CN1508076A - Method for retarding and washing membrane pollution during synthesizing polymer flocculant using membrane reactor - Google Patents
Method for retarding and washing membrane pollution during synthesizing polymer flocculant using membrane reactor Download PDFInfo
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- CN1508076A CN1508076A CNA021573085A CN02157308A CN1508076A CN 1508076 A CN1508076 A CN 1508076A CN A021573085 A CNA021573085 A CN A021573085A CN 02157308 A CN02157308 A CN 02157308A CN 1508076 A CN1508076 A CN 1508076A
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Abstract
The present invention relates to a method for retarding and cleaning membrane pollution when the membrane reactor is used for synthesizing high-molecular flocculant. It utilizes the reverse negative-pressure back-purge process to reduce membrane internal cavity pollution, so that the formed hydroxide quantity is reduced obviously, the aluminium salt solution flow rate reduced extent also is obviously reduced so as to ensure the mixing intensity of fluid in the cavity interior and can ensure the quality of synthetic inorganic high-molecular flocculant. After the synthesis is completed, it uses soft water-acid solution-soft water to make three step washing so as to eliminate hydroxide layer on the membrane surface and can prolong the service life of membrane component.
Description
Technical field
The invention belongs to the water treatment flocculant synthesis technical field, slow down and clean the method for film pollution when referring more particularly to the membrane reactor synthetic polymeric flocculant.
Background technology
Advantages such as inorganic polymer flocculant is a class novel water-treatment medicament that grows up on the basis of traditional aluminum salt flocculant, and this class medicament has efficiently, and is cheap and being widely used.
Utilize membrane reactor synthetic flocculant process, utilize fenestra in the membrane structure as the micro-amounts of liquids sparger, under pressure-driven, exactly with the reactant solution of film one side, evenly be pressed into lentamente in another reactant solution of film opposite side, and react with it.Because it is suitable to see through the drop yardstick and the membrane pore size of liquid, therefore, can guarantee that certain sodium hydroxide adds under the situation of speed, reduces to nano level with sodium hydroxide drop yardstick, thereby effectively reduce sodium hydroxide feature diffusion time, avoid local instantaneous generation Al (OH)
3Precipitation.It is generally acknowledged poly-13 aluminium (Al
13) be the best cohesion flocculation composition in the polymeric aluminum, its content can reflect the validity of goods, utilizes membrane reactor synthesized polymer aluminum chloride, Al in its product
bContent can be brought up to more than 80%, and is easy to amplify, and has good industrialization prospect.Utilizing membrane reactor synthesized polymer aluminum chloride at present seldom, is 99109853.6 disclosed as number of patent application, but this application is polluted for the film that occurs in the embrane method synthesized polymer aluminum chloride process and do not proposed rational solution.
Summary of the invention
The objective of the invention is to alleviate aluminium and be in the inorganic polymer flocculant building-up process that film pollutes and hollow-fibre membrane silk inner chamber in aluminum hydroxide precipitation, guarantee crossflow velocity, a kind of method of slowing down and cleaning the film pollution during with the membrane reactor synthetic polymeric flocculant is provided in order to avoid instantaneous mixing stirring intensity reduces, improves Al in the polymerize aluminum chloride inorganic polymer flocculant solution on the one hand in the hope of utilizing this method
bContent improves basicity on the other hand, increases the usefulness of inorganic flocculating agent; And after reaction finishes, clean, just can recover the flux of film silk, the life-span of membrane component and prolong by using acid solution.
The principle of technical solution of the present invention is: in utilizing membrane reactor synthetic macromolecule inorganic flocculating agent process, along with the carrying out of reaction, the increasing of the viscosity of aluminum salt solution and basicity is in the moment that alkali is added into, because OH
-Can not be spread apart rapidly, inevitably local high-basicity can occur, this just makes Al
3+With OH
-The chance of contact increases greatly, and the quantity and the speed that generate the nucleus of oxyhydroxide can increase.If under the condition of low basicity, by vigorous stirring, make that the nucleus of the oxyhydroxide that generates in the aluminum salt solution is less, newly-generated polymeric species will progressively change into stable polymer, can not generate precipitation of hydroxide.If under the high-basicity condition, the time that local high-basicity exists can extend, and has increased the quantity that generates the oxyhydroxide nucleus, the polymkeric substance that generates then can be converted into precipitation of hydroxide, these crystal are adsorbed on the film inwall, and aging gradually growing up stopped up the film inner chamber.The present invention is exactly by negative pressure commutation charging, changes the flow state of chamber inner fluid, strengthens mixture strength.This programme adopts negative pressure, because being the outside surface by the film silk, sodium hydroxide flows to internal surface, if adopt the malleation commutation, might make aluminum salt solution contact in the fenestra road with sodium hydroxide solution reacts, the aluminium hydroxide nucleus that generates might be adsorbed in the fenestra road and obstruction fenestra road, cause membrane flux to descend, cause the expendable pollution of flux.
At the aluminum hydroxide precipitation that is generally metal that film silk internal surface forms, it is dissolved in strong acid solution, therefore behind end of synthesis, by using strong acid it is got off from the film surface dissolution, recovers the internal diameter of membrane flux and film silk.
The used equipment of the present invention is the combination device that utilizes existing preparation inorganic polymer flocculant, connects with pipeline between each parts, as shown in Figure 1.Slowing down and clean the method that film pollutes during with the membrane reactor synthetic polymeric flocculant is:
One. the counterflush in the building-up process:
In synthetic macromolecule inorganic flocculating agent process, T-valve 4-1 is forward condition, and the aluminum salt solution among the retort 1-1 flows to arm U by arm W, T-valve 4-6 is forward condition, aluminum salt solution flows to arm T by arm M, and T-valve 4-7 is forward condition, and aluminum salt solution flows to arm S by arm R; Constant flow pump 8 pumps the sodium hydroxide solution in the sodium hydroxide jar 9, and flows to arm T through the arm M of T-valve 4-6, joins in the membrane module shell, sees through membranous wall in film silk inner chamber and aluminum salt solution reaction;
(1). when membrane module does not recoil with aluminum salt solution, the aluminum salt solution in Open valve 3-4 and the valve 3-5, blowdown piping BaG and FbK.Aluminum salt solution is sucking-off from circulating reaction jar 1-1 under the suction function of recycle pump 6, and through the T-valve 4-1 and the spinner-type flowmeter 2 of forward condition, the flow of aluminum salt solution is regulated by control valve 3-1; T-valve 4-2 is forward condition, flow to arm C from spinner-type flowmeter 2 effusive aluminum salt solutions by the arm A of T-valve 4-2, T-valve 4-3 is forward condition, flow to arm E from the effusive aluminum salt solution of arm C by the arm D of T-valve 4-3, enter hollow fiber film assembly 5 by an end of hollow fiber film assembly 5 from the effusive aluminum salt solution of arm E; Constant flow pump 8 pumps the sodium hydroxide solution in the sodium hydroxide solution jar 9 and flows to arm T through the arm M of T-valve 4-6, joins in the membrane module shell, and institute's hydro-oxidation sodium volume is as the criterion with each synthetic desired basicity; And with enter membrane module in aluminum salt solution mix after, flow out through the other end of film silk inner chamber from hollow fiber film assembly 5, T-valve 4-4 is forward condition, flow to arm I from membrane module 5 effusive aluminum salt solutions by the arm H of T-valve 4-4, T-valve 4-5 is forward condition, flow to arm L from the effusive aluminum salt solution of arm I by the arm J of T-valve 4-5, last, will increase the aluminum salt solution of sodium hydroxide in T-valve 4-7 delivers to circulating reaction jar 1-1 through recycle pump 6.The aluminum salt solution that contains sodium hydroxide constantly circulates, till reaching desired basicity.
The flow process that is the forward synthesizing inorganic macromolecule flocculant is: 1-1 → 4-1 → 2 → 3-1 → 4-2 → 4-3 → 5 → 4-4 → 4-5 → 6 → 4-7 → 1-1.
(2). when membrane module need be used the aluminum salt solution counterflush, at first blow-off valve 3-4 and 3-5 are closed.Contain aluminum salt solution sucking-off from circulating reaction jar 1-1 under the suction function of recycle pump 6 of sodium hydroxide, through the T-valve 4-1 and the spinner-type flowmeter 2 of forward condition; T-valve 4-2 is commutation states, flow to arm B from spinner-type flowmeter 2 effusive aluminum salt solutions by the arm A of T-valve 4-2, T-valve 4-4 is commutation states, flow to arm H from the effusive solution of arm B by the arm G of T-valve 4-4, enter hollow fiber film assembly 5 by an end of hollow fiber film assembly 5 from the effusive aluminum salt solution of arm H; Stop hydro-oxidation sodium this moment, flow out through the other end of film silk inner chamber from hollow fiber film assembly 5; T-valve 4-3 is commutation states, aluminum salt solution flows to arm F by the arm E of T-valve 4-3, T-valve 4-5 is commutation states, flow to arm L from the effusive aluminum salt solution of arm F by the arm K of T-valve 4-5, last aluminum salt solution sends back to aluminum salt solution in the circulating reaction jar 1-1 by recycle pump 6.
Aluminum salt solution flows to during recoil: 1-1 → 4-1 → 2 → 3-1 → 4-2 → 4-4 → 5 → 4-3 → 4-5 → 6 → 4-7 → 1-1.
After counterflush finished, T-valve returned forward condition by the commutation states adjustment, the state when total system is back to membrane module not with the flushing of aluminium salt, the aluminum salt solution in Open valve 3-4 and the valve 3-5, blowdown piping BaG and FbK.
In the whole synthetic reaction process, counterflush will be carried out repeatedly, and till reaching needed basicity, last synthetic inorganic polymer flocculant solution is the solution that slightly has muddiness that contains a small amount of fine particle.
After the back flushing of commutation negative pressure, film silk inner chamber pollutes and alleviates, and the inner chamber amount of scale buildup obviously reduces, and aluminum salt solution flow velocity fall diminishes, and has guaranteed the quality of synthesizing inorganic macromolecule flocculant.
Two. the cleaning behind the end of synthesis is the flocculation agent aluminum salt solution in the emptying pipeline: stop constant flow pump 8 runnings, valve-off 3-11 opens valve 3-10, the sodium hydroxide in the emptying membrane module 5.Recycle pump 6 remains in operation, and the flocculation agent aluminum salt solution in the emptying pipeline stops the running of recycle pump 6 then.With T-valve 4-1 commutation, make soft water or acid solution flow to arm U by T-valve 4-1 arm V, T-valve 4-6 commutation, aluminum salt solution flows to arm T by T-valve 4-6 arm N, T-valve 4-7 commutation, aluminum salt solution flows to arm Q by T-valve 4-7 arm R.T-valve 4-2,4-3,4-4 and 4-5 are forward condition.
Specific implementation method is:
(1). soft water cleans, and behind the end of synthesis, opens valve 3-10, the sodium hydroxide solution in the emptying membrane module, valve-off 3-10 then.Valve 3-2,3-7,3-9 and 3-11 are opened, and valve 3-3,3-6 and 3-8 close; Sodium hydroxide in the emptying membrane module shell, valve-off 3-10 then, the soft water in the Open valve 3-11, water softening tank 10-1 is gone in the membrane module shell by flow by gravity, with soft water flushing membrane assembly inner casing at first; Soft water in the ON cycle pump 6, water softening tank 1-3 relies on being used for to membrane surface flushing of recycle pump 6, and regulated valve 3-1 keeps high flow rate that face was washed 5 minutes, and T-valve 4-2,4-3,4-4 and 4-5 are commutation states then, wash 5 minutes again; Soft water in valve-off 3-7 and the 3-2, emptying circuit and elements is closed recycle pump 6, adjusts T-valve 4-2,4-3,4-4 and 4-5 and is forward condition.
(2). acid solution is cleaned, and valve-off 3-11 and 3-9 open valve 3-3,3-6 and 3-8, and the acid solution in the acid solution jar 10-2 is gone into the membrane module inner casing by flow by gravity; Acid solution in the ON cycle pump 6, acid solution jar 1-2, is cleaned after 30 minutes at the pipeline internal recycle by recycle pump 6, stops recycle pump 6; Adjust T-valve 4-2,4-3,4-4 and 4-5 and be commutation states, the ON cycle pump 6 again, with acid flushing 5 minutes.Valve-off 3-3 and 3-6 open valve 3-11, and the acid solution in emptying assembly and the pipeline is adjusted T-valve 4-2,4-3,4-4 and 4-5 and is forward condition.
(3). soft water cleans, and Open valve 3-2 and 3-11 with soft water flushing membrane assembly inner casing at first, are neutrality until the soft pH value that flows out valve 3-11.Open valve 3-7 and 3-9, valve-off 3-6 and 3-8, ON cycle pump 6 is neutral until valve 3-9 water outlet; Stop pump 6 runnings, change T-valve 4-2,4-3,4-4 and 4-5 and be commutation states, open pump 6 flushing pipeline BaG and pipeline FbK, be neutral until valve 3-9 water outlet.
Described film silk is selected the hollow fiber ultrafiltration membrane of molecular weight cut off less than 10,000 daltonian all high temperature-resistant acid-resistant alkali for use, as polysulfones, polyethersulfone or SPSF etc.
The starting point concentration of described sodium hydroxide is 1～2mol/l, and aluminium salt starting point concentration is 0.2～2mol/l, and used aluminum salt solution comprises aluminum chloride or Tai-Ace S 150 etc.
Described reverse negative pressure is cleaned required saturating mould and is controlled at 0.015～0.025MPa.
In each building-up process, before basicity is less than 1.5, and crossflow velocity needs counterflush, each washing length 1～2 minute during less than initial flow rate 90%.
In each building-up process, after basicity is greater than 1.5, and crossflow velocity needs counterflush, each washing length 1～2 minute during less than initial flow rate 80%.
The liquid effluent of described counterflush needs to filter with 400 order stainless steel filtering nets, and filter screen is immersed in the aluminum salt solution of circulating reaction jar.
Oppositely clean aluminum salt solution and be the metal salt solution in the retort after the filtration of 400 order stainless steel filtering nets.
Described hollow fiber film assembly, pipeline BaG or pipeline FbK are that level is installed.
The installation site of described circulating reaction jar is lower than the installation site of pipeline BaG and pipeline FbK.
On described pipeline BaG and the pipeline DbI blow-off valve must be installed, blow-off valve links to each other with the circulating reaction jar.
The working pressure that described soft water cleans is 0.015～0.02MPa.
The saturating mould of cleaning hollow fiber film assembly with acid solution is controlled at 0.015～0.02MPa, and the pickling time remained on 40～60 minutes, and used sour pH value is 1.5～3, can use hydrochloric acid, sulfuric acid or nitric acid.
Assembly inner chamber Acidwash solution is gone in the membrane module shell by flow by gravity, sees through ultra-filtration membrane under negative pressure, cleans the ultrafiltration fenestra.
The characteristics of the inventive method are by the back flushing of commutation negative pressure, film silk inner chamber pollutes and alleviates, and the hydroxide quantity of formation obviously reduces, and aluminum salt solution flow velocity fall obviously reduces, guarantee the mixture strength of chamber inner fluid, guaranteed the quality of synthesizing inorganic macromolecule flocculant.Behind end of synthesis, clean by using soft water-acid solution-three steps of soft water, can be so that the hydroxide layer of face disappears the work-ing life of membrane component and prolong.
Description of drawings
Fig. 1. the equipment synoptic diagram that the present invention is used.
Fig. 2. the embodiment of the invention 1 is promptly utilized NaOH and AlCl
3Flow velocity-time plot when membrane module oppositely cleans and oppositely do not clean in the synthesized polymer aluminum chloride PAC process.
Reference numeral
1-1. retort 1-2. acid solution jar 1-3. water softening tank 2. spinner-type flowmeters
3-1,3-2,3-3,3-4,3-5,3-6,3-7,3-8,3-9,3-10,3-11. valve
4-1,4-2,4-3,4-4,4-5,4-6,4-7. T-valve
5. membrane module 6. recycle pump 7-1,7-2. vacuum table
8. constant flow pump 9. sodium hydroxide jar 10-1. water softening tank 10-2. acid solution jars
11-1,11-2,11-3,11-4,11-5. tee branch BaG, FbK. pipeline
A、B、C、D、E、F、G、H、I、J、K、L、M、N、Q、R、S、T、U、V、
W. tee branch
Embodiment
Below in conjunction with example and accompanying drawing technical scheme of the present invention is further described.
Embodiment 1: utilize NaOH and AlCl
3Synthesized polymer aluminum chloride PAC (referring to Fig. 1)
(1). in retort 1-1, add 150ml 0.2mol/l AlCl
3Solution adds the NaOH solution of 1mol/l in sodium hydroxide jar 9.T-valve 4-1,4-2,4-3,4-4,4-5,4-6 and 4-7 are adjusted to forward condition, ejector priming 6, regulated valve 3-1 makes AlCl
3Flow control at 30l/h, open hydroxide sodium pump 8, dominant discharge is 0.3ml/min, synthetic beginning.Work as AlCl
3Circular flow is 26.5l/h, recoils.Valve-off 3-4 and 3-5 stop recycle pump 6 and 8 runnings, and commutation T-valve 4-2,4-3,4-4,4-5 are reverse state, i.e. AlCl
3Solution flows to arm B, AlCl by arm A
3Solution flows to arm H, AlCl by arm G
3Solution flows to arm F, AlCl by arm E
3Solution flows to arm L by arm K, and all three-way valves will be finished switch operation at short notice, and ON cycle pump 6 is regulated AlCl
3Circular flow is 45l/h, recoils 1 minute at a high speed.Stop recycle pump 6 runnings, change T-valve 4-2,4-3,4-4 and 4-5 and be forward condition, be i.e. AlCl
3Solution flows to arm C, AlCl by arm A
3Solution flows to arm E, AlCl by arm D
3Solution flows to arm I, AlCl by arm H
3Solution flows to arm L by arm J, opens valve 3-4 and 3-5, residual liquid in vent line BaG and the pipeline FbK section pipe.ON cycle pump 6 and constant flow pump 8 continue to synthesize AlCl
3Internal circulating load rises to 27.5l/h.Using such method is until meeting the requirements of basicity, the polymerize aluminum chloride end of synthesis.Counterflush and Fig. 2 as a result of counterflush not.
(2). behind the end of synthesis, stop pump 6 and 8 runnings, change T-valve 4-1,4-6 and 4-7 and be commutation states, be i.e. AlCl
3Solution flows to arm U by arm V, flows to arm Q by arm R, flows to arm T by arm N.
A. soft water cleans.Keeping T-valve 4-2,4-3,4-4 and 4-5 is forward condition, opens valve 3-7 and 3-9, ON cycle pump 6, regulated valve 3-1, keep spinner-type flowmeter 2 flows at 45l/h, washed 5 minutes, regulating T-valve 4-2,4-3,4-4 and 4-5 is commutation states flushing 5 minutes.Soft water in the valve-off 3-7, emptying pipeline stops pump 6 runnings, valve-off 3-9 then.Simultaneously, open 3-10, the 1mol/l sodium hydroxide solution in the emptying membrane module, valve-off 3-10 opens valve 3-2 and 3-11, with soft water flushing membrane assembly inner casing, is neutral to water outlet pH value, closes 3-2 and 3-11.
B. acid solution is cleaned.In acid solution jar 1-2,10-2, inject the hydrochloric acid soln of pH=1～1.5.Open valve 3-6 and 3-8, ON cycle pump 6, regulated valve 3-1, keep spinner-type flowmeter 2 flows at 30l/h, washed 45 minutes, and stopped recycle pump 6 operations, adjusting T-valve 4-2,4-3,4-4 and 4-5 is forward condition flushing 10 minutes, hydrochloric acid in the valve-off 3-6 emptying pipeline, valve-off 3-8; Open valve 3-3 simultaneously, make hydrochloric acid be full of membrane module, after recycle pump 6 shuts down, open valve 3-11, the hydrochloric acid in the emptying membrane module.
C. soft water cleans.Open valve 3-7 and 3-9, ON cycle pump 6, regulated valve 3-1, keep spinner-type flowmeter 2 flows at 30l/h, till valve 3-9 water outlet pH value remains on neutrality, adjusting T-valve 4-2,4-3,4-4 and 4-5 is reverse state flushing membrane assembly, till valve 3-9 water outlet pH value remains on neutrality.Close the soft water in the 3-7 emptying pipeline, stop pump 6 runnings then, close 3-9.Simultaneously, opening valve 3-2, with soft water flushing membrane assembly inner chamber, is neutral to valve 3-11 water outlet pH value, closes 3-2.
After soft water-acid solution-soft water cleaning, flux has obtained recovery, the results are shown in following table.
| Intake pressure (MPa) | Top hole pressure (MPa) | Pure water flow (l/h) | Pure water flux (ml/min) | |
| Before not using | 0.005 | 0.08 | 30 | 0.795 |
| Not pickling | 0.004 | 0.0015 | 24 | 0.245 |
| After the pickling | 0.005 | 0.010 | 28 | 0.539 |
Claims (10)
1. one kind is slowed down during with the membrane reactor synthetic polymeric flocculant and cleans the method that film pollutes, and the cleaning process of this method is divided two stages, it is characterized in that: described cleaning process is:
One. the counterflush in the building-up process,
Two. the cleaning behind the end of synthesis comprises:
(1). soft water cleans;
(2). acid solution is cleaned;
(3). soft water cleans.
2. the method for claim 1, it is characterized in that: the counterflush in the described building-up process is in synthetic macromolecule inorganic flocculating agent process, T-valve (4-1) is forward condition, aluminum salt solution flows to arm U by arm W, T-valve (4-6) is forward condition, aluminum salt solution flows to arm T by arm M, and T-valve (4-7) is forward condition, and aluminum salt solution flows to arm S by arm R; Constant flow pump (8) pumps the sodium hydroxide solution in the sodium hydroxide jar (9), and flows to arm T through the arm M of T-valve (4-6), joins in the membrane module shell, sees through membranous wall in film silk inner chamber and aluminum salt solution reaction;
(1). during not with aluminum salt solution recoil membrane module, at first Open valve (3-4) and valve (3-5), aluminum salt solution is sucking-off from circulating reaction jar (1-1) under the suction function of recycle pump (6), through the T-valve (4-1) and the spinner-type flowmeter (2) of forward condition, the flow of aluminum salt solution is regulated by control valve (3-1); T-valve (4-2) is forward condition, flow to arm C from the effusive aluminum salt solution of spinner-type flowmeter (2) by the arm A of T-valve (4-2), T-valve (4-3) is forward condition, flow to arm E from the effusive aluminum salt solution of arm C by the arm D of T-valve (4-3), enter hollow fiber film assembly (5) from the effusive aluminum salt solution of arm E by an end of hollow fiber film assembly (5): constant flow pump (8) pumps the sodium hydroxide solution the sodium hydroxide solution jar (9) and flows to arm T through the arm M of T-valve (4-6), join in the membrane module shell, institute's hydro-oxidation sodium volume is as the criterion with each synthetic desired basicity; And with enter membrane module in aluminum salt solution mix after, flow out through the other end of film silk inner chamber from hollow fiber film assembly (5), T-valve (4-4) is forward condition, flow to arm I from the effusive aluminum salt solution of membrane module (5) by the arm H of T-valve (4-4), T-valve (4-5) is forward condition, flow to arm L from the effusive aluminum salt solution of arm I by the arm J of T-valve (4-5), at last, will increase the aluminum salt solution of sodium hydroxide in T-valve (4-7) is delivered to circulating reaction jar (1-1) through recycle pump (6); The aluminum salt solution that contains sodium hydroxide constantly circulates, till meeting the requirements of basicity;
(2). when membrane module need be used the aluminum salt solution counterflush, close with blow-off valve (3-4) with (3-5); Contain aluminum salt solution sucking-off from circulating reaction jar (1-1) under the suction function of recycle pump (6) of sodium hydroxide, through the T-valve (4-1) and the spinner-type flowmeter (2) of forward condition; T-valve (4-2) is commutation states, flow to arm B from the effusive aluminum salt solution of spinner-type flowmeter (2) by the arm A of T-valve (4-2), T-valve (4-4) is commutation states, flow to arm H from the effusive solution of arm B by the arm G of T-valve (4-4), enter hollow fiber film assembly (5) by an end of hollow fiber film assembly (5) from the effusive aluminum salt solution of arm H; Stop hydro-oxidation sodium this moment, flow out through the other end of film silk inner chamber from hollow fiber film assembly (5); T-valve (4-3) is commutation states, aluminum salt solution flows to arm F by the arm E of T-valve (4-3), T-valve (4-5) is commutation states, flow to arm L from the effusive aluminum salt solution of arm F by the arm K of T-valve (4-5), last aluminum salt solution sends back to aluminum salt solution in the circulating reaction jar (1-1) by recycle pump (6);
After counterflush finished, T-valve returned forward condition by the commutation states adjustment, the state when total system is back to membrane module not with the flushing of aluminium salt, the aluminum salt solution in Open valve (3-4) and the valve (3-5), blowdown piping BaG and FbK.
3. the method for claim 1, it is characterized in that: the cleaning behind the described end of synthesis is the flocculation agent aluminum salt solution in the emptying pipeline: stop constant flow pump (8) running, valve-off (3-11) is opened valve (3-10), the sodium hydroxide in the emptying membrane module (5); Recycle pump (6) remains in operation, and the flocculation agent aluminum salt solution in the emptying pipeline stops the running of recycle pump (6); Then T-valve (4-1) is commutated, make soft water or acid solution flow to arm U by T-valve (4-1) arm V, T-valve (4-6) commutation, aluminum salt solution flows to arm T by T-valve (4-6) arm N, T-valve (4-7) commutation, aluminum salt solution flows to arm Q by T-valve (4-7) arm R; T-valve (4-2), (4-3), (4-4) and (4-5) be forward condition;
Specific implementation method is:
(1). soft water cleans, and behind the end of synthesis, opens valve (3-10), the sodium hydroxide solution in the antiaircraft membrane module, valve-off (3-10) then; Open valve (3-3), (3-6) and (3-8) close with valve (3-2), (3-7), (3-9) with (3-11); Sodium hydroxide in the emptying membrane module shell, valve-off (3-10) then, the soft water in the Open valve (3-11), water softening tank (10-1) is gone in the membrane module shell by flow by gravity, with soft water flushing membrane assembly inner casing at first; ON cycle pump (6), soft water in the water softening tank (1-3) relies on being used for to membrane surface flushing of recycle pump (6), regulated valve (3-1) keeps high flow rate that face is washed, and T-valve (4-2), (4-3), (4-4) and (4-5) be commutation states wash again then; Soft water in the valve-off (3-7) and (3-2), emptying circuit and elements is closed recycle pump (6), adjusts T-valve (4-2), (4-3), (4-4) and (4-5) is forward condition;
(2). acid solution is cleaned, and valve-off (3-11) and (3-9) is opened valve (3-3), (3-6) and (3-8), and the interior acid solution of acid solution jar (10-2) is gone into the membrane module inner casing by flow by gravity; Acid solution in the ON cycle pump (6), acid solution jar (1-2) is cleaned at the pipeline internal recycle by recycle pump (6), stops recycle pump (6); Adjust T-valve (4-2), (4-3), (4-4) and (4-5) be commutation states, ON cycle pump (6) washes with acid again; Valve-off (3-3) and (3-6) is opened valve (3-11), and the acid solution in emptying assembly and the pipeline is adjusted T-valve (4-2), (4-3), (4-4) and (4-5) is forward condition;
(3). soft water cleans, and Open valve (3-2) and valve (3-11) they with soft water flushing membrane assembly inner casing at first, are neutrality until the soft pH value that flows out valve (3-11); Open valve (3-7) and valve (3-9), valve-off (3-6) and valve (3-8), ON cycle pump (6) is neutral until valve (3-9) water outlet; Stop pump (6) running, change T-valve (4-2), (4-3), (4-4) and (4-5) be commutation states, open pump (6) flushing pipeline BaG and pipeline FbK, be neutrality until valve (3-9) water outlet.
4. method as claimed in claim 2 is characterized in that: described film silk is selected polysulfones, polyethersulfone or the SPSF hollow fiber ultrafiltration membrane of molecular weight cut off less than 10,000 daltonian high temperature-resistant acid-resistant alkali for use.
5. as claim 2 or 3 described methods, it is characterized in that: described aluminum salt solution comprises aluminum chloride or alum liquor, and the aluminum salt solution starting point concentration is 0.2～2mol/l; The starting point concentration of described sodium hydroxide is 1～2mol/l.
6. method as claimed in claim 2 is characterized in that: the required saturating mould of described counterflush is controlled at 0.015～0.025MPa.
7. method as claimed in claim 1 or 2 is characterized in that: in each building-up process, before basicity is less than 1.5 and crossflow velocity during less than initial flow rate 90%, need counterflush; In each building-up process, after basicity is greater than 1.5 and crossflow velocity during, need counterflush less than initial flow rate 80%.
8. method as claimed in claim 3 is characterized in that: the working pressure that described soft water cleans is 0.015～0.02MPa.
9. method as claimed in claim 3 is characterized in that: the saturating mould that described acid solution is cleaned hollow fiber film assembly is controlled at 0.015～0.02MPa, and the pickling time remained on 40～60 minutes, and used sour pH value is 1.5～3.
10. as claim 1,3 or 9 described methods, it is characterized in that: described acid is hydrochloric acid, sulfuric acid or nitric acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA021573085A CN1508076A (en) | 2002-12-19 | 2002-12-19 | Method for retarding and washing membrane pollution during synthesizing polymer flocculant using membrane reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CNA021573085A CN1508076A (en) | 2002-12-19 | 2002-12-19 | Method for retarding and washing membrane pollution during synthesizing polymer flocculant using membrane reactor |
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| CN1508076A true CN1508076A (en) | 2004-06-30 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101734789B (en) * | 2009-12-24 | 2011-08-17 | 清华大学 | Method for controlling severe membrane fouling caused by membrane bioreactor mixed solution |
| CN101773787B (en) * | 2009-12-31 | 2012-05-30 | 南京工业大学 | Membrane pollution cleaning method for membrane-process brine refining process |
| CN102880199A (en) * | 2012-09-27 | 2013-01-16 | 东莞市劲升无尘涂装科技有限公司 | Full-automatic PH (potential of hydrogen) value detecting and monitoring and automatic chemical replenishing system for metal spraying |
| CN110960825A (en) * | 2019-12-12 | 2020-04-07 | 北京化工大学 | Double-functional chemical warfare agent degradation material and preparation method thereof |
| CN113493278A (en) * | 2021-03-17 | 2021-10-12 | 波塞冬(江苏)新材料科技有限公司 | Membrane reactor system for preparing polyaluminum chloride from aluminum-containing wastewater |
-
2002
- 2002-12-19 CN CNA021573085A patent/CN1508076A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101734789B (en) * | 2009-12-24 | 2011-08-17 | 清华大学 | Method for controlling severe membrane fouling caused by membrane bioreactor mixed solution |
| CN101773787B (en) * | 2009-12-31 | 2012-05-30 | 南京工业大学 | Membrane pollution cleaning method for membrane-process brine refining process |
| CN102880199A (en) * | 2012-09-27 | 2013-01-16 | 东莞市劲升无尘涂装科技有限公司 | Full-automatic PH (potential of hydrogen) value detecting and monitoring and automatic chemical replenishing system for metal spraying |
| CN110960825A (en) * | 2019-12-12 | 2020-04-07 | 北京化工大学 | Double-functional chemical warfare agent degradation material and preparation method thereof |
| CN110960825B (en) * | 2019-12-12 | 2021-07-30 | 北京化工大学 | Double-functional chemical warfare agent degradation material and preparation method thereof |
| CN113493278A (en) * | 2021-03-17 | 2021-10-12 | 波塞冬(江苏)新材料科技有限公司 | Membrane reactor system for preparing polyaluminum chloride from aluminum-containing wastewater |
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