CN113024038A - Low-carbon treatment system and method for high-concentration organic wastewater - Google Patents
Low-carbon treatment system and method for high-concentration organic wastewater Download PDFInfo
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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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
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
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- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention discloses a low-carbon treatment system and a low-carbon treatment method for high-concentration organic wastewater, which comprise an adjusting tank, an inner pipe of an energy exchange system I, an inner pipe of an energy exchange system II, an inner pipe of an energy exchange system III, a hydrothermal oxidation system, a gas-liquid separation device, an outer pipe of the energy exchange system II, a sludge filter pressing device, an anaerobic reaction system, an aerobic reaction system and a wetland treatment system which are sequentially connected through a liquid pipeline, and finally, the adjusting tank is discharged; the gas pipeline is sequentially connected with the hydrothermal oxidation system, the gas-liquid separation device, the outer pipe of the energy exchange system I and the alkaline ionic liquid carbon absorption system and is finally discharged; the gas generated by the anaerobic reaction system is sequentially connected with a biogas purification device, a biogas incinerator and an alkaline ionic liquid absorption system through pipelines and is finally discharged; the sludge generated by the aerobic reaction system flows back to the regulating tank through a pump suction pipeline; and the heat conducting oil circulates between the biogas incinerator and the outer pipe of the energy exchange system III through a pipeline.
Description
Technical Field
The invention relates to a wastewater treatment technology, in particular to a high-concentration organic wastewater treatment and low-carbon treatment system and method.
Background
The high-concentration organic wastewater generally refers to wastewater containing high-concentration organic matters discharged by industries such as food, paper making, pesticide and the like, and the COD content of the wastewater is more than 2000 mg/L. These high concentration organic waste water usually contain a large amount of carbohydrates, fats, fibers and the like, even with strong biological toxicity, if the waste water is not properly treated, the ecological environment is extremely easy to be seriously damaged, and the human health is threatened, but the conventional biological treatment process is difficult to directly treat.
The hydrothermal oxidation and oxidation technology is a hydrothermal oxidation process which is provided in the 50 th century and can effectively treat high-concentration, toxic and harmful waste water. The process is characterized in that under the conditions of high temperature (250-350 ℃) and high pressure (0.5-20 MPa), organic matters in the wastewater are converted into H as far as possible by using a strong oxidant2O、CO2And other small molecule organics. In order to further improve the removal rate of COD in the sewage and increase CO2The production rate of the catalyst is increased, and the process adds a supported metal catalyst in the hydrothermal oxidation process, so that the reaction activation energy is reduced, the reaction efficiency is improved, and the energy consumption is reduced.
9 months in 2020, China seriously declares to the world: china strives to reach the peak value of carbon dioxide emission before 2030 years, and strives to realize carbon neutralization before 2060 years. On the national level, the aim of realizing the synergy of pollution reduction and carbon reduction is also provided. Subsequently, more and more experts and scholars are concerned about the research on the synergy of 'pollution reduction and carbon reduction', but are often concerned about the energy consumption part, and CO is generated in the process2Emissions tend to be overlooked. The process mainly aims at a process flow for realizing the synergy of pollution reduction and carbon reduction in the treatment process of high-concentration organic wastewater, finally utilizes the wetland advanced treatment process to further reduce pollutants, realizes tail water recycling, and simultaneously synergistically increases carbon sink energyThe force causes the entire treatment system to reach substantially "near zero carbon".
Disclosure of Invention
The purpose of the invention is as follows: aiming at CO which is often ignored in the current process of treating high-concentration organic wastewater2The application provides a process for removing organic pollutants efficiently and greatly reducing CO2The treatment system and the treatment method have the advantages of discharging, reducing sludge generation, realizing green and environment-friendly tail water recycling, and having good treatment effect.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
a low-carbon treatment system for high-concentration organic wastewater comprises a regulating tank, an energy exchange system I, an energy exchange system II, an energy exchange system III, a hydrothermal oxidation system, a gas-liquid separation device, a sludge filter pressing device, an anaerobic reaction system, an aerobic reaction system, a wetland treatment system, a biogas purification device, a biogas incinerator and an alkaline ionic liquid carbon absorption system;
the regulating tank, the inner pipe of the energy exchange system I, the inner pipe of the energy exchange system II, the inner pipe of the energy exchange system III, the hydrothermal oxidation system and the gas-liquid separation device are sequentially connected through pipelines;
the gas generated by the gas-liquid separation device is sequentially connected with an outer pipe of the energy exchange system I and the alkaline ionic liquid carbon absorption system through pipelines and is finally discharged; liquid generated by the gas-liquid separation device is sequentially connected with an outer pipe of the energy exchange system II, the sludge filter pressing device, the anaerobic reaction system, the aerobic reaction system and the wetland treatment system through pipelines and is finally discharged;
the gas generated by the anaerobic reaction system is sequentially connected with a biogas purification device and a biogas incinerator through pipelines; gas generated by the anaerobic reaction system is purified by a biogas purification device and then is used as fuel of a biogas incinerator to heat conducting oil;
the gas generated by the methane incinerator is led into an alkaline ionic liquid carbon absorption system through a pipeline;
and the outer pipe of the energy exchange system III is filled with heat conduction oil and is connected with the methane incinerator through a pipeline, so that the heat conduction oil is circulated between the outer pipe of the energy exchange system III and the methane incinerator.
Specifically, an outlet of the regulating reservoir is communicated with an inlet of an inner tube of an energy exchange system I, an outlet of the inner tube of the energy exchange system I is communicated with an inlet of an inner tube of an energy exchange system II, an outlet of the inner tube of the energy exchange system II is communicated with an inlet of an inner tube of an energy exchange system III, an outlet of the inner tube of the energy exchange system III is connected with an inlet of a hydrothermal oxidation system, an outlet of the hydrothermal oxidation system is connected with an inlet of a gas-liquid separation device, a gas outlet of the gas-liquid separation device is connected with an inlet of an outer tube of the energy exchange system I, an outlet of the outer tube of the energy exchange system I is connected with an; the liquid outlet of the gas-liquid separation device is connected with the inlet of an outer pipe of an energy exchange system II, the outlet of the outer pipe of the energy exchange system II is connected with the inlet of a sludge press-filtering device, the water outlet of the sludge press-filtering device is connected with the inlet of an anaerobic reaction system, the liquid outlet of the anaerobic reaction system is connected with the inlet of an aerobic reaction system, the outlet of the aerobic reaction system is connected with the inlet of a wetland treatment system, the outlet of the wetland treatment system is recycled for the production process, the gas outlet of the anaerobic reaction system is connected with the inlet of a biogas purification device, the biogas outlet of the biogas purification device is connected with the inlet of a biogas incinerator, the residual gas outlet of the biogas purification device is connected with the inlet of an alkaline ionic liquid carbon absorption system, the outlet of the biogas incinerator is connected with the inlet of an alkaline ionic liquid carbon absorption; the hydrothermal oxidation system is provided with an oxidant inlet.
Preferably, a catalyst is arranged in the hydrothermal oxidation system, the catalyst consists of an integral zeolite carrier and an active component loaded on the carrier, the active component consists of a copper oxide, a manganese oxide and an auxiliary agent cerium oxide, and the catalyst is replaced periodically; the hydrothermal oxidation system adds high-concentration strong oxidants such as: oxygen with the concentration of more than 95 percent, ozone or hydrogen peroxide and the like are used together.
Preferably, the alkaline ionic liquid carbon absorption system adopts a weak-base type ionic liquid, and the weak-base type ionic liquid is preferably an alkyl alcohol amine solution, such as Diethanolamine (DEA) and the like.
Furthermore, the aerobic reaction system is connected to the regulating tank through a return pipeline, the generated sludge is returned to the regulating tank and enters the hydrothermal oxidation system again for thermal decomposition, and the sludge-water separation performance is improved.
Preferably, the anaerobic reaction system is an up-flow anaerobic sludge blanket, the sedimentation zone in the up-flow anaerobic sludge blanket accounts for 20-30% of the total volume, a continuous stirrer is arranged in the anaerobic sludge blanket and is used for fully and uniformly mixing sludge which flows back to the regulating tank from the aerobic reaction system and untreated wastewater, then the sludge is guided into the heat exchange device, and finally the sludge enters the hydrothermal oxidation system for treatment.
Preferably, the biogas generated by the biogas purification system is input into the biogas incinerator through a pipeline and used as fuel of the biogas incinerator to provide heat for the heat conduction oil, so that the consumption of additional energy is reduced.
Preferably, the aerobic reaction system adopts a medium bubble aeration mode, and the aeration quantity is gradually reduced along with the reduction of the COD of the sewage.
Preferably, the wetland system plants in the wetland treatment system mainly select herbaceous plants with strong carbon fixing capacity and fast production, such as bermudagrass, liangyue yuehong, radix ophiopogonis and the like, and the rest are doped with evergreen coniferous trees and evergreen broad-leaved trees (such as masson pine, grifola frondosa and the like).
In order to make the system operate smoothly, the water pumps can be connected in series on the pipeline as required. For example, liquid in the anaerobic reaction system is pumped into the aerobic reaction system between the regulating tank and the energy exchange system I through a water pump, and sludge in the aerobic reaction system is pumped and conveyed to the regulating tank through a sludge pump.
After the high-concentration wastewater is treated by the hydrothermal oxidation system, the anaerobic reaction system, the aerobic reaction system and the wetland treatment system, the near zero emission of organic pollutants is basically realized.
Further, the invention also provides a method for treating high-concentration organic wastewater by adopting the low-carbon treatment system, which comprises the following steps:
(1) hydrothermal oxidation reaction: filtering and deslagging the wastewater to be treated, then guiding the wastewater into an adjusting tank, uniformly stirring, and adjusting the pH value to 7-9; then, the mixture enters a hydrothermal oxidation system after heat exchange of an energy exchange system, a high-concentration strong oxidant is used as an oxidant, the oxidation coefficient is greater than 1.5, the temperature is 280-320 ℃, the pressure is 7-9 Mpa, and the reaction time is 1.5-2.5 hours;
(2) anaerobic reaction treatment: exchanging heat and cooling the liquid product reacted in the step (1), then entering a sludge filter-pressing device for filter pressing and mud removal, and introducing the liquid product into an anaerobic reaction system, wherein a settling zone in an up-flow anaerobic sludge bed accounts for 20-30% of the total volume, a continuous stirrer is arranged in the anaerobic sludge bed, and the reaction time is 2-4 days;
(3) aerobic reaction treatment: and (3) directly introducing the effluent treated in the step (2) into an aerobic reaction system, after 1.5-3 days of aerobic reaction, directly introducing the effluent into a wetland treatment system, wherein the retention time of the wastewater in the wetland treatment system is 5-15 days, and reusing the effluent in a production process.
(4) A carbon absorption system: exchanging heat and cooling the gas product reacted in the step (1), and then introducing the gas product into an alkaline ionic liquid carbon absorption system; and (3) treating the gas generated in the step (2) by using a methane purification device, introducing methane into a methane incinerator for combustion, introducing the gas generated after combustion and the residual gas of the methane purification device into an alkaline ionic liquid carbon absorption system together, performing absorption reaction for 0.5-2 h, performing reaction pressure of 0.1-0.5 MPa, performing reaction temperature of 30-70 ℃, discharging the residual gas after absorption, and performing high-temperature desorption when the alkaline ionic liquid is nearly saturated.
In the step (1), the mass concentration of the catalyst is maintained at 0.1-0.3%; the oxidant is one or more of pure oxygen, ozone or excessive hydrogen peroxide in sufficient quantity.
In the step (3), the aeration rate of the aeration device of the aerobic reaction system is gradually reduced along with the reduction of COD (chemical oxygen demand) of the sewage, and the aeration rate of air for degrading BOD per kilogram is kept to be 85m3Left and right.
Has the advantages that:
(1) the invention adopts a method of combining a hydrothermal oxidation process, a biological treatment process and a wetland treatment process, can effectively reduce residual organic pollutants, chromaticity and heavy metals in the effluent, has the COD removal rate of the wastewater more than or equal to 99.8 percent, and basically realizes near zero emission of COD.
(2) The marsh gas separated by the marsh gas purifying device is burnt by the marsh gas incinerator and then enters the alkaline ionic liquid carbon absorption system together with the residual gas discharged by the marsh gas purifying device, and the gas separated by the gas-liquid separating device also enters the alkaline ionic liquid carbon absorption system, so that the near zero emission of the residual carbon dioxide is basically realized except the carbon dioxide generated by the biological action.
(3) The energy exchange system is arranged behind the hydrothermal oxidation system, so that the reaction waste heat is fully utilized, the energy consumption is reduced, and the CO generated by the external energy consumption is reduced2And (5) discharging. Biogas generated by the anaerobic reaction system is used as a heat source of the heating system, so that the consumption of fossil energy is reduced.
(4) The sludge generated by the aerobic reaction system of the invention flows back to the regulating tank and then enters the hydrothermal oxidation system again to carry out high-temperature pyrolysis on the sludge, thereby improving the dehydration performance of the sludge.
(5) The traditional hydrothermal oxidation treatment hardly realizes the thorough oxidation of organic matters, the invention uses a high-performance catalyst and enough strong oxidant in a hydrothermal oxidation system to treat the organic matters to the maximum extent, the treated effluent is guided into an anaerobic reaction system, micromolecule organic acid generated by the hydrothermal oxidation system is used as nutrient substances of methane bacteria, and the treatment pressure of the aerobic reactor is reduced. On one hand, the organic matter can be fully oxidized and decomposed into CO2The subsequent recovery is convenient; on the other hand, the treatment efficiency of the organic matters is greatly improved.
(6) The wetland system plant of the invention mainly selects herbaceous plants with stronger carbon fixing capacity and faster production, such as bermudagrass, liangyouyuehong, dwarf lilyturf tuber and the like, and the rest is doped with evergreen coniferous trees and evergreen broad-leaved trees (such as masson pine, grifola frondosa and the like), so that the whole wetland system has stronger carbon fixing capacity and organic matter degradation effect.
Drawings
The foregoing and/or other advantages of the invention will become further apparent from the following detailed description of the invention when taken in conjunction with the accompanying drawings.
FIG. 1 is a schematic flow diagram of a high concentration organic wastewater low carbon treatment system according to the present invention.
Detailed Description
The invention will be better understood from the following examples.
The structures, proportions, and dimensions shown in the drawings and described in the specification are for understanding and reading the present disclosure, and are not intended to limit the scope of the present disclosure, which is defined in the claims, and are not essential to the skilled in the art. In addition, the terms "upper", "lower", "front", "rear" and "middle" used in the present specification are for clarity of description, and are not intended to limit the scope of the present invention, and the relative relationship between the terms and the relative positions may be changed or adjusted without substantial technical changes.
Example 1
As shown in fig. 1, the low-carbon treatment system for high-concentration organic wastewater of the invention comprises an adjusting tank, an energy exchange system i, an energy exchange system ii, an energy exchange system iii, a hydrothermal oxidation system, a gas-liquid separation device, a sludge press filtration device, an anaerobic reaction system, an aerobic reaction system, a wetland treatment system, a biogas purification device, a biogas incinerator and an alkaline ionic liquid carbon absorption system.
Wherein, the regulating reservoir, the inner tube of the energy exchange system I, the inner tube of the energy exchange system II, the inner tube of the energy exchange system III, the hydrothermal oxidation system and the gas-liquid separation device are sequentially connected through pipelines.
Gas generated by the gas-liquid separation device is sequentially connected with an outer pipe of the energy exchange system I and the alkaline ionic liquid carbon absorption system through pipelines and is finally discharged; and liquid generated by the gas-liquid separation device is sequentially connected with an outer pipe of the energy exchange system II, the sludge filter pressing device, the anaerobic reaction system, the aerobic reaction system and the wetland treatment system through pipelines and is finally discharged.
The gas generated by the anaerobic reaction system is sequentially connected with a biogas purification device and a biogas incinerator through pipelines; gas generated by the anaerobic reaction system is purified by a biogas purification device and then is used as fuel of a biogas incinerator to heat conducting oil;
and introducing gas generated by the methane incinerator into the alkaline ionic liquid carbon absorption system through a pipeline.
And the outer pipe of the energy exchange system III is filled with heat conduction oil and is connected with the methane incinerator through a pipeline, so that the heat conduction oil is circulated between the outer pipe of the energy exchange system III and the methane incinerator.
Specifically, an outlet of the regulating reservoir is communicated with an inlet of an inner tube of an energy exchange system I, an outlet of the inner tube of the energy exchange system I is communicated with an inlet of an inner tube of an energy exchange system II, an outlet of the inner tube of the energy exchange system II is communicated with an inlet of an inner tube of an energy exchange system III, an outlet of the inner tube of the energy exchange system III is connected with an inlet of a hydrothermal oxidation system, an outlet of the hydrothermal oxidation system is connected with an inlet of a gas-liquid separation device, a gas outlet of the gas-liquid separation device is connected with an inlet of an outer tube of the energy exchange system I, an outlet of the outer tube of the energy exchange system I is connected with; the liquid outlet of the gas-liquid separation device is connected with the inlet of an outer pipe of an energy exchange system II, the outlet of the outer pipe of the energy exchange system II is connected with the inlet of a sludge press-filtering device, the water outlet of the sludge press-filtering device is connected with the inlet of an anaerobic reaction system, the liquid outlet of the anaerobic reaction system is connected with the inlet of an aerobic reaction system, the outlet of the aerobic reaction system is connected with the inlet of a wetland treatment system, the outlet of the wetland treatment system is recycled for the production process, the gas outlet of the anaerobic reaction system is connected with the inlet of a biogas purification device, the biogas outlet of the biogas purification device is connected with the inlet of a biogas incinerator, the residual gas outlet of the biogas purification device is connected with the inlet of an alkaline ionic liquid carbon absorption system, the outlet of the biogas incinerator is connected with the inlet of an alkaline ionic liquid carbon absorption; the hydrothermal oxidation system is provided with an oxidant inlet.
The hydrothermal oxidation system is internally provided with a catalyst, the catalyst consists of an integral zeolite carrier and an active component loaded on the carrier, the active component consists of a copper oxide, a manganese oxide and an auxiliary agent cerium oxide, and the catalyst is replaced periodically; the hydrothermal oxidation system adds high-concentration strong oxidants such as: oxygen with the concentration of more than 95 percent, ozone or hydrogen peroxide and the like are used together.
The alkaline ionic liquid carbon absorption system adopts weak-alkaline ionic liquid, and the weak-alkaline ionic liquid is preferably alkylol amine concentrated solution, such as diethanol amine (DEA) and the like.
The aerobic reaction system is connected to the regulating tank through a backflow pipeline, generated sludge flows back to the regulating tank and enters the hydrothermal oxidation system again for thermal decomposition, and the sludge-water separation performance is improved.
The anaerobic reaction system is an up-flow anaerobic sludge blanket, the sedimentation zone in the up-flow anaerobic sludge blanket accounts for 20-30% of the total volume, a continuous stirrer is arranged in the anaerobic sludge blanket and is used for fully and uniformly mixing sludge which flows back to the regulating tank from the aerobic reaction system and untreated wastewater, then the sludge is guided into a heat exchange device, and finally the sludge enters a hydrothermal oxidation system for treatment.
The wetland system plants in the wetland treatment system mainly select herbaceous plants with strong carbon fixing capacity and fast production, such as bermuda grass, liangyuehong, radix ophiopogonis and the like, and the rest are doped with evergreen coniferous trees and evergreen broad-leaved trees (such as masson pine, grifola frondosa and the like).
The high-concentration organic wastewater low-carbon treatment system is adopted to treat high-concentration organic wastewater in a certain place:
the wastewater to be treated is: the pH value of the wastewater produced by a certain chemical plant is 7.3, and the COD is 19500 mg/L.
The processing steps are as follows: introducing wastewater to be treated into a regulating tank, adding 30% sodium hydroxide alkali liquor according to actual conditions, regulating the pH of the wastewater to 9, uniformly stirring, introducing into a three-stage energy exchange system, and then introducing into a reactorTreating by a hydrothermal oxidation system; the reaction temperature of the continuous hydrothermal oxidation system is controlled to be 300 ℃, oxygen is taken as an oxidant, the purity of the oxygen is 96 percent, the oxidation coefficient is 1.5, the reaction pressure is 7MPa, the reaction time is 2 hours, the COD conversion rate of the wastewater treated by the continuous hydrothermal oxidation system is 86.1 percent, the biodegradability of effluent is 0.51, and the pH value is 7.6; performing gas-liquid separation on the effluent, then performing heat exchange and cooling, separating sludge through a sludge filter pressing device, adjusting the pH of the filter pressing effluent and sludge drying effluent to be 7 through an acetic acid concentrated solution, discharging the water into an anaerobic reaction system, and standing for 3 days at the temperature of 32 ℃; the effluent of the anaerobic reaction system is conveyed to an aerobic reaction system through a pipeline, the aeration rate of the aerobic aeration system is gradually reduced along with the reduction of COD of the sewage, the effluent is directly guided into a wetland treatment system after the sewage stays in the aerobic reaction system for 1.5 days, the stay time of the wastewater in the wetland treatment system is 10 days, the effluent is discharged outside, and the removal rate of the COD of the wastewater after the treatment of the anaerobic and aerobic processes reaches 97.8 percent; and returning the sludge in the secondary sedimentation tank of the aerobic reaction system to the regulating tank. Introducing gas separated by the gas-liquid separation device, gas generated by the biogas purification device and incineration tail gas generated by the biogas incinerator into an alkaline ionic liquid carbon absorption system through a pipeline, wherein the ionic liquid is DEA concentrated solution, the absorption reaction time is 2h, the reaction pressure is 0.3MPa, the reaction temperature is 35 ℃, and CO is generated2The absorption rate exceeds 90 percent, and the residual gas after absorption is discharged outside.
Comparative example 1
The wastewater to be treated in the comparative example is the same as that in example 1, and the specific operation is different from that in example 1 in that: only hydrothermal oxidation treatment is carried out, and biological treatment is not carried out. The COD conversion rate of the wastewater is 82.1 percent, the residual COD exceeds 3500mg/L, the biodegradability of the effluent is 0.4, the pH value is 7.2, and the three-level standard of the Integrated wastewater discharge Standard GB8978-1996 cannot be met.
Comparative example 2
The wastewater to be treated in the comparative example is the same as that in example 1, and the specific operation is different from that in example 1 in that: the hydrothermal oxidation system is not suitable for high-concentration oxidants and does not contain catalysts. After continuous wet oxidation, the COD conversion rate of the wastewater is 57%, a subsequent anaerobic reaction system and an aerobic reaction system cannot normally operate, a large amount of precipitates are generated, the concentration of effluent is high, and the three-level standard of Integrated wastewater discharge Standard GB8978-1996 cannot be met.
Comparative example 3
The wastewater to be treated in the comparative example is the same as that in example 1, and the specific operation is different from that in example 1 in that: does not adopt alkaline ionic liquid for absorption, thereby causing CO in the experimental process2A large amount of carbon cannot reach the carbon emission reduction target because of direct discharge.
Comparative example 4
The wastewater to be treated in the comparative example is the same as that in example 1, and the specific operation is different from that in example 1 in that: the gas generated by the anaerobic reaction system is not collected and utilized, a heat exchange system is not adopted, the heat conducting oil is additionally heated, so that high-temperature effluent cannot enter the subsequent biological treatment, a cooling pool needs to be built, a large amount of electric power needs to be consumed, and a large amount of electric power containing CO is caused2Therefore, the energy-saving and carbon-reducing goals cannot be achieved.
Comparative example 5
The wastewater to be treated in the comparative example is the same as that in example 1, and the specific operation is different from that in example 1 in that: the sludge in the system is not subjected to backflow treatment, a large amount of anaerobic sludge and aerobic sludge are generated, the sludge contains a large amount of organic matters, and the water content of the sludge reaches more than 98%.
Example 2
A method for treating high concentration organic wastewater using the system described in example 1:
the wastewater to be treated is: the pH value of the wastewater produced by a certain chemical plant is 9, and the COD is 21100 mg/L.
The processing steps are as follows: introducing wastewater to be treated into a regulating tank, uniformly stirring, introducing into a three-level energy exchange system, and then introducing into a hydrothermal oxidation system for treatment; the reaction temperature of the continuous hydrothermal oxidation system is controlled to be 300 ℃, 30% hydrogen peroxide is used as an oxidant, 96% pure oxygen is used as an auxiliary material, the oxidation coefficient is 2, the reaction pressure is 7MPa, the reaction time is 2 hours, the COD conversion rate of the wastewater treated by the continuous hydrothermal oxidation system is 93.1%, the biodegradability of effluent is 0.51, and the pH is 7.2; the effluent is subjected to gas-liquid separation, then heat exchange and temperature reduction, sludge is separated by a sludge filter pressing device, and the content of the sludge at the momentThe water amount is lower than 50%, the pH value of the filter-pressing effluent and the sludge drying effluent is adjusted to 7 by acetic acid concentrated solution, the filtrate is discharged into an anaerobic reaction system, the temperature is 32 ℃, and the filtrate stays for 3 days; the effluent of the anaerobic reaction system is conveyed to an aerobic reaction system through a pipeline, the aeration rate of the aerobic aeration system is gradually reduced along with the reduction of COD of the sewage, the effluent is directly guided into a wetland treatment system after the sewage stays in the aerobic reaction system for 1.5 days, the stay time of the wastewater in the wetland treatment system is 10 days, the effluent is discharged outside, and the removal rate of the COD of the wastewater after the treatment of the anaerobic and aerobic processes reaches 99.2%; the sludge is circularly treated in the system. Introducing gas separated by the gas-liquid separation device, gas generated by the biogas purification device and incineration tail gas generated by the biogas incinerator into an alkaline ionic liquid carbon absorption system through a pipeline, wherein the ionic liquid is a mixed solution of Diethanolamine (DEA) and diisopropanolamine concentrated solution, the absorption reaction time is 2 hours, the reaction pressure is 0.3MPa, the reaction temperature is 35 ℃, and CO is generated2The absorption rate exceeds 92 percent, and the residual gas after absorption is discharged outside.
Example 3
A method for treating high concentration organic wastewater using the system described in example 1:
the wastewater to be treated is: the pH value of the wastewater produced by a certain chemical plant is 9, and the COD is 21100 mg/L.
The processing steps are as follows: introducing wastewater to be treated into a regulating tank, uniformly stirring, introducing into a three-level energy exchange system, and then introducing into a hydrothermal oxidation system for treatment; the reaction temperature of the continuous hydrothermal oxidation system is controlled to be 300 ℃, 30% hydrogen peroxide is used as an oxidant, 96% ozone and the oxidant are used for assisting in being excessive for many times, the reaction pressure is 7MPa, the reaction time is 2 hours, the COD conversion rate of the wastewater treated by the continuous hydrothermal oxidation system is 94.1%, the biodegradability of effluent is 0.53, and the pH is 7.2; performing gas-liquid separation on effluent, performing heat exchange and cooling, separating sludge through a sludge filter pressing device, adjusting the pH of the filter pressing effluent and sludge drying effluent liquid to be 7 through acetic acid concentrated solution, discharging the water and sludge drying effluent liquid into an anaerobic reaction system, and standing for 3 days at the temperature of 32 ℃; the effluent of the anaerobic reaction system is conveyed to an aerobic reaction system through a pipeline, the aeration rate of the aerobic aeration system is gradually reduced along with the reduction of COD (chemical oxygen demand) of the sewage, and the sewageAfter the water stays in the aerobic reaction system for 1.5 days, the effluent is directly led into the wetland treatment system, the residence time of the wastewater in the wetland treatment system is 10 days, the effluent is discharged, and the COD removal rate of the wastewater after the anaerobic and aerobic processes is more than 99.7 percent; the sludge is circularly treated in the system. Introducing gas separated by the gas-liquid separation device, gas generated by the biogas purification device and incineration tail gas generated by the biogas incinerator into an alkaline ionic liquid carbon absorption system through a pipeline, wherein the ionic liquid is DEA concentrated solution, the absorption reaction time is 2h, the reaction pressure is 0.3MPa, the reaction temperature is 35 ℃, and CO is generated2The absorption rate exceeds 90 percent, and the residual gas after absorption is discharged outside.
The invention provides a system and a method for low-carbon treatment of high-concentration organic wastewater, and a method for realizing the technical scheme, and the above description is only a preferred embodiment of the invention, and it should be noted that, for those skilled in the art, a plurality of improvements and modifications can be made without departing from the principle of the invention, and these improvements and modifications should also be regarded as the protection scope of the invention. All the components not specified in the present embodiment can be realized by the prior art.
Claims (10)
1. A low-carbon treatment system for high-concentration organic wastewater is characterized by comprising a regulating tank, an energy exchange system I, an energy exchange system II, an energy exchange system III, a hydrothermal oxidation system, a gas-liquid separation device, a sludge filter pressing device, an anaerobic reaction system, an aerobic reaction system, a wetland treatment system, a methane purification device, a methane incinerator and an alkaline ionic liquid carbon absorption system;
the regulating tank, the inner pipe of the energy exchange system I, the inner pipe of the energy exchange system II, the inner pipe of the energy exchange system III, the hydrothermal oxidation system and the gas-liquid separation device are sequentially connected through pipelines;
the gas generated by the gas-liquid separation device is sequentially connected with an outer pipe of the energy exchange system I and the alkaline ionic liquid carbon absorption system through pipelines and is finally discharged; liquid generated by the gas-liquid separation device is sequentially connected with an outer pipe of the energy exchange system II, the sludge filter pressing device, the anaerobic reaction system, the aerobic reaction system and the wetland treatment system through pipelines and is finally discharged;
the gas generated by the anaerobic reaction system is sequentially connected with a biogas purification device and a biogas incinerator through pipelines; gas generated by the anaerobic reaction system is purified by a biogas purification device and then is used as fuel of a biogas incinerator to heat conducting oil;
the gas generated by the methane incinerator is led into an alkaline ionic liquid carbon absorption system through a pipeline;
and the outer pipe of the energy exchange system III is filled with heat conduction oil and is connected with the methane incinerator through a pipeline, so that the heat conduction oil is circulated between the outer pipe of the energy exchange system III and the methane incinerator.
2. The high-concentration organic wastewater low-carbon treatment system according to claim 1, wherein an outlet of the regulating tank is communicated with an inlet of an inner tube of an energy exchange system I, an outlet of the inner tube of the energy exchange system I is communicated with an inlet of an inner tube of an energy exchange system II, an outlet of the inner tube of the energy exchange system II is communicated with an inlet of an inner tube of an energy exchange system III, an outlet of the inner tube of the energy exchange system III is connected with an inlet of a hydrothermal oxidation system, an outlet of the hydrothermal oxidation system is connected with an inlet of a gas-liquid separation device, a gas outlet of the gas-liquid separation device is connected with an inlet of an outer tube of the energy exchange system I, an outlet of the outer tube of the energy exchange system I is connected with an; the liquid outlet of the gas-liquid separation device is connected with the inlet of an outer pipe of an energy exchange system II, the outlet of the outer pipe of the energy exchange system II is connected with the inlet of a sludge press-filtering device, the water outlet of the sludge press-filtering device is connected with the inlet of an anaerobic reaction system, the liquid outlet of the anaerobic reaction system is connected with the inlet of an aerobic reaction system, the outlet of the aerobic reaction system is connected with the inlet of a wetland treatment system, the outlet of the wetland treatment system is recycled for the production process, the gas outlet of the anaerobic reaction system is connected with the inlet of a biogas purification device, the biogas outlet of the biogas purification device is connected with the inlet of a biogas incinerator, the residual gas outlet of the biogas purification device is connected with the inlet of an alkaline ionic liquid carbon absorption system, the outlet of the biogas incinerator is connected with the inlet of an alkaline ionic liquid carbon absorption; the hydrothermal oxidation system is provided with an oxidant inlet.
3. The high-concentration organic wastewater low-carbon treatment system according to claim 1, wherein a catalyst is arranged in the hydrothermal oxidation system, the catalyst consists of an integral zeolite carrier and active components loaded on the carrier, and the active components consist of copper oxide, manganese oxide and auxiliary cerium oxide;
the hydrothermal oxidation system is added with an oxidant through a pipeline, wherein the oxidant is more than 95% of oxygen, ozone or hydrogen peroxide.
4. The high-concentration organic wastewater low-carbon treatment system according to claim 1, wherein the alkaline ionic liquid carbon absorption system adopts weak alkaline ionic liquid.
5. The high-concentration organic wastewater low-carbon treatment system according to claim 1, wherein the aerobic reaction system is connected to the regulating tank through a return pipeline, and the generated sludge is returned to the regulating tank and enters the hydrothermal oxidation system again for treatment.
6. The high-concentration organic wastewater low-carbon treatment system according to claim 1, wherein the anaerobic reaction system is an upflow anaerobic sludge blanket, the sedimentation zone in the upflow anaerobic sludge blanket accounts for 20-30% of the total volume, and a continuous stirrer is arranged in the upflow anaerobic sludge blanket.
7. The high concentration organic wastewater low carbon treatment system according to claim 1, wherein the aerobic reaction system is of an aeration type.
8. The high-concentration organic wastewater low-carbon treatment system according to claim 1, wherein herbaceous plants are planted in the wetland treatment system.
9. The method for treating high-concentration organic wastewater by using the low-carbon treatment system as claimed in claim 1, which is characterized by comprising the following steps of:
(1) hydrothermal oxidation reaction: filtering and deslagging the wastewater to be treated, then guiding the wastewater into an adjusting tank, uniformly stirring, and adjusting the pH value to 7-9; then, the mixture enters a hydrothermal oxidation system after heat exchange of an energy exchange system, a high-concentration strong oxidant is used as an oxidant, the oxidation coefficient is greater than 1.5, the temperature is 280-320 ℃, the pressure is 7-9 Mpa, and the reaction time is 1.5-2.5 hours;
(2) anaerobic reaction treatment: exchanging heat and cooling the liquid product reacted in the step (1), then entering a sludge filter-pressing device for filter pressing and mud removal, and introducing the liquid product into an anaerobic reaction system, wherein a settling zone in an up-flow anaerobic sludge bed accounts for 20-30% of the total volume, a continuous stirrer is arranged in the anaerobic sludge bed, and the reaction time is 2-4 days;
(3) aerobic reaction treatment: directly introducing the effluent treated in the step (2) into an aerobic reaction system, directly introducing the effluent into a wetland treatment system after 1.5-3 days of aerobic reaction, wherein the retention time of wastewater in the wetland treatment system is 5-15 days, and reusing the effluent in a production process;
(4) a carbon absorption system: exchanging heat and cooling the gas product reacted in the step (1), and then introducing the gas product into an alkaline ionic liquid carbon absorption system; and (3) treating the gas generated in the step (2) by using a methane purification device, introducing methane into a methane incinerator for combustion, introducing the gas generated after combustion and the residual gas of the methane purification device into an alkaline ionic liquid carbon absorption system together, performing absorption reaction for 0.5-2 h, performing reaction pressure of 0.1-0.5 MPa, performing reaction temperature of 30-70 ℃, discharging the residual gas after absorption, and performing high-temperature desorption when the alkaline ionic liquid is nearly saturated.
10. The method for treating high concentration organic wastewater according to claim 9, wherein in the step (3), the aeration rate of the aeration device of the aerobic reaction system is changed along with the wastewaterThe COD is reduced gradually, and the aeration quantity of air for degrading each kilogram of BOD is kept to be 80-90 m3。
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