Short-path total physical and chemical treatment method for organic wastewater

Abstract

The application discloses a short-range full physical and chemical treatment method for organic wastewater, which comprises the following steps: S1, fine air bubbles are introduced into the organic wastewater to adsorb suspended oil beads and solid particles in the wastewater, and the bubbles float to the water surface to form dregs and remove waste oil; S2, a coagulant is added to gather colloidal particles and small suspended matters in the water to form large particles, and the particles are separated by sedimentation; S3, a particulate catalyst is arranged in a filler tower, and the effluent of S2 is introduced into the filler tower to remove most of COD; S4, a composite catalytic ceramic membrane is fixed in a reflux reactor, and the effluent of S3 is introduced into the reflux reactor to remove residual COD in the effluent of S3; S5, most of ammonia nitrogen in the effluent of S4 is recovered by using a membrane distillation mode, and the residual ammonia nitrogen content in the effluent is controlled to be lower than 100 mg / L; S6, a powder catalyst is fixed in a trickle bed, and the effluent of S5 is introduced into the trickle bed to remove residual ammonia nitrogen in the effluent of S5; S7, a chemical agent is added to generate insoluble phosphate to remove phosphorus in the water; and S8, after the reaction is completed, waste liquid is discharged.

Description

A Short-Cut, Fully Physicochemical Treatment Method for Organic Wastewater Technical Field

[0001] This invention relates to the field of wastewater treatment, specifically to a short-range, fully physicochemical treatment method for organic wastewater. Background Technology

[0002] Organic wastewater is generated in large quantities, has complex composition, and comes from a wide range of sources. Industries such as coking, pharmaceuticals, petrochemicals, anaerobic digestion, and waste treatment all produce large amounts of organic wastewater during production processes. This type of industrial wastewater poses a significant and long-lasting environmental pollution hazard. Improper treatment can not only impact the ecological environment but also harm human health. Currently, organic wastewater is mainly treated using a combination of "pretreatment + biological methods + membrane filtration": first, coagulation and sedimentation or flotation separation is performed to remove particulate matter and some COD, then it enters a traditional anaerobic-anoxic-aerobic (AAO) or membrane bioreactor (MBR) treatment process. The biochemical effluent undergoes final purification through various membrane separation, activated carbon, and advanced oxidation technologies to meet effluent quality standards. These processes are relatively complex, require large land areas, are easily affected by fluctuations in the properties of organic wastewater, and have high investment and operating costs.

[0003] Advanced oxidation processes can degrade various organic pollutants, such as Fenton oxidation, ozone oxidation, photocatalysis, and wet oxidation. These processes generate free radicals that react with the target pollutants to directly decompose organic pollutants into smaller molecules, ultimately achieving mineralization. However, these technologies generally suffer from problems such as high reagent consumption, demanding reaction conditions (high temperature and high pressure), and the potential to generate corrosive environments, resulting in high facility investment and operating costs. Summary of the Invention

[0004] To overcome the shortcomings of existing technologies, this invention proposes a short-range, fully physicochemical treatment method for organic wastewater.

[0005] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0006] A short-cut, fully physicochemical treatment method for organic wastewater includes the following steps:

[0007] S1. Air is introduced into the organic wastewater to generate fine bubbles, which adsorb suspended oil droplets and solid particles in the organic wastewater. The particles float to the surface with the bubbles to form scum, thus removing the waste oil.

[0008] S2. Add coagulant to the organic wastewater after treatment in step S1 to aggregate colloidal particles and tiny suspended solids in the water into larger particles, which are then separated by gravity sedimentation.

[0009] S3. Place the granular catalyst in a packed tower, introduce the effluent from step S2, and control the predetermined heating temperature and aeration rate of air and / or oxygen to carry out a catalytic oxidation reaction to remove most of the COD.

[0010] S4. Fix the composite catalytic ceramic membrane in the reflux reactor, introduce the effluent from step S3, control the predetermined heating temperature and the aeration rate of air and / or oxygen to carry out the catalytic oxidation reaction, and treat the residual COD in the effluent from step S3.

[0011] S5. Recover most of the ammonia nitrogen in the effluent from step S4 using membrane distillation, and control the residual ammonia nitrogen content in the effluent to be below 100 mg / L;

[0012] S6. Fix the powdered catalyst in the trickling bed, and pass the effluent from step S5 through it. Use air and / or oxygen as oxidant to carry out a catalytic oxidation reaction to remove the remaining ammonia nitrogen in the effluent from step S5.

[0013] S7. Add chemical reagents to the effluent from step S6 to generate insoluble phosphates, and then precipitate to remove phosphorus from the water.

[0014] S8. After the reaction is complete, the waste liquid treated in step S7 is discharged.

[0015] Preferably, in step S1, a blower is used to blow air into the organic wastewater, thereby generating a large number of highly dispersed fine bubbles. The buoyancy generated by the bubbles directly carries the adsorbed oil to the surface of the water, achieving separation from the water.

[0016] Preferably, in step S2, the coagulant is an aluminum salt or an iron salt.

[0017] Preferably, the particulate catalyst in step S3 is formed by loading an oxide of a first metal onto a first powder; the composite catalytic ceramic film in step S4 is formed by loading an oxide of a second metal onto a ceramic film.

[0018] Preferably, the first metal in the oxide of the first metal in step S3 is iron or copper; and the second metal in the oxide of the second metal in step S4 is iron or copper.

[0019] Preferably, the particulate catalyst in step S3 is prepared by an impregnation method: an impregnation solution is prepared using a nitrate of a first metal, the first powder is immersed in the impregnation solution for a predetermined time, and then calcined in air at 600-700°C for 3-4 hours; the concentration of the impregnation solution is 0.5 mol / L to 2 mol / L; preferably, the first powder is γ-Al2O3; preferably, the average particle size of the particulate catalyst is 5 mm. The composite catalytic ceramic membrane in step S4 is prepared by an impregnation method: an impregnation solution is prepared using a nitrate of a second metal, the ceramic membrane is immersed in the impregnation solution for a predetermined time, and then calcined in air at 600-700°C for 3-4 hours; the concentration of the impregnation solution is 0.5 mol / L to 2 mol / L.

[0020] Preferably, in steps S3 and S4, the reaction conditions are atmospheric pressure aeration, heating temperature of 60-90℃, air-to-water ratio of 3.5-7.0 L / g COD, and hydraulic retention time of 1-5 h.

[0021] Preferably, in step S5, most of the ammonia nitrogen in the effluent from step S4 is recovered by membrane distillation driven by a low-grade heat source.

[0022] Preferably, in step S6, the powdered catalyst is a ruthenium-based catalyst. Preferably, the ruthenium-based catalyst is prepared by impregnation: the second powder is placed in a ruthenium chloride solution and fully impregnated by vacuum rotary evaporation to control the metal loading to be 1wt% to 2wt%, and then calcined in a nitrogen atmosphere at 350 to 550°C for 3.5 to 5.5 hours. Preferably, the second powder is γ-Al2O3.

[0023] Preferably, the reaction conditions in step S6 are 0.5 MPa oxygen pressure and heating at 60–90°C; in step S7, the chemical agent is Fe. 3+ Salt, Fe 2+ Salt and Al 3+ At least one of the salts.

[0024] Compared with existing organic wastewater treatment processes, the beneficial effects of this invention include: This invention eliminates the biochemical treatment step, instead employing a full-process physicochemical method to purify the water. Specifically, after air flotation for oil removal and coagulation sedimentation, the wastewater undergoes a two-step reaction—using a packed tower equipped with an iron-based catalyst and a reflux reactor—to synergistically mineralize COD. The effluent then undergoes membrane distillation to recover most of the ammonia nitrogen, and finally, a trickle bed loaded with a powdered catalyst is used as the primary catalytic oxidation reaction site to remove residual ammonia nitrogen, which is ultimately released as N2. This invention's short-cut, full-physicochemical treatment method for organic wastewater uses only air and / or oxygen as oxidants, conducting catalytic oxidation reactions at low temperatures. It eliminates the need for additional strong oxidants such as ozone or persulfate, efficiently and thoroughly removing COD, ammonia nitrogen, and phosphorus from organic wastewater, achieving a highly efficient, green, and economical treatment method for organic wastewater. This invention can overcome the limitations of traditional processes, such as large land area, high treatment costs, long operating time, and susceptibility to external influences in the biochemical section. It improves the treatment efficiency and stability of organic wastewater and has many advantages, such as fast reaction speed, wide applicability, and clean and safe process. Attached Figure Description

[0025] Figure 1 is a process flow diagram of the short-range full physicochemical treatment method for organic wastewater according to a specific embodiment of the present invention. Detailed Implementation

[0026] The present invention will be further described below with reference to specific embodiments.

[0027] The short-range, fully physicochemical treatment method for organic wastewater according to a specific embodiment of the present invention includes the following steps:

[0028] S1. Air is introduced into the organic wastewater to generate fine bubbles, which adsorb suspended oil droplets and solid particles in the organic wastewater. The particles float to the surface with the bubbles to form scum, thus removing the waste oil.

[0029] S2. Add coagulant to the organic wastewater after treatment in step S1 to aggregate colloidal particles and tiny suspended solids in the water into larger particles, which are then separated by gravity sedimentation.

[0030] S3. Place the granular catalyst in a packed tower, introduce the effluent from step S2, and control the predetermined heating temperature and aeration rate of air and / or oxygen to carry out a catalytic oxidation reaction to remove most of the COD.

[0031] S4. Fix the composite catalytic ceramic membrane in the reflux reactor, introduce the effluent from step S3, control the predetermined heating temperature and the aeration rate of air and / or oxygen to carry out the catalytic oxidation reaction, and treat the residual COD in the effluent from step S3.

[0032] S5. Recover most of the ammonia nitrogen in the effluent from step S4 using membrane distillation, and control the residual ammonia nitrogen content in the effluent to be below 100 mg / L;

[0033] S6. Fix the powdered catalyst in the trickling bed, and pass the effluent from step S5 through it. Use air and / or oxygen as oxidant to carry out a catalytic oxidation reaction to remove the remaining ammonia nitrogen in the effluent from step S5.

[0034] S7. Add chemical reagents to the effluent from step S6 to generate insoluble phosphates, and then precipitate to remove phosphorus from the water.

[0035] S8. After the reaction is completed, the waste liquid treated in step S7 is discharged, and the effluent meets the discharge standards.

[0036] In a preferred embodiment, in step S1, a blower is used to blow air into the organic wastewater, thereby generating a large number of highly dispersed fine bubbles. The buoyancy generated by the bubbles directly carries the adsorbed oil to the surface of the water, achieving separation from the water.

[0037] In a preferred embodiment, in step S2, the coagulant is an aluminum salt or an iron salt, such as polyaluminum chloride, polyferric sulfate, aluminum sulfate, etc. After the coagulant is added, it is thoroughly stirred and mixed to flocculate and precipitate the organic and inorganic pollutants in the water that are in colloidal and micro-suspended states. This step S2 mainly removes color, turbidity, heavy metal ions and some phosphorus elements from the wastewater.

[0038] To increase the number of contact times between the reactants and the particulate catalyst, the present invention preferably prepares the particulate catalyst as packing material in a packed tower. The effluent from step S2 is passed into the packed tower, and a catalytic oxidation reaction is carried out at a predetermined heating temperature and an aeration rate of air and / or oxygen to remove most of the COD. In a preferred embodiment, the particulate catalyst in step S3 is formed by loading a first metal oxide (a first metal oxide nanocluster) onto a first powder; the composite catalytic ceramic membrane in step S4 is formed by loading a second metal oxide (a second metal oxide nanocluster) onto a ceramic membrane.

[0039] In a preferred embodiment, the first metal in the oxide of the first metal in step S3 is iron or copper; and the second metal in the oxide of the second metal in step S4 is iron or copper.

[0040] In a preferred embodiment, the particulate catalyst in step S3 is prepared by an impregnation method: an impregnation solution is prepared using a nitrate of a first metal, the first powder is immersed in the impregnation solution for a predetermined time, and then calcined in air at 600–700°C for 3–4 hours; the concentration of the impregnation solution is 0.5 mol / L–2 mol / L; preferably, the first powder is γ-Al₂O₃; preferably, the average particle size of the particulate catalyst is 5 mm. The composite catalytic ceramic membrane in step S4 is prepared by an impregnation method: an impregnation solution is prepared using a nitrate of a second metal, the ceramic membrane is immersed in the impregnation solution for a predetermined time, and then calcined in air at 600–700°C for 3–4 hours; the concentration of the impregnation solution is 0.5 mol / L–2 mol / L. In a specific catalyst preparation example, it is preferable to first clean the first powder or ceramic membrane with a weak acid or weak base, then rinse it with deionized water, and then thoroughly dry it before impregnation.

[0041] In a preferred embodiment, in steps S3 and S4, the reaction conditions are atmospheric pressure aeration, heating temperature of 60–90°C, air-to-water ratio of 3.5–7.0 L / g COD, and hydraulic retention time of 1–5 h.

[0042] In a preferred embodiment, the reflux reactor in step S4 is a cylindrical reflux reactor, with the composite catalytic ceramic membrane fixed in the upper middle part of the cylindrical reflux reactor. An inlet and a circular aerator are provided at the bottom of the cylindrical reflux reactor. The effluent from step S3 passes through the composite catalytic ceramic membrane from bottom to top. The reaction system has the retention and filtration function of the ceramic membrane itself and the catalytic performance of the loaded catalyst.

[0043] After the synergistic catalytic treatment of COD in wastewater in steps S3 and S4, the catalytic oxidation process in the packed tower in step S3 can remove most of the COD in the water. Then, the effluent from step S3 is passed into the reflux reactor with a composite catalytic ceramic membrane in step S4. The composite catalytic ceramic membrane is used to further filter and catalytically oxidize the wastewater, decompose the residual small molecule organic matter, and remove the residual COD in the effluent from step S3.

[0044] In a preferred embodiment, in step S5, most of the ammonia nitrogen in the effluent from step S4 is recovered by membrane distillation driven by a low-grade heat source. Taking advantage of the higher volatility of ammonia than water, ammonia nitrogen in wastewater can be effectively recovered. After treatment in step S5, the ammonia nitrogen concentration in the effluent can be controlled to be below 100 mg / L, which facilitates subsequent treatment.

[0045] In a preferred embodiment, in step S6, the powdered catalyst is a noble metal powdered catalyst, preferably at least one of ruthenium-based, gold-based, silver-based, and platinum-based catalysts. Considering both the economic cost and catalytic effect of the catalyst, it is further preferred that the powdered catalyst be a ruthenium-based catalyst. Even more preferably, the ruthenium-based catalyst is prepared by an impregnation method: a second powder is placed in a ruthenium chloride solution and fully impregnated by vacuum rotary evaporation to control the metal loading at 1wt%–2wt%, followed by calcination at 350–550°C in a nitrogen atmosphere for 3.5–5.5 h. Preferably, the second powder is γ-Al₂O₃. Through the above vacuum impregnation, a ruthenium-based catalyst (ruthenium oxide nanoclusters supported on γ-Al₂O₃ powder (micrometer scale)) is obtained.

[0046] In a preferred embodiment, in step S6, the powdered catalyst is fixed in a trickle bed, and the effluent from step S5 is introduced. The reaction conditions are an oxygen pressure of 0.5 MPa and heating at 60–90°C. After the treatment in step S6, the residual ammonia nitrogen is finally converted into N2 and a small amount of NO3. - Salt discharge.

[0047] The ammonia nitrogen in the water is removed through the synergistic process of steps S5 and S6. Step S5 is the main step for removing ammonia nitrogen from the water, while step S6 is the catalytic oxidation step for removing the remaining ammonia nitrogen from the water. The two steps work together to remove ammonia nitrogen from the wastewater.

[0048] In a preferred embodiment, Fe is added to the effluent in step S6. 3+ Salt, Fe 2+ Salt or Al 3+ Salts (including but not limited to polyaluminum ferric chloride, polyferric chloride, etc.) combine with soluble phosphate ions in water to form poorly soluble phosphates, which are then precipitated to remove phosphorus from the water.

[0049] The present invention will be further illustrated by a specific embodiment below.

[0050] Example 1

[0051] As shown in Figure 1, the treatment object in this embodiment is actual organic wastewater with an initial COD of 1000 mg / L. The treatment process is as follows:

[0052] 1. Air flotation for oil removal: Air is introduced into organic wastewater to generate fine bubbles, which adsorb suspended oil droplets and solid particles in the wastewater. The particles float to the surface with the bubbles to form scum, thus removing the waste oil.

[0053] 2. Coagulation and sedimentation: Add an appropriate amount of coagulant (polyferric sulfate) to the effluent from step 1, and after thorough stirring, remove colloidal and micro-suspended organic and inorganic matter from the wastewater. Simultaneously, this step significantly reduces the color and turbidity of the wastewater.

[0054] 3. First Short-Range Physicochemical Treatment of COD: The granular catalyst is placed in a packed tower, and the effluent from step 2 is introduced. A catalytic oxidation reaction is carried out under controlled heating temperature and aeration rate to remove most of the COD. The granular catalyst is prepared as follows: Unloaded blank γ-Al₂O₃ ceramic particles are soaked in dilute hydrochloric acid for 12 hours to remove impurities, then rinsed with deionized water and thoroughly dried in an oven. After removal, they are immersed in a 1 mol / L ferric nitrate solution for 24 hours, dried in an oven at 120℃ for 2 hours, and calcined at 700℃ for 4 hours (heating rate 5℃ / min) to obtain a granular catalyst loaded with iron oxide nanoclusters. The effluent, after air flotation for oil removal and coagulation sedimentation, is introduced into the packed tower containing the above granular catalyst. The reaction conditions are atmospheric pressure air aeration, heating temperature of 90℃, and hydraulic retention time of 5 hours. Organic matter in the wastewater reacts on the catalyst surface, and the catalyst's catalytic properties promote the generation of active free radicals, thereby promoting the degradation of organic pollutants.

[0055] 4. Second COD Short-Range Physicochemical Treatment: The composite catalytic ceramic membrane is fixed in a reflux reactor, and the effluent from step 3 is introduced. A catalytic oxidation reaction is carried out under controlled heating temperature and aeration rate to treat the residual COD in the effluent from step 3. The composite catalytic ceramic membrane is prepared as follows: an unloaded blank ceramic membrane is soaked in dilute hydrochloric acid for 12 hours to remove impurities, then rinsed with deionized water and thoroughly dried in an oven. After removal, it is immersed in a 1 mol / L ferric nitrate solution for 24 hours, dried in an oven at 120℃ for 2 hours, and calcined at 700℃ for 4 hours (heating rate 5℃ / min) to obtain a composite catalytic ceramic membrane loaded with iron oxide nanoclusters. The effluent from step 3 is fed into a cylindrical reflux reactor equipped with the aforementioned composite catalytic ceramic membrane (the composite catalytic ceramic membrane is fixed in the upper middle part of the cylindrical reflux reactor). An inlet and a ring-shaped aeration head are installed at the bottom of the reflux reactor. The effluent from step 3 passes through the composite catalytic ceramic membrane from bottom to top. Air aeration is used to increase oxygen mass transfer. The reaction conditions are atmospheric pressure aeration, a heating temperature of 90℃ (water bath heating), and a hydraulic retention time of 5 hours. Organic matter in the wastewater reacts on the catalyst surface. The catalyst's own catalytic properties promote the generation of active free radicals, thereby further promoting the degradation of organic pollutants. In addition to catalytic oxidation performance, the composite catalytic ceramic membrane also has a filtration function. Through the synergistic effect of steps 3 and 4, 90% of the COD in the wastewater can be removed, and the effluent is basically clear and transparent.

[0056] 5. First-stage ammonia nitrogen short-range physicochemical treatment: Most of the ammonia nitrogen in the effluent from step 4 is recovered using membrane distillation, controlling the residual ammonia nitrogen content in the effluent to be below 100 mg / L. In this example, the effluent treated in step 4 is then recovered through membrane distillation, which can reduce the ammonia nitrogen content in the wastewater to 90–100 mg / L.

[0057] 6. Second Short-Range Physicochemical Treatment of Ammonia Nitrogen: The powdered catalyst is fixed in a trickle bed, and the effluent from step S5 is introduced. Using oxygen as an oxidant, a catalytic oxidation reaction occurs to remove the remaining ammonia nitrogen in the effluent from step S5. The powdered catalyst is prepared as follows: Unloaded blank γ-Al₂O₃ powder is soaked in deionized water for 2 hours, washed, and then thoroughly dried in an oven. After removal, it is vacuum impregnated in a certain amount of ruthenium chloride solution for 3 hours, controlling the metal loading at 2 wt%. After calcination at 350℃ for 3.5 hours (heating rate of 5℃ / min), ruthenium oxide nanoclusters (powdered catalyst) are obtained. The ruthenium-based powdered catalyst prepared above is fixed in a trickle bed and reacted under conditions of 90℃ and 0.5 MPa (low-pressure oxygen). After treatment by the above-described combined physicochemical device (as shown in Figure 1), 90% of the ammonia nitrogen in the organic wastewater can be treated.

[0058] 7. Chemical phosphorus removal: Add a chemical agent (in this example, polyaluminum ferric chloride) to the effluent from step 6 to generate insoluble phosphate, which then precipitates and removes phosphorus from the water. In this example, all phosphorus in the effluent was removed, and the effluent was completely clear and transparent.

[0059] 8. Discharge meets standards: After the reaction is completed, the waste liquid treated in step 7 is discharged, and the effluent meets the discharge standards.

[0060] In other embodiments, the active elements in the particulate catalyst and the composite catalytic ceramic membrane in steps 3 and 4 of Example 1 were replaced with copper instead of iron. The results showed that the catalyst supported on copper oxide nanoclusters could also degrade about 90% of COD after 5 h of reaction at 90 °C and an oxygen flow rate of 0.8 L / min.

[0061] The inventors also compared the catalytic effects of various transition metals such as iron ions, copper ions, cobalt ions, nickel ions, and manganese ions. As a comparison, the active elements in the particulate catalyst and the composite catalytic ceramic membrane in steps 3 and 4 of Example 1 were replaced with cobalt, nickel, or manganese instead of iron. The results showed that at 90°C and an oxygen flow rate of 0.8 L / min, after 5 hours of reaction, the catalysts supported on cobalt, nickel, or manganese could only degrade about 60% of COD.

[0062] The above description, in conjunction with specific preferred embodiments, provides a further detailed explanation of the present invention. It should not be construed that the specific implementation of the present invention is limited to these descriptions. For those skilled in the art, several equivalent substitutions or obvious modifications can be made without departing from the concept of the present invention, and all such modifications, achieving the same performance or purpose, should be considered within the scope of protection of the present invention.

Claims

1. A short-cut, fully physicochemical treatment method for organic wastewater, characterized in that, The process includes the following steps: S1. Air is introduced into the organic wastewater to generate fine bubbles, which adsorb suspended oil droplets and solid particles in the wastewater. These particles float to the surface with the bubbles, forming scum and removing waste oil. S2. A coagulant is added to the organic wastewater treated in step S1 to aggregate colloidal particles and fine suspended matter in the water into larger particles, which are then separated by gravity sedimentation. S3. A granular catalyst is placed in a packed tower, and the effluent from step S2 is introduced. The heating temperature is controlled at 60-90°C, and the aeration rate of air and / or oxygen is controlled under atmospheric pressure aeration conditions to carry out a catalytic oxidation reaction and remove most of the COD. The granular catalyst is formed by an oxide of a first metal loaded on a first powder, and the first metal is iron or copper. S4. A composite catalytic ceramic membrane is fixed in a reflux reactor, and the effluent from step S3 is introduced. The heating temperature is controlled at 60-90°C, and the aeration rate of air and / or oxygen is controlled under atmospheric pressure aeration conditions. The aeration rate is used for catalytic oxidation to treat the residual COD in the effluent of step S3; wherein, the composite catalytic ceramic membrane is formed by loading a second metal oxide onto a ceramic membrane, and the second metal is iron or copper; S5, most of the ammonia nitrogen in the effluent of step S4 is recovered by membrane distillation, and the residual ammonia nitrogen content in the effluent is controlled to be less than 100 mg / L; S6, the powdered catalyst is fixed in a trickle bed, and the effluent of step S5 is introduced, using air and / or oxygen as oxidants, and a catalytic oxidation reaction is carried out at an oxygen pressure of 0.5 MPa and a heating temperature of 60~90℃ to remove the residual ammonia nitrogen in the effluent of step S5; wherein, the powdered catalyst is a ruthenium-based catalyst, and the ruthenium-based catalyst is a ruthenium oxide nanocluster loaded on γ-Al2O3 powder, prepared by impregnation method: γ-Al2O3 powder is placed in a ruthenium chloride solution and fully impregnated by vacuum rotary evaporation to control the metal loading to be 1 S7. Add chemical reagents to the effluent from step S6 to generate insoluble phosphate, and then precipitate and remove phosphorus from the water; S8. After the reaction is completed, discharge the waste liquid treated in step S7.

2. The short-cut, full physicochemical treatment method for organic wastewater as described in claim 1, characterized in that, In step S1, a blower is used to blow air into the organic wastewater, thereby generating a large number of highly dispersed fine bubbles. The buoyancy generated by the bubbles directly carries the adsorbed oil to the surface of the water, achieving separation from the water.

3. The short-range, fully physicochemical treatment method for organic wastewater as described in claim 1, characterized in that, In step S2, the coagulant is an aluminum salt or an iron salt.

4. The short-cut, fully physicochemical treatment method for organic wastewater as described in claim 1, characterized in that, The particulate catalyst in step S3 is prepared by impregnation: an impregnation solution is prepared using a nitrate of a first metal, the first powder is immersed in the impregnation solution for a predetermined time, and then calcined in air at 600~700℃ for 3h~4h; the concentration of the impregnation solution is 0.5mol / L~2mol / L; the first powder is γ-Al2O3; the composite catalytic ceramic membrane in step S4 is prepared by impregnation: an impregnation solution is prepared using a nitrate of a second metal, the ceramic membrane is immersed in the impregnation solution for a predetermined time, and then calcined in air at 600~700℃ for 3h~4h. The concentration of the impregnation solution is 0.5 mol / L to 2 mol / L.

5. The short-cut, full physicochemical treatment method for organic wastewater as described in claim 4, characterized in that, The average particle size of the particulate catalyst is 5 mm.

6. The short-cut, fully physicochemical treatment method for organic wastewater as described in claim 1, characterized in that, In steps S3 and S4, the gas-to-water ratio is 3.5~7.0 L / g COD, and the hydraulic retention time is 1~5h.

7. The short-cut, fully physicochemical treatment method for organic wastewater as described in claim 1, characterized in that: In step S5, most of the ammonia nitrogen in the effluent from step S4 is recovered by membrane distillation driven by a low-grade heat source.

8. The short-range, fully physicochemical treatment method for organic wastewater as described in claim 1, characterized in that, In step S7, the chemical agent is Fe. 3+ Salt, Fe 2+ Salt and Al 3+ At least one of the salts.

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