CN104016539B - The treatment process of production of raw medicine waste water - Google Patents
The treatment process of production of raw medicine waste water Download PDFInfo
- Publication number
- CN104016539B CN104016539B CN201310066457.8A CN201310066457A CN104016539B CN 104016539 B CN104016539 B CN 104016539B CN 201310066457 A CN201310066457 A CN 201310066457A CN 104016539 B CN104016539 B CN 104016539B
- Authority
- CN
- China
- Prior art keywords
- waste water
- production
- raw medicine
- suction
- auto
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention relates to a kind for the treatment of process of production of raw medicine waste water, mainly solving prior art, to there is the periodical operation time long, and equipment volume is large, and personal protection is poor, easily causes secondary pollution, human metering out of true, processes the problem that 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, control end reaction liquid pH >=13 or pH≤1, 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 production of raw medicine wastewater treatment.
Description
Technical field
The present invention relates to a kind for the treatment of process of production of raw medicine waste water.
Background technology
Bulk drug, English name Active Pharmaceutical Ingredients, be called for short API, be a kind of activeconstituents of medicine, it is prepared by methods such as chemosynthesis, plant extract, biotechnologies, and its finished product is then for the raw material of pharmaceutical preparation.Due to various chemical and inflammable and explosive solvent can be used in production of raw medicine process, and some biologically active substances, the certain active by product of some tools and intermediate etc. can be produced in preparation process, so the production process of whole bulk drug has certain danger and hazardness to environment and human body simultaneously.As in bulk drug itraconazole preparation process, intermediate hydroxyl thing and first semi-annular jade pendant acyl ester carry out association reaction at toluene, water, sodium hydroxide under existing, and reaction terminates rear upper organic phase and enters next step crystallizing and drying as reaction product and obtain itraconazole crude product.And the aqueous phase layer that reaction produces contains a large amount of first semi-annular jade pendant acyl esters and Residual Toluene etc., have chemical toxicity, it is disposed to three-protection design station and is carried out subsequent disposal as waste reaction solution.And for example cephalosporin analog antibiotic product cefazolin is received the parent nucleus of bulk drug and is produced, and 7-ACA raw material and thiadiazoles, Glacial acetic acid, ethyl acetate, lays particular stress on sodium sulphite etc. and carries out salt-forming reaction, then through centrifugal, filter, wash after obtain cefazolin parent nucleus.The waste liquid that this process produces, containing organic solvent and active Kefzol composition, must carry out follow-up process.In addition production of raw medicine terminate after equipment washing and the lower water of place cleaning, also containing certain pharmaceutical cpd, these waste liquids also must be collected and be processed.
The waste water of current production of raw medicine 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, respectively by the acting in conjunction of anaerobion and aerobic microbiological, with the organic pollutant in degrading waste water, waste water is purified.
The waste water produced due to production of raw medicine process contains certain chemical toxicity and biological activity, the particularly factory effluent of some microbiotic bulk drug, microbiotic (as penicillin, cynnematin etc.) contained by it has the effect of stronger killing microorganisms, the anaerobic and aerobic microorganism needed for biochemical treatment can be made to lose efficacy, do not reach the object of wastewater treatment.In addition due to the high sensitization of these materials, as environmental pollution produced without degradation treatment, there is threat to there being the crowd of allergic constitution.As residued in animals and plants, also can enter human body by food chain and health is had a negative impact.
These active and toxicants in waste water, the method by chemistry and physics is degraded, to reduce and to eliminate its toxicity/activity.A kind of comparatively conventional method is acid-alkali treatment method.Because chemical toxicity/biologically active substance is the organism/protein of macromole backbone, under the effect of strong acid/highly basic, organic long-chain macromolecular structure can be cut off and degrade, and its activity/toxicity have also been obtained alleviation/elimination like this.Therefore by regulating the method for the pH value of waste water, changing and eliminating its toxicity and activity.
But, traditional chemical degradation method, the process adding hydrochloric acid and 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 soda acid, 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) degradation solution 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, and equipment volume is large, and 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 for the treatment of process of new production of raw medicine waste water.The method can process production of raw medicine waste water continuously and can immediately degrade, and ensure that the safe and effective controlled of wastewater treatment process.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind for the treatment of process of production of raw medicine waste water, comprises the following steps:
A) production of raw medicine waste water and degraded reagent enter auto-suction pipe mixing reactor, mix, react in described reactor;
B) described auto-suction pipe mixing reactor ingress is provided with the ratio control device of bulk drug wastewater flow, degraded reagent flow, auto-suction pipe mixing reactor exit arranges automatic pH meter, by the pH value of monitoring outlet reaction solution, control the degraded reagent liquid measure added, after outlet effluent stream keeps pH >=13 or pH≤1, drain into follow-up waste water processing station and carry out biochemical treatment;
C) wherein, 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.
In technique scheme, production of raw medicine waste water is (5: 1) ~ (50: 1) with the weight ratio preferable range of degraded reagent.Production of raw medicine waste water enters auto-suction pipe mixing reactor from fluid inlet conduit 3, and degraded reagent enters auto-suction pipe mixing reactor from suction logistics pipeline 6.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.Different according to the characteristic of handled material, one of selected degraded reagent be weight percentage concentration be 2 ~ 5% NaOH solution, after auto-suction pipe mixing reactor outlet material keeps pH >=13, drain into follow-up waste water processing station and carry out biochemical treatment.Two of selected degraded reagent be weight percentage concentration be 1 ~ 4% HCl solution, after auto-suction pipe mixing reactor outlet material keeps pH≤1, drain into follow-up waste water processing station and carry out biochemical treatment.
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 (Giovanni Battista Venturi).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 bulk drug produce negative pressure by Venturi tube, reagent 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 reagent 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 maximum physical length 50% reducing mixing tank, facilitates the installation of mixing tank, reduces 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, production of raw medicine waste water and degraded reagent are completed mixing by certain proportioning automatically, and mix fully in pipeline reactor, react, eventually through the judgement of reaction end pH value, automatic stopping hybrid reaction process, completes 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 production of raw medicine waste water streams, and 9 is the logistics of degraded reagent, and 10 is reacted logistics, and 12 is waste water basin, and 13 is degraded reagent 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 reagent 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 production of raw medicine waste water enters reactor suction casing 1 from fluid inlet conduit 3, and reagent of suction logistics 9 being degraded sucks from suction logistics pipeline 6.Due to the dissemination of fluid distributor, the streams of degraded reagent 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 degraded reagent flow in pipes 6, reactor outlet mixed solution 10 is made to remain at pH >=13 or pH≤1, 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]
Waste liquid run by gravity containing endoxan kind anti-cancer drugs thing is disposed to waste collection tank, be furnished with after this holding tank one therewith tank liquid level interlock transferpump, waste liquid is delivered to mixing reactor.Line-blending reactor is provided with degraded reagent 2% hydrochloric acid liquid storage tank, corrosion resisting centrifugal pump and ratio adjusting valve, and by being arranged on the pH detection instrument of line-blending reactor discharge port, the pH value of detection reaction liquid, by the open degree regulating hydrochloric acid to add the ratio adjusting valve on pipeline, make reactor outlet mixed solution remain at pH≤1, degrading to make endoxan loses toxicity.Enter follow-up wastewater treatment equipment again, biochemical treatment rear discharge up to standard.
Wherein, the overall length of whole self-priming 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: 16, 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.
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.
The flow velocity of pending waste water in mixing section is 0.2m/s, and waste water is only 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 2.8m
3/ h.
[embodiment 2]
The major ingredient of irinotecan hydrochloride medicines is U 101440E, chemistry (+)-(4S)-4 by name, 11-diethyl-4-hydroxyl-9-(4-sends pyridine base to send pyridine) carbonyl-1H-pyrans 3,4:6,7 indolizine 1,2b quinoline-3,14-(4H, 12H)-dione hydrochloride trihydrate, is mainly used in treating Colorectal cancer metastasis.Production process can produce the washes of a large amount of hydrochloric irinotecan cancer therapy drug composition.Adopt the auto-suction pipe mixing reactor of [embodiment 1], the waste water of hydrochloric irinotecan is disposed to waste collection tank by run by gravity, is furnished with the transferpump of a tank liquid level interlock therewith, waste liquid is delivered to mixing reactor after this holding tank.Line-blending reactor is provided with 4% sodium hydroxide liquid basin of degradation compound, corrosion resisting centrifugal pump and ratio adjusting valve, and 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, make reactor outlet mixed solution remain at pH >=13, degrading to make endoxan loses toxicity.Enter follow-up wastewater treatment equipment again, discharge after biochemical treatment is up to standard.
In this example, self-priming mixing reactor overall length is 2.6m, mixing section diameter 100mm, built-in corrugated filler, valid circulation area 50%.The length ratio of suction chamber section 4, expansion section 5 and mixing section 2 is 1:2:10.Fluid inlet conduit 3 diameter 25mm is 25:100=1:4 with the ratio of the internal diameter of suction chamber section 4, and inhalation pipe material 6 diameter 15mm is 15:100=1:6.7. with suction chamber section diameter ratio
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=2mm, 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.
Complete assembly processing power is 5m
3/ h, wherein the flow velocity of fluid in mixing section is 0.4m/s, and the residence time is 5s.
[embodiment 3]
Material handling is with [embodiment 2], and waste treatment capacity increases, and requires to reach 15m
3/ h.The overall length of whole suction mixing reactor is 3.6m, and mixing section diameter is amplified to 150mm, 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: 20, fluid inlet conduit 3 diameter 40mm, the internal diameter of suction chamber section 4 is 150mm, and ratio between two is 40:150=1: 3.75, sucking logistics pipeline 6 diameter is 25mm, is 1: 6 with the internal diameter ratio of suction chamber section 4.
The position that fluid distributor 7 gos deep into suction chamber section 4 is 1/4 of suction chamber section 4 internal diameter.The semisphere hollow cavity 72 of fluid distributor 7 is provided with n=70 circular hole, the diameter of circular hole is d=4mm, the central axis of semisphere hollow cavity 72 and angle theta=135 ° 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.
Waste water is 6s 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 15m
3, mixing section inner fluid speed is 0.5m/s.
[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 hydrochloric acid 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 1], the end just sucking logistics pipeline 6 does not arrange fluid distributor.Think the abundant mixing reaching fluid, to need to increase in mixing tank residence time of material fully to react.In this example, after tested, the residence time needs this to increase to 20s, and the length ratio of corresponding suction casing, expansion section and mixing section need reach 1: 3: 36, and wherein length of mixing increases to 3.6m by 1.6m, 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 adds more than 2 times, so equipment takes up an area and investment also corresponding raising.
Claims (7)
1. a treatment process for production of raw medicine waste water, comprises the following steps:
A) production of raw medicine waste water and degraded reagent enter auto-suction pipe mixing reactor, mix, react in described reactor;
B) described auto-suction pipe mixing reactor ingress is provided with the ratio control device of bulk drug wastewater flow, degraded reagent flow, auto-suction pipe mixing reactor exit arranges automatic pH meter, by the pH value of monitoring outlet reaction solution, control the degraded reagent liquid measure added, after outlet effluent stream keeps pH >=13 or pH≤1, drain into follow-up waste water processing station and carry out biochemical treatment;
C) wherein, 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);
Production of raw medicine waste water is (5:1) ~ (50:1) with the weight ratio of degraded reagent;
Described degraded reagent be weight percentage concentration be 2 ~ 5% NaOH solution, when auto-suction pipe mixing reactor outlet effluent stream keeps behind pH >=13, drain into follow-up waste water processing station and carry out biochemical treatment;
Described degraded reagent be weight percentage concentration be 1 ~ 4% HCl solution, when auto-suction pipe mixing reactor outlet effluent stream keeps behind pH≤1, drain into follow-up waste water processing station and carry out biochemical treatment.
2. the treatment process of production of raw medicine waste water according to claim 1, it is characterized in that production of raw medicine waste water enters auto-suction pipe mixing reactor from fluid inlet conduit (3), degraded reagent enters auto-suction pipe mixing reactor from suction logistics pipeline (6).
3. the treatment process of production of raw medicine waste water 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); 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. the treatment process of production of raw medicine waste water 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. the treatment process of production of raw medicine waste water 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. the treatment process of production of raw medicine waste water according to claim 5, is characterized in that diameter d=1 ~ 4 millimeter of the upper circular hole of semisphere hollow cavity (72).
7. the treatment process of production of raw medicine waste water according to claim 6, is characterized in that diameter d=2 ~ 3 millimeter of the upper circular hole of semisphere hollow cavity (72).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310066457.8A CN104016539B (en) | 2013-03-01 | 2013-03-01 | The treatment process of production of raw medicine waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310066457.8A CN104016539B (en) | 2013-03-01 | 2013-03-01 | The treatment process of production of raw medicine waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104016539A CN104016539A (en) | 2014-09-03 |
| CN104016539B true CN104016539B (en) | 2015-10-21 |
Family
ID=51433599
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310066457.8A Active CN104016539B (en) | 2013-03-01 | 2013-03-01 | The treatment process of production of raw medicine waste water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104016539B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107020007A (en) * | 2017-06-05 | 2017-08-08 | 成都绿水科技有限公司 | A kind of economic benefits and social benefits reaction of high order type desulfurization slurry oxidization processing system and technique |
| CN114436428A (en) * | 2021-10-26 | 2022-05-06 | 武汉天空蓝环保科技有限公司 | Integrated wastewater treatment system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1095695A (en) * | 1993-05-27 | 1994-11-30 | 中国纺织大学 | The biochemical treatment of antibiotic waste water |
| US5525239A (en) * | 1993-07-20 | 1996-06-11 | Duske Design & Equipment Co., Inc. | Method for completing the transformation of waste water sludge into spreadable fertilizer and product thereby |
| CN201543393U (en) * | 2009-08-19 | 2010-08-11 | 黄剑亭 | Static pipe mixer device |
| WO2011112199A8 (en) * | 2010-03-12 | 2011-10-27 | Exxonmobil Chemical Patents Inc. | Polyethylene manufacturing system and method |
| CN102441332A (en) * | 2011-10-10 | 2012-05-09 | 浙江省海洋开发研究院 | Static mixer for pipeline |
| CN103706319A (en) * | 2012-10-08 | 2014-04-09 | 中国石油化工集团公司 | Self-suction pipeline mixing reactor |
-
2013
- 2013-03-01 CN CN201310066457.8A patent/CN104016539B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1095695A (en) * | 1993-05-27 | 1994-11-30 | 中国纺织大学 | The biochemical treatment of antibiotic waste water |
| US5525239A (en) * | 1993-07-20 | 1996-06-11 | Duske Design & Equipment Co., Inc. | Method for completing the transformation of waste water sludge into spreadable fertilizer and product thereby |
| CN201543393U (en) * | 2009-08-19 | 2010-08-11 | 黄剑亭 | Static pipe mixer device |
| WO2011112199A8 (en) * | 2010-03-12 | 2011-10-27 | Exxonmobil Chemical Patents Inc. | Polyethylene manufacturing system and method |
| CN102441332A (en) * | 2011-10-10 | 2012-05-09 | 浙江省海洋开发研究院 | Static mixer for pipeline |
| CN103706319A (en) * | 2012-10-08 | 2014-04-09 | 中国石油化工集团公司 | Self-suction pipeline mixing reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104016539A (en) | 2014-09-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103706319B (en) | Auto-suction pipe mixing reactor | |
| CN104016539B (en) | The treatment process of production of raw medicine waste water | |
| CN209292136U (en) | A kind of sewage disposal device of veterinary drug fermenting and producing | |
| CN209034138U (en) | A kind of pipeline mixer | |
| CN208275360U (en) | A kind of device for the treatment of reaction pond center addition medicament high-speed stirred | |
| CN209934498U (en) | Diffusion device for accelerating dissolution of medicament | |
| CN205023987U (en) | Take sewage treatment plant in charge device and flocculation air supporting pond | |
| CN209668848U (en) | A kind of sewage treatment eddy flow mixing medicine system | |
| CN104016468B (en) | Cephalosporins drug manufacture pretreatment method for wastewater | |
| CN202170264U (en) | Solid catalyst Fenton reaction unit | |
| CN203139932U (en) | Automatic dosing device for sewage treatment | |
| CN109052820A (en) | A kind of substation's sewage treatment Zero emission device | |
| CN202236475U (en) | Disinfectant dosage and supply system | |
| CN210646164U (en) | Solid medicament dissolves and throws integrated device with | |
| CN205974169U (en) | Coking wastewater nitrate nitrogen removing device | |
| CN208115673U (en) | A kind of novel bubble medicine machine | |
| CN203513336U (en) | Pharmaceutical wastewater treatment equipment | |
| CN202785879U (en) | Laboratory wastewater treatment system | |
| CN213112961U (en) | Advanced oxidation-biological coupling reactor | |
| CN207986773U (en) | A kind of dystopy emergency processing reaction system for sudden water pollution accident | |
| CN213326791U (en) | Automatic chemical adding equipment matched with mine water treatment equipment | |
| CN215277042U (en) | Carbon source charge device for wastewater treatment | |
| CN215196698U (en) | Novel three-cavity full-automatic dosing device | |
| CN217230542U (en) | Self-adaptive mixing device for sludge conditioning | |
| CN107758873A (en) | The pharmaceutical intermediate wastewater cleaning system of microbial reproduction can be promoted |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |