CN103803754A - Method and device for processing dye acid waste water - Google Patents
Method and device for processing dye acid waste water Download PDFInfo
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- CN103803754A CN103803754A CN201410078376.4A CN201410078376A CN103803754A CN 103803754 A CN103803754 A CN 103803754A CN 201410078376 A CN201410078376 A CN 201410078376A CN 103803754 A CN103803754 A CN 103803754A
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Abstract
The invention relates to a method and a device for processing dye acid waste water. The method comprises the following steps: treating the collected dye waste acid which is classified through the steps of distilling concentration, neutralization, adsorption, micro-electrolysis, coagulating sedimentation, adsorption by active carbon column, concentration crystallization and separation for preparing sodium (ammonium) sulfate or sodium (ammonium) chloride, further treating the distilled water, feeding the further-treated water into an industrial water storage pool after reaching the industrial recycled water standard, and circulating the water to the dye production step. The method and the device are especially suitable for the industry for producing dye, titanium dioxide and the like and having a great amount of waste sulfuric acid and waste hydrochloric acid, the waste sulfuric acid and the waste hydrochloric acid produced in the production process can be used for preparing the sodium (ammonium) sulfate or sodium (ammonium) chloride, the acid waste water can be recycled, the waste can be converted into treasure, the distilled water can be circulated to the industrial production after being further treated, and the emission of the waste water can be reduced.
Description
The application is to be that on 03 12nd, 2013, application number are the divisional application of 201310078739.X, the denomination of invention application that is " a kind for the treatment of process of dyestuff acid waste water and device " the applying date.
Technical field
The present invention relates to a kind for the treatment of process of dyestuff acid waste water, and the device that uses the method to carry out the processing of dyestuff acid waste water.
Background technology
Along with the fast development of China's dyestuffs industries, dyestuff has become an important mainstay industry of China in recent years.Due to the continuous innovation of dye technology, new synthetic materials is widely used in whole industry simultaneously, causes the difficulty of three wastes processing also to increase thereupon.Acid is as a kind of important starting material in dyestuffs industries, in various dye well intermediate production processes, producing a large amount of spent acid is discharged in water together in company with the organism, the by product that do not utilize, the difficulty that has not only increased enterprise's sewage disposal causes a large amount of wastings of resources simultaneously.During " 12 ", along with carrying out of national energy-saving reduction of discharging activity, the three wastes processing of dyestuffs industries is faced with stern challenge more especially.
At present domestic dyestuff acid waste water improvement thinking is mainly that the qualified discharge based on spent acid designs, and usual method comprises lime neutralisation, chemical oxidization method and wet oxidation process etc.In lime neutralisation, due to a large amount of lime of needs consumption and produce the waste residues such as a large amount of calcium sulfate, cause follow-up disposition of solid waste cost to increase; Chemical oxidization method is as too high in dioxygen water law, Ozonation, the general running cost of Fenton oxidation style, and enterprise cannot bear; Although wet oxidation process effect is fairly obvious, also exist cost of investment larger, equipment requirements is higher, problem that cannot be extensively universal.
Micro-electrolysis be a kind of economical, efficiently, wastewater processing technology easily.Micro electrolysis tech is existing application in dye wastewater treatment (CN102260009A), but be the micro-electrolysis of common iron charcoal due to what adopt in this patent, pH to waste water has relatively high expectations, sludge creation amount is larger, this patent adopts simultaneously nanofiltration investment and maintenance cost are higher, though concentrated solution can reach reuse standard after treatment, but high salinity the having relatively high expectations to microorganism and operative technique in concentrated solution, process and accidentally can cause treatment effect obviously to decline, cannot extensively popularize the dye chemical industry enterprise of big yield.Compare the micro-electrolysis of iron charcoal, the micro-electrolysis of iron copper not only has more wide in range pH use range, and sludge creation amount is 1/3 left and right of the micro-electrolysis of iron charcoal simultaneously.Iron copper micro electrolysis tech starts to obtain gradually application in dyeing wastewater through organic matter and colourity processing (CN102311205A), high-concentration wastewater containing alkaline mud processing (CN101693579A) and refractory wastewater (CN102774935A) at present, but has not yet to see report in the resource utilization method of being prepared the byproduct such as sodium sulfate (ammonium) or sodium-chlor (ammonium) by Acid Dye Wastewater.Specifically how micro electrolysis tech and other are processed to means fit applications in this recycling, still need deep exploration.Prepare in the existing method of the byproduct such as sodium sulfate (ammonium) or sodium-chlor (ammonium) and adopt oxygenant (clorox, hydrogen peroxide etc.) to process (CN102826673A) Acid Dye Wastewater, in order to reach comparatively satisfied treatment effect, not only oxygenant large usage quantity, processing cost is higher, and the pH value of waste water is had to strict control requirement, be not suitable for extensively promoting the use of.
In the face of increasingly serious environmental protection pressure, dye industry is in the urgent need to carrying out technical renovation to the links of existing waste water treatment process, finding suitable wastewater treatment means carries out system, organically coordinates, adapt to the requirement of dyestuff acid waste water processing, explore best treatment process, thus by waste water recycling after treatment in producing, control total emission volumn, and realize the recycling of dyestuff acid waste water, and make DYE PRODUCTION reach the target of cleaner production, reduce running cost simultaneously.
Summary of the invention
The object of the invention is to provide a kind for the treatment of process of dyestuff acid waste water and the device that uses the method to carry out the processing of dyestuff acid waste water.The method is by being optimized, coordinating coupling by various wastewater treatment means, make it be applicable to dyestuff acid waste water, and make each wastewater treatment means bring into play best effect in dyestuff acid waste water is processed, thereby obtain the treatment process of improved dyestuff acid waste water of the present invention.This states method can be prepared into dyestuff acid waste water the byproduct such as sodium sulfate (ammonium) or sodium-chlor (ammonium) after the processing by a series of automatizations, distillation water outlet in concentration process is carried out to advanced treatment simultaneously and carried out recycling to reach service water reuse standard, significantly cut down enterprise pollution thing discharge object thereby reach.
The technical solution used in the present invention is:
A treatment process for dyestuff acid waste water, described method comprises the following steps:
(a) classification is processed: by the Waste Sulfuric Acid producing in DYE PRODUCTION or waste hydrochloric acid according to sour content categorised collection in collecting tank;
(b) neutralization, absorption: by Waste Sulfuric Acid or the waste hydrochloric acid of the regulation content of gained in step (a), in proceeding to continuously and in still, simultaneously continuously in and in still, feed alkali and neutralize, by online pH meter control pH value, neutralizer flow to absorption still, in absorption still, add sorbent material to adsorb continuously and automatically according to flooding velocity simultaneously, the mixed solution after absorption is filtered through pressure filter;
(c) micro-electrolysis: the filtrate obtaining in step (b) is gone in micro cell and carries out redox, control the hydraulic detention time in micro cell simultaneously;
(d) coagulating sedimentation: in step (c), the water outlet of micro cell flow to coagulation still, adds continuously the liquid material that comprises coagulating agent and flocculation agent simultaneously, stirs; Then by mixed solution through Filter Press;
(e) charcoal absorption: the filtrate obtaining in step (d) is gone to activated carbon column and decolour, take off organic adsorption treatment, control hydraulic detention time, the mixed solution after absorption flows in storage tanks and stores;
(f) condensing crystal: by the mixed solution in storage tanks in step (e) go to that evaporation equipment concentrates, crystallization, separation, obtain sodium sulfate (ammonium) or sodium-chlor (ammonium) crystal, collect distillation water outlet simultaneously and recycle.
The treatment process of dyestuff acid waste water of the present invention, preferably also comprises: (g) advanced treatment: after BAF is processed, make water outlet reach service water reuse standard the distillation water outlet of collecting in step (f), enter service water reuse tank.
The treatment process of dyestuff acid waste water of the present invention, it is 10%～20% that the regulation content described in preferred steps (b) is calculated in mass percent.
The treatment process of dyestuff acid waste water of the present invention, preferably in step (a), Waste Sulfuric Acid is carried out to categorised collection by the concentration rank of mass percent 2%～10%, 10%～20%, 20%～75%, and waste hydrochloric acid is pressed the concentration rank categorised collection of mass percent 2%～10%, 10%～20%.
The treatment process of dyestuff acid waste water of the present invention, preferably in step (a), Waste Sulfuric Acid, waste hydrochloric acid that also to comprise the mass percent of collection be 2%～10% are concentrated into 10%～20% by evaporation equipment, and the Waste Sulfuric Acid that is 10%～20% by content mass percent or waste hydrochloric acid are for step (b); The spent acid that exceedes 20% content after the pre-treatment such as sorbent material absorption, separation reuse to DYE PRODUCTION.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (b), described spent acid flooding velocity, alkali adds inbound traffics and pH value tripartite automatic interlock.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (b), controls the scope of pH value to 8.1～9.5.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (b), described alkali is to be selected from one or more in sodium hydroxide, sodium carbonate, liquefied ammonia or ammoniacal liquor.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (b), described sorbent material by cage device continuous uniform feed intake, add-on and the automatic interlock of absorption still flooding velocity.Control adsorption time is 0.5～2h.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (b), described sorbent material is to be selected from one or more in carclazyte, wilkinite, silica gel, clay, activated alumina, zeolite, Powdered Activated Carbon.
Sorbent material after separation preferably carries out harmless treatment through burning, and removes the organism of absorption, and residue is as brickmaking and material of construction.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (b), with respect to flooding velocity, the mass ratio that adds sorbent material is 0.1%～6%.
The treatment process of dyestuff acid waste water of the present invention, the filler of the described micro-electrolysis of preferred steps (c) is iron, copper, zinc, manganese, silver.Preferably wherein the mass ratio of iron is 60%～90%, and the total mass ratio of copper, zinc, manganese, silver is 10%～40%.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (c), hydraulic detention time control is 0.5～4 hour.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (d), described coagulating agent and the add-on of flocculation agent are by on-line automatic Controlling System and coagulation still flooding velocity interlocking.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (d), to add coagulating agent be to be selected from one or more in aluminum chloride, polymerize aluminum chloride, Tai-Ace S 150, ferrous sulfate, poly-ferric chloride, aluminium iron polychloride.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (d), with respect to flooding velocity, the mass ratio that adds coagulating agent is 0.2%～5%, the concentration of coagulant solution is 2%～20%.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (d), flocculation agent is polyacrylamide (PAM).
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (d), with respect to flooding velocity, the mass ratio that adds flocculation agent is 0.02%～2%, the concentration of flocculant solution is 0.1%～0.5%.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (d), the filter cake that press filtration obtains burns.
The treatment process of dyestuff acid waste water of the present invention, the activated carbon granule particle diameter in preferred steps (e) in activated carbon column is 0.5mm～5mm.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (e), hydraulic detention time control is 0.5～4 hour.
The treatment process of dyestuff acid waste water of the present invention, the activated carbon column described in preferred steps (e) is 2 grades of above activated carbon columns, activated carbon column water outlet is carried out endpoint monitoring through online colourity monitor.
The treatment process of dyestuff acid waste water of the present invention, the process that the online colourity monitor of preferred steps (e) carries out terminal control is: in the time that activated carbon column effluent color dilution is below 10 times, water outlet flows in storage tanks, in the time that colourity is more than 10 times, water outlet flows into next stage activated carbon column and proceeds decolouring processing, until effluent color dilution flows in storage tanks 10 times of following rear water outlets.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (a), step (f), evaporation equipment is MVR equipment.The distillation effluent COD concentration of MVR equipment is lower than 500mg/L, and colourity is colourless.
The treatment process of dyestuff acid waste water of the present invention, in preferred steps (a), the distillation water outlet of evaporation equipment makes water outlet reach industrial reuse water quality standard after BAF is processed.
The treatment process of preferred dyestuff acid waste water of the present invention comprises: it is 10%～20% that the spent acid that in collecting tank A, mass percent is 2%～10% is first concentrated into mass percent with a MVR equipment S1, by 10%～20% spent acid pump in and still B neutralize, after neutralization, solution enters absorption still C, add sorbent material to adsorb by cage device W simultaneously, then overflow is to transfer still D, pump to the first pressure filter E filters again, filtrate is after micro cell G redox, carry out coagulation from flowing to coagulation still H, mixed solution overflow is to transfer still J, pump to the second pressure filter L filters, filtrate after more than 1 grade or 2 grades activated carbon column decoloring overflow to storage tanks Q, and pump to the two MVR equipment S2 concentrate, crystallization, separate and obtain sodium sulfate finally by whizzer T, ammonium sulfate, sodium-chlor or ammonium chloride, collect distillation water outlet simultaneously, after advanced treatment, be back to production.
The treatment unit that the invention still further relates to a kind of dyestuff acid waste water, comprising:
Collecting tank A, carries out categorised collection for Waste Sulfuric Acid or waste hydrochloric acid that DYE PRODUCTION is produced;
In and still B, for being 10%～20% by mass percent, Waste Sulfuric Acid or waste hydrochloric acid neutralize with alkali;
Absorption still C, for future, the neutralizer of self-neutralization still B carries out adsorption treatment with the sorbent material adding;
The first pressure filter E, carries out press filtration for the mixed solution to after adsorption treatment;
Micro cell G, carries out oxide treatment for the filtrate that the first pressure filter E press filtration is obtained;
Coagulation still H, for adding the liquid material that comprises coagulating agent and flocculation agent to carry out coagulation to the water outlet of micro cell G;
The second pressure filter L, carries out press filtration for the mixed solution to after coagulation;
More than 1 grade or 2 grades activated carbon column, for carrying out adsorption treatment to the filtrate of the second pressure filter L press filtration gained;
Storage tanks Q, for storing the filtrate after adsorption treatment;
The 2nd MVR equipment S2, the water outlet for concentrated, crystallization from storage tanks Q;
Whizzer T, for by the solid of enriched material, liquid separation;
BAF, for processing the distillation water outlet of the 2nd MVR equipment S2 to make it reach service water reuse standard.
The treatment unit of dyestuff acid waste water of the present invention, preferably also comprises:
The one MVR equipment S1, the waste acid concentration that is 2%～10% for the mass percent that collecting tank A is collected to mass percent is 10%～20%; BAF, for processing the distillation water outlet of a MVR equipment S1 to make it reach service water reuse standard.
In said apparatus of the present invention, preferably by the 3rd volume pump P3 in and still B in be continuously pumped into spent acid, by the 4th volume pump P4 continuously in and still B in pump into alkali, detect pH value by online pH meter, wherein, the 3rd volume pump P3, the 4th volume pump P4 and pH meter tripartite are carried out to automatic linkage control.
In said apparatus of the present invention, preferably the neutralizer after neutralization goes to absorption still C continuously through first flow meter F1, and in absorption still C, feed sorbent material continuously by cage device W, wherein, the solid measuring apparatus of first flow meter F1 and cage device W is carried out to automatic linkage control.
In said apparatus of the present invention, the preferably water outlet after redox in micro cell G, proceed to continuously coagulation still H through the second under meter F1, and in coagulation still H, pump into the liquid material containing coagulating agent and flocculation agent continuously by the tenth volume pump P10, wherein, the second under meter F1 and the tenth volume pump P10 are carried out to automatic linkage control.
In said apparatus of the present invention, preferably wherein said activated carbon column water outlet is carried out endpoint monitoring through online colourity monitor.
The treatment process of dyestuff acid waste water of the present invention and device, its superiority is mainly reflected in: the present invention is by being optimized, coordinating coupling by the Waste Sulfuric Acid in DYE PRODUCTION process or waste hydrochloric acid by various wastewater treatment means, after the processing of a series of automatizations, prepare sodium sulfate (ammonium) or sodium-chlor (ammonium), spent acid is carried out to recycling, turn waste into wealth.The present invention has not only abandoned in conventional dyes spent acid use lime and has produced the method for the dirty slags such as a large amount of calcium sulfate, and has lowered energy consumption, has reduced personnel cost.Method of the present invention has not only been widened the pH scope of wastewater treatment, and greatly reduces processing cost under same treatment effect, and has greatly reduced the sludge quantity because using oxygenant to produce.In addition the distillation water outlet producing in concentration process reuse capable of circulation after advanced treatment, to DYE PRODUCTION process, is no longer received tube drainage, has greatly alleviated the environmental protection treatment pressure of enterprise.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the treatment process of dyestuff acid waste water of the present invention.
Fig. 2 is the automatic flow schematic diagram for the treatment of process one example of dyestuff acid waste water of the present invention.
The implication of the Reference numeral in Fig. 2 is as follows: A-collecting tank, B-in and still, C-absorption still, D-transfer still, E-the first pressure filter, G-micro cell, H-coagulation still, J-transfer still, L-the second pressure filter, M1-one-level activated carbon column, M2-secondary activated carbon column, Q-storage tanks, S1, S2-first, second MVR equipment, T-whizzer, W-cage device, X-containing the liquid material of coagulating agent and flocculation agent, Y-alkali, F1, F2-under meter, K1, K2-colourity monitor, P1～P10-the first is to the tenth pump or volume pump.
Embodiment
Referring to accompanying drawing, the present invention is further described.
Fig. 2 shown device carries out automatization control by DCS Controlling System.
In Fig. 2, in collecting tank A, spent acid is carried out to categorised collection, it is 10%～20% that the spent acid that wherein mass percent is 2%～10% is first concentrated into mass percent with a MVR equipment S1.10%～20% spent acid through the 3rd volume pump P3, alkali through the 4th volume pump P4 continuous pump in and still B neutralize, and detect pH value by online pH meter.Wherein, the 3rd volume pump P3, the 4th volume pump P4 and pH meter tripartite are carried out to automatic linkage control.
After neutralization, solution goes to absorption still C continuously through first flow meter F1, and adsorbs to feeding sorbent material in absorption still C continuously by cage device W.Wherein, the solid measuring apparatus of first flow meter F1 and cage device W is carried out to automatic linkage control.Then overflow is to transfer still D, then pump to the first pressure filter E filters.
Filtrate is after micro cell G redox, go to continuously in coagulation still H through the second under meter F1, and carry out coagulation to pumping into containing the liquid material of coagulating agent and flocculation agent in coagulation still H continuously by the tenth volume pump P10, wherein, the second under meter F1 and the tenth volume pump P10 are carried out to automatic linkage control.
Mixed solution overflow after coagulation is to transfer still J, pump to the second pressure filter L filters, filtrate after more than 1 grade or 2 grades activated carbon column decoloring overflow to storage tanks Q, and pump to the two MVR equipment S2 concentrate, crystallization, separate and obtain sodium sulfate, ammonium sulfate, sodium-chlor or ammonium chloride finally by whizzer T, collect distillation water outlet simultaneously, after advanced treatment, be back to production.
Embodiment
The Waste Sulfuric Acid that is 2% by the mass percent of categorised collection (wherein 256 times of colourities, TOC value 1000mg/L), with pump P1 pump to the, a MVR equipment S1 is concentrated into sulfuric acid mass percent approximately 11% left and right.By the Waste Sulfuric Acid after concentrated through the 3rd volume pump P3 continuous pump in and still B, be continuously pumped into sodium hydroxide solution through the 4th volume pump P4 simultaneously, after recording pH value and be 8.1 by online pH meter, neutralizer continuously flows into absorption still C through overflow port, simultaneously by the continuous automatic uniform of cage device W add the carclazyte that quality is 0.3% with respect to flooding velocity to adsorb, mixed solution after absorption is from flowing into transfer still D, with pump P5, mixture pump to the first pressure filter E in transfer still D is filtered simultaneously, filtrate through volume pump P6 pump to micro cell G(wherein weight of iron ratio be 90%, copper mass ratio is 5%, zinc mass ratio is 2%, manganese mass ratio is 2%, silver mass ratio is 1%), control hydraulic detention time 1 hour, micro cell G water outlet is from flowing into coagulation still H, add continuously the PAM solution (concentration is 0.1%) that the polymeric aluminum chlorides solution that quality is 0.5% with respect to flooding velocity (concentration is 20%) and quality are 0.1% with respect to flooding velocity simultaneously, after coagulating sedimentation 1 hour, mixed solution flows into transfer still J from overflow port, mixed solution in transfer still J is filtered with pump P7 pump to the second pressure filter L, filter pump P8 pump is to one-level activated carbon column M1, in post, activated carbon granule particle diameter is 4mm～5mm, controlling hydraulic detention time in post is 1 hour, it is 5 times by online the first colourity monitor K1 monitoring analysis colourity, TOC value is 83mg/L, water outlet flow to storage tanks Q from top overflow port, metabisulfite solution after treatment is concentrated with pump P9 pump to the two MVR equipment S2, crystallization, separate finally by whizzer T, obtain sodium sulfate crystal.The distillation water outlet producing in concentration process is analyzed simultaneously, result is colourless for distilling out colority of water, COD is 300mg/L, the water pump that goes out after analyzing is carried out to biochemical treatment to BAF, it is colourless going out water analysis Dry Sack degree, COD is 53mg/L, meets industrial reuse water quality standard, pumps into industrial reuse water storage pond reuse.
Embodiment 2
The waste hydrochloric acid that is 8% by the mass percent of categorised collection (256 times of colourities, TOC value 1200mg/L), pumping into a MVR equipment S1 with pump P1, to be concentrated into hydrochloric acid mass percent be approximately 11% left and right, by the waste hydrochloric acid after concentrated through the 3rd volume pump P3 continuous pump in and still B, be continuously pumped into sodium hydroxide solution through the 4th volume pump P4 simultaneously, recording pH value by online pH meter is that 9.2 rear neutralizers continuously flow into absorption still C through overflow port, simultaneously by the continuous automatic uniform of cage device W add the wilkinite that quality is 1% with respect to flooding velocity to adsorb, mixed solution after absorption is from flowing into transfer still D, with pump P5, mixture pump to the first pressure filter E in transfer still D is filtered simultaneously, filtrate through volume pump P6 pump to micro cell G(wherein weight of iron ratio be 80%, copper mass ratio is 10%, zinc mass ratio is 5%, manganese mass ratio is 3%, silver mass ratio is 2%), controlling hydraulic detention time is 1.5 hours, micro cell G water outlet is from flowing into coagulation still H, add continuously the PAM solution (concentration is 0.3%) that the copperas solution that quality is 1% with respect to flooding velocity (concentration is 12%) and quality are 0.08% with respect to flooding velocity simultaneously, after coagulating sedimentation 45 minutes, mixed solution flows into transfer still J from overflow port, mixed solution in transfer still J is filtered with pump P7 pump to the second pressure filter L, filter pump P8 pump is to one-level activated carbon column M1, in post, activated carbon granule particle diameter is 2mm～3mm, controlling hydraulic detention time in post is 2 hours, it is 9 times by online the first colourity monitor K1 monitoring analysis colourity, TOC value is 90mg/L, water outlet flow to storage tanks Q from top overflow port, sodium chloride solution after treatment is concentrated with pump P9 pump to the two MVR equipment S2, crystallization, separate finally by whizzer T, obtain sodium chloride crystal.The distillation water outlet producing in concentration process is analyzed simultaneously, result is colourless for distilling out colority of water, COD is 500mg/L, the water pump that goes out after analyzing is carried out to biochemical treatment to BAF, it is colourless going out water analysis Dry Sack degree, COD is 45mg/L, meets industrial reuse water quality standard, pumps into industrial reuse water storage pond reuse.
Embodiment 3
The waste hydrochloric acid that is 12% by the mass percent of categorised collection (512 times of colourities, TOC value 1500mg/L), through the 3rd volume pump P3 continuous pump in and still B, be continuously pumped into liquefied ammonia through the 4th volume pump P4 simultaneously, after recording pH value and be 8.5 by online pH meter, neutralizer flows into absorption still C through overflow port, simultaneously by the continuous automatic uniform of cage device W add the clay that quality is 5% with respect to flooding velocity to adsorb, mixed solution after absorption is from flowing into transfer still D, with pump P5, mixture pump to the first pressure filter E in transfer still D is filtered simultaneously, filtrate through volume pump P6 pump to micro cell G(wherein weight of iron ratio be 70%, copper mass ratio is 20%, zinc mass ratio is 6%, manganese mass ratio is 2%, silver mass ratio is 2%), controlling hydraulic detention time is 3 hours, micro cell G water outlet is from flowing into coagulation still H, add continuously the PAM solution (concentration is 0.1%) that the poly-ferric chloride solution that quality is 1.5% with respect to flooding velocity (concentration is 10%) and quality are 0.3% with respect to flooding velocity simultaneously, after coagulating sedimentation 90 minutes, mixed solution flows into transfer still J from overflow port, mixed solution in transfer still J is filtered with pump P7 pump to the second pressure filter L, filter pump P8 pump is to one-level activated carbon column M1, in post, activated carbon granule particle diameter is 0.5mm～1mm, controlling hydraulic detention time in post is 3 hours, by 20 times of online the first colourity monitor K1 monitoring analysis colourities, TOC value is 108mg/L, water outlet flow to secondary activated carbon column M2 from top overflow port, controlling hydraulic detention time is 3 hours, by 8 times of online the second colourity monitor K2 monitoring analysis colourities, TOC value is 68mg/L, water outlet flow to storage tanks Q from top overflow port, ammonium chloride solution after treatment is concentrated with pump P9 pump to the two MVR equipment S2, crystallization, separate finally by whizzer T, obtain ammonia chloride crystal.The distillation water outlet producing in concentration process is analyzed simultaneously, result is colourless for distilling out colority of water, COD is 480mg/L, the water pump that goes out after analyzing is carried out to biochemical treatment to BAF, it is colourless going out water analysis Dry Sack degree, COD is 50mg/L, meets industrial reuse water quality standard, pumps into industrial reuse water storage pond reuse.
Embodiment 4
The Waste Sulfuric Acid that is 15% by the mass percent of categorised collection (512 times of colourities, TOC value 1800mg/L), through the 3rd volume pump P3 continuous pump in and still B, be continuously pumped into liquefied ammonia through the 4th volume pump P4 simultaneously, after recording pH value and be 8.7 by online pH meter, neutralizer flows into absorption still C through overflow port, simultaneously by the continuous automatic uniform of cage device W add the silica gel that quality is 1.5% with respect to flooding velocity to adsorb, mixed solution after absorption is from flowing into transfer still D, with pump P5, mixture pump to the first pressure filter E in transfer still D is filtered simultaneously, filtrate through volume pump P6 pump to micro cell G(wherein weight of iron ratio be 60%, copper mass ratio is 25%, zinc mass ratio is 8%, manganese mass ratio is 4%, silver mass ratio is 3%), controlling hydraulic detention time is 2.5 hours, micro cell G water outlet is from flowing into coagulation still H, add continuously the PAM solution (concentration is 0.15%) that the polymerize aluminum chloride ferrous solution that quality is 0.8% with respect to flooding velocity (concentration is 10%) and quality are 0.6% with respect to flooding velocity simultaneously, after coagulating sedimentation 80 minutes, mixed solution flows into transfer still J from overflow port, mixed solution in transfer still J is filtered with pump P7 pump to the second pressure filter L, filter pump P8 pump is to one-level activated carbon column M1, in post, activated carbon granule particle diameter is 1mm～2mm, controlling hydraulic detention time in post is 2.5 hours, by 30 times of online the first colourity monitor K1 monitoring analysis colourities, TOC value is 137mg/L, water outlet flow to secondary activated carbon column M2 from top overflow port, controlling hydraulic detention time is 2.5 hours, by 10 times of online the second colourity monitor K2 monitoring analysis colourities, TOC value is 80mg/L, water outlet flow to storage tanks Q from top overflow port, ammoniumsulphate soln after treatment is concentrated with pump P9 pump to the two MVR equipment S2, crystallization, separate finally by whizzer T, obtain ammonia sulfate crystal.The distillation water outlet producing in concentration process is analyzed simultaneously, result is colourless for distilling out colority of water, COD is 450mg/L, the water pump that goes out after analyzing is carried out to biochemical treatment to BAF, it is colourless going out water analysis Dry Sack degree, COD is 47mg/L, meets industrial reuse water quality standard, pumps into industrial reuse water storage pond reuse.
Comparative example 1:
The Waste Sulfuric Acid that is 18% by the mass percent of categorised collection (256 times of colourities, TOC value 1200mg/L), through the 3rd volume pump P3 continuous pump in and still B, be continuously pumped into sodium carbonate through the 4th volume pump P4 simultaneously, by online pH meter to record pH value be 9.0 rear neutralizers through overflow port flow into micro cell G(wherein weight of iron ratio be 75%, copper mass ratio is 15%, zinc mass ratio is 5%, manganese mass ratio is 4%, silver mass ratio is 1%), controlling hydraulic detention time is 2.5 hours, micro cell G water outlet is from flowing into coagulation still H, add continuously the PAM solution (concentration is 0.2%) that the alum liquor that quality is 2% with respect to flooding velocity (concentration is 15%) and quality are 0.2% with respect to flooding velocity, after coagulating sedimentation 60 minutes, mixed solution flows into transfer still J from overflow port, mixed solution in transfer still J is filtered with pump P7 pump to the second pressure filter L, filter pump P8 pump is to one-level activated carbon column M1, in post, activated carbon granule particle diameter is 2mm～3mm, controlling hydraulic detention time in post is 1.5 hours, it is 7 times by online the first colourity monitor K1 monitoring analysis colourity, TOC value is 177mg/L, water outlet flow to storage tanks Q from top overflow port, metabisulfite solution after treatment is concentrated with pump P9 pump to the two MVR equipment S2, crystallization, separate finally by whizzer T, obtain sodium sulfate crystal.The distillation water outlet producing in concentration process is analyzed simultaneously, result is dark green for distilling out colority of water, COD is 800mg/L, the water pump that goes out after analyzing is carried out to biochemical treatment to BAF, it is colourless going out water analysis Dry Sack degree, COD is 200mg/L, cannot meet industrial reuse water quality standard.
Comparative example 2
The Waste Sulfuric Acid that is 20% by the mass percent of categorised collection (256 times of colourities, TOC value 1300mg/L), through the 3rd volume pump P3 continuous pump in and still B, be continuously pumped into ammoniacal liquor through the 4th volume pump P4 simultaneously, after recording pH value and be 8.3 by online pH meter, neutralizer flows into absorption still C through overflow port, simultaneously by the continuous automatic uniform of cage device W add the wilkinite that quality is 2% with respect to flooding velocity to adsorb, mixed solution after absorption is from flowing into transfer still D, with pump P5, mixture pump to the first pressure filter E in transfer still D is filtered simultaneously, filtrate through volume pump P6 pump to micro cell G(wherein weight of iron ratio be 85%, copper mass ratio is 8%, zinc mass ratio is 3%, manganese mass ratio is 2%, silver mass ratio is 2%), controlling hydraulic detention time is 3 hours, micro cell G water outlet uses pump P8 pump to one-level activated carbon column M1, in post, activated carbon granule particle diameter is 1mm～2mm, controlling hydraulic detention time in post is 2.5 hours, by 25 times of online the first colourity monitor K1 monitoring analysis colourities, TOC value is 168mg/L, water outlet flow to secondary activated carbon column M2 from top overflow port, controlling hydraulic detention time is 2.5 hours, by 6 times of online the second colourity monitor K2 monitoring analysis colourities, TOC value is 107mg/L, water outlet flow to storage tanks Q from top overflow port, ammoniumsulphate soln pump to the two MVR equipment S2 after treatment are concentrated, crystallization, separate finally by whizzer T, obtain ammonia sulfate crystal.The distillation water outlet producing in concentration process is analyzed simultaneously, result is for distilling out colority of water for green, COD is 780mg/L, the water pump that goes out after analyzing is carried out to biochemical treatment to BAF, it is colourless going out water analysis Dry Sack degree, COD is 151mg/L, cannot meet industrial reuse water quality standard.
Application examples 1:
According to standard GB/T 6009-2003, the sodium sulfate product of by-product in embodiment is carried out to mass analysis, the results are shown in following table:
Application examples 2:
According to standard GB/T/T5462-2003, the sodium-chlor product of by-product in embodiment is carried out to mass analysis, the results are shown in following table:
| Index/(%) | Top grade | One-level | Secondary | Embodiment 2 |
| Sodium-chlor/(%) >= | 96.00 | 94.50 | 92.00 | 96.37 |
| Moisture/(%)≤ | 3.00 | 4.10 | 6.00 | 2.80 |
| Water-insoluble/(%)≤ | 0.20 | 0.30 | 0.40 | 0.18 |
| Calcium ions and magnesium ions/(%)≤ | 0.30 | 0.40 | 0.60 | 0.25 |
| Sulfate ion/(%)≤ | 0.50 | 0.70 | 1.00 | 0.40 |
Application examples 3:
According to standard GB/T 535-1995, producing ammonium sulfate byproduct product in embodiment is carried out to mass analysis, the results are shown in following table:
Application examples 4:
According to standard GB/T/T2946-2008, the ammonium chloride product of by-product in embodiment 3 is carried out to mass analysis, the results are shown in following table:
| Index/(%) | Acceptable end product | Salable product | Embodiment 3 |
| Ammonium chloride massfraction (in butt) >= | 99.3 | 99.0 | 99.3 |
| Moisture (H2O)≤ | 0.7 | 1.0 | 0.7 |
| Ignition residue massfraction≤ | 0.4 | 0.4 | 0.3 |
| The massfraction of iron (Fe)≤ | 0.001 | 0.003 | 0.001 |
| The massfraction of heavy metal (in Pb)≤ | 0.0005 | 0.001 | 0.0004 |
| Vitriol (in SO4) massfraction≤ | 0.05 | / | 0.03 |
| PH value (200g/L solution) | 4.0 | ～5.8 | 5.8 |
(/ represent, this index did not have specific requirement)
Application examples 5:
According to standard GB/T 19923-2005, water outlet after advanced treatment in embodiment 1～6 is analyzed, the results are shown in following table:
As seen from the above table, the byproduct sulfite (ammonium) or the sodium-chlor (ammonium) that adopt method and apparatus of the present invention to obtain, meet industrial goods or agriculture product service requirements completely, and distillation water outlet is after advanced treatment, meet industrial reuse water quality standard, can be used for DYE PRODUCTION, accomplish spent acid recycling, turn waste into wealth.
Claims (25)
1. a treatment process for dyestuff acid waste water, described method comprises the following steps:
(a) classification is processed: by the Waste Sulfuric Acid producing in DYE PRODUCTION or waste hydrochloric acid according to sour content categorised collection in collecting tank;
(b) neutralization, absorption: by Waste Sulfuric Acid or the waste hydrochloric acid of the regulation content of gained in step (a), in proceeding to continuously and in still, simultaneously continuously in and in still, feed alkali and neutralize, by online pH meter control pH value, neutralizer flow to absorption still, in absorption still, add sorbent material to adsorb continuously and automatically according to flooding velocity simultaneously, the mixed solution after absorption is filtered through pressure filter;
(c) micro-electrolysis: the filtrate obtaining in step (b) is gone in micro cell and carries out redox, control the hydraulic detention time in micro cell simultaneously;
(d) coagulating sedimentation: in step (c), the water outlet of micro cell flow to coagulation still, adds continuously the liquid material that comprises coagulating agent and flocculation agent simultaneously, stirs; Then by mixed solution through Filter Press;
(e) charcoal absorption: the filtrate obtaining in step (d) is gone to activated carbon column and decolour, take off organic adsorption treatment, control hydraulic detention time, the mixed solution after absorption flows in storage tanks and stores;
(f) condensing crystal: the mixed solution in storage tanks in step (e) is gone to evaporation equipment concentrates, crystallization, through centrifugation, obtain sodium sulfate, ammonium sulfate, sodium-chlor or ammonia chloride crystal, collect distillation water outlet simultaneously and recycle.
2. the method for claim 1, characterized by further comprising: (g) advanced treatment, and after processing, BAF make water outlet reach service water reuse standard the distillation water outlet of collecting in step (f), enter service water reuse tank.
3. method as claimed in claim 1 or 2, to be wherein calculated in mass percent be 10%～20% to the regulation content described in step (b).
4. method as claimed in claim 1 or 2, it is characterized in that: in step (a), Waste Sulfuric Acid is carried out to categorised collection by the concentration rank of mass percent 2%～10%, 10%～20%, 20%～75%, and waste hydrochloric acid is pressed the concentration rank categorised collection of mass percent 2%～10%, 10%～20%.
5. method as claimed in claim 1 or 2, it is characterized in that, in step (a), Waste Sulfuric Acid, waste hydrochloric acid that also to comprise the mass percent of collection be 2%～10% are concentrated into 10%～20% by evaporation equipment, and the Waste Sulfuric Acid that is 10%～20% by mass percent or waste hydrochloric acid are for step (b); The spent acid that exceedes 20% content after pretreatment reuse to DYE PRODUCTION.
6. method as claimed in claim 1 or 2, is characterized in that in step (b), and described spent acid flooding velocity, alkali adds inbound traffics and pH value tripartite automatic interlock; Control the scope of pH value to 8.1～9.5; Described alkali is to be selected from one or more in sodium hydroxide, sodium carbonate, liquefied ammonia or ammoniacal liquor; Described sorbent material by cage device continuous uniform feed intake, add-on and the automatic interlock of absorption still flooding velocity, described sorbent material is to be selected from one or more in carclazyte, wilkinite, silica gel, clay, activated alumina, zeolite, Powdered Activated Carbon, with respect to flooding velocity, the mass ratio that adds sorbent material is 0.1%～6%.
7. method as claimed in claim 1 or 2, wherein in step (c), hydraulic detention time control is 0.5～4 hour.
8. method as claimed in claim 1 or 2, it is characterized in that in step (d), described coagulating agent and the add-on of flocculation agent are by on-line automatic Controlling System and coagulation still flooding velocity interlocking, institute adds coagulating agent for being selected from aluminum chloride, polymerize aluminum chloride, Tai-Ace S 150, ferrous sulfate, poly-ferric chloride, one or more in aluminium iron polychloride, with respect to flooding velocity, the mass ratio that adds coagulating agent is 0.2%～5%, the concentration of coagulant solution is 2%～20%, flocculation agent is polyacrylamide, with respect to flooding velocity, the mass ratio that adds flocculation agent is 0.02%～2%, the concentration of flocculant solution is 0.1%～0.5%.
9. method as claimed in claim 1 or 2, is characterized in that, the activated carbon granule particle diameter in step (e) in activated carbon column is 0.5mm～5mm.
10. method as claimed in claim 1 or 2, is characterized in that, in step (e), hydraulic detention time control is 0.5～4 hour.
11. methods as claimed in claim 9, is characterized in that the activated carbon column described in step (e) is 2 grades of above activated carbon columns, and activated carbon column water outlet is carried out endpoint monitoring through online colourity monitor.
12. methods as claimed in claim 11, it is characterized in that, the process that the online colourity monitor of step (e) carries out terminal control is: in the time that activated carbon column effluent color dilution is below 10 times, water outlet flows in storage tanks, in the time that colourity is more than 10 times, water outlet flows into next stage activated carbon column and proceeds decolouring processing, until effluent color dilution flows in storage tanks 10 times of following rear water outlets.
13. methods as claimed in claim 1 or 2, is characterized in that, in step (f), evaporation equipment is MVR equipment.
14. methods as claimed in claim 5, is characterized in that, step (a) and (f) described in evaporation equipment be MVR equipment, the distillation water outlet of evaporation equipment through BAF process after make water outlet reach industrial reuse water quality standard.
15. the method for claim 1, it is characterized in that it is 10%～20% that mass percent is 2%～10% in described collecting tank (A) spent acid first uses a MVR equipment (S1) to be concentrated into mass percent, by 10%～20% spent acid pump in and still (B) neutralize, after neutralization, solution enters absorption still (C), add sorbent material to adsorb by cage device (W) simultaneously, then overflow is to transfer still (D), pump to the first pressure filter (E) filters again, filtrate is after micro cell (G) redox, carry out coagulation from flowing to coagulation still (H), mixed solution overflow is to transfer still (J), pump to the second pressure filter (L) filters, filtrate after more than 1 grade or 2 grades activated carbon column decoloring overflow to storage tanks (Q), and pump to the two MVR equipment (S2) concentrate, crystallization, separate and obtain sodium sulfate finally by whizzer (T), ammonium sulfate, sodium-chlor or ammonium chloride, collect distillation water outlet simultaneously, after advanced treatment, be back to production.
The treatment unit of the dyestuff acid waste water using in method described in 16. 1 kinds of claim 1～15 any one, comprising:
Collecting tank (A), carries out categorised collection for Waste Sulfuric Acid or waste hydrochloric acid that DYE PRODUCTION is produced;
In and still (B), for be 10%～20% by mass percent Waste Sulfuric Acid or waste hydrochloric acid and alkali neutralization;
Absorption still (C), carries out adsorption treatment for neutralizer and the sorbent material adding of self-neutralization still in future (B);
The first pressure filter (E), carries out press filtration for the mixed solution to after adsorption treatment;
Micro cell (G), carries out redox processing for the filtrate that press filtration obtains to the first pressure filter (E);
Coagulation still (H), for adding the liquid material that comprises coagulating agent and flocculation agent to carry out coagulation to the water outlet of micro cell (G);
The second pressure filter (L); For the mixed solution after coagulation is carried out to press filtration;
More than 1 grade or 2 grades activated carbon column, for carrying out adsorption treatment to the filtrate of the second pressure filter (L) press filtration gained;
Storage tanks (Q), for storing the filtrate after adsorption treatment;
The 2nd MVR equipment (S2), the water outlet for concentrated, crystallization from storage tanks (Q);
Whizzer (T), for by the solid of enriched material, liquid separation;
BAF, for processing the distillation water outlet of the 2nd MVR equipment (S2) to make it reach service water reuse standard.
17. devices as claimed in claim 16, also comprise:
The one MVR equipment (S1), waste acid concentration to the concentration mass percent that is 2%～10% for the mass percent that collecting tank (A) is collected is 10%～20%; BAF, for processing the distillation water outlet of a MVR equipment (S1) to make it reach service water reuse standard.
18. devices as described in claim 16 or 17, it is characterized in that, by the 3rd volume pump (P3) in and in still (B), be continuously pumped into spent acid, by the 4th volume pump (P4) continuously in and in still (B), pump into alkali, detect pH value by online pH meter, wherein, the 3rd volume pump (P3), the 4th volume pump (P4) and pH meter tripartite are carried out to automatic linkage control.
19. devices as described in claim 16 or 17, it is characterized in that, neutralizer after neutralization goes to absorption still (C) continuously through first flow meter (F1), and in absorption still (C), feed sorbent material continuously by cage device (W), wherein, the solid measuring apparatus of first flow meter (F1) and cage device (W) is carried out to automatic linkage control.
20. devices as claimed in claim 18, it is characterized in that, neutralizer after neutralization goes to absorption still (C) continuously through first flow meter (F1), and in absorption still (C), feed sorbent material continuously by cage device (W), wherein, the solid measuring apparatus of first flow meter (F1) and cage device (W) is carried out to automatic linkage control.
21. devices as described in claim 16 or 17, it is characterized in that, water outlet in micro cell (G) after redox, proceed to continuously coagulation still (H) through the second under meter (F2), and in coagulation still (H), pump into the liquid material containing coagulating agent and flocculation agent continuously by the tenth volume pump (P10), wherein, the second under meter (F2) and the tenth volume pump (P10) are carried out to automatic linkage control.
22. devices as claimed in claim 18, it is characterized in that, water outlet in micro cell (G) after redox, proceed to continuously coagulation still (H) through the second under meter (F2), and in coagulation still (H), pump into the liquid material containing coagulating agent and flocculation agent continuously by the tenth volume pump (P10), wherein, the second under meter (F2) and the tenth volume pump (P10) are carried out to automatic linkage control.
23. devices as claimed in claim 19, it is characterized in that, water outlet in micro cell (G) after redox, proceed to continuously coagulation still (H) through the second under meter (F2), and in coagulation still (H), pump into the liquid material containing coagulating agent and flocculation agent continuously by the tenth volume pump (P10), wherein, the second under meter (F2) and the tenth volume pump (P10) are carried out to automatic linkage control.
24. devices as claimed in claim 20, it is characterized in that, water outlet in micro cell (G) after redox, proceed to continuously coagulation still (H) through the second under meter (F2), and in coagulation still (H), pump into the liquid material containing coagulating agent and flocculation agent continuously by the tenth volume pump (P10), wherein, the second under meter (F2) and the tenth volume pump (P10) are carried out to automatic linkage control.
25. devices as described in claim 16 or 17, wherein said activated carbon column water outlet is carried out endpoint monitoring through online colourity monitor.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53129165A (en) * | 1977-04-18 | 1978-11-10 | Toshihiko Kobayashi | Waste water treatment by supersonic wave |
| JP2005169208A (en) * | 2003-12-09 | 2005-06-30 | Canon Inc | Method and apparatus for concentrating anionic material using adsorption and desorption support of anionic material |
| CN102260009A (en) * | 2010-05-29 | 2011-11-30 | 厦门理工学院 | Method for processing dye wastewater |
| CN102826673A (en) * | 2011-06-15 | 2012-12-19 | 浙江龙盛化工研究有限公司 | Cleaning treatment method of dying industrial acidic wastewater |
| CN202671337U (en) * | 2012-07-23 | 2013-01-16 | 上海将峰环保科技有限公司 | Printing and dyeing wastewater purifying device |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07124569A (en) * | 1993-11-08 | 1995-05-16 | Wasen Kogyo Kk | Decoloration treatment of printing/dyeing waste water |
| IL160384A (en) * | 2004-02-12 | 2007-10-31 | Edward Brook-Levinson | System and method for treatment of industrial wastewater |
| CN102050535B (en) * | 2010-11-10 | 2012-02-29 | 浙江大学 | Processing method for resource recovery of acidic dye waste water |
-
2013
- 2013-03-12 CN CN201310078739.XA patent/CN103130370B/en active Active
- 2013-03-12 CN CN201410078376.4A patent/CN103803754B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53129165A (en) * | 1977-04-18 | 1978-11-10 | Toshihiko Kobayashi | Waste water treatment by supersonic wave |
| JP2005169208A (en) * | 2003-12-09 | 2005-06-30 | Canon Inc | Method and apparatus for concentrating anionic material using adsorption and desorption support of anionic material |
| CN102260009A (en) * | 2010-05-29 | 2011-11-30 | 厦门理工学院 | Method for processing dye wastewater |
| CN102826673A (en) * | 2011-06-15 | 2012-12-19 | 浙江龙盛化工研究有限公司 | Cleaning treatment method of dying industrial acidic wastewater |
| CN202671337U (en) * | 2012-07-23 | 2013-01-16 | 上海将峰环保科技有限公司 | Printing and dyeing wastewater purifying device |
Non-Patent Citations (1)
| Title |
|---|
| 马宏瑞等: "高浓度分散染料废水电渗析脱盐可行性试验", 《水处理技术》, vol. 38, no. 6, 10 June 2012 (2012-06-10) * |
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| Publication number | Priority date | Publication date | Assignee | Title |
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Also Published As
| Publication number | Publication date |
|---|---|
| CN103130370A (en) | 2013-06-05 |
| CN103130370B (en) | 2014-03-26 |
| CN103803754B (en) | 2016-03-30 |
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