CN102690003B - Device and method for performing advanced treatment on citric acid waste water through dual membrane process - Google Patents
Device and method for performing advanced treatment on citric acid waste water through dual membrane process Download PDFInfo
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- CN102690003B CN102690003B CN201210202945.2A CN201210202945A CN102690003B CN 102690003 B CN102690003 B CN 102690003B CN 201210202945 A CN201210202945 A CN 201210202945A CN 102690003 B CN102690003 B CN 102690003B
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Abstract
The invention relates to a device and a method for performing advanced treatment on citric acid waste water through dual membrane process. The device comprises an inflow system, a flocculating settling system, a ceramic membrane ultrafiltration system and a reverse osmosis system which are connected in sequence. The method is characterized in that citric acid waste water processed after (Anoxic/Oxic) A/O process is further flocculated and settled and then enters into the ceramic membrane ultrafiltration system. Effluent of the ceramic membrane ultrafiltration system meets requirements that Silting Density Index (SDI) is equal to or less than 2 and is then processed by the reverse osmosis system. Reverse osmosis (RO) effluent can be directly used as process water (workshop section including size mixing, fermentation, extraction, lime milk configuration and the like) for producing citric acid and softening water (circulating cooling water and make-up water). By means of the dual membrane process, the device and the method realize treatment and reuse of citric acid waste water, the equipment is compact, the automation degree is high, the operation is simple and convenient, effluent quality is good and stable and the device and method have remarkable environmental benefit and economic benefit.
Description
Technical field
The present invention relates to the device and method of a kind of pair of embrane method advanced treatment citric acid wastewater, relate in particular to a kind of employing flocculation+sedimentation+ceramic super-filtering film+RO combination process and process citric acid wastewater, and reach the device and method of reuse standard, belong to wastewater treatment and reuse field.
Background technology
Along with the fast development of China's economy, the consumption of water resources is multiplied, and has caused the in short supply of water resources on the one hand, and meanwhile, a large amount of discharges of sewage are on the rise water environment pollution.Improving constantly of water quality emission standard, impels increasing enterprise to stand in the angle of economic benefit and social benefit, and sewage qualified discharge or reuse are risen to very high status.
Citric acid is widely used as a kind of important industrial chemicals and foodstuff additive, and its production is that to take the dry or corn of potato be raw material, successively through raw material process, fermentation, extract, the operation such as refining makes product, tool has been widely used.In foodstuffs industry, add the conversion that citric acid can reduce sucrose, increase the effect of sanitas, improve the local flavor of spices, stablize oxidation inhibitor, prevent the catalysis of enzyme and catalyzed oxidation that trace metal causes etc.In food, add citric acid except increasing tart flavour, also can be used for controlling suitable pH value; In medicine industry, the sodium salt of citric acid can be used as blood anti gelling agent and diuretic(s), and sylvite can be used as antacid, and molysite can be used as hematinic, and mantoquita can be used as astringent matter.Citric acid replaces tripoly phosphate sodium STPP as household detergent, and not only decontamination and cleaning performance are good, and are easy to biological degradation, can not bring environmental pollution and public hazards.
Citric acid production wastewater is mainly from the useless neutralizer, affination water, cleaning of evaporator water and the filter wash water distribution that ferment and abstraction process produces, mainly contain starchiness, protein, various organic acid, produce the organism such as the secreted enzyme of thalline, fermentation residue, glucose, ammonia nitrogen and fat, the mass concentration of COD is 20000-30000 mg/L, belongs to high concentration organic waste water.According to statistics, China's citric acid annual production reaches more than 600,000 tons, and every production 1 t citric acid, produces 7.5 m
3waste water, Gao Shikeda 10-15 m
3waste water, calculates that the annual citric acid wastewater of discharging of China can reach 4,500,000 m thus
3above.
Citric acid production wastewater generation is large, and Pollutant levels are high, and directly discharge will cause severe contamination to environment.For many years, people, from the angle of decontamination, protection of the environment, changing waste into resources, study the processing of citric acid wastewater and comprehensive utilization.
At present, the technology for the treatment of citric acid production wastewater mainly contains aerobe facture, Anaerobic biotreatment method, anaerobic-aerobic facture, Photosynthetic Bacteria etc.But these methods often can only cannot reach reuse standard by wastewater treatment to qualified discharge standard, do not have economic benefit.
Patent CN200810117645.8 discloses a kind for the treatment of process of citric acid production wastewater, adopt two-phase anaerobic-aerobic combination process, production technique waste water enters sedimentary adjustive pool by grating tank, air flotation pool, the pollutents such as the suspended substance in removal waste water and colloidalmaterial, then enter two-phase anaerobic reactor, various complicated organic substance decomposing in waste water changes into small organic molecule, the materials such as methane and carbon dioxide, postdigestive waste water enters extended aeration pond again, further act on the aerobic microbiological in mud, remove remaining organism, after being precipitated out in inclined tube settling bowl, the suspended substance that part is taken out of with current reaches emission standard.Effluent index: COD is 86.4 mg/L, BOD
5be that 19.8 mg/L, SS are that 66.2 mg/L pH are 7.43.But above-mentioned treatment process is complicated, running cost is large and produce little effect, and is not suitable for applying.
In view of this, special proposition the present invention.
Summary of the invention
The first object of the present invention is, large for the citric acid production wastewater water yield, COD is high, variation water quality is large, after biochemical, water outlet still has compared with features such as high chroma and saltiness, the object that is recycling as with water resources, realize the target that water outlet can reuse, propose a kind of citric acid wastewater advanced treatment apparatus based on two embrane methods.
For realizing the first object, the present invention adopts following technical scheme:
A device for pair embrane method advanced treatment citric acid wastewater, described device comprises water inlet system, flocculating settling system, ceramic membrane ultrafitration system and the reverse osmosis system connecting successively.
Described water inlet system comprises intake pump; Flocculating settling system comprises flocculation agent hold-up vessel, flocculation agent volume pump, inclined tube settling bowl and clean solution tank; Described ceramic membrane ultrafitration system comprises ceramic membrane ultrafitration assembly and ceramic membrane charging pump; Described reverse osmosis system comprises reverse osmosis module, charging pump and reverse osmosis concentrated pond; Citric acid wastewater enters inclined tube settling bowl through intake pump, after carrying out flocculating settling processing, flocculation agent drains into clean solution tank, by ceramic membrane charging pump pump to ceramic membrane ultrafitration assembly, carry out uf processing, ceramic membrane penetrating fluid after processing enters intermediate pool, through reverse osmosis charging pump pump to reverse osmosis module, carry out reverse-osmosis treated again, the concentrated solution after processing enters the advanced treatment that reverse osmosis concentrated pond completes lemon waste water.
Preferably described inclined tube settling bowl adopts Ф 50-Ф 100 honeycomb fillers.
Preferably described ceramic membrane ultrafitration assembly comprises ceramic super-filtering film and ceramic membrane recoil pump; Described Ceramic excessive filtration membrane material is aluminum oxide, zirconium white or titanium oxide, and the mean pore size scope of ceramic super-filtering film is 0.02-1 μ m.
Preferably described reverse osmosis module is tubular fibre formula reverse osmosis membrane, coiled reverse osmosis membrane, plate and frame reverse osmosis membrane or tubular type reverse osmosis membrane.
The second object of the present invention is to provide a kind of method of utilizing said apparatus to carry out two embrane method advanced treatment citric acid wastewaters, finally to realize the recycle of water resources, and the target that water outlet can reuse, for realizing the second object, the present invention adopts following technical scheme:
1) citric acid production wastewater a is delivered to inclined tube settling bowl by intake pump, carries in way, and the flocculation agent in flocculation agent hold-up vessel injects inlet channel by flocculation agent volume pump, and mixes by the turbulent flow in pipeline;
2) the waste water b after mixing completely with flocculation agent is through the sedimentation of inclined tube settling bowl, enters clean solution tank after removing suspended substance and colloid;
3) the waste water c in clean solution tank through ceramic membrane charging pump pump to Ceramic excessive filtration membrane module;
4) waste water c is after Ceramic excessive filtration membrane module is processed, and gained ceramic membrane penetrating fluid d enters intermediate pool, and as the water inlet of reverse osmosis, ceramic membrane concentrated solution e arranges outward;
5) enter ceramic membrane penetrating fluid d in intermediate pool through reverse osmosis charging pump pump to reverse osmosis module, gained reverse osmosis membrane penetrating fluid f returns in citric acid production, concentrated solution g enters reverse osmosis concentrated pond.
Wherein, preferably described waste water b is 0.5-1 h in the settling region residence time of inclined tube settling bowl, preferably 0.8h.
Preferably flocculant concentration concentration is 30-50ppm.
Wherein, preferably, in described step 4, waste water c, after Ceramic excessive filtration membrane module is processed, guarantees water outlet SDI≤2; Described ceramic membrane ultrafitration assembly comprises ceramic super-filtering film, and described ceramic super-filtering film adopts micro-cross flow filter, and crossflow velocity is 0.05 m/s-1 m/s, and operating pressure scope is 0.02-0.3 MPa; Pressure cleans while reaching the operational limit of 0.25-0.3 MPa.
Preferably described ceramic membrane ultrafitration assembly is provided with ceramic membrane recoil pump, and described ceramic membrane recoil pump adopts the dense water of reverse osmosis membrane intermittently ceramic super-filtering film to be recoiled automatically, and recoil is spaced apart 30 min-60 min, and the recoil time is 10-30 s; .
Preferably it is characterized in that reverse osmosis adopts low pressure reverse osmosis, working pressure is 5-40 bar.
Below in conjunction with accompanying drawing, the present invention is further described in detail:
Two embrane methods using ultrafiltration (UF) and reverse osmosis (RO) as core processing technique, two membrane treatment process are as a kind of new life's water technology, powerful advantages with its low cost, high-level efficiency, low consumption environment protection is universal rapidly, has become the best general scheme that current water depth is processed.
The molecular size range that the lower pressure-driven of ultrafiltration utilization is also pressed solute comes separated and filters, and is a kind of physical separating process.The aperture of ultra-filtration membrane is within the scope of 0.002-0.1 μ m, it can remove the colloid of macromolecule organic, mushroom, suspended particulates, heat source body and various types of silicon, iron and aluminium in water, can be used as the processing of direct-drinking water, the pre-treatment of all kinds of reverse osmosiss, can greatly improve the operation of follow-up equipment, reduce the frequency that reverse osmosis membrane cleans and changes.
Reverse osmosis unit is topmost desalting plant in two membrane process crafts, reverse osmosis system utilizes the characteristic of reverse osmosis membrane to make a return journey to dewater that middle most of soluble salt is divided, colloid, organism and microorganism, thereby obtain high-quality water outlet, common COD ﹤ 20 mg/L, colourity ﹤ 5 degree, hardness is (with CaCO
3meter) ﹤ 0.5 mg/L, electricity is led ﹤ 30, water outlet can be directly as the process water of citric acid production workshop sections such as (size mixing, ferment) extractions, milk of lime configuration and softening water (recirculated cooling water and make up water), there is obvious environmental benefit and economic benefit.
It is water inlet that the water outlet of A/O art breading is take in the present invention, take flocculation+sedimentation+ceramic super-filtering film+reverse osmosis system as main process, advanced treatment citric acid production wastewater, obtain high-quality reuse water, the process water (size mixing, ferment, the workshop section such as extraction, milk of lime configuration) and the softening water (recirculated cooling water and make up water) that can be used as citric acid production, the reclamation rate of water is 60% ~ 70%.In order to realize technical purpose of the present invention and technique effect, the present invention adopts following technical scheme.
The device of of the present invention pair of embrane method advanced treatment citric acid wastewater comprises water inlet system, flocculating settling system, ceramic membrane ultrafitration system and the reverse osmosis system connecting successively.Wherein, described water inlet system comprises intake pump; Flocculating settling system comprises flocculation agent hold-up vessel, flocculation agent volume pump, inclined tube settling bowl and clean solution tank; Described ceramic membrane ultrafitration system comprises ceramic membrane ultrafitration assembly and ceramic membrane charging pump; Described reverse osmosis system comprises reverse osmosis module, charging pump and reverse osmosis concentrated pond; Citric acid wastewater enters inclined tube settling bowl through intake pump, after carrying out flocculating settling processing, flocculation agent drains into clean solution tank, by ceramic membrane charging pump pump to ceramic membrane ultrafitration assembly, carry out uf processing, ceramic membrane penetrating fluid after processing enters intermediate pool, through reverse osmosis charging pump pump to reverse osmosis module, carry out reverse-osmosis treated again, the concentrated solution after processing enters the advanced treatment that reverse osmosis concentrated pond completes lemon waste water.
As a kind of preferred implementation, ceramic membrane ultrafitration assembly of the present invention is also with recoiling device, this recoiling device adopts the dense water of reverse osmosis membrane intermittently Ceramic excessive filtration film filter to be recoiled automatically, the filter cake that is attached to film surface is come off, effectively alleviating film pollutes, improve membrane flux, extend the cleaning interval of film, contribute to ultrafiltration system operation steady in a long-term.In order further to obtain best repercussion effect, contriver has done a large amount of simultaneous tests to recoil interval and recoil time, and result shows, with recoil, be spaced apart 30-60 min, the recoil time is that 10-30s is best, and wherein more preferably recoil is spaced apart 45-50min, and the recoil time is 20-25s.
In addition, inclined tube settling bowl of the present invention adopts Ф 50-Ф 100 honeycomb fillers, and the concrete those skilled in the art that are chosen as grasp.
As a kind of preferred implementation of the present invention, described Ceramic excessive filtration membrane material adopts aluminum oxide, zirconium white or titanium oxide, and its mean pore size scope is 0.02-1 μ m.
Described reverse osmosis module is selected from tubular fibre formula reverse osmosis membrane, coiled reverse osmosis membrane, plate and frame reverse osmosis membrane or tubular type reverse osmosis membrane.
Of the present invention pair of embrane method advanced treatment citric acid wastewater method, its key step comprises:
1) citric acid production wastewater a is delivered to inclined tube settling bowl by intake pump, carries in way, and the flocculation agent in flocculation agent hold-up vessel injects inlet channel by flocculation agent volume pump, and mixes by the turbulent flow in pipeline;
2) the waste water b after mixing completely with flocculation agent is through the sedimentation of inclined tube settling bowl, enters clean solution tank after removing suspended substance and colloid;
3) the waste water c in clean solution tank through ceramic membrane charging pump pump to Ceramic excessive filtration membrane module;
4) waste water c is after Ceramic excessive filtration membrane module is processed, and gained ceramic membrane penetrating fluid d enters intermediate pool, and as the water inlet of reverse osmosis, ceramic membrane concentrated solution e arranges outward;
5) enter ceramic membrane penetrating fluid d in intermediate pool through reverse osmosis charging pump pump to reverse osmosis module, gained reverse osmosis membrane penetrating fluid f returns in citric acid production, concentrated solution g enters reverse osmosis concentrated pond.
In order to obtain more preferably treatment effect, contriver has launched further investigation to the concrete operations of aforesaid method, and has further proposed following preferred implementation:
1,, in order to make citric acid wastewater obtain sufficient flocculating settling, preferably described waste water b is 0.5-1 h, more preferably 0.8h in the settling region residence time of inclined tube settling bowl.Flocculation agent of the present invention can adopt the disclosed multiple product of commonly using of prior art, and as aluminium iron polychloride, the concrete those skilled in the art that are chosen as grasp.In order to obtain desirable flocculating effect, the preferred flocculant concentration concentration of the present invention is 30-50ppm.
2,, in above-mentioned step 4, waste water c guarantees that after Ceramic excessive filtration membrane module is processed water outlet SDI≤2 are advisable.Ceramic excessive filtration membrane module filter method described in step 3) and step 4) is preferably micro-cross flow filter, and specifically adopting crossflow velocity is 0.05 m/s-1 m/s., operating pressure scope is the operational condition of 0.02-0.3 MPa, preferably crossflow velocity is 0.5 m/s – 0.8 m/s., operating pressure scope is 0.18-0.24 MPa.Under this condition, the ultrafiltration best results of citric acid wastewater.When operating pressure is between 0.25-0.3 MPa, ceramic super-filtering film reaches operational limit, can produce the pressure phenomenon that rises sharply, and needs cleaning and regeneration.Ceramic membrane ultrafitration system adopts charging pump automatic frequency-conversion to realize the constant water outlet of ultrafiltration system.Switching between the operation of ultrafiltration system standard state and recoil state adopts PLC to control, and by controlling the on off state of each pneumavalve and recoil pump, controls.
3, the ceramic membrane ultrafitration assembly described in the present invention is preferably provided with ceramic membrane recoil pump, and described ceramic membrane recoil pump adopts the dense water of reverse osmosis membrane intermittently ceramic super-filtering film to be recoiled automatically, and recoil is spaced apart 30 min-60 min, and the recoil time is 10-30 s; Preferably recoil is spaced apart 45-50min, and the recoil time is 20-25s.
4, preferred steps 4) and step 5) described in reverse osmosis module adopt low pressure reverse osmosis, working pressure is 5-40 bar, preferably 20-25 bar.
Adopt technique scheme, the present invention obtains following beneficial effect: the device and method that the invention provides a kind of pair of embrane method advanced treatment citric acid wastewater, described flocculation agent directly injects inlet channel by flocculation agent volume pump, utilize the turbulent flow in pipeline to mix, omitted flocculation tank, compact construction, floor space is little.During Ceramic excessive filtration membrane filtration, adopt micro-cross flow filter, crossflow velocity is 0.05-1 m/s, and operation energy consumption is lower.Ceramic excessive filtration membrane filter unit adopts ceramic honey comb ultra-filtration membrane while filtering, filling area is large.Reverse osmosis units adopts ultralow pressure reverse osmosis, and working pressure is 5-40 bar, and the more common reverse osmosis of operation energy consumption is low.
In addition, the device of a kind of pair of embrane method advanced treatment citric acid wastewater of the present invention can adapt to harsh influent quality condition.Ceramic super-filtering film can contact chloride flocculation agent, and is difficult for being flocculated alumen ustum obstruction fenestra; Ceramic super-filtering film can utilize reverse osmosis concentrated water counterflush to recover membrane flux, has reduced the waste that water is produced in ultrafiltration, has improved overall producing water ratio, and continuous operating time is long, stable, has reduced working cost.
Further, the water outlet after reverse-osmosis treated of the present invention is back to use in citric acid production as the process water of citric acid production (size mixing, ferment, the workshop section such as extraction, milk of lime configuration) and softening water (recirculated cooling water and make up water).Dense water enters dense pond, can be used as ceramic super-filtering film recoil water, improves the producing water ratio of system.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
Main figure elements explanation:
1-intake pump, 2-flocculation agent storage tank, 3-flocculation agent volume pump, 4-inclined tube settling bowl, 5-clean solution tank, 6-ceramic membrane ultrafitration assembly, 7-ceramic membrane charging pump, 8-ceramic membrane recoil pump, 9-intermediate pool, 10-reverse osmosis module, 11-reverse osmosis charging pump, the reverse osmosis concentrated pond of 12-, 13,14,15-pneumavalve.A-citric acid wastewater, b-waste water, c-waste water, d-ceramic membrane penetrating fluid, e-ceramic membrane concentrated solution, f-reverse osmosis membrane penetrating fluid, g-reverse osmosis membrane concentrated solution.
Embodiment
Below in conjunction with embodiment, the present invention is described further.
As shown in Figure 1, the device of a kind of advanced treatment citric acid wastewater of the present invention, comprises the water inlet system, flocculating settling system, ceramic membrane ultrafitration system and the reverse osmosis system that connect successively.This water inlet system comprises intake pump 1; Flocculating settling system comprises flocculation agent hold-up vessel 2, flocculation agent volume pump 3, inclined tube settling bowl 4 and clean solution tank 5; Ceramic membrane ultrafitration system comprises ceramic membrane ultrafitration assembly 6 and ceramic membrane charging pump 7; Reverse osmosis system comprises reverse osmosis module 10, charging pump 11 and reverse osmosis concentrated pond 12; Citric acid wastewater enters inclined tube settling bowl 4 through intake pump 1, after carrying out flocculating settling processing, flocculation agent drains into clean solution tank 5, by ceramic membrane charging pump 7 pumps to ceramic membrane ultrafitration assembly 6, carry out uf processing, ceramic membrane penetrating fluid after processing enters intermediate pool 9, through reverse osmosis charging pump 11 pumps, to reverse osmosis module 10, carry out reverse-osmosis treated again, the concentrated solution after processing enters the advanced treatment that reverse osmosis concentrated pond 12 completes lemon waste water.
Compare with embodiment 1, distinctive points is only, in the present embodiment, in ceramic membrane ultrafitration assembly 6, be provided with ceramic membrane recoil pump 8, the order of connection of each several part is as follows: intake pump 1 connects inclined tube settling bowl 4, between intake pump 1 and inclined tube settling bowl 4, be provided with flocculation agent hold-up vessel 2 and flocculation agent volume pump 3, wherein inclined tube settling bowl 4, clean solution tank 5, ceramic membrane ultrafitration assembly 6, ceramic membrane charging pump 7, ceramic membrane recoil pump 8, intermediate pool 9, reverse osmosis module 10, reverse osmosis charging pump 11 and reverse osmosis concentrated pond 12 are connected successively.
In the present embodiment, inclined tube settling bowl 4 adopts the honeycomb filler of Ф 60.
In the present embodiment, Ceramic excessive filtration membrane material is aluminum oxide, and the mean pore size scope of ceramic super-filtering film is 0.5-0.6 μ m.
In the present embodiment, reverse osmosis module is tubular fibre formula reverse osmosis membrane.
Compare with embodiment 2, distinctive points is only: in the present embodiment, ceramic membrane ultrafitration assembly comprises ceramic super-filtering film and ceramic membrane recoil pump; Described Ceramic excessive filtration membrane material is zirconium white, and the mean pore size scope of ceramic super-filtering film is 0.02-0.1 μ m.Reverse osmosis module is coiled reverse osmosis membrane.
Embodiment 4
Citric acid production wastewater a is delivered to inclined tube settling bowl 4 by intake pump 1, carries in way, and the flocculation agent in flocculation agent hold-up vessel 2 injects inlet channel by flocculation agent volume pump 3, and mixes by the turbulent flow in pipeline; Waste water b mix completely with flocculation agent after, through 4 sedimentations of inclined tube settling bowl, removes most suspended substances and colloid, enters afterwards clean solution tank 5; Waste water c in clean solution tank 5 enters ceramic super-filtering film assembly 6 after ceramic membrane charging pump 7; Waste water, after ultrafiltration module 6 is processed, guarantees water outlet SDI≤2, and water outlet d enters intermediate pool 9, and as the water inlet of reverse osmosis, ceramic membrane concentrated solution e arranges outward; Waste water d in intermediate pool 9 enters reverse osmosis module 10 after reverse osmosis charging pump 11, and reverse osmosis membrane water outlet f returns in citric acid production, and concentrated solution g enters reverse osmosis concentrated pond 12.
In the present embodiment, the waste water of sewage source Wei Mou citric acid production producer is through the water outlet later of A/O art breading, and condition of water quality is: COD 140-170 mg/L, doubly, hardness is (with CaCO for colourity 260-320
3meter) 900-1000 mg/L, electricity is led 2700-3200 μ s/cm.First by flocculation agent volume pump 3, flocculation agent is injected to the inlet channel of waste water, along with ducted turbulent flow mixes, flocculant concentration concentration is 35ppm.Then enter inclined tube settling bowl 4 and carry out the sedimentation of 0.5 h, then enter ceramic membrane ultrafitration assembly 6.Ceramic excessive filtration membrane material is aluminum oxide and zirconium white, and mean pore size is 50 nm.Employing charging pump automatic frequency-conversion constant flux control in service, it is 70 L/m that ceramic super-filtering film arranges flux
2h, crossflow velocity is 0.2 m/s, coordinates regularly recoil, recoil is spaced apart 30 min, the recoil time is 15 s, kickback pressure by initial 0.3MPa rising to 0.65MPa.Ceramic super-filtering film initial launch pressure is 0.03-0.04MPa, along with the process rising of operation reaches operational limit during to 0.3MPa, completes a cycle of operation, then carries out matting regeneration.
Ro components operation pressure is at 8-15 bar, and reverse osmosis flux is set to 15 L/m
2h, producing water ratio is 65%, can steady in a long-term move, and the cleaning interval of film was about about 10 days, and after cleaning, flux recovers substantially completely.After this art breading, water outlet COD ﹤ 10 mg/L, 5 times of colourity ﹤, hardness is (with CaCO
3meter) ﹤ 0.5mg/L, ratio of desalinization ﹥ 99%, the workshop sections such as this water is back to use the sizing mixing of this factory's citric acid production, ferments, extraction.
Embodiment 5
The water that in the present embodiment, sewage source Wei Mou citric acid production producer discharges later through A/O art breading, condition of water quality is: COD 120-150 mg/L, colourity is 180-260 times, hardness is (with CaCO
3meter) be 500-700 mg/L, electricity is led the s/cm into 2100-2500 μ.Waste water is carried out to membrane fouling agent and add, then pass through tube settler 4 sedimentations.Flocculant concentration concentration is 50 ppm, and the settling time is 1 h.Then enter ceramic membrane ultrafitration assembly 6, Ceramic excessive filtration membrane material is aluminum oxide and zirconium white, and mean pore size is 200 nm.It is 80 L/m that ceramic super-filtering film arranges flux
2h, crossflow velocity is that 0.8 m/s adopts charging pump automatic frequency-conversion constant flux control, coordinates regularly recoil.Recoil be spaced apart 60 min, the recoil time is 25 s, kickback pressure by initial 0.25MPa rising to 0.5MPa.Ceramic super-filtering film initial launch pressure is 0.02-0.03MPa, along with the process rising of operation reaches operational limit during to 0.25MPa, completes a cycle of operation, then carries out matting regeneration.
The flux of reverse osmosis setting is 16.5 L/m
2h, operating pressure is at 10-20 bar, and producing water ratio, 62.5%, can steady in a long-term move, and the cleaning interval was about about 7 days, and after cleaning, flux recovers substantially completely.After this art breading, effluent quality is good, and each index all reaches that this factory sizes mixing, ferments, the use standard of extraction, milk of lime configuration, recirculated cooling water and make up water.
Embodiment in above-described embodiment can further combine or replace; and embodiment is described the preferred embodiments of the present invention; not the spirit and scope of the present invention are limited; do not departing under the prerequisite of design philosophy of the present invention; the various changes and modifications that in this area, professional and technical personnel makes technical scheme of the present invention, all belong to protection scope of the present invention.
Claims (7)
1. a device for two embrane method advanced treatment citric acid wastewaters, is characterized in that: described device comprises water inlet system, flocculating settling system, ceramic membrane ultrafitration system and the reverse osmosis system connecting successively; Described water inlet system comprises intake pump (1); Flocculating settling system comprises flocculation agent hold-up vessel (2), flocculation agent volume pump (3), inclined tube settling bowl (4) and clean solution tank (5); Described ceramic membrane ultrafitration system comprises ceramic membrane ultrafitration assembly (6) and ceramic membrane charging pump (7); Described reverse osmosis system comprises reverse osmosis module (10), charging pump (11) and reverse osmosis concentrated pond (12); Citric acid wastewater enters inclined tube settling bowl (4) through intake pump (1), after carrying out flocculating settling processing, flocculation agent drains into clean solution tank (5), by ceramic membrane charging pump (7) pump to ceramic membrane ultrafitration assembly (6), carry out uf processing, ceramic membrane penetrating fluid after processing enters intermediate pool (9), through reverse osmosis charging pump (11) pump, to reverse osmosis module (10), carry out reverse-osmosis treated again, the concentrated solution after processing enters the advanced treatment that reverse osmosis concentrated pond (12) completes lemon waste water;
Described ceramic membrane ultrafitration assembly (6) comprises ceramic super-filtering film and ceramic membrane recoil pump (8); Described Ceramic excessive filtration membrane material is aluminum oxide, zirconium white or titanium oxide, and the mean pore size scope of ceramic super-filtering film is 0.02-1 μ m.
2. the device of according to claim 1 pair of embrane method advanced treatment citric acid production wastewater, is characterized in that, described inclined tube settling bowl adopts Ф 50-Ф 100 honeycomb fillers.
3. the device of according to claim 1 pair of embrane method advanced treatment citric acid production wastewater, is characterized in that described reverse osmosis module (10) is tubular fibre formula reverse osmosis membrane, coiled reverse osmosis membrane, plate and frame reverse osmosis membrane or tubular type reverse osmosis membrane.
4. utilize device described in claim 1 to carry out a method for two embrane method advanced treatment citric acid wastewaters, it is characterized in that: described method comprises the following steps:
1) citric acid production wastewater a is delivered to inclined tube settling bowl (4) by intake pump (1), carries in way, and the flocculation agent in flocculation agent hold-up vessel (2) injects inlet channel by flocculation agent volume pump (3), and mixes by the turbulent flow in pipeline;
2) the waste water b after mixing completely with flocculation agent is through inclined tube settling bowl (4) sedimentation, enters clean solution tank (5) after removing suspended substance and colloid;
3) the waste water c in clean solution tank (5) through ceramic membrane charging pump (7) pump to Ceramic excessive filtration membrane module (6);
4) waste water c is after Ceramic excessive filtration membrane module (6) is processed, and gained ceramic membrane penetrating fluid d enters intermediate pool (9), and as the water inlet of reverse osmosis, ceramic membrane concentrated solution e arranges outward; Wherein, waste water c, after Ceramic excessive filtration membrane module (6) is processed, guarantees water outlet SDI≤2; Described ceramic membrane ultrafitration assembly (6) comprises ceramic super-filtering film, and described ceramic super-filtering film adopts micro-cross flow filter, and crossflow velocity is 0.05 m/s-1 m/s, and operating pressure scope is 0.02-0.3 MPa;
5) enter ceramic membrane penetrating fluid d in intermediate pool (9) through reverse osmosis charging pump (11) pump to reverse osmosis module (10), gained reverse osmosis membrane penetrating fluid f returns in citric acid production, concentrated solution g enters reverse osmosis concentrated pond (12); Reverse osmosis adopts low pressure reverse osmosis, and working pressure is 5-40 bar.
5. method according to claim 4, is characterized in that, described waste water b is 0.5-1 h in the settling region residence time of inclined tube settling bowl (4), and flocculant concentration concentration is 30-50ppm.
6. method according to claim 4, is characterized in that, operating pressure cleans ceramic super-filtering film while reaching the operational limit of 0.25-0.3 MPa.
7. method according to claim 4, it is characterized in that, described ceramic membrane ultrafitration assembly (6) is provided with ceramic membrane recoil pump (8), described ceramic membrane recoil pump (8) adopts the dense water of reverse osmosis membrane intermittently ceramic super-filtering film to be recoiled automatically, recoil is spaced apart 30 min-60 min, and the recoil time is 10-30 s.
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| CN201210202945.2A CN102690003B (en) | 2012-06-19 | 2012-06-19 | Device and method for performing advanced treatment on citric acid waste water through dual membrane process |
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| CN201210202945.2A CN102690003B (en) | 2012-06-19 | 2012-06-19 | Device and method for performing advanced treatment on citric acid waste water through dual membrane process |
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| CN102690003B true CN102690003B (en) | 2014-03-12 |
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| CN105016533A (en) * | 2015-08-14 | 2015-11-04 | 铁道第三勘察设计院集团有限公司 | Combined processing system for using reclaimed water as subway air conditioner circulation cooling water for water supplementing |
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| CN106673136A (en) * | 2016-12-21 | 2017-05-17 | 安徽金川活动坝科技有限公司 | Double-membrane method waste water apparatus based on flat ceramic membrane |
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| CN109022502B (en) * | 2018-08-17 | 2020-10-09 | 江南大学 | Method for producing citric acid by recycling anaerobic digestion solution |
| CN110217929A (en) * | 2019-05-15 | 2019-09-10 | 华电电力科学研究院有限公司 | A kind of make up water treatment system and method suitable for Distribution of Natural formula energy source station |
| CN112645505A (en) * | 2021-01-18 | 2021-04-13 | 上海密特印制有限公司 | Method and system for treating electronic travel document production sewage |
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