CN104692580A - Novel fermentation-type pharmaceutical wastewater overall treatment system and method - Google Patents
Novel fermentation-type pharmaceutical wastewater overall treatment system and method Download PDFInfo
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- 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
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- Environmental & Geological Engineering (AREA)
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Abstract
The invention relates to a novel fermentation-type pharmaceutical wastewater overall treatment system. The novel fermentation-type pharmaceutical wastewater overall treatment system comprises a pretreatment unit, a sewage gathering unit and a supercritical water oxidation unit, wherein an inlet of the sewage gathering unit is connected with the pretreatment unit; sewage is subjected to membrane filtration and membrane concentration in the sewage gathering unit; a clean water outlet of the sewage gathering unit is connected with a clean water reservoir; a staring fuel system, a supercritical water oxidation reactor, a gas-solid separation system and a gas-liquid separation system of the supercritical water oxidation unit are sequentially connected; a sewage inlet of the supercritical water oxidation reactor is connected with a concentrated water outlet of the sewage gathering unit; an oxygen inlet of the supercritical water oxidation reactor is connected with an oxygen supply system; an outlet of the gas-liquid separation system is connected with the clean water reservoir. Membrane enrichment and supercritical water oxidation are combined for application, so that fermentation-type pharmaceutical wastewater of the COD value within a large range can be subjected to supercritical water oxidation processing, the removal rate of organics is more than 99%, treatment is thorough, and the cost is low.
Description
Technical field
The invention belongs to sewage disposal and energy resource circulation and stress technical field, relate to a kind of novel fermentation class pharmacy waste water total system and method.
Background technology
Fermented pharmaceutical waste water derives from fermentation, filtration, extractive crystallization, refinement, the process such as refining.Principal pollutant index is PH, colourity, BOD
5, COD, SS, vegetable and animals oils, ammonia nitrogen and TOC content, acute toxicity, total Zn content and total cyanide content etc.Complicated component, carbon-nitrogen ratio is lacked of proper care, and biodegradability is poor, and containing a large amount of vitriol, the biochemical inhibitor such as drug titers and degradation product thereof.At present, domestic and international application is few and not mature enough in the fermented pharmaceutical waste water treatment technology of engineering practice.The complicated component had for fermented pharmaceutical waste water, the feature such as Pollutant levels are high, biodegradability is poor, what mainly adopt the process of such waste water at present is the combination process of physico-chemical process (comprising entrapping method, coagulant sedimentation, photodegradation method, reverse osmosis and membrane separation technique, absorption method and electrolytic process), biochemical process and multiple method.Though current technique can remove the most of pollutent in waste water, but it is not good to the removal effect of organic pollutant, often there is the phenomenon that exceeds standard in effluent color dilution, can not meet " fermentation class pharmaceutical industry pollution discharge standard " requirement, also need to carry out successive depths process; Particularly in wastewater treatment process, resource utilization is also desirable not to the utmost.Therefore, need to seek a kind of fermented pharmaceutical waste water total system of being more suitable for and method.
Summary of the invention
The object of the invention is to overcome prior art Problems existing and deficiency, provide that a kind of processing efficiency is high, no pollution discharge, simple to operate, the novel fermentation class pharmacy waste water total system that simultaneously can realize the energy and resource reclaim and method.
The present invention solves its technical problem and is achieved through the following technical solutions:
A kind of novel fermentation class pharmacy waste water total system, is characterized in that: it comprises pretreatment unit, sewage enrichment unit and supercritical water oxidation unit; Wherein, the entrance of described sewage enrichment unit connects described pretreatment unit, and sewage carries out membrane filtration and membrane concentration in described sewage enrichment unit, and the clear water output of sewage enrichment unit connects clean water basin; Described supercritical water oxidation unit comprises oxygen supply system, starting fluid system, overcritical water oxidization reactor, gas solid separation system, Separate System of Water-jet, wherein, starting fluid system, overcritical water oxidization reactor, gas solid separation system, Separate System of Water-jet connect successively, the sewage inlet of described overcritical water oxidization reactor connects the dense water out of described sewage enrichment unit, the oxygen intake of overcritical water oxidization reactor connects described oxygen supply system, and the outlet of described Separate System of Water-jet connects described clean water basin.
Described sewage enrichment unit comprises intermediate pool, the first strainer, the second strainer, the 3rd strainer; The entrance of described intermediate pool connects described pretreatment unit, the product water out of described second strainer, the dense water out of described 3rd strainer are connected with intermediate pool, and the outlet of described intermediate pool connects the entrance of described first strainer in order to carry out membrane filtration; The dense water out of described first strainer connects the entrance of described second strainer, the product water out of described first strainer connects the entrance of described 3rd strainer, the clear water output of described 3rd strainer connects described clean water basin, the dense water out of described second strainer connects the material inlet of described overcritical water oxidization reactor, realizes membrane concentration.
Described first strainer, the second strainer and the 3rd strainer are dish tubular membrane tripping device, dish tubular membrane tripping 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 formed, power supply end cap, multiple flow guiding disc and intake end cover stack successively, and adopt center pull rod to install fixing in the middle; Pressure casing sealing is installed in outside power supply end cap and intake end cover, forms former aquaporin between described flow guiding disc periphery and pressure casing; Notch is shaped with, to form filtration channel in the middle part of flow guiding disc; Formed between flow guiding disc Center-to-Center pull bar and produce aquaporin, between adjacent two flow guiding discs, closed assembly disc-type film bag, does not contact between disc-type film bag and upper and lower flow guiding disc, forms filtration channel; At the inner installing electrodes plate of stacked film bag.
Described pretreatment unit comprise be communicated with successively equalizing tank, coagulative precipitation tank, membrane filtration pond.
Described overcritical water oxidization reactor comprises cylindrical shell, burner, evaporation wall; Described inner barrel arranges evaporation wall with one heart, the narrow gap closed of the multistage annular along cylindrical shell axial distribution is formed between described evaporation wall and cylindrical shell, each described narrow gap has water inlet on cylindrical shell, the liquid passed into via water inlet can be infiltrated by described evaporation wall, forms moisture film at evaporation wall internal surface; Burner stretches into from cylindrical shell top, and the burner of described burner is positioned at cylindrical shell, and evaporation wall is made of porous materials, described liquid is subcritical water, cylindrical shell top is shaped with sewage inlet and oxygen intake, and burner is shaped with fuel inlet and oxygen intake, and cylinder body bottom is shaped with liquid outlet.
Arrange heat exchange system after described gas solid separation system, the vapour outlet of described heat exchange system connects steam utilization equipment.
Pressure energy recovery system is set after it is characterized in that described heat exchange system, after step-down, connects Separate System of Water-jet.
A kind of novel fermentation class pharmacy waste water integrated conduct method, step comprises:
1) homogeneous: homogeneous is carried out to fermented pharmaceutical waste water and all measures adjustment;
2) coagulating sedimentation: namely enter in coagulative precipitation tank through the homogeneous waste water all measured after adjustment, removes most suspended substances and colloidalmaterial;
3) filter, concentrate: the waste water namely after coagulating sedimentation carries out membrane filtration, remove suspended substance residual in waste water and turbidity, and membrane concentration is carried out to the water after membrane filtration, export dense water;
4) supercritical water oxidation: by described dense water input overcritical water oxidization reactor, the fuel that the oxygen of oxygen supply system output simultaneously, starting fluid equipment export enters overcritical water oxidization reactor respectively and carries out oxidizing reaction, remove the organism in described dense water, generate supercutical fluid and inorganic salt;
5) gas solid separation: carry out desalination by cyclonic separator at the reacted supercutical fluid of overcritical water oxidization reactor internal oxidition and inorganic salt;
6) gas-liquid separation: carry out gas phase and liquid phase separation, gas fraction is carbonic acid gas and unnecessary oxygen, and liquid portion is water.
Described step 3) in concentration process comprise: by the concentrating for twice successively through the first strainer and the second strainer of the water after membrane filtration, the dense water finally produced is carried out supercritical water oxidation, and the product water of the second strainer returns intermediate pool; The product water of described first strainer is again concentrated in the 3rd strainer, produces water and return intermediate pool; The clear water that described 3rd strainer produces reclaims.
Described step 6) enter Separate System of Water-jet before, need the step-down of excess pressure energy recovery system, gas produce gas enter oxygen enrichment reclaiming system, through dehydration, heat exchange cooling, rectifying, obtain liquid CO
2and oxygen rich gas, described oxygen rich gas inputs described oxygen supply system.
Advantage of the present invention and beneficial effect are:
The present invention is directed to the situation that fermented pharmaceutical waste water COD variation range is larger, by the R. concomitans of film enrichment (MET) with supercritical water oxidation (SCWO), add film enrichment (MET:Membrane Enrich Treatment) technique to concentrate waste water in the front end of supercritical water oxidation technique, the fermented pharmaceutical waste water of wider COD value can be enable to carry out supercritical water oxidation process, realize minimizing, resource utilization, innoxious, organic removal rate can reach more than 99 percent, and effluent color dilution is up to standard; Directly utilize the resource produced in fermented pharmaceutical waste water treating processes, the energy or reclaim, reduce processing cost, economic benefit is better.
Accompanying drawing explanation
Fig. 1 is the structural representation of novel fermentation class pharmacy waste water total system of the present invention;
Fig. 2 is the structural representation of the dish tubular membrane tripping device in the present invention;
Fig. 3 is the structural representation of the battery lead plate in the dish tubular membrane tripping device in the present invention;
Fig. 4 is the structural representation of the overcritical water oxidization reactor in the present invention.
Description of reference numerals
1-equalizing tank, 2-coagulative precipitation tank, 3-medicine system, 4-membrane filtration pond, 5-intermediate pool, 6-first dish tubular membrane tripping device (DTNF1), 7-second dish tubular membrane tripping device (DTNF2), 8-the 3rd dish tubular membrane tripping device (DTNF3), 9-clean water basin, 10-starting fluid system, 11-supercritical water oxidation (SCWO) reactor, 12-oxygen supply system, 13-gas solid separation system, 14-solid salt collecting device, 15-heat exchange system, 16-pressure energy recovery system, 17-Separate System of Water-jet, 18-oxygen enrichment reclaiming system, 19-steam utilization equipment, 20-center pull rod, 21-power supply end cap, 22-pressure casing, the dense water out of 23-, 24-produces water out, 25-intake end cover, 26-original water inlet, the former aquaporin of 27-, 28-flow guiding disc, 29-disc-type film bag, 30-battery lead plate, 31-filtration channel, 32-notch, 33-produces aquaporin, 34-terminal stud dodges hole, 35-terminal stud open holes, 36-cylindrical shell, 37-water inlet, the narrow gap of 38-, 39-sewage inlet and oxygen intake, 40-fuel inlet and oxygen intake, 41-burner, 42-evaporation wall, 43-liquid outlet.
Embodiment
Below by specific embodiment, the invention will be further described, and following examples are descriptive, is not determinate, can not limit protection scope of the present invention with this.
A kind of novel fermentation class pharmacy waste water total system, is made up of pretreatment unit, sewage enrichment unit, supercritical water oxidation unit and Energy resources range site.Pretreatment unit, sewage enrichment unit, supercritical water oxidation unit, Energy resources range site are communicated with successively.
Pretreatment unit comprises equalizing tank 1, medicine system 3, coagulative precipitation tank 2, membrane filtration pond 4, intermediate pool 5, and equalizing tank, coagulative precipitation tank, membrane filtration pond, intermediate pool are communicated with successively, and medicine system is communicated with coagulative precipitation tank.The water inlet of waste water enters intermediate pool by equalizing tank, coagulative precipitation tank, membrane filtration pond successively.
Sewage enrichment unit comprises the first dish tubular membrane tripping device (DTNF1) 6, second dish tubular membrane tripping device (DTNF2) 7, 3rd dish tubular membrane tripping device (DTNF3) 8, clean water basin 9, first dish tubular membrane tripping device (DTNF1), 3rd dish tubular membrane tripping device (DTNF3), clean water basin are communicated with successively, first dish tubular membrane tripping device (DTNF1), second dish tubular membrane tripping device (DTNF2), overcritical water oxidization reactor is communicated with successively, second dish tubular membrane tripping device (DTNF1), 3rd dish tubular membrane tripping device (DTNF3) is communicated with intermediate pool simultaneously, in pretreatment unit, the water outlet of intermediate pool is connected with the water-in of the first dish tubular membrane tripping device (DTNF1), the dense water out of the first dish tubular membrane tripping device (DTNF1) is connected with the water-in of the second dish tubular membrane tripping device (DTNF2), and the dense water out of the second dish tubular membrane tripping device (DTNF1) is connected with overcritical water oxidization reactor, the product mouth of a river of the first dish tubular membrane tripping device (DTNF1) is connected with the water-in of the 3rd dish tubular membrane tripping device (DTNF3), the product water of the 3rd dish tubular membrane tripping device (DTNF3) is connected with clean water basin, and the dense water out of the 3rd dish tubular membrane tripping device (DTNF1) is all connected with intermediate pool with the product mouth of a river of the second dish tubular membrane tripping device (DTNF2).
As shown in Figure 2, above-mentioned dish tubular membrane tripping device is by pressure casing 22, power supply end cap 21, intake end cover 25, flow guiding disc 28, disc-type film bag 29, battery lead plate 30 and center pull rod 20 are formed, power supply end cap, multiple flow guiding disc and intake end cover stack successively, and adopt center pull rod to install fixing in the middle.Pressure casing sealing is installed in outside power supply end cap and intake end cover, former aquaporin 27 is formed between flow guiding disc periphery and pressure casing, notch 32 is shaped with in the middle part of flow guiding disc, to form filtration channel 31, formed between flow guiding disc Center-to-Center pull bar and produce aquaporin 33, between adjacent two flow guiding discs, closed assembly disc-type film bag, does not contact between disc-type film bag and upper and lower flow guiding disc, forms filtration channel.At the inner installing electrodes plate of stacked film bag.
As shown in Figure 3, battery lead plate is shaped with terminal stud open holes 35, and side relative to terminal stud open holes is shaped with terminal stud and dodges hole 34, and two battery lead plates forming interdigital electrode are symmetrical placement, and two adjacent electrode plates form interdigital electrode.Intake end cover is shaped with the original water inlet 26 be communicated with former aquaporin, and intake end cover is also shaped with the dense water out 23 be communicated with filtration channel, and the product water out 24 be communicated with product aquaporin.Produce water out and be formed on lower jacket sidewall.
Supercritical water oxidation unit, comprises 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 enrichment reclaiming system 18; Oxygen supply system is connected with the oxygen intake of overcritical water oxidization reactor, starting fluid system is communicated with the fuel inlet of supercritical water oxidation (SCWO) reactor, supercritical water oxidation (SCWO) reactor, gas solid separation system, heat exchange system, pressure energy recovery system, Separate System of Water-jet, oxygen enrichment reclaiming system are communicated with successively, the vapour outlet of heat exchange system connects steam utilization equipment 19, and the solid outlet of gas solid separation system is connected to solid salt collecting device 14.Separate System of Water-jet is communicated with clean water basin simultaneously.
As shown in Figure 4, supercritical water oxidation (SCWO) reactor, it comprises cylindrical shell 36, burner 41, evaporation wall 42; Described inner barrel arranges evaporation wall with one heart, the narrow gap 38 closed of the multistage annular along cylindrical shell axial distribution is formed between described evaporation wall and cylindrical shell, each described narrow gap has water inlet 37 on cylindrical shell, the liquid passed into via water inlet can be infiltrated by described evaporation wall, forms moisture film at evaporation wall internal surface; Burner stretches into from cylindrical shell top, the burner of described burner is positioned at cylindrical shell, evaporation wall is made of porous materials, described liquid is subcritical water, cylindrical shell top is shaped with sewage inlet and oxygen intake 39, burner is shaped with fuel inlet and oxygen intake 40, and cylinder body bottom is shaped with liquid outlet 43.
A kind of novel fermentation class pharmacy waste water integrated conduct method, comprises the steps:
In the present embodiment, design influent COD is 14400mg/L, PH is 6.3;
(1) homogeneous: fermented pharmaceutical waste water enters equalizing tank, carries out homogeneous and all measures adjustment.
(2) coagulating sedimentation: the waste water after equal quality regulate enters in coagulative precipitation tank by equalizing tank, medicine system adds PAC medicament in this pond, removes most suspended substances and colloidalmaterial.
(3) membrane filtration: the waste water after coagulating sedimentation enters membrane filtration pond by coagulative precipitation tank, remove suspended substance residual in waste water and turbidity, the water after membrane filtration is stored in intermediate pool.
(4) membrane concentration: the water outlet in intermediate pool enters the first dish tubular membrane tripping device (DTNF1) and carries out filtering and concentrating, its dense water enters the second dish tubular membrane tripping device (DTNF2) to carry out secondary filtration and concentrates, and the dense water after secondary filtration concentrates enters supercritical water oxidation (SCWO) reactor; Produce mouth of a river water out from the first dish tubular membrane tripping device (DTNF1) to enter the 3rd dish tubular membrane tripping device (DTNF3) and carry out filtering and concentrating again, the product water of the 3rd dish tubular membrane tripping device (DTNF3) enters clean water basin reuse; Through the dense water of the 3rd dish tubular membrane tripping device (DTNF3) with get back to intermediate pool through the product water cycle of the second dish tubular membrane tripping device (DTNF2).
(5) supercritical water oxidation (SCWO): oxygen prepared by the dense water after membrane concentration, oxygen preparation system, the fuel of starting fluid system enter overcritical water oxidization reactor respectively and carries out oxidizing reaction, operating pressure is at 25-28MPa, working temperature is at 400-500 DEG C, by supercritical water oxidation, generate supercutical fluid and inorganic salt.
(6) gas solid separation: be separated by gas solid separation system with inorganic salt at the reacted supercutical fluid of overcritical water oxidization reactor internal oxidition, inorganic salt remove in solid form to be collected by solid salt collecting device.
(7) gas-liquid separation: the supercutical fluid after desalination enters heat exchange system multi-stage heat exchanger, thermal power transfer is that steam enters steam utilization equipment and carries out generating electricity or heating etc.; Supercutical fluid after multipole heat exchange, its temperature 100 ~ 200 DEG C, pressure at 22 ~ 35MPa, enter into pressure energy recovery system, relief pressure also enters Separate System of Water-jet after output kinetic energy; Separate System of Water-jet passes through back pressure valve control pressure to 5 ~ 10MPa, carry out gas phase and liquid phase separation, gas fraction is carbonic acid gas and unnecessary oxygen, and liquid portion is water, the clear water that gas-liquid separation obtains directly enters clean water basin and is utilized, and gas fraction enters oxygen enrichment reclaiming system.
(8) oxygen enrichment reuse: the gas of the carbonated after gas-liquid separation, unnecessary oxygen through dehydration, heat exchange cooling, rectifying, obtains liquid CO at oxygen enrichment reclaiming system
2and oxygen rich gas, liquid CO
2collecting device is had to collect, rich
Carrier of oxygen is collected in gas reservoir, and the oxygen preparation system that directly can enter native system is utilized.
Claims (10)
1. a novel fermentation class pharmacy waste water total system, is characterized in that: it comprises pretreatment unit, sewage enrichment unit and supercritical water oxidation unit; Wherein, the entrance of described sewage enrichment unit connects described pretreatment unit, and sewage carries out membrane filtration and membrane concentration in described sewage enrichment unit, and the clear water output of sewage enrichment unit connects clean water basin; Described supercritical water oxidation unit comprises oxygen supply system, starting fluid system, overcritical water oxidization reactor, gas solid separation system, Separate System of Water-jet, wherein, starting fluid system, overcritical water oxidization reactor, gas solid separation system, Separate System of Water-jet connect successively, the sewage inlet of described overcritical water oxidization reactor connects the dense water out of described sewage enrichment unit, the oxygen intake of overcritical water oxidization reactor connects described oxygen supply system, and the outlet of described Separate System of Water-jet connects described clean water basin.
2. a kind of novel fermentation class pharmacy waste water total system as claimed in claim 1, is characterized in that: described sewage enrichment unit comprises intermediate pool, the first strainer, the second strainer, the 3rd strainer; The entrance of described intermediate pool connects described pretreatment unit, the product water out of described second strainer, the dense water out of described 3rd strainer are connected with intermediate pool, and the outlet of described intermediate pool connects the entrance of described first strainer in order to carry out membrane filtration; The dense water out of described first strainer connects the entrance of described second strainer, the product water out of described first strainer connects the entrance of described 3rd strainer, the clear water output of described 3rd strainer connects described clean water basin, the dense water out of described second strainer connects the material inlet of described overcritical water oxidization reactor, realizes membrane concentration.
3. a kind of novel fermentation class pharmacy waste water total system as claimed in claim 2, it is characterized in that: described first strainer, the second strainer and the 3rd strainer are dish tubular membrane tripping device, dish tubular membrane tripping 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 formed, power supply end cap, multiple flow guiding disc and intake end cover stack successively, and adopt center pull rod to install fixing in the middle; Pressure casing sealing is installed in outside power supply end cap and intake end cover, forms former aquaporin between described flow guiding disc periphery and pressure casing; Notch is shaped with, to form filtration channel in the middle part of flow guiding disc; Formed between flow guiding disc Center-to-Center pull bar and produce aquaporin, between adjacent two flow guiding discs, closed assembly disc-type film bag, does not contact between disc-type film bag and upper and lower flow guiding disc, forms filtration channel; At the inner installing electrodes plate of stacked film bag.
4. a kind of novel fermentation class pharmacy waste water total system as claimed in claim 1, is characterized in that: described pretreatment unit comprise be communicated with successively equalizing tank, coagulative precipitation tank, membrane filtration pond.
5. novel fermentation class pharmacy waste water total system according to claim 1, is characterized in that: described overcritical water oxidization reactor comprises cylindrical shell, burner, evaporation wall; Described inner barrel arranges evaporation wall with one heart, the narrow gap closed of the multistage annular along cylindrical shell axial distribution is formed between described evaporation wall and cylindrical shell, each described narrow gap has water inlet on cylindrical shell, the liquid passed into via water inlet can be infiltrated by described evaporation wall, forms moisture film at evaporation wall internal surface; Burner stretches into from cylindrical shell top, and the burner of described burner is positioned at cylindrical shell, and evaporation wall is made of porous materials, described liquid is subcritical water, cylindrical shell top is shaped with sewage inlet and oxygen intake, and burner is shaped with fuel inlet and oxygen intake, and cylinder body bottom is shaped with liquid outlet.
6. according to a kind of novel fermentation class pharmacy waste water total system one of claim 1-5 Suo Shu, it is characterized in that: arrange heat exchange system after described gas solid separation system, the vapour outlet of described heat exchange system connects steam utilization equipment.
7., according to a kind of novel fermentation class pharmacy waste water total system one of claim 1-5 Suo Shu, it is characterized in that: pressure energy recovery system is set after described heat exchange system, after step-down, connects Separate System of Water-jet.
8. a novel fermentation class pharmacy waste water integrated conduct method, step comprises:
1) homogeneous: homogeneous is carried out to fermented pharmaceutical waste water and all measures adjustment;
2) coagulating sedimentation: namely enter in coagulative precipitation tank through the homogeneous waste water all measured after adjustment, removes most suspended substances and colloidalmaterial;
3) filter, concentrate: the waste water namely after coagulating sedimentation carries out membrane filtration, remove suspended substance residual in waste water and turbidity, and membrane concentration is carried out to the water after membrane filtration, export dense water;
4) supercritical water oxidation: by described dense water input overcritical water oxidization reactor, the fuel that the oxygen of oxygen supply system output simultaneously, starting fluid equipment export enters overcritical water oxidization reactor respectively and carries out oxidizing reaction, remove the organism in described dense water, generate supercutical fluid and inorganic salt;
5) gas solid separation: carry out desalination by cyclonic separator at the reacted supercutical fluid of overcritical water oxidization reactor internal oxidition and inorganic salt;
6) gas-liquid separation: carry out gas phase and liquid phase separation, gas fraction is carbonic acid gas and unnecessary oxygen, and liquid portion is water.
9. a kind of novel fermentation class pharmacy waste water integrated conduct method as claimed in claim 8, it is characterized in that: described step 3) in concentration process comprise: by the concentrating for twice successively through the first strainer and the second strainer of the water after membrane filtration, the dense water finally produced is carried out supercritical water oxidation, and the product water of the second strainer returns intermediate pool; The product water of described first strainer is again concentrated in the 3rd strainer, produces water and return intermediate pool; The clear water that described 3rd strainer produces reclaims.
10. a kind of novel fermentation class pharmacy waste water integrated conduct method as claimed in claim 8 or 9, it is characterized in that: described step 6) enter Separate System of Water-jet before, need the step-down of excess pressure energy recovery system, the gas that gas produces enters oxygen enrichment reclaiming system, through dehydration, heat exchange cooling, rectifying, obtain liquid CO
2and oxygen rich gas, described oxygen rich gas inputs described oxygen supply system.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108562634A (en) * | 2018-06-11 | 2018-09-21 | 遵义师范学院 | A kind of novel C OD measurement devices and its assay method |
| CN109574194A (en) * | 2019-01-23 | 2019-04-05 | 南京新奥环保技术有限公司 | Supercritical water oxidation treatment system |
| CN115093073A (en) * | 2022-06-13 | 2022-09-23 | 逸辰环保科技(厦门)有限公司 | Biogas slurry concentration system and method |
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| CN204058560U (en) * | 2014-09-03 | 2014-12-31 | 彭英利 | The supercritical water treatment device of discarded circuit board |
| CN104402077A (en) * | 2014-12-05 | 2015-03-11 | 内蒙古天一环境技术有限公司 | 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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| 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 |
| CN104402077A (en) * | 2014-12-05 | 2015-03-11 | 内蒙古天一环境技术有限公司 | 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 |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108562634A (en) * | 2018-06-11 | 2018-09-21 | 遵义师范学院 | A kind of novel C OD measurement devices and its assay method |
| 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 |
| CN109574194A (en) * | 2019-01-23 | 2019-04-05 | 南京新奥环保技术有限公司 | Supercritical water oxidation treatment system |
| 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 |
| CN115093073A (en) * | 2022-06-13 | 2022-09-23 | 逸辰环保科技(厦门)有限公司 | Biogas slurry concentration system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104692580B (en) | 2017-08-01 |
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