CN1012358B - Method of treating penicillin waste water - Google Patents
Method of treating penicillin waste waterInfo
- Publication number
- CN1012358B CN1012358B CN88107206A CN88107206A CN1012358B CN 1012358 B CN1012358 B CN 1012358B CN 88107206 A CN88107206 A CN 88107206A CN 88107206 A CN88107206 A CN 88107206A CN 1012358 B CN1012358 B CN 1012358B
- Authority
- CN
- China
- Prior art keywords
- waste water
- add
- biochemical
- treating
- flocculation separation
- 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.)
- Expired
Links
Classifications
-
- Y02W10/12—
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The present invention relates to a method for treating penicillin waste water, particularly to a method for treating penicillin waste water comprising a poisonous demulsifying agent. The method for treating penicillin waste water comprising a poisonous demulsifying agent comprises the following steps: the waste water is treated by flocculating separation and precipitating desulphurization before biochemical treatment, and the toxicity of the demulsifying agent and other biochemical inhibition objects in the waste water can be separated and removed; the waste water is purified by a high-efficiency reluctance biochemical treatment system, an aerobic biochemical treatment system and a flocculating dewatering system of sewage sludge. Compared with the prior art for treating the penicillin waste water, the present invention saves motive power, appliance investment and operation cost. Simultaneously, the present invention does not need a great amount of water for diluting in the process of the treatment of the waste water, and the present invention can provide much methane energy source.
Description
The present invention relates to a kind of treatment process of waste water produced from penicillin production.
At present, the treatment process to waste water produced from penicillin production has three kinds.The first, with waste water doubly, make in the waste water after the diluted elimination of the influence of contained biochemical inhibitor through dilution 10-20, carry out biochemical aerobic treatment again.This treatment process need consume a large amount of water and power, and processing cost is too high.The second, do not add dilution and directly carry out the pressurized aeration biochemical treatment.The 3rd, adopt anaerobic biological-5 times-aerobic biochemical of water dilution to handle.The two kinds of treatment processs in back are subjected to use in the penicillin production technology restriction of broken floating agent kind, and most penicillin production factory can not be suitable for.
The objective of the invention is at above-mentioned the deficiencies in the prior art part, and provide a kind of simple, save power and cost, and be applicable to the treatment process of the penicillin wastewater that contains any emulsion splitter.
The present invention is achieved in that
According to the characteristic of various biochemical inhibitors in the penicillin wastewater, add specific medicament inhibition is separated, and then waste water is purified with the anaerobic and aerobic biochemical processing process.
1. the separation of inhibition:
It comprises flocculation separation and desulfurization precipitation.
A. flocculation separation:
The temperature of control waste water is 30-60 ℃, adds inorganic flocculating agent and macromolecule organic flocculating agent in waste water, makes macromole class and colloidal type inhibition in the waste water generate dehydration property floss preferably, makes its separation by air supporting or precipitation means.
B. precipitate desulfurization:
Add the soluble barium salt in the supernatant liquor after flocculation separation, make that the sulfur-bearing inhibition obtains precipitate and separate in the waste water.
Inorganic flocculating agent can be selected any in the following kind for use in flocculation separation:
(1) ferrous sulfate+lime adding amount 200-400ppm
(2) phosphoric acid+lime 100-300ppm
(3) aluminium chlorohydroxide 100-200ppm
(4) polymerization ferrous sulfate 100-300ppm
Above-mentioned lime consumption is 7-9 for the pH value of control waste water,
Macromolecule organic flocculating agent can be selected any in the following kind for use:
Polyacrylamide consumption 1.5-5ppm
Sodium polyacrylate 2-10ppm
In the precipitation desulfurization, can add BaC
12Crystal, its add-on are controlled at and make SO in the precipitation clear liquid
Two 4Concentration is below 1500ppm.
2. biochemical treatment:
Waste water through having removed biochemical inhibitor makes in the waste water organism be degraded significantly by an efficient anaerobic digestive organ.In anaerobic digestion process, the organism that is not degraded is 4-6 hour aerobic biochemical treatment system and mud separation system again by a hydraulic detention time, makes waste water reach the purpose of purification.The biogas that generates at anaerobic digestion process is made for fuel through a desulfurizer after the purification.
The invention will be further described below in conjunction with drawings and Examples:
Fig. 1 is a process flow diagram of the present invention.
Process explanation following (referring to Fig. 1):
1. flocculation separation:
Refine the waste liquid that workshop waste water distillation tower is discharged by mould, through plate-type heat exchanger with advance tower cold burden heat exchange cooling after enter waste water basin 1, further lower the temperature naturally, the waste water of getting temperature and be 30-60 ℃ is to flocculation separation groove 3.If the water temperature in the waste water basin 1 is lower than 30 ℃, after being heated to 30-60 ℃, waste water heater via 2 enters again in the flocculation separation groove 3.Under fully stirring, use Ca(OH)
2The pH value of control waste water is 7-9.Accurately add FeSO
4: 200-400ppm and macromolecule organic flocculating agent polyacrylamide 1.5-5ppm.(deciding) according to the waste water situation.Slowly stir back waste water neutrality and carve the alumen ustum that now flocculates in a large number.After treating flocculation sediment, supernatant liquor introduced in the settling bath 6 take off SO
Two 4Handle.
2. precipitation is taken off SO
Two 4:
Under agitation, slowly add a certain amount of BaCl
2Crystal.Ba salt carries out conversion reaction rapidly, after dosing finishes, and a large amount of deposit B aSO
4Separate out, treat turbid solution clarification after, throw supernatant liquor into water quality regulation jar 8 by clear liquid pump 7, as anaerobic biological liquid.Deposit B aSO
4Squeeze into barium mud storage tank 4 with barium dredge pump 5.Prepare washing, reclaim after decolouring is handled and pay product B aSO
4
3. anaerobic digestion:
Penicillin wastewater after flocculation, precipitate and separate enters anaerobic mud bed reactor 11 by the Flow-rate adjustment control of being made up of biochemistry water inlet test tank 9 and spinner-type flowmeter 10 from the bottom.Reactor 11 temperature are controlled at 38-40 ℃.The biogas that produces in the digestive process is collected in biogas basin 17 then through water seal 12 behind gas flow meter 16.The digestion water outlet is advanced next procedure and is handled after test tank 13 meterings.
4. aerobic biochemical:
Its COD value of waste water of being come out by anaeroic digestor 11 is still about 1500mg/l, and needing to go out water measuring tank 13 through anaerobic biological, to enter 14 cycles of carrying out of aerobe aerating apparatus again be 4-6 hour bio-aeration, and the organism in the waste water obtains degree of depth degraded.The suspended substance that is being mingled with some active sludge from the waste water that aerobic biochemical device 14 comes out makes its separation by adding the polymer organic floculant once more at flocculation separator 15, separates the back supernatant liquor and can discharge.
Another embodiment is basic identical with embodiment shown in Figure 1, and is as follows with Fig. 1 difference:
1. not to adopt precipitate and separate in the flocculation separation process, but adopt dissolved air flotation.
2. not to adopt anaerobic sludge reactor at anaerobic digestion process, but adopt anaerobic sludge digester.It comprises an anaerobic mud bed reactor and two anaerobic biological strainers.
3. not to adopt the bio-aeration device in the aerobic biochemical treating processes, but adopt aerobic biofilter.
Adopt the present invention better to waste water produced from penicillin production treatment and purification effect, the total clearance of COD reaches 97.6%, BOD
5Total clearance reaches 99%.
Anaerobic digestion process wherein:
COD clearance: 86.15%
BOD
5Clearance: 97%
COD volumetric loading: 6.1kg/m
3Day
Water outlet COD:1500-2000mg/l
Water outlet BOD
5: 190-279mg/l
Aerobic biochemical and mud sepn process:
COD clearance: 41-57%
BOD
5Clearance:＞80%
Aerobic biochemical hydraulic detention time: 4-6 hour
Mud separates hydraulic detention time: 2 hours
Water outlet COD:450-608mg/l
Water outlet BOD
5:＜40mg/l
Flocculation-precipitation SO among the present invention
Two 4Better to penicillin wastewater mesophytization inhibition separation removal effect, the waste water after inhibition separates does not need a large amount of water dilutions just can carry out biochemical treatment.Therefore, power and facility investment and running cost have been saved.And more biogas can be provided, and the present invention is suitable for the improvement of the penicillin wastewater that contains any emulsion splitter.
Claims (5)
1, a kind of biochemical processing method of penicillin wastewater, it is characterized in that before biochemical treatment, waste water being carried out flocculation separation and precipitating the desulfurization processing, at first adding inorganic flocculating agent and macromolecule organic flocculating agent carry out flocculation separation in waste water, add the soluble barium salt then in the supernatant liquor after flocculation separation and precipitate desulfurization.
2, method according to claim 1 is characterized in that when flocculation separation is handled, and the temperature of control waste water is 30-60 ℃, behind the adding flocculation agent, by air supporting or precipitation means floss is separated.
3, method according to claim 2 is characterized in that:
A. inorganic flocculating agent is selected in the following kind any for use in flocculation separation:
(1) ferrous sulfate+lime adding amount 200-400ppm
(2) phosphoric acid+lime adding amount 100-300ppm
(3) aluminium chlorohydroxide add-on 100-200ppm
(4) polymerization ferrous sulfate add-on 100-300ppm
Above-mentioned lime consumption separates sub-organic floculant and selects in the following kind any for use for the pH value of control waste water is 7-9:
Polyacrylamide consumption 1.5-5ppm
Sodium polyacrylate consumption 2-10ppm
B. precipitate and add the BaCl2 crystal in the desulfurization, its add-on is controlled at and makes in the precipitation clear liquid SO4 concentration below 1500ppm.
4, method according to claim 1 is characterized in that the anaerobic digestion process in biochemical processing process adopts anaerobic mud bed reactor, perhaps adopts anaerobic sludge digester.
5, method according to claim 1 is characterized in that the aerobic biochemical treating processes in biochemical processing process adopts the bio-aeration device, perhaps adopts aerobic biofilter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN88107206A CN1012358B (en) | 1988-10-15 | 1988-10-15 | Method of treating penicillin waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN88107206A CN1012358B (en) | 1988-10-15 | 1988-10-15 | Method of treating penicillin waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1041927A CN1041927A (en) | 1990-05-09 |
| CN1012358B true CN1012358B (en) | 1991-04-17 |
Family
ID=4834561
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN88107206A Expired CN1012358B (en) | 1988-10-15 | 1988-10-15 | Method of treating penicillin waste water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1012358B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103146762B (en) * | 2013-03-22 | 2015-05-20 | 河北华药环境保护研究所有限公司 | Treatment method of penicillin mushroom dregs |
| CN108653971B (en) * | 2018-03-27 | 2021-03-09 | 上海化工研究院有限公司 | Method for removing residual penicillin antibiotics in biological medicine waste residues |
| CN108314156A (en) * | 2018-03-27 | 2018-07-24 | 宁夏宝塔化工中心实验室(有限公司) | A kind of thick waste liquid solid-liquid separating agent and preparation method thereof |
-
1988
- 1988-10-15 CN CN88107206A patent/CN1012358B/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| CN1041927A (en) | 1990-05-09 |
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