Organic waste liquid directional conversion recycling method and system

Abstract

The invention relates to an organic waste liquid directional conversion recycling method and system, and belongs to the technical field of organic waste liquid treatment. The method comprises the following steps: inputting toxic organic waste liquid into a catalytic oxidation reactor, continuously introducing air, and carrying out catalytic oxidation reaction to obtain pretreated waste liquid; the pretreatment waste liquid is sequentially input into a first anaerobic tower, an air stripping tower and a second anaerobic tower to be treated, and methane is introduced into the first anaerobic tower, the air stripping tower and the second anaerobic tower. Through relatively low-temperature and low-pressure catalytic oxidation pretreatment, the pretreatment time is shortened, detoxification of the high-concentration organic waste liquid is realized, and meanwhile, the energy consumption and the cost of catalytic oxidation pretreatment are reduced; by arranging the catalytic oxidation reactor, the first anaerobic tower, the air stripping tower and the second anaerobic tower, catalytic oxidation pretreatment and biochemical treatment are combined, and the device has the advantages of low investment and operation cost and is suitable for treating high-concentration organic waste liquid.

Description

Technical Field

[0001] The present invention relates to the technical field of organic waste liquid treatment, and in particular to a method and system for directional conversion and resource utilization of organic waste liquid. Background Art

[0002] In the chemical production process, due to the limitation of conversion rate, a large amount of high-concentration organic waste liquid composed of organic raw materials, by-products, products, inorganic salts, etc. is usually produced, and the chemical oxygen demand of the organic waste liquid is high.

[0003] At present, organic waste liquid is mainly treated by incineration, dilution, evaporation concentration and landfill, cement kiln co-treatment, wet oxidation (WAO) or catalytic wet oxidation (CWAO), anaerobic treatment and other methods. The incineration treatment method is relatively efficient and stable, but the cost of incineration treatment is more than 600 yuan / ton, the investment and operation costs are high, and a large amount of carbon dioxide will be emitted; in addition, the inorganic slag produced by incineration treatment is more corrosive and still needs to be treated as hazardous waste, because the tail gas produced may contain risky chlorinated organic matter (such as dioxins). The evaporation concentration and landfill method has problems such as difficulty in evaporating and concentrating organic waste liquid, land occupation by landfill, and high risk of leakage when treating organic waste liquid. The cement kiln co-treatment method requires that chloride ions, sulfate ions, fluoride ions, heavy metals, etc. need to be at a lower concentration, and is not suitable for waste liquid with a high salt content; in addition, if the water content in the organic waste liquid is high, it will affect the normal production of the cement kiln. Traditional wet oxidation (WAO) or catalytic wet oxidation (CWAO) methods require high temperatures (200-300°C) and high pressures (3-8Mpa), resulting in high investment and operating costs. At the same time, the design concept is based on the complete mineralization of organic matter as the main goal, and it is impossible to recycle resources and energy, which limits its large-scale application; in addition, this method has the risk of rapid temperature rise and coking problems when treating high-concentration organic waste liquid. Anaerobic treatment is a low-energy method that can be used to recycle organic matter, but it is limited by the degradation capacity of microorganisms and cannot be applied to high-concentration toxic or difficult-to-degrade organic waste liquids, and the investment and operating costs are high. When facing high-sulfate waste liquid, hydrogen sulfide is mainly produced, and the methane production capacity is greatly inhibited. Hydrogen sulfide accumulates in the system, which can easily lead to system collapse and inability to operate continuously to realize the resource utilization of waste liquid.

[0004] Therefore, how to realize resource processing of waste liquid without incineration and evaporation landfill is an important issue currently facing this field. Summary of the invention

[0005] The purpose of the present invention is to overcome the shortcomings of the prior art and provide a method and system for directional conversion and resource utilization of organic waste liquid.

[0006] To achieve the above object, the technical solution adopted by the present invention is:

[0007] In a first aspect, the present invention provides a method for directional conversion of organic waste liquid into resources, comprising the following steps:

[0008] S1, inputting toxic organic waste liquid into a catalytic oxidation reactor, and continuously introducing air into the catalytic oxidation reactor to perform a catalytic oxidation reaction to obtain a pretreated waste liquid;

[0009] S2, inputting the pretreated waste liquid into the first anaerobic tower, the air stripping tower and the second anaerobic tower in sequence for treatment, and introducing methane into the first anaerobic tower, the air stripping tower and the second anaerobic tower respectively.

[0010] Preferably, in step S1, the temperature of the catalytic oxidation reaction is 150-200°C, the pressure is 1-3 MPa, and the time is 30-120 min.

[0011] Preferably, in step S1, the ratio between the air intake flow rate and the toxic organic waste liquid input flow rate is (20-100):1.

[0012] Preferably, in step S1, a catalyst cartridge is provided in the catalytic oxidation reactor, wherein the catalyst cartridge comprises a cylindrical carrier and a catalyst attached to the surface of the cylindrical carrier, and the chemical formula of the catalyst is La 1～ x Ce x Fe y Ru 1～y O3, wherein x is 0.3-1, y is 0.2-0.6; the porosity of the catalyst is not less than 30%, and the volume space velocity is 0.5-2h ～1 .

[0013] Preferably, in step S1, the toxic organic waste liquid has at least one of the following (I) to (V):

[0014] (I) Chemical oxygen demand 20,000 to 700,000 mg / L;

[0015] (II) Biochemical inhibitory aldehyde organic matter is not less than 0.5 g / L;

[0016] (III) The adsorbable total organic halogen content is not less than 0.5 g / L;

[0017] (IV) a sodium salt content of not less than 10,000 mg / L;

[0018] (V) Potassium salt content is not less than 10,000 mg / L.

[0019] Preferably, when step S2 is performed, the pH value of the liquid in the first anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the first anaerobic tower is (3-9):1; the pH value of the liquid in the second anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the second anaerobic tower is (3-9):1; the pH value of the liquid in the stripping tower is adjusted to 5.0-6.0, and the gas-liquid ratio of the stripping tower is (3-9):1.

[0020] Preferably, the first anaerobic tower is inoculated with activated sludge and ferrous carbonate particles, and the concentration of the activated sludge in the first anaerobic tower is 100-200 g / L, and the concentration of ferrous sulfate is 2-10 g / L; the second anaerobic tower is inoculated with activated sludge and ferrous carbonate particles, and the concentration of the activated sludge in the second anaerobic tower is 100-200 g / L, and the concentration of ferrous sulfate is 2-10 g / L.

[0021] Preferably, step S2 further comprises: recirculating part of the effluent from the second anaerobic tower as reflux liquid into the first anaerobic tower for treatment, and recirculating part of the effluent from the second anaerobic tower as second reflux liquid into the second anaerobic tower for treatment, the reflux ratio within the tower is 1000-1500%, and the reflux ratio between towers is 100-800%.

[0022] In a second aspect, the present invention provides an organic waste liquid directional conversion resource utilization device, comprising a catalytic oxidation reactor, a first anaerobic tower, a stripping tower, and a second anaerobic tower, wherein the liquid outlet of the catalytic oxidation reactor is connected to the liquid inlet of the first anaerobic tower via a pipeline, the liquid outlet of the first anaerobic tower is connected to the liquid inlet of the stripping tower via a pipeline, the liquid outlet of the stripping tower is connected to the liquid inlet of the second anaerobic tower via a pipeline, and the liquid inlet of the second anaerobic tower is connected to the liquid outlet of the second anaerobic tower via a pipeline.

[0023] Compared with the prior art, the present invention has the following beneficial effects:

[0024] The present invention reduces the pretreatment time through relatively low-temperature and low-pressure catalytic oxidation pretreatment, thereby achieving detoxification of high-concentration organic waste liquid and reducing the energy consumption and cost of catalytic oxidation pretreatment; by regulating the process parameters of the biochemical treatment process, the anaerobic decomposition of organic matter is stably and efficiently achieved under high sulfate conditions.

[0025] The present invention provides a catalytic oxidation reactor, a first anaerobic tower, a stripping tower, and a second anaerobic tower, so as to combine catalytic oxidation pretreatment with biochemical treatment, which has the advantages of low investment and operation costs, is suitable for treating high-concentration organic waste liquid, can effectively reduce the emission of pollutants, and realize the source resource utilization of pollutants. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1This is a schematic diagram of the structure of the organic waste liquid directional conversion resource utilization system provided by the present invention. DETAILED DESCRIPTION

[0027] In order to better illustrate the purpose, technical solutions and advantages of the present invention, the present invention will be further described below in conjunction with specific embodiments.

[0028] In a first aspect, the present invention provides a method for directional conversion of organic waste liquid into resources, comprising the following steps:

[0029] S1, inputting toxic organic waste liquid into a catalytic oxidation reactor, and continuously introducing air into the catalytic oxidation reactor to perform a catalytic oxidation reaction to obtain a pretreated waste liquid;

[0030] S2, inputting the pretreated waste liquid into the first anaerobic tower, the air stripping tower and the second anaerobic tower in sequence for treatment, and introducing methane into the first anaerobic tower, the air stripping tower and the second anaerobic tower respectively.

[0031] In one embodiment, in step S1, the catalytic oxidation reaction is carried out at a temperature of 150 to 220°C, a pressure of 1 to 3 MPa, and a time of 30 to 150 min.

[0032] Furthermore, in step S1, the temperature of the catalytic oxidation reaction is 150-200°C, the pressure is 1-3 MPa, and the time is 30-120 min.

[0033] Furthermore, in step S1, the temperature of the catalytic oxidation reaction is 160-180°C, the pressure is 1.5-2.5 MPa, and the time is 60-100 min.

[0034] The present invention controls the temperature, pressure and time of the catalytic oxidation reaction within appropriate ranges, and can effectively reduce the adsorbed total organic halogen (AOX) content and chemical oxygen demand in the waste liquid.

[0035] In one embodiment, in step S1, the ratio between the air flow rate and the toxic organic waste liquid input flow rate is (20-100):1.

[0036] In one embodiment, in step S1, a catalyst cartridge is provided in the catalytic oxidation reactor, wherein the catalyst cartridge comprises a cylindrical carrier and a catalyst attached to the surface of the cylindrical carrier, wherein the general chemical formula of the catalyst is La 1～ x Ce x Fe y Ru 1～y O3, wherein x is 0.3-1, y is 0.2-0.6; the porosity of the catalyst is not less than 30%, and the volume space velocity is 0.5-2h ～1 .

[0037] Furthermore, x is 0.6-0.7, y is 0.3-0.5, the porosity of the catalyst is 50-60%, and the volume space velocity is 1-1.5h ～1 .

[0038] In the present invention, the material of the cylindrical carrier can be aluminum oxide or titanium oxide.

[0039] In one embodiment, in step S1, the toxic organic waste liquid has at least one of the following (I) to (V):

[0040] (I) Chemical oxygen demand not less than 20,000 to 700,000 mg / L;

[0041] (II) Biochemical inhibitory aldehyde organic matter is not less than 0.5 g / L;

[0042] (III) The adsorbable total organic halogen content is not less than 0.5 g / L;

[0043] (IV) a sodium salt content of not less than 10,000 mg / L;

[0044] (V) Potassium salt content is not less than 10,000 mg / L.

[0045] The present invention optimizes the process parameters and catalytic materials in step S1, changes the effluent index of catalytic pretreatment, does not use COD removal rate as the effluent index, but uses the adsorbable total organic halogen (AOX) content, methane production potential or organic acid ratio as the effluent index, performs catalytic oxidation reaction on the organic waste liquid at relatively low temperature and low pressure, realizes the detoxification pretreatment of high-concentration organic waste liquid, and has high safety in the treatment process, solves the problems of high investment, high energy consumption and high cost in the existing catalytic pretreatment process, and also makes the AOX content in the obtained pretreated waste liquid less than 20 mg / L, and the methane production potential greater than 0.2-0.3 Nm 3 / kg COD, the ratio of organic carbon in organic acids to total organic carbon (TOC) is reduced to 0.3-0.9.

[0046] In one embodiment, when step S2 is performed, the pH value of the liquid in the first anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the first anaerobic tower is (3-9):1; the pH value of the liquid in the second anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the second anaerobic tower is (3-9):1; the pH value of the liquid in the stripping tower is adjusted to 5.0-6.0, and the gas-liquid ratio of the stripping tower is (3-9):1.

[0047] In one embodiment, in step S2, the first anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 100-200 g / L, the concentration of the ferrous sulfate particles is 2-10 g / L, and the particle size of the ferrous sulfate particles is 200-400 mesh.

[0048] In one embodiment, in step S2, the second anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 100-200 g / L, the concentration of the ferrous sulfate particles is 2-10 g / L, and the particle size of the ferrous sulfate particles is 200-400 mesh.

[0049] The present invention arranges ferrous carbonate particles and activated sludge in a first anaerobic tower and a second anaerobic tower respectively. During the treatment process, the activated sludge can wrap the ferrous carbonate particles to form granular sludge. The ferrous carbonate particles, as the inner core of the granular sludge, can effectively improve the sedimentability of the sludge, and provide an iron source and carbonate ions to react with sulfides (such as hydrogen sulfide, etc.) in the waste liquid to generate ferrous sulfide precipitation, thereby reducing the concentration of sulfides in the waste liquid. The ferrous carbonate particles can also promote electron transfer, thereby promoting the anaerobic microorganisms in each anaerobic tower to decompose organic matter in the waste liquid.

[0050] In one embodiment, step S2 also includes: recirculating part of the effluent from the second anaerobic tower as the first reflux liquid into the first anaerobic tower for treatment, and recirculating part of the effluent from the second anaerobic tower as the second reflux liquid into the second anaerobic tower for treatment, the reflux ratio within the tower is 1000-1500%, and the reflux ratio between towers is 100-800%.

[0051] In the present invention, the intra-tower reflux refers to the reflux inside the tower, and the inter-tower reflux refers to the reflux of the outlet water of the subsequent tower to the water inlet of the preceding tower.

[0052] In one embodiment, the method of introducing methane in step S2 includes: collecting the gas discharged from the first anaerobic tower 2, the gas discharged from the stripping tower 3 and the gas discharged from the second anaerobic tower 4, and then inputting them into the methane purification system for purification, and then pressurizing them with a fan 9 and respectively inputting them into the first anaerobic tower 2, the stripping tower 3 and the second anaerobic tower 4 for aeration.

[0053] The present invention provides an anaerobic environment for microorganisms by introducing methane for continuous aeration during the biochemical treatment process, thereby promoting the contact between organic matter in the waste liquid and microorganisms (such as methanogens) in the activated sludge, and effectively blowing out hydrogen sulfide gas in the waste liquid, reducing the toxic effect of the waste liquid on the methanogens, promoting the growth and reproduction of the methanogens, and increasing the degradation rate of organic matter.

[0054] The inventors have found through research that controlling the reflux ratio within the tower at 1000-1500% and the reflux ratio between towers at 100-400% can effectively dilute the influent of the first anaerobic tower 2, reduce the concentration of hydrogen sulfide and the like in the influent of the first anaerobic tower 2, avoid excessively high content of hydrogen sulfide and the like in the liquid entering the first anaerobic tower 2, and thereby avoid the system from easily collapsing due to excessively high toxicity of the influent during long-term operation.

[0055] In a second aspect, the present invention provides an organic waste liquid directional conversion resource utilization device, comprising a catalytic oxidation reactor 1, a first anaerobic tower 2, a stripping tower 3, and a second anaerobic tower 4, wherein the liquid outlet of the catalytic oxidation reactor 1 is connected to the liquid inlet of the first anaerobic tower 2 through a pipeline, the liquid outlet of the first anaerobic tower 2 is connected to the liquid inlet of the stripping tower 3 through a pipeline, the liquid outlet of the stripping tower 3 is connected to the liquid inlet of the second anaerobic tower 4 through a pipeline, the liquid inlet of the second anaerobic tower 4 is connected to the liquid outlet of the second anaerobic tower 4 through a reflux pump (not shown in the figure) and a pipeline, and the liquid outlet of the second anaerobic tower 4 is connected to the liquid inlet of the second anaerobic tower 4 through a reflux pump (not shown in the figure) and a pipeline.

[0056] The present invention provides a catalytic oxidation reactor 1, a first anaerobic tower 2, a stripping tower 3, and a second anaerobic tower 4, so as to combine catalytic oxidation pretreatment with biochemical treatment, and has the advantages of low investment and operation costs, and is suitable for treating high-concentration organic waste liquid, reducing the emission of pollutants, and realizing the source resource utilization of pollutants.

[0057] In one embodiment, a gas outlet is disposed at the top of the catalytic oxidation reactor 1 , a gas inlet is disposed at the bottom of the catalytic oxidation reactor 1 , and a liquid inlet of the catalytic oxidation reactor 1 is located below a liquid outlet of the catalytic oxidation reactor 1 .

[0058] Specifically, the catalytic oxidation reactor 1 is equipped with a heating device. For example, the heating device may be a heating resistance wire or a heating resistance rod arranged in the side wall of the reactor 1 .

[0059] In one embodiment, a gas outlet is provided at the top of the first anaerobic tower 2, a plurality of first aeration heads 6 are provided at the bottom of the first anaerobic tower 2, a gas outlet is provided at the top of the second anaerobic tower 4, a plurality of second aeration heads 7 are provided at the bottom of the second anaerobic tower 4, a gas outlet is provided at the top of the stripping tower 3, a plurality of third aeration heads 8 are provided at the bottom of the stripping tower 3, and the first aeration head 6, the second aeration head 7 and the third aeration head 8 are respectively connected to the fan 9 through pipes.

[0060] Specifically, the fan 9 is connected to an external methane purification system or a gas storage tank storing methane through a pipeline.

[0061] Specifically, the gas outlet of the first anaerobic tower 2, the gas outlet of the air stripping tower 3 and the gas outlet of the second anaerobic tower 4 are respectively connected to the external methane purification system through pipelines.

[0062] In one embodiment, a demister 5 is provided on the upper portion of the stripping tower 3 , and the demister 5 is a titanium mesh. The liquid inlet of the stripping tower 3 is located below the liquid outlet of the stripping tower 3 .

[0063] In the present invention, each pipeline is provided with a flow control valve.

[0064] In the present invention, the method for directional conversion and resource utilization of organic waste liquid described in the first aspect is implemented by the system for directional conversion and resource utilization of organic waste liquid described in the second aspect.

[0065] The present invention provides the following examples to facilitate understanding of the present invention. The present invention provides these examples but is not intended to limit the scope of the claims.

[0066] The method for directional conversion and resource utilization of organic waste liquid in the following embodiment is implemented by a directional conversion and resource utilization system for organic waste liquid, which comprises a catalytic oxidation reactor 1, a first anaerobic tower 2, a stripping tower 3, and a second anaerobic tower 4, wherein the liquid outlet of the catalytic oxidation reactor 1 is connected to the liquid inlet of the first anaerobic tower 2 through a pipeline, the liquid outlet of the first anaerobic tower 2 is connected to the liquid inlet of the stripping tower 3 through a pipeline, the liquid outlet of the stripping tower 3 is connected to the liquid inlet of the second anaerobic tower 4 through a pipeline, the liquid inlet of the second anaerobic tower 4 is connected to the liquid outlet of the second anaerobic tower 4 through a reflux pump (not shown in the figure) and a pipeline, and the liquid outlet of the second anaerobic tower 4 is connected to the liquid inlet of the second anaerobic tower 4 through a reflux pump (not shown in the figure) and a pipeline.

[0067] An air outlet is arranged at the top of the catalytic oxidation reactor 1, an air inlet is arranged at the bottom of the catalytic oxidation reactor 1, and a liquid inlet of the catalytic oxidation reactor 1 is located below the liquid outlet of the catalytic oxidation reactor 1; the catalytic oxidation reactor 1 is equipped with a heating device, which is a heating resistance wire arranged in the side wall of the reactor 1.

[0068] A gas outlet is arranged at the top of the first anaerobic tower 2, a plurality of first aeration heads 6 are arranged at the bottom of the first anaerobic tower 2, a gas outlet is arranged at the top of the second anaerobic tower 4, a plurality of second aeration heads 7 are arranged at the bottom of the second anaerobic tower 4, a gas outlet is arranged at the top of the stripping tower 3, a plurality of third aeration heads 8 are arranged at the bottom of the stripping tower 3, the first aeration head 6, the second aeration head 7 and the third aeration head 8 are respectively connected to the fan 9 through pipelines; the fan 9 is connected to an external methane purification system or a gas storage tank storing methane through a pipeline; the gas outlet of the first anaerobic tower 2, the gas outlet of the stripping tower 3 and the gas outlet of the second anaerobic tower 4 are respectively connected to the external methane purification system through pipelines.

[0069] A first three-phase separation device 10 is disposed in the first anaerobic tower 2, and a second three-phase separation device 11 is disposed in the second anaerobic tower.

[0070] A demister 5 is provided on the upper part of the stripping tower 3 , and the demister 5 is a titanium mesh. The liquid inlet of the stripping tower 3 is located below the liquid outlet of the stripping tower 3 .

[0071] Each pipeline is provided with a flow control valve.

[0072] Examples 1 to 8

[0073] The embodiment of the method for directional conversion and resource utilization of organic waste liquid of the present invention comprises the following steps:

[0074] S1, inputting toxic organic waste liquid into the catalytic oxidation reactor 1, continuously introducing air into the catalytic oxidation reactor 1, performing catalytic oxidation reaction, and obtaining pretreated waste liquid;

[0075] In step S1, the toxic organic waste liquid is organic waste liquid generated by a pharmaceutical factory in Tianjin, wherein the content of sodium chloride is 30,000 mg / L, the chemical oxygen demand is 320,000 mg / L, the main components of AOX are dichloromethane, chloroform, etc., and the content of AOX is 1 g / L;

[0076] The catalytic oxidation reactor is provided with a catalyst cartridge, and the chemical formula of the catalyst in the catalyst cartridge is La 1～x Ce x Fe y Ru 1～y O3, the preparation method of the catalyst cartridge is: according to La 1～x Ce x Fe y Ru 1～y O3, weigh the following inorganic salts: LaCl3, CeCl3, FeCl3, RuCl3, dissolve the inorganic salts in water to prepare an impregnation solution, the mass ratio of the inorganic salt to water is 3:100, soak the cylindrical carrier in the impregnation solution and then dry it, and sinter it at high temperature to obtain a catalyst cylinder, the material of the cylindrical carrier is alumina;

[0077] x, y, the porosity of the catalyst, the volume space velocity, the ratio between the air flow rate and the input flow rate of the organic waste liquid, the input flow rate of the organic waste liquid, the temperature, pressure and time of the catalytic oxidation reaction are shown in Table 1;

[0078] S2, the pre-treated waste liquid is sequentially input into the first anaerobic tower 2, the air stripping tower 3 and the second anaerobic tower 4 for treatment, and methane is introduced into the first anaerobic tower 2, the air stripping tower 3 and the second anaerobic tower 4 for aeration.

[0079] In step S2, the liquid inlet flow rate of the first anaerobic tower, the second anaerobic tower and the stripping tower is 5m 3 / h, adjust the pH value of the liquid in the first anaerobic tower to 8.2-8.8, and the gas-liquid ratio of the first anaerobic tower is 5:1; adjust the pH value of the liquid in the second anaerobic tower to 8.2-8.8, and the gas-liquid ratio of the second anaerobic tower is 5:1; adjust the pH value of the liquid in the stripping tower to 5.0-6.0, and the gas-liquid ratio of the stripping tower is 5:1.

[0080] The first anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 150g / L, the concentration of the ferrous sulfate particles is 5g / L, and the particle size of the ferrous sulfate particles is 300 meshes.

[0081] The second anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 150 g / L, the concentration of the ferrous sulfate particles is 5 g / L, and the particle size of the ferrous sulfate particles is 300 meshes.

[0082] The hydraulic retention time of the first anaerobic tower is 3 days; the hydraulic retention time of the second anaerobic tower is 3 days, and the hydraulic retention time of the stripping tower is 2 days.

[0083] The aeration step includes: collecting the gas discharged from the first anaerobic tower 2, the gas discharged from the stripping tower 3 and the gas discharged from the second anaerobic tower 4, and inputting them into the methane purification system for purification, and then pressurizing them through the fan 9 and inputting them into the first anaerobic tower 2, the stripping tower 3 and the second anaerobic tower 4 for aeration.

[0084] Step S2 also includes: returning part of the effluent from the second anaerobic tower 4 as reflux liquid to the first anaerobic tower 2 for treatment, and returning part of the effluent from the second anaerobic tower as second reflux liquid to the second anaerobic tower for treatment, with the reflux ratio within the tower being 1200% and the reflux ratio between towers being 300%.

[0085] During the implementation process, the chemical oxygen demand of the pretreated wastewater obtained in step S1 and the chemical oxygen demand of the effluent of the second anaerobic tower 4 in step S2 are detected by the method of "Determination of Chemical Oxygen Demand (GB11914-89)".

[0086] The AOX content in the pretreated waste liquid obtained in step S1 is detected by the method of "Determination of Adsorbable Organic Halogen (AOX) in Water - Ion Chromatography (HJ / T 83-2001)".

[0087] Table 1

[0088]

[0089]

[0090] Example 9

[0091] The difference between this embodiment and embodiment 1 is that the organic waste liquid in step S1 of this embodiment is a high-concentration organic waste liquid produced by a pharmaceutical factory in Sichuan, with a sodium chloride content of 40,000 mg / L, a sodium sulfate concentration of 20,000 mg / L, and a COD of 700,000 mg / L. AOX is mainly chlorinated pharmaceutical intermediates and dichloromethane, etc., with a content of 0.8 g / L.

[0092] In step S1 of this embodiment, the reaction temperature is 150-160° C., the reaction pressure is 1.5 MPa, the reaction time is 60 min, the COD removal amount is 100,000 mg / L, and the AOX content in the pretreated waste liquid is 8 mg / L.

[0093] In step S2 of this embodiment, the pH value of the liquid in the first anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the first anaerobic tower is 9:1; the pH value of the liquid in the second anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the second anaerobic tower is 9:1; the pH value of the liquid in the stripping tower is adjusted to 5.0-6.0, and the gas-liquid ratio of the stripping tower is 9:1;

[0094] The first anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 100 g / L, the concentration of the ferrous sulfate particles is 2 g / L, and the particle size of the ferrous sulfate particles is 200 meshes;

[0095] The second anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 100g / L, the concentration of the ferrous sulfate particles is 2g / L, and the particle size of the ferrous sulfate particles is 200 meshes;

[0096] The liquid inlet flow rate of the first anaerobic tower, the second anaerobic tower and the stripping tower is 2m 3 / h, hydraulic retention time is 4d; hydraulic retention time of the stripping tower is 2h; hydraulic retention time of the second anaerobic tower is 2d;

[0097] The reflux ratio within the tower is 1000%, and the reflux ratio between towers is 100%.

[0098] The COD content in the effluent of the second anaerobic tower 4 of this embodiment is 3000 mg / L, and the operating cost is 40 yuan / ton of waste liquid.

[0099] Example 10

[0100] The difference between this embodiment and embodiment 1 is that:

[0101] The organic waste liquid in step S1 of this embodiment is a high-concentration organic waste liquid produced by a pharmaceutical factory in Sichuan, with a sodium chloride content of 30,000 mg / L, a sodium sulfate concentration of 40,000 mg / L, and a COD of 600,000 mg / L.

[0102] In step S1 of this embodiment, the reaction temperature is 140° C., the reaction pressure is 1.1 MPa, the reaction time is 30 min, and the COD removal amount is 20,000 mg / L.

[0103] In step S2 of this embodiment, the pH value of the liquid in the first anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the first anaerobic tower is 6:1; the pH value of the liquid in the second anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the second anaerobic tower is 6:1; the pH value of the liquid in the stripping tower is adjusted to 5.0-6.0, and the gas-liquid ratio of the stripping tower is 6:1;

[0104] The first anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 200g / L, the concentration of the ferrous sulfate particles is 10g / L, and the particle size of the ferrous sulfate particles is 400 meshes;

[0105] The second anaerobic tower is pre-inoculated with activated sludge, the activated sludge is mixed with ferrous carbonate particles, the concentration of the activated sludge is 200g / L, the concentration of the ferrous sulfate particles is 10g / L, and the particle size of the ferrous sulfate particles is 400 meshes;

[0106] The liquid inlet flow rate of the first anaerobic tower, the second anaerobic tower and the stripping tower is 3m 3 / h, hydraulic retention time is 3d; hydraulic retention time of the stripping tower is 3h; hydraulic retention time of the second anaerobic tower is 3d;

[0107] The reflux ratio within the tower is 1500%, and the reflux ratio between towers is 800%.

[0108] In this embodiment, the COD content in the effluent of the second anaerobic tower 4 is 3000 mg / L, and the operating cost is 40 yuan / ton of waste liquid.

[0109] In the description of the present invention, it should be noted that the terms "first" and "second" are only used for descriptive purposes and cannot be understood as indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. All directional indicators (such as up and down) in the present invention are only used to explain the relative position relationship, movement, etc. between the various parts under a certain specific posture (as shown in the accompanying drawings). If the specific posture changes, the directional indication will also change accordingly.

[0110] In the description of the present invention, it should also be noted that the terms "include", "have" and any variations thereof are intended to cover non-exclusive inclusions.

[0111] For those skilled in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0112] Finally, it should be noted that the above embodiments are only used to illustrate the technical solution of the present invention rather than to limit the scope of protection of the present invention. Although the present invention has been described in detail with reference to the preferred embodiments, those skilled in the art should understand that the technical solution of the present invention can be modified or replaced by equivalents without departing from the essence and scope of the technical solution of the present invention.

Claims

1. A method for directional conversion and resource utilization of organic waste liquid, characterized in that: The steps include: S1, inputting toxic organic waste liquid into a catalytic oxidation reactor, and continuously introducing air into the catalytic oxidation reactor to perform a catalytic oxidation reaction to obtain a pretreated waste liquid; S2, inputting the pretreated waste liquid into the first anaerobic tower, the air stripping tower and the second anaerobic tower in sequence for treatment, and introducing methane into the first anaerobic tower, the air stripping tower and the second anaerobic tower respectively.

2. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: In step S1, the catalytic oxidation reaction is carried out at a temperature of 150 to 220°C, a pressure of 1 to 3 MPa, and a time of 30 to 150 min.

3. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: In step S1, the ratio between the air flow rate and the toxic organic waste liquid input flow rate is (20-100):

1.

4. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: In step S1, a catalyst cartridge is provided in the catalytic oxidation reactor, wherein the catalyst cartridge comprises a cylindrical carrier and a catalyst attached to the surface of the cylindrical carrier, and the chemical formula of the catalyst is La 1～x Ce x Fe y Ru 1～y O3, wherein x is 0.3-1, y is 0.2-0.6; the porosity of the catalyst is not less than 30%, and the volume space velocity is 0.5-2h ～1 .

5. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: In step S1, in step S1, the toxic organic waste liquid has at least one of the following (I) to (V): (I) Chemical oxygen demand 20,000 to 700,000 mg / L; (II) Biochemical inhibitory aldehyde organic matter is not less than 0.5 g / L; (III) The adsorbable total organic halogen content is not less than 0.5 g / L; (IV) a sodium salt content of not less than 10,000 mg / L; (V) Potassium salt content is not less than 10,000 mg / L.

6. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: When step S2 is performed, the pH value of the liquid in the first anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the first anaerobic tower is (3-9):1; the pH value of the liquid in the second anaerobic tower is adjusted to 8.2-8.8, and the gas-liquid ratio of the second anaerobic tower is (3-9):1; the pH value of the liquid in the stripping tower is adjusted to 5.0-6.0, and the gas-liquid ratio of the stripping tower is (3-9):

1.

7. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: The first anaerobic tower is inoculated with activated sludge and ferrous carbonate particles. In the first anaerobic tower, the concentration of the activated sludge is 100-200 g / L, and the concentration of the ferrous sulfate particles is 2-10 g / L. The second anaerobic tower is inoculated with activated sludge and ferrous carbonate particles. In the second anaerobic tower, the concentration of the activated sludge is 100-200 g / L, and the concentration of the ferrous sulfate particles is 2-10 g / L.

8. The method for directional conversion and resource utilization of organic waste liquid according to claim 1, characterized in that: Step S2 also includes: returning part of the effluent from the second anaerobic tower as reflux liquid to the first anaerobic tower for treatment, returning part of the effluent from the second anaerobic tower as second reflux liquid to the second anaerobic tower for treatment, the reflux ratio within the tower is 1000-1500%, and the reflux ratio between towers is 100-800%.

9. An organic waste liquid directional conversion resource device, characterized in that: It includes a catalytic oxidation reactor, a first anaerobic tower, a stripping tower, and a second anaerobic tower, wherein the liquid outlet of the catalytic oxidation reactor is connected to the liquid inlet of the first anaerobic tower through a pipeline, the liquid outlet of the first anaerobic tower is connected to the liquid inlet of the stripping tower through a pipeline, the liquid outlet of the stripping tower is connected to the liquid inlet of the second anaerobic tower through a pipeline, and the liquid inlet of the second anaerobic tower is connected to the liquid outlet of the second anaerobic tower through a pipeline.

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