CN104692580B - A kind of fermented pharmaceutical waste water total system and method - Google Patents
A kind of fermented pharmaceutical waste water total system and method Download PDFInfo
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- CN104692580B CN104692580B CN201510126594.5A CN201510126594A CN104692580B CN 104692580 B CN104692580 B CN 104692580B CN 201510126594 A CN201510126594 A CN 201510126594A CN 104692580 B CN104692580 B CN 104692580B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 160
- 239000010826 pharmaceutical waste Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims description 22
- 238000000926 separation method Methods 0.000 claims abstract description 55
- 239000001301 oxygen Substances 0.000 claims abstract description 49
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 49
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 32
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 32
- 239000010865 sewage Substances 0.000 claims abstract description 30
- 238000009284 supercritical water oxidation Methods 0.000 claims abstract description 24
- 238000005374 membrane filtration Methods 0.000 claims abstract description 20
- 239000007787 solid Substances 0.000 claims abstract description 20
- 239000012530 fluid Substances 0.000 claims abstract description 18
- 239000002351 wastewater Substances 0.000 claims abstract description 15
- 239000012528 membrane Substances 0.000 claims description 37
- 239000007788 liquid Substances 0.000 claims description 27
- 238000004519 manufacturing process Methods 0.000 claims description 21
- 238000001704 evaporation Methods 0.000 claims description 18
- 230000008020 evaporation Effects 0.000 claims description 18
- 230000001112 coagulating effect Effects 0.000 claims description 17
- 238000001914 filtration Methods 0.000 claims description 11
- 238000001556 precipitation Methods 0.000 claims description 11
- 150000003839 salts Chemical class 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical group O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 8
- 108091006146 Channels Proteins 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims description 7
- 238000004062 sedimentation Methods 0.000 claims description 7
- 230000003647 oxidation Effects 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 102000010637 Aquaporins Human genes 0.000 claims description 4
- 108010063290 Aquaporins Proteins 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- 238000010612 desalination reaction Methods 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 238000005191 phase separation Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 claims description 2
- 230000006837 decompression Effects 0.000 claims description 2
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 239000005416 organic matter Substances 0.000 claims description 2
- 238000000855 fermentation Methods 0.000 abstract description 2
- 230000004151 fermentation Effects 0.000 abstract description 2
- 239000003814 drug Substances 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000007059 acute toxicity Effects 0.000 description 1
- 231100000403 acute toxicity Toxicity 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000003851 biochemical process Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 230000005405 multipole Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 239000003403 water pollutant Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
- C02F1/003—Processes for the treatment of water whereby the filtration technique is of importance using household-type filters for producing potable water, e.g. pitchers, bottles, faucet mounted devices
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/343—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the pharmaceutical industry, e.g. containing antibiotics
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/043—Treatment of partial or bypass streams
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention relates to a kind of novel fermentation class pharmacy waste water total system, it includes pretreatment unit, sewage enrichment unit and supercritical water oxidation unit；The entrance of sewage enrichment unit connects the pretreatment unit, and sewage carries out membrane filtration and film concentration in the sewage enrichment unit, and the clear water output of sewage enrichment unit connects a clear water reserviors；Starting fluid system, overcritical water oxidization reactor, gas solid separation system, the Separate System of Water-jet of the supercritical water oxidation unit are sequentially connected, the sewage inlet of overcritical water oxidization reactor connects the concentrated water outlet of the sewage enrichment unit, the oxygen intake of overcritical water oxidization reactor connects the oxygen supply system, and the outlet of Separate System of Water-jet connects the clear water reserviors.Film enrichment and supercritical water oxidation R. concomitans are enable the fermented pharmaceutical waste water of wider COD value to carry out supercritical water oxidation processing, organic removal rate more than 99 percent administers thorough, cost is relatively low by the present invention.
Description
Technical field
The invention belongs to sewage disposal and energy resource circulation and stress technical field, it is related to a kind of fermented pharmaceutical waste water comprehensive
Close processing system and method.
Background technology
Fermented pharmaceutical waste water is from the process such as fermentation, filtering, extractive crystallization, refinement, refined.Major pollutants index
It is PH, colourity, BOD5, COD, SS, vegetable and animals oils, ammonia nitrogen and TOC contents, acute toxicity, total Zn content and total cyanide content
Deng.Complicated component, carbon-nitrogen ratio imbalance, biodegradability is poor, and contains a large amount of sulfate, the biochemistry such as drug titers and its degradation product
Mortifier.At present, domestic and international application is few and not mature enough in the fermented pharmaceutical waste water treatment technology of engineering practice.For hair
The features such as complicated component that ferment class pharmacy waste water has, pollutant concentration are high, biodegradability is poor, at present to the processing of such waste water
It is main use physico-chemical process (including investment, coagulant sedimentation, light degradation method, counter-infiltration and membrane separation technique, absorption method and
Electrolysis), the group technology of biochemical process and a variety of methods.Though current technique can remove most of pollutant in waste water,
But the removal effect to organic pollution is not good, and exceeded phenomenon often occurs in effluent color dilution, it is impossible to meet《Ferment class pharmaceuticals industry water
Pollutant emission standard》It is required that, in addition it is also necessary to carry out successive depths processing；Particularly recycling is also managed not to the utmost in wastewater treatment process
Think.Accordingly, it would be desirable to seek a kind of fermented pharmaceutical waste water total system being more suitable for and method.
The content of the invention
The object of the present invention is to overcome the problems of the prior art and there is provided a kind for the treatment of effeciency height, zero dirt for deficiency
Dye discharge, fermented pharmaceutical waste water total system and method simple to operate, that the energy and resource reclaim can be realized simultaneously.
The present invention solves its technical problem and is achieved through the following technical solutions：
A kind of fermented pharmaceutical waste water total system, it is characterised in that：It includes pretreatment unit, sewage enrichment list
Member and supercritical water oxidation unit；Wherein, the entrance of the sewage enrichment unit connects the pretreatment unit, and sewage is described
Membrane filtration and film concentration are carried out in sewage enrichment unit, the clear water output of sewage enrichment unit connects a clear water reserviors；It is described super to face
Boundary's water oxidation unit includes oxygen supply system, starting fluid system, overcritical water oxidization reactor, gas solid separation system, gas
Liquid separation system, wherein, starting fluid system, overcritical water oxidization reactor, gas solid separation system, Separate System of Water-jet are successively
Connection, the sewage inlet of the overcritical water oxidization reactor connects the concentrated water outlet of the sewage enrichment unit, supercritical water
The oxygen intake of oxidation reactor connects the oxygen supply system, and the outlet of the Separate System of Water-jet connects the clear water
Pond.
The sewage enrichment unit includes intermediate pool, the first filter, the second filter, the 3rd filter；In described
Between the entrance in pond connect the pretreatment unit, the production water out of second filter, the concentrated water of the 3rd filter
Outlet is connected with intermediate pool, and the entrance of outlet connection first filter of the intermediate pool is to carry out membrane filtration；
The entrance of concentrated water outlet connection second filter of first filter, the production water out connection of first filter
The entrance of 3rd filter, the clear water output of the 3rd filter connects the clear water reserviors, second filter
The material inlet of the concentrated water outlet connection overcritical water oxidization reactor, realizes that film is concentrated.
First filter, the second filter and the 3rd filter are dish tubular type membrane separation device, dish tubular membrane point
From device by pressure casing, power supply end cap, intake end cover, flow guiding disc, disc-type film bag, battery lead plate and center pull rod are constituted, electricity
Source lid, multiple flow guiding discs and intake end cover are stacked successively, and install fixation using center pull rod in the middle；Pressure casing is close
Sealing is loaded on outside power supply end cap and intake end cover, and raw water passage is formed between the flow guiding disc periphery and pressure casing；Flow guiding disc
Middle part is formed with notch, to form filtration channel；Production aquaporin is formed between flow guiding disc Center-to-Center pull bar, in adjacent two water conservancy diversion
Closed assembly disc-type film bag between disk, disc-type film bag forms filtration channel with not contacted between flow guiding disc up and down；Stacked
Film bag is internal to install battery lead plate.
The pretreatment unit includes the regulating reservoir being sequentially communicated, coagulative precipitation tank, membrane filtration pond.
Described overcritical water oxidization reactor includes cylinder, burner, evaporation wall；The inner barrel is arranged concentrically steaming
Wall is sent out, the narrow gap of the closing for the multistage annular being axially distributed along cylinder is formed between the evaporation wall and cylinder, it is each described narrow
Gap is provided with water inlet on cylinder, and the liquid being passed through via water inlet can be penetrated into by the evaporation wall, the table in evaporation wall
Face forms moisture film；Burner is stretched into from the top of cylinder, and the burner of the burner is located in cylinder, and evaporation wall is by porous material
It is made, the liquid is subcritical water, cylinder top is formed with sewage inlet and oxygen intake, and burner is formed with fuel inlet and oxygen
Gas entrance, cylinder body bottom is formed with liquid outlet.
Heat-exchange system, the steam (vapor) outlet connection steam utilization of the heat-exchange system are set after the gas solid separation system
Equipment.
It is characterized in that setting pressure energy recovery system after described heat-exchange system, gas-liquid separation system is connected after decompression
System.
A kind of fermented pharmaceutical waste water integrated conduct method, step includes：
1) homogeneous：Homogeneous is carried out to fermented pharmaceutical waste water and measures regulation；
2) coagulating sedimentation：Waste water i.e. after homogeneous measures regulation enters in coagulative precipitation tank, removes most of suspend
Thing and colloidal substance；
3) filter, concentrate：Waste water i.e. after coagulating sedimentation carries out membrane filtration, remove the suspension that is remained in waste water with
And turbidity, and film concentration is carried out to the water after membrane filtration, export concentrated water；
4) supercritical water oxidation：The concentrated water is inputted into overcritical water oxidization reactor, while oxygen supply system is exported
Oxygen, the fuel of starting fluid equipment output respectively enter overcritical water oxidization reactor and carry out oxidation reaction, remove described
Organic matter in concentrated water, generation supercritical fluid and inorganic salts；
5) gas solid separation：Pass through rotation in the reacted supercritical fluid of overcritical water oxidization reactor internal oxidition and inorganic salts
Wind separator carries out desalination；
6) gas-liquid separation：Gas phase and liquid phase separation are carried out, gas part is carbon dioxide and unnecessary oxygen, and liquid portion is
Water.
The step 3) in concentration process include：By the water after membrane filtration successively through the first filter and the second mistake
The concentration twice of filter, supercritical water oxidation is carried out by the concentrated water finally produced, and the production water of the second filter returns to intermediate pool；
The production water of first filter is concentrated again in the 3rd filter, production water returns to intermediate pool；3rd filter
The clear water of generation is reclaimed.
The step 6) enter before Separate System of Water-jet, need excess pressure energy recovery system to be depressured, the gas that gas is produced
Into oxygen-enriched reclaiming system, by dehydration, heat exchange cooling, rectifying, liquid CO is obtained2And oxygen rich gas, the oxygen rich gas is defeated
Enter the oxygen supply system.
The advantages of the present invention are：
The present invention for fermented pharmaceutical waste water COD excursions than larger situation, by film be enriched with (MET) with it is overcritical
The R. concomitans of water oxygen (SCWO), in the front end addition film enrichment (MET of supercritical water oxidation technique：Membrane Enrich
Treatment) technique is concentrated to waste water, can enable wider COD value fermented pharmaceutical waste water carry out it is overcritical
Water oxidation processes, realize minimizing, recycling, innoxious, and organic removal rate is up to more than 99 percent, effluent color dilution
It is up to standard；The resource that is produced in fermented pharmaceutical waste water processing procedure, the energy are directly utilized or reclaimed, processing cost, warp is reduced
Benefit of helping is more preferable.
Brief description of the drawings
Fig. 1 is the structural representation of fermented pharmaceutical waste water total system of the present invention；
Fig. 2 for the present invention in dish tubular type membrane separation device structural representation；
Fig. 3 for the present invention in dish tubular type membrane separation device in battery lead plate structural representation；
Fig. 4 for the present invention in overcritical water oxidization reactor structural representation.
Description of reference numerals
1- regulating reservoirs, 2- coagulative precipitation tanks, 3- medicine systems, 4- membrane filtrations pond, 5- intermediate pools, 6- the first dish tubular membranes
Separator (DTNF1), 7- the second dish tubular type membrane separation devices (DTNF2), the dish tubular type membrane separation devices (DTNF3) of 8- the 3rd,
9- clear water reserviors, 10- starting fluids system, 11- supercritical water oxidations (SCWO) reactor, 12- oxygen supplies system, 13- gas-solids
Piece-rate system, 14- solid salts collecting device, 15- heat-exchange systems, 16- pressure energies recovery system, 17- Separate System of Water-jet,
The oxygen-enriched reclaiming systems of 18-, 19- steam utilizations equipment, 20- center pull rods, 21- power supplys end cap, 22- pressure casings, 23- concentrated waters go out
Mouth, 24- productions water out, 25- intake end covers, 26- original water inlets, 27- raw waters passage, 28- flow guiding discs, 29- disc-types film bag,
30- battery lead plates, 31- filtration channels, 32- notches, 33- productions aquaporin, 34- binding posts avoid hole, 35- binding posts mounting hole, 36-
Cylinder, 37- water inlets, 38- narrow gaps, 39- sewage inlets and oxygen intake, 40- fuel inlets and oxygen intake, 41- burners,
42- evaporation walls, 43- liquid outlets.
Embodiment
Below by specific embodiment, the invention will be further described, and following examples are descriptive, is not limit
Qualitatively, it is impossible to which protection scope of the present invention is limited with this.
A kind of fermented pharmaceutical waste water total system, by pretreatment unit, sewage enrichment unit, supercritical water oxidation
Unit and energy resources range site are constituted.Pretreatment unit, sewage enrichment unit, supercritical water oxidation unit, energy resources
Range site is sequentially communicated.
Pretreatment unit includes regulating reservoir 1, medicine system 3, coagulative precipitation tank 2, membrane filtration pond 4, intermediate pool 5, regulation
Pond, coagulative precipitation tank, membrane filtration pond, intermediate pool are sequentially communicated, and medicine system is connected with coagulative precipitation tank.The water inlet of waste water according to
It is secondary that intermediate pool is entered by regulating reservoir, coagulative precipitation tank, membrane filtration pond.
Sewage enrichment unit includes first dish tubular type membrane separation device (DTNF1) the 6, second dish tubular type membrane separation device
(DTNF2) the 7, the 3rd dish tubular type membrane separation device (DTNF3) 8, clear water reserviors 9, the first dish tubular type membrane separation device (DTNF1),
Three dish tubular type membrane separation devices (DTNF3), clear water reserviors are sequentially communicated, the first dish tubular type membrane separation device (DTNF1), the second dish pipe
Formula membrane separation device (DTNF2), overcritical water oxidization reactor are sequentially communicated, the second dish tubular type membrane separation device (DTNF1),
Three dish tubular type membrane separation devices (DTNF3) with intermediate pool while connect；The delivery port of intermediate pool and in pretreatment unit
The water inlet of a dishful of tubular type membrane separation device (DTNF1) is connected, the concentrated water outlet of the first dish tubular type membrane separation device (DTNF1)
It is connected with the water inlet of the second dish tubular type membrane separation device (DTNF2), the concentrated water of the second dish tubular type membrane separation device (DTNF1)
Outlet is connected with overcritical water oxidization reactor；The production mouth of a river of first dish tubular type membrane separation device (DTNF1) and the 3rd dish pipe
The water inlet of formula membrane separation device (DTNF3) is connected, the production water and clear water reserviors phase of the 3rd dish tubular type membrane separation device (DTNF3)
Connection, the concentrated water outlet of the 3rd dish tubular type membrane separation device (DTNF1) and the production water of the second dish tubular type membrane separation device (DTNF2)
Mouth is connected with intermediate pool.
As shown in Fig. 2 above-mentioned dish tubular type membrane separation device is by pressure casing 22, power supply end cap 21, intake end cover 25, water conservancy diversion
Disk 28, disc-type film bag 29, battery lead plate 30 and center pull rod 20 are constituted, and power supply end cap, multiple flow guiding discs and intake end cover are successively
Stack, and fixation is installed using center pull rod in the middle.Pressure casing sealing is installed in outside power supply end cap and intake end cover, is led
Formed between flow table periphery and pressure casing in the middle part of raw water passage 27, flow guiding disc and be formed with notch 32, to form filtration channel 31, led
Production aquaporin 33 is formed between flow table Center-to-Center pull bar, closed assembly disc-type film bag, disc-type between adjacent two flow guiding disc
Film bag forms filtration channel with not contacted between flow guiding disc up and down.Battery lead plate is installed inside stacked film bag.
As shown in figure 3, battery lead plate is formed with binding post mounting hole 35, being formed with binding post with binding post mounting hole opposite side keeps away
Allow hole 34, it is symmetrically placed, two adjacent electrode plates formation interdigital electrode to form two battery lead plates of interdigital electrode.Intake end cover is formed with
The original water inlet 26 connected with raw water passage, intake end cover is also formed with the concentrated water outlet 23 connected with filtration channel, and with producing water
The production water out 24 of passage connection.Production water out is formed on lower jacket side wall.
Supercritical water oxidation unit, includes oxygen supply system 12, starting fluid system 10, supercritical water oxidation (SCWO)
Reactor 11, gas solid separation system 13, heat-exchange system 15, pressure energy recovery system 16, Separate System of Water-jet 17, oxygen-enriched reuse
System 18；The oxygen intake connection of oxygen supply system and overcritical water oxidization reactor, starting fluid system and supercritical water
Aoxidize the fuel inlet connection of (SCWO) reactor, supercritical water oxidation (SCWO) reactor, gas solid separation system, heat exchange series
System, pressure energy recovery system, Separate System of Water-jet, oxygen-enriched reclaiming system are sequentially communicated, the steam (vapor) outlet connection of heat-exchange system
Steam utilization equipment 19, the solid outlet of gas solid separation system is connected to solid salt collecting device 14.Separate System of Water-jet is same
When connected with clear water reserviors.
As shown in figure 4, supercritical water oxidation (SCWO) reactor, it includes cylinder 36, burner 41, evaporation wall 42；Institute
State inner barrel and be arranged concentrically evaporation wall, the envelope for the multistage annular being axially distributed along cylinder is formed between the evaporation wall and cylinder
The narrow gap 38 closed, each narrow gap is provided with water inlet 37 on cylinder, and the liquid being passed through via water inlet can be by described
Evaporation wall is penetrated into, in evaporation wall inner surface formation moisture film；Burner is stretched into from the top of cylinder, and the burner of the burner is located at
In cylinder, evaporation wall is made of porous materials, and the liquid is subcritical water, and cylinder top is formed with sewage inlet and oxygen intake
39, burner is formed with fuel inlet and oxygen intake 40, and cylinder body bottom is formed with liquid outlet 43.
A kind of fermented pharmaceutical waste water integrated conduct method, comprises the following steps：
In the present embodiment, design influent COD is 14400mg/L, and PH is 6.3；
(1) homogeneous：Fermented pharmaceutical waste water enters regulating reservoir, carries out homogeneous and measures regulation.
(2) coagulating sedimentation：Waste water after homogeneous is adjusted is entered in coagulative precipitation tank by regulating reservoir, medicine system to this
PAC medicaments are added in pond, most suspended substances and colloidal substance is removed.
(3) membrane filtration：Waste water after coagulating sedimentation enters membrane filtration pond by coagulative precipitation tank, removes in waste water and remains
Suspension and turbidity, the water after membrane filtration is stored in intermediate pool.
(4) film is concentrated：Water outlet in intermediate pool enters the first dish tubular type membrane separation device (DTNF1) and carries out filtering dense
Contracting, its concentrated water enters the second dish tubular type membrane separation device (DTNF2) and carries out secondary filter concentration, after secondary filter is concentrated
Concentrated water enters supercritical water oxidation (SCWO) reactor；The water that the mouth of a river comes out is produced from the first dish tubular type membrane separation device (DTNF1)
Filtering and concentrating again is carried out into the 3rd dish tubular type membrane separation device (DTNF3), the 3rd dish tubular type membrane separation device (DTNF3)
Produce water and enter clear water reserviors reuse；Concentrated water and process the second dish tubular membrane point by the 3rd dish tubular type membrane separation device (DTNF3)
Production water circulation from device (DTNF2) returns to intermediate pool.
(5) supercritical water oxidation (SCWO)：Concentrated water, the oxygen of oxygen preparation system preparation after film is concentrated, startup
The fuel of fuel system respectively enters overcritical water oxidization reactor and carries out oxidation reaction, and operating pressure is in 25-28MPa, work
Temperature is at 400-500 DEG C, by supercritical water oxidation, generation supercritical fluid and inorganic salts.
(6) gas solid separation：Pass through in the reacted supercritical fluid of overcritical water oxidization reactor internal oxidition and inorganic salts
Gas solid separation system is separated, and inorganic salts are removed in solid form to be collected by solid salt collecting device.
(7) gas-liquid separation：Supercritical fluid after desalination enters heat-exchange system multi-stage heat exchanger, and heat energy is converted to steam and entered
Enter steam utilization equipment to be generated electricity or heated；After supercritical fluid exchanges heat through multipole, its temperature is in 100~200 DEG C, pressure
In 22~35MPa, enter Separate System of Water-jet after entering pressure energy recovery system, release pressure and output kinetic energy；Gas-liquid point
From system by counterbalance valve control pressure to 5~10MPa, gas phase and liquid phase separation are carried out, gas part is carbon dioxide and many
Remaining oxygen, liquid portion is water, and the clear water that gas-liquid separation is obtained is directly entered clear water reserviors and utilized, and gas part enters oxygen-enriched
Reclaiming system.
(8) oxygen-enriched reuse：The gas of carbonated, unnecessary oxygen after gas-liquid separation is in oxygen-enriched reclaiming system by de-
Water, heat exchange cooling, rectifying, obtain liquid CO2And oxygen rich gas, liquid CO2There is collecting device collection, it is rich
Carrier of oxygen is collected in gas reservoir, and the oxygen preparation system that can be directly entered the system is utilized.
Claims (8)
1. a kind of fermented pharmaceutical waste water total system, it is characterised in that：It includes pretreatment unit, sewage enrichment unit
With supercritical water oxidation unit；Wherein, the entrance of the sewage enrichment unit connects the pretreatment unit, and sewage is in the dirt
Membrane filtration and film concentration are carried out in water enrichment unit, the clear water output of sewage enrichment unit connects a clear water reserviors；It is described overcritical
Water oxidation unit includes oxygen supply system, starting fluid system, overcritical water oxidization reactor, gas solid separation system, gas-liquid
Piece-rate system, wherein, starting fluid system, overcritical water oxidization reactor, gas solid separation system, Separate System of Water-jet connect successively
Connect, the sewage inlet of the overcritical water oxidization reactor connects the concentrated water outlet of the sewage enrichment unit, overcritical water oxygen
The oxygen intake for changing reactor connects the oxygen supply system, and the outlet of the Separate System of Water-jet connects the clear water reserviors；
Described overcritical water oxidization reactor includes cylinder, burner, evaporation wall；The inner barrel is arranged concentrically evaporation
Wall, forms the narrow gap of the closing for the multistage annular being axially distributed along cylinder, each narrow gap between the evaporation wall and cylinder
Water inlet is provided with cylinder, the liquid being passed through via water inlet can be penetrated into by the evaporation wall, in evaporation wall inner surface
Form moisture film；Burner is stretched into from the top of cylinder, and the burner of the burner is located in cylinder, and evaporation wall is by porous material system
Into the liquid is subcritical water, and cylinder top is formed with sewage inlet and oxygen intake, and burner is formed with fuel inlet and oxygen
Entrance, cylinder body bottom is formed with liquid outlet.
2. a kind of fermented pharmaceutical waste water total system as claimed in claim 1, it is characterised in that：The sewage enrichment
Unit includes intermediate pool, the first filter, the second filter, the 3rd filter；The entrance connection of the intermediate pool is described
Pretreatment unit, the concentrated water outlet of the production water out, the 3rd filter of second filter is connected with intermediate pool, institute
The entrance of outlet connection first filter of intermediate pool is stated to carry out membrane filtration；The concentrated water of first filter goes out
The entrance of mouth connection second filter, the production water out of first filter connects the entrance of the 3rd filter,
The clear water output of 3rd filter connects the clear water reserviors, and the concentrated water outlet connection of second filter is described overcritical
The material inlet of water oxidation reactor, realizes that film is concentrated.
3. a kind of fermented pharmaceutical waste water total system as claimed in claim 2, it is characterised in that：First filtering
Device, the second filter and the 3rd filter are dish tubular type membrane separation device, and dish tubular type membrane separation device is by pressure casing, power supply
End cap, intake end cover, flow guiding disc, disc-type film bag, battery lead plate and center pull rod are constituted, and power supply end cap, multiple flow guiding discs and are entered
Water end (W.E.) lid is stacked successively, and installs fixation using center pull rod in the middle；Pressure casing sealing is installed in power supply end cap and entered
Outside water end (W.E.) lid, raw water passage is formed between the flow guiding disc periphery and pressure casing；Notch is formed with the middle part of flow guiding disc, to be formed
Filter passage；Production aquaporin is formed between flow guiding disc Center-to-Center pull bar, the closed assembly disc-type film bag between adjacent two flow guiding disc,
Disc-type film bag forms filtration channel with not contacted between flow guiding disc up and down；Battery lead plate is installed inside stacked film bag.
4. a kind of fermented pharmaceutical waste water total system as claimed in claim 1, it is characterised in that：The pretreatment is single
Member includes the regulating reservoir, coagulative precipitation tank, membrane filtration pond being sequentially communicated.
5. a kind of fermented pharmaceutical waste water total system according to one of claim 1-4, it is characterised in that：It is described
Heat-exchange system, the steam (vapor) outlet connection steam utilization equipment of the heat-exchange system are set after gas solid separation system.
6. a kind of fermented pharmaceutical waste water total system according to claim 5, it is characterised in that：Described heat friendship
Setting pressure energy recovery system after system is changed, Separate System of Water-jet is connected after decompression.
7. a kind of fermented pharmaceutical waste water integrated conduct method, step includes：
1) homogeneous：Homogeneous is carried out to fermented pharmaceutical waste water and measures regulation；
2) coagulating sedimentation：I.e. by homogeneous measure regulation after waste water enter coagulative precipitation tank in, remove most suspended substances and
Colloidal substance；
3) filter, concentrate：Waste water i.e. after coagulating sedimentation carries out the suspension remained in membrane filtration, removal waste water and turbid
Degree, and film concentration is carried out to the water after membrane filtration, export concentrated water；
4) supercritical water oxidation：The concentrated water is inputted into overcritical water oxidization reactor, while the oxygen of oxygen supply system output
Gas, the fuel of starting fluid equipment output respectively enter overcritical water oxidization reactor and carry out oxidation reaction, remove the concentrated water
In organic matter, generation supercritical fluid and inorganic salts；
5) gas solid separation：Pass through whirlwind point in the reacted supercritical fluid of overcritical water oxidization reactor internal oxidition and inorganic salts
Desalination is carried out from device；
6) gas-liquid separation：Gas phase and liquid phase separation are carried out, gas part is carbon dioxide and unnecessary oxygen, and liquid portion is water；
The step 3) in concentration process include：By the water after membrane filtration successively through the first filter and the second filter
Concentration twice, the concentrated water finally produced is subjected to supercritical water oxidation, the production water of the second filter returns to intermediate pool；By institute
The production water for stating the first filter is concentrated again in the 3rd filter, and production water returns to intermediate pool；3rd filter is produced
Clear water reclaim.
8. a kind of fermented pharmaceutical waste water integrated conduct method as claimed in claim 7, it is characterised in that：The step 6) enter
Enter before Separate System of Water-jet, need excess pressure energy recovery system to be depressured, carbon dioxide and oxygen is obtained after gas-liquid separation and enters rich
Oxygen reclaiming system, by dehydration, heat exchange cooling, rectifying, obtains liquid CO2And oxygen rich gas, the oxygen rich gas inputs described
Oxygen supply system.
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| CN201510126594.5A CN104692580B (en) | 2015-03-23 | 2015-03-23 | A kind of fermented pharmaceutical waste water total system and method |
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| CN201510126594.5A CN104692580B (en) | 2015-03-23 | 2015-03-23 | A kind of fermented pharmaceutical waste water total system and method |
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| CN108562634B (en) * | 2018-06-11 | 2023-07-07 | 遵义师范学院 | Novel COD (chemical oxygen demand) measuring device and measuring method thereof |
| CN109574194B (en) * | 2019-01-23 | 2024-06-07 | 南京新奥环保技术有限公司 | Supercritical water oxidation treatment system |
| CN115093073B (en) * | 2022-06-13 | 2024-08-02 | 逸辰环保科技(厦门)有限公司 | Biogas slurry concentration system and method |
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| JP2004033910A (en) * | 2002-07-03 | 2004-02-05 | General Atomics Inc | Treatment method for organic acid washing waste liquid and apparatus therefor |
| CN204058560U (en) * | 2014-09-03 | 2014-12-31 | 彭英利 | The supercritical water treatment device of discarded circuit board |
| CN104402077B (en) * | 2014-12-05 | 2017-01-11 | 王冰 | Novel transpiring wall reactor for supercritical sewage treatment |
| CN204490673U (en) * | 2015-03-23 | 2015-07-22 | 王冰 | A kind of novel fermentation class pharmacy waste water total system |
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