CN104211203B - A kind of bittern or seawater ultrafiltration pretreatment technique and pretreatment system - Google Patents
A kind of bittern or seawater ultrafiltration pretreatment technique and pretreatment system Download PDFInfo
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- CN104211203B CN104211203B CN201410508085.4A CN201410508085A CN104211203B CN 104211203 B CN104211203 B CN 104211203B CN 201410508085 A CN201410508085 A CN 201410508085A CN 104211203 B CN104211203 B CN 104211203B
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- 238000000108 ultra-filtration Methods 0.000 title claims abstract description 96
- 238000000034 method Methods 0.000 title claims abstract description 91
- 241001131796 Botaurus stellaris Species 0.000 title claims abstract description 38
- 239000013535 sea water Substances 0.000 title claims abstract description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 269
- 239000012528 membrane Substances 0.000 claims abstract description 96
- 230000008569 process Effects 0.000 claims abstract description 53
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 238000001914 filtration Methods 0.000 claims abstract description 18
- 238000001728 nano-filtration Methods 0.000 claims abstract description 17
- 230000009471 action Effects 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims abstract description 5
- 230000010355 oscillation Effects 0.000 claims abstract description 5
- 238000004140 cleaning Methods 0.000 claims description 112
- 238000011001 backwashing Methods 0.000 claims description 28
- 230000002000 scavenging effect Effects 0.000 claims description 26
- 239000000126 substance Substances 0.000 claims description 25
- 230000008676 import Effects 0.000 claims description 17
- 239000002253 acid Substances 0.000 claims description 16
- 238000010992 reflux Methods 0.000 claims description 13
- 238000005273 aeration Methods 0.000 claims description 12
- 238000010926 purge Methods 0.000 claims description 9
- 239000000835 fiber Substances 0.000 claims description 7
- 238000005406 washing Methods 0.000 claims description 7
- 238000007654 immersion Methods 0.000 claims description 6
- 230000004907 flux Effects 0.000 claims description 5
- 239000012510 hollow fiber Substances 0.000 claims description 4
- 238000009991 scouring Methods 0.000 claims description 4
- 230000000712 assembly Effects 0.000 claims description 3
- 238000000429 assembly Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 6
- 238000007670 refining Methods 0.000 abstract description 6
- 230000003245 working effect Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 6
- 239000003814 drug Substances 0.000 description 5
- 238000002203 pretreatment Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000001954 sterilising effect Effects 0.000 description 3
- 239000012267 brine Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
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- 238000010586 diagram Methods 0.000 description 2
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- 230000009467 reduction Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
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- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
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- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
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Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a kind of bittern or seawater ultrafiltration pretreatment technique and pretreatment system, the filtered water meeting nanofiltration inflow requirement is provided.Belong to water-treatment technology field.Each process cycle comprises filtration stage successively, produces water stage, wash phase and discharge phase, and wash phase comprises gas scouring-air water backwash-gas discharge process; Bittern or seawater are filtered by cartridge filter, secondary filter liquid is carried out filtration by ultrafiltration membrane filter device and produces water, gas discharge process is influent side oil-free compressed air being passed into film silk in membrane module evacuation procedure, pressurized air and water mixing oscillation action are in film silk surface, along with in discharge process, liquid level constantly declines, differentiated levels section air water is washed intensity and is changed, and film silk is from top to bottom cleaned.Technique of the present invention makes the process of bittern or seawater that membrane filtering method can be adopted to carry out, and reduces refining cost, simplifies process for refining, stable water outlet, is conducive to extending nanofiltration membrane work-ing life.
Description
Technical field
The present invention relates to water-treatment technology field, particularly relate to a kind of bittern or seawater ultrafiltration pretreatment technique and pretreatment system.
Background technology
Containing abundant chemical resource in bittern, saltiness is up to 2-6 times of seawater, what wherein content was maximum is sodium-chlor, and sodium-chlor is the basic material of soda ash manufacturing, calcium in bittern, magnesium, sulfate ion can be effectively removed by bittern nanofiltration process for refining, produce water and be used for the industry-specific salt of alkaline, the crude salt consumption during reduction salt is greatly produced, reduction soda manufacture cost.Bittern water quality is complicated, there is the impurity such as suspended substance, microorganism, need to carry out pre-treatment to meet nanofiltration inflow requirement in water body.
At present, bittern mainly contains coagulation-precipitation, clarification, multi-medium filtering etc. in nanofiltration pretreated method before treatment, adopt coagulation-settlement process to need to add chemical agent, drug dosage is large, utilization ratio is low, and the waste residue simultaneously precipitating generation such as to pollute at the environmental problem; Adopt multi-medium filtering Process for Effluent variation water quality large, be difficult to effectively ensure subsequent nano-filtration unit water supply quality.
Water treatment by membrane has without separating proces due to it, does not need to add medicament, does not change the advantages such as water body ion content and is applied in water treatment field.But, bittern water quality is complicated, the impurity such as suspended substance, microorganism is there is in water body, for with supersalinity bittern or seawater for handling object adopts embrane method to process, technique and equipment Design need to consider that bittern pre-treatment may occur to pollute and fouling risk, and pretreated efficiency and feasibility, be not also suitable for the proven technique scheme that bittern adopts embrane method process at present.
Summary of the invention
The object of the invention is the technological deficiency for existing in prior art, and a kind of bittern or seawater ultrafiltration pretreatment technique are provided, the filtered water meeting nanofiltration inflow requirement is provided.
Another object of the present invention is to provide a kind of bittern or seawater ultrafiltration pretreatment system.
The technical scheme adopted for realizing object of the present invention is:
A kind of bittern or seawater ultrafiltration pretreatment technique, each process cycle comprises filtration stage successively, produces water stage, wash phase and discharge phase, and described wash phase comprises the gas scouring-air water backwash-gas discharge process carried out successively; In-site chemical cleaning is carried out after multiple described process cycle;
Described filtration stage: bittern or seawater are filtered by the cartridge filter of precision 100 μm, obtains secondary filter liquid;
The described product water stage: secondary filter liquid is carried out filtration by ultrafiltration membrane filter device and produces water, obtain ultrafiltrated; The pore size filter of ultrafiltration membrane filter device is 0.03-0.1 μm, and producing water phases-time in each process cycle is 20-60 minute, and adopt dead end full dose to filter, flux is 50-80L/ ㎡ h, and water temperature is 20-25 DEG C; Described ultrafiltration membrane filter device adopts external pressure type hollow fiber pillar hyperfiltration membrane assembly; Run transmembrane pressure≤0.15MPa, intake pressure≤0.25MPa;
Described wash phase: described gas discharge process is influent side oil-free compressed air being passed into film silk in described ultrafiltration membrane filter device in membrane module evacuation procedure, pressurized air and water mixing oscillation action are in film silk surface, along with in ultrafiltration membrane filter device described in discharge process, liquid level constantly declines, differentiated levels section air water is washed intensity and is changed, and film silk is from top to bottom cleaned; It is 5-10Nm that gas cleans single assembly tolerance
3/ h, time 20-60s; It is 1-2m that air water washes single the assembly water yield
3/ h, gas-water ratio is 2.5:1-10:1, time 20-60s; It is 5-10Nm that gas discharges single assembly tolerance
3/ h, time 10-30s; Aeration intensity is 248-497m
3/ (m
2h).
Described ultrafiltration pretreatment in-site chemical cleaning, cleaning interval and single scavenging period and nanofiltration process are synchronously carried out.
In-site chemical cleaning adopts circulation/immersion alternate run mode.
Described gas scouring, air water backwash, gas discharge and total time of discharge process are 2-3min.
The pretreatment system that bittern or seawater ultrafiltration pretreatment technique adopt, comprises water feed apparatus, ultrafiltration membrane filter device, buffer tank, back washing device, washing unit, air feeder, reflux and chemicals dosing plant; Described ultrafiltration membrane filter device adopts tubular fibre external pressure pillar hyperfiltration membrane assembly;
Manually-operated gate, raw water box, cartridge filter, water supply magnetic flow meter, water supply automatic valve after described water feed apparatus comprises manually-operated gate before working shaft, working shaft, working shaft, produce water working barrel before manually-operated gate, produce water working barrel, produce water working barrel after manually-operated gate, water inlet automatic valve, described water supply pump outlet is connected with the entrance of described cartridge filter, and the outlet of described cartridge filter is connected with the water-in of described raw water box by described water supply magnetic flow meter, water supply automatic valve; The water outlet of described raw water box is connected with the water-in of described ultrafiltration membrane filter device by manually-operated gate, water inlet automatic valve, inlet gage after manually-operated gate, product water working barrel, product water working barrel before described product water working barrel;
The product mouth of a river of described ultrafiltration membrane filter device be connected with tensimeter and produce water power magnetic flowmeter, the product mouth of a river of described ultrafiltration membrane filter device is connected with the water-in of described buffer tank by producing water automatic valve; Concentrated solution outlet one tunnel of described ultrafiltration membrane filter device is connected with upper valve, and a road is connected with described reflux, and a road is connected with described cleaning; The water-in of described ultrafiltration membrane filter device is connected with lower valve;
Described reflux comprises return pressure table, backflow automatic valve, backflow manually-operated gate and return flow meter, and the concentrated solution outlet of described ultrafiltration membrane filter device is connected with the refluxing opening of return flow meter with described raw water box by described return pressure table, backflow automatic valve, backflow manually-operated gate;
Described back washing device comprises manually-operated gate, backwash under meter, backwash automatic valve after manually-operated gate before backwashing pump, backwashing pump, backwashing pump, and the water outlet of described buffer tank is connected with the product mouth of a river of described ultrafiltration membrane filter device by manually-operated gate, backwash under meter, backwash automatic valve after manually-operated gate, backwashing pump, backwashing pump before described backwashing pump;
Described air feeder comprises air compressor, reducing valve, breather check valve, gas meter, air inlet automatic valve, air inlet manually-operated gate and aeration switch-valve, and the air outlet of described air compressor is connected with the aeration opening of aeration switch-valve with described ultrafiltration membrane filter device through described reducing valve, breather check valve, gas meter, air inlet automatic valve, air inlet manually-operated gate;
Described washing unit comprises cleaning water tank, manually-operated gate before scavenging pump, scavenging pump, manually-operated gate after scavenging pump, cleaning water inlet self-acting valve, clean dense time automatic valve, clean dense movable valve of turning round and stretching out the hand, automatic valve is produced back in cleaning, cleaning product turns round and stretches out the hand movable valve, purge flow gauge, the outlet of described cleaning water tank is by manually-operated gate before described scavenging pump, scavenging pump, manually-operated gate after scavenging pump, cleaning water inlet self-acting valve is connected with the water-in of described ultrafiltration membrane filter device, the concentrated solution outlet of described ultrafiltration membrane filter device is by described cleaning dense time automatic valve, clean dense movable valve of turning round and stretching out the hand, purge flow gauge is connected with the import of described cleaning water tank, automatic valve is produced back by described cleaning in the product mouth of a river of described ultrafiltration membrane filter device, cleaning product turns round and stretches out the hand movable valve, purge flow gauge is connected with the import of described cleaning water tank,
Described chemicals dosing plant comprises cleaning dosing tank, cleaning acid adding case, cleaning dosing volume pump, cleaning acid adding volume pump, the outlet of described cleaning dosing tank is connected with the import of described cleaning dosing volume pump, the outlet of described cleaning acid adding case is connected with the import of described cleaning acid adding volume pump, described cleaning acid adding metering pump outlet and described cleaning dosing measure pump outlet in parallel after be connected to described scavenging pump after manually-operated gate and the cleaning pipeline of intaking between self-acting valve.
Raw water box liquidometer is installed in described raw water box, buffer tank liquidometer is installed in described buffer tank, cleaning water tank liquidometer is installed in described cleaning water tank.
Described chemicals dosing plant also comprises into water dosing tank and water inlet dosing pump, the outlet of described water inlet dosing tank is connected with the import of described water inlet dosing pump, and described water inlet dosing pump outlet is connected to the suction culvert after described product water working barrel between manually-operated gate and water inlet automatic valve.
Described ultrafiltration membrane filter device adopts many group tubular fibre external pressure pillar hyperfiltration membrane assemblies to compose in parallel.
Described raw water box lower end is provided with raw water box discharge manually-operated gate, and described buffer tank lower end is provided with buffer tank exhaust-valve, and the lower end of described cleaning water tank is separately installed with the emptying manually-operated gate of cleaning water tank.
The hyperfiltration membrane assembly bypass outlet Guan Gaodian of described ultrafiltration membrane filter device is provided with vent valve.
Compared with prior art, the invention has the beneficial effects as follows:
1, ultrafiltration pretreatment technique of the present invention is according to the feature of the bittern of supersalinity or seawater self, by rationally determining process means and the technical parameter of hyperfiltration membrane assembly filtration treatment, make the process of bittern or seawater that membrane filtering method can be adopted to carry out, reduce refining cost, simplify process for refining, technique has without phase transformation, less energy-consumption, simple to operate.And, without separating proces, do not need to add medicament, do not change water body ion content, stable water outlet, produce water turbidity <0.1NTU, SDI
15<2, is conducive to extending nanofiltration membrane work-ing life, ensures the steady running of nanofiltration system.
2, technique of the present invention adopts gas to clean, air water backwash, gas discharges three kinds of air water process integrations and carries out physical cleaning to ultra-filtration membrane, gas discharge phase is, in membrane module evacuation procedure, oil-free compressed air is passed into hollow fiber film thread influent side, pressurized air and water mixing oscillation action are in film silk surface, along with in membrane module in discharge process, liquid level constantly declines, differentiated levels section air water is washed intensity and is changed, film silk is from top to bottom cleaned, air water discharge technology is owing to passing into pressurized air in assembly discharge phase, blowing time will be shortened, the pollutant load on film surface is re-attached to because water flow velocity is spent slowly in emissions reduction process, improve cleaning performance.
3, technique of the present invention adopts external pressure process, and water environment capacity is strong, and gas can be adopted to clean, and is more applicable to the subsurface brine that SS content is high, water quality is complicated.
4, because the suspension content of bittern and high viscosity made membrane resistance larger, higher transmembrane pressure is needed in filtration, compared with immersion ultrafiltration, technique of the present invention adopts tubular fibre external pressure pillar hyperfiltration membrane assembly to filter, can be provided by pressurization when cross-film resistance is larger and filter necessary power, thus ensure normally carrying out of subsequent technique.
5, the stop cleaning of technique ultrafiltration system of the present invention and nanofiltration system synchronously carries out, and decreases the cost of manufacture of robot control system(RCS), meanwhile, makes robot control system(RCS) be more convenient for operating.
6, pretreatment system of the present invention is applicable to uf processing bittern or seawater, and structure is simple, convenient operation.
Accompanying drawing explanation
Figure 1 shows that the schematic diagram of bittern of the present invention or seawater ultrafiltration pretreatment system;
Figure 2 shows that 100m
3/ d running situation.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
The schematic diagram of bittern of the present invention or seawater ultrafiltration pretreatment system as shown in Figure 1, comprises water feed apparatus, ultrafiltration membrane filter device 55, buffer tank 56, back washing device, washing unit, air feeder, reflux and chemicals dosing plant; Described ultrafiltration membrane filter device 55 adopts tubular fibre external pressure pillar hyperfiltration membrane assembly.Described ultrafiltration membrane filter device 55 can adopt many group tubular fibre external pressure pillar hyperfiltration membrane assemblies to compose in parallel according to actual needs.
Manually-operated gate 3, raw water box 23, cartridge filter 4, water supply magnetic flow meter 5, water supply automatic valve 6 after described water feed apparatus comprises manually-operated gate 1 before working shaft, working shaft 2, working shaft, produce water working barrel before manually-operated gate 17, produce water working barrel 18, produce water working barrel after manually-operated gate 19, water inlet automatic valve 20, the outlet of described working shaft 2 is connected with the entrance of described cartridge filter 4, and the outlet of described cartridge filter 4 is connected with the water-in of described raw water box 23 by described water supply magnetic flow meter 5, water supply automatic valve 6; The water outlet of described raw water box 23 is connected with the water-in of described ultrafiltration membrane filter device 55 by manually-operated gate 19, water inlet automatic valve 20, inlet gage 21 after manually-operated gate 17, product water working barrel 18, product water working barrel before described product water working barrel.
The product mouth of a river of described ultrafiltration membrane filter device 55 be connected with tensimeter 38 and produce water power magnetic flowmeter 39, the product mouth of a river of described ultrafiltration membrane filter device 55 is connected with the water-in of described buffer tank 56 by producing water automatic valve 40; Concentrated solution outlet one tunnel of described ultrafiltration membrane filter device 55 is connected with upper valve 12, and a road is connected with described reflux, and a road is connected with described cleaning; The water-in of described ultrafiltration membrane filter device 55 is connected with lower valve 25.
Described reflux comprises return pressure table 11, backflow automatic valve 10, backflow manually-operated gate 9 and return flow meter 8, and the concentrated solution outlet of described ultrafiltration membrane filter device is connected with the refluxing opening of return flow meter 8 with described raw water box 23 by described return pressure table 11, backflow automatic valve 10, backflow manually-operated gate 9.
Described back washing device comprises manually-operated gate 46, backwash under meter 45, backwash automatic valve 44 after manually-operated gate 48 before backwashing pump, backwashing pump 47, backwashing pump, and the water outlet of described buffer tank 56 is connected with the product mouth of a river of described ultrafiltration membrane filter device 55 by manually-operated gate 46, backwash under meter 45, backwash automatic valve 44 after manually-operated gate 48, backwashing pump 47, backwashing pump before described backwashing pump.
Described air feeder comprises air compressor 36, reducing valve 35, breather check valve 34, gas meter 33, air inlet automatic valve 32, air inlet manually-operated gate 31 and aeration switch-valve 22, and the air outlet of described air compressor 36 is connected through described reducing valve 35, breather check valve 34, gas meter 33, air inlet automatic valve 32, air inlet manually-operated gate 31 and aeration switch-valve 22 aeration opening with described ultrafiltration membrane filter device 55.
Described washing unit comprises cleaning water tank 57, manually-operated gate 29 before scavenging pump, scavenging pump 28, manually-operated gate 27 after scavenging pump, cleaning water inlet self-acting valve 26, clean dense time automatic valve 13, clean dense movable valve 14 of turning round and stretching out the hand, automatic valve 42 is produced back in cleaning, cleaning product turns round and stretches out the hand movable valve 43, purge flow gauge 15, the outlet of described cleaning water tank 57 is by manually-operated gate 29 before described scavenging pump, scavenging pump 28, manually-operated gate 27 after scavenging pump, cleaning water inlet self-acting valve 26 is connected with the water-in of described ultrafiltration membrane filter device 55, the concentrated solution outlet of described ultrafiltration membrane filter device 55 is by described cleaning dense time automatic valve 13, clean dense movable valve 14 of turning round and stretching out the hand, purge flow gauge 15 is connected with the import of described cleaning water tank 57, automatic valve 42 is produced back by described cleaning in the product mouth of a river of described ultrafiltration membrane filter device 55, cleaning product turns round and stretches out the hand movable valve 43, purge flow gauge 15 is connected with the import of described cleaning water tank 57.
Described chemicals dosing plant comprises cleaning dosing tank 52, cleaning acid adding case 54, cleaning dosing volume pump 50, cleaning acid adding volume pump 51, the outlet of described water inlet dosing tank 53 is connected with the import of described water inlet dosing pump 24, and the outlet of described water inlet dosing pump 24 is connected to the suction culvert after described product water working barrel between manually-operated gate 19 and water inlet automatic valve 20; The outlet of described cleaning dosing tank 52 is connected with the import of described cleaning dosing volume pump 50, the outlet of described cleaning acid adding case 54 is connected with the import of described cleaning acid adding volume pump 51, manually-operated gate 27 and clean the pipeline of intaking between self-acting valve 26 after being connected to described scavenging pump after the outlet of described cleaning acid adding volume pump 51 is in parallel with the outlet of described cleaning dosing volume pump 50.
When former water raw water quality is poor, when needing to carry out sterilization deactivation pre-treatment, described chemicals dosing plant also comprises into water dosing tank 53 and water inlet dosing pump 24, the outlet of described water inlet dosing tank 53 is connected with the import of described water inlet dosing pump 24, and the outlet of described water inlet dosing pump 24 is connected to the suction culvert after described product water working barrel between manually-operated gate 19 and water inlet automatic valve 20.
For the ease of Liquid level, in described raw water box 23, raw water box liquidometer 7 is installed, in described buffer tank 56, buffer tank liquidometer 41 is installed, cleaning water tank liquidometer 37 is installed in described cleaning water tank 57.
For the ease of the cleaning of liquid water tank, described raw water box 23 lower end is provided with raw water box discharge manually-operated gate 16, and described buffer tank 56 lower end is provided with buffer tank exhaust-valve 49, and the lower end of described cleaning water tank 57 is separately installed with the emptying manually-operated gate 30 of cleaning water tank.
For the ease of gaseous emission, the hyperfiltration membrane assembly bypass outlet Guan Gaodian of described ultrafiltration membrane filter device 55 is provided with vent valve 58, prevents in dead end full dose filtration procedure, have gas residue to affect in return line and produces water.
In bittern of the present invention or seawater ultrafiltration pretreatment technique, each process cycle comprises filtration stage successively, produces water stage, wash phase and discharge phase, described wash phase comprises the gas scouring-air water backwash-gas discharge process carried out successively, after multiple described process cycle, carry out in-site chemical cleaning.Different according to former water pollution degree, generally after 80-440 process cycle, carry out in-site chemical cleaning.
Described filtration stage: bittern or seawater are filtered by the cartridge filter of precision 100 μm, obtains secondary filter liquid.
The described product water stage: secondary filter liquid is carried out filtration by ultrafiltration membrane filter device and produces water, obtain ultrafiltrated; The pore size filter of ultrafiltration membrane filter device is 0.03-0.1 μm, and producing water phases-time in each process cycle is 20-60 minute, and adopt dead end full dose to filter, flux is 50-80L/ ㎡ h, and water temperature is 20-25 DEG C; Described ultrafiltration membrane filter device adopts external pressure type hollow fiber pillar hyperfiltration membrane assembly; Run transmembrane pressure≤0.15MPa, intake pressure≤0.25MPa.
Described wash phase: gas scouring-air water backwash process is same as the prior art, adds gas discharge process.Described gas discharge process is influent side oil-free compressed air being passed into film silk in described ultrafiltration membrane filter device in membrane module evacuation procedure, pressurized air and water mixing oscillation action are in film silk surface, along with in ultrafiltration membrane filter device described in discharge process, liquid level constantly declines, differentiated levels section air water is washed intensity and is changed, and film silk is from top to bottom cleaned; It is 5-10Nm that gas cleans single assembly tolerance
3/ h, time 20-60s; It is 1-2m that air water washes single the assembly water yield
3/ h, gas-water ratio is 2.5:1-10:1, time 20-60s; It is 5-10Nm that gas discharges single assembly tolerance
3/ h, time 10-30s; Aeration intensity is 248-497m
3/ (m
2h).
For the ease of controlling, described ultrafiltration pretreatment in-site chemical cleaning, cleaning interval and single scavenging period and nanofiltration process are synchronously carried out.
In-site chemical cleaning adopts circulation/immersion alternate run mode.
Described gas scouring, air water backwash, gas discharge and total time of discharge process are 2-3min.
The detailed process of technique is: all manually-operated gates except raw water box discharge manually-operated gate 16, backwash water tank exhaust-valve 49, the emptying manually-operated gate of cleaning water tank 30 are opened before opening by system, start water supply automatic valve 6, working shaft 2, former water enters raw water box 23 through working shaft 2, cartridge filter 4, the precision of cartridge filter is 100 μm, to meet the water supply needs of ultrafiltration technology.The startup of water supply automatic valve 6, working shaft 2 stops being controlled by raw water box liquidometer 7, and the raw water box high liquid level that liquid level reaches setting is then shut down, and liquid level then starts lower than the low liquid level of raw water box of setting.Then first carry out the product water stage, start after opening water inlet automatic valve 20, backflow automatic valve 10, product water automatic valve 40 and produce water working barrel 18, now former water can be injected in ultrafiltration membrane filter device 55 from bottom to top by raw water box 23, after being full of water in assembly, unnecessary water can be overflowed by refluxing opening, be back to raw water box 23 by backflow automatic valve 10, then closing volume automatic valve 10 carries out product water.Run transmembrane pressure≤0.15MPa, intake pressure≤0.25MPa.It is inner that former water enters film silk by film silk outside surface under the effect of pressure difference, is transported to buffer tank 56 after the production water convergence of film silk inside by producing water producing pipe road, water automatic valve 40 place.Stating chemicals dosing plant also comprises into water dosing tank 53 and water inlet dosing pump 24, the outlet of described water inlet dosing tank 53 is connected with described import, and the outlet of described water inlet dosing pump 24 is connected to the suction culvert after described product water working barrel between manually-operated gate 19 and water inlet automatic valve 20.If process raw water quality is poor, when needing to carry out sterilization deactivation pre-treatment, then sterilant to be prepared and add in water dosing tank 53, added by water inlet dosing pump 24 afterwards in the suction culvert produced after water working barrel between manually-operated gate 19 and water inlet automatic valve 20, water inlet dosing pump 24 with produce water working barrel 18 and link, the medicine added in pipeline mixes with water inlet that to carry out sterilizing alive.Step sequence is cleaned in the laggard promoting the circulation of qi of product water through 20-60min.Close and produce water working barrel 18, water inlet automatic valve 20, produce water automatic valve 40, air inlet automatic valve 32 is opened after unlatching being arranged automatic valve 12, now gas is entered by cleaning film silk with the combined action of water in ultrafiltration membrane filter device 55 by assembly bottom, and gas and a part of water are discharged by upper row's automatic valve 12.It is 20-60s that gas cleans the step sequence time.After gas is cleaned and is terminated, carry out air water backwash step sequence, open backwash automatic valve 44, backwashing pump 47, the product water in buffer tank 56 produces water end (W.E.) by film silk and oppositely enters membrane module, carry out combined cleaning to film silk together with the gas entering membrane module, gas and sewage are discharged by upper row's automatic valve 12.Air water backwash step sequence time 20-60s.Air water backwash terminates laggard promoting the circulation of qi discharge step sequence, close backwashing pump 47, backwash automatic valve 44, open lower row's automatic valve 25, the liquid level now in membrane module reduces gradually, gas and the film silk of water combined action to different levels section clean, gas discharge step sequence time 10-30s.After gas discharge technology terminates, enter discharge phase, close air inlet automatic valve 32, drain time is as the criterion to be emptied completely water in assembly, the general time is at 30-100s, time closes row automatic valve 12, lower row's automatic valve 25 to rear pass, now complete a process cycle, enter next process cycle afterwards.Circulation like this repeatedly, carries out ultrafiltration pretreatment.Generation after ultrafiltration pretreatment enters nanofiltration treatment system from buffer tank 56 and carries out nanofiltration process.
After the work through 80-440 process cycle, needing to be serviced property in-site chemical cleaning.After discharge step sequence terminates, open backwash automatic valve 44, automatic valve 42, backwashing pump 47 are produced back in cleaning, cleaning water tank 57 is injected by producing water in buffer tank, arrive after specifying liquid level and close backwashing pump 47, backwash automatic valve 44, open cleaning dense time automatic valve 13, cleaning water inlet self-acting valve 26, scavenging pump 28, cleaning dosing volume pump 50 or cleaning acid adding volume pump 51 to circulate, the working time of cleaning dosing volume pump sets according to required medicine calculation, cycling time 10-30min, circular flow 2-6m
3/ h.Close scavenging pump 28 after loop ends, clean dense time automatic valve 13, cleaning water inlet self-acting valve 26, cleaning produce back automatic valve 42, immersion membrane module, soak time 30-90min.The normal process cycle is entered after carrying out gas scouring, air water backwash, gas discharge, discharge step sequence according to normal process after immersion terminates.
Shandong alkaline plant area 100m
3/ d brine refining project adopts above-mentioned ultrafiltration pretreatment technique to carry out ultra-filtration filters bittern, and test-results is as follows:
1, by evaluating the place to go effect of SS, turbidity after ultrafiltration pretreatment, result is as shown in table 1.
Table 1
| Water-quality guideline | Former water | Film produces water |
| Turbidity (NTU) | 15.4 | 0.097 |
| SS(mg/L) | 65.2 | 0 |
| SDI 15 | <2 |
Through the bittern water turbidity <0.1NTU of this art breading, SDI
15<2, meets nanofiltration inflow requirement completely.
2, by ultra-filtration filters bittern, evaluate ultra-filtration membrane place to go effect and system run all right, running situation as shown in Figure 2.
Ultrafiltration pretreatment system technique described in design flux 60LMH down-sampling is run as shown in Figure 2, system running pressure is stablized, transmembrane pressure maintains 55-62kPa, and the lower level before operation 140 cycles (about 72h) make pressure recovery arrive cleaning by described maintainability in-site chemical cleaning technique afterwards, entire system operates steadily.
3, the running condition of ultrafiltration module when designing flux 40-70LMH (standard water temperature condition 20 DEG C) was once investigated in pilot scale in carrying out, and overall operation is steady, and TMP maintains 30-60KPa.
4, after adopting hyperfiltration process to carry out pre-treatment to bittern, nanofiltration membrane pollution speed obviously slows down, and the cleaning interval extends 1 times.
The above is only the preferred embodiment of the present invention; it should be pointed out that for those skilled in the art, under the premise without departing from the principles of the invention; can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (10)
1. bittern or a seawater ultrafiltration pretreatment technique, is characterized in that, each process cycle comprises filtration stage successively, produces water stage, wash phase and discharge phase, and described wash phase comprises the gas scouring-air water backwash-gas discharge process carried out successively; In-site chemical cleaning is carried out after multiple described process cycle;
Described filtration stage: bittern or seawater are filtered by the cartridge filter of precision 100 μm, obtains secondary filter liquid;
The described product water stage: secondary filter liquid is carried out filtration by ultrafiltration membrane filter device and produces water, obtain ultrafiltrated; The pore size filter of ultrafiltration membrane filter device is 0.03-0.1 μm, and producing water phases-time in each process cycle is 20-60 minute, and adopt dead end full dose to filter, flux is 50-80L/ ㎡ h, and water temperature is 20-25 DEG C; Described ultrafiltration membrane filter device adopts external pressure type hollow fiber pillar hyperfiltration membrane assembly; Run transmembrane pressure≤0.15MPa, intake pressure≤0.25MPa;
Described wash phase: described gas discharge process is influent side oil-free compressed air being passed into film silk in described ultrafiltration membrane filter device in membrane module evacuation procedure, pressurized air and water mixing oscillation action are in film silk surface, along with in ultrafiltration membrane filter device described in discharge process, liquid level constantly declines, differentiated levels section air water is washed intensity and is changed, and film silk is from top to bottom cleaned; It is 5-10Nm that gas cleans single assembly tolerance
3/ h, time 20-60s; It is 1-2m that air water washes single the assembly water yield
3/ h, gas-water ratio is 2.5:1-10:1, time 20-60s; It is 5-10Nm that gas discharges single assembly tolerance
3/ h, time 10-30s; Aeration intensity is 248-497m
3/ (m
2h).
2. bittern according to claim 1 or seawater ultrafiltration pretreatment technique, is characterized in that, described ultrafiltration pretreatment in-site chemical cleaning, cleaning interval and single scavenging period and nanofiltration process are synchronously carried out.
3. bittern according to claim 1 and 2 or seawater ultrafiltration pretreatment technique, is characterized in that, in-site chemical cleaning adopts circulation/immersion alternate run mode.
4. bittern according to claim 1 and 2 or seawater ultrafiltration pretreatment technique, is characterized in that, described gas scouring, air water backwash, gas discharge and total time of discharge process are 2-3min.
5. the pretreatment system that adopts of a bittern according to claim 1 or seawater ultrafiltration pretreatment technique, it is characterized in that, comprise water feed apparatus, ultrafiltration membrane filter device, buffer tank, back washing device, washing unit, air feeder, reflux and chemicals dosing plant; Described ultrafiltration membrane filter device adopts tubular fibre external pressure pillar hyperfiltration membrane assembly;
Manually-operated gate, raw water box, cartridge filter, water supply magnetic flow meter, water supply automatic valve after described water feed apparatus comprises manually-operated gate before working shaft, working shaft, working shaft, produce water working barrel before manually-operated gate, produce water working barrel, produce water working barrel after manually-operated gate, water inlet automatic valve, described water supply pump outlet is connected with the entrance of described cartridge filter, and the outlet of described cartridge filter is connected with the water-in of described raw water box by described water supply magnetic flow meter, water supply automatic valve; The water outlet of described raw water box is connected with the water-in of described ultrafiltration membrane filter device by manually-operated gate, water inlet automatic valve, inlet gage after manually-operated gate, product water working barrel, product water working barrel before described product water working barrel;
The product mouth of a river of described ultrafiltration membrane filter device be connected with tensimeter and produce water power magnetic flowmeter, the product mouth of a river of described ultrafiltration membrane filter device is connected with the water-in of described buffer tank by producing water automatic valve; Concentrated solution outlet one tunnel of described ultrafiltration membrane filter device is connected with upper valve, and a road is connected with described reflux, and a road is connected with described washing unit; The water-in of described ultrafiltration membrane filter device is connected with lower valve;
Described reflux comprises return pressure table, backflow automatic valve, backflow manually-operated gate and return flow meter, and the concentrated solution outlet of described ultrafiltration membrane filter device is connected with the refluxing opening of return flow meter with described raw water box by described return pressure table, backflow automatic valve, backflow manually-operated gate;
Described back washing device comprises manually-operated gate, backwash under meter, backwash automatic valve after manually-operated gate before backwashing pump, backwashing pump, backwashing pump, and the water outlet of described buffer tank is connected with the product mouth of a river of described ultrafiltration membrane filter device by manually-operated gate, backwash under meter, backwash automatic valve after manually-operated gate, backwashing pump, backwashing pump before described backwashing pump;
Described air feeder comprises air compressor, reducing valve, breather check valve, gas meter, air inlet automatic valve, air inlet manually-operated gate and aeration switch-valve, and the air outlet of described air compressor is connected with the aeration opening of aeration switch-valve with described ultrafiltration membrane filter device through described reducing valve, breather check valve, gas meter, air inlet automatic valve, air inlet manually-operated gate;
Described washing unit comprises cleaning water tank, manually-operated gate before scavenging pump, scavenging pump, manually-operated gate after scavenging pump, cleaning water inlet self-acting valve, clean dense time automatic valve, clean dense movable valve of turning round and stretching out the hand, automatic valve is produced back in cleaning, cleaning product turns round and stretches out the hand movable valve, purge flow gauge, the outlet of described cleaning water tank is by manually-operated gate before described scavenging pump, scavenging pump, manually-operated gate after scavenging pump, cleaning water inlet self-acting valve is connected with the water-in of described ultrafiltration membrane filter device, the concentrated solution outlet of described ultrafiltration membrane filter device is by described cleaning dense time automatic valve, clean dense movable valve of turning round and stretching out the hand, purge flow gauge is connected with the import of described cleaning water tank, automatic valve is produced back by described cleaning in the product mouth of a river of described ultrafiltration membrane filter device, cleaning product turns round and stretches out the hand movable valve, purge flow gauge is connected with the import of described cleaning water tank,
Described chemicals dosing plant comprises cleaning dosing tank, cleaning acid adding case, cleaning dosing volume pump, cleaning acid adding volume pump, the outlet of described cleaning dosing tank is connected with the import of described cleaning dosing volume pump, the outlet of described cleaning acid adding case is connected with the import of described cleaning acid adding volume pump, described cleaning acid adding metering pump outlet and described cleaning dosing measure pump outlet in parallel after be connected to described scavenging pump after manually-operated gate and the cleaning pipeline of intaking between self-acting valve.
6. pretreatment system according to claim 5, is characterized in that, is provided with raw water box liquidometer in described raw water box, is provided with buffer tank liquidometer in described buffer tank, is provided with cleaning water tank liquidometer in described cleaning water tank.
7. the pretreatment system according to claim 5 or 6, it is characterized in that, described chemicals dosing plant also comprises into water dosing tank and water inlet dosing pump, the outlet of described water inlet dosing tank is connected with the import of described water inlet dosing pump, and described water inlet dosing pump outlet is connected to the suction culvert after described product water working barrel between manually-operated gate and water inlet automatic valve.
8. pretreatment system according to claim 7, is characterized in that, described ultrafiltration membrane filter device adopts many group tubular fibre external pressure pillar hyperfiltration membrane assemblies to compose in parallel.
9. pretreatment system according to claim 7, it is characterized in that, described raw water box lower end is provided with raw water box discharge manually-operated gate, and described buffer tank lower end is provided with buffer tank exhaust-valve, and the lower end of described cleaning water tank is separately installed with the emptying manually-operated gate of cleaning water tank.
10. pretreatment system according to claim 7, is characterized in that, the hyperfiltration membrane assembly bypass outlet Guan Gaodian of described ultrafiltration membrane filter device is provided with vent valve.
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| CN106630299A (en) * | 2017-01-22 | 2017-05-10 | 新疆莱特莱德环境工程有限公司 | Recycling utilization system and method for regenerated brine waste liquid |
| CN109607683B (en) * | 2018-12-27 | 2024-02-06 | 三达膜科技（厦门）有限公司 | Mutual backwashing ultrafiltration device |
| CN110981001A (en) * | 2019-11-26 | 2020-04-10 | 浙江津膜环境科技有限公司 | Immersed high-strength membrane filtration process and system for pretreatment of printing and dyeing wastewater |
| CN110845034A (en) * | 2019-11-27 | 2020-02-28 | 四川铭优阳水处理工程技术有限公司 | Process for regenerating and recycling waste strong brine from pickled vegetable and pickle |
| CN111498949A (en) * | 2020-04-30 | 2020-08-07 | 苏州宝典环保科技有限公司 | Ultrafiltration membrane separation device |
| CN111701455A (en) * | 2020-06-12 | 2020-09-25 | 山信软件股份有限公司 | Ultrafiltration system |
| CN111747568A (en) * | 2020-07-06 | 2020-10-09 | 金盛海洋科技有限公司 | Large-scale continuous seawater salt manufacturing bittern refining system |
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