CN102633402A - Method for treating chitin waste water - Google Patents
Method for treating chitin waste water Download PDFInfo
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- CN102633402A CN102633402A CN2011100856831A CN201110085683A CN102633402A CN 102633402 A CN102633402 A CN 102633402A CN 2011100856831 A CN2011100856831 A CN 2011100856831A CN 201110085683 A CN201110085683 A CN 201110085683A CN 102633402 A CN102633402 A CN 102633402A
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- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract
The invention provides a method for treating chitin waste water, wherein the method comprises the following steps of: (1) conveying soda boiling water and pickling waste water into a first-level coagulation tank for first-level coagulation sedimentation; (2) conveying yielding water of the step (1) and washing waste water into a regulating tank; (3) conveying the yielding water in the regulating tank into a second-level coagulation air floatation tank; (4) conveying the yielding water of the step (3) into an up-flow anaerobic sludge blanket; (5) conveying the yielding water of the step (4) into a hydrolysis acidification tank, and carrying out hydrolysis acidification; (6) conveying the yielding water in the hydrolysis acidification tank into a contact oxidization tank; (7) carrying out partial reflux of the yielding water in the contact oxidization tank to the hydrolysis acidification tank; and (8) conveying the residual yielding water in the contact oxidization tank into a three-level coagulation sedimentation tank for coagulation sedimentation, and discharging the obtained clean water. According to the invention, the waster water in the production of chitin is treated comprehensively, the treating expense is lowered, and the yielding water is superior to the first level discharge standard stipulated by Integrated Waste Water Discharge Standard of People's Republic of China (GB8978-1996).
Description
Technical field
The present invention relates to poor, the high salinity of biodegradability, high ammonia nitrogen and high organic concentration wastewater treatment method, relate in particular to the chitin method of wastewater treatment.
Background technology
Chitin (chitin, Regitex FA) is to utilize shrimp, crab shell as basic material, removes albumen through diluted alkaline, and the hydrochloric acid deliming obtains thick product, through further concentrated base processing, just can be made into and contains amino chitin (chitosan or Viartril-S).Produce the chitin of 1t, produce 50t left and right sides waste water to I haven't seen you for ages.This waste water is mainly derived from: the soda boiling water that (1) produces when removing albumen through diluted alkaline; (2) pickling waste waters that produces in the hydrochloric acid deliming process; (3) washes that produces during the thick product of washing.
Contain amounts of protein, fat, ionized calcium, inorganic salt etc. in the waste water.Belong to high organic concentration, high salinity, indegradable industrial effluent.
Traditional liquid waste disposal mode is directly to be discharged in the environment behind the acid-base neutralisation to go, and perhaps with after other waste water that factory produces mix carries out simple biochemical treatment, perhaps uses membrane technique.But above-mentioned treatment process perhaps can not reach national grade one discharge standard, and perhaps processing cost is very high, and the treatment process of therefore seeking a kind of highly economical is extremely urgent.
Chinese patent (CN10333021B) discloses a kind of pretreatment process of chitin waste water, through changing the pH of waste water, the protein of different iso-electric points in the waste water is separated out to greatest extent, and in conjunction with adding flocculation agent, the air supporting method is removed organism.This method operation is simple, and cost is low, but can only if want the processing chitin waste water of system, also need further research as biochemical pre-treatment.
Chinese patent (CN100567183C) discloses and has a kind ofly made chitin waste water be converted into agricultural fertilizer through replenishing N, P, K; Its key step comprises: decalcification behind the first deproteinated; After the Deproteinated alkali lye reuse 2～4 times; Isolate the alkali lye that concentrates and add N, P, K one-tenth farming fertilizer, after the acid solution reuse 2～4 of decalcification, isolate the acid solution that concentrates and directly to be used for agricultural.
Chinese patent (CN100402445C) discloses the treatment process of waste liquid in a kind of chitin production process, and the traditional end treatment process is changed in each operation stage difference individual curing.But avoid crossed contamination and reuse part useful matter.
Chinese patent (CN1119298C) discloses a kind of chitin method of wastewater treatment, and high content acid wastewater in the chitin production and alkaline waste water are not got into follow-up biochemical treatment; Only washes gets into coagulating sedimentation+A/O treatment process, and the washes water outlet can reach state three grade emissioning standard, but fails to reach national grade one discharge standard.
Chinese patent (CN101215066) all discloses with " isoelectric precipitation+flocculation sediment+A/O is biochemical " and has handled acid waste water and alkaline waste water treatment method in the chitin, but treat effluent only can reach state three grade emissioning standard; The treatment process of the washes of big flow during not mentioned chitin is produced.
Summary of the invention
The purpose of this invention is to provide a kind of chitin wastewater treatment method, to overcome the above-mentioned defective that prior art exists.
Method of the present invention comprises the steps:
(1) soda boiling water and pickling waste waters are sent into the one-level coagulation basin; Add coagulating agent and anionic polyacrylamide; The pH that adds sodium hydroxide adjusting coagulation basin composite waste is 6.5～8.5, carries out the one-level coagulation, and the one-level coagulation time is 5-30 minute; Carry out the one-level coagulating sedimentation then, the residence time of one-level coagulating sedimentation is 2-6 hour;
Described coagulating agent is selected from Poly aluminum Chloride (PAC), bodied ferric sulfate, ferrous sulfate, Tai-Ace S 150 or iron protochloride coagulating agent;
Coagulant charging quantity is 30～300mg/l, in 100% dry powder, down together;
The molecular weight of anionic polyacrylamide is 5,000,000～2,500 ten thousand, and dosage is 1～5mg/l;
Said soda boiling water derives from diluted alkaline and removes the waste water that produces in the protein process, COD
CrBe 60000～100000mg/L, ammonia nitrogen is 3000～5000mg/L;
Said pickling waste waters derives from hydrochloric acid deliming workshop section, COD
CrBe 20000～40000mg/L, ammonia nitrogen is 800～3000mg/L;
Soda boiling water: pickling waste waters=1: 0.5～2, volume ratio;
(2) water outlet and the washes of one-level coagulation basin are sent into equalizing tank, with the even water quality and the water yield;
Described washes derives from the washing room of thick product, COD
CrBe 2000～4000mg/L, ammonia nitrogen is 100～300mg/L;
(soda boiling water+acid washing water): washes=1: 60～100, volume ratio;
(3) then the two-stage coagulation air flotation pool is sent in the water outlet of equalizing tank, using NaOH to regulate its pH is 6.5～8.5, adds flocculation agent, and bubbling air carries out two-stage coagulation air supporting;
Said flocculation agent is selected from Poly aluminum Chloride (PAC) or Tai-Ace S 150, and dosage is 10～100mg/l, 100% dry powder meter, down together;
GWR 1: 3～1: 1, the residence time is 0.5～1 hour;
(4) up-flow anaerobic sludge blanket is sent in the water outlet of two-stage coagulation air flotation pool, be called for short the UASB pond, (UpFlow Anaerobic Sludge Blanketk) carries out anaerobic biological treatment; Adding sodium hydroxide adjusting pH is 6.0～9.0; Temperature is 30～50 ℃, and the residence time, the bacterial classification in the UASB pond was a salt-durable microbe in order to be 1～7d; Preferred pseudomonas putida belongs to more than one in (Pseudomonas putida) or the Plesiomonas (Plesiomonas Habs and Schubert, 1962);
The structure of said up-flow anaerobic sludge blanket is in Fang Zhanqiang etc., the structure of outer circulation UASB and method of design; Treatment of Industrial Water; 2003 04 phases; Detailed report is arranged in the document, and the present invention repeats no more;
Described pseudomonas can be adopted bacterial classification well known in the art, is the bacterial classification of CGMCC 2600 like Chinese patent 2008101368547 disclosed preserving numbers, need to prove that the bacterial classification of every Rhodopseudomonas all can be used in the present invention, not restriction;
Said Plesiomonas also is a bacterial classification well known in the art, and many documents all have detailed report to this bacterial classification, like the Plesiomonas Plesiomonas of Shanghai Ai Yan bio tech ltd;
(5) hydrolysis acidification pool is sent in the water outlet of up-flow anaerobic sludge blanket, added sodium hydroxide, and the bubbling air stirring, the acidifying that is hydrolyzed, the pH of acidication is 6.0～9.0, and dissolved oxygen concentration is 0.1～1.0mg/L, and the residence time is 1～7d;
(6) contact-oxidation pool is sent in the hydrolysis acidification pool water outlet, the bubbling air aeration carries out aerobic contact oxidation, in order to improve biodegradability and ammonia nitrogen removal efficient; In contact-oxidation pool, add alkaline matter,, replenish basicity like yellow soda ash, sodium hydrogencarbonate or sodium hydroxide; Make in the described contact-oxidation pool; The pH of water is 7.0～9.0, and dissolved oxygen concentration is 1.5～5.0mg/L, and the residence time is 1～7d;
(6) the contact-oxidation pool water part is back to hydrolysis acidification pool, reflux ratio is 30%-300%, when biochemistry is removed CODcr, accomplishes nitrification and denitrification, reaches the purpose of removing ammonia nitrogen;
The definition of said reflux ratio is following:
Reflux ratio=quantity of reflux/(soda boiling water+pickling waste waters+washes), volume ratio;
(7) three grades of coagulative precipitation tanks are sent in the remaining water outlet of contact-oxidation pool, added coagulating agent and anionic polyacrylamide, add sodium hydroxide; Control pH is 6.5～8.5; 5-15 minute coagulation time, the coagulating sedimentation residence time is 2-6 hour, the clear water after can obtaining to handle; Its water outlet reaches the People's Republic of China's integrated wastewater discharge standard " GB8978-1996 " I level emission standard, can directly discharge;
Coagulating agent is selected from Poly aluminum Chloride (PAC), bodied ferric sulfate, ferrous sulfate, Tai-Ace S 150 or iron protochloride, and dosage is 30-300mg/l, 100% dry powder meter, down together;
The molecular weight 5,000,000-2,500 ten thousand of anionic polyacrylamide, dosage are 1-5mg/l;
(8) one-level coagulative precipitation tank, two-stage coagulation air flotation pool and get into sludge thickener with the mud of three grades of coagulative precipitation tanks after sludge dewatering equipment is dehydrated into mud cake, can be used as the fertilizer outward transport.
The present invention adopts efficient biological treatment method; Waste water is carried out separation of cloudy and clear earlier; High density pickling and boil alkali waste water and carry out pre-treatment-(one-level coagulative precipitation tank) earlier; Produce washes with other lower concentrations again and get into main body treatment system-(equalizing tank+two-stage coagulation air flotation pool+UASB+ hydrolysis acidification pool+contact-oxidation pool+three grade coagulative precipitation tank); To the relatively poor biodegradability of waste water, supersalinity, high ammonia nitrogen, present method has adopted three kinds of methods simultaneously: the one, but adopted UASB and acidication bio-reactor to improve the biodegradability of waste water; The 2nd, in contact-oxidation pool, add OH
-, CO
3 2-, HCO
3 2-Plasma is kept the basicity balance of system, and aerobic stage PH is controlled at 7.0-9.0, improves biochemical nitrification and denitrification efficient, improves ammonia-N removal rate; The 3rd, to the high salinity of waste water, the mikrobe that present method adopts the domestication salt tolerant to divide is handled, and guarantees that follow-up water outlet reaches national grade one discharge standard.Present method adopts kinds of processes and Parameter Optimization combination, and three types of waste water that open circuit in the chitin production is discharged have carried out comprehensive treating process, with compared with techniques such as employing vaporizer, reverse osmosis membranes, greatly reduces processing costs.The efficient biological treatment method of present method is economy but also efficient not only, and water outlet is superior to the People's Republic of China's integrated wastewater discharge standard " GB8978-1996 " I level emission standard.
Description of drawings
Fig. 1 is a schema of the present invention
Embodiment
Referring to Fig. 1, method of the present invention comprises the steps:
(1) soda boiling water, pickling waste waters mixing, coagulating agent and anionic polyacrylamide are sent into one-level coagulation basin 1, carry out the one-level coagulation;
(2) water behind one-level coagulation basin 1 coagulating sedimentation is got into equalizing tank 2 with washes;
(3) then two-stage coagulation air flotation pool 3 is sent in the water outlet of equalizing tank 2, regulated its pH with NaOH, add flocculation agent, bubbling air carries out two-stage coagulation air supporting;
(4) up-flow anaerobic sludge blanket 4 is sent in the water outlet of two-stage coagulation air flotation pool, carried out anaerobic biological treatment;
(5) hydrolysis acidification pool 5 acidifying that is hydrolyzed is sent in the water outlet of up-flow anaerobic sludge blanket 4;
(6) contact-oxidation pool 6 is sent in hydrolysis acidification pool 5 water outlets and carried out aerobic contact oxidation;
(6) contact-oxidation pool 6 water parts are back to hydrolysis acidification pool 5;
(7) three grades of coagulative precipitation tanks 7 are sent in contact-oxidation pool 6 remaining water outlets, coagulating sedimentation, the clear water after can obtaining to handle, directly discharging;
(8) one-level coagulative precipitation tank 1, two-stage coagulation air flotation pool 3 and get into sludge thickener 8 with the mud of three grades of coagulative precipitation tanks 7 after sludge dewatering equipment 9 is dehydrated into mud cake, can be used as the fertilizer outward transport.
The waste water that the flow processing chitin of employing Fig. 1 produces when producing, wherein:
The COD of soda boiling water, pickling waste waters and production washes
CrBe respectively 92500mg/L, 37200mg/L, 3510mg/L, ammonia nitrogen are respectively 3800mg/L, 2300mg/L, 170mg/L's;
Soda boiling water: washes=1: 1, volume ratio;
(1) soda boiling water and pickling waste waters are sent into one-level coagulation basin 1; The pH that adds sodium hydroxide adjusting waste water is 8.5, adds coagulant polymeric ferric sulfate 520mg/L, anionic polyacrylamide (molecular weight 1,800 ten thousand) 2.0mg/l.; 15 minutes coagulating time, 3 hours coagulant precipitation time;
(2) water outlet and the washes of one-level coagulation basin 1 are sent into equalizing tank 2;
(soda boiling water+acid washing water): washes=1: 80, volume ratio;
(3) two-stage coagulation air flotation pool 3 is sent in the water outlet of equalizing tank; The pH that uses NaOH to regulate waste water is 7.6, adds flocculation agent Tai-Ace S 150 120mg/L;
(4) UASB pond 4 is sent in the water outlet of two-stage coagulation air flotation pool; Adding sodium hydroxide adjusting pH is 7.1,35 ℃ of temperature, and the residence time is 3d, the bacterial classification in the UASB pond is a pseudomonas putida;
(5) hydrolysis acidification pool 5 is sent in the water outlet of UASB; Adding sodium hydroxide adjusting pH is 7.0, and bubbling air, the acidifying that is hydrolyzed, and dissolved oxygen 0.5mg/L, the residence time is 3d;
(6) contact-oxidation pool 6 is sent in the water outlet of hydrolysis acidification pool, bubbling air carries out aerobic contact oxidation, and adding yellow soda ash, to keep pH value be 7.5, dissolved oxygen 2.5mg/L, and the residence time is 2d, being back to hydrolysis acidification pool water yield control reflux ratio is 120%.
(7) three grades of coagulative precipitation tanks 7 are sent in the contact-oxidation pool water outlet, added coagulant polymeric aluminium chloride 120mg/L, anionic polyacrylamide (molecular weight 1,300 ten thousand) 3.0mg/l; 15 minutes coagulation time, 4 hours coagulant precipitation time,
(8) one-level coagulative precipitation tank 1, two-stage coagulation air flotation pool 3 and get into sludge thickener 8 with the mud of three grades of coagulative precipitation tanks 7 are transported outward after pressure filter 9 is pressed into mud cake.
Adopt GB detection methods such as GB11914-89, the result is following:
Water outlet PH7.4, CODcr 72mg/l, total phosphorus 0.3mg/L, ammonia nitrogen 2mg/L, SS20mg/L.
Water outlet is superior to the People's Republic of China's integrated wastewater discharge standard " GB8978-1996 " I level emission standard.
The waste water that the flow processing chitin of employing Fig. 1 produces when producing, wherein:
Handle soda boiling water, pickling waste waters and washes COD
CrBe respectively 64300mg/L, 27400mg/L, 2640mg/L, ammonia nitrogen are respectively 4100mg/L, 1290mg/L, 136mg/L;
Soda boiling water: pickling waste waters=1: 2, volume ratio;
(1) soda boiling water and pickling waste waters are sent into one-level coagulation basin 1; The pH that adds sodium hydroxide adjusting waste water is 8.5, adds coagulant polymeric aluminium iron sulfate 430mg/L, anionic polyacrylamide (molecular weight 1,800 ten thousand) 3.0mg/l; 15 minutes coagulating time; 2 hours coagulant precipitation time, mud gets into sludge thickener 8, carries out the sludge dewatering minimizing.
(2) water outlet and the washes of one-level coagulation basin 1 are sent into equalizing tank 2;
(soda boiling water+acid washing water): washes=1: 75, volume ratio;
(3) two-stage coagulation air flotation pool 3 is sent in the water outlet of equalizing tank; The pH that uses NaOH to regulate waste water is 8.0, adds flocculant poly aluminum chloride 60mg/L;
(4) UASB pond 4 is sent in the water outlet of two-stage coagulation air flotation pool; Adding liquid caustic soda adjusting pH is 7.4,30 ℃ of temperature, and the residence time is 4d, the bacterial classification in the UASB pond is a pseudomonas putida;
(5) hydrolysis acidification pool 5 is sent in the water outlet of UASB; Adding liquid caustic soda adjusting pH is 7.2, and feeds an amount of pneumatic blending, the acidifying that is hydrolyzed, and dissolved oxygen 0.3mg/L, the residence time is 3d;
(6) contact-oxidation pool 6 is sent in the water outlet of hydrolysis acidification pool, the bubbling air aeration carries out aerobic contact oxidation, and adding sodium hydrogencarbonate, to keep pH value be 7.0, dissolved oxygen 2.8mg/L, and the residence time is 1d, being back to hydrolysis acidification pool water yield control reflux ratio is 150%.
(7) three grades of coagulative precipitation tanks 7 are sent in the contact-oxidation pool water outlet, added coagulating agent calcium chloride 80mg/L, anionic polyacrylamide (molecular weight 1,300 ten thousand) 2.0mg/l; 20 minutes coagulation time, 4.2 hours coagulant precipitation time;
(8) one-level coagulative precipitation tank 1, two-stage coagulation air flotation pool 3 and get into sludge thickener 8 with the mud of three grades of coagulative precipitation tanks 7 are transported outward after sludge dewatering equipment 9 is pressed into mud cake.
Adopt GB detection methods such as GB11914-89, the result is following:
Water outlet PH7.2, CODcr 81mg/l, total phosphorus 0.2mg/L, ammonia nitrogen 4.5mg/L, SS15mg/L.
Water outlet is superior to the People's Republic of China's integrated wastewater discharge standard " GB8978-1996 " I level emission standard.
Adopt the method identical with embodiment 1, wherein, the bacterial classification of step (4) employing is a Plesiomonas;
Adopt GB detection methods such as GB11914-89, the result is following:
Water outlet pH is 7.1, CODcr 80mg/l, total phosphorus 0.25mg/L, ammonia nitrogen 3.1mg/L, SS14mg/L.
Water outlet is superior to the People's Republic of China's integrated wastewater discharge standard " GB8978-1996 " I level emission standard.
Claims (11)
1. a chitin wastewater treatment method is characterized in that, comprises the steps:
(1) soda boiling water and pickling waste waters are sent into the one-level coagulation basin, add coagulating agent and anionic polyacrylamide, regulate the pH of coagulation basin composite waste, carry out the one-level coagulation, deposition;
(2) water outlet and the washes of one-level coagulation basin are sent into equalizing tank;
(3) the two-stage coagulation air flotation pool is sent in the water outlet of equalizing tank, regulated pH, add flocculation agent, bubbling air carries out two-stage coagulation air supporting;
(4) up-flow anaerobic sludge blanket is sent in the water outlet of two-stage coagulation air flotation pool, regulated pH, the bacterial classification in the up-flow anaerobic sludge blanket is a salt-durable microbe;
(5) hydrolysis acidification pool is sent in the water outlet of step (4), bubbling air stirs, and acidifying is hydrolyzed;
(6) contact-oxidation pool is sent in the hydrolysis acidification pool water outlet, the bubbling air aeration carries out aerobic contact oxidation;
(6) the contact-oxidation pool water part is back to hydrolysis acidification pool;
(7) three grades of coagulative precipitation tanks are sent in the remaining water outlet of contact-oxidation pool, added coagulating agent and anionic polyacrylamide, control pH, the clear water after can obtaining to handle, directly discharging.
2. method according to claim 1; It is characterized in that in the step (1), the pH that adds sodium hydroxide adjusting coagulation basin composite waste is 6.5～8.5; Carry out the one-level coagulation; The one-level coagulation time is 5-30 minute, carries out the one-level coagulating sedimentation then, and the residence time of one-level coagulating sedimentation is 2-6 hour.
3. method according to claim 2 is characterized in that, described coagulating agent is selected from Poly aluminum Chloride (PAC), bodied ferric sulfate, ferrous sulfate, Tai-Ace S 150 or iron protochloride coagulating agent;
Coagulant charging quantity is 30-300mg/l;
The molecular weight of anionic polyacrylamide is 5,000,000-2,500 ten thousand, and dosage is 1-5mg/l;
Said soda boiling water derives from diluted alkaline and removes the waste water that produces in the protein process, COD
CrBe 60000～100000mg/L, ammonia nitrogen is 3000～5000mg/L;
Said pickling waste waters derives from hydrochloric acid deliming workshop section, COD
CrBe 20000～40000mg/L, ammonia nitrogen is 800～3000mg/L;
Soda boiling water: pickling waste waters=1: 0.5～2, volume ratio.
4. method according to claim 1 is characterized in that, in the step (2), described washes derives from the washing room of thick product, COD
CrBe 2000～4000mg/L, ammonia nitrogen is 100～300mg/L;
Soda boiling water and acid washing water: washes=1: 60～100, volume ratio.
5. method according to claim 1 is characterized in that, in the step (3), using NaOH to regulate pH is 6.5～8.5;
Said flocculation agent is selected from Poly aluminum Chloride (PAC) or Tai-Ace S 150, and dosage is 10～100mg/l;
Steam-water ratio 1: 3～1: 1, the residence time is 0.5～1 hour.
6. method according to claim 1 is characterized in that, in the step (4); Adding sodium hydroxide adjusting pH is 6.0～9.0; Temperature is 30～50 ℃, and the residence time, the bacterial classification in the up-flow anaerobic sludge blanket was more than one in pseudomonas putida genus or the Plesiomonas in order to be 1～7d.
7. method according to claim 1 is characterized in that, in the step (5), adds sodium hydroxide, and the bubbling air stirring, the acidifying that is hydrolyzed, and the pH of acidication is 6.0～9.0, and dissolved oxygen concentration is 0.1～1.0mg/L, and the residence time is 1～7d.
8. method according to claim 1 is characterized in that, in the step (6), in contact-oxidation pool, adds alkaline matter, and the pH of water is 7.0～9.0, and dissolved oxygen concentration is 1.5～5.0mg/L, and the residence time is 1～7d.
9. method according to claim 1 is characterized in that, is 30%～300% with the reflux ratio of contact-oxidation pool effluent recycling to hydrolysis acidification pool.
10. method according to claim 1 is characterized in that, in the step (7), adds sodium hydroxide, and control pH is 6.5～8.5, and 5～15 minutes coagulation time, the coagulating sedimentation residence time is 2～6 hours, the clear water after the processing, directly discharging;
Coagulating agent is selected from Poly aluminum Chloride (PAC), bodied ferric sulfate, ferrous sulfate, Tai-Ace S 150 or iron protochloride, and dosage is 30～300mg/l;
The molecular weight 5,000,000 of anionic polyacrylamide～2,500 ten thousand, dosage are 1～5mg/l.
11. according to each described method of claim 1～10, it is characterized in that, one-level coagulative precipitation tank, two-stage coagulation air flotation pool and get into sludge thickener with the mud of three grades of coagulative precipitation tanks, after sludge dewatering equipment is dehydrated into mud cake, the as fertilizer sources outward transport.
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| CN104448036A (en) * | 2014-12-02 | 2015-03-25 | 岭南师范学院 | Method for recycling waste hydrochloric acid in process of producing chitin |
| CN104478989A (en) * | 2014-12-20 | 2015-04-01 | 山东绅联生物科技有限公司 | Method for recovering protein from heparin sodium extraction waste liquid |
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| CN107162335A (en) * | 2017-06-21 | 2017-09-15 | 江苏蓝必盛化工环保股份有限公司 | A kind of method for handling chitin pharmaceutical wastewater |
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