CN101565257A - Method and device for treating and purifying sewage in a membrane coupling way - Google Patents
Method and device for treating and purifying sewage in a membrane coupling way Download PDFInfo
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- CN101565257A CN101565257A CNA2008100528619A CN200810052861A CN101565257A CN 101565257 A CN101565257 A CN 101565257A CN A2008100528619 A CNA2008100528619 A CN A2008100528619A CN 200810052861 A CN200810052861 A CN 200810052861A CN 101565257 A CN101565257 A CN 101565257A
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Abstract
The invention provides a device and a method for treating and purifying high-concentration industrial sewage in a membrane coupling way. Raw water primarily enters a membrane evaporation tank for primary circulation evaporation, alkali is added into overflowed concentrated water, primary reaction filtration is performed in an immersing ultrafiltration reactor, filtered water enters a secondary membrane evaporation tank for secondary circulation evaporation after being pumped by a pump, and overflowed concentrated water enters a secondary immersing ultrafiltration reactor for reaction filtration after alkali and flocculating agent are added. A membrane evaporation assembly adopts a hollow fiber membrane assembly with a casing, and is vertically immersed into or half immersed into an evaporation tank, hot water enters from a lower opening of the hollow fiber membrane assembly through the pumping of the circulation pump and is upwards pumped out through a tube pass, and the hot water is circulated and evaporated through a reducing membrane. The membrane evaporation tanks are internally provided with baffle plates, and supernatant liquid after being settled primarily enters membrane regions through the baffle plate, thereby the membrane pollution is reduced. The invention greatly reduces the sewage emission, lowers the operation cost of a membrane evaporation and concentration system, realizes the purification and the recycling of the industrial sewage and achieves the purposes of saving water and reducing the emission. The invention can concentrate the reverse osmosis by about 100 times usually and can greatly reduce the sewage emission. Concentrated liquid and sludge can be directly dried by a general evaporator so as to achieve zero emission.
Description
Technical field
The present invention relates to a kind of water treatment system and treatment process, relate in particular to the film coupling purifying treatment method that industrial sewage purification is handled.
Background technology
Recirculated cooling water is the water sport in the process water, and in industries such as petrochemical complex, electric power, iron and steel, metallurgy, the consumption of recirculated cooling water accounts for the 50-90% of enterprise water use total amount, and the water coolant of some power plant, chemical enterprise accounts for the 90-95% of total water amount.Recirculated cooling water is in system constantly recycles, because the variation of water temperature, flow velocity, moisture constantly evaporates, and mineral ion and organism concentrate gradually, the Ca in the water
2+, Mg
2+, Cl
-The corresponding increase of plasma, dissolved solids and suspended substance, pollutent such as dust, foreign material, soluble gas and the leakage of interchanger material etc. in the air in addition, cause that circulating cooling water quality degenerates, cause equipment generation incrusted deposit and corrosion such as water-cooled heat exchange, cause service efficiency and life-span to reduce, even the normal operation of the system of obstruction.In order to prevent calcium, separating out of magnesium ion incrustation scale, reduce the influences of dirt to conducting heat such as walk impurity, multiplying of metallic corrosion of Control Circulation cooling water system and Control Circulation cooling water system microorganism, effective and the most the most frequently used method then is to add a large amount of inhibiter in recirculated water at present, Scale inhibitors, dispersion agent, chemical agents such as biocide, but these traditional treatment method, can not fundamentally solve salt and organism and concentrate the variety of issue that causes, and add the operating system complexity of various water conditioners, medicament expense makes the overall cycles of concentration of recirculated water not high with high, the operational management cost is very high.
After general sewage was handled through I and II, total suspended solid removed 70%～80%, and BOD removes 80%～90%, basically, reach emission standard, but second-stage treatment can not be removed some pollutents, comprising microorganism, and the organism of failing to degrade, phosphorus, fluorine and solubility inorganics.At present, the resource utilization of municipal effluent and trade effluent has become the development trend of the world today.Normally after the biochemical treatment of routine, adopt ultrafiltration or micro-filtration to add reverse osmosis, make most sewage obtain cleansing and recycling again, but, adopt reverse osmosis technology, still there are two problems: the one, reverse osmosis technology is to processed water quality pre-treatment requirement height, common requirement employing is super, the micro-filtration technology is handled as prime, and former water temp must not be higher than 40 ℃ usually, causes the high and working cost height of facility investment, the 2nd, the water recovery utilization rate is low, generally can only reach about 70%, still have 30% left and right sides concentrated water discharge, quantity discharged is big.
Therefore,, study new water technology, reduce investment and working cost, improve the utilization ratio of water, reduce sewage discharge, can obtain remarkable economic efficiency and social benefit at high density sewage such as industrial circulating water, second pond discharge water, reverse osmosis concentrated waters.
(Membrane Distillation MD) has attracted worldwide concern and research to membrane distillation in recent years.Compare with distillation (Distillation) process of routine, the service temperature of MD is low, need not solution is heated to boiling, and evaporation area is big, the vapour space is little; Compare with other pressure-actuated membrane sepn process, the working pressure of MD is low, the ratio of desalinization height, and film pollutes few.It is low that the MD technology has a working pressure, non-volatile substance decreasing ratio near 100% and under the excellent operation condition with high product water flux, shown its application potential that substitutes (extensive pure water preparation) or additional technology (as being used for boats and ships tap water etc.), can be used for sea water desaltination and concentrated salt manufacturing, industrial circulating water and purify in aspects such as product condensing crystal such as minimizing sewage discharge, fermented liquid amino acid and medicine purifies and separates as the RO technology.The special advantages that film distillation technology is applied to the industrial cycle water treatment is that it not only can produce pure water in the side that sees through of film, and it is very high even near saturated height condensed water to produce saltiness in dense water side, highly spissated sewage then can further adopt other physical chemistry methods such as chemical flocculation to handle, thereby significantly reduces the sewage emissions amount.
Summary of the invention
The objective of the invention is to overcome defective of the prior art, a kind of high-concentration industrial sewage film coupling purification process technique apparatus and method are provided.
The invention provides a kind of film coupling treatment unit of purifying waste water, comprise two filtration treatment, it is characterized in that comprise: first step film evaporation tank 5 is used for the first step and filters, handles the former water through preheating; The steam outlet 43 of above-mentioned first step film evaporation tank 5 is connected to first step condensing unit 111, is used for condensation, recovered steam; Behind the dense water outlet 46 process first step chemicals dosing plants of first step film evaporation tank 5, be connected to above-mentioned first step immersion ultrafiltration reaction filtering basin 7; In above-mentioned first step immersion ultrafiltration reaction filtering basin 7, mixed solution continues to mix, reaction; The relief outlet of first step immersion ultrafiltration reaction filtering basin 7 communicates with second stage film evaporation tank 10 pipelines, and above-mentioned second stage film evaporation tank 10 is used for two not good liquors are carried out second stage evaporation process; The steam outlet 54 of second stage film evaporation tank 10 is connected to second stage condensing unit 222; The dense water outlet of second stage film evaporation tank 10 through second stage chemicals dosing plant after, be connected to second stage immersion ultrafiltration reaction filtering basin 12; The outlet pipe of above-mentioned second stage immersion ultrafiltration reaction filtering basin 12 is connected to second stage film evaporation tank 10, treatment solution is turned back to continue evaporation process in the membrane cisterna.
Be connected with heat pump 3 on the first step film evaporation tank 5, heat pump 3 connects the outlet of former water prefilter 2; The cold junction interface 70 of heat pump 3 is connected with the cold junction inlet 65 of the interchanger 4 of first step condensing unit 111; The hot water outlet 69 of heat pump 3 is connected to the former water inlet 41 of film evaporation tank 5 by pipeline; Above-mentioned cold junction liquid of drawing from heat pump 3 enters interchanger 4, makes to draw the steam cooling that interface 43 draws from film evaporation tank 5 steam and condense, and returns heat pump 3 former water inlets by interchanger 4 cold side outlets 66 again.
Include in first step film evaporation tank 5 and the second stage film evaporation tank 10: be arranged on the film unit 27,34 in the film evaporation tank 5,10; Hang down as for the dividing plate 28,37 of film evaporation tank 5,10 diapires, aforementioned barriers 28,37 is divided into preliminary sedimentation district and film district with film evaporation tank 5,10, and above-mentioned film unit 27,34 is arranged on the film district; Hang down as for the high-order upflow tube 29,38 of film evaporation tank 5,10 diapires, above-mentioned high-order upflow tube 29 is arranged at the preliminary sedimentation district of film evaporation tank; Be provided with heater block 30,35 in the bottom of above-mentioned film unit 27,34, former water is heated; The top set handling liquid import 41,57 of film evaporation tank 5,10, the stoste import is incorporated into the preliminary sedimentation district with stoste; Film evaporation tank 5,10 tops also are provided with hot water and extract mouth 42,53 out, will extract out from the hot water that film unit 27,34 is discharged; Hot water return port 44,55 pipes that above-mentioned hot water is extracted out on mouth 42,53 and film evaporation tank 5,10 diapires connect, and recycle hot water; On the pipeline between above-mentioned hot water extraction mouth 42,53 and the hot water return port 44,55, recycle pump 26,33 is set; On the diapire in the preliminary sedimentation district of above-mentioned film evaporation tank 5,10 slag-drip opening is set also, is used for dense slag is discharged; Above-mentioned high-order upflow tube 29,38 leads to the outside of film evaporation tank 5,10; At the sidepiece of film evaporation tank 5,10 steam is set and draws the steam that interface 43,53 is used for drawing film evaporation tank 5.
The steam outlet of first step film evaporation tank 5 and second stage film evaporation tank 10 divides no matter is connected to the first step condensing unit 111 and second condensing unit 222; Above-mentioned condensing unit 111,222 comprises: interchanger 4,15; Be connected in the gas-liquid separator 16,21 of interchanger 4,15 outlets; The temporary container 18,23 of the liquid outlet of above-mentioned gas-liquid separator 16,21 and distilled water is connected, and after the steam of interchanger discharging is condensed, is temporarily stored in the temporary container of distilled water; The steam side outlet of above-mentioned gas-liquid separator 16,21 connects vacuum pump 20, steam is summarized in the vapour outlet (43,54) of film evaporation tank 5,10.
The dense water outlet of film evaporation tank 5,10 through buck dosing mouth 47,58 after, pipe is connected to and adds alkali line mixer 6,11,6,11 pairs of dense water of above-mentioned mixing tank and remove the hard base aqueous solution and mix; Above-mentioned outlet and the immersion ultrafiltration reaction filtering basin 7,61 that add alkali line mixer 6,11 are connected; Above-mentioned immersion ultrafiltration is reacted the outlet of filtering basin 7,12 through behind the acid-adding port 51,63, is connected to add acid tube road mixing tank 9,14, adds the mixed solution continuation mixing after 9,14 pairs in acid tube road mixing tank adds acid.
Be provided with in the immersion ultrafiltration reaction filtering basin 7,12 and see through submerged ultrafiltration assembly 31,39, above-mentioned membrane module is no shell submerged ultrafiltration; Through submerged ultrafiltration assembly 31,39 belows boring aeration pipe 32,40 is being set, mixing water continues down to mix, react in the bubble effect of boring aeration pipe 32,40 dischargings; Filtering basin 7,12 tops are set to the ultra-filtration membrane filtered solution and extract mouthfuls 49,61 out, lift pump 8,13 are set with extracting out on the pipeline that mouthful 49,61 pipes connect, and, link to each other with the inlet that adds acid tube road mixing tank 9,14 by acid-adding port 51,63 in lift pump 8,13 outlets; 51,63 places add acid at above-mentioned acid-adding port, recall to the pH value of mixing water after, mixing water enters and adds acid tube road mixing tank; The acid amount that adds that online pH meter 52,64 is used to control the acid-adding port place is set in the exit that adds acid tube road mixing tank.
Interchanger is the tubular fibre interchanger, and the tubular fibre material adopts polyvinylidene fluoride material, and polyvinylidene difluoride (PVDF) tubular fibre, internal diameter are 0.2-3.0mm, and wall thickness is 0.05-1.0mm, according to the difference of treatment capacity, and the in parallel or series connection use simultaneously of a plurality of membrane modules.
The present invention also provides a kind of film coupling purified water processing method, it is characterized in that comprise: former water at first enters first step film evaporation tank and carries out first step circulating and evaporating; Add alkali in the dense water that in first step film evaporation tank, overflows, then mixed solution is incorporated in the first step immersion ultrafiltration reactor, carry out first step reaction and filter in first step immersion ultrafiltration reactor, cleaner liquid is drawn out of and enters second stage film evaporation tank and carry out second stage circulating and evaporating; After the dense water that overflows from the film evaporation tank of the second stage adds alkali and flocculation agent, enter in the immersion ultrafiltration reactor of the second stage and react filtration.
Obtain following effect by the present invention:
1, the film evaporative component among the present invention adopts the pillar hollow fiber film assembly of band shell, vertical immersion or partly be immersed in the evaporation tank by the suction of recycle pump, is entered hot water by the hollow fiber film assembly end opening, upwards extract out through tube side, the film evaporation of reducing pressure circulates.Steam is extracted out from the upside mouth of membrane module, if film produces seepage because of hydrophilization, effusion can be discharged from membrane module downside mouth.Membrane module places evaporation tank to be incubated membrane module easily, prevents to see through steam condensation in membrane module of film.
2, the present invention is provided with dividing plate in the film evaporation tank, covers dividing plate through the supernatant liquor after the pre-sedimentation and enters the film district, can decelerating membrane pollution.
3, the present invention adds alkali again and removes hardness after process first step evaporation concentration, and have following benefit: the alkali number of consumption is few, hardness is removed the rate height.But if cycles of concentration is too high, then can cause membrane flux to descend fast, therefore, pre-concentration of the present invention 1.5～5 times (preferred 1.5～2.5) doubly after, add alkali and carry out chemistry and remove firmly.
4, the present invention through 3～10 times of second stage film evaporation tank reconcentration after, a part is directly discharged, a part is proceeded chemical treatment.Because COD concentration increases in the water, learn to remove and also need to add flocculation agent in hard and carry out chemical flocculation adding alkalization, remove organic pollutant.Chemistry removes hard-condition: NaOH800～1200mg/L, Na
2CO
3200～600, after hard, calcium, magnesium ion concentration all are lower than 100mg/L, preferably are lower than 50mg/L.When small-molecule substance content is higher in the COD constituent, also needs to add gac and adsorb low molecule organic matter.Flocculation agent can adopt the conventional flocculation agent of water treatment, as inorganic flocculating agents such as iron(ic) chloride, polyaluminium sulfate, bodied ferric sulfates, or organic floculants such as polyacrylamide, modified polyacrylamide, the present invention does not do qualification at this.Through chemistry remove hard and flocculation absorption after, clear liquid COD should be lower than 200mg/L, the preferred COD of the present invention is lower than 100mg/L.Behind the immersion ultrafiltration reactor of the second stage, the ultrafiltration cleaner liquid returns second stage film evaporation tank again.
5, the present invention adopts heat pump that former water is preheated, the cold junction liquid of discharging then enters interchanger 4 and makes through the steam cooling of film 27 and condense, such structure is particularly useful for handling with the recirculated cooling water of used heat, utilizes recirculated water used heat can reduce system energy consumption greatly.Also can adopt heat pump techniques that other water source used heat is reclaimed.Heat pump can be selected the heat pump of compression heat pump, absorption heat pump or other principle for use, and the present invention does not do qualification at this, the preferred mechanical compression heat pump.
For the common industrial sewage reverse osmosis concentrated water after the purifying treatment again, adopt the technology of the present invention, generally about 100 times of reverse osmosis reconcentration can be significantly reduced wastewater discharge.Concentrated solution and mud can directly be used conventional evaporator dry, accomplish zero release.
Description of drawings
Fig. 1 is a high-concentration industrial sewage film coupling purification process technique device synoptic diagram of the present invention.
Fig. 2 is a film evaporative component synoptic diagram used in the present invention.
Embodiment
System of the present invention as shown in Figure 1.See that on the whole high-concentration industrial sewage film of the present invention coupling purification process technique system comprises two filtration treatment, mainly by constituting with lower member: first step film evaporation tank 5 is used for the first step and filters, handles the former water through preheating; First step condensing unit 111 with the steam outlet of above-mentioned first step film evaporation tank 5 is connected is used for condensation, recovered steam; Behind the dense water outlet process first step buck dosing mouth 47 of first step film evaporation tank 5, pipe is connected to the first step and adds alkali line mixer 6, and the 6 pairs of dense water of above-mentioned mixing tank and the first step are removed the hard base aqueous solution and mixed; The outlet that the above-mentioned first step adds alkali line mixer 6 is connected with first step immersion ultrafiltration reaction filtering basin 7, and in above-mentioned first step immersion ultrafiltration reaction filtering basin 7, mixed solution continues to mix, reaction; Behind the outlet process first step acid-adding port 51 of above-mentioned first step immersion ultrafiltration reaction filtering basin 7, be connected to the first step and add acid tube road mixing tank 9, the first step adds the mixed solution continuation mixing after 9 pairs in acid tube road mixing tank adds acid.Through after the above-mentioned processing, former water is finished first step filtration treatment.
The relief outlet that the first step adds acid tube road mixing tank 9 connects second stage film evaporation tank 10, and it is used for second stage evaporation process; Second stage condensing unit 222 is connected to the steam outlet of second stage film evaporation tank 10; The dense water outlet of second stage film evaporation tank 10 through second stage buck dosing mouth 59 after, be connected to the second stage and add alkali line mixer 11; The outlet that the above-mentioned second stage adds alkali line mixer 11 is connected to second stage immersion ultrafiltration reaction filtering basin 12; The outlet 61 of above-mentioned second stage immersion ultrafiltration reaction filtering basin 12 adds acid tube road mixing tank 14 through the second stage acid-adding port 63 and the second stage and is connected; The relief outlet pipe that the second stage adds acid tube road mixing tank 14 is connected to second stage film evaporation tank 10, continues evaporation.
More than, specifically describe each building block of cleaning treatment system of the present invention below for describing high-concentration industrial sewage film coupling cleaning treatment system of the present invention on the whole.
As shown in Figure 1, the film of the present invention coupling former water prefilter 2 that treatment unit connects successively of purifying waste water; Heat pump 3; Interchanger 4; First step film evaporation tank 5.Above-mentioned heat pump 3 is connected with former water prefilter 2 outlets; The cold junction interface 70 of heat pump 3 is connected with the cold junction of interchanger 4 inlet 65, the hot water outlet 69 of heat pump 3 is connected to the former water inlet 41 of film evaporation tank 5 by pipeline, above-mentioned cold junction liquid of drawing from heat pump 3 enters interchanger 4, make and draw the steam cooling that interface 43 draws from film evaporation tank 5 steam and condense, return heat pump 3 former water inlets by interchanger 4 cold side outlets 66 again.Can also drain into water cooling pond by interchanger 4 cold side outlets 66 for industrial circulating cooling water.
Describe the structure of first step film evaporation tank 5 below in detail.In the film evaporation tank 5, comprising: be arranged on the film unit 27 in the film evaporation tank 5, hang down as for the dividing plate 28 of film evaporation tank 5 diapires, aforementioned barriers 28 is divided into preliminary sedimentation district and film district with film evaporation tank 5, and above-mentioned film unit 27 is arranged on the film district; Hang down as for the high-order upflow tube 29 of film evaporation tank 5 diapires, above-mentioned high-order upflow tube 29 is arranged at the preliminary sedimentation district of film evaporation tank.In addition, be provided with heater block 30, former water is heated in the bottom of above-mentioned film unit 27.Film evaporation tank 5 tops are provided with stoste import 41, and the stoste import is incorporated into the preliminary sedimentation district with stoste, and film evaporation tank 5 tops also are provided with hot water and extract mouth 42 out, will extract out from the hot water that film unit 27 is discharged.By above-mentioned stoste import 41, introduce the former water through preheating of discharging from heat pump 3 hot water outlets 69, extract mouth 42 out by hot water, hot water is discharged to the hot water return port 44 that is arranged on film evaporation tank 5 diapires, recycle hot water.On the pipeline between above-mentioned hot water extraction mouth 42 and the hot water return port 44, recycle pump 26 is set.On the diapire in the preliminary sedimentation district of above-mentioned film evaporation tank 5 slag-drip opening 45 is set also, is used for dense slag is discharged.Above-mentioned high-order upflow tube 29 leads to the outside of film evaporation tank 5, has dense water outlet 46.At film evaporation tank 5 sidepieces steam is set and draws interface 43, be used for drawing the steam of film evaporation tank 5.
Describe the structure that is arranged on the film evaporative component in the film evaporation tank in detail below in conjunction with Fig. 2.In Fig. 2, the film evaporative component comprises membrane module shell 71, is arranged on the film silk 72 in the film shell, film evaporative component bottom casting epoxy resin 75, and the top is provided with hot water outlet 73, and sidepiece is provided with steam outlet 74.Above-mentioned hot water outlet 73 connects hot water and extracts mouth 42 out, and above-mentioned steam outlet 74 connects steam and draws interface 43.
The treating processes of former once water in film evaporation tank 5 is described below.
Be connected to the former water inlet 41 of film evaporation tank 5 by the pre-warmed former water of heat pump by hot water outlet 69, after entering the preliminary sedimentation district and carrying out preliminary natural subsidence, supernatant liquor covers dividing plate 28 and enters the film district.Film evaporative component 27 adopts the pillar hollow fiber film assembly of band shells, and vertical immersion or partly be immersed in the hot water of evaporation tank is by the suction of recycle pump 26, hot water is entered by the hollow fiber film assembly end opening, make progress, from extracting mouthful 42 extractions out through tube side, returned by import 44, circulation is carried out again.The dense water that overflows is drawn by outlet 46.
The steam outlet pipe of first step film evaporation tank 5 is connected to first step condensing unit 111.Above-mentioned first step condensing unit 111 comprises above-mentioned interchanger 4, is connected in the gas-liquid separator 16 of interchanger 4 tube sides outlet, and the liquid outlet of above-mentioned gas-liquid separator 16 is connected by the temporary container 18 of valve 17 and distilled water.After the steam of interchanger 4 dischargings is condensed, be temporarily stored in the temporary container 18 of distilled water.Distilled water in the temporary container 18 of distilled water discharges under the control of valve 19.The steam side outlet of above-mentioned gas-liquid separator 16 connects vacuum pump 20, steam is summarized in the vapour outlet 43 of film evaporation tank 5.
Among the present invention, also to carrying out the dosing of first step buck from the first step film evaporation tank 5 outlets 46 dense water of drawing.First step buck dosing mouth 47 is set on the pipeline that is connected in dense water outlet 46, quantitatively adds from above-mentioned dosing mouth 47 and remove the hard base aqueous solution.Through behind the dosing mouth 47, above-mentioned pipeline is connected to the first step and adds alkali line mixer 6.After in line mixer 6, mixing dense water and removing the hard base aqueous solution, mixing water is entered first step immersion ultrafiltration reaction filtering basin 7 by the interface 48 that is arranged on the immersion ultrafiltration reaction filtering basin 7.
Be provided with in the first step immersion ultrafiltration reaction filtering basin 7 and see through submerged ultrafiltration assembly 31, above-mentioned membrane module is no shell submerged ultrafiltration.Below seeing through submerged ultrafiltration assembly 31 boring aeration pipe 32 is set, mixing water continues to mix under the bubble effect of boring aeration pipe 32 dischargings, reaction.Filtering basin 7 tops are set to the ultra-filtration membrane filtered solution and extract mouthfuls 49 out, lift pump 8 are set with extracting out on the pipeline that mouthful 49 pipes connect.By first step acid-adding port 51, the inlet that adds acid tube road mixing tank 9 with the first step links to each other in lift pump 8 outlets.51 places add acid at acid-adding port, recall to the pH value of mixing water after, mixing water enters the first step and adds acid tube road mixing tank 9.The outlet that adds acid tube road mixing tank in the first step can locate to be provided with online pH meter 52, is used to control the acid amount that adds at acid-adding port 51 places.
In addition, the boring aeration pipe 32 in immersion ultrafiltration reaction filtering basin 7 be an intermittent aeration, prevents Pollution of Ultrafiltration Membrane, and aeration tube has enough height bottom reaction tank, make most of mud flco can be when stopping aeration natural subsidence.In several aeration periods, when certain being set once stopping aeration, carry out automatic sludge discharge by the outlet 50 that is arranged on filtering basin 7 bottoms.
The mixed solution of discharging from first step mixing tank 9 enters second stage film evaporation tank 10.The similar of second stage film evaporation tank 10 is in first step film evaporation tank 5, also comprise: be arranged on the film unit 34 in the film evaporation tank 10, hang down as for the dividing plate 37 of film evaporation tank 10 diapires, aforementioned barriers 37 is divided into preliminary sedimentation district and film district with film evaporation tank 10, and above-mentioned film unit 34 is arranged on the film district; Hang down as for the high-order upflow tube 38 of film evaporation tank 10 diapires, above-mentioned high-order upflow tube 38 is arranged at the preliminary sedimentation district of film evaporation tank.In addition, be provided with heater block 35, former water is heated in the bottom of above-mentioned film unit 34.Film evaporation tank 10 tops are provided with two not good liquor liquid imports, 57, two not good liquor imports two not good liquor liquid are incorporated into the preliminary sedimentation district, and film evaporation tank 10 tops also are provided with hot water and extract mouth 53 out, will extract out from the hot water that film unit 37 is discharged.By above-mentioned two not good liquor imports 57, introduce that line mixer 52 discharges through two not good liquors, extract mouthfuls 53 out by hot water, hot water is discharged to the hot water return port 55 that is arranged on film evaporation tank 10 diapires of the second stage, recycle hot water.On the pipeline between above-mentioned hot water extraction mouth 53 and the hot water return port 55, recycle pump 33 is set.On the diapire in the preliminary sedimentation district of above-mentioned film evaporation tank 10 slag-drip opening 56 is set also, is used for dense slag is discharged.Above-mentioned high-order upflow tube 38 leads to the outside of film evaporation tank 10, has dense water outlet.At film evaporation tank 10 sidepieces steam outlet 54 is set, is used for drawing the steam of film evaporation tank 10.
In addition, according to concrete service condition, first step condensing unit 111 can be separate part with second stage condensing unit 222, also can be a shared fully cover steam cooling separating component.
By after buck dosing mouth 59 dosings of the second stage, enter the second stage and add alkali line mixer 11 in the water of from second stage film evaporation tank 10, discharging.Second stage dosing and first step dosing difference are: except that adding alkali aqueous solution with except that hardness, also need to add flocculation agent even gac etc., enter second stage immersion ultrafiltration reaction filtering basin 12 then.
The outlet that the second stage adds alkali line mixer 11 is connected to the interface 60 on the roof that is arranged at second stage immersion ultrafiltration reaction filtering basin 12.
Second stage immersion ultrafiltration reaction filtering basin 12 are identical with first step filtering basin 7 structures, are provided with in filtering basin and see through submerged ultrafiltration assembly 39, and above-mentioned membrane module is no shell submerged ultrafiltration.Below seeing through submerged ultrafiltration assembly 39 boring aeration pipe 40 is set, mixing water continues to mix under the bubble effect of boring aeration pipe 40 dischargings, reaction.Filtering basin 12 tops are provided with the ultra-filtration membrane filtered solution and extract mouthfuls 61 out, lift pump 13 are set with extracting out on the pipeline that mouthful 61 pipes connect.Outlet at lift pump 13 connects by the inlet tube of second stage acid-adding port 63 with second stage line mixer 9.Add before the acid tube road mixing tank 11 entering the second stage, 63 places add acid at acid-adding port, recall to the pH value of mixing water after, mixing water enters the second stage and adds acid tube road mixing tank 9.The outlet that adds acid tube road mixing tank in the second stage can locate to be provided with online pH meter 64, is used for the acid amount that adds at acid-adding port 63 places.
Because the common fouling situation of interchanger is serious, the intermediary and later stages of regular circulation water system operation, often, also exist saltiness in service to increase in addition because serious fouling influences the heat exchange effect, corrode interchanger, and the bacterium algae such as grows at problem.In the present invention, can adopt conventional interchanger, but preferably adopt the tubular fibre interchanger, because of it has higher heat transfer area, and, the hollow-fibre membrane wall thickness is thinner, can offset the shortcoming that the macromolecular material thermal conductivity is lower than metal, simultaneously, the salt tolerant class corrodibility of macromolecular material is far above metallic substance, therefore, the expected service life of tubular fibre interchanger is long.The tubular fibre material can be macromolecular materials such as polyvinylidene difluoride (PVDF) or polypropylene, polyethylene.Preferably adopt polyvinylidene fluoride material as interchanger.The polyvinylidene difluoride (PVDF) tubular fibre, internal diameter: 0.2-3.0mm, wall thickness: 0.05-1.0mm.According to the difference of treatment capacity, can in parallel or series connection use simultaneously with a plurality of membrane modules.Interchanger 4,15 is formed one section side by side by many, and the multistage series connection constitutes one group.
Contact tubular fibre hydrophobic membrane in hydrophobic membrane adopts, the i.e. former water of side contacts in the hollow fiber film tube.Membrane material can be polyethylene, polypropylene, polyvinylidene difluoride (PVDF), tetrafluoroethylene, preferred polyvinylidene difluoride (PVDF) tubular fibre hydrophobic membrane, internal diameter: 0.2-3.0mm, wall thickness: 0.05-1.0mm.Film evaporator 5 is by many component film arranged side by side unit.
Heater block is set in the evaporation tank, and type of heating can be the interchanger heating, also can adopt steam or electrically heated rod direct heating.50～90 ℃ of film evaporation tank temperature, preferred 60～70 ℃.
Film evaporation tank cycles of concentration is the ratio that former water enters amount with the dense water yield of discharging membrane cisterna of membrane cisterna.
Describe film coupling purified water processing method of the present invention below in detail:
1, former water enters heat pump 3 through behind the prefilter 2, and the cold junction liquid of drawing from the interface 70 of heat pump 3 enters interchanger 4, and the steam cooling of drawing from film evaporation tank 5 interfaces 43 is condensed, and returns heat pump 3 former water inlets by interchanger 4 cold side outlets 66 again.Can also drain into water cooling pond by interchanger 4 cold side outlets 66 for industrial circulating cooling water.
2, be connected to the former water inlet 41 of film evaporation tank 5 by the pre-warmed former water of heat pump by hot water outlet 69, after the preliminary natural subsidence, supernatant liquor covers dividing plate 28 and enters the film district.Film evaporative component 27 adopts the pillar hollow fiber film assembly of band shells, and vertical immersion or partly be immersed in the hot water of evaporation tank is by the suction of recycle pump 26, hot water is entered by the hollow fiber film assembly end opening, make progress, extract out from exporting 42 through tube side, returned by import 44, circulation is carried out again.The dense water that overflows is drawn by outlet 46.Dense slag is discharged from dense slag outlet 45.
3, steam is extracted out from the upside mouth of membrane module under the suction function of vacuum pump 20, is summarized in film evaporation tank 5 vapour outlets 43, and pipe is connected to the tube side of interchanger 4, after the liquefaction that is condensed, via gas-liquid separator 16, flows into the temporary container 18 of distilled water.If film produces seepage because of hydrophilization, effusion can be discharged from membrane module downside mouth.Membrane module places evaporation tank to help membrane module is incubated, and prevents to see through steam condensation in membrane module of film.
4, for from the first step film evaporation tank 5 outlets 46 dense water of drawing, carry out first step dosing.Quantitatively added except that the hard base aqueous solution at pipeline 47 places, after mixing, line mixer 6 enters immersion ultrafiltration reaction filtering basin 7 by interface 48, under the effect of boring aeration pipe 32, continue to mix, react, under the suction of lift pump 8, see through submerged ultrafiltration assembly 31, after pipeline 51 places are added acid and recall to the pH value, enter line mixer 9.The acid amount that adds at online pH meter pilot piping 51 places is set at pipeline 52 places.Boring aeration pipe 32 is for intermittent aeration prevents Pollution of Ultrafiltration Membrane, and aeration tube has enough height apart from the reaction tank bottom, make most of mud flco can be when stopping aeration natural subsidence.In several aeration periods, carry out automatic sludge discharge by outlet 50 when certain being set once stopping aeration.
5, through adding 7 water outlets of sour mixed immersion ultrafiltration reaction filtering basin, be delivered to the import 57 of second stage film evaporation tank 10 by pump 8, carry out second stage evaporation.The same first step of its method.
6, steam is extracted out from the upside mouth of membrane module under the suction function of vacuum pump 25, is summarized in film evaporation tank 10 vapour outlets 54, and pipe is connected to the tube side of interchanger 15, after the liquefaction that is condensed, via gas-liquid separator 21, flows into the temporary container 23 of distilled water.
7, concentrate through second stage film evaporation tank 10 after, the dense water of drawing carries out second stage dosing.The same first step of method.Difference is: except that adding alkali aqueous solution with except that hardness, also need to add flocculation agent even gac etc., enter second stage immersion ultrafiltration reaction filtering basin 12 then.
8, the working method of second stage immersion ultrafiltration reaction filtering basin 12 is analogous to first step immersion ultrafiltration reaction filtering basin 7.
9, the ultrafiltration clear liquid of second stage immersion ultrafiltration reaction filtering basin 12 is by pump 13 suctions, add acid through pipeline 63 places, mix at line mixer 14, pipeline 64 is in line pH meter Monitoring and Controlling pipeline 63 places and adds the acid amount, return the water-in 58 of second stage film evaporation tank 10 again, continue evaporation.Owing to removal of impurity height in the water, can improve the multiple of second stage film evaporation concentration.
Behind 3～10 times of second stage film evaporation tank reconcentration, a part is directly discharged, and a part is proceeded chemical treatment.Because COD concentration increases in the water, learn to remove and also need to add flocculation agent in hard and carry out chemical flocculation adding alkalization, remove organic pollutant.Chemistry removes hard-condition: NaOH800～1200mg/L, Na
2CO
3200～600, after hard, calcium, magnesium ion concentration all are lower than 100mg/L, preferably are lower than 50mg/L.When small-molecule substance content is higher in the COD constituent, also needs to add gac and adsorb low molecule organic matter.Flocculation agent can adopt the conventional flocculation agent of water treatment, as inorganic flocculating agents such as iron(ic) chloride, polyaluminium sulfate, bodied ferric sulfates, or organic floculants such as polyacrylamide, modified polyacrylamide, the present invention does not do qualification at this.Through chemistry remove hard and flocculation absorption after, clear liquid COD should be lower than 200mg/L, the preferred COD of the present invention is lower than 100mg/L.The present invention is not directly discharging preferably, and concentrated solution is all proceeded chemical treatment.
Claims (8)
1, a kind of film coupling treatment unit of purifying waste water comprises two filtration treatment, it is characterized in that, comprising:
First step film evaporation tank (5) is used for the first step and filters, handles the former water through preheating;
The steam outlet (43) of above-mentioned first step film evaporation tank (5) is connected to first step condensing unit (111), is used for condensation, recovered steam;
Behind dense water outlet (46) the process first step chemicals dosing plant of first step film evaporation tank (5), be connected to above-mentioned first step immersion ultrafiltration reaction filtering basin (7);
In above-mentioned first step immersion ultrafiltration reaction filtering basin (7), mixed solution continues to mix, reaction;
The relief outlet of first step immersion ultrafiltration reaction filtering basin (7) communicates with second stage film evaporation tank (10) pipeline, and above-mentioned second stage film evaporation tank (10) is used for two not good liquors are carried out second stage evaporation process;
The steam outlet (54) of second stage film evaporation tank (10) is connected to second stage condensing unit (222);
The dense water outlet of second stage film evaporation tank (10) through second stage chemicals dosing plant after, be connected to second stage immersion ultrafiltration reaction filtering basin (12);
The outlet pipe of above-mentioned second stage immersion ultrafiltration reaction filtering basin (12) is connected to second stage film evaporation tank 10, treatment solution is turned back to continue evaporation process in the membrane cisterna.
2, the film according to claim 1 coupling treatment unit of purifying waste water is characterized in that:
Be connected with heat pump (3) on the first step film evaporation tank (5), heat pump (3) connects the outlet of former water prefilter (2);
The cold junction interface (70) of heat pump (3) is connected with the cold junction inlet (65) of the interchanger (4) of first step condensing unit (111);
The hot water outlet (69) of heat pump (3) is connected to the former water inlet (41) of film evaporation tank (5) by pipeline;
Above-mentioned cold junction liquid of drawing from heat pump (3) enters interchanger (4), makes to draw the steam cooling that interface (43) draws from film evaporation tank (5) steam and condense, and returns the former water inlet of heat pump (3) by interchanger 4 cold side outlets (66) again.
3, the film according to claim 1 coupling treatment unit of purifying waste water is characterized in that:
Include in first step film evaporation tank (5) and the second stage film evaporation tank (10):
Be arranged on the film unit (27,34) in the film evaporation tank (5,10);
Hang down as for the dividing plate (28,37) of film evaporation tank (5,10) diapire, aforementioned barriers (28,37) is divided into preliminary sedimentation district and film district with film evaporation tank (5,10), and above-mentioned film unit (27,34) is arranged on the film district;
Hang down as for the high-order upflow tube (29,38) of film evaporation tank (5,10) diapire, above-mentioned high-order upflow tube (29) is arranged at the preliminary sedimentation district of film evaporation tank;
Be provided with heater block (30,35) in the bottom of above-mentioned film unit (27,34), former water is heated;
The top set handling liquid import (41,57) of film evaporation tank (5,10), the stoste import is incorporated into the preliminary sedimentation district with stoste;
Film evaporation tank (5,10) top also is provided with hot water and extracts mouthful (42,53) out, will extract out from the hot water that film unit (27,34) is discharged;
Hot water return port (44, the 55) pipe that above-mentioned hot water is extracted out on mouthful (42,53) and film evaporation tank (5, the 10) diapire connects, and recycles hot water;
On the pipeline between above-mentioned hot water extraction mouthful (42,53) and the hot water return port (44,55), recycle pump (26,33) is set;
On the diapire in the preliminary sedimentation district of above-mentioned film evaporation tank (5,10) slag-drip opening is set also, is used for dense slag is discharged;
Above-mentioned high-order upflow tube (29,38) leads to the outside of film evaporation tank (5,10);
At the sidepiece of film evaporation tank (5,10) steam is set and draws the steam that interface (43,53) is used for drawing film evaporation tank (5).
4, the film according to claim 3 coupling treatment unit of purifying waste water is characterized in that:
The steam outlet of first step film evaporation tank (5) and second stage film evaporation tank (10) divides no matter is connected to first step condensing unit (111) and second condensing unit (222);
Above-mentioned condensing unit (111,222) comprising:
Interchanger (4,15);
Be connected in the gas-liquid separator (16,21) of interchanger (4,15) outlet;
The temporary container (18,23) of the liquid outlet of above-mentioned gas-liquid separator (16,21) and distilled water is connected, and after the steam of interchanger discharging is condensed, is temporarily stored in the temporary container of distilled water;
The steam side outlet of above-mentioned gas-liquid separator (16,21) connects vacuum pump (20), steam is summarized in the vapour outlet (43,54) of film evaporation tank (5,10).
5, the film according to claim 3 coupling treatment unit of purifying waste water is characterized in that:
The dense water outlet of film evaporation tank (5,10) through buck dosing mouth (47,58) after, pipe is connected to and adds alkali line mixer (6,11), above-mentioned mixing tank (6,11) is to dense water and remove the hard base aqueous solution and mix;
Above-mentioned outlet and the immersion ultrafiltration reaction filtering basin (7,61) that add alkali line mixer (6,11) are connected;
The outlet of above-mentioned immersion ultrafiltration reaction filtering basin (7,12) through acid-adding port (51,63) after, be connected to and add acid tube road mixing tank (9,14), add acid tube road mixing tank (9,14) mixed solution that adds after the acid continued to mix.
6, the film according to claim 5 coupling treatment unit of purifying waste water is characterized in that:
Be provided with in the immersion ultrafiltration reaction filtering basin (7,12) and see through submerged ultrafiltration assembly (31,39), above-mentioned membrane module is no shell submerged ultrafiltration;
Below seeing through submerged ultrafiltration assembly (31,39) boring aeration pipe (32,40) is set, mixing water continues down to mix, react in the bubble effect of boring aeration pipe (32,40) discharging;
Filtering basin (7,12) top is set to the ultra-filtration membrane filtered solution and extracts mouthful (49,61) out, with extraction mouth (49,61) lift pump (8,13) is set on the pipeline that pipe connects, passes through acid-adding port (51 in lift pump (8,13) outlet, 63), link to each other with the inlet that adds acid tube road mixing tank (9,14); Locate to add acid at above-mentioned acid-adding port (51,63), recall to the pH value of mixing water after, mixing water enters and adds acid tube road mixing tank;
The acid amount that adds that online pH meter (52,64) is used to control the acid-adding port place is set in the exit that adds acid tube road mixing tank.
7, the film according to claim 4 coupling treatment unit of purifying waste water is characterized in that:
Interchanger is the tubular fibre interchanger, and the tubular fibre material adopts polyvinylidene fluoride material, and polyvinylidene difluoride (PVDF) tubular fibre, internal diameter are 0.2-3.0mm, and wall thickness is 0.05-1.0mm, according to the difference of treatment capacity, and the in parallel or series connection use simultaneously of a plurality of membrane modules.
8, a kind of film coupling purified water processing method is characterized in that, comprising:
Former water at first enters first step film evaporation tank and carries out first step circulating and evaporating;
Add alkali in the dense water that in first step film evaporation tank, overflows, then mixed solution be incorporated in the first step immersion ultrafiltration reactor,
Carry out first step reaction and filter in first step immersion ultrafiltration reactor, cleaner liquid is drawn out of and enters second stage film evaporation tank and carry out second stage circulating and evaporating;
After the dense water that overflows from the film evaporation tank of the second stage adds alkali and flocculation agent, enter in the immersion ultrafiltration reactor of the second stage and react filtration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100528619A CN101565257A (en) | 2008-04-23 | 2008-04-23 | Method and device for treating and purifying sewage in a membrane coupling way |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100528619A CN101565257A (en) | 2008-04-23 | 2008-04-23 | Method and device for treating and purifying sewage in a membrane coupling way |
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| Publication Number | Publication Date |
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| CN101565257A true CN101565257A (en) | 2009-10-28 |
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ID=41281658
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2008100528619A Pending CN101565257A (en) | 2008-04-23 | 2008-04-23 | Method and device for treating and purifying sewage in a membrane coupling way |
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| CN (1) | CN101565257A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108283834A (en) * | 2018-03-20 | 2018-07-17 | 浦华环保股份有限公司 | For advanced treatment of wastewater and the partially submerged turntable filter chamber of Treated sewage reusing |
| CN114058482A (en) * | 2022-01-11 | 2022-02-18 | 中国农业科学院农业环境与可持续发展研究所 | Anaerobic digestion system for improving biogas production efficiency |
| CN117945581A (en) * | 2024-01-11 | 2024-04-30 | 苏州苏科环保科技有限公司 | Reciprocating membrane bioreactor and method for efficient sewage treatment |
-
2008
- 2008-04-23 CN CNA2008100528619A patent/CN101565257A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108283834A (en) * | 2018-03-20 | 2018-07-17 | 浦华环保股份有限公司 | For advanced treatment of wastewater and the partially submerged turntable filter chamber of Treated sewage reusing |
| CN108283834B (en) * | 2018-03-20 | 2024-01-12 | 浦华环保股份有限公司 | Partially immersed rotary disc filter tank for advanced sewage treatment and reclaimed water recycling |
| CN114058482A (en) * | 2022-01-11 | 2022-02-18 | 中国农业科学院农业环境与可持续发展研究所 | Anaerobic digestion system for improving biogas production efficiency |
| CN117945581A (en) * | 2024-01-11 | 2024-04-30 | 苏州苏科环保科技有限公司 | Reciprocating membrane bioreactor and method for efficient sewage treatment |
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Open date: 20091028 |