CN105000734A - Pharmaceutical wastewater treating system and method - Google Patents
Pharmaceutical wastewater treating system and method Download PDFInfo
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- CN105000734A CN105000734A CN201510339732.8A CN201510339732A CN105000734A CN 105000734 A CN105000734 A CN 105000734A CN 201510339732 A CN201510339732 A CN 201510339732A CN 105000734 A CN105000734 A CN 105000734A
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Abstract
The invention provides a pharmaceutical wastewater treating system, and relates to the field of environmental protection. The pharmaceutical wastewater treating system comprises a mixing tank, a settling tank, a multi-stage electrolytic tank, a multi-stage Fenton phase tank, a first heater, a first evaporator, a second heater, a second evaporator, a third heater, a third evaporator, a gas-liquid separator and an intermediate tank. The mixing tank is communicated with the settling tank, the multi-stage electrolytic tank is connected with the multi-stage Fenton phase tank, the multi-stage Fenton phase tank is connected with the first heater, the first evaporator is communicated with the second heater, the second evaporator is communicated with the third heater, the third evaporator is connected with the gas-liquid separator, the intermediate tank is connected with the multi-stage Fenton phase tank, and the intermediate tank is connected with a third circulation pipe through a vacuum pipe. The pharmaceutical wastewater treating system is high in waste treatment efficiency, the pollution index of treated waste water is greatly reduced, and the content of organics and the content of hazardous substance are obviously reduced. The invention further provides a treating method.
Description
Technical field
The present invention relates to field of Environment Protection, especially relate to a kind of pharmacy wastewater treatment system and method.
Background technology
Along with the development of modern medicine technology and synthesis medicine industry, chemical pharmacy waste water has become one of serious source of pollution.Pharmaceutical industry is one of 12 industries of keypoint treatment in national environmental protection planning.According to statistics, pharmaceutical industry accounts for 1.7% of national gross industrial output value, and quantity of wastewater effluent accounts for 2%.Because chemical composition is various in style, in pharmaceutical manufacturing process, employ plurality of raw materials, the compositions such as complex manufacturing is changeable, the waste water of generation are also very complicated.This has manufactured a difficult problem just to current environment protection.
Through research, organic content high, complicated component, the especially organism of chemical pharmacy waste water in chemical pharmacy waste water, have up to several ten thousand even hundreds of thousands of, waste water, once entering in water body, will consume oxygen in water in a large number, cause water hypoxia.
Microorganism processes chemical pharmacy waste water in prior art many employings, but the salt concentration in waste water is too high has obvious restraining effect to microorganism, when chlorion is more than 3000mg/L, activity without acclimated microorganism will obviously be suppressed, have a strong impact on the efficiency of wastewater treatment, even cause sludge bulking, the phenomenon of microbial death, and be difficult to degraded containing microorganisms such as cyanogen, phenol or aromatic amine, nitrogen heterocyclic and polycyclic aromatic compounds in waste water, even have inhibiting material to microorganism, microbiological treatment waste water efficiency is low.
Summary of the invention
In view of this, the invention provides a kind of pharmacy wastewater treatment system and method, with improve prior art carry out wastewater treatment time, easily cause water hypoxia, and the problem that processing efficiency is low.
For achieving the above object, the invention provides following technical scheme:
A kind of pharmacy wastewater treatment system, comprise mixing pit, settling tank, multistage electrolyzer, multistage Fenton stage pond, primary heater, the first vaporizer, secondary heater, the second vaporizer, the 3rd well heater, the 3rd vaporizer, gas-liquid separator and tundish, described mixing pit is communicated with described settling tank, described multistage electrolyzer is connected with described multistage Fenton stage pond, and described multistage Fenton stage pond is connected with described primary heater, described primary heater is communicated with the first circulation tube respectively by the first feed-pipe with the first vaporizer, first vaporizer is communicated with described secondary heater, secondary heater is communicated with the second circulation tube respectively by the second feed-pipe with the second vaporizer, described second vaporizer is communicated with described 3rd well heater, 3rd well heater is communicated with the 3rd circulation tube respectively by the 3rd feed-pipe with the 3rd vaporizer, described 3rd vaporizer is connected with described gas-liquid separator, described relay tank is connected with described multistage Fenton stage pond, described relay tank is connected with described 3rd circulation tube by valve tube.
Preferably, in above-mentioned pharmacy wastewater treatment system, described pharmacy wastewater treatment system also comprises neutralization tank, and described neutralization tank is communicated with described gas-liquid separator.
Preferably, in above-mentioned pharmacy wastewater treatment system, described pharmacy wastewater treatment system also comprises filtering basin, is provided with multi-stage activated carbon filtration structure layer in described filtering basin.
Preferably, in above-mentioned pharmacy wastewater treatment system, described first vaporizer, the second vaporizer are communicated with condensation water respectively by Clean water valve with the top of the 3rd vaporizer.
Preferably, in above-mentioned pharmacy wastewater treatment system, described pharmacy wastewater treatment system also comprises condenser, and described 3rd vaporizer is connected with described condenser, and described condenser is connected with described gas-liquid separator.
Present invention also offers a kind of method processing above-mentioned pharmacy waste water, comprise the steps:
A., in mixing pit, add dilute sulphuric acid and make the pH value of waste water be 3 ~ 4, retention time of sewage is 2 ~ 6h, then passes into settling tank;
B. in settling tank, add coagulating agent 300 ~ 500mg/L, retention time of sewage 4 ~ 6h, flocculation sediment is carried out to the colloid in waste water and fine suspension, then passes into electrolyzer;
C. in electrolyzer, adopt iron-carbon micro-electrolysis filler to degrade under electrochemical action partial organic substances, retention time of sewage 0.5 ~ 1h, remove water pollutant, toxic substance is become nontoxic, low toxicity material, pass into multistage Fenton stage pond;
D. add hydrogen peroxide in multistage Fenton stage pond, adding concentration is 120 ~ 200mg/L, and retention time of sewage is 1 ~ 2h, utilizes electrochemical reaction degradation of organic substances, then passes in tundish;
E. the liquid entered in tundish sucks the 3rd vaporizer by vacuum and evaporates; When the vacuum tightness of the 3rd evaporator system reaches-0.04Mpa, open the 3rd evaporation feed liquor valve, when material liquid surface reaches the 3rd vaporizer more than height 80cm, start the 3rd discharging pump and the 3rd discharge valve and carry out self-circulation and to the second evaporation feed liquor;
F., when material liquid surface reaches the second vaporizer more than height 80cm in the second vaporizer, start the second discharging pump and the second bleeder valve and carry out self-circulation and to the first evaporation feed liquor;
G. the 3rd evaporation feed liquor valve and the second bleeder valve and the 3rd bleeder valve is closed when the first vaporizer, the second vaporizer, the 3rd vaporizer material liquid surface all reach 90cm;
H. slowly open primary heater steam inlet valve and start heating, when the first evaporator temperature reaches 90 ~ 100 DEG C, when vacuum tightness is 0, open the first circulation tube, the steam of the first vaporizer enters the thermal source of secondary heater as secondary heater for heating the material in the second vapo(u)rization system;
I. when temperature of charge in the second vaporizer is raised to 90 ~ 100 DEG C, when vacuum tightness is 0, the second forced circulation pump is opened; The gas evaporated in second vapo(u)rization system enters the thermal source of the 3rd well heater as the 3rd well heater for heating the material in the 3rd vapo(u)rization system, when in the 3rd vaporizer, temperature of charge is raised to 60 ~ 70 DEG C, when vacuum tightness is 0, open the 3rd forced circulation pump, the steam in the 3rd vaporizer becomes liquid collecting in steam-water separation tank through condenser condenses;
J. when the 3rd vaporizer, when dropping to below 80cm after the liquid surface evaporation in the second vaporizer and the first vaporizer, material is added to three vaporizers, make liquid level at 90 ~ 100cm, continue evaporation, get solution in the first vaporizer in evaporative process and survey degree Beaume, when degree Beaume is less than 15, survey the degree Beaume of solution in first vaporizer per half an hour, when degree Beaume higher than 17 time, interval 20min surveys the degree Beaume of solution in first vaporizer, until when in the first vaporizer, the degree Beaume of solution is 20, first vaporizer middle and high concentration material is being passed into detritus pool crystallization, complete the 3rd vapo(u)rization system and complete a work period,
K. the 3rd vapo(u)rization system carries out the wastewater treatment cycle by the operation steps of step e ~ j repetition the 3rd vapo(u)rization system after completing a work period.
Relative to prior art, pharmacy wastewater treatment system and method provided by the invention comprises following beneficial effect: pharmacy wastewater treatment system provided by the invention utilizes through mixing pit, settling tank, multistage electrolyzer, multistage Fenton stage pond, primary heater, first vaporizer, secondary heater, second vaporizer, 3rd well heater, 3rd vaporizer, gas-liquid separator and tundish carry out filtration treatment and evaporation process step by step, waste water treatment efficiency is high, contaminated wastewater index simultaneously after process reduces greatly, the content of organic content and objectionable impurities obviously reduces.
Accompanying drawing explanation
In order to the clearer explanation embodiment of the present invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in embodiment or description of the prior art below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the structural representation of the pharmacy wastewater treatment system that first embodiment of the invention provides.
Wherein, the corresponding relation between Reference numeral and component names is as follows: mixing pit 101, settling tank 102, multistage electrolyzer 103, multistage Fenton stage pond 104, primary heater 105, first vaporizer 106, secondary heater 107, the second vaporizer 108,3rd well heater the 109, three vaporizer 110, gas-liquid separator 111, tundish 112, neutralization tank 113, filtering basin 114, Clean water valve 115, condenser 116.
Embodiment
Also by reference to the accompanying drawings the present invention is described in further detail below by specific embodiment.
In the present invention, first, second, third, etc. are difference signal, are not limit.
Fig. 1 is the structural representation of the pharmacy wastewater treatment system that first embodiment of the invention provides.As shown in Figure 1, the pharmacy wastewater treatment system and method that first embodiment of the invention provides comprises mixing pit 101, settling tank 102, multistage electrolyzer 103, multistage Fenton stage pond 104, primary heater 105, first vaporizer 106, secondary heater 107, second vaporizer 108, the 3rd well heater 109, the 3rd vaporizer 110, gas-liquid separator 111 and tundish 112.
Mixing pit 101 is communicated with settling tank 102, and multistage electrolyzer 103 is connected with multistage Fenton stage pond 104, and multistage Fenton stage pond 104 is connected with primary heater 105, primary heater 105 be communicated with the first circulation tube respectively by the first feed-pipe with the first vaporizer 106, first vaporizer 106 is communicated with secondary heater 107, secondary heater 107 is communicated with the second circulation tube respectively by the second feed-pipe with the second vaporizer 108, second vaporizer 108 is communicated with the 3rd well heater 109, 3rd well heater 109 is communicated with the 3rd circulation tube respectively by the 3rd feed-pipe with the 3rd vaporizer 110, 3rd vaporizer 110 is connected with gas-liquid separator 111, relay tank is connected with multistage Fenton stage pond 104, relay tank is connected with the 3rd circulation tube by valve tube.First circulation tube, the second circulation tube and the 3rd circulation tube being all provided with corresponding forced circulation pump, carrying out circulating-heating for making primary heater 105, first vaporizer 106, secondary heater 107, second vaporizer 108, the 3rd well heater 109, the 3rd vaporizer 110.
First pharmacy waste water mixes with water in interior mixing pit 101, the pH value of balanced water quality, ensure the continuous operation of follow-up waste water processes, then be passed in settling tank 102, under the effect of the coagulating agent in settling tank 102, suspended solids in waste water and partial organic substances settle down, then waste water is passed in multistage electrolyzer 103, in multistage electrolyzer 103, take waste water as ionogen, cell reaction and throwing out are carried out to waste water, by pollutent component generation redox reactions many in active ion and waste water, macromolecular substance is made to be decomposed into small-molecule substance, or make the mass transfer of some bio-refractory become easy to handle material, improve the biodegradability of waste water, then waste water is passed in multistage Fenton stage pond 104, organic pollutant in further removing waste water, then waste water is transferred to primary heater 105 by tundish 112, first vaporizer 106, secondary heater 107, second vaporizer 108, 3rd well heater 109, 3rd vaporizer 110 carries out multi source heating distillation, primary heater 105, first vaporizer 106, secondary heater 107, second vaporizer 108, 3rd well heater 109, 3rd vaporizer 110 complete assembly is that vacuum is run in closed system, heating efficiency is high, multiple stage circulation evaporates, good to the organism distilling effect in waste water, without efflux gas, simultaneously waste water is through repeatedly circulation time, water of condensation also returns not outer row in production process as process water, environmental pollution is little to external world, save energy, running cost is low.
In the present embodiment, pharmacy wastewater treatment system also comprises neutralization tank 113 and filtering basin 114.Neutralization tank 113 is communicated with gas-liquid separator 111, in neutralization tank 113, adding calcium hydroxide regulates PH to neutral, the iron ion before produced in technique also can form colloidal precipitation in this stage, the effect of further raising pharmacy wastewater treatment, reduce the inorganic salt in pharmacy waste water, reduce pharmacy waste water to the pollution of environment.
On the other hand, after filtering basin 114 are arranged on neutralization tank 113, filtering basin 114 are connected with neutralization tank 113, multi-stage activated carbon filtration structure layer is provided with in filtering basin 114, fine material in charcoal absorption waste water in filtering basin 114, waste water is carried out to the heavy metal in decoloration and deodorization, removal waste water, synthetic detergent, bacterium and virus, reduce pharmacy waste water further to the pollution of environment.
Further, the first vaporizer 106, second vaporizer 108 is communicated with condensation water respectively by Clean water valve 115 with the top of the 3rd vaporizer 110 in the present embodiment.Back flushing can be carried out when system shutdown to the first vaporizer 106, second vaporizer 108 and the 3rd vaporizer 110 by Clean water valve 115, be convenient to safeguard the first vaporizer 106, second vaporizer 108 and the 3rd vaporizer 110 and clean.
Condenser 116 is also comprised in the pharmacy wastewater treatment system that the present embodiment provides, 3rd vaporizer 110 is connected with condenser 116, condenser 116 is connected with gas-liquid separator 111, condenser 116 was set before gas-liquid separator 111, be convenient to cool from the 3rd vaporizer 110 hot gas out, the heat of these hot gas is utilized simultaneously, improve the separation efficiency of gas-liquid separator 111, and then improve the efficiency of Pharmaceutical Wastewater Treatment.
Present invention also offers a kind of method processing above-mentioned pharmacy waste water:
A., in mixing pit 101, add dilute sulphuric acid and make the PH of waste water be 3 ~ 4, retention time of sewage is 2 ~ 6h, then passes into settling tank 102;
B. in settling tank 102, add coagulating agent 300 ~ 500mg/L, retention time of sewage 4 ~ 6h, flocculation sediment is carried out to the colloid in waste water and fine suspension, then passes into electrolyzer;
C., in multistage electrolyzer 103, adopt iron-carbon micro-electrolysis filler to degrade under electrochemical action partial organic substances, retention time of sewage 0.5 ~ 1h, remove water pollutant, toxic substance is become nontoxic, low toxicity material.
In multistage electrolyzer 103, be provided with filler, filler adopts irony and carbonaceous, and under the condition of weak acid environment, waste water becomes ionogen, and microbattery reaction and flocculation reaction occur.Microbattery reaction product has very high chemically reactive, at anode, produces ferrous ion; At negative electrode, produce active [H], all can with most pollutent component generation redox reaction in waste water, make the mass transfer of some bio-refractory become easy to handle material, improve the biodegradability of waste water.
D. the waste water after multistage electrolyzer 103 contains a large amount of ferrous ions, iron ion active colloidal flocculation agent, these materials enter in multistage Fenton stage pond 104 together with waste water, oxygenant is added in multistage Fenton stage pond 104, catalyzer, produce the free radical that a large amount of oxidation capacity is extremely strong, by organic molecule oxygenolysis, change its chemical structure, can about 50% be removed to the organism in waste water, hydrogen peroxide is added in multistage Fenton stage pond 104, adding concentration is 120 ~ 200mg/L, retention time of sewage is 1 ~ 2h, utilize electrochemical reaction degradation of organic substances, then pass in tundish 112,
E. the liquid entered in tundish 112 sucks the 3rd vaporizer 110 by vacuum and evaporates; When the vacuum tightness of the 3rd vaporizer 110 system reaches-0.04Mpa, open the 3rd vaporizer 110 feed valve, when material liquid surface reaches the 3rd vaporizer 110 height more than 80cm, start the 3rd discharging pump and the 3rd discharge valve and carry out self-circulation and to the second vaporizer 108 charging;
F., when material liquid surface in the second vaporizer 108 reaches the second vaporizer 108 height more than 80cm, start the second discharging pump and the second bleeder valve and carry out self-circulation and to the first vaporizer 106 charging;
G. the 3rd vaporizer 110 feed valve and the second bleeder valve and the 3rd bleeder valve is closed when the first vaporizer 106, second vaporizer 108, the 3rd vaporizer 110 material liquid surface all reach 90cm;
H. slowly open primary heater 105 steam inlet valve and start heating, when the first vaporizer 106 temperature reaches 90 ~ 100 DEG C, when vacuum tightness is 0, open the first circulation tube, the steam of the first vaporizer 106 enters the thermal source of secondary heater 107 as secondary heater 107 for heating the material in the second vapo(u)rization system;
I. when temperature of charge in the second vaporizer 108 is raised to 90 ~ 100 DEG C, when vacuum tightness is 0, the second forced circulation pump is opened; The gas evaporated in second vapo(u)rization system enters the thermal source of the 3rd well heater 109 as the 3rd well heater 109 for heating the material in the 3rd vapo(u)rization system, when in the 3rd vaporizer 110, temperature of charge is raised to 60 ~ 70 DEG C, when vacuum tightness is 0, open the 3rd forced circulation pump, the steam in the 3rd vaporizer 110 is condensed into liquid collecting in steam-water separation tank through condenser 116;
J. when the 3rd vaporizer 110, when dropping to below 80cm after the liquid surface evaporation in the second vaporizer 108 and the first vaporizer 106, material is added to three vaporizers, make liquid level at 90 ~ 100cm, continue evaporation, get solution in the first vaporizer 106 in evaporative process and survey degree Beaume, when degree Beaume is less than 15, survey the degree Beaume of solution in first vaporizer 106 per half an hour, when degree Beaume higher than 17 time, interval 20min surveys the degree Beaume of solution in first vaporizer 106, until when in the first vaporizer 106, the degree Beaume of solution is 20, first vaporizer 106 middle and high concentration material is being passed into detritus pool crystallization, complete the 3rd vapo(u)rization system and complete a work period,
K. the 3rd vapo(u)rization system carries out the wastewater treatment cycle by the operation steps of step e ~ j repetition the 3rd vapo(u)rization system after completing a work period.
After the above step, can also carry out the waste water of S11 output and neutralize, adding calcium hydroxide regulates PH to neutral, produce colloidal precipitation in waste water just can precipitate, gac can also utilized to filter afterwards, fine material in charcoal absorption waste water, carries out the heavy metal in decoloration and deodorization, removal waste water, synthetic detergent, bacterium and virus, reduces pharmacy waste water further to the pollution of environment to waste water.
The waste water of pharmacy wastewater treatment method to county, Aba state of Sichuan province pharmaceutical factory output that theres is provided of the present embodiment is adopted to carry out treatment effect through test good.The per day generation of county, Aba state of Sichuan province pharmaceutical factory 100 ~ 150 tons of waste water, when the method provided not adopting the present embodiment carries out wastewater treatment, per day treatment capacity is 120 ~ 200 tons, waste water after treatment, after testing, result meets substantially " pharmaceutical industry pollution discharge standard ", but wherein COD(chemical oxygen demand (COD)) still trace over standard, exceed standard 0.002% ~ 0.004%, and adopt after present method processes, although capital improvement takes certain cost, but, after transformation, the method utilizing the present embodiment to provide carries out wastewater treatment, per day treatment capacity improves 20%, the indices of the waste water after process is detected, detected result is as following table,
Index after detection meets ISO14001 certification and EHS(environment, safety, Occupational health series) index of authentication requesting, water treatment effect comparatively before ordinary student pond method process after stain index declines 43%, treatment effect is splendid, and processing efficiency improves, and processing cost compares decline 12%.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (6)
1. a pharmacy wastewater treatment system, it is characterized in that: comprise mixing pit, settling tank, multistage electrolyzer, multistage Fenton stage pond, primary heater, the first vaporizer, secondary heater, the second vaporizer, the 3rd well heater, the 3rd vaporizer, gas-liquid separator and tundish, described mixing pit is communicated with described settling tank, described multistage electrolyzer is connected with described multistage Fenton stage pond, and described multistage Fenton stage pond is connected with described primary heater, described primary heater is communicated with the first circulation tube respectively by the first feed-pipe with the first vaporizer, first vaporizer is communicated with described secondary heater, secondary heater is communicated with the second circulation tube respectively by the second feed-pipe with the second vaporizer, described second vaporizer is communicated with described 3rd well heater, 3rd well heater is communicated with the 3rd circulation tube respectively by the 3rd feed-pipe with the 3rd vaporizer, described 3rd vaporizer is connected with described gas-liquid separator, described relay tank is connected with described multistage Fenton stage pond, described relay tank is connected with described 3rd circulation tube by valve tube.
2. pharmacy wastewater treatment system according to claim 1, is characterized in that: described pharmacy wastewater treatment system also comprises neutralization tank, and described neutralization tank is communicated with described gas-liquid separator.
3. pharmacy wastewater treatment system according to claim 1, is characterized in that: described pharmacy wastewater treatment system also comprises filtering basin, is provided with multi-stage activated carbon filtration structure layer in described filtering basin.
4. pharmacy wastewater treatment system according to claim 1, is characterized in that: described first vaporizer, the second vaporizer are communicated with condensation water respectively by Clean water valve with the top of the 3rd vaporizer.
5. pharmacy wastewater treatment system according to claim 1, is characterized in that: described pharmacy wastewater treatment system also comprises condenser, and described 3rd vaporizer is connected with described condenser, and described condenser is connected with described gas-liquid separator.
6. process a method for the pharmacy waste water described in any one of claim 1 ~ 5, it is characterized in that, comprise the steps:
A., in mixing pit, add dilute sulphuric acid and make the pH value of waste water be 3 ~ 4, retention time of sewage is 2 ~ 6h, then passes into settling tank;
B. in settling tank, add coagulating agent 300 ~ 500mg/L, retention time of sewage 4 ~ 6h, flocculation sediment is carried out to the colloid in waste water and fine suspension, then passes into electrolyzer;
C. in electrolyzer, adopt iron-carbon micro-electrolysis filler to degrade under electrochemical action partial organic substances, retention time of sewage 0.5 ~ 1h, remove water pollutant, toxic substance is become nontoxic, low toxicity material, pass into multistage Fenton stage pond;
D. add hydrogen peroxide in multistage Fenton stage pond, adding concentration is 120 ~ 200mg/L, and retention time of sewage is 1 ~ 2h, utilizes electrochemical reaction degradation of organic substances, then passes in tundish;
E. the liquid entered in tundish sucks the 3rd vaporizer by vacuum and evaporates; When the vacuum tightness of the 3rd evaporator system reaches-0.04Mpa, open the 3rd evaporation feed liquor valve, when material liquid surface reaches the 3rd vaporizer more than height 80cm, start the 3rd discharging pump and the 3rd discharge valve and carry out self-circulation and to the second evaporation feed liquor;
F., when material liquid surface reaches the second vaporizer more than height 80cm in the second vaporizer, start the second discharging pump and the second bleeder valve and carry out self-circulation and to the first evaporation feed liquor;
G. the 3rd evaporation feed liquor valve and the second bleeder valve and the 3rd bleeder valve is closed when the first vaporizer, the second vaporizer, the 3rd vaporizer material liquid surface all reach 90cm;
H. slowly open primary heater steam inlet valve and start heating, when the first evaporator temperature reaches 90 ~ 100 DEG C, when vacuum tightness is 0, open the first circulation tube, the steam of the first vaporizer enters the thermal source of secondary heater as secondary heater for heating the material in the second vapo(u)rization system;
I. when temperature of charge in the second vaporizer is raised to 90 ~ 100 DEG C, when vacuum tightness is 0, the second forced circulation pump is opened; The gas evaporated in second vapo(u)rization system enters the thermal source of the 3rd well heater as the 3rd well heater for heating the material in the 3rd vapo(u)rization system, when in the 3rd vaporizer, temperature of charge is raised to 60 ~ 70 DEG C, when vacuum tightness is 0, open the 3rd forced circulation pump, the steam in the 3rd vaporizer becomes liquid collecting in steam-water separation tank through condenser condenses;
J. when the 3rd vaporizer, when dropping to below 80cm after the liquid surface evaporation in the second vaporizer and the first vaporizer, material is added to three vaporizers, make liquid level at 90 ~ 100cm, continue evaporation, get solution in the first vaporizer in evaporative process and survey degree Beaume, when degree Beaume is less than 15, survey the degree Beaume of solution in first vaporizer per half an hour, when degree Beaume higher than 17 time, interval 20min surveys the degree Beaume of solution in first vaporizer, until when in the first vaporizer, the degree Beaume of solution is 20, first vaporizer middle and high concentration material is being passed into detritus pool crystallization, complete the 3rd vapo(u)rization system and complete a work period,
K. the 3rd vapo(u)rization system carries out the wastewater treatment cycle by the operation steps of step e ~ j repetition the 3rd vapo(u)rization system after completing a work period.
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105366863A (en) * | 2015-11-24 | 2016-03-02 | 山东东岳氟硅材料有限公司 | High-efficient eco-friendly processing method for reducing COD in sewage |
| CN105923869A (en) * | 2016-05-03 | 2016-09-07 | 安徽南风环境工程技术有限公司 | Pretreatment method for chemical industry wastewater |
| CN107265738A (en) * | 2017-08-15 | 2017-10-20 | 广州市勃发环境科技有限公司 | Pharmacy wastewater treatment system and processing method |
| CN108249647A (en) * | 2018-03-23 | 2018-07-06 | 中山大学 | Laboratory wastewater treatment technology |
| CN110066077A (en) * | 2019-06-11 | 2019-07-30 | 泉州南京大学环保产业研究院 | A kind of processing method of cymoxanil agricultural chemicals waste water |
| CN110902978A (en) * | 2019-12-27 | 2020-03-24 | 苏州苏沃特环境科技有限公司 | Method and device for treating high-salt-content high-organic-matter chemical wastewater |
| CN111646625A (en) * | 2020-06-19 | 2020-09-11 | 见嘉环境科技（苏州）有限公司 | Water treatment device adopting multistage electrocatalysis evaporation and application method |
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2015
- 2015-06-18 CN CN201510339732.8A patent/CN105000734A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105366863A (en) * | 2015-11-24 | 2016-03-02 | 山东东岳氟硅材料有限公司 | High-efficient eco-friendly processing method for reducing COD in sewage |
| CN105366863B (en) * | 2015-11-24 | 2018-06-05 | 山东东岳氟硅材料有限公司 | The processing method of COD in a kind of reduction sewage |
| CN105923869A (en) * | 2016-05-03 | 2016-09-07 | 安徽南风环境工程技术有限公司 | Pretreatment method for chemical industry wastewater |
| CN107265738A (en) * | 2017-08-15 | 2017-10-20 | 广州市勃发环境科技有限公司 | Pharmacy wastewater treatment system and processing method |
| CN108249647A (en) * | 2018-03-23 | 2018-07-06 | 中山大学 | Laboratory wastewater treatment technology |
| CN110066077A (en) * | 2019-06-11 | 2019-07-30 | 泉州南京大学环保产业研究院 | A kind of processing method of cymoxanil agricultural chemicals waste water |
| CN110902978A (en) * | 2019-12-27 | 2020-03-24 | 苏州苏沃特环境科技有限公司 | Method and device for treating high-salt-content high-organic-matter chemical wastewater |
| CN110902978B (en) * | 2019-12-27 | 2023-09-26 | 苏州苏沃特环境科技股份有限公司 | Method and device for treating high-salt-content high-organic chemical wastewater |
| CN111646625A (en) * | 2020-06-19 | 2020-09-11 | 见嘉环境科技（苏州）有限公司 | Water treatment device adopting multistage electrocatalysis evaporation and application method |
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Application publication date: 20151028 |