CN104016468B - Cephalosporins drug manufacture pretreatment method for wastewater - Google Patents
Cephalosporins drug manufacture pretreatment method for wastewater Download PDFInfo
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- CN104016468B CN104016468B CN201310066472.2A CN201310066472A CN104016468B CN 104016468 B CN104016468 B CN 104016468B CN 201310066472 A CN201310066472 A CN 201310066472A CN 104016468 B CN104016468 B CN 104016468B
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- 239000002351 wastewater Substances 0.000 title claims abstract description 57
- 239000003814 drug Substances 0.000 title claims abstract description 40
- 229930186147 Cephalosporin Natural products 0.000 title claims abstract description 30
- 229940124587 cephalosporin Drugs 0.000 title claims abstract description 30
- 150000001780 cephalosporins Chemical class 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 21
- 229940079593 drug Drugs 0.000 title claims abstract description 16
- 238000002203 pretreatment Methods 0.000 title claims abstract description 14
- 238000002156 mixing Methods 0.000 claims abstract description 70
- 238000012545 processing Methods 0.000 claims abstract description 5
- 239000012530 fluid Substances 0.000 claims description 59
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 39
- 239000007788 liquid Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 150000003851 azoles Chemical class 0.000 claims description 5
- 239000010977 jade Substances 0.000 claims description 5
- GCFBRXLSHGKWDP-XCGNWRKASA-N cefoperazone Chemical compound O=C1C(=O)N(CC)CCN1C(=O)N[C@H](C=1C=CC(O)=CC=1)C(=O)N[C@@H]1C(=O)N2C(C(O)=O)=C(CSC=3N(N=NN=3)C)CS[C@@H]21 GCFBRXLSHGKWDP-XCGNWRKASA-N 0.000 claims description 3
- 229960004682 cefoperazone Drugs 0.000 claims description 3
- 229960002588 cefradine Drugs 0.000 claims description 3
- VAAUVRVFOQPIGI-SPQHTLEESA-N ceftriaxone Chemical compound S([C@@H]1[C@@H](C(N1C=1C(O)=O)=O)NC(=O)\C(=N/OC)C=2N=C(N)SC=2)CC=1CSC1=NC(=O)C(=O)NN1C VAAUVRVFOQPIGI-SPQHTLEESA-N 0.000 claims description 3
- 229960004755 ceftriaxone Drugs 0.000 claims description 3
- RDLPVSKMFDYCOR-UEKVPHQBSA-N cephradine Chemical compound C1([C@@H](N)C(=O)N[C@H]2[C@@H]3N(C2=O)C(=C(CS3)C)C(O)=O)=CCC=CC1 RDLPVSKMFDYCOR-UEKVPHQBSA-N 0.000 claims description 3
- 230000004907 flux Effects 0.000 claims description 2
- 238000012544 monitoring process Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 36
- 230000008569 process Effects 0.000 abstract description 20
- 239000012295 chemical reaction liquid Substances 0.000 abstract description 2
- 239000003153 chemical reaction reagent Substances 0.000 abstract 2
- 238000009776 industrial production Methods 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 20
- 230000003115 biocidal effect Effects 0.000 description 9
- 229940088710 antibiotic agent Drugs 0.000 description 8
- 239000003242 anti bacterial agent Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- 241000894006 Bacteria Species 0.000 description 4
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- 239000000463 material Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- HSHGZXNAXBPPDL-HZGVNTEJSA-N 7beta-aminocephalosporanic acid Chemical compound S1CC(COC(=O)C)=C(C([O-])=O)N2C(=O)[C@@H]([NH3+])[C@@H]12 HSHGZXNAXBPPDL-HZGVNTEJSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 229930182555 Penicillin Natural products 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000945 filler Substances 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- JGSARLDLIJGVTE-MBNYWOFBSA-N Penicillin G Chemical compound N([C@H]1[C@H]2SC([C@@H](N2C1=O)C(O)=O)(C)C)C(=O)CC1=CC=CC=C1 JGSARLDLIJGVTE-MBNYWOFBSA-N 0.000 description 2
- 229960000583 acetic acid Drugs 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- WTEOIRVLGSZEPR-UHFFFAOYSA-N boron trifluoride Chemical compound FB(F)F WTEOIRVLGSZEPR-UHFFFAOYSA-N 0.000 description 2
- MLYYVTUWGNIJIB-BXKDBHETSA-N cefazolin Chemical compound S1C(C)=NN=C1SCC1=C(C(O)=O)N2C(=O)[C@@H](NC(=O)CN3N=NN=C3)[C@H]2SC1 MLYYVTUWGNIJIB-BXKDBHETSA-N 0.000 description 2
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- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000036783 anaphylactic response Effects 0.000 description 1
- 208000003455 anaphylaxis Diseases 0.000 description 1
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Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention relates to a kind of cephalosporins drug manufacture pretreatment method for wastewater, mainly solving prior art, to there is the periodical operation time long, and equipment volume is large; personal protection is poor; easily cause secondary pollution, human metering out of true, the problem that process terminal can not effectively control.The present invention automatically mixes waste water by adopting auto-suction pipe mixing reactor, adds degraded reagent in proportion, degraded reagent is dispersed in waste water timely and effectively, contact mixing fully, after controlling end reaction liquid pH >=13, drain into the technical scheme that follow-up waste water processing station carries out biochemical treatment, solve this problem preferably, can be applicable in the industrial production of cephalosporins drug manufacture Wastewater Pretreatment.
Description
Technical field
The present invention relates to a kind of cephalosporins drug manufacture pretreatment method for wastewater.
Background technology
Microbiotic is a kind of antibacterials conventional in people's daily life, is commonly used to treat various bacteriological infection or suppress pathogenic microorganism infection.The mankind, from the therapeutic action of nineteen twenties Late Cambrian penicillin, have had been found that nearly ten thousand kinds of microbiotic up to now, are wherein used for the treatment of the antibiotics nearly nearly hundred kinds of human diseases.
Cephalosporins is the semisynthetic antibiotics containing cephem in molecule, and it belongs to β-lactam antibitics, is the derivative of the 7-amino-cephalosporanic acid (7-ACA) in β-lactam antibitics.Cynnematin is efficient, low toxicity, clinical application are extensive, the advantage such as have that has a broad antifungal spectrum, anti-microbial effect are strong, penicillin resistant enzyme, anaphylaxis are rare compared with penicillins, it not only can destroy the cell walls of bacterium, can also sterilization within the nursery stage of bacterium, and toxicity is not almost had to body, be therefore widely used clinical.
Adopt the technique of chemosynthesis mode synthetic antibiotic, again referred to as semisynthetic antibiotics, most of cephalosporins is all adopted and is obtained in this way, as cephalo azoles beautiful jade, Cephradine, cefoperazone, ceftriaxone etc.
In the production process of this type of semisynthetic antibiotics, due to the reason of production technique, inevitably produce a large amount of organic liquid wastes, as the production process of cefazolin, starting raw material 7-ACA and thiadiazoles, acetic acid etc. at ethyl acetate, boron trifluoride, Glacial acetic acid, lay particular stress under sulfurous acid, hydrochloric acid, sodium hydroxide, acetone etc. acts on, through polystep reaction finally obtained cefazolin.Can produce a large amount of waste liquids in this production process, the content of COD reaches 10000-15000mg/L up to 3000 ~ 40000mg/L, BOD5 content.These waste liquids have to pass through certain waste water treatment process, make its COD/BOD content reach the wastewater discharge standard of national regulation, can be discharged.
The waste water of current production of antibiotics adopts biochemical method to process mostly.Document CN101746919A discloses the metabolism utilizing microorganism, makes in waste water in dissolve and the organic pollutant of colloidal state is converted into innoxious substance.Biochemical treatment process can be divided into anaerobic biological treatment and aerobiont process, to become reconciled foster microorganism by cultivating specific anaerobism, the long-chain microorganism (as celloglobulin) in waste water is made to carry out fracture Sum decomposition under the effect of microorganism, thus reduce the content of the COD/BOD in waste water, and reach the emission concentration of national regulation.
Cephalosporin analog antibiotic factory effluent, except containing except large amount of organic matter, remains the composition of cephalosporin analog antibiotic toward contact.Because cephalosporins is a kind of broad-spectrum antibiotics, it can destroy the cell walls of bacterium, and bacterium is lost activity.Therefore, containing cephalosporin analog antibiotic medicine waste water, must in advance through DeR, remove the activity of cephalosporin composition, so just can enter follow-up biochemical treatment process, support the acting in conjunction of microorganism in anaerobism/well under, carry out biochemical reaction, thus reduce the content of the COD/BOD in its waste water, make it the emission standard reaching country.
At present in the cephalosporins semisynthetic antibiotics of routine is produced, to the waste water produced by adding the method for sodium hydroxide solution, making the pH value of its solution in alkalescence, removing the biological activity of cephalosporin material.
But, in traditional chemical degradation method, the process adding sodium hydroxide adopts manual operation mostly, and whole process is all exposed in environment, add quantity and mode, the safeguard procedures of operative employee, the equal imperfection of judgement of degradation results of alkali lye, there is very large room for improvement.The shortcoming of this technique is: a) periodical operation, purification tank for liquid waste enlarged volume; B) wastewater disposal basin opens wide, and be subject to rainwater impact, overflow pollutes; C) alkali lye manually adds, metering out of true; D) process terminal can not effectively control.
Summary of the invention
It is long that technical problem to be solved by this invention is that prior art exists the periodical operation time; equipment volume is large; personal protection is poor; easily cause secondary pollution; human metering out of true; the problem that process terminal can not effectively control, provides a kind of new cephalosporins drug manufacture pretreatment method for wastewater.The method can process the waste water containing antibiotic active ingredient produced in antibiotic medicine production process continuously and also can immediately degrade, and ensure that the safe and effective controlled of Wastewater Pretreatment process.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of cephalosporins drug manufacture pretreatment method for wastewater, comprises the following steps:
A) provide auto-suction pipe mixing reactor, described auto-suction pipe mixing reactor comprises suction casing 1 and mixing section 2 successively along fluid flow direction; Suction casing 1 comprises fluid inlet conduit 3, suction chamber section 4 and expansion section 5; Fluid inlet conduit 3 stretches in suction chamber section 4, and end-contraction is conical; The tube wall of suction chamber section 4 is provided with and sucks logistics pipeline 6, suck logistics pipeline 6 end goed deep in suction chamber section 4 and be provided with fluid distributor 7; Mixing section 2 tube wall is provided with flow apron; Along fluid flow direction, the dead in line of fluid inlet conduit 3, suction chamber section 4, expansion section 5 and mixing section 2;
B) factory effluent containing cephalosporins medicine enters auto-suction pipe mixing reactor from fluid inlet conduit (3), and degraded medicine enters auto-suction pipe mixing reactor from suction logistics pipeline (6); Described waste water and degraded medicine mix, react in auto-suction pipe mixing reactor;
C) ratio control device of wastewater flow, degraded drug flux is set, and automatic pH meter is set in auto-suction pipe mixing reactor exit, by the pH value of monitoring outlet reaction solution, control the degraded medicine liquid measure added, after outlet effluent stream keeps pH >=13, drain into follow-up waste water processing station and carry out biochemical treatment.
In technique scheme, the length of the suction chamber section 4 of described auto-suction pipe mixing reactor, expansion section 5 and mixing section 2 is 1 than preferable range: (2 ~ 4): (10 ~ 20).The internal diameter of fluid inlet conduit 3 and suction chamber section 4 is 3 ~ 6 than preferable range.The internal diameter sucking logistics pipeline 6 and suction chamber section 4 is 5 ~ 10 than preferable range.Suction chamber section 4, expansion section 5 are identical with the internal diameter of mixing section 2.The position preferable range that described fluid distributor 7 gos deep into suction chamber section 4 is 1/4 ~ 1/2 of suction chamber section 4 internal diameter.Described fluid distributor 7 preferred version is the semisphere hollow cavity 72 comprising feed-pipe 71 and its end, semisphere hollow cavity 72 is provided with at least one circular hole; Wherein, the central axis of semisphere hollow cavity 72 and the angle theta preferable range of fluid flow direction are 120 ° ~ 135 °.The diameter D of feed-pipe 71
1with the diameter D of semisphere hollow cavity 72
2preferred version is for meeting D
1/ D
2≤ 0.5, on semisphere hollow cavity 72, the quantity n of circular hole and the diameter d preferred version of circular hole are for meeting (D
1/ d)
2≤ n≤0.5 (D
2/ d)
2.On semisphere hollow cavity 72, the diameter d preferable range of circular hole is 1 ~ 4 millimeter, and more preferably scope is 2 ~ 3 millimeters.According to the factory effluent characteristic of constituents of satisfying containing head, selected degraded medicine be weight percentage concentration be 2 ~ 5% NaOH solution.Cephalosporins medicine preferred version is for being selected from cephalo azoles beautiful jade, Cephradine, cefoperazone or ceftriaxone.
Venturi effect, refers to and can produce low pressure near swiftly flowing fluid, thus produces adsorption.This phenomenon is named, so be Venturi effect with its discoverer Italy physicist's Venturi (GiovanniBattistaVenturi).According to the equipment that this effect is made, be Venturi tube again.Venturi tube is used widely at industrial circle at present, as the water-jetting type vacuum pump for generation of vacuum, utilizes venturi principle to produce vacuum exactly.
Auto-suction pipe mixing reactor in the inventive method, suction casing essence is wherein Venturi tube, by Venturi effect, makes the factory effluent containing cephalosporins medicine produce negative pressure by Venturi tube, medicine intake system of degrading.Then in follow-up line mixer, carry out the raw reaction of abundant hybrid concurrency, namely its outlet obtains reaction product.The proportioning of two kinds of fluids regulates by imported valve, makes it meet the requirement of reactant ratio.
In the inventive method, the suction casing 1 of auto-suction pipe mixing reactor, a fluid distributor 7 is set, by the aperture of particular design, degraded medicine is dispersed into tiny liquid stream, in advance when principal goods stream waste water high speed flow is out-of-date, produce negative pressure, be inhaled into material under the effect of negative pressure, formed at a high speed the streams of several strands tiny by decollator dispersion, and enter mixing section 2 with principal goods stream.Under flow apron effect in mixing section, fluid by further dispersion, mixing, shock etc., thus completes hybrid reaction process.Wherein, on fluid distributor small sircle hole diameter d be inhaled into the viscosity of fluid, density, solid content, degree of scatter in main fluid, relevant with the factor such as the mutual solubility of main fluid.Diameter is too little, can increase resistance to flow, slowing down fluid mixing velocity, and easily blocked.And diameter is too large, then can not play the effect of dispersion in advance.General diameter preferable range can be 1 ~ 4 millimeter, and more preferably scope is 2 ~ 3 millimeters.The quantity n of small sircle hole, then relevant with the surface-area of suction velocity and dome-type hollow cavity, very little, because the tiny amount of fluid formed is less, make fluid soakage little, pre-mixing is insufficient for quantity.And quantity is too many, then affect the intensity of hollow cavity.N must meet: (D
1/ d)
2≤ n≤0.5 (D
2/ d)
2.
The inventive method is after suction casing increases fluid distributor, make degraded medicine can be dispersed into the streams of several strands tiny in advance, increase its degree of scatter in waste water streams, increase both contacts area, shorten and reach the well-mixed time (time can reduce 30 ~ 60%), the carrying out of favourable follow-up hybrid reaction.After have employed special fluid distributor, due to the shortening of mixing time simultaneously, the physical length of mixing tank can be greatly reduced, facilitate the installation of mixing tank, reduce the investment of mixing tank.
The inventive method have employed automatic pipeline mixing and reaction technology, in the auto-suction pipe mixing reactor of particular design, automatically mix containing cephalosporins medicine waste water and sodium hydroxide solution fully in pipeline reactor, react by certain proportioning, eventually through the judgement of reaction end pH value, automatic stopping hybrid reaction process, complete the pre-treatment degradation process of waste water, for follow-up wastewater treatment qualified discharge is laid a good foundation.Whole process stabilizing, efficient, energy-conservation, and automatically run under controllable state, achieve good technique effect.
Accompanying drawing explanation
Fig. 1 is the inventive method schematic flow sheet.
The auto-suction pipe mixing reactor schematic diagram used in Fig. 2 the inventive method.
Fig. 3 is the fluid distributor schematic diagram in auto-suction pipe mixing reactor.
In Fig. 1,8 is waste water streams, and 9 is the logistics of degraded medicine, and 10 is reacted logistics, and 12 is waste water basin, and 13 is degraded medicine basin, and 14 is auto-suction pipe mixing reactor.
In Fig. 2,1 is suction casing, and 2 is mixing section, and 3 is fluid inlet conduit, and 4 is suction chamber section, and 5 is expansion section, and 6 for sucking logistics pipeline, and 7 is fluid distributor, and 11 is flow apron.
In Fig. 3,71 is feed-pipe, and 72 is semisphere hollow cavity, and θ is the central axis of semisphere hollow cavity 72 and the angle of fluid flow direction.
Be furnished with after waste water basin one therewith tank liquid level interlock transferpump, waste liquid is delivered to auto-suction pipe mixing reactor.Be provided with the degraded medicine basin of energy degrading waste water, corrosion resisting centrifugal pump and ratio adjusting valve.When reactor of the present invention uses, principal goods stream 8 enters reactor suction casing 1 from fluid inlet conduit 3 at a high speed containing antibiotic waste water, is sucked by suction logistics 9 sodium hydroxide solution from suction logistics pipeline 6.Due to the dissemination of fluid distributor, the streams of sodium hydroxide liquid by being dispersed into several strands tiny after fluid distributor of suction, and enter mixing section 2 with principal goods stream.Under the effect of mixing section Inner guide baffle plate, fluid, by further dispersion, mixing, turbulent flow and shock, reaches well-mixed effect.By being arranged on the pH detection instrument of line-blending reactor discharge port, the pH value of detection reaction liquid, by regulating the open degree of the ratio adjusting valve on sodium hydroxide flow in pipes 6, reactor outlet mixed solution 10 is made to remain at pH >=13, lose activity to make waste water, and then drain into follow-up waste water processing station and carry out biochemical treatment, until qualified discharge.
Below by embodiment, the invention will be further elaborated.
Embodiment
[embodiment 1]
Adopt auto-suction pipe mixing reactor of the present invention process containing cephalo azoles beautiful jade class antibiotic waste water.Due to the dissemination of sparger, the 4% weight percent sodium hydroxide liquid sucked is by mixing with waste water in tiny shape after fluid distributor, and then after being mixed further by follow-up line mixer, after pH meets the requirements after measured, (pH value >=13) directly can enter follow-up biochemical treatment station and process further.
The overall length of whole suction mixing reactor is 2m, mixing section diameter 100mm, built-in corrugated filler, and valid circulation area is 50%.The length ratio of suction chamber section 4, expansion section 5 and mixing section 2 is 1: 3: 15, fluid inlet conduit 3 diameter 25mm, and the internal diameter of suction chamber section 4 is 100mm, and ratio between two is 4, and sucking logistics pipeline 6 diameter is 15mm, is 6.7 with the internal diameter ratio of suction chamber section 4.The flow velocity of pending waste water in mixing section is 0.2m/s.Waste water is only 10s from suction casing to the discharging section whole residence time, can reach and mix effect.Whole device is per hour can Continuous Wastewater Treatment amount 3m
3/ h.
The position that fluid distributor 7 gos deep into suction chamber section 4 is 1/3 of suction chamber section 4 internal diameter.The semisphere hollow cavity 72 of fluid distributor 7 is provided with n=40 circular hole, the diameter of circular hole is d=3mm, the central axis of semisphere hollow cavity 72 and angle theta=120 ° of fluid flow direction.The diameter D of feed-pipe 71
1=15mm, the diameter D of semisphere hollow cavity 72
2=30mm, meets D
1/d
2≤ 0.5 and (D
1/ d)
2≤ n≤0.5 (D
2/ d)
2.) mutual relationship.
[embodiment 2]
Same process cephalo azoles beautiful jade class antibiotic production wastewater, treatment process is with [embodiment 1], and treatment capacity requires to reach 10m
3/ h.The overall length of whole suction mixing reactor is 2.6m, mixing section diameter 125mm, built-in corrugated filler, and valid circulation area is 50%.The length ratio of suction chamber section 4, expansion section 5 and mixing section 2 is 1: 3: 15, fluid inlet conduit 3 diameter 40mm, the internal diameter of suction chamber section 4 is 125mm, and ratio between two is 40:125=3, sucking logistics pipeline 6 diameter is 15mm, is 15: 125=1: 8.3 with the internal diameter ratio of suction chamber section 4.
The position that fluid distributor 7 gos deep into suction chamber section 4 is 1/3 of suction chamber section 4 internal diameter.The semisphere hollow cavity 72 of fluid distributor 7 is provided with n=60 circular hole, the diameter of circular hole is d=3mm, the central axis of semisphere hollow cavity 72 and angle theta=135 ° of fluid flow direction.The diameter D of feed-pipe 71
1=15mm, the diameter D of semisphere hollow cavity 72
2=40mm, meets D
1/d
2≤ 0.5 and (D
1/ d)
2≤ n≤0.5 (D
2/ d)
2.) mutual relationship.
Waste water is 4.8s from suction casing to the discharging section whole residence time, can reach and mix effect.Whole device is per hour can Continuous Wastewater Treatment amount 10m
3, mixing section inner fluid speed is 0.45m/s.
[embodiment 3]
Process waste water classification and technique are with example 1,2, and treatment capacity is increased to 20m
3/ h.The overall length of whole suction mixing reactor is 2.6m, mixing section diameter 200mm, built-in corrugated filler, and valid circulation area is 50%.The length ratio of suction chamber section 4, expansion section 5 and mixing section 2 is 1: 4: 21, fluid inlet conduit 3 diameter 50mm, the internal diameter of suction chamber section 4 is 200mm, and ratio between two is 4, sucking logistics pipeline 6 diameter is 20mm, is 20: 200=1: 10 with the internal diameter ratio of suction chamber section 4.
The position that fluid distributor 7 gos deep into suction chamber section 4 is 1/2 of suction chamber section 4 internal diameter.The semisphere hollow cavity 72 of fluid distributor 7 is provided with n=60 circular hole, the diameter of circular hole is d=4mm, the central axis of semisphere hollow cavity 72 and angle theta=120 ° of fluid flow direction.The diameter D of feed-pipe 71
1=20mm, the diameter D of semisphere hollow cavity 72
2=50mm, meets D
1/d
2≤ 0.5 and (D
1/ d)
2≤ n≤0.5 (D
2/ d)
2.) mutual relationship.
Mixing section inner fluid speed is about 0.4m/s, and waste water is 6.5s from suction casing to the discharging section whole residence time, can reach and mix effect.Whole device is per hour can Continuous Wastewater Treatment 20m
3.
[comparative example 1]
The common Venturi tube of direct employing (not being with subsequent pipeline mixing tank), waste water sends into Venturi tube through force (forcing) pump, and sodium hydroxide lye is mixed with waste water after being inhaled into by Venturi effect.Because Venturi tube only plays material suction function, the pH of actual measurement discharging liquid presents fluctuation situation, illustrates that mixed effect is not good, so must increase a mixing tank, the pH value of mixed solution is stablized and after meeting the requirements through being uniformly mixed, then deliver to waste water processing station and carry out biochemical treatment.Due to waste liquid need mixing in-tank mixing, so whole process cannot complete continuously.
[comparative example 2]
Adopt the auto-suction pipe mixing reactor of [embodiment 3], process per hour to be satisfied waste water 20m containing head
3.Because the end sucking logistics pipeline 6 does not arrange fluid distributor.Think the abundant mixing reaching fluid, need increase liquid mixing time to more than 20s guarantee outlet liquid pH value be stabilized in more than 13.Now the length ratio of suction casing, expansion section and mixing section need reach 1: 4: 75, and the material pH of discharge end just can be made to be stabilized in preset value.Thus reach the effect of abundant hybrid reaction.Because length of mixing increases, equipment is taken up an area and investment also corresponding increase.
Claims (7)
1. a cephalosporins drug manufacture pretreatment method for wastewater, comprises the following steps:
A) provide auto-suction pipe mixing reactor, described auto-suction pipe mixing reactor comprises suction casing (1) and mixing section (2) successively along fluid flow direction; Suction casing (1) comprises fluid inlet conduit (3), suction chamber section (4) and expansion section (5); Fluid inlet conduit (3) stretches in suction chamber section (4), and end-contraction is conical; The tube wall of suction chamber section (4) is provided with and sucks logistics pipeline (6), suck logistics pipeline (6) end goed deep in suction chamber section (4) and be provided with fluid distributor (7); Mixing section (2) tube wall is provided with flow apron; Along fluid flow direction, the dead in line of fluid inlet conduit (3), suction chamber section (4), expansion section (5) and mixing section (2);
B) factory effluent containing cephalosporins medicine enters auto-suction pipe mixing reactor from fluid inlet conduit (3), and degraded medicine enters auto-suction pipe mixing reactor from suction logistics pipeline (6); Described waste water and degraded medicine mix, react in auto-suction pipe mixing reactor;
C) ratio control device of wastewater flow, degraded drug flux is set, and automatic pH meter is set in auto-suction pipe mixing reactor exit, by the pH value of monitoring outlet reaction solution, control the degraded medicine liquid measure added, after outlet effluent stream keeps pH >=13, drain into follow-up waste water processing station and carry out biochemical treatment;
Containing cephalosporins medicine factory effluent with degraded medicine weight ratio be (5:1) ~ (50:1);
Described degraded medicine be weight percentage concentration be 2 ~ 5% NaOH solution;
Described cephalosporins medicine is selected from cephalo azoles beautiful jade, Cephradine, cefoperazone or ceftriaxone.
2. cephalosporins drug manufacture pretreatment method for wastewater according to claim 1, is characterized in that the length of the suction chamber section (4) of described auto-suction pipe mixing reactor, expansion section (5) and mixing section (2) than being 1:(2 ~ 4): (10 ~ 20).
3. cephalosporins drug manufacture pretreatment method for wastewater according to claim 1, is characterized in that the position that described fluid distributor (7) gos deep into suction chamber section (4) is 1/4 ~ 1/2 of suction chamber section (4) internal diameter.
4. cephalosporins drug manufacture pretreatment method for wastewater according to claim 1, it is characterized in that described fluid distributor (7) comprises the semisphere hollow cavity (72) of feed-pipe (71) and its end, (72) are provided with at least one circular hole to semisphere hollow cavity; Wherein, angle theta=120 ° ~ 135 ° of the central axis of semisphere hollow cavity (72) and fluid flow direction.
5. cephalosporins drug manufacture pretreatment method for wastewater according to claim 4, is characterized in that the diameter D of feed-pipe (71)
1with the diameter D of semisphere hollow cavity (72)
2meet D
1/ D
2≤ 0.5, semisphere hollow cavity (72) the above quantity n of circular hole and the diameter d of circular hole meets (D
1/ d)
2≤ n≤0.5 (D
2/ d)
2.
6. cephalosporins drug manufacture pretreatment method for wastewater according to claim 5, is characterized in that diameter d=1 ~ 4 millimeter of the upper circular hole of semisphere hollow cavity (72).
7. cephalosporins drug manufacture pretreatment method for wastewater according to claim 6, is characterized in that diameter d=2 ~ 3 millimeter of the upper circular hole of semisphere hollow cavity (72).
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| US5037616A (en) * | 1987-10-14 | 1991-08-06 | Compagnie De Raffinage Et De Distribution Total France | Device for injection of a hydrocarbon feedstock into a catalytic cracking reactor |
| CN1095695A (en) * | 1993-05-27 | 1994-11-30 | 中国纺织大学 | The biochemical treatment of antibiotic waste water |
| CN101157510A (en) * | 2007-09-19 | 2008-04-09 | 北京盖雅环境科技有限公司 | Process for treating antibiotic waste water and usage thereof |
| CN103706319A (en) * | 2012-10-08 | 2014-04-09 | 中国石油化工集团公司 | Self-suction pipeline mixing reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5037616A (en) * | 1987-10-14 | 1991-08-06 | Compagnie De Raffinage Et De Distribution Total France | Device for injection of a hydrocarbon feedstock into a catalytic cracking reactor |
| CN1095695A (en) * | 1993-05-27 | 1994-11-30 | 中国纺织大学 | The biochemical treatment of antibiotic waste water |
| CN101157510A (en) * | 2007-09-19 | 2008-04-09 | 北京盖雅环境科技有限公司 | Process for treating antibiotic waste water and usage thereof |
| CN103706319A (en) * | 2012-10-08 | 2014-04-09 | 中国石油化工集团公司 | Self-suction pipeline mixing reactor |
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