1. A pharmaceutical wastewater treatment process is characterized in that: the method comprises the following specific steps:

s1, firstly, collecting each strand of wastewater according to quality, wherein salicylic acid wastewater adopts a Fenton oxidation and coagulating sedimentation pretreatment process, the Fenton oxidation non-selectivity and strong oxidation property are utilized to greatly reduce the concentration of organic pollutants, particularly the concentration of difficultly-degraded pollutants, and the biodegradability of the wastewater can be improved at the same time, the salicylic acid wastewater treated by the method can selectively enter a prehydrolysis acidification tank (13), a nitrification and denitrification tank (15) or a standard discharge water tank (17) according to the water quality condition, the process wastewater adopts a microelectrolysis, Fenton oxidation and coagulating sedimentation pretreatment process, the acidity of raw water and the strong oxidation property of Fenton oxidation are utilized to greatly reduce the difficultly-degraded organic pollutants in the wastewater and improve the biodegradability of the wastewater, and the treated wastewater enters the prehydrolysis acidification tank (13);

s2, aiming at high-concentration biochemical organic pollutants in pretreated effluent, firstly adopting a mature, stable and reliable prehydrolysis acidification and deep hydrolysis acidification process, then adopting an efficient, economic and high-impact-resistance integrated A/O process aiming at low-concentration organic matters, total nitrogen, ammonia nitrogen and other pollutants, and purifying by an air floatation device (23), wherein effluent wastewater can be stably discharged up to the standard;

s3, sludge treatment, wherein sludge generated by the salicylic acid coagulation sedimentation tank (7) and residual sludge generated by the biochemical treatment system enter a materialized sludge concentration tank (18) and a biochemical sludge concentration tank (19) respectively for primary concentration, after the concentration, the materialized sludge is dewatered to the water content of about 80% through a box type automatic filter press (20) and a stacked spiral filter press (21), the dewatered sludge is entrusted with qualified unit treatment, supernatant of the materialized sludge concentration tank (18) and the biochemical sludge concentration tank (19) flows into a collection tank III (2), filter pressing liquid of the materialized sludge concentration tank (20) and the stacked spiral filter press (21) flows into a residual liquid tank (22), and after the filter pressing liquid flows into a prehydrolysis acidification tank (13) for biochemical treatment.

2. The pharmaceutical wastewater treatment process according to claim 1, wherein: the device also comprises an initial rainwater collecting pool (1), a collecting pool III (2), a collecting pool II (3) and a collecting pool I (4);

a discharge port of the first collecting tank (4) is connected with a salicylic acid Fenton oxidation tank (5), a discharge port of the salicylic acid Fenton oxidation tank (5) is connected with a salicylic acid coagulation reaction tank (6), one end of a discharge port of the salicylic acid coagulation reaction tank (6) is connected with a salicylic acid coagulation sedimentation tank (7), one end of a discharge port of the salicylic acid coagulation sedimentation tank (7) is connected with a salicylic acid intermediate water tank (8), one end of a discharge port of the salicylic acid intermediate water tank (8) is connected with a prehydrolysis acidification tank (13), a nitrification and denitrification tank (15) and a discharge water tank (17);

the salicylic acid Fenton oxidation tank (5), the salicylic acid coagulation reaction tank (6), the salicylic acid coagulation sedimentation tank (7) and the salicylic acid intermediate water tank (8) form a physical and chemical treatment system.

3. The pharmaceutical wastewater treatment process according to claim 2, characterized in that: one end of a discharge hole of the salicylic acid coagulating sedimentation tank (7) is connected with a materialized sludge concentration tank (18) and a biochemical sludge concentration tank (19).

4. The pharmaceutical wastewater treatment process according to claim 2, characterized in that: the discharge port of the second collecting tank (3) is connected with a micro-electrolysis tank (9), the discharge port of the micro-electrolysis tank (9) is connected with a Fenton oxidation tank (10), the discharge port of the Fenton oxidation tank (10) is connected with a coagulation reaction tank (11), the discharge port of the coagulation reaction tank (11) is connected with a coagulation sedimentation tank (12), the discharge port of the coagulation sedimentation tank (12) is connected with a pre-hydrolysis acidification tank (13), one end of the discharge port of the pre-hydrolysis acidification tank (13) is connected with a deep hydrolysis acidification tank (14), one end of the discharge port of the deep hydrolysis acidification tank (14) is connected with a nitrification and denitrification tank (15), one end of the discharge port of the nitrification and denitrification tank (15) is connected with a secondary sedimentation tank (16), one end of the discharge port of the secondary sedimentation tank (16) is connected with an air flotation device (23), and one end of the discharge port of the air flotation device (23) is connected with a discharge tank (17);

the micro-electrolysis tank (9), the Fenton oxidation tank (10), the coagulation reaction tank (11) and the coagulation sedimentation tank (12) form a physicochemical treatment system II.

5. The pharmaceutical wastewater treatment process according to claim 4, wherein: the device is characterized in that the prehydrolysis acidification tank (13), the deep hydrolysis acidification tank (14), the nitrification and denitrification tank (15) and the secondary sedimentation tank (16) form a biochemical treatment system, and one end of a discharge hole of the prehydrolysis acidification tank (13), the deep hydrolysis acidification tank (14), the nitrification and denitrification tank (15) and the secondary sedimentation tank (16) is connected with a materialized sludge concentration tank (18) and a biochemical sludge concentration tank (19).

6. The pharmaceutical wastewater treatment process according to claim 2, characterized in that: and a discharge hole of the third collecting tank (2) is connected with a prehydrolysis acidification tank (13).

7. The pharmaceutical wastewater treatment process according to claim 2, characterized in that: and a discharge hole of the initial rainwater collecting tank (1) is connected with the collecting tank III (2).

8. The pharmaceutical wastewater treatment process according to claim 3, wherein: one end of a discharge hole of each of the materialized sludge concentration tank (18) and the biochemical sludge concentration tank (19) is connected with the third collection tank (2).

9. The pharmaceutical wastewater treatment process according to claim 3, wherein: one end of a discharge hole of the materialized sludge concentration tank (18) is connected with a box-type automatic filter press (20), one end of a discharge hole of the box-type automatic filter press (20) is connected with a residual liquid tank (22), one end of a discharge hole of the box-type automatic filter press (20) is connected with a sludge outward transport device (24), one end of a discharge hole of the biochemical sludge concentration tank (19) is connected with a screw lamination filter press (21), one end of a discharge hole of the screw lamination filter press (21) is connected with the residual liquid tank (22), one end of a discharge hole of the screw lamination filter press (21) is connected with the sludge outward transport device (24), and a discharge hole of the residual liquid tank (22) is connected with the prehydrolysis acidification tank (13);

the biochemical sludge concentration tank (19), the automatic chamber filter press (20), the screw-stacking filter press (21) and the residual liquid tank (22) form a sludge treatment system.

10. The pharmaceutical wastewater treatment process according to claim 4, wherein: one end of a discharge hole of the air flotation device (23) is connected with the materialized sludge concentration tank (18) and the biochemical sludge concentration tank (19).

Background

The waste water is a general term of water and runoff rainwater discharged in the process of resident activities, and comprises domestic sewage, industrial waste water and other useless water such as primary rainwater runoff inflow drainage pipe canal, and generally refers to water which can not be recycled after being treated by a certain technology or can not reach a certain standard after being subjected to primary pollution to prepare pure water, and the pharmaceutical waste water belongs to industrial waste water.

The prior art has the following defects: the existing pharmaceutical wastewater treatment process has poor treatment effect, large equipment floor area and high cost investment.

Therefore, the invention is necessary to develop a pharmaceutical wastewater treatment process.

Disclosure of Invention

Therefore, the invention provides a pharmaceutical wastewater treatment process, which comprises the steps of adopting a Fenton oxidation and coagulation sedimentation pretreatment process for salicylic acid wastewater, adopting a micro-electrolysis, Fenton oxidation and coagulation sedimentation pretreatment process for process wastewater, firstly adopting a mature, stable and reliable prehydrolysis acidification and deep hydrolysis acidification process to treat high-concentration biochemical organic pollutants in pretreated effluent water, and then treating the pretreated wastewater through an A/O process and an air flotation device 23, so as to solve the problems of poor treatment effect, large equipment floor area and high cost investment of the conventional pharmaceutical wastewater treatment process.

In order to achieve the above purpose, the invention provides the following technical scheme: a pharmaceutical wastewater treatment process comprises the following specific steps:

s1, firstly, collecting each strand of wastewater according to quality, wherein salicylic acid wastewater adopts a Fenton oxidation and coagulating sedimentation pretreatment process, the Fenton oxidation non-selectivity and strong oxidation property are utilized to greatly reduce the concentration of organic pollutants, especially the concentration of difficultly-degraded pollutants, and the biodegradability of the wastewater can be improved at the same time, the salicylic acid wastewater treated by the method can selectively enter a prehydrolysis acidification tank, a nitrification and denitrification tank or a standard discharge water tank according to the water quality condition, the process wastewater adopts a microelectrolysis, Fenton oxidation and coagulating sedimentation pretreatment process, the acidity of raw water and the strong oxidation property of Fenton oxidation are utilized to greatly reduce the difficultly-degraded organic pollutants in the wastewater and improve the biodegradability of the wastewater, and the treated wastewater enters a prehydrolysis acidification tank;

s2, aiming at high-concentration biochemical organic pollutants in pretreated effluent, firstly adopting a mature, stable and reliable prehydrolysis acidification and deep hydrolysis acidification process, then adopting an efficient, economic and high-impact-resistance integrated A/O process aiming at low-concentration organic matters, total nitrogen, ammonia nitrogen and other pollutants, and purifying by an air flotation device, wherein effluent wastewater can be stably discharged up to the standard;

s3, sludge treatment, wherein sludge generated by the salicylic acid coagulation sedimentation tank and residual sludge generated by the biochemical treatment system respectively enter a materialized sludge concentration tank and a biochemical sludge concentration tank for primary concentration, after concentration, the materialized sludge concentration tank and the biochemical sludge concentration tank are respectively dewatered to the water content of about 80% by a van-type automatic filter press and a screw-stacking filter press, dewatered sludge is entrusted with qualified unit treatment, supernatant of the materialized sludge concentration tank and the biochemical sludge concentration tank flows into a collection tank III, filter pressing liquid of the van-type automatic filter press and the screw-stacking filter press flows into a residual liquid tank, and after the residual liquid flows into the prehydrolysis acidification tank, the prehydrolysis tank is pumped for biochemical treatment.

Preferably, the system also comprises an initial rainwater collecting tank, a collecting tank III, a collecting tank II and a collecting tank I;

a discharge port of the first collecting tank is connected with a salicylic acid Fenton oxidation tank, a discharge port of the salicylic acid Fenton oxidation tank is connected with a salicylic acid coagulation reaction tank, one end of a discharge port of the salicylic acid coagulation reaction tank is connected with a salicylic acid coagulation sedimentation tank, one end of a discharge port of the salicylic acid coagulation sedimentation tank is connected with a salicylic acid intermediate water tank, and one end of a discharge port of the salicylic acid intermediate water tank is connected with a prehydrolysis acidification tank, a nitrification and denitrification tank and a discharge water tank;

the salicylic acid Fenton oxidation tank, the salicylic acid coagulation reaction tank, the salicylic acid coagulation sedimentation tank and the salicylic acid intermediate water tank form a physical and chemical treatment system.

Preferably, one end of the discharge hole of the salicylic acid coagulating sedimentation tank is connected with the materialized sludge concentration tank and the biochemical sludge concentration tank.

Preferably, the second discharge port of the collecting tank is connected with a micro-electrolysis tank, the discharge port of the micro-electrolysis tank is connected with a Fenton oxidation tank, the discharge port of the Fenton oxidation tank is connected with a coagulation reaction tank, the discharge port of the coagulation reaction tank is connected with a coagulation sedimentation tank, the discharge port of the coagulation sedimentation tank is connected with a prehydrolysis acidification tank, one end of the discharge port of the prehydrolysis acidification tank is connected with a deep hydrolysis acidification tank, one end of the discharge port of the deep hydrolysis acidification tank is connected with a nitrification and denitrification tank, one end of the discharge port of the nitrification and denitrification tank is connected with a secondary sedimentation tank, one end of the discharge port of the secondary sedimentation tank is connected with an air flotation device, and one end of the discharge port of the air flotation device is connected with a discharge water tank;

the micro-electrolysis tank, the Fenton oxidation tank, the coagulation reaction tank and the coagulation sedimentation tank form a second physicochemical treatment system.

Preferably, the prehydrolysis acidification tank, the deep hydrolysis acidification tank, the nitrification and denitrification tank and the secondary sedimentation tank form a biochemical treatment system, and one end of a discharge hole of the prehydrolysis acidification tank, one end of the deep hydrolysis acidification tank, one end of the nitrification and denitrification tank and one end of a discharge hole of the secondary sedimentation tank are connected with the materialized sludge concentration tank and the biochemical sludge concentration tank.

Preferably, the three discharge ports of the collecting tank are connected with the prehydrolysis acidification tank.

Preferably, the discharge hole of the initial rainwater collecting tank is connected with the third collecting tank.

Preferably, one end of the discharge hole of the materialized sludge concentration tank and one end of the discharge hole of the biochemical sludge concentration tank are connected with a third collection tank.

Preferably, one end of a discharge port of the materialized sludge concentration tank is connected with a chamber type automatic filter press, one end of a discharge port of the chamber type automatic filter press is connected with a residual liquid tank, one end of a discharge port of the chamber type automatic filter press is connected with a sludge outward conveying device, one end of a discharge port of the biochemical sludge concentration tank is connected with a screw lamination filter press, one end of a discharge port of the screw lamination filter press is connected with the residual liquid tank, one end of a discharge port of the screw lamination filter press is connected with the sludge outward conveying device, and a discharge port of the residual liquid tank is connected with a pre-hydrolysis acidification tank;

the biochemical sludge concentration tank, the chamber type automatic filter press, the screw-stacking filter press and the residual liquid tank form a sludge treatment system.

Preferably, one end of a discharge port of the air floatation device is connected with the materialized sludge concentration tank and the biochemical sludge concentration tank.

The invention has the beneficial effects that:

1. the Fenton oxidation process has the following advantages that:

a. the use of the high-efficiency catalyst improves the reaction rate and the oxidation efficiency, overcomes the selectivity of organic oxidation and has good treatment effect;

b. the oxidant and the catalyst are easy to purchase and prepare, the investment and the operation cost are low, and compared with the cost of other treatment methods, the cost is low;

c. the oxidant H202 is a green oxidant, and is changed into H2O and O2 after decomposition, so that secondary pollution is avoided;

d. the oxidation reaction is carried out at normal temperature and normal pressure, the reaction condition is mild, the operation is easy, and the equipment investment is low;

2. the invention adopts the micro-electrolysis process, and has the following advantages:

a. the catalytic micro-electrolysis tower always keeps high activity in long-term operation, frequent activation is not needed, the operation quality is stable and reliable, and the device does not have scabbing and passivation phenomena in dozens of sewage treatment projects and still operates efficiently till now;

b. the catalytic micro-electrolysis tower has high treatment efficiency and good effect, the removal rate of CODcr is about 30-50%, and meanwhile, the oxidability of sewage can be improved, and the B/C ratio is increased by 0.1-0.3;

c. the catalytic micro-electrolysis tower has compact, novel and integrated structure, small occupied area and low energy consumption;

3. by adopting a hydrolysis acidification process, the invention has the following advantages:

a. under normal conditions, after biochemical reaction for 2-4 days, the time is short, a large-volume digestion tank is not needed, 15-25% of COD in the wastewater can be removed, the COD is reduced, the demand on oxygen is reduced, the oxygen supply load is reduced, and the amount of nutrients added into the wastewater due to the deficiency of comprehensive N, P nutrients is reduced;

b. hydrolyzing insoluble organic matter into soluble organic matter, and converting difficultly biochemical macromolecular matter into easily biodegradable micromolecular matter, such as methyl acetate, which is decomposed into acetic acid and methanol under the action of hydrolytic acidification bacteria enzyme;

the BOD/COD value of the original wastewater with the BOD/COD less than 0.3 is increased to 0.4-0.5 after anaerobic treatment, so that the biodegradability of the wastewater is improved;

4. the invention adopts the A/O process, and has the following advantages:

a. in the front of the anoxic tank, organic carbon in the wastewater is utilized by denitrifying bacteria, so that the organic load of a subsequent aerobic tank can be reduced, and the alkalinity generated by denitrification can compensate the requirement of nitrification reaction in the aerobic tank on the alkalinity;

b. after the aerobic treatment is carried out in the anoxic tank, the organic pollutants remained in the denitrification can be further removed, and the effluent quality is improved;

the removal rate of the BOD5 is higher and can reach more than 90-95%, and the denitrification and dephosphorization effect can reach more than 80%;

5. the invention has the advantages of integration of the air floatation device, compact structure, small occupied area, convenient installation and good treatment effect by adopting the air floatation device, and adopts the TJ type releaser designed by college of the same university, so that the air release is perfect and the blockage is not easy to occur.

Drawings

FIG. 1 is a schematic view of a process structure provided by the present invention;

FIG. 2 is a schematic view of a process flow provided by the present invention;

FIG. 3 is a schematic view of a collecting tank according to the present invention;

FIG. 4 is a schematic structural view of a second collecting tank provided by the present invention;

FIG. 5 is a schematic view of a third embodiment of a collecting tank according to the present invention;

FIG. 6 is a schematic structural diagram of a system for materialization processing according to the present invention;

FIG. 7 is a schematic structural diagram of a second physicochemical processing system provided by the present invention;

FIG. 8 is a schematic view of a biochemical processing system according to the present invention;

FIG. 9 is a schematic view of a second exemplary embodiment of a biochemical processing system according to the present invention;

FIG. 10 is a schematic view of a sludge treatment system according to the present invention;

FIG. 11 is a schematic view of a second embodiment of the sludge treatment system according to the present invention;

FIG. 12 is a schematic view of a drug administration system according to the present invention;

FIG. 13 is a schematic view of a second embodiment of the dosing system of the present invention;

FIG. 14 is a schematic view of a third embodiment of the present invention;

FIG. 15 is a schematic view of a fan system according to the present invention;

FIG. 16 is a schematic view of a second fan system according to the present invention;

FIG. 17 is a flow chart of biochemical waste gas treatment provided by the present invention;

FIG. 18 is a flow chart of the materialized waste gas treatment provided by the present invention.

In the figure: the system comprises an initial rainwater collecting tank 1, a collecting tank III 2, a collecting tank II 3, a collecting tank I4, a salicylic acid Fenton oxidation tank 5, a salicylic acid coagulation reaction tank 6, a salicylic acid coagulation sedimentation tank 7, a salicylic acid intermediate water tank 8, a micro-electrolysis tank 9, a Fenton oxidation tank 10, a coagulation reaction tank 11, a coagulation sedimentation tank 12, a pre-hydrolysis acidification tank 13, a deep hydrolysis acidification tank 14, a nitrification and denitrification tank 15, a secondary sedimentation tank 16, a discharge water tank 17, a physicochemical sludge concentration tank 18, a biochemical sludge concentration tank 19, a van-type automatic filter press 20, a stacked spiral filter press 21, a residual liquid tank 22, an air floatation device 23 and a sludge outward transportation device 24.

Detailed Description

The preferred embodiments of the present invention will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein for the purpose of illustration and explanation and not limitation.

Referring to the attached drawings 1-18, the pharmaceutical wastewater treatment process provided by the invention comprises the following specific steps:

s1, firstly, collecting each strand of wastewater according to quality, wherein salicylic acid wastewater adopts a Fenton oxidation and coagulating sedimentation pretreatment process, the Fenton oxidation non-selectivity and strong oxidation property are utilized to greatly reduce the concentration of organic pollutants, especially the concentration of pollutants difficult to degrade, and the biodegradability of the wastewater can be improved at the same time, the salicylic acid wastewater treated by the method can selectively enter a prehydrolysis acidification tank 13, a nitrification and denitrification tank 15 or a standard discharge water tank 17 according to the water quality condition, the process wastewater adopts a microelectrolysis, Fenton oxidation and coagulating sedimentation pretreatment process, the acidity of raw water and the strong oxidation property of the Fenton oxidation are utilized to greatly reduce the degradation-resistant organic pollutants in the wastewater and improve the biodegradability of the wastewater, and the treated wastewater enters the prehydrolysis acidification tank 13;

further, the Fenton oxidation core process is an H202/catalyst oxidation process;

the H202 oxidation in the process is a catalytic oxidation reaction which actually takes Fe/Cu/Mn/Co and the like as catalysts and takes H202 as an oxidant, namely what we say is a Fenton reagent which is discovered by Fenton in 1894 and is applied to the oxidation treatment of organic wastewater, for example, ferrous ions (Fe)²⁺) The chain reaction between hydrogen peroxide and HO is catalyzed to generate HO & free radical, and the basic action principle is as follows:

Fe²⁺+H₂O₂→Fe³⁺+HO·+OH^-

Fe³⁺+H₂O₂→Fe²⁺+HO^2·+H⁺

HO^2·+H₂O₂→O₂+H₂O+HO^·

RH+HO·→R·+H₂O

R·+Fe³⁺→R⁺+Fe²⁺

R⁺+O₂→ROO⁺→CO₂+H₂O

in the above series of reactions, HO & free radical reacts with organic RH to generate free radical R & lt- & gt, which is further oxidized to generate CO2 and H2O, thereby greatly reducing COD of the wastewater, and when the pH of the wastewater is adjusted to be alkaline and O2 exists, the following reactions also occur:

Fe²⁺+1/2O₂+H₂O+OH^-→Fe(OH)₃

2Fe³⁺+3H₂O₂+2H₂O→2H₂FeO₄+6H⁺

2H₂FeO₄+3H₂O₂→Fe(OH)₃+2H₂O+3O₂

under a certain acidity, Fe (OH)3 exists in a colloid form, has the properties of agglomeration and adsorption, and can remove metallic lead and metallic chromium in water as well as partial suspended matters and impurities;

the hydrogen peroxide as a strong oxidant can oxidize organic and inorganic toxic pollutants in water into compounds which are nontoxic or are easily decomposed by microorganisms, but generally speaking, the effect of only using the hydrogen peroxide is not ideal for high-concentration organic pollutants which are difficult to degrade, the treatment effect of the hydrogen peroxide is greatly improved by introducing FeSO4, and the catalytic oxidation treatment by using H2O2 is a treatment method which is simple to operate and very effective for common organic wastewater;

the micro-electrolysis process mainly utilizes the combined action of the reducibility of iron, the electrochemistry of iron and the flocculation adsorption of iron ions to purify the wastewater;

the treatment principle is that under the condition of the existence of acid and metal catalyst, a plurality of micro-current reactors are formed between iron and carbon, so that organic matters in the wastewater are reduced and oxidized under the action of the micro-current;

when the wastewater passes through the filler containing iron and carbon, the iron becomes an anode, the carbon becomes a cathode, and micro-current flows to form countless small batteries to generate corrosion;

the relevant reactions are as follows:

and (3) anode reaction:

Fe-2e→Fe²⁺ E0(Fe²⁺/Fe)＝-0.44V

and (3) cathode reaction:

2H⁺+2e→H2↑E0(H2+/H2)＝0.00V

when oxygen is available:

O2+4H⁺+4e→2H2O E0(O2)＝1.23V

O2+4 H2O+4e→4OH- E0(02/OH-)＝0.40V

the above reaction corrodes most in the acidic and oxygenated conditions and has the following proven functions: because the organic matter participates in the reduction reaction of the cathode, the functional group is changed, the property of the original organic matter is changed, the chroma is reduced, and the B/C value is improved;

under the action of an electric field, colloidal particles and micro dispersed pollutants of the wastewater generate an electrophoresis phenomenon, move to an electrode with opposite charges and are gathered on the electrode to clarify water; the nascent state Fe2+ of the anode is neutralized by lime to generate Fe (OH)2 and Fe (OH)3 which have extremely strong adsorption capacity, so that water is clarified; the hydrogen generated by the anode has reducibility, can reduce nitrobenzene into aniline, reduces the toxicity of the wastewater, increases the oxidability of the wastewater, and is beneficial to improving the treatment effect of a subsequent oxidation method;

s2, aiming at high-concentration biochemical organic pollutants in pretreated effluent, firstly adopting a mature, stable and reliable prehydrolysis acidification and deep hydrolysis acidification process, then adopting an efficient, economic and high-impact-resistance integrated A/O process aiming at low-concentration organic matters, total nitrogen, ammonia nitrogen and other pollutants, and purifying by an air floatation device 23, wherein effluent wastewater can be stably discharged up to the standard;

further, a hydrolytic acidification process: the hydrolysis acidification pool is divided into 4 reaction chambers, each reaction chamber is of an up-flow reaction type, namely, wastewater is distributed by a water distribution pipe at the bottom and then passes through a carrier layer in an up-flow mode, the hydraulic characteristic is close to a complete mixing type, the whole reactor is similar to a plug-flow type, the wastewater enters the reaction chambers and then flows back and forth, and sequentially passes through the carrier layer of each reaction chamber, organic matters in the wastewater are removed by fully contacting with microorganisms, the wastewater in the reaction chambers operates up and down under the flowing action of the wastewater, due to the blocking action of the carrier layer and the self-settling property of the sludge, the sludge generated in the treatment process is intercepted in the reaction chambers, an ABR biochemical pool is filled with biological carriers, the carriers are 1-6 meshes of active carbon filter materials, and inoculated with efficient composite microorganism strains, and domestication culture is carried out, so that an environment and microecological balance mainly comprising hydrolysis acidification flora and alkali-producing bacillus flora are formed in the ABR biochemical pool, the wastewater is contacted with strains growing on a carrier in an ABR biochemical pool, macromolecular insoluble organic matters in the wastewater are firstly hydrolyzed into micromolecular soluble organic matters by hydrolytic bacteria, then the micromolecular soluble organic matters are acidified into lower fatty acids such as acetic acid by acidification bacteria, and then the lower fatty acids are converted into stable inorganic substances by the alcaligenes by taking H & lt + & gt in the wastewater as an electron acceptor, so that the hydrolytic acidification of organic pollutants is realized;

the ABR wastewater automatically flows and continuously enters an aerobic biochemical tank;

hydrolytic acidification, namely anaerobic hydrolysis in which an anaerobic process is controlled at a hydrolytic acidification stage, wherein the hydrolytic acidification process is a biochemical reaction of an incomplete anaerobic method, hydrolytic acidification bacteria are dominant strains, methanogens are difficult to reproduce due to the elutriation effect of water flow in a reaction structure in consideration of different production speeds of the methanogens and the hydrolytic acidification bacteria, and dissolved oxygen in wastewater is reduced as much as possible, so that the hydrolytic acidification bacteria are more suitable for reproduction;

the hydrolysis acidification reaction tank consists of a sludge bed area, a suspension area and a clarification area, when sewage flows through the three areas from bottom to top, the anaerobic microorganisms in the sludge bed area and the suspension area complete the change of organic matters to change the organic matters into methane, carbon dioxide and water; or nitrate and nitrite are used as electron acceptors to release nitrogen in the electron acceptors, and finally, the gas, solid and liquid three-phase separation is completed in a clarification zone;

the hydrolysis acidification treatment technology is a sewage treatment process aiming at the treatment of long-chain high molecular polymers and heterocyclic organic matters, hydrolysis acidification bacteria can hydrolyze and acidify the long-chain high molecular polymers into organic micromolecule alcohol or acid with stronger biodegradability, and can also destroy and degrade partial heterocyclic organic matters which are not biochemical or have weaker biodegradability into biochemical organic molecules, so that the BOD5/CODCr value of organic pollutants in sewage is improved, and the biodegradability of the whole sewage is improved;

the anaerobic hydrolysis technology can be widely applied to high-concentration difficult-biochemical sewage treatment projects in the industries of brewing, food, cultivation, medicine, pesticide, chemical industry, dye and the like, can change non-biochemical substances in the waste water into biochemical substances, improve the B/C ratio and remove CODcr;

wherein the high-efficiency compound microorganism protects more than 100 microorganisms, including microbial flora with three functions, and compared with the traditional activated sludge or anaerobic sludge, the high-efficiency compound microorganism has the following advantages:

1. the strains are complete in variety and sufficient in quantity, so that the decomposition of various complex organic matters difficult to treat is smoothly completed;

2. the strains have various types, can adapt to toxic environment, can work and cooperate to exert full strength and complete difficult tasks;

3. the high-efficiency composite bacteria has strong decomposition capability, so that odor can be eliminated, the amount of fixed products is reduced, the sludge yield is greatly reduced, and the subsequent treatment cost is reduced;

4. compared with the traditional biological treatment process matched with a physical and chemical method, the decolorizing capacity is stronger, and simultaneously, many traditional biochemical treatment concepts are broken;

5. meanwhile, the fertilizer has the capability of eliminating COD, BOD, ammonia nitrogen, sulfides and the like;

6. the device can work normally under the environment of high chloride ions, high sulfate and high ammonia nitrogen;

7. the reactor has lower requirement on temperature, only needs more than 25 ℃, and has no obvious influence on the temperature change;

the efficient composite flora has the following advantages in the aspects of toxicity resistance and degradation resistance of organic wastewater:

1. high-resolution strains constitute the finished molecular fraction:

the efficiency of decomposing organic matters by the flora is more effective than that of common pure strains, one organic matter is utilized and decomposed by the composite bacteria microbial strains until the organic matter is decomposed into a harmless final product, the harmful matters are decomposed by the pure strains and can be stopped at a certain intermediate stage, if no other bacteria continuously decompose residual intermediate products, the treatment of the waste water cannot be finished, and if common activated sludge is used, a long time is needed for gradually acclimating and converting microbial flora;

2. elimination of various interference factors:

a. the composite bacteria microorganism has stronger desulfurization capacity, the desulfurization efficiency can reach more than 60 percent, the anaerobic system can still effectively perform methanation process in the presence of 40000mg/LSO42-, and the high-efficiency bacteria can tolerate high sulfide toxicity mainly based on acid-producing and oxygen-producing bacteria with rich varieties;

b. due to the change of microbial sources and the improvement of a biological engineering technology, the compound bacteria microbial flora can effectively decompose organic matters and remove ammonia nitrogen under the condition of Cl-40000mg/L concentration;

c. the tolerance of high-concentration NH3-N reaches 5000mg/L, and meanwhile, the ammonia nitrogen is also partially removed under the anaerobic condition;

the A/O process is a process flow developed in the beginning of 80 years, after the water quality of the wastewater is regulated, the wastewater firstly enters an anoxic tank, organic nitrogen in the wastewater is converted into NH4-N by using ammoniation bacteria, the wastewater and NH4-N in the original wastewater enter an aerobic tank, in the aerobic tank, except for oxidizing carbon-containing organic matters like a conventional activated sludge method, under a proper condition, nitrosation bacteria and nitrobacteria are used for nitrifying NH4-N in the wastewater to generate NOx-N, in order to achieve the purpose of denitrification of the wastewater, nitrified mixed liquid in the aerobic tank flows back to the anoxic tank through internal circulation, organic carbon in the original wastewater is used as an electron donor for denitrification, and the NOx-N is reduced into nitrogen;

compared with the traditional biological denitrification process, the A/O system can utilize organic matters in the original wastewater as a carbon source for denitrification so as to achieve the purposes of reducing COD and denitrification simultaneously, and the anoxic tank is arranged in front of the aerobic tank, so that when the alkalinity in water is insufficient, the alkalinity can be increased due to denitrification, and the consumption of part of the nitrification process on the alkalinity can be compensated;

the A/O process has only one sludge system, the mixed flora is alternately in an aerobic state and an anoxic state, the organic matter concentration is alternately high and low, the sludge expansion is favorably controlled, the A/O process is fast in application development at home and abroad in recent decades, and the A/O process is considered as an effective process for solving the nitrogen pollution of urban sewage and nitrogenous industrial wastewater;

in the traditional nitrification process, ammonia is thoroughly oxidized into nitrate (NH4+ → NO2- → NO3-, and full-course nitrification) all the time, and the biological denitrification of the wastewater adopts the full-course nitrification and the full-course denitrification for a long time, and the main reasons are as follows:

1) the purpose of the initial application of the nitrification process is to eliminate the adverse effect of ammonia on the water body, if the nitrification is incomplete, the formed nitrite is a triple-cause substance and can threaten the safety of aquatic organisms and human beings;

2) nitrite still has oxygen consumption capacity and consumes Dissolved Oxygen (DO) in water;

3) nitrite bacteria and nitrate bacteria commonly exist and live together, a wastewater treatment system is an open system, the two bacteria enter and exit together, and the two bacteria cannot be easily separated in engineering;

4) in nature or wastewater treatment systems, ammonia oxidation is often the rate-limiting step of the entire nitration process, with little nitrite accumulation; because the substrate provided by the nitration process is nitrate, the denitrification process can only carry out whole-course denitrification;

the air floating device has the working principle that under a certain condition, a large amount of air is dissolved in water to form solution air water which is used as a working medium, the pressure is suddenly reduced through a releaser and is quickly released, a large amount of air micro bubbles are generated to be adhered to impurities in the wastewater after coagulation reaction, the specific gravity of the flocs is smaller than 1, and the flocs float on the liquid level to form foam, namely a three-phase mixture of air, water and particles, so that pollutants are separated from the wastewater to achieve the purification effect;

the air floatation device consists of four parts: a dosing coagulation reaction part, a reflux water-soluble gas release part, an air flotation separation part, an electric appliance control part and the like;

adding a medicine coagulation part:

sewage is pumped from a sewage pool to a pipeline mixer by a sewage pump, generally, chemicals are added before a sewage inlet pump, so that liquid medicine and sewage can be fully mixed by rotating an impeller of the sewage pump, the liquid medicine is supplied by a chemical adding device, the sewage after chemical adding enters a reaction pool, and the coagulation effect is improved and the efficiency is increased by adding chemicals to the pipeline mixer for coagulation stirring;

reflux water-soluble gas release part:

the quality of the air flotation effect mainly depends on the effects of dissolving air and releasing reflux water, the air flotation adopts high-efficiency and energy-saving air dissolving and releasing equipment, compressed air of an air compressor and the treated reflux water pressurized by a water pump are fully mixed and dissolved in a dissolved air tank to form dissolved air water, and the working pressure of the dissolved air tank is generally 3-4 kg/cm 2;

an air floatation part:

sewage coagulated by adding medicine enters air flotation, the dissolved air water in the dissolved air tank is suddenly decompressed by a dissolved air releaser at the lower part of a water inlet pipe orifice, so that the air dissolved in the water is suddenly decompressed to release a large amount of micro bubbles, the micro bubbles meet condensed suspended matters in the sewage in the rising process, the micro bubbles are attached to the suspended matters to quickly float upwards, thus the suspended matters treated in the sewage are completely floated on the water surface, and then the suspended matters are scraped and discharged into a sludge tank through a foam scraper at the upper part of the air flotation, and the tank bottom is discharged through treated clean water;

an electric appliance control part:

the equipment is additionally provided with an electric appliance control cabinet, an unmanned operation state can be achieved after debugging and installation, and the electric control cabinet controls the operation of a dissolved air water pump, a foam scraper and an air compressor;

s3, sludge treatment, wherein sludge generated by the salicylic acid coagulating sedimentation tank 7 and residual sludge generated by the biochemical treatment system enter the materialized sludge concentration tank 18 and the biochemical sludge concentration tank 19 respectively for preliminary concentration, after concentration, the materialized sludge is dewatered to the water content of about 80% through the box-type automatic filter press 20 and the screw-stacking filter press 21 respectively, dewatered sludge is entrusted with qualified unit treatment, supernatant of the materialized sludge concentration tank 18 and the biochemical sludge concentration tank 19 flows into the collection tank III 2, filter liquor pressed by the box-type automatic filter press 20 and the screw-stacking filter press 21 flows into the residual liquid tank 22, and after flowing, the residual liquid is pumped into the prehydrolysis acidification tank 13 for biochemical treatment.

Further, the system also comprises an initial rainwater collecting pool 1, a collecting pool III 2, a collecting pool II 3 and a collecting pool I4;

further, salicylic acid fenton oxidation pond 5 is connected to a 4 discharge gates of collecting pit, salicylic acid coagulation reaction pond 6 is connected to 5 discharge gates of salicylic acid fenton oxidation pond, salicylic acid coagulation reaction pond 6 discharge gate one end is connected salicylic acid coagulating sedimentation tank 7, pool 8 in the middle of the salicylic acid is connected to 7 discharge gate one end of salicylic acid coagulating sedimentation tank, 8 discharge gate one end in the middle of the salicylic acid is connected prehydrolysis acidizing pond 13, is nitrified and denitrified pond 15 and is discharged pond 17, and is concrete, and collecting pit 4 has the effect of collecting the salicylic acid waste water, has the effect of realizing the fenton oxidation technology through salicylic acid fenton oxidation pond 5, has the effect of realizing the coagulating sedimentation technology through salicylic acid coagulating sedimentation tank 7.

Further, the salicylic acid Fenton oxidation tank 5, the salicylic acid coagulation reaction tank 6, the salicylic acid coagulation sedimentation tank 7 and the salicylic acid intermediate water tank 8 form a physical and chemical treatment system.

Furthermore, one end of a discharge hole of the salicylic acid coagulating sedimentation tank 7 is connected with a materialized sludge concentration tank 18 and a biochemical sludge concentration tank 19.

Further, the discharge port of the second collecting tank 3 is connected with a micro-electrolysis tank 9, the discharge port of the micro-electrolysis tank 9 is connected with a Fenton oxidation tank 10, the discharge port of the Fenton oxidation tank 10 is connected with a coagulation reaction tank 11, the discharge port of the coagulation reaction tank 11 is connected with a coagulation sedimentation tank 12, the discharge port of the coagulation sedimentation tank 12 is connected with a pre-hydrolysis acidification tank 13, one end of the discharge port of the pre-hydrolysis acidification tank 13 is connected with a deep hydrolysis acidification tank 14, one end of the discharge port of the deep hydrolysis acidification tank 14 is connected with a nitrification and denitrification tank 15, one end of the discharge port of the nitrification and denitrification tank 15 is connected with a secondary sedimentation tank 16, one end of the discharge port of the secondary sedimentation tank 16 is connected with an air flotation device 23, one end of the discharge port of the air flotation device 23 is connected with a discharge tank 17, specifically, the micro-electrolysis tank 9 has the function of realizing the micro-electrolysis process, and the Fenton oxidation tank 10 has the function of realizing the Fenton oxidation process, the coagulating sedimentation tank 12 has the function of realizing the coagulating sedimentation process, the prehydrolysis acidification tank 13 and the deep hydrolysis acidification tank 14 have the function of realizing the hydrolysis acidification process, the nitrification and denitrification tank 15 has the function of realizing the A/O process, and the collection tank II 3 has the functions of collecting methyl salicylate wastewater, methyl salicylate high-concentration wastewater, medical methyl ester wastewater, octyl salicylate wastewater, benzyl salicylate wastewater, workshop waste gas treatment wastewater and accident wastewater.

Further, the micro-electrolysis tank 9, the fenton oxidation tank 10, the coagulation reaction tank 11 and the coagulation sedimentation tank 12 form a physicochemical treatment system two.

Further, the prehydrolysis acidification tank 13, the deep hydrolysis acidification tank 14, the nitrification and denitrification tank 15 and the secondary sedimentation tank 16 form a biochemical treatment system, and one end of the discharge hole of the prehydrolysis acidification tank 13, the deep hydrolysis acidification tank 14, the nitrification and denitrification tank 15 and the secondary sedimentation tank 16 is connected with a materialized sludge concentration tank 18 and a biochemical sludge concentration tank 19.

Further, a discharge hole of the collection tank III 2 is connected with the prehydrolysis acidification tank 13, and particularly, the collection tank III 2 has the function of collecting salicylamide wastewater, equipment washing water, wastewater in an analysis chamber and other low-concentration wastewater.

Further, 1 discharge gate of initial stage rainwater collecting pool is connected collecting pool three 2, specifically, initial stage rainwater collecting pool 1 has the effect of collecting the initial stage rainwater.

Further, one end of a discharge hole of each of the materialized sludge concentration tank 18 and the biochemical sludge concentration tank 19 is connected with the collection tank III 2.

Further, one end of a discharge port of the materialized sludge concentration tank 18 is connected with a box-type automatic filter press 20, one end of a discharge port of the box-type automatic filter press 20 is connected with a residual liquid tank 22, one end of a discharge port of the box-type automatic filter press 20 is connected with a sludge outward transport device 24, one end of a discharge port of the biochemical sludge concentration tank 19 is connected with a laminated spiral filter press 21, one end of a discharge port of the laminated spiral filter press 21 is connected with the residual liquid tank 22, one end of a discharge port of the laminated spiral filter press 21 is connected with the sludge outward transport device 24, and a discharge port of the residual liquid tank 22 is connected with a prehydrolysis acidification tank 13. specifically, the box-type filter press adopts the working principle that filter plates are arranged to form a filter chamber (the two sides of the filter plates are concave, every two filter plates are combined into a box-type filter chamber), pocks and bosses are arranged on the surfaces of the filter plates and used for supporting filter cloth, through holes are arranged on the centers and corners of the filter plates to form a complete channel after being assembled, the suspension, washing water and filtrate can be introduced, two sides of the filter plate are respectively provided with a handle which is supported on the cross beam, the filter plate is pressed by a pressing device, and the filter cloth between the filter plates plays a role in sealing.

Further, the biochemical sludge concentration tank 19, the automatic chamber filter press 20, the stacked spiral filter press 21 and the residual liquid tank 22 form a sludge treatment system.

Furthermore, one end of the discharge port of the air flotation device 23 is connected with the materialized sludge concentration tank 18 and the biochemical sludge concentration tank 19.

The using process of the invention is as follows: when the method is used, firstly, each strand of wastewater is collected according to the quality, wherein the salicylic acid wastewater adopts a pretreatment process of Fenton oxidation and coagulating sedimentation, the Fenton oxidation non-selectivity and strong oxidation property are utilized to greatly reduce the concentration of organic pollutants, particularly the concentration of difficultly-degradable pollutants, and simultaneously the biodegradability of the wastewater can be improved, the salicylic acid wastewater treated by the method can selectively enter a prehydrolysis acidification tank, a nitrification and denitrification tank or a discharge water tank reaching the standard according to the water quality condition, the process wastewater adopts a pretreatment process of micro-electrolysis, Fenton oxidation and coagulating sedimentation, the acidity of raw water and the strong oxidation property of Fenton oxidation are utilized to greatly reduce the difficultly-degradable organic pollutants in the wastewater and simultaneously improve the biodegradability of the wastewater, the treated wastewater enters a prehydrolysis acidification tank, and the high-concentration biochemical organic pollutants in the pretreated effluent are treated, firstly, adopting a mature, stable and reliable prehydrolysis acidification and deep hydrolysis acidification process, then adopting an efficient, economic and high-impact-resistance integrated A/O process for pollutants such as medium-low-concentration organic matters, total nitrogen, ammonia nitrogen and the like, purifying by an air flotation device, stably discharging effluent wastewater up to the standard, when sludge is treated, sludge generated by a salicylic acid coagulation sedimentation tank and residual sludge generated by a biochemical treatment system respectively enter a materialized sludge concentration tank and a biochemical sludge concentration tank for primary concentration, after concentration, dehydrating to the water content of about 80% by respectively passing through a box type automatic filter press and a spiral filter press, entrusting qualified unit treatment to the dehydrated sludge, enabling supernatant of the materialized sludge concentration tank and the biochemical sludge concentration tank to flow into a collection tank III, and enabling filter press liquid of the box type automatic filter press and the spiral filter press to flow into a residual liquid tank, pumping the sewage into a prehydrolysis acidification pool for biochemical treatment after the sewage flows in;

wherein when the biochemical sludge is treated, the residual sludge in the biochemical sedimentation tank is discharged to a biochemical sludge concentration tank 19 by a pump or gravity flow, then is lifted by a pneumatic diaphragm pump to enter a laminated spiral filter press 21 for dehydration treatment, in order to increase the dehydration effect, a certain amount of coagulant aid is added, the water content of a dry sludge cake is below 60 percent, the dry sludge cake can be periodically transported out by a sludge transporting device 24 and can be used as a building material or other purposes, filter liquor and flushing water flow back into an organic wastewater biochemical water inlet tank for retreatment, when the materialized sludge is treated, the sludge generated in each process section is lifted to a materialized sludge concentration tank 18 by the pneumatic diaphragm pump, is lifted to a van-type automatic filter press 20 by a sludge pump for filter pressing, filter pressing effluent flows back to an inorganic wastewater collection tank, the sludge after the filter pressing by the van-type automatic filter press 20 is dried by compressed air, the filter plate is pulled open, the mud automatically falls into a mud groove, a gate valve is opened, the mud automatically falls into a mud outward transporting device 24 for outward transporting and landfill, and the water content of the mud after filter pressing is less than 60%;

when waste gas is required to be cleaned, the odor of a waste water tank is changed from unorganized emission to organized collection, the main method is that a cover plate is additionally arranged above the waste water tank, malodorous waste gas enters an alkali liquor spray tower after being collected, pollutants in the gas are conveyed into liquid by utilizing the contact between the gas and the liquid in the washing process, then clean gas is separated from the polluted liquid, the aim of cleaning air is fulfilled, the waste gas is treated in a gas-liquid reverse absorption mode, namely the liquid is sprayed downwards from the top of the tower in a vaporific or small liquid drop manner, the malodorous waste gas is in gas-liquid contact by the reverse flow of the tower body, partial water vapor is separated after demisting fillers and flows into the bottom of the tower body, and the malodorous waste gas is washed in the spray tower to purify and pretreat water-soluble parts in the waste gas;

the malodorous gas is absorbed by the aqueous solution on the biological filler, and then the aerobic reaction is carried out on the biological film, so that the malodorous gas is degraded and decomposed; the core of the technology is to culture high-efficiency deodorant strains and a reasonable equipment structure;

a biological filter deodorization device is a method for processing malodorous gas which is most researched, technically mature and most commonly used in practice at present, the processing flow is that gas containing malodorous substances passes through a filter bed from bottom to top after being subjected to pretreatment processes such as dust removal, humidification or temperature reduction and the like, the malodorous substances are transferred to a water-microorganism mixed phase (biological layer) from gas phase when passing through the filter layer and are decomposed by the metabolism of microorganisms attached to and grown on the filter material, the method mainly utilizes the biochemical action of the microorganisms to decompose pollutants and convert the pollutants into harmless substances, the microorganisms utilize organic substances as substrates required by the growth and propagation of the microorganisms, and finally oxidize and decompose macromolecules or organic substances with complex structures into inorganic substances such as simple water, carbon dioxide and the like through different conversion ways, and simultaneously utilizes energy generated in the process of the isomerization action through assimilation and utilization, the method has the advantages that the organisms of the microorganisms are increased and propagated, favorable conditions are created for further exerting the processing capacity of the organisms on the organic matters, the essence of pollutant removal is that the organic matters are absorbed, metabolized and utilized by the microorganisms as nutrient substances, and the process is a complex process consisting of physics, chemistry, physical chemistry and biochemistry;

can be simplified to the following expression:

malodorous substance + O2+ microorganisms → cell metabolites + CO2+ H2O.

The experimental results are as follows:

the above description is only a preferred embodiment of the present invention, and any person skilled in the art may modify the present invention or modify it into an equivalent technical solution by using the technical solution described above. Therefore, any simple modifications or equivalent substitutions made in accordance with the technical solution of the present invention are within the scope of the claims of the present invention.