CN100343187C - Treatment process for industrial wastewater of VB12 production and dedicated wastewater treatment machine therefor - Google Patents

Abstract

The present invention relates to a resource-based treatment process for industrial waste water produced by VB12 and a special waste water treatment machine thereof. The process steps are protein extraction by chemical flocculation → extraction, back extraction to extract propionic acid, preparation of calcium propionate → extraction, back extraction and extraction Acetic acid, preparation of glacial acetic acid → raffinate water AOPs superoxidation, O ₃ /H ₂ O ₂ composite microwave treatment; the invention also provides a special wastewater treatment machine for extracting protein by chemical flocculation and extracting protein and propionic acid from industrial wastewater producing VB12 , A special wastewater treatment machine for superoxidation treatment of wastewater after acetic acid. Using a special wastewater treatment machine, the industrial wastewater produced by VB12 can be treated as a resource through this process, and the protein, propionic acid, acetic acid, etc. in the wastewater can be extracted and further made into additional products, which can realize zero discharge of industrial wastewater and no secondary Pollution, the raffinate water is further processed to become reclaimed water for reuse, and the sludge is turned into high-quality organic fertilizer.

Description

Recycling process of industrial wastewater producing VB12 and its special wastewater treatment machine

technical field

The invention belongs to the field of industrial waste water treatment, and specifically relates to a resource treatment process and a special waste water treatment machine for producing VB12 industrial waste water.

Background technique

The concentration of COD _Cr in the wastewater discharged from the production process of VB12 is about (6~7)×10 ⁴ mg/l, the concentration of sulfate is about 3000mg/l, and the water quality contains 1.9% propionic acid and about 1% acetic acid As well as a large amount of amino acid protein, the treatment of the high-concentration and high-color organic wastewater formed has become an old, big, and difficult problem in the industry. The existing technical means make it difficult to meet the discharge standards. The traditional treatment technology is to mix this water with other slightly polluted wastewater in proportion to dilute the concentration of COD _Cr to about 1000mg/l, SO ₄ ^2- to about 700mg/l, and use UASB anaerobic reactor. A large amount of biogas and H ₂ S are produced during the process of treatment, which has a foul smell and causes secondary pollution to the atmosphere. The process operation time is about 20 hours, and the structure is huge, requiring an investment of about 15 million yuan. However, the removal rate of COD _Cr It is only about 80%. If the daily processing capacity is 500 tons, the operation cost will reach more than 3 million yuan per year.

Contents of the invention

The technical problem to be solved by the present invention is to provide a resource-based treatment process for the production of VB12 industrial wastewater to achieve zero discharge and no secondary pollution, and to extract protein, propionic acid, acetic acid, etc. in the wastewater and further make As an additional product, the remaining waste water is finally treated as reclaimed water for reuse, and the sludge is turned into high-quality organic fertilizer.

Another object of the present invention is to provide a special waste water treatment machine for extracting protein by chemical flocculation, so as to extract the protein in the industrial waste water producing VB12.

The further object of the present invention is to provide a kind of special-purpose waste water treatment machine that the waste water after the industrial waste water extraction albumen, propionic acid, acetic acid of producing VB12 is carried out superoxidation treatment, terminal links to each other with microwave processor, the drainage after microwave treatment is Reclaimed water can be reused.

The present invention will solve above-mentioned technical problem to be realized by following technical scheme: a kind of resource treatment process of producing VB12 industrial waste water, comprises following method steps:

a. Extract protein from VB12 production wastewater by chemical flocculation method, and the remaining wastewater A is for use;

b. Waste water A extracts propionic acid by extraction and back extraction to prepare calcium propionate, and the remaining waste water B is used for subsequent use;

c. Waste water B utilizes extraction, back extraction method to extract acetic acid, prepares glacial acetic acid, remaining waste water E;

d. Wastewater E is subjected to solid-liquid separation after AOPs superoxidation, O ₃ /H ₂ O ₂ , and microwave composite treatment, and the liquid part is reclaimed water, and the solid part is sludge D.

in,

The chemical flocculation method for extracting protein is carried out through the following method steps:

E. drop into the chitosan aqueous solution that weight percent concentration is 2-4‰ in VB12 production waste water, and its input amount is 80-100mg/L; Then

f. drop into the basic aluminum chloride aqueous solution of 4-6% concentration, and its input amount is 60-80mg/L; Then

g. Add 0.5-1.5‰ sodium polyacrylate aqueous solution, the input amount is 4-6mg/L, so that the protein contained in the waste water is fully flocculated to form flocs and add clear liquid; then

h. The above-mentioned flocs and clear liquid are filtered, concentrated and dried to obtain the finished protein.

The extraction and stripping methods extract propionic acid, and the preparation of calcium propionate is carried out through the following method steps:

i. waste water A adds extraction agent to extraction propionic acid in extraction tower, then adds stripping agent in stripping tower, makes calcium propionate lye, obtains calcium propionate crude product through neutralization filtration, concentrated cooling, crystallization filtration;

j. The crude calcium propionate is dissolved by heating, decolorized, concentrated by filtration, crystallized by cooling, and dried by filtration to obtain the refined calcium propionate, that is, edible grade calcium propionate.

The extraction and back extraction method extracts acetic acid, and the preparation of glacial acetic acid is carried out through the following method steps:

k. Wastewater B obtains acetic acid aqueous solution through extraction, back extraction, and distillation;

l. Acetic acid obtains glacial acetic acid after rectification.

The step d is carried out in sequence according to the following steps:

Wastewater E is stripped of ammonia nitrogen by O ₂ +O ₃ , flocculated to remove excess protein, precipitated in an intermediate sedimentation tank, decolorized and internally electrolyzed, O ₃ /H ₂ O ₂ reaction, microwave treatment, solid-liquid separation, and the liquid part obtained is reclaimed water. The solid part is sludge D;

The sludge D is subjected to physical treatment such as concentration and centrifugal compression, and finally becomes a sterile organic fertilizer.

The extractant mentioned above is trioctylamine, tributylphosphine oxide, n-octanol, tributyl phosphate; the stripping agent is Ca(OH) ₂ and NaOH aqueous solution.

A special wastewater treatment machine for extracting protein by chemical flocculation, including dosing tanks 1, 2, and 3 controlled by flowmeters, mixed into the flocculation reaction tank 8 through pipelines and pumps, and dried after solid-liquid separation in the centrifuge 5 The machine 6 forms an assembly line; its front end, that is, the water inlet, is connected to the storage tank 7 for storing and producing VB12 industrial wastewater, and its terminal is the liquid outlet; there are chitosan dosing tanks sequentially on the pipeline between the water inlet and the pump body before filtration 1. The PAC dosing tank 2 and the sodium polyacrylate dosing tank 3 communicate with it;

Chitosan dosing tank 1, filled with an aqueous solution of chitosan at a concentration of 2 to 4 ‰ by weight;

PAC dosing tank 2, containing aluminum salt PAC, that is, an aqueous solution of basic aluminum chloride with a concentration of 4-6%;

Sodium polyacrylate dosing tank 3 contains the auxiliary agent sodium polyacrylate, that is, 0.5-1.5‰ sodium polyacrylate solution.

The present invention also provides a special wastewater treatment machine for wastewater superoxidation treatment, including dosing tanks 11, 121, 122, 131, 132, 14 and 15 controlled by flowmeters, ozone generators 171 and 171, intermediate sedimentation tanks 191 and 192, reactors 18 and 20, inner electrolytic tank 21, static mixers 221, 222, 223 and 224, pump bodies 241, 242, 243, 244 and 245, corresponding anti-corrosion liquid pipelines, the main body of which consists of reactor 18, pump Body 241, intermediate sedimentation tank 191, pump body 242, inner electrolytic tank 21, reactor 20, pump body 243, intermediate sedimentation tank 192, and pump body 245 are sequentially connected in series through pipelines, and the front end, namely, the water inlet, is connected to the extracted protein , calcium propionate, glacial acetic acid after the production VB12 industrial wastewater pipeline, its terminal links to each other with microwave processor; There is dosing tank 11 to be connected with it above the pipeline between water inlet and reactor 18; Reactor 18 and Between the pump body 241, the pipeline between the pump body 242 and the intermediate sedimentation tank 191, there are successively drug dosing tanks 121, 131, static mixers 221, 222 communicating with it; between the intermediate sedimentation tank 191 and the inner electrolytic tank 21 _H2SO4 dosing tank ₁₄ is connected to it on the pipeline; _{H2O2 dosing} tank 15 is connected to it on the pipeline between reactor 20 and pump body 243; The dosing tank 122, the static mixer 223, the pump body 244, the dosing tank 132, and the static mixer 224 reach the intermediate sedimentation tank 192, and then connect to the terminal water outlet through the pump body 245; at the bottom of the two reactors 18 and 20, Ozone generators 171, 172 vent pipes are respectively connected to their inner chambers;

Above-mentioned dosing tanks 11, 121, 131, 14, 15, 122, 132 contain medicaments in each dosing tanks from the water inlet as follows:

20-25% concentration of Ca(OH) ₂ + 1-2% concentration of MgCl ₂ + 1-2% concentration of Ca(ClO) ₂ mixed water;

Mixed aqueous solution of basic aluminum chloride PAC+3-5% concentration of fly ash;

Sodium polyacrylate (anion) solution with a concentration of 1-2‰;

20-25% _H2SO4 aqueous _solution ;

5-10% H ₂ O ₂ aqueous solution;

Mixed aqueous solution of basic aluminum chloride PAC+3-5% concentration of fly ash;

Sodium polyacrylate (anion) solution with a concentration of 1-2‰;

The medium Fe+C+TiO ₂ is placed in the inner electrolytic tank.

Through the above treatment process, the present invention sequentially extracts a large amount of amino acid protein, propionic acid and acetic acid contained in the waste water in the VB12 production process, and further can be used to prepare food additives, sterile organic fertilizers, etc., and sell them as commercial products , realized turning waste into wealth and increasing income; this process treats sludge into organic fertilizer, which not only completely solves the problems of environmental pollution, garbage storage and treatment in the original technology, but also realizes the increase of agricultural product income; the final wastewater treatment The reclaimed water with COD _Cr <60 can be reused, so that the environmental pollution caused by the wastewater discharged in the original VB12 production process can be completely solved, and a win-win situation of social and economic benefits can be achieved. The process is applicable to the treatment of industrial waste water produced by VB12, and can be extended to the fermentation process pharmaceutical industry.

The wastewater treatment machine for flocculating and extracting protein provided by the present invention is used to extract protein from industrial wastewater producing VB12.

The waste water superoxidation microwave processor provided by the present invention is used to process the industrial waste water produced by extracting protein, propionic acid and acetic acid to produce VB12, and the terminal drainage is recycled water.

The present invention will be further described in detail below in conjunction with the accompanying drawings and specific embodiments.

Description of drawings

Fig. 1 is the technical block diagram of extracting protein by chemical flocculation method of the present invention;

Fig. 2 is the schematic diagram of the wastewater treatment machine of extracting protein by chemical flocculation;

Fig. 3 is the process block diagram that extraction of the present invention, stripping method prepare calcium propionate;

Fig. 4 is the process block diagram that extraction of the present invention, back extraction method prepares glacial acetic acid;

Fig. 5 is the process block diagram of waste water E in the technological process of the present invention;

Fig. 6 is the process schematic diagram of the waste water superoxidation microwave treatment machine of technology shown in Fig. 5;

Fig. 7 is a block diagram of the overall process flow of the present invention.

1- Chitosan dosing tank, containing chitosan aqueous solution with a concentration of 2-4‰;

2-PAC dosing tank, containing aluminum salt PAC, that is, a 4-6% aqueous solution of basic aluminum chloride;

3- Sodium polyacrylate dosing tank, containing sodium polyacrylate additive, that is, sodium polyacrylate aqueous solution with a concentration of 0.5-1.5‰;

41-static mixer; 42-filter; 5-centrifuge; 6-dryer; 7-storage tank; 8-flocculation tank;

11-dosing tank, filled with 20-25% concentration of Ca(OH) ₂ + 1-2% concentration of MgCl ₂ + 1-2% concentration of Ca(ClO) ₂ mixed aqueous solution;

121, 122-dosing tanks, containing the fly ash aqueous solution of basic aluminum chloride PAC+3-5% solution;

131, 132-Dosing tanks containing sodium polyacrylate, that is, sodium polyacrylate (anion) aqueous solution with a concentration of 1-2‰;

14-Dosing tank, filled with 20-25% _H2SO4 aqueous solution _;

15-dosing tank, filled with 5-10% _{H2O2 aqueous} solution;

16-flow meter; 171, 172-ozone generator; 18-reactor;

191, 192-intermediate sedimentation tank; 20-reactor; 21-inner electrolytic tank;

221, 222, 223, 224-static mixer; 23-pipeline;

241, 242, 243, 244, 245 - pump body.

Detailed ways

A resource treatment process for industrial wastewater producing VB12 is carried out according to the process flow shown in Figure 7, namely: industrial wastewater producing VB12→protein extraction by chemical flocculation→extraction and back extraction of propionic acid to prepare calcium propionate →Extract acetic acid by extracting and back-extracting methods to prepare glacial acetic acid→superoxidize raffinate water with AOPs, and treat with O ₃ /H ₂ O ₂ compound microwave.

Specifically, this technique is realized according to the following method steps:

①Use the chemical flocculation method to extract protein from the production of VB12 wastewater, and use the chemical flocculation method shown in Figure 2 to extract the protein waste water treatment machine, according to the process steps shown in Figure 1.

Figure 2 is a special wastewater treatment machine for chemical flocculation to extract protein, which is an assembly line. Including dosing tank 1-3 controlled by flowmeter, centrifugal sewage pump and connecting valve, static mixer 41, filter 42, flocculation tank 8, centrifuge 5, dryer 6 and corresponding anti-corrosion liquid pipeline, mixing front pump Body, static mixer 41, flocculation tank 8, pump body before filtration, filter 42, centrifuge 5 and dryer 6 are sequentially connected in series through pipelines, and its front end is the water inlet and the storage tank for storing the production of VB12 industrial wastewater 7 are connected, and the terminal is the liquid outlet; on the pipeline between the water inlet and the pre-mixing pump body, there are chitosan dosing tank 1 and PAC dosing tank 2 connected to it; the pre-mixing pump body and the static mixer 41 Sodium polyacrylate dosing tank 3 communicates with it on the pipeline;

Chitosan dosing tank 1, containing chitosan aqueous solution with a concentration of 2-4‰;

PAC dosing tank 2, containing aluminum salt PAC, that is, basic aluminum chloride solution with a concentration of 4-6%;

The sodium polyacrylate dosing tank 3 contains the additive sodium polyacrylate, that is, an aqueous solution of sodium polyacrylate with a concentration of 0.5-1.5‰.

Fig. 1 is the process of extracting protein by chemical flocculation, which is realized through the following method steps:

(1) in storage tank 7, be the industrial waste water of producing VB12, before the pump, drop into the chitosan aqueous solution of 2-4‰ concentration in dosing tank 1; Then

(2) drop into the basic aluminum chloride solution of PAC i.e. 4-6% concentration in the dosing tank 2; then

(3) Add additive sodium polyacrylate from the dosing tank 3 after the pump, that is, sodium polyacrylate solution with a concentration of 0.5-1.5‰, and then introduce it into the flocculation tank 8 after passing through the static mixer 41, so that the protein contained in the waste water is fully flocculated , forming flocs and adding clear liquid;

(4) add clear liquid to above-mentioned floc and filter through filter 42 again, centrifuge 5 carries out solid-liquid separation and concentration, then dries through drier 6, obtains finished protein, can be further used as feed additive; Surplus waste water A is standby;

② Utilize waste water A extraction, back extraction method to extract propionic acid, further prepare calcium propionate, realize by the method steps shown in Figure 3:

(1) Wastewater A is added to the reciprocating vibration extraction tower to extract propionic acid, and then added to the stripping tower - lime is NaOH+Ca(OH) ₂ (select clean lime, wherein Mg content ≤ 0.5%) , the calcium propionate lye is prepared, neutralized by about 20% industrial sulfuric acid, concentrated and cooled by membrane filtration and multi-effect evaporator, and the lye is refluxed by a conical liquid separator, 20M ² plate and frame filter press Crystallization filtration obtains calcium propionate crude product;

(2) Calcium propionate crude product plus deionized water is heated and dissolved below 100°C, decolorized by activated carbon, filtered and concentrated in a vacuum filter, then filtered by cooling crystallization, and filtered in a 20M ² plate and frame filter press , after drying in a 100Kg, 100°C drying oven to obtain calcium propionate fine-quality food-grade calcium propionate;

The remaining waste water B is for use.

3. Utilize waste water B extraction, back extraction method to extract acetic acid, further prepare glacial acetic acid, carry out by the method step shown in Fig. 4:

Wastewater B is extracted by adding an extractant prepared with n-octanol and tributyl phosphate in the reciprocating vibration extraction tower, and then stripped with soda lime as the stripping agent in the stripping tower. After filtering, about 20% of the industrial Neutralize with sulfuric acid, add deionized water to filter, use a crude distillation tower to obtain crude acetic acid, and then pass through a rectification tower to obtain glacial acetic acid.

Remaining waste water E.

④Wastewater E treatment

Use the special wastewater treatment machine for superoxidation treatment of wastewater as shown in Figure 6 to perform superoxidation treatment, and then perform microwave treatment and solid-liquid separation. This processor comprises the dosing tanks 11, 121, 122, 131, 132, 14 and 15 controlled by flow meters, ozone generators 171 and 171, intermediate sedimentation tanks 191 and 192, reactors 18 and 20, and inner electrolytic tank 21 , static mixers 221, 222, 223 and 224, pump bodies 241, 242, 243, 244 and 245, corresponding anti-corrosion liquid pipelines, the main body of which is composed of reactor 18, pump body 241, intermediate sedimentation tank 191, pump body 242, The inner electrolytic tank 21, the reactor 20, the pump body 243, the intermediate sedimentation tank 192, and the pump body 245 are sequentially connected in series through pipelines, and the front end, that is, the water inlet, is connected to the production VB12 industry after extracting protein, calcium propionate, and glacial acetic acid. Waste water pipeline, its terminal links to each other with microwave processor; There is dosing tank 11 to communicate with it above the pipeline between water inlet and reactor 18; Between reactor 18 and pump body 241, pump body 242 and intermediate sedimentation tank The pipelines between 191 are respectively connected with dosing tanks 121, 131 and static mixers 221, 222 in turn; on the pipelines between the _intermediate sedimentation tank 191 and the inner electrolytic tank 21, there are _H2SO4 dosing tanks 14 and On the pipeline between the reactor 20 and the pump body 243 there is H ₂ O ₂ dosing tank 15 communicates with it; the outlet pipe of the reactor 20 passes through the dosing tank 122, the static mixer 223, the pump body 244. The dosing tank 132 and the static mixer 224 reach the intermediate sedimentation tank 192, and then connect to the terminal water outlet through the pump body 245; at the bottom of the two reactors 18, 20, there are respectively ozone generators 171, 172 ventilation pipes and their internal cavities connected;

Above-mentioned dosing tanks 11, 121, 131, 14, 15, 122, 132 contain medicaments in each dosing tanks from the water inlet as follows:

20-25% Ca(OH) ₂ + 1-2% MgCl ₂ + 1-2% Ca(ClO ₎ 2 mixed water;

Mixed aqueous solution of basic aluminum chloride PAC+3-5% concentration of fly ash;

Sodium polyacrylate (anion) solution with a concentration of 1-2‰;

20-25% _H2SO4 aqueous _solution ;

5-10% H ₂ O ₂ aqueous solution;

Mixed aqueous solution of basic aluminum chloride PAC+3-5% concentration of fly ash;

Sodium polyacrylate (anion) solution with a concentration of 1-2‰;

The inner electrolytic tank is provided with a medium Fe+C+TiO ₂ , the weight ratio of Fe and C is 1:1, and the TiO ₂ is an aqueous solution with a concentration of 1-2%.

The technological process of processing is referring to Fig. 5, carries out by following method step:

(1) The waste water E is input from the water inlet pipe, and No. 1 medicine is added from the dosing tank 11 through the flow meter 16, mixed and then enters the reactor 18; at the same time, O ₂ and O ₃ are sent to the reactor 18 by the ozone generator 171. After the reaction, the remaining protein and acetic acid, propionic acid and other derivatives in the wastewater E are oxidized and decomposed to generate NO, CO ₂ , H ₂ O;

(2) pump the water in the reactor 18 into the pipe and add No. 2 medicine from the dosing tank 121, stay in the mixer 221 and fully react;

(3) The liquid is stirred and mixed by the pump, and then No. 3 medicine is added from the dosing tank 131 after the pump, fully mixed in the mixer 222 and then enters the intermediate sedimentation tank 191, and then pumped into the pipe, and before the pump by Dosing tank 14 adds No. 4 drug to adjust the pH value of the liquid to about 4;

(4) The liquid enters the decolorization inner electrolytic tank 21 after the pump, and stays for 30 seconds. After going out of the inner electrolytic tank 21, the No. 5 drug is dropped into the pipe by the dosing tank 15, enters the reactor 20, and stays for 60 minutes;

(5) In the reactor 20, drop No. 1 medicine, make PH>9, blow in O ₂ , O ₃ by the ozone generator 172, oxidize and react again for 30 seconds, the reaction gas is blown into the water tank to absorb by the pipe 23, and the reaction The water in the device 20 is pumped out again, and the above-mentioned steps of adding No. 2 drug and No. 3 drug are repeated to form a two-phase floc plus water, and then enter the post-treatment microwave system, and then undergo solid-liquid separation to obtain a qualified product with COD _Cr <60. reclaimed water.

⑤ The sludge D is concentrated and centrifugally compressed to become a sterile organic fertilizer.

Claims (9)

1. A resource treatment process for industrial wastewater from VB12 production is characterized in that: the treatment process comprises the following method steps:

a. extracting protein from VB12 production wastewater by a chemical flocculation method, and reserving the rest wastewater A for later use;

b. extracting propionic acid from the wastewater A by an extraction and back extraction method to prepare calcium propionate, and reserving the residual wastewater B for later use;

b. extracting acetic acid from the wastewater B by an extraction and back extraction method to prepare glacial acetic acid and obtain the residual wastewater E;

d. treating wastewater E with super-oxidized microwaves: by passingSuper oxidation of AOPs, O₃/H₂O₂And performing solid-liquid separation after microwave composite treatment to obtain a liquid part which is reclaimed water and a solid part which is sludge D.

2. The resource treatment process of industrial wastewater for producing VB12, according to claim 1, characterized in that: the chemical flocculation method is used for extracting protein by the following method steps:

e. adding 2-4 per mill chitosan aqueous solution into VB12 production wastewater, wherein the adding amount is 80-100 mg/L; then the

f. Adding 4-6% basic aluminum chloride aqueous solution with the addition amount of 60-80 mg/L; then the

g. Adding 0.5-1.5 per mill of sodium polyacrylate water solution at a dosage of 4-6mg/L to flocculate protein in the wastewater sufficiently to form floc and clear liquid; then the

h. And (3) adding the supernatant into the flocs, filtering, concentrating and drying to obtain the finished product protein.

3. The resource treatment process of industrial wastewater for producing VB12, according to claim 1, characterized in that: the extraction and back extraction method is used for extracting the propionic acid, and the preparation of the calcium propionate is carried out by the following method steps:

i. adding an extractant into the wastewater A in an extraction tower to extract propionic acid, then adding a back extractant into a back extractant to prepare a calcium propionate alkali liquor, and performing neutralization filtration, concentration cooling, crystallization filtration to obtain a calcium propionate crude product;

j. the crude product of calcium propionate is heated, dissolved, decolored, filtered, concentrated, cooled, crystallized, filtered and dried to obtain the refined product of calcium propionate, namely the edible calcium propionate.

4. The resource treatment process of industrial wastewater for producing VB12, according to claim 1, characterized in that: the extraction and back extraction method is used for extracting acetic acid, and the preparation of glacial acetic acid is carried out by the following method steps:

k. extracting, back-extracting and distilling the wastewater B to obtain an acetic acid aqueous solution;

rectifying acetic acid to obtain glacial acetic acid.

5. The resource treatment process of industrial wastewater for producing VB12, according to claim 1, characterized in that: the superoxide microwave treatment is carried out according to the following steps in sequence:

wastewater E through O₂+O₃Air stripping ammonia nitrogen, flocculating to remove residual protein, settling in intermediate settling tank, decoloring and internal electrolysis, and O₃/H₂O₂Reacting, microwave treating and solid-liquid separating to obtain a liquid part which is reclaimed water and a solid part which is sludge D.

6. The resource treatment process of industrial wastewater for producing VB12, according to claim 1 or 5, characterized in that: and the sludge D is subjected to concentration, centrifugal compression and physical treatment to finally obtain the sterile organic fertilizer.

7. The process for recycling industrial wastewater containing VB12 according to any one of claims 1, 3 and 4, wherein the process comprises the following steps: the extractant is trioctylamine, tributylphosphine oxide, n-octanol and tributyl phosphate; the stripping agent is Ca (OH)₂And aqueous NaOH solution.

8. A special wastewater treatment machine for extracting protein by a chemical flocculation method is characterized in that: the treatment machine comprises dosing tanks (1, 2 and 3) controlled by a flow meter, the dosing tanks are mixed by a pipeline and a pump, enter a flocculation reaction tank (8), are subjected to solid-liquid separation by a centrifugal machine (5) and then form a production line by a dryer (6); the front end, namely a water inlet, is connected with a storage tank (7) for storing industrial wastewater of VB12, and the terminal is a liquid outlet; a chitosan dosing tank (1), a PAC dosing tank (2) and a sodium polyacrylate dosing tank (3) are communicated with the pipeline between the water inlet and the pump body before filtration in sequence;

a chitosan medicine adding tank (1) filled with 2-4 per mill chitosan water solution by weight percentage;

a PAC dosing tank (2) filled with aluminum salt PAC, namely 4-6% basic aluminum chloride aqueous solution;

a sodium polyacrylate medicine adding tank (3) which is internally filled with an auxiliary agent sodium polyacrylate, namely 0.5-1.5 per mill of sodium polyacrylate solution.

9. A special waste water processor for waste water super-oxidation treatment is characterized in that: the device comprises a dosing tank (11, 121, 122, 131, 132, 14, 15), an ozone generator (17), an intermediate sedimentation tank (191, 192), a reactor (18, 20), an inner electrolytic tank (21), a static mixer (221, 222, 223, 224), a pump body (241, 242, 243, 244, 245) and corresponding anti-corrosive liquid pipelines, wherein the dosing tank is controlled by a flow meter, the main body of the device is formed by sequentially connecting the reactor (18), the pump body (241), the intermediate sedimentation tank (191), the pump body (242), the inner electrolytic tank (21), the reactor (20), the pump body (243), the intermediate sedimentation tank (192) and the pump body (245) in series through pipelines, the front end, namely a water inlet, of the device is connected with a VB12 industrial wastewater pipeline after protein extraction, calcium propionate extraction and glacial acetic acid extraction, and the terminal of the device is connected with a microwave processor; a medicine adding tank (11) is arranged above the pipeline between the water inlet and the reactor (18) and communicated with the pipeline; the pipelines between the reactor (18) and the pump body (241) and between the pump body (242) and the intermediate sedimentation tank (191) are respectively communicated with the medicine adding tanks (121, 131) and the static mixers (221, 222) in sequence; h is arranged on a pipeline between the intermediate sedimentation tank (191) and the inner electrolytic tank (21)₂SO₄The medicine feeding tank (14) is communicated with the medicine feeding tank; the pipeline between the reactor (20) and the pump body (243) is provided with H₂O₂The medicine feeding pot (15) is communicated with the medicine feeding pot; a liquid outlet pipe of the reactor (20) reaches the intermediate sedimentation tank (192) through the dosing tank (122), the static mixer (223), the pump body (244), the dosing tank (132) and the static mixer (224), and is connected with a terminal water outlet through the pump body (245); at the bottom of the two reactors (18, 20), an air pipe of an ozone generator (17) is respectively communicated with the inner cavities of the reactors;

the medicine adding tanks (11, 121, 131, 14, 15, 122 and 132) are filled with the following medicines from the water inlet in sequence:

20-25% Ca (OH)₂+ 1-2% MgCl₂+1 to 2% Ca (ClO)₂Mixing water;

a mixed aqueous solution of basic aluminum chloride PAC + 3-5% of fly ash;

1-2 per mill sodium polyacrylate (anion) solution;

20～25％H₂SO₄an aqueous solution;

h with a concentration of 5-10%₂O₂An aqueous solution;

a mixed aqueous solution of basic aluminum chloride PAC + 3-5% of fly ash;

1-2 per mill sodium polyacrylate (anion) solution;

a medium Fe + C + TiO is arranged in the inner electrolytic tank₂。

Images