CN204310915U - Laboratory waste liquid treatment unit - Google Patents
Laboratory waste liquid treatment unit Download PDFInfo
- Publication number
- CN204310915U CN204310915U CN201420717359.6U CN201420717359U CN204310915U CN 204310915 U CN204310915 U CN 204310915U CN 201420717359 U CN201420717359 U CN 201420717359U CN 204310915 U CN204310915 U CN 204310915U
- Authority
- CN
- China
- Prior art keywords
- baf
- reactor
- outlet
- waste
- explosive box
- 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.)
- Withdrawn - After Issue
Links
Abstract
The utility model relates to a kind of laboratory waste liquid treatment unit in pollution control equipment field, and it comprises the classification of multiple waste liquid storage tank, oxidation-reduction reactor, mixing pit, pH regulator groove, micro-electrolysis reactor, reactor for hydrolysis and acidification, DN BAF, C/N BAF, inclined-plate clarifying basin, sludge thickener, multiple explosive box and chamber-type press filter; The medicament of the spent acid solution collected as treatment unit uses, with adjust ph by this device; Waste liquid classification carries out pre-treatment through oxidation-reduction reactor, adopts materialization and biochemical treatment apparatus to remove water pollutant further, discharge after up to standard again after then being mixed; Mud is disposed by regulation after adopting dewatering unit process to form mud cake.This device can process high density laboratory waste liquid, and construction investment is economized, and floor space is little, convenient operation and management.Can effectively remove COD, ammonia nitrogen, phosphorus and heavy metal, average removal rate reaches more than 99.5%.
Description
Technical field
The utility model relates to a kind of prevention and cure of pollution device, particularly a kind of device for the treatment of lab waste liquid.
Background technology
Laboratory waste liquid is mainly from scientific research and the school duty room of each R&D institution's experimental study room and institution of higher learning.Waste liquid can be divided into high density laboratory waste liquid and lower concentration laboratory waste water by pollution level.High density laboratory waste liquid main component is liquid failed reagent (useless washing lotion, useless potassium cyanide, spent organic solvent etc.), liquid experiment waste products or intermediate product (as various organic solvent, centrifugate, liquid by-product etc.) and various washings (the high density washings of product or intermediate product, instrument or the rinse liquid of vessel and the washes etc. of high density).Lower concentration laboratory waste water refers to the concentration of discharging in experimentation and the lower experimental water of toxicity, generally comprise the washes using large water gaging to clean experimental ware and experimental product, the useless test solution that toxicity is little, concentration is low, and the water being used as cooling, heating use.In the laboratory waste liquid formed, COD, ammonia nitrogen, phosphorus, mercury and chromium equal size are higher.
Although the waste liquid total amount that laboratory produces every year is fewer, but belong to high toxicity, complicated components and unmanageable environmental pollutant, middle-size and small-size laboratory waste liquid output is few, and generation time is indefinite, adopts traditional technique for treating industrial wastewater to be difficult to obtain ideal treatment effect.At present, laboratory waste liquid major part all adopts directly discharge or concentrated dilution discharge, severe contamination environment.Utilization burning-catalytic oxidation technique the new technology of recent report, first by these pollutent predecomposition in the container of temperature-controllable, then make it to transform into carbonic acid gas, water and corresponding inorganics by efficient catalyticreactor, thus realize the harmless treatment of laboratory waste liquid.But it is high that this type for the treatment of technology exists processing costs, combustion tail gas is difficult to the problems such as effectively process.
Utility model content
For overcoming the deficiencies in the prior art, the utility model provides a kind of laboratory waste liquid treatment unit, efficiently can remove the pollutent in waste liquid, to meet the requirement of qualified discharge.
The purpose of this utility model is achieved in that a kind of laboratory waste liquid treatment unit, comprises the classification of multiple waste liquid storage tank, oxidation-reduction reactor, mixing pit, pH regulator groove, micro-electrolysis reactor, reactor for hydrolysis and acidification, DN BAF, C/N BAF, inclined-plate clarifying basin, sludge thickener, multiple explosive box and chamber-type press filter; Described waste liquid classification storage tank comprises spent acid solution storage tank, organic liquid waste storage tank, mercury system waste tank, sexavalent chrome waste tank, heavy metal waste tank and cyanide bearing waste solution storage tank; Described explosive box comprises calcium hydroxide explosive box, sodium hydroxide explosive box, polyacrylamide explosive box, polymerize aluminum chloride explosive box, ferrous sulfate explosive box, hydrogen peroxide explosive box, acid solution explosive box, chlorine bleach liquor's explosive box and sodium sulphite explosive box; The outlet of described organic liquid waste storage tank, mercury system waste tank, sexavalent chrome waste tank, heavy metal waste tank, cyanide bearing waste solution storage tank is connected to oxidation-reduction reactor through transportation by lighter pump respectively; Spent acid solution outlet is connected to acid solution explosive box; Each explosive box outlet is also connected to the import of oxidation-reduction reactor respectively through volume pump; Outlet one road bottom oxidation-reduction reactor is connected to mixing pit, and another road is connected to sludge thickener; Described pH regulator groove comprises pH regulator groove A and pH regulator groove B; PH regulator groove A is connected with the outlet of acid solution explosive box, and pH regulator groove B is connected with the outlet of sodium hydroxide explosive box; The outlet of mixing pit is connected to the lower inlet of pH regulator groove A through sump pump, the top water outlet of pH regulator groove A is connected to the import of micro-electrolysis reactor, the outlet of micro-electrolysis reactor is connected to the bottom inlet of pH regulator groove B, the top water outlet of pH regulator groove B is connected to the import of vertical-flow settling vessel, the water outlet on vertical-flow settling vessel top is connected to the import of tilted plate separator, and the water outlet of tilted plate separator is connected to the import of reactor for hydrolysis and acidification; The water outlet of reactor for hydrolysis and acidification is connected to the import of DN BAF, and the water outlet of DN BAF connects the import as C/N BAF, and the outlet of C/N BAF connects discharge tube; Sludge outlet bottom described vertical-flow settling vessel, tilted plate separator and reactor for hydrolysis and acidification is connected to sludge thickener through valve; Described sludge thickener apical supernatant fluid outlet is connected to mixing pit, and the outlet of sludge thickener base sludge is connected to chamber-type press filter through sludge pump, and the filtrate outlet of chamber-type press filter is connected to mixing pit; Be respectively equipped with aeration tube in described micro-electrolysis reactor, DN BAF and C/N BAF, described aeration tube is connected with blower fan.
Compared with prior art, tool has the following advantages the utility model:
(1) for the process of high density laboratory waste liquid, general employing combination treatment technique, or adopt incineration treatment technology, be difficult to meet the requirement of environmental protection.The utility model adopts same reactor gap pre-treatment remix successively of classifying to carry out Physiochemical and biochemical treatment process, can realize the qualified discharge of liquid waste disposal completely, and construction investment is economized, and floor space is little, convenient operation and management.
(2) oxidation-reduction reactor, mixing pit, water pump, apparatus for physical Chemical treating, biochemical treatment apparatus, chemicals dosing plant, chamber-type press filter, gas blower, settling vessel spoil disposal etc. all adopt computer program to control, achieve the accurate control of reaction conditions and treating processes, ensure that the waste water quality index after process reaches emission standard, greatly reduce the labour intensity of operating process simultaneously.
(3) device adopts modular design, has stronger combined, open and extensibility.Increase waste liquid kind, only need increase the handling procedure of storing device and oxidation-reduction reactor, other device is then without the need to changing.
(4) the utility model process high density laboratory waste liquid Be very effective, COD, ammonia nitrogen average removal rate reach more than 90%, and total phosphorus average removal rate reaches more than 99%, and the average removal rate of the heavy metal such as mercury and total chromium reaches more than 99.5%.The utility model is applicable to the sorted comprehensive treating process of high density laboratory waste liquid.
For ensureing that control is reliable, convenient, described oxidation-reduction reactor is provided with supersonic liquid level controller, pH controller, ORP controller, frequency conversion agitator motor, with the stir shaft of agitating vane and tachogenerator, output shaft and the stir shaft of frequency conversion agitator motor are in transmission connection.
For ensureing that corresponding biological filter can non-stop run, described DN BAF and C/N BAF are connected to Backwash pipeline, the backwashing water outlet of DN BAF and C/N BAF is connected to sludge thickener.
Be as further improvement of the utility model, described C/N BAF top is connected to the import of DN BAF through reflux pump.
Further improvement of the utility model is, described reactor for hydrolysis and acidification is connected with self-circulating pump and corresponding self-circulation pipeline.
What the utility model was preferred is in the filler loaded in described reactor for hydrolysis and acidification is half soft biologic packing material; Filling ceramic grain filter in DN BAF, C/N BAF, and dissolved oxygen monitor 1 is set respectively overlaps.
Accompanying drawing explanation
Fig. 1 is laboratory waste liquid processing technological flow figure of the present utility model.
Fig. 2, Fig. 3 are the partial enlarged drawing of Fig. 1.
In figure: 1 spent acid solution storage tank; 1P spent acid liquid pump; 2 organic liquid waste storage tanks; 2P organic waste liquid pump; 3 mercury system waste tank; 3P mercury system waste drains pump; 4 sexavalent chrome waste tank; 4P sexavalent chrome waste drains pump; 5 heavy metal waste tank; 5P heavy metal waste drains pump; 6 cyanide bearing waste solution storage tanks; 6P cyanide bearing waste solution pump; 7 oxidation-reduction reactors; 8 mixing pits; 9 sump pumps; 10pH regulating tank A; 11 micro-electrolysis reactors; 12 pH regulator groove B; 13 vertical-flow settling vessels; 14 tilted plate separators; 15 reactor for hydrolysis and acidification; 15P self-circulating pump; 16 DN BAF; 17 C/N BAF; 18 sludge thickeners; 19 spiral pumps; 20 chamber-type press filters; 21 sodium sulphite explosive boxs; 21P sodium sulphite volume pump; 22 calcium hydroxide explosive boxs; 22P calcium hydroxide volume pump; 23 hydrogen peroxide explosive boxs; 23P hydrogen peroxide volume pump; 24 sodium hydroxide explosive boxs; 24A, 24B sodium hydroxide volume pump; 25 acid solution explosive boxs; 25A, 25B acid solution volume pump; 26 chlorine bleach liquor's explosive boxs; 26P chlorine bleach liquor volume pump; 27 ferrous sulfate explosive boxs; 27P ferrous sulfate volume pump; 28 polymerize aluminum chloride explosive boxs; 28A, 28B polymerize aluminum chloride volume pump; 29 polyacrylamide explosive boxs; 29A, 29B polyacrylamide volume pump; 30A, 30B blower fan.
Embodiment
As Figure 1-3, this device comprises waste liquid classification storage tank, oxidation-reduction reactor 7, mixing pit 8, pH regulator groove, micro-electrolysis reactor 11, reactor for hydrolysis and acidification 15, DN BAF 16, C/N BAF 17, inclined-plate clarifying basin, sludge thickener 18, multiple explosive box and chamber-type press filter 20; Waste liquid classification storage tank has multiple, is respectively spent acid solution storage tank 1, organic liquid waste storage tank 2, mercury system waste tank 3, sexavalent chrome waste tank 4, heavy metal waste tank 5 and cyanide bearing waste solution storage tank 6; Described explosive box comprises calcium hydroxide explosive box 22, sodium hydroxide explosive box 24, polyacrylamide explosive box 29, polymerize aluminum chloride explosive box 28, ferrous sulfate explosive box 27, hydrogen peroxide explosive box 23, acid solution explosive box 25, chlorine bleach liquor's explosive box 26 and sodium sulphite explosive box 21; The outlet of organic liquid waste storage tank 2, mercury system waste tank 3, sexavalent chrome waste tank 4, heavy metal waste tank 5, cyanide bearing waste solution storage tank 6 is connected to oxidation-reduction reactor 7 through transportation by lighter pump respectively; Spent acid solution storage tank 1 outlet is connected to acid solution explosive box 25; Each explosive box outlet is also connected to the import of oxidation-reduction reactor 7 respectively through volume pump; Outlet one road bottom oxidation-reduction reactor 7 is connected to mixing pit 8, and another road is connected to sludge thickener 18; PH regulator groove has two, is respectively pH regulator groove A10 and pH regulator groove B12; PH regulator groove A10 is connected with the outlet of acid solution explosive box 25, and pH regulator groove B12 is connected with the outlet of sodium hydroxide explosive box 24; The outlet of mixing pit 8 is connected to the lower inlet of pH regulator groove A10 through sump pump 9, the top water outlet of pH regulator groove A10 is connected to the import of micro-electrolysis reactor 11, the outlet of micro-electrolysis reactor 11 is connected to the bottom inlet of pH regulator groove B12, the top water outlet of pH regulator groove B12 is connected to the import of vertical-flow settling vessel 13, the water outlet on vertical-flow settling vessel 13 top is connected to the import of tilted plate separator 14, and the water outlet of tilted plate separator 14 is connected to the import of reactor for hydrolysis and acidification 15; The water outlet of reactor for hydrolysis and acidification 15 is connected to the import of DN BAF 16, and the water outlet of DN BAF 16 connects the import as C/N BAF 17, and the outlet of C/N BAF 17 connects discharge tube; Sludge outlet bottom described vertical-flow settling vessel 13, tilted plate separator 14 and reactor for hydrolysis and acidification 15 is connected to sludge thickener 18 through valve; The outlet of sludge thickener 18 apical supernatant fluid is connected to mixing pit 8, and the outlet of sludge thickener 18 base sludge is connected to chamber-type press filter 20 through sludge pump, and the filtrate outlet of chamber-type press filter 20 is connected to mixing pit 8; Be respectively equipped with aeration tube in micro-electrolysis reactor 11, DN BAF 16 and C/N BAF 17, aeration tube is connected respectively with blower fan 30A with 30B.
Oxidation-reduction reactor 7 is provided with supersonic liquid level controller, pH controller, ORP controller, frequency conversion agitator motor, with the stir shaft of agitating vane and tachogenerator, output shaft and the stir shaft of frequency conversion agitator motor are in transmission connection.DN BAF 16 and C/N BAF 17 are connected to Backwash pipeline, and the backwashing water outlet of DN BAF 16 and C/N BAF 17 is connected to sludge thickener 18.C/N BAF 17 top is connected to the import of DN BAF 16 through reflux pump.
Reactor for hydrolysis and acidification 15 is connected with self-circulating pump 15P and corresponding self-circulation pipeline.In reactor for hydrolysis and acidification 15, the filler of filling is half soft biologic packing material; Filling ceramic grain filter in DN BAF 16, C/N BAF 17, and dissolved oxygen monitor 1 is set respectively overlaps.
Specifically, above-mentioned organic liquid waste storage tank 2 adopts UPVC pipe to be connected with oxidation-reduction reactor 7 by organic waste liquid pump 2P, mercurous waste tank 3 adopts UPVC pipe to be connected with oxidation-reduction reactor 7 by mercurous waste drains pump 3P, sexavalent chrome waste tank 4 adopts UPVC pipe to be connected with oxidation-reduction reactor 7 by sexavalent chrome waste drains pump 4P, heavy metal waste tank 5 adopts UPVC pipe to be connected with oxidation-reduction reactor 7 by heavy metal waste drains pump 5P, and cyanide bearing waste solution storage tank 6 adopts UPVC pipe to be connected with oxidation-reduction reactor 7 by cyanide bearing waste solution pump 6P.Each waste tank is equipped with anticorrosion ultrasonic level gage, when COMPUTER DETECTION reaches set(ting)value to (as the organic waste tank 2) liquid level of in waste tank, starting waste drains pump (as organic waste drains pump 2P) pumps in oxidation-reduction reactor 7 by the waste liquid in this waste tank, oxidation-reduction reactor 7 is provided with anticorrosion ultrasonic level gage, when in oxidation-reduction reactor 7, liquid level reaches set(ting)value, waste drains pump (as organic waste drains pump 2P) termination of pumping, and start waste liquid (as organic liquid waste) handling procedure carry out computer program control under automatic treating processes.
Spent acid solution storage tank 1 adopts UPVC pipe to be connected with acid solution explosive box 25 by spent acid liquid pump 1P, using the medicament in addition utilization of waste material of spent acid as reaction process.Finished acid is added when spent acid amount is inadequate.
The setting of various waste liquid redox classification pre-reaction program is that the ripe treatment technology removed according to the characteristic contamination of such waste liquid is determined, now presses waste liquid classification declaration treating processes.
Organic liquid waste process adopts Fenton oxidation method.Organic waste liquid pump 2P by waste liquid from organic waste tank 2 pump in oxidation-reduction reactor 7, when filling organic liquid waste in oxidation-reduction reactor 7, start spent acid volume pump 25A and add acid solution in oxidation-reduction reactor 7, start stirrer to stir simultaneously, stirrer rotating speed is set to 120 revs/min (rotating speed can be adjusted by variable-frequency motor according to practical situation setting computer parameter), belonging to oxidation-reduction reactor 7, signal is reached computer by pH instrument, when pH value is 4, acid solution volume pump 25A stops, start ferrous sulfate volume pump 27P, add ferrous sulfate, after reaching add-on, stop ferrous sulfate volume pump 27P, start hydrogen peroxide volume pump 23P and add hydrogen peroxide solution, after reaching add-on, stop hydrogen peroxide volume pump 23P, stirrer rotating speed is set to 80 revs/min, react after 1.5 hours, stirrer stops, open oxidation-reduction reactor 7 bottom discharge valve, draining is to mixing pit, emptying rear closedown water discharge valve.Wait for the execution instruction of next class liquid waste disposal program.
Mercurous liquid waste disposal adopts chemical precipitation method.Mercurous waste drains pump 3P by waste liquid from mercurous waste tank 3 pump in oxidation-reduction reactor 7, when filling mercurous waste liquid in oxidation-reduction reactor 7, start sodium sulphite volume pump 21P and add sodium sulfide solution in oxidation-reduction reactor 7, start stirrer to stir simultaneously, stirrer rotating speed is set to 120 revs/min, after reaching add-on, sodium sulphite volume pump 21P stops, start ferrous sulfate volume pump 27P, add ferrous sulfate, after reaching add-on, stop ferrous sulfate volume pump 27P, stirrer rotating speed is set to 80 revs/min, react after 0.5 hour, stirrer stops, staticly settle 0.5 hour, open mud valve bottom oxidation-reduction reactor 7, spoil disposal is to sludge sump, mud valve is closed after draining into designated water level.Open oxidation-reduction reactor 7 bottom discharge valve, draining to mixing pit, emptying rear closedown water discharge valve.Wait for the execution instruction of next class liquid waste disposal program.
Heavy metal liquid waste disposal adopts chemical precipitation method.Heavy metal waste drains pump 5P by waste liquid from heavy metal waste tank 5 pump in oxidation-reduction reactor 7, when filling heavy metal waste liquid in oxidation-reduction reactor 7, start calcium hydroxide volume pump 22P and add aqua calcis in oxidation-reduction reactor 7, start stirrer to stir simultaneously, stirrer rotating speed is set to 120 revs/min, belonging to oxidation-reduction reactor 7, signal is reached computer by pH instrument, when pH value is 8, calcium hydroxide volume pump 22P stops, start polymerize aluminum chloride volume pump 28A, add polymerize aluminum chloride, after reaching add-on, stop polymerize aluminum chloride volume pump 28A, stirrer rotating speed is set to 80 revs/min, react after 0.5 hour, stirrer stops, staticly settle 0.5 hour, open mud valve bottom oxidation-reduction reactor 7, spoil disposal is to sludge sump, mud valve is closed after draining into designated water level.Open oxidation-reduction reactor 7 bottom discharge valve, draining to mixing pit, emptying rear closedown water discharge valve.Wait for the execution instruction of next class liquid waste disposal program.
Sexavalent chrome liquid waste disposal adopts reduction precipitation method.Sexavalent chrome waste drains pump 4P by waste liquid from sexavalent chrome waste tank 4 pump in oxidation-reduction reactor 7, after filling sexavalent chrome waste liquid to designated water level in oxidation-reduction reactor 7, sexavalent chrome waste drains pump 4P closes, start ferrous sulfate volume pump 27P and add copperas solution in oxidation-reduction reactor 7, start stirrer to stir simultaneously, stirrer rotating speed is set to 120 revs/min, after reaching add-on, stop ferrous sulfate volume pump 27P, start calcium hydroxide volume pump 22P, add calcium hydroxide, after reaching add-on, stop calcium hydroxide volume pump 22P, stirrer rotating speed is set to 80 revs/min, react after 0.5 hour, stirrer stops, staticly settle 0.5 hour, open mud valve bottom oxidation-reduction reactor 7, spoil disposal is to sludge sump, mud valve is closed after draining into designated water level.Open oxidation-reduction reactor 7 bottom discharge valve, draining to mixing pit, emptying rear closedown water discharge valve.Wait for the execution instruction of next class liquid waste disposal program.
Cyanide bearing waste solution process adopts chemical oxidization method.Cyanide bearing waste solution pump 6P by self-contained for waste liquid cyanogen waste tank 6 pump in oxidation-reduction reactor 7, after filling cyanide bearing waste solution to designated water level in oxidation-reduction reactor 7, cyanide bearing waste solution pump 6P closes, start sodium hydroxide volume pump 24A and add sodium hydroxide solution in oxidation-reduction reactor 7, start stirrer to stir simultaneously, stirrer rotating speed is set to 120 revs/min, when belonging to oxidation-reduction reactor 7, pH instrument indicating value is 11, sodium hydroxide volume pump 24A stops, start volume pump 26P and add chlorine bleach liquor, when belonging to oxidation-reduction reactor 7, ORP instrument indicating value is 300mV, stop clorox volume pump 26P, stirrer rotating speed is set to 80 revs/min, react after 0.5 hour, start volume pump 24A and add sodium hydroxide solution in oxidation-reduction reactor 7, stirrer rotating speed is set to 120 revs/min simultaneously, when belonging to oxidation-reduction reactor 7, pH instrument indicating value is 9, sodium hydroxide volume pump 24A stops, start volume pump 26P and add chlorine bleach liquor, when belonging to oxidation-reduction reactor 7, ORP instrument indicating value is 650mV, stop clorox volume pump 26P, stirrer rotating speed is set to 80 revs/min, react after 0.5 hour, stirrer stops, open oxidation-reduction reactor 7 bottom discharge valve, draining is to mixing pit, emptying rear closedown water discharge valve.Wait for the execution instruction of next class liquid waste disposal program.
Pretreated waste liquid of classifying all enters mixing pit 8, realizes even water quality.Waste liquid in mixing pit 8 pumps into pH regulator groove A by sump pump 9, adds acid solution by volume pump 25B, under continual stirring conditions, realizes the pH regulator of waste liquid in pH regulator groove A, and pH value is adjusted to 4 by the pH instrument control volume pump 25B of pH regulator groove A.PH regulator groove A water outlet gravity flow enters micro-electrolysis reactor 11 and carries out micro-electrolysis reaction, electrolysis reactor 11 water outlet gravity flow enters pH regulator groove B, sodium hydroxide solution is added by volume pump 24B, under continual stirring conditions, in pH regulator groove B, realize the pH regulator of waste liquid, pH value is adjusted to 8 by the pH instrument control volume pump 24B of pH regulator groove B.PH regulator groove B water outlet gravity flow enters vertical-flow settling vessel 13, carry out preliminary solid-liquid separation, water outlet is flow automatically the coagulation tank entered in tilted plate separator 14, add polymerize aluminum chloride and polyacrylamide polymeric flocculant respectively by volume pump 28B and 29B simultaneously, under air slowly stirs, various suspended particle is mutually built bridge and is formed larger heavier flco, bottom coagulation tank, water outlet flows automatically to the negative area of tilted plate separator 14, flco is separated with water, supernatant liquor is from flowing into reactor for hydrolysis and acidification 15, at a large amount of hydrolytic bacteria, be dissolved organic matter by insoluble hydrolysis of organic matter under the effect of acidifying bacterium, the larger molecular organics of difficult for biological degradation is converted into the small organic molecule of readily biodegradable, improve the biodegradability of waste water.Reactor for hydrolysis and acidification 15 water outlet gravity flow enters DN BAF 16, remove organic pollutant, supernatant liquor gravity flow enters C/N BAF 17 and carries out nitration reaction, mainly carry out nitrated to the ammonia nitrogen in sewage, water outlet is back to BAF 16 by a reflux pump 17P part and carries out denitrification denitrogenation.Standard water discharge discharge the most at last.Bottom oxidation-reduction reactor 7, vertical-flow settling vessel 13 ﹑ inclined-plate clarifying basin 14, in cone bucket, mud timing automatic enters sludge thickener 18.BAF 16 and BAF 17 backwash water outlet gravity flow enter sludge thickener 18.After sludge condensation in sludge thickener 18, squeeze into chamber-type press filter 20 dewater through spiral pump 19, mud cake is transported outward.Mixing pit 8 got back to by sludge thickener supernatant liquor.
In figure, sodium hydroxide volume pump 24A and 24B; Acid solution volume pump 25A and 25B; Polymerize aluminum chloride volume pump 28A and 28B; Polyacrylamide volume pump 29A and 29B is respectively provided with two, can respectively to outer feed flow, also can be for subsequent use each other.
The utility model, for the water quality shown in table 1, is specifically described.
The main water-quality guideline of table 1 waste liquid
Liquid waste disposal amount is determined according to collecting amount.Table 1 is the treatment capacity of process peak period, each 1.0m of cyanide bearing waste solution treatment capacity
3, process in every 2 weeks 1 time; The each 1.0m of heavy metal liquid waste disposal amount
3, process in every 2 days 1 time; The each 1.0m of organic liquid waste treatment capacity
3, process 1 every day; The each 1.0m of mercurous liquid waste disposal amount
3, process in every 2 weeks 1 time; The each 1.0m of chrome waste liquid treatment capacity
3, process in every 2 weeks 1 time.Waste liquid classification preprocessor and optimum configurations are as described in six (embodiments).
Pretreated mixed waste liquor treatment capacity 1.0m
3/ h, processes by flow process shown in Fig. 1.Micro-electrolysis reactor 11 pH value of intaking is adjusted to 4.0, and water outlet pH value is adjusted to 8.0, and inclined-plate clarifying basin 14 feed-water end coagulation district adds polymerize aluminum chloride and polyacrylamide polymeric flocculant, and dosage is respectively 200-260mg/L and 2.5mg/L.Once, inclined-plate clarifying basin 14 every 4 hours automatic mud removings once for vertical sedimentation basin 13 every 2 hours automatic mud removings.Reactor for hydrolysis and acidification hydraulic detention time 4h, DN BAF 16 and C/N BAF 17 hydraulic load are respectively 3.56m
3/ (m
2and 3.32m h)
3/ (m
2h), mixed liquid recycle ratio 120%, BAF 16,17 backwash in every 12 hours once.Sludge dewatering spiral pump 19 operating pressure controls at 0.6MPa, and chamber-type press filter 20 work period is 6 hours.Equipment continuous and steady operation, result is in table 2 and table 3.Table 2 is device process effluent quality, the every pollutent average removal rate of table 3.
The comprehensive waste liquid water quality situation of table 2
The every pollutent average removal rate of table 3
Note: in table 3, COD, SS press weighted mean and calculate clearance.
According to table 2 and table 3, adopt classification redox pre-treatment+micro-electrolysis reaction+coagulating sedimentation+biochemistry combination process process high density laboratory waste liquid, COD, ammonia nitrogen removal frank reach more than 90%, the clearance of lead, zinc, copper, total chromium, cyanogen and mercury all reaches more than 99. 5%, the clearance of total phosphorus reaches more than 99%, and water outlet is better than " sewage enters town sewer water quality standard " (CJ343-2010).
The utility model is not limited to above-described embodiment; on the basis of technical scheme disclosed in the utility model; those skilled in the art is according to disclosed technology contents; do not need performing creative labour just can make some to some technical characteristics wherein to replace and distortion, these are replaced and are out of shape all in protection domain of the present utility model.
Claims (6)
1. a laboratory waste liquid treatment unit, is characterized in that: comprise the classification of multiple waste liquid storage tank, oxidation-reduction reactor, mixing pit, pH regulator groove, micro-electrolysis reactor, reactor for hydrolysis and acidification, DN BAF, C/N BAF, inclined-plate clarifying basin, sludge thickener, multiple explosive box and chamber-type press filter;
Described waste liquid classification storage tank comprises spent acid solution storage tank, organic liquid waste storage tank, mercury system waste tank, sexavalent chrome waste tank, heavy metal waste tank and cyanide bearing waste solution storage tank; Described explosive box comprises calcium hydroxide explosive box, sodium hydroxide explosive box, polyacrylamide explosive box, polymerize aluminum chloride explosive box, ferrous sulfate explosive box, hydrogen peroxide explosive box, acid solution explosive box, chlorine bleach liquor's explosive box and sodium sulphite explosive box;
The outlet of described organic liquid waste storage tank, mercury system waste tank, sexavalent chrome waste tank, heavy metal waste tank, cyanide bearing waste solution storage tank is connected to oxidation-reduction reactor through transportation by lighter pump respectively; Spent acid solution outlet is connected to acid solution explosive box; Each explosive box outlet is also connected to the import of oxidation-reduction reactor respectively through volume pump; Outlet one road bottom oxidation-reduction reactor is connected to mixing pit, and another road is connected to sludge thickener;
Described pH regulator groove comprises pH regulator groove A and pH regulator groove B; PH regulator groove A is connected with the outlet of acid solution explosive box, and pH regulator groove B is connected with the outlet of sodium hydroxide explosive box; The outlet of mixing pit is connected to the lower inlet of pH regulator groove A through sump pump, the top water outlet of pH regulator groove A is connected to the import of micro-electrolysis reactor, the outlet of micro-electrolysis reactor is connected to the bottom inlet of pH regulator groove B, the top water outlet of pH regulator groove B is connected to the import of vertical-flow settling vessel, the water outlet on vertical-flow settling vessel top is connected to the import of tilted plate separator, and the water outlet of tilted plate separator is connected to the import of reactor for hydrolysis and acidification; The water outlet of reactor for hydrolysis and acidification is connected to the import of DN BAF, and the water outlet of DN BAF connects the import as C/N BAF, and the outlet of C/N BAF connects discharge tube; Sludge outlet bottom described vertical-flow settling vessel, tilted plate separator and reactor for hydrolysis and acidification is connected to sludge thickener through valve;
Described sludge thickener apical supernatant fluid outlet is connected to mixing pit, and the outlet of sludge thickener base sludge is connected to chamber-type press filter through sludge pump, and the filtrate outlet of chamber-type press filter is connected to mixing pit;
Be respectively equipped with aeration tube in described micro-electrolysis reactor, DN BAF and C/N BAF, described aeration tube is connected with blower fan.
2. laboratory waste liquid treatment unit according to claim 1, it is characterized in that: described oxidation-reduction reactor is provided with supersonic liquid level controller, pH controller, ORP controller, frequency conversion agitator motor, with the stir shaft of agitating vane and tachogenerator, output shaft and the stir shaft of frequency conversion agitator motor are in transmission connection.
3. laboratory waste liquid treatment unit according to claim 1, it is characterized in that: described DN BAF and C/N BAF are connected to Backwash pipeline, the backwashing water outlet of DN BAF and C/N BAF is connected to sludge thickener.
4. the laboratory waste liquid treatment unit according to claim 1-3 any one, is characterized in that: described C/N BAF top is connected to the import of DN BAF through reflux pump.
5. the laboratory waste liquid treatment unit according to claim 1-3 any one, is characterized in that: described reactor for hydrolysis and acidification is connected with self-circulating pump and corresponding self-circulation pipeline.
6. the laboratory waste liquid treatment unit according to claim 1-3 any one, is characterized in that: in described reactor for hydrolysis and acidification, the filler of filling is half soft biologic packing material; Filling ceramic grain filter in DN BAF, C/N BAF, and dissolved oxygen monitor 1 is set respectively overlaps.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420717359.6U CN204310915U (en) | 2014-11-26 | 2014-11-26 | Laboratory waste liquid treatment unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420717359.6U CN204310915U (en) | 2014-11-26 | 2014-11-26 | Laboratory waste liquid treatment unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204310915U true CN204310915U (en) | 2015-05-06 |
Family
ID=53133242
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420717359.6U Withdrawn - After Issue CN204310915U (en) | 2014-11-26 | 2014-11-26 | Laboratory waste liquid treatment unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204310915U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104370423A (en) * | 2014-11-26 | 2015-02-25 | 扬州大学 | Laboratory effluent treatment device |
| CN108455722A (en) * | 2018-02-06 | 2018-08-28 | 安庆师范大学 | A kind of collection of laboratory waste liquid and processing system |
| CN108706840A (en) * | 2018-08-15 | 2018-10-26 | 成都优浦水务科技有限公司 | A kind of laboratory waste water integrated treatment unit |
-
2014
- 2014-11-26 CN CN201420717359.6U patent/CN204310915U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104370423A (en) * | 2014-11-26 | 2015-02-25 | 扬州大学 | Laboratory effluent treatment device |
| CN108455722A (en) * | 2018-02-06 | 2018-08-28 | 安庆师范大学 | A kind of collection of laboratory waste liquid and processing system |
| CN108706840A (en) * | 2018-08-15 | 2018-10-26 | 成都优浦水务科技有限公司 | A kind of laboratory waste water integrated treatment unit |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104370423B (en) | Laboratory waste liquid treatment unit | |
| CN106830544A (en) | Light electrolysis Fenton EGSB A/O BCO BAF coagulating treatment pharmacy waste water systems | |
| CN201033757Y (en) | Sewage water treatment system for fruit juice waste water | |
| CN203866098U (en) | High-efficiency anaerobic and aerobic integrated reactor | |
| CN103435235A (en) | Kitchen waste filtrate treatment equipment and method | |
| CN101565261A (en) | Treatment process for medical intermediate production waste water | |
| CN110104908A (en) | A kind of hair product waste water efficient denitrification system and efficient denitrification technique | |
| CN204310915U (en) | Laboratory waste liquid treatment unit | |
| CN102642995B (en) | Method and system for physicochemical biological combined treatment of drilling wastewater of oil and gas field | |
| CN107555600A (en) | A kind of sewage disposal system | |
| CN106277553A (en) | The processing method of the dense water of reverse osmosis (RO) and equipment | |
| CN110386689A (en) | Pretreatment system for bed mud residual water treatment equipment | |
| CN220132055U (en) | Treatment system for special industrial wastewater | |
| CN207259325U (en) | A kind of cooperating type emulsifying liquid waste water processing system | |
| CN211497303U (en) | Pig raising wastewater treatment system | |
| CN205258202U (en) | Pharmaceutical chemical engineering effluent treatment plant | |
| CN209276327U (en) | Integrated CASS biological tank process spent water processing equipment | |
| CN109422412A (en) | A kind of Integrated Processing Unit of coating waste-water and sanitary sewage | |
| JP2002531250A (en) | Biological treatment equipment for leather wastewater and sludge reduction | |
| CN110563285B (en) | Integrated biogas slurry wastewater treatment system and treatment process thereof | |
| CN211284066U (en) | Kitchen waste fermentation liquor treatment system | |
| CN211847575U (en) | Integrated sewage treatment system | |
| CN203653367U (en) | Hydrochloric acid wastewater treatment equipment | |
| CN205501046U (en) | Contain chromium electroplating industry sewage treatment system | |
| CN207811366U (en) | A kind of sewage disposal system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20150506 Effective date of abandoning: 20160309 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20150506 Effective date of abandoning: 20160309 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |