CN104973658A - Concentrating method of low-concentration phosphoric acid waste liquid - Google Patents
Concentrating method of low-concentration phosphoric acid waste liquid Download PDFInfo
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Abstract
The invention relates to the field of industrial waste water treatment and particularly discloses a concentrating method of a low-concentration phosphoric acid waste liquid which is a relative pure dilute phosphoric acid waste liquid, herein the "relative pure" means that the phosphoric acid waste liquid does not contain or contain few other impurity ions. In the method, the low-concentration phosphoric acid waste liquid is concentrated through a two-stage membrane distillation process, wherein the liquid remained in the two-stage membrane distillation unit is a pure phosphoric acid solution which satisfies a reuse concentration and can be used in a production process. The concentrating method of the low-concentration phosphoric acid waste liquid is carried out through the two-stage membrane distillation process to the low-concentration phosphoric acid waste liquid for recycling the phosphoric acid therein, so that the method can not only save resource but also protect natural ecologic environment, and can be used for treating the relative pure dilute phosphoric acid waste liquid generated in production processes of various industries.
Description
Technical field
The present invention relates to field of industrial waste water treatment, is a kind of concentration method of low phosphorus acid waste liquid specifically.Espespecially adopt the concentration method of two-stage film distillation technology process low phosphorus acid waste liquid.
Background technology
Phosphoric acid is widely used in the industries such as iron and steel, metallurgy, petrochemical industry, and can discharge the waste liquid (phosphate discharge liquid) containing a large amount of waste phosphoric acid in its use procedure, the direct discharge of this kind of waste liquid not only causes serious environmental pollution, and causes the great wasting of resources.Phosphorus is the important indicator of evaluating water quality.When the mass concentration of phosphorus in water body is more than 0.01mg/L, the eutrophication of water just may be caused.
The treatment process of existing phosphate discharge liquid mainly contains biological treatment and method of chemical treatment.Biological treatment long processing period, facility floor space are large, investment is large, and can not recycle the phosphoric acid in waste liquid; Method of chemical treatment mainly adopts the material such as carbide slag, lime to neutralize, and produces the body refuses such as a large amount of phosphoric acid salt in N-process, can not recycle the phosphoric acid in waste liquid, waste ample resources.Therefore, the phosphoric acid recycled in waste liquid is all significant in economy and environment.
In prior art, conventional recovery process has diffusion dialysis, electrodialysis, ion-exchange, extraction etc., but often produces dilute acid soln in these processes, and before recycling, these dilute acid solns have to pass through to concentrate and just can reach reuse desired concn.The method of current industrial concentrated phosphoric acid is the concentrated and vacuum evaporation of high temperature mainly.These concentration process energy consumptions are high, and equipment volume is large, and investment is large, and easily produce phenomenons such as carrying secretly.
Membrane distillation (MD) technology is a kind of new separation technology combined with distillation technique by membrane technique, and it adopts microporous hydrophobic membrane, a kind of Aspect of some new membrane processes being motivating force with film both sides steam pressure difference.The process driving force of membrane distillation is the steam pressure difference of film both sides, the water vapor of higher vapor pressure side and the steam molecule of other volatile constituents spread to low-steam pressure side through fenestra, and in the condensation of low-steam pressure side, formed and produce water, thus reach separation or concentrated object.The advantage of membrane distillation is mainly: it is good to produce water water quality, and the rate of recovery is high, can utilize industrial waste heat.Membrane distillation is compared with multiple-effect evaporation: membrane distillation can cold operation, and it is better to produce water water quality, and distillation efficiency is higher, and there is not fouling and the etching problem of evaporator tower, equipment manufacturing cost is also low than conventional distil-lation tower.
Chinese patent CN103011460A relates to a kind of dephosphorization process of metal-containing salt waste phosphoric acid, adopts the technical process of limestone vegetation+preliminary filtration+anionresin.The method of this patent effectively can remove the phosphorus in phosphate discharge liquid, makes it be transformed into calcium phosphate precipitation.Phosphate discharge liquid after this patent process, the phosphorus content in waste liquid reaches discharging standards.This patent does not relate to the recovery problem of phosphorus in phosphate discharge liquid, is only by phosphate discharge liquid process qualified discharge.
Chinese patent CN101254966A relates to a kind of recovery method of phosphate discharge liquid, adopts the technical process of filtration+ion-exchange+vacuum-evaporation.Adopt this patent, phosphate discharge liquid is after common filtration, and enter ion exchange column and carry out ion-exchange, the phosphoric acid solution after ion-exchange carries out vacuum-evaporation, and by vacuum-evaporation, the major part in phosphoric acid solution or all moisture are removed and are discharged in air.The method that this patent relates to is applicable to the lower phosphate discharge liquid process of concentration.
Summary of the invention
For the defect existed in prior art, the object of the present invention is to provide a kind of concentration method of low phosphorus acid waste liquid, described low phosphorus acid waste liquid is purer dilute phosphoric acid waste liquid, because its relative concentration is lower, can not direct reuse, could reuse after having to pass through concentration.Low phosphorus acid waste liquid described in the method process that the present invention adopts two-stage membrane distillation, is met the pure phosphoric acid solution of reuse concentration after the process of two-stage membrane distillation, can direct reuse in production technique.
For reaching above object, the technical scheme that the present invention takes is:
A concentration method for low phosphorus acid waste liquid, is characterized in that: adopt two-stage film distillation technology to carry out concentration to low phosphorus acid waste liquid.
On the basis of technique scheme, described low phosphorus acid waste liquid is purer dilute phosphoric acid waste liquid, does not contain or contain other foreign ions of minute quantity in described purer finger phosphate discharge liquid.
On the basis of technique scheme, the mass concentration scope of described low phosphorus acid waste liquid is 5% ~ 10%.
On the basis of technique scheme, concrete steps are:
One-level membrane distillation: first, described low phosphorus acid waste liquid enters one-level membrane distillation unit and carries out concentration, and after one-level membrane distillation unit concentration, the trapped fluid of one-level membrane distillation unit is the phosphate discharge liquid after primary concentration;
Secondary membrane is distilled: described phosphate discharge liquid after primary concentration enters secondary membrane distillation unit and carries out concentration further, through secondary membrane distillation unit concentration, phosphate discharge liquid after primary concentration is concentrated to again the concentration of reuse through secondary, the trapped fluid of secondary membrane distillation unit is the pure phosphoric acid solution meeting reuse concentration, can be back to production technique;
In above-mentioned concentration process, the membrane distillation that one-level membrane distillation unit and secondary membrane distillation unit produce produces water combination treatment and recycles or directly discharge.
On the basis of technique scheme, after described low phosphorus acid waste liquid reaches certain temperature, pump into one-level membrane distillation unit as feeding liquid and carry out concentration, after one-level membrane distillation unit concentration, if the trapped fluid of one-level membrane distillation unit does not reach setting concentration, after then the trapped fluid of one-level membrane distillation unit mixes with feeding liquid, again turn back to one-level membrane distillation unit and carry out concentration, if the trapped fluid of one-level membrane distillation unit reaches setting concentration, then one-level membrane distillation unit trapped fluid as the phosphate discharge liquid after primary concentration pump into secondary membrane distillation unit carry out concentration further.
On the basis of technique scheme, there is the phosphate discharge liquid after primary concentration of certain temperature, pump into secondary membrane distillation unit and carry out concentration, after secondary membrane distillation unit concentration, if the trapped fluid of secondary membrane distillation unit does not reach setting concentration, after then the secondary membrane distillation trapped fluid of unit mixes with the phosphate discharge liquid after primary concentration, again turn back to secondary membrane distillation unit and carry out concentration, if the trapped fluid of secondary membrane distillation unit reaches setting concentration, then the trapped fluid of secondary membrane distillation unit is recycled as the pure phosphoric acid solution meeting reuse concentration.
On the basis of technique scheme, described low phosphorus acid waste liquid adopts type of heating to be heated to 67 ~ 85 DEG C.
On the basis of technique scheme, adopt the trapped fluid heat exchange of plastic heat exchanger 1 and secondary membrane distillation unit that low phosphorus acid waste liquid is heated to 67 ~ 85 DEG C.
On the basis of technique scheme, the setting concentration of one-level membrane distillation counts 30% ~ 40% by mass concentration.
On the basis of technique scheme, the setting concentration of secondary membrane distillation is counted by mass concentration and is more than or equal to 50%.
On the basis of technique scheme, the membrane distillation of one-level membrane distillation unit and secondary membrane distillation unit all adopts inner pressed vacuum membrane distillation;
The operational condition of inner pressed vacuum membrane distillation is: one-level membrane distillation crossflow velocity 0.1 ~ 0.6m/s, and secondary membrane distillation crossflow velocity 0.5 ~ 1.0m/s, the cold side vacuum tightness of one-level membrane distillation and secondary membrane distillation is-0.075 ~-0.095MPa.
On the basis of technique scheme, the membrane component form of one-level membrane distillation unit and secondary membrane distillation unit is board-like, hollow fiber form or tubular type;
The mould material of described membrane component is tetrafluoroethylene, and membrane component is one or more groups serial or parallel connection;
The membrane pore size of described membrane component is 0.1 ~ 0.3 μm.
The concentration method of low phosphorus acid waste liquid of the present invention, described low phosphorus acid waste liquid is purer dilute phosphoric acid waste liquid, it is adopted to the method process of two-stage membrane distillation, reclaims phosphoric acid wherein, while saving resource, protects natural ecological environment.Method of the present invention, may be used for processing the purer dilute phosphoric acid waste liquid produced in every profession and trade production process.
The concentration method of low phosphorus acid waste liquid of the present invention, has following beneficial effect:
1, the present invention's dilute phosphoric acid waste liquid of adopting the process of two-stage film distillation technology comparatively pure, in Recycling of waste liquid to greatest extent while phosphoric acid, has also reclaimed the water resources in phosphate discharge liquid, has solved the process of phosphate discharge liquid, discharge and recovery problem;
2, the present invention adopts the advantage of two-stage membrane distillation process process phosphate discharge liquid to be, the concentrated of different phosphate acid waste liquid concentration range is completed by adopting two-stage membrane distillation process, effectively slow down the fouling membrane of two-stage membrane distillation process, extend the stable operation cycle of two-stage membrane distillation process;
3, the membrane distillation process in the present invention do not need impressed pressure or outer pressure pressure very little, method is simple, easily operates;
4, the fouling membrane in the membrane distillation process in the present invention is comparatively light, extends the continuous and steady operation time of membrane distillation process;
5, the distillation device in the present invention adopts plastic piping, and interchanger adopts polytetrafluoroethylplastic plastic interchanger, effectively prevent the etching problem of phosphate discharge liquid to pipeline, and improves heating efficiency;
6, the recovery method of phosphate discharge liquid of the present invention is more simple, efficient, adopts the method for the invention process to reclaim dilute phosphoric acid waste liquid, while turning waste into wealth, solves problem of environmental pollution, have important environmental benefit.
Accompanying drawing explanation
The present invention has following accompanying drawing:
Fig. 1 process flow diagram 1 of the present invention,
Fig. 2 process flow diagram 2 of the present invention.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
The present invention gives a kind of concentration method of low phosphorus acid waste liquid, two-stage film distillation technology is adopted to carry out concentration, described low phosphorus acid waste liquid is purer dilute phosphoric acid waste liquid, do not contain in described purer finger phosphate discharge liquid or contain other foreign ions of minute quantity, the mass concentration scope of described low phosphorus acid waste liquid is 5% ~ 10%, as shown in Figure 1, concrete steps are:
One-level membrane distillation: first, described low phosphorus acid waste liquid (i.e. feeding liquid) enters one-level membrane distillation unit and carries out concentration, after one-level membrane distillation unit concentration, the trapped fluid of one-level membrane distillation unit is the phosphate discharge liquid after primary concentration (i.e. primary concentration liquid);
Secondary membrane is distilled: described phosphate discharge liquid after primary concentration enters secondary membrane distillation unit and carries out concentration further, through secondary membrane distillation unit concentration, phosphate discharge liquid after primary concentration is concentrated to again the concentration of reuse through secondary, the trapped fluid of secondary membrane distillation unit is the pure phosphoric acid solution (i.e. secondary concentration liquid) meeting reuse concentration, can be back to production technique;
In above-mentioned concentration process, the membrane distillation that one-level membrane distillation unit and secondary membrane distillation unit produce produces water (one-level produces water and secondary produces water) combination treatment and recycles or directly discharge.
On the basis of technique scheme, after described low phosphorus acid waste liquid reaches certain temperature (67 ~ 85 DEG C), pump into one-level membrane distillation unit as feeding liquid and carry out concentration, after one-level membrane distillation unit concentration, if the trapped fluid of one-level membrane distillation unit does not reach setting concentration, after then the trapped fluid of one-level membrane distillation unit mixes with feeding liquid, again turn back to one-level membrane distillation unit and carry out concentration, if the trapped fluid of one-level membrane distillation unit reaches setting concentration, then one-level membrane distillation unit trapped fluid as the phosphate discharge liquid after primary concentration pump into secondary membrane distillation unit carry out concentration further.
On the basis of technique scheme, (temperature is by loss 2 DEG C calculation to have certain temperature, then low than one-level membrane distillation feeding liquid 2 DEG C, namely 65 ~ 83 DEG C) the phosphate discharge liquid after primary concentration, pump into secondary membrane distillation unit and carry out concentration, after secondary membrane distillation unit concentration, if the trapped fluid of secondary membrane distillation unit does not reach setting concentration, after then the secondary membrane distillation trapped fluid of unit mixes with the phosphate discharge liquid after primary concentration, again turn back to secondary membrane distillation unit and carry out concentration, if the trapped fluid of secondary membrane distillation unit reaches setting concentration, then the trapped fluid of secondary membrane distillation unit is recycled as the pure phosphoric acid solution meeting reuse concentration.
On the basis of technique scheme, described low phosphorus acid waste liquid, type of heating is adopted to be heated to 67 ~ 85 DEG C, concrete type of heating can be implemented by prior art, not shown in Fig. 1, or as shown in Figure 2, adopt the trapped fluid heat exchange of plastic heat exchanger 1 and secondary membrane distillation unit, low phosphorus acid waste liquid is heated to 67 ~ 85 DEG C, after low phosphorus acid waste liquid reaches 67 ~ 85 DEG C, pump into one-level membrane distillation unit 2 as feeding liquid and carry out concentration, and then pump into secondary membrane distillation unit 3 carry out concentration.
The temperature range of one-level membrane distillation process is 67 ~ 85 DEG C.
Further, the material of described plastic heat exchanger is polytetrafluoroethylmaterial material.
Further, described plastic heat exchanger adopts board-like, hollow fiber form or tubular heat exchanger.
On the basis of technique scheme, the setting concentration of one-level membrane distillation counts 30% ~ 40% by mass concentration.That is: the mass concentration of the phosphate discharge liquid after primary concentration is 30% ~ 40%.
On the basis of technique scheme, the setting concentration of secondary membrane distillation is counted by mass concentration and is more than or equal to 50%.That is: the mass concentration of the pure phosphoric acid solution of reuse concentration is met for being more than or equal to 50%.
On the basis of technique scheme, the membrane distillation of one-level membrane distillation unit and secondary membrane distillation unit all adopts inner pressed vacuum membrane distillation;
The operational condition of inner pressed vacuum membrane distillation is: one-level membrane distillation crossflow velocity 0.1 ~ 0.6m/s, and secondary membrane distillation crossflow velocity 0.5 ~ 1.0m/s, the cold side vacuum tightness of one-level membrane distillation and secondary membrane distillation is-0.075 ~-0.095MPa.
On the basis of technique scheme, the membrane component form of one-level membrane distillation unit and secondary membrane distillation unit is board-like, hollow fiber form or tubular type;
The mould material of described membrane component is tetrafluoroethylene, and membrane component is one or more groups serial or parallel connection;
The membrane pore size of described membrane component is 0.1 ~ 0.3 μm.
The essential distinction of the present invention and prior art is, the present invention adopts two-stage membrane distillation process, processes, the phosphoric acid in concentration and recovery waste liquid for purer dilute phosphoric acid waste liquid.Compared to the prior art, the recovery method of phosphate discharge liquid of the present invention is more simple, efficient, in Recycling of waste liquid to greatest extent while phosphoric acid, also reclaimed the water resources in phosphate discharge liquid, solved the process of phosphate discharge liquid, discharge and recovery problem.
It is below specific embodiment.
Embodiment 1
Process flow diagram is shown in Fig. 1 and Fig. 2.Described phosphate discharge liquid is the dilute phosphoric acid waste liquid of phosphoric acid quality concentration 5%.
Operation steps is as follows:
(1) one-level membrane distillation.First, described phosphate discharge liquid adopts heating or adopts the concentrated solution heat exchange of the board-like interchanger of tetrafluoroethylene and secondary membrane distillation unit to after 67 DEG C, pump into one-level membrane distillation unit and carry out concentration, after one-level membrane distillation circulation concentration, when concentrated solution mass concentration reaches 30%, primary concentration liquid enters step (2) and proceeds the process of secondary membrane distillation and concentration;
(2) secondary membrane distillation.The phosphate discharge liquid of temperature after one-level membrane distillation concentration about 65 DEG C is pumped into secondary membrane distillation unit and proceed concentration, when secondary membrane distillation circulation concentration is recycled to during phosphoric acid quality concentration 50%.In the process, the membrane distillation produced in one-level membrane distillation and secondary membrane still-process produces water combination treatment and recycles or directly discharge;
In above-mentioned steps, membrane component used is the board-like hydrophobic membrane assembly of polytetrafluoroethylene (PTFE), and membrane pore size is 0.2 μm, and membrane distillation form is inner pressed vacuum membrane distillation;
In above-mentioned steps, other operational conditions of membrane distillation process are: one-level membrane distillation crossflow velocity 0.1m/s, secondary membrane distillation crossflow velocity 0.5m/s, cold side vacuum tightness-0.095MPa.Under these conditions, in operational process for three days on end, one-level membrane distillation membrane flux remains on 10 ~ 14L/m
2h, secondary membrane distillation membrane flux remains on 6 ~ 9L/m
2h;
The concentrated phosphoric acid reclaimed after the inventive method process, can be back to production technique.
Embodiment 2
Process flow diagram is shown in Fig. 1 and Fig. 2.Described phosphate discharge liquid is the dilute phosphoric acid waste liquid of phosphoric acid quality concentration 7%.
Operation steps is as follows:
(1) one-level membrane distillation.First, described phosphate discharge liquid adopts heating or adopts the concentrated solution heat exchange of polytetrafluoroethylhollow hollow fiber formula interchanger and secondary membrane distillation unit to after 75 DEG C, pump into one-level membrane distillation unit and carry out concentration, after one-level membrane distillation circulation concentration, when concentrated solution mass concentration reaches 35%, primary concentration liquid enters step (2) and proceeds the process of secondary membrane distillation and concentration;
(2) secondary membrane distillation.The phosphate discharge liquid of temperature after one-level membrane distillation concentration about 73 DEG C is pumped into secondary membrane distillation unit and proceed concentration, when secondary membrane distillation circulation concentration is recycled to during phosphoric acid quality concentration 55%.In the process, the membrane distillation produced in one-level membrane distillation and secondary membrane still-process produces water combination treatment and recycles or directly discharge;
In above-mentioned steps, membrane component used is polytetrafluoroethylene (PTFE) plate and frame hydrophobic membrane assembly, and membrane pore size is 0.3 μm, and membrane distillation form is inner pressed vacuum membrane distillation;
In above-mentioned steps, other operational conditions of membrane distillation process are: one-level membrane distillation crossflow velocity 0.3m/s, secondary membrane distillation crossflow velocity 0.6m/s, cold side vacuum tightness-0.085MPa.Under these conditions, in operational process for three days on end, one-level membrane distillation membrane flux remains on 11 ~ 14L/m
2h, secondary membrane distillation membrane flux remains on 5 ~ 8L/m
2h;
The concentrated phosphoric acid reclaimed after the inventive method process, can be back to production technique.
Embodiment 3
Process flow diagram is shown in Fig. 1 and Fig. 2.Described phosphate discharge liquid is the dilute phosphoric acid waste liquid of phosphoric acid quality concentration 10%.
Operation steps is as follows:
(1) one-level membrane distillation.First, described phosphate discharge liquid adopts heating or adopts the concentrated solution heat exchange of polytetrafluoroethylhollow hollow fiber formula interchanger and secondary membrane distillation unit to after 80 DEG C, pump into one-level membrane distillation unit and carry out concentration, after one-level membrane distillation circulation concentration, when concentrated solution mass concentration reaches 40%, primary concentration liquid enters step (2) and proceeds the process of secondary membrane distillation and concentration;
(2) secondary membrane distillation.The phosphate discharge liquid of temperature after one-level membrane distillation concentration about 78 DEG C is pumped into secondary membrane distillation unit and proceed concentration, when secondary membrane distillation circulation concentration is recycled to during phosphoric acid quality concentration 60%.In the process, the membrane distillation produced in one-level membrane distillation and secondary membrane still-process produces water combination treatment and recycles or directly discharge.
In above-mentioned steps, membrane component used is polytetrafluoroethylene (PTFE) plate and frame hydrophobic membrane assembly, and membrane pore size is 0.2 μm, and membrane distillation form is inner pressed vacuum membrane distillation;
In above-mentioned steps, other operational conditions of membrane distillation process are: one-level membrane distillation crossflow velocity 0.4m/s, secondary membrane distillation crossflow velocity 0.8m/s, cold side vacuum tightness-0.075MPa.Under these conditions, in operational process for three days on end, one-level membrane distillation membrane flux remains on 10 ~ 13L/m
2h, secondary membrane distillation membrane flux remains on 5 ~ 7L/m
2h;
The concentrated phosphoric acid reclaimed after the inventive method process, can be back to production technique.
Embodiment 4
Process flow diagram is shown in Fig. 1 and Fig. 2.Described phosphate discharge liquid is the dilute phosphoric acid waste liquid of phosphoric acid quality concentration 5%.
Operation steps is as follows:
(1) one-level membrane distillation.First, described phosphate discharge liquid adopts heating or adopts the concentrated solution heat exchange of the board-like interchanger of tetrafluoroethylene and secondary membrane distillation unit to after 85 DEG C, pump into one-level membrane distillation unit and carry out concentration, after one-level membrane distillation circulation concentration, when concentrated solution mass concentration reaches 30%, primary concentration liquid enters step (2) and proceeds the process of secondary membrane distillation and concentration;
(2) secondary membrane distillation.The phosphate discharge liquid of temperature after one-level membrane distillation concentration about 83 DEG C is pumped into secondary membrane distillation unit and proceed concentration, when secondary membrane distillation circulation concentration is recycled to during phosphoric acid quality concentration 50%.In the process, the membrane distillation produced in one-level membrane distillation and secondary membrane still-process produces water combination treatment and recycles or directly discharge;
In above-mentioned steps, membrane component used is polytetrafluoroethylene (PTFE) hollow fiber form hydrophobic membrane assembly, and membrane pore size is 0.1 μm, and membrane distillation form is inner pressed vacuum membrane distillation;
In above-mentioned steps, other operational conditions of membrane distillation process are: one-level membrane distillation crossflow velocity 0.6m/s, secondary membrane distillation crossflow velocity 1.0m/s, cold side vacuum tightness-0.085MPa.Under these conditions, in operational process for three days on end, one-level membrane distillation membrane flux remains on 8 ~ 11L/m
2h, secondary membrane distillation membrane flux remains on 6 ~ 9L/m
2h;
The concentrated phosphoric acid reclaimed after the inventive method process, can be back to production technique.
The foregoing is only better possible embodiments of the present invention, not thereby limit to the scope of the claims of the present invention, therefore the equivalence change that every utilization specification sheets of the present invention and accompanying drawing content are done, be all contained in protection scope of the present invention.
The content be not described in detail in this specification sheets belongs to the known prior art of professional and technical personnel in the field.
Claims (12)
1. a concentration method for low phosphorus acid waste liquid, is characterized in that: adopt two-stage film distillation technology to carry out concentration to low phosphorus acid waste liquid.
2. the concentration method of low phosphorus acid waste liquid as claimed in claim 1, is characterized in that: described low phosphorus acid waste liquid is purer dilute phosphoric acid waste liquid, does not contain or contain other foreign ions of minute quantity in described purer finger phosphate discharge liquid.
3. the concentration method of low phosphorus acid waste liquid as claimed in claim 1, is characterized in that: the mass concentration scope of described low phosphorus acid waste liquid is 5% ~ 10%.
4. the concentration method of the low phosphorus acid waste liquid as described in claim 1 or 2 or 3, it is characterized in that, concrete steps are:
One-level membrane distillation: first, described low phosphorus acid waste liquid enters one-level membrane distillation unit and carries out concentration, and after one-level membrane distillation unit concentration, the trapped fluid of one-level membrane distillation unit is the phosphate discharge liquid after primary concentration;
Secondary membrane is distilled: described phosphate discharge liquid after primary concentration enters secondary membrane distillation unit and carries out concentration further, through secondary membrane distillation unit concentration, phosphate discharge liquid after primary concentration is concentrated to again the concentration of reuse through secondary, the trapped fluid of secondary membrane distillation unit is the pure phosphoric acid solution meeting reuse concentration, can be back to production technique;
In above-mentioned concentration process, the membrane distillation that one-level membrane distillation unit and secondary membrane distillation unit produce produces water combination treatment and recycles or directly discharge.
5. the concentration method of low phosphorus acid waste liquid as claimed in claim 4, it is characterized in that: after described low phosphorus acid waste liquid reaches certain temperature, pump into one-level membrane distillation unit as feeding liquid and carry out concentration, after one-level membrane distillation unit concentration, if the trapped fluid of one-level membrane distillation unit does not reach setting concentration, after then the trapped fluid of one-level membrane distillation unit mixes with feeding liquid, again turn back to one-level membrane distillation unit and carry out concentration, if the trapped fluid of one-level membrane distillation unit reaches setting concentration, then one-level membrane distillation unit trapped fluid as the phosphate discharge liquid after primary concentration pump into secondary membrane distillation unit carry out concentration further.
6. the concentration method of low phosphorus acid waste liquid as claimed in claim 4, it is characterized in that: the phosphate discharge liquid after primary concentration with certain temperature, pump into secondary membrane distillation unit and carry out concentration, after secondary membrane distillation unit concentration, if the trapped fluid of secondary membrane distillation unit does not reach setting concentration, after then the secondary membrane distillation trapped fluid of unit mixes with the phosphate discharge liquid after primary concentration, again turn back to secondary membrane distillation unit and carry out concentration, if the trapped fluid of secondary membrane distillation unit reaches setting concentration, then the trapped fluid of secondary membrane distillation unit is recycled as the pure phosphoric acid solution meeting reuse concentration.
7. the concentration method of low phosphorus acid waste liquid as claimed in claim 5, is characterized in that: described low phosphorus acid waste liquid adopts type of heating to be heated to 67 ~ 85 DEG C.
8. the concentration method of low phosphorus acid waste liquid as claimed in claim 7, is characterized in that: adopt the trapped fluid heat exchange of plastic heat exchanger 1 and secondary membrane distillation unit that low phosphorus acid waste liquid is heated to 67 ~ 85 DEG C.
9. the concentration method of low phosphorus acid waste liquid as claimed in claim 5, is characterized in that: the setting concentration of one-level membrane distillation counts 30% ~ 40% by mass concentration.
10. the concentration method of low phosphorus acid waste liquid as claimed in claim 6, is characterized in that: the setting concentration of secondary membrane distillation is counted by mass concentration and is more than or equal to 50%.
The concentration method of 11. low phosphorus acid waste liquids as claimed in claim 4, is characterized in that: the membrane distillation of one-level membrane distillation unit and secondary membrane distillation unit all adopts inner pressed vacuum membrane distillation;
The operational condition of inner pressed vacuum membrane distillation is: one-level membrane distillation crossflow velocity 0.1 ~ 0.6m/s, and secondary membrane distillation crossflow velocity 0.5 ~ 1.0m/s, the cold side vacuum tightness of one-level membrane distillation and secondary membrane distillation is-0.075 ~-0.095MPa.
The concentration method of 12. low phosphorus acid waste liquids as claimed in claim 4, is characterized in that: the membrane component form of one-level membrane distillation unit and secondary membrane distillation unit is board-like, hollow fiber form or tubular type;
The mould material of described membrane component is tetrafluoroethylene, and membrane component is one or more groups serial or parallel connection;
The membrane pore size of described membrane component is 0.1 ~ 0.3 μm.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112499606A (en) * | 2021-01-20 | 2021-03-16 | 江苏电科环保有限公司 | Purification method of phosphoric acid waste liquid |
| CN113772785A (en) * | 2021-09-23 | 2021-12-10 | 苏州华辰净化股份有限公司 | Method and system for treating phosphoric acid waste liquid |
| CN113830744A (en) * | 2021-09-14 | 2021-12-24 | 成都市科隆化学品有限公司 | Method for efficiently concentrating and dechlorinating phosphoric acid |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2504848C (en) * | 2004-06-04 | 2006-08-22 | Aker Kvaerner Canada Inc. | Apparatus and method for osmotic membrane distillation |
| CN101270372A (en) * | 2008-04-15 | 2008-09-24 | 中国石油化工股份有限公司 | Concentration method for sugar liquid in cellulose alcoholic fermentation |
| CN101767847A (en) * | 2010-02-10 | 2010-07-07 | 大连屹东膜工程设备有限公司 | Method for purifying and recycling acid waste liquor based on membrane technology |
| CN102030441A (en) * | 2009-09-29 | 2011-04-27 | 天津膜科力科技有限公司 | Method for treating wastewater in production of sebacic acid |
| CN102491577A (en) * | 2011-06-21 | 2012-06-13 | 天津科技大学 | Multi-stage series membrane distillation strong brine desalting method and device |
| CN102688706A (en) * | 2012-05-18 | 2012-09-26 | 厦门鲲扬膜科技有限公司 | Dilute sulfuric acid membrane distillation and concentration device and concentration method |
| CN102765839A (en) * | 2011-05-05 | 2012-11-07 | 中国科学院生态环境研究中心 | Method for treating wastewater by sodium saccharin acidification and technology thereof |
| CN102923894A (en) * | 2012-10-30 | 2013-02-13 | 北京理工大学 | Process and device for treating reverse osmosis concentrated water through dual-membrane distillation |
| CN202829636U (en) * | 2012-05-04 | 2013-03-27 | 北京能泰高科环保技术股份有限公司 | Device for processing reverse osmosis concentrated brine by using decompressing membrane distillation |
-
2014
- 2014-04-09 CN CN201410141548.8A patent/CN104973658A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2504848C (en) * | 2004-06-04 | 2006-08-22 | Aker Kvaerner Canada Inc. | Apparatus and method for osmotic membrane distillation |
| CN101270372A (en) * | 2008-04-15 | 2008-09-24 | 中国石油化工股份有限公司 | Concentration method for sugar liquid in cellulose alcoholic fermentation |
| CN102030441A (en) * | 2009-09-29 | 2011-04-27 | 天津膜科力科技有限公司 | Method for treating wastewater in production of sebacic acid |
| CN101767847A (en) * | 2010-02-10 | 2010-07-07 | 大连屹东膜工程设备有限公司 | Method for purifying and recycling acid waste liquor based on membrane technology |
| CN102765839A (en) * | 2011-05-05 | 2012-11-07 | 中国科学院生态环境研究中心 | Method for treating wastewater by sodium saccharin acidification and technology thereof |
| CN102491577A (en) * | 2011-06-21 | 2012-06-13 | 天津科技大学 | Multi-stage series membrane distillation strong brine desalting method and device |
| CN202829636U (en) * | 2012-05-04 | 2013-03-27 | 北京能泰高科环保技术股份有限公司 | Device for processing reverse osmosis concentrated brine by using decompressing membrane distillation |
| CN102688706A (en) * | 2012-05-18 | 2012-09-26 | 厦门鲲扬膜科技有限公司 | Dilute sulfuric acid membrane distillation and concentration device and concentration method |
| CN102923894A (en) * | 2012-10-30 | 2013-02-13 | 北京理工大学 | Process and device for treating reverse osmosis concentrated water through dual-membrane distillation |
Non-Patent Citations (1)
| Title |
|---|
| M.TOMASZEWSKA ET AL.: "Study on the concentration of acids by membrane distillation", 《JOURNAL OF MEMBRANE SCIENCE》 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112499606A (en) * | 2021-01-20 | 2021-03-16 | 江苏电科环保有限公司 | Purification method of phosphoric acid waste liquid |
| CN112499606B (en) * | 2021-01-20 | 2022-04-08 | 江苏电科环保有限公司 | Purification method of phosphoric acid waste liquid |
| CN113830744A (en) * | 2021-09-14 | 2021-12-24 | 成都市科隆化学品有限公司 | Method for efficiently concentrating and dechlorinating phosphoric acid |
| CN113772785A (en) * | 2021-09-23 | 2021-12-10 | 苏州华辰净化股份有限公司 | Method and system for treating phosphoric acid waste liquid |
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