed again (a large number of rotational flow mixing structures are arranged in the winding pipeline type channel, the mixing of fluid can be realized when the sludge and water flow in the winding pipeline type channel, and the winding pipeline type channel reaches hundreds of meters or even thousands of meters, so that the flowing sludge and water can be fully mixed), the hardening and tempering process that the stirring and mixing are required to be arranged before the sludge with high solid content enters the heat exchanger in the conventional technology is simplified (the hardening and tempering tank is arranged in the conventional technology, the raw sludge and the water are fully mixed by injecting water in the raw sludge with high solid content), the process equipment is simplified, and the energy consumption of sludge hardening and tempering is saved.

As shown in fig. 1, the low-temperature second sludge-water mixed sludge S2 flows into the first heat exchange pipeline 211 of the pipeline-type sludge heat exchanger 21 and the second heat exchange pipeline 212, and part of the exhaust gas flowing from the pipeline-type sludge reactor 23 in the wet-type oxidation high-temperature sludge S6 exchanges heat, and the heat exchange of the high-temperature sludge and the low-temperature sludge is set as counter-current heat exchange, so that the logarithmic heat exchange temperature difference is smaller, and the heat exchange effect is efficient, therefore, the low-temperature sludge S2 after the low-temperature second sludge S2 is heated up to form the high-temperature sludge S3 before the wet-type oxidation, and the high-temperature sludge S6 after the partial exhaust gas wet-type oxidation is cooled to the low-temperature sludge S7 under pressure after the wet-type oxidation, and the pipeline-type sludge heat exchanger 21 can realize self-heating process, i.e. sludge-sludge heat exchange, thereby recovering process heat energy to the maximum, even under some circumstances can realize the self-sustaining of the process, and remarkably reduce the energy consumption of the organic solid waste sludge wet-type oxidation treatment system, the energy-saving economic benefit is also obviously improved, and the operation cost of the organic solid waste wet oxidation treatment is extremely low. The first heat exchange pipeline 211 of the pipeline type sludge heat exchanger 21 is internally provided with a plurality of mixed rotational flow structures, so that the sludge-water mixed sludge can be fully mixed and tempered to improve the fluidity of the sludge-water mixed sludge and the heat exchange process can be enhanced, the second heat exchange pipeline 212 of the pipeline type sludge heat exchanger 21 is internally provided with a plurality of mixed rotational flow structures, so that the sludge and the reaction generated gas can be fully mixed and homogenized after the reaction, and the problems of plunger flow, stratified flow, local deposition, large pressure fluctuation and the like of gas-liquid-solid three-phase flow can be avoided.

As shown in FIG. 1, oxygen-enriched air G1 is mixed with the high-temperature sludge before wet oxidation S3 by the static mixer 26 to form high-temperature sludge before wet oxidation S4 added with oxygen-enriched air, and then enters the pipeline type sludge reactor 23. A plurality of mixed rotational flow structures are arranged in a reaction pipeline 231 of the pipeline type sludge reactor 23, so that the sludge and the oxidant (oxygen-enriched air) can be fully mixed and tempered to strengthen the reaction process. The pipe-type sludge reactor 23 is provided therein with a heater 22 for further raising the sludge temperature, thereby regulating the temperature of the wet oxidation reaction.

As shown in fig. 1, a part of organic matters in the reaction sludge reacts with oxygen under high temperature and high pressure to degrade macromolecular organic matters into small molecular organic acids, a part of or no part of reaction gas generated by the reaction is discharged through a gas-liquid separator 25 (the discharge ratio is 0-50%), a part of discharged reactor part generated gas G2 is discharged into a reaction gas absorption tank 5, most or all of the reaction gas is discharged into a reaction sludge pressure storage tank 3 along with the reaction sludge through a pipeline type sludge heat exchanger 21, and the reaction gas and sludge water are separated and layered in the reaction sludge pressure storage tank 3 under the action of gravity. Therefore, the solid-liquid-gas (solid phase in mud + sewage liquid phase + reaction gas phase) three-phase flow in the pipeline type sludge heat exchanger 21 can regulate and control the pressure drop of the reaction high-temperature sludge in the pipeline type sludge heat exchanger 21 through the gas-liquid separator 25, the pressure drop (pressure energy) of the sludge after the reaction is utilized to the maximum extent, the abrasion of a subsequent regulating valve can be reduced while the heat exchange is enhanced, the stability and controllability of the technological process are improved (the reaction gas is increased, the flow resistance is correspondingly increased, the heat exchange is enhanced, and the service life of the regulating valve can be obviously prolonged by obviously reducing the pressure drop of the regulating valve). The pressure of the sludge after reaction in the pipeline type sludge heat exchanger 21 is generally 1.8-5.4MPa, the pressure of the materials needs to be reduced before the materials are discharged into the reaction sludge pressure storage tank 3, and the regulation and control purposes can be realized by retaining part or all of the reaction gas (50% -100% of the reaction gas is retained in the general regulation and control range) in the pipeline type sludge heat exchanger 21, and the heat energy of the reaction gas is also recovered, so that the effects of saving energy and reducing consumption are achieved. The conventional technology is that reaction gas is discharged from the outlet of the reactor, the pressure of reaction sludge is regulated and controlled by a subsequent valve, the valve is easy to damage, and the valve is usually replaced for several days; moreover, the reaction gas needs to be cooled in the subsequent process, and the heat energy is also wasted. If the fluid in the conventional heat exchanger is a three-phase material, plug flow, stratified flow, local deposition, large pressure fluctuation and the like easily occur, the heat exchanger adopts a winding pipeline type organic solid waste self-heat exchange and reaction assembly, the reaction gas flows in a long pipeline with the same diameter or close to the same diameter and gradually flows from bottom to top in a winding manner, and a large number of rotational flow mixing structures are arranged in the pipeline, so that the three-phase material and the reaction gas can be uniformly mixed without the phenomena of plug flow, stratified flow, local deposition, large pressure fluctuation and the like.

As shown in fig. 1, the ducted self heat exchanging and reaction assembly 2 includes a ducted sludge heat exchanger 21 for self heat exchange and a ducted sludge reactor 23 for wet oxidation reaction. The pipe-type sludge heat exchanger 21 and the pipe-type sludge reactor 23 of the embodiment shown in fig. 1 are connected into a whole, and the formed pipe-type self-heat-exchange and reaction assembly 2 is of an integrated structure, or can be of a separate structure, and is selected according to requirements.

As shown in fig. 1, the wet-oxidized high-temperature sludge S6 is heat-exchanged and cooled with the low-temperature second sludge-water mixed sludge S2 in the pipe-type sludge heat exchanger 21 to prepare wet-oxidized pressurized low-temperature sludge S7, and then the wet-oxidized pressurized low-temperature sludge flows into the reaction sludge pressure storage tank 3. Low temperature mud S7 takes pressure to store residual pressure energy through receiving wet oxidation back pressure in the reaction mud pressure storage tank 3, can regulate and control the pressure in the storage tank through setting up the relief valve in reaction mud pressure storage tank 3, reducible reaction mud gets into the pressure control range and the range of the pressure control valve of reaction mud pressure storage tank 3 on the one hand, improve the life-span and the technology reliability and stability of this governing valve, on the other hand can be used for this pressure energy in subsequent reaction mud dehydration technology (as follow-up reaction mud dehydration power of carrying), thereby can reduce reaction mud dehydration energy consumption by a wide margin. Specifically, as shown in fig. 1, the wet oxidized sludge S8 can be directly fed into the mechanical dewatering unit 6 for dewatering under pressure transmission, if the pressure in the reaction sludge pressure storage tank 3 is insufficient for sludge dewatering, the wet oxidized sludge S8 can be fed into the mechanical dewatering unit 6 under the transmission of the dewatering water pump 10, the dewatered solid product OSP forms a recyclable product, and the mechanical dewatered sewage W2 separated in the dewatering process flows into the sewage tank 7. The solid phase product of the wet oxidation process, namely the organic solid product OSP after wet oxidation, meets the standard and standard requirements of paper packaging material raw materials, can be used as the adding raw materials of (corrugated) paper for packaging and wood substitutes, can be added by 30-50 percent generally, not only can save wood raw material resources and save raw material cost, but also improves the strength and heat insulation performance of the packaging paper boards and the wood substitutes after the organic solid waste treatment product of the process is added, is a high-quality packaging paper board and wood substitute raw material, and has huge demand; in addition, the solid phase product of the process, namely the organic solid product after wet oxidation, meets the requirements of standards of gardens, land restoration, even agriculture and the like, and can be used as organic fertile soil for resource utilization.

As shown in fig. 1, the excess reaction sludge pressure storage tank generated gas G3 is mixed with the reactor section generated gas G2 discharged from the gas-liquid separator to form a mixed reaction gas G4, and the mixed reaction gas is introduced into the reaction gas absorption tank 5. The absorption wastewater W6 from the sewage tank 7 is sprayed down from the middle 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, part of the condensable gas is dissolved in the water body to form absorption gas wastewater W7 which flows back to the sewage tank 7, and the non-condensable gas G5 reaches the standard and is discharged to the atmosphere.

As can be seen from a comparison of fig. 1 and 3: the embodiment in fig. 3 also provides a reaction mud pressure storage tank 3 with a built-in floating suction unit 31, wherein the lower part of the floating suction unit 31 is connected with a hose and then is connected with a water filling port of a mud pump 9 through a pipeline. After the sludge subjected to the wet oxidation treatment is kept stand in the reaction sludge pressure storage tank 3 for a period of time, the mud and water are obviously layered, the mud content in the upper layer liquid is obviously reduced, and the floating suction unit 31 floats on the upper part of the supernatant of the reaction sludge pressure storage tank 3. The floating suction unit 31 can inject the supernatant of the reaction mud pressure storage tank 3 into the sludge pump 9 to be mixed with the sludge by regulating the pressure in the reaction mud pressure storage tank 3, and the injection flow can be regulated by regulating the electric valve. The arrangement of the parts can not only save the power consumption of the water injection pump 11 for extracting the reinjection sewage W3 from the sewage tank 7, but also greatly reduce the sludge amount required to be treated by the processes such as the mechanical dehydration unit 6 and the like, and obviously improve the economical efficiency of the processes. In order to improve the flexibility of the operation, a water injection pump 11 can be arranged at the same time to extract process water from the sewage tank 7 and inject the process water into the sludge pump 9 to be mixed with sludge, and a floating suction unit 31 is arranged in the reaction sludge pressure storage tank 3 to inject supernatant in the reaction sludge pressure storage tank 3 into the sludge pump 9 to be mixed with sludge, as shown in fig. 4. That is, in the raw sludge water injection process with high solid content in the embodiment shown in fig. 1, 3 and 4, the organic solid waste sludge OSW from the sludge storage tank 1 and the reinjection sewage W3 from the sewage tank 7 are primarily mixed by the sludge pump 9, and/or the supernatant W1 of the storage tank upper layer can be injected into the sludge pump 9 by utilizing the pressure in the reaction sludge pressure storage tank 3 to be mixed with the organic solid waste sludge OSW, so as to prepare the first sludge-water mixed sludge S1. Process water injection W0 at least partially from the return sewage of the sewage tank and/or the supernatant of the pressure tank for reaction sludge

As can be seen from the comparison between fig. 3 and 5: in fig. 3, the discharged sewage W4 of the sewage tank 7 needs to be treated to reach the discharge standard, and is mainly suitable for the situation far away from the sewage treatment plant. The mechanically dewatered sewage W2 of the sewage tank 7 contains a large amount of small molecular acids such as acetic acid, and can be used as a carbon source for sewage denitrification process in a sewage treatment plant, and thus can be directly sent to the sewage treatment plant. The difference between the embodiments of fig. 3 and fig. 5, the mechanically dewatered sewage of fig. 3 needs to be treated for standard discharge, which is mainly suitable for the situation far away from the sewage treatment plant; whereas the mechanically dewatered sewage in fig. 5 is sent to a sewage treatment plant as a carbon source for the denitrification process of sewage, which is mainly suitable for construction adjacent to or in the sewage treatment plant. The organic solid waste wet oxidation treatment device illustrated in fig. 3 and 5 of the present invention can be selected according to specific situations.

As can be seen from a comparison of fig. 1 and 6: in fig. 1, the return sewage W3 of the sewage tank 7 is fed into the sludge pump 9 through an interface of the sewage pump 9 and premixed with the external sludge OSP inside the sludge pump 9; in fig. 6, the returned sewage W3 of the sewage tank 7 is connected to the connecting pipeline between the sludge pump 9 and the pipeline-type sludge heat exchanger 21 or to the static mixer 24 (an interface is provided on the static mixer 24, and the embodiment is not shown), and the OSP and the process water W0 are mixed during the flowing process in the pipeline. Although the injection of process water from the piping and static mixer 24 of sludge and water of figure 6 is an option, it is more reasonable to inject process water from the interface of the sewage pump 9 as shown in figure 1, as the case may be.

As can be seen from a comparison of fig. 5 and 7: in fig. 5, a gas-liquid separator 25 is provided, and the wet-oxidized high-temperature sludge S5 is subjected to partial separation and discharge of gas and liquid (discharge ratio ranges from about 0% to 50%) by the gas-liquid separator 25 to form a reactor section produced gas G2 and a partial exhaust wet-oxidized high-temperature sludge S6; and the generated gas G2 in the reactor part enters a reaction gas absorption tank 3 and absorbs waste water W6 for condensation heat exchange, and the non-condensable gas reaches the standard and is discharged into the atmosphere; the condensed liquid forms absorption gas waste water W7 and flows back to the sewage tank 7. However, in some cases, the entire gas phase in the wet-oxidized high-temperature sludge S5 is allowed to enter the second heat exchange pipeline 212 in the pipeline-type sludge heat exchanger 21 without discharging part of the reactor section generated gas G2 to the reaction gas absorption tank 3, so that the entire sludge treatment process is only to discharge the gas phase from the upper part of the reaction sludge pressure storage tank 3, and the gas phase discharged from the upper part of the reaction sludge pressure storage tank 3 basically meets the standard requirement without secondary absorption of the contaminated gas phase by the reaction gas absorption tank 5, and therefore, the reaction gas absorption tank 5 and the spray pipeline system (including the spray water pump 12 and the corresponding connecting pipeline) may not be provided in this case, as shown in fig. 7. However, from the viewpoint of easy operation control, it is preferable to provide the gas-liquid separator 25 and the reaction gas absorption tank 3 and the shower piping system as shown in fig. 5.

As shown in fig. 1, fig. 3, fig. 4, fig. 8, fig. 9, and fig. 10, the present invention further provides an organic solid waste wet oxidation treatment process, wherein the organic solid waste wet oxidation treatment system is used for treating organic solid waste, and the process comprises the following steps:

the method comprises the following process steps: mixing the organic solid waste sludge with water to form a sludge-water mixture (optional)

As shown in fig. 1, 3, 4, 8, 9 and 10, the organic solid sludge OSW from the sludge storage tank 1 and the process water injection W0 are primarily mixed by the sludge pump 9 to prepare the first sludge-water mixed sludge S1, and/or the supernatant of the upper layer of the storage tank is injected into the sludge pump 9 by the pressure energy of the reaction sludge pressure storage tank 3 and mixed with the organic solid sludge OSW to prepare the first sludge-water mixed sludge S1. The fluidity of the mixed sludge with increased water content is obviously improved, and particularly, the sludge is wrapped by the commonly added process water injection, namely the water-wrapped sludge, so that the energy consumption for conveying the sludge can be obviously reduced; (it means that if the sludge treatment plant is close to, the solid content of the sludge to be treated can be properly reduced, the energy consumption for dewatering the preorder sludge can be saved, and the fluidity of the sludge to be treated is better, so that water does not need to be injected into the sludge to be treated.)

Further, large-particle matters and long-fiber matters in the first sludge-water mixed sludge S1 may be optionally subjected to shear crushing by the crusher 13, and if the sludge is relatively fine, the sludge crushing process step may be generally omitted;

further, the first sludge-water mixed sludge S1 and the process water injection W0 are mixed optionally by the static sludge-water mixer 24 to prepare a second sludge-water mixed sludge S2.

The process comprises the first step of injecting water into external raw mud with high solid content to obtain mud-water mixed mud with good fluidity, which is convenient for pumping and can be selected according to requirements.

The second process step: sludge heat exchange and temperature rise in pipeline type sludge heat exchanger

As shown in fig. 2, 3 and 9, the low-temperature second sludge-water mixed sludge S2 and the part of the exhaust gas after wet oxidation high-temperature sludge S6 flowing out of the pipeline sludge reactor unit 23 are heat exchanged by the winding pipeline sludge heat exchanger unit 21, so that the low-temperature second sludge-water mixed sludge S2 is heated to form the before-wet oxidation high-temperature sludge S3, and the high-temperature part of the exhaust gas after wet oxidation high-temperature sludge S6 is cooled to form the after-wet oxidation pressurized low-temperature sludge S7.

The third process step: addition of Wet oxidizing Agents (oxygen-enriched air)

As shown in fig. 2, 3 and 9, the high-temperature sludge before wet oxidation S3 is mixed with oxygen-enriched air G1 produced from the oxygen-enriched air machine unit 4 by the sludge gas static mixer 26 to produce high-temperature sludge before wet oxidation S4 to which oxygen-enriched air is added. If the economy is reasonable, hydrogen peroxide and pure oxygen can be selected to replace oxygen-enriched air. The added wet oxidation oxidant (oxygen-enriched air) is proper, so that the added wet oxidation oxidant is not beneficial and consumes more energy, and the added wet oxidation product cannot reach the standard.

The process comprises the following four steps: the sludge is reacted in a pipeline type sludge reactor

As shown in fig. 2, 3 and 9, the high-temperature sludge S4 before wet oxidation to which oxygen-enriched air is added flows into the serpentine pipe reactor 23, and wet oxidation reaction occurs in the pipe reactor to produce wet-oxidized high-temperature sludge S5;

further, the high temperature sludge before wet oxidation added with oxygen-enriched air is heated by turning on the heater 22 according to the reaction requirement to control the reaction temperature of the wet oxidation.

It should be noted that the oxidation reactant added in this embodiment is oxygen-enriched air, which is relatively safe, stable and economical, and hydrogen peroxide and pure oxygen can be selected according to actual situations, and even a certain amount of oxidation reaction catalyst can be added as necessary.

The process comprises the following five steps: partial exhaust of reaction gas and regulation of system pressure

As shown in fig. 2, 3 and 9, the wet-oxidized high-temperature sludge S5 is subjected to partial separation and discharge of gas and liquid (discharge ratio ranges from about 0 to 50%) by the gas-liquid separator 25 to form a reactor section generation gas G2 and a partial exhaust wet-oxidized high-temperature sludge S6;

further, the generated gas G2 in the reactor part enters a reaction gas absorption tank 3 and absorbs waste water W6 for condensation heat exchange, and the non-condensable gas reaches the standard and is discharged into the atmosphere; the condensed liquid forms absorption gas waste water W7 and flows back to the sewage tank 7.

It should be noted that, in the prior art, the non-condensable gas (mainly oxygen and nitrogen) which can overflow from the reactor is discharged to avoid entering the subsequent process equipment and pipelines such as heat exchangers to generate plug flow, stratified flow, local deposition, large pressure fluctuation and the like (the phenomenon that gas-liquid-solid three-phase flow is particularly easy to occur), but the pipeline type organic solid waste self-heat exchange and reaction unit component adopted by the invention has the advantages that the reaction gas flows in a long pipeline with equal diameter or nearly equal diameter and gradually flows from bottom to top in a winding manner, and a large number of rotational flow mixing structures are arranged in the pipeline, so that the phenomena of plug flow, stratified flow, local deposition, large pressure fluctuation and the like of three-phase materials can be ensured not to occur, therefore, the scheme of the invention is to control the discharge proportion of the non-condensable gas which can overflow from the high-temperature sludge S5 after wet oxidation, the discharge proportion range is 0-50%, the effects of properly improving the subsequent flowing pressure drop to obtain the effects of strengthening heat exchange, prolonging the service life of a control valve of the reacted sludge and recovering the heat energy of the reaction gas can be realized.

The process comprises the following six steps: cooling of reaction mud

Part of the exhaust gas (including non-exhaust gas) wet-oxidized high-temperature sludge S6 flows into the second heat exchange pipeline 212 of the pipeline type sludge heat exchanger 21 to exchange heat with the low-temperature second mud-water mixed sludge S2 in the first heat exchange pipeline 211 to reduce the temperature, so as to prepare wet-oxidized pressurized low-temperature sludge S7. Description of the drawings: the heat energy in the process can be recovered to the maximum extent through mud heat exchange; the fluid in the second heat exchange pipeline 212 of the pipeline type sludge heater 21 is gas-liquid-solid three-phase flow, and a plurality of mixed rotational flow structures are arranged in the first heat exchange pipeline 211 and the second heat exchange pipeline 212, so that layering, deposition, plunger flow and the like can be prevented, and good effects of homogeneous gas-liquid-solid flow, heat transfer enhancement and the like can be realized.

The process comprises the following seven steps: reaction mud pressure storage tank stores mud, stores pressure energy and regulates and controls system pressure

And (3) the wet-oxidized pressurized low-temperature sludge S7 enters the reaction sludge pressure storage tank 3 for storage to prepare wet-oxidized sludge S8, and the reaction gas is separated out in the reaction sludge pressure storage tank 3 and stores pressure energy. Specifically, part or reactor portion generated gas G2 is discharged into the reaction gas absorption tank 5, most or all of the reaction gas (generally, the regulation ratio is 50% to 100%) is discharged into the reaction sludge pressure storage tank 3 along with the reaction sludge through the pipeline-type sludge heat exchanger 21, the reaction gas and the sludge water are separated in the reaction sludge pressure storage tank 3 and stored at the upper part of the reaction sludge pressure storage tank 3 under the action of gravity, and the pressure of the reaction sludge pressure storage tank 3 (the upper part of the reaction sludge pressure storage tank 3 is provided with an exhaust pressure regulation valve) can regulate and control the pressure of the preorder system (mainly, the pressure in the reactor).

In addition, after wet-type oxidized pressurized low-temperature sludge S7 enters the reaction sludge pressure storage tank 3 to be stored and placed for a certain time, the reacted sludge can be layered, the upper part of a liquid phase is supernatant (sewage containing a small amount of solid phase) and the lower part of the liquid phase is sludge with high solid content rate, a floating supernatant suction unit 31 is arranged in the reaction sludge pressure storage tank 3 and can float on the upper part of the reacted sludge stored in the reaction sludge pressure storage tank 3, a hose is connected with the floating supernatant suction unit 31 and is connected with an injection pipeline of a sludge pump 9 through a pipeline, and the supernatant on the upper part is injected into the sludge pump 9 under the pressure action of the reaction sludge pressure storage tank 3, so that the sludge treatment capacity of a mechanical dehydration unit can be greatly reduced, and the power consumption of a water injection pump 11 for injecting water from a sewage tank to the sludge pump 9 is also saved.

Description of the drawings: the process steps are that the sludge after reaction is stored for subsequent intermittent dehydration, and the surplus residual pressure in the system can be stored to reduce the energy consumption of the subsequent dehydration process, on the other hand, water can be injected into the sludge pump by utilizing the pressure energy and the primary sedimentation effect of the storage tank to reduce the energy consumption of the water injection pump, namely the energy consumption of the sludge water injection tempering process, on the other hand, the system pressure is realized by adjusting the controllable exhaust valve, so that the pressure drop range of the sludge after reaction in the heat exchanger in the prior art is smaller, the service life of the controllable valve can be greatly prolonged, the stability of the system can be improved, and the heat exchange can be enhanced. The wet oxidation reaction process of the sludge in the reactor is carried out under certain pressure and temperature, the pressure is generally over 2.0MPa, and the pressure in the subsequent processes of heat exchange and the like is not enough to consume the pressure energy, so that the problems of short service life, poor reliability and the like of a subsequent control valve are caused, and therefore, a plurality of positive benefits can be obtained by storing a part of pressure energy by using the reaction sludge pressure storage tank 3.

The process comprises the following steps: sludge dewatering

The wet-oxidized sludge S8 is subjected to solid-liquid separation by a mechanical dehydration unit 6 to obtain a sludge cake OSP and a separation liquid, namely mechanical dehydration sewage W2.

Description of the drawings: the wet oxidation treated mud cake OSP can be used as a blending raw material of packaging (corrugated) paper, the optimal proportion can be added generally by 30-50%, good social benefits can be obtained, namely, the organic solid waste is recycled, and the economical efficiency is obviously improved due to recycling; in addition, the fertilizer can also be used as nutrient soil for landscaping land.

In addition, the mechanically dewatered sewage W2 flows into the sewage tank 7 to be used as process water injection W0 (reinjection sewage W3) required by other parts of the system, and the redundant sewage can be discharged after reaching the standard after being treated by the sewage treatment unit 8 or can be used as a carbon source for denitrification of a sewage treatment plant.

As shown in fig. 1, the wet oxidation process and parameters are specifically designed as follows: for municipal sludge with 80% of water content of organic solid waste (assuming that the content of solid organic matters is about 35% -65%), the water content of the first sludge-water mixed sludge S1 is about 90% (generally 87% -93% is appropriate in fluidity, and the optimal water content is related to sludge), the temperature is 30 ℃, the pressure is about 2.4MPa to 3.5MPa under the pumping of a sludge pump 9, and the sludge-water mixed sludge S2 is obtained after preliminary mixing and tempering by a sludge-water static mixer. The second sludge-water mixed sludge S2 flows through the pipeline type sludge heat exchanger and is heated to the temperature of 170-. The reaction sludge enters a pipeline type sludge reactor for wet oxidation reaction under the conditions that the pressure is about 2.0MPa to 3.2MPa and the temperature is 200 ℃, oxygen-enriched air (generally the oxygen concentration is about 60 percent) is added before the wet oxidation process, the oxygen-enriched air is provided by an oxygen-enriched air machine unit, the temperature of the sludge is continuously increased by about 10 to 30 ℃ because of the heat released by the oxidation reaction in the wet oxidation reaction process, therefore, the temperature of the high-temperature sludge after the wet oxidation of the sludge is 200 ℃ and the pressure is about 2.0 to 3.2MPa, then the temperature is reduced to about 40 to 50 ℃ and the pressure is about 0.5 to 2.0MPa through the heat exchange of a pipeline type sludge heat exchanger, then the sludge flows into a reaction sludge pressure storage tank, under the designed working condition, the pressure in the reaction sludge pressure storage tank is 1.0 to 1.2MPa as much as possible, thus, the heat exchange can be strengthened by utilizing the pressure reduction to the greatest extent, the abrasion of a regulating valve on an outlet pipeline of the pipeline type sludge heat exchanger can be slowed down, and the stability and controllability of the process are improved (the flow resistance is correspondingly increased and the heat exchange is strengthened by increasing the reaction gas); in addition, the reaction mud pressure storage tank stores a part of pressure energy, and the pressure energy can be used in a subsequent reaction mud dehydration process (as subsequent reaction mud dehydration conveying power), so that the reaction mud dehydration energy consumption can be greatly reduced, and the reaction mud pressure storage tank can also be used in an original mud water injection tempering process to reduce the energy consumption of a water injection pump. It should be noted that under certain conditions, for example, organic matter in organic solid waste sludge is low, environmental temperature is low, heat exchange efficiency is reduced due to scaling of a heat exchanger, and the like, a heater is required to supplement heat properly; and, during system start-up, a heater is required to provide start-up heat energy for the sludge. In addition, under the condition of design working conditions, reasonable totaling can ensure that a heater heating process is not needed basically, and the wet oxidation process can be self-sustained under the condition of design process parameters, namely self-sustained can be realized in most of the time, so that the energy consumption of the process is extremely low.

By the wet oxidation process, the treatment targets of reduction, stabilization, harmlessness, recycling and the like of the organic solid wastes can be completely realized. For municipal sludge with water content of about 80%, the wet oxidation process of the invention is adopted, and the perishable and easily degradable organic matters (protein, fat, sugar, antibiotics and the like) are oxidized into stable and pollution-free small molecular organic acid mainly comprising acetic acid and enter a liquid phase to neutralize CO gas₂The pathogenic bacteria are completely inactivated when discharged into the atmosphere, and the heavy metal part is removed, so that the requirements of stabilization and harmlessness are met; the water content of the solid product after mechanical dehydration is below 40 percent, the weight of the solid product is only below 25 percent of the original weight, and the reduction is over 75 percent; the solid phase product adopting the wet oxidation process of the invention has the advantages that lignin, cellulose and insoluble humic acid are reserved in the solid phase product, the grain diameter can also meet the requirements of relevant standard specifications of raw materials for producing packaging paperboards or packaging composite boards, the solid phase product can be added into the original raw materials, tests show that the optimal range of the adding proportion is 30-50%, the solid phase product can be used as a fertilizer base for agriculture and forestry besides being used as a raw material for producing the packaging paperboards and a substitute wood, and meets the standards of gardens, land restoration, even agriculture and the like, thereby not only realizing full-resource but also obtaining remarkable resource economic benefits.

Compared with the prior art, the invention has simple and reasonable structure, realizes the high-efficiency heat exchange of the low-temperature sludge and the high-temperature sludge through the winding pipeline type self-heat exchange and reaction assembly, recovers most of process heat and greatly reduces the process energy consumption; meanwhile, the mixing of sludge and process water injection (plate frame filtrate and/or supernatant in a reaction sludge pressure storage tank) is realized in the sludge-water static mixer and a sewage pump or a pipeline, so that parts and process links such as a conditioning tank are reduced, the process flow is simplified, and meanwhile, a large number of rotational flow mixing structures are arranged in a pipeline type channel in the pipeline type self-heat exchange and reaction assembly, so that the sludge and water can be mixed in a flowing process, and in addition, the winding pipeline type channel reaches hundreds of meters or even kilometers, so that the flowing sludge and water can be fully mixed. The reaction gas generated by the reactor can be released through the gas-liquid separator selectively so as to adjust the pressure drop of the high-temperature sludge flowing into the second heat exchange pipeline of the pipeline type sludge heat exchanger, the abrasion of a subsequent regulating valve can be reduced while the heat exchange is enhanced by utilizing the pressure drop to the maximum extent, and the stability and controllability of the technological process are improved. The pressure energy of the reaction mud stored in the reaction mud pressure storage tank, which is part of the reaction mud discharged into the reaction mud pressure storage tank from the reactor, can be used in a subsequent reaction mud dehydration process (as subsequent reaction mud dehydration conveying power, and the insufficient part can be supplemented by pumping), and can also be used in a raw mud water injection conditioning process (as conveying power of the supernatant 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.

The above disclosure is only an example of the present invention, but the present invention is not limited thereto, and any variations that can be made by those skilled in the art should fall within the scope of the present invention.

Claims

1. An organic solid waste wet oxidation treatment system is characterized by comprising a sludge storage tank, a pipeline type self-heat exchange and reaction assembly component, a reaction sludge pressure storage tank, a mechanical dehydration unit, a sewage tank and a sludge pump;

2. The organic solid waste wet oxidation treatment system according to claim 1, further comprising a reaction gas absorption tank for receiving the reaction gas separated by the gas-liquid separator and the reaction gas discharged from the reaction sludge pressure storage tank.

3. The organic solid waste wet oxidation treatment system according to claim 1, further comprising a static mixer for muddy water, which is disposed on the transportation pipeline between the sludge pump and the assembly of the pipe-type self heat exchange and reaction assembly, for realizing the remixing of the organic solid waste sludge and the process water injection.

4. The organic solid waste wet oxidation treatment system according to claim 1, further comprising an oxygen-enriched air machine unit, wherein the oxygen-enriched air machine unit is used for preparing oxygen-enriched air, is connected with the sludge gas static mixer, and is used for injecting the oxygen-enriched air into the sludge gas static mixer, mixing the oxygen-enriched air and injecting the mixed air into the pipeline type sludge reactor to participate in wet oxidation reaction.

5. The organic solid waste wet oxidation treatment system according to claim 1, further comprising a crusher disposed on the transport pipeline between the sludge pump and the pipeline type self heat exchange and reaction assembly for shearing and crushing the sludge mixed with the muddy water.

6. The organic solid waste wet oxidation treatment system according to claim 1, wherein a floating suction unit is provided in the reaction sludge pressure storage tank, and floats on an upper portion of the supernatant fluid layered above the reaction sludge pressure storage tank and discharges the supernatant fluid through a connection pipe.

7. The organic solid waste wet oxidation treatment system of claim 1, wherein the ducted self heat exchange and reaction assembly further comprises a heater for heating the ducted sludge reactor to control the wet oxidation reaction temperature.

8. The organic solid waste wet oxidation treatment system according to claim 1, wherein a plurality of mixed cyclone structures are arranged in the first heat exchange pipeline and/or the second heat exchange pipeline and/or the reaction pipeline.

9. The organic solid waste wet oxidation treatment system according to claim 1, wherein the first heat exchange pipeline and the second heat exchange pipeline of the pipeline type sludge heat exchanger are arranged in a serpentine structure;

10. The organic solid waste pyrohydrolysis treatment system according to claim 6, wherein the process injection water of the organic solid waste sludge water-blending modification at least comprises supernatant in the reaction sludge pressure storage tank and/or reinjection sewage from the sewage tank.

11. The organic solid waste pyrohydrolysis treatment system according to claims 1, 3 and 10, wherein the process water injection is injected into the organic solid waste sludge through a pipeline and a device between the sludge storage tank and the tubular self heat exchange and reaction assembly.

12. The wet oxidation treatment process for the organic solid wastes is characterized by comprising the following steps of:

step three: addition of wet-oxidised oxidant

step four: the sludge is reacted in a pipeline type sludge reactor

step five: partial exhaust of reaction gas and regulation of system pressure

step six: cooling of reaction mud

step eight: sludge dewatering

13. The wet oxidation treatment process for organic solid wastes according to claim 12, wherein the process water injection of the sludge pump blending in the first step is at least partially from the sewage tank reinjection sewage and/or the supernatant of the reaction sludge pressure storage tank.

14. The wet oxidation treatment process for organic solid waste according to claim 12, further comprising mixing the first sludge-water mixed sludge with water again by the static sludge-water mixer to obtain a second sludge-water mixed sludge in the first step.

15. The wet oxidation treatment process for organic solid waste according to claim 12, further comprising the step of subjecting the first sludge-water mixed sludge to shearing and crushing by a crusher in the first step.

16. The organic solid waste wet oxidation treatment process as claimed in claim 12, further comprising the step of heating the pipe type sludge reactor by a heater to control the temperature of the wet oxidation reaction in the fourth step.

17. The wet oxidation treatment process for organic solid wastes according to claim 12, wherein the proportion of the reaction gas discharged by the gas-liquid separator in the fifth step is 0 to 50%.

18. The wet oxidation treatment process for organic solid wastes according to claim 12, further comprising a step seven of pumping supernatant stratified above the reaction sludge pressure storage tank through a floating suction unit and at least partially supplying the supernatant to a sludge pump.

19. The wet oxidation treatment process for organic solid waste according to claim 12, further comprising receiving and storing the sewage from the mechanical dewatering unit through a sewage tank and supplying at least a portion of the sewage to a sludge pump through a water injection pump in step eight.