CN109455808A - A kind of technique of catalytic wet oxidation processing high concentrated organic wastewater - Google Patents
A kind of technique of catalytic wet oxidation processing high concentrated organic wastewater Download PDFInfo
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- CN109455808A CN109455808A CN201811459079.9A CN201811459079A CN109455808A CN 109455808 A CN109455808 A CN 109455808A CN 201811459079 A CN201811459079 A CN 201811459079A CN 109455808 A CN109455808 A CN 109455808A
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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
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic 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
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
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Abstract
A kind of technique of catalytic wet oxidation processing high concentrated organic wastewater be using COD concentration on-line checking and with oxygen concentration adjusting device auto-associating, by COD content be 10000-50000 mg/L, wastewater liquid air speed is 0.5-2.5 h‑1Organic wastewater mixed with oxygen rich gas, oxygen rich gas air speed is 34-39 times of wastewater liquid air speed, oxygen supply amount is theoretical oxygen demand 1.1-1.2 times, it is 25%-99% that device, which automatically adjusts oxygen volumetric concentration, the direct outlet of water or the next processing section of feeding, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour after being sent into the waste water reactor reaction treatment equipped with catalyst are directly discharged into atmosphere.The advantages of present invention tool can effectively remove acid or alkalinity organic wastewater middle and high concentration COD.
Description
Technical field
The present invention relates to a kind of techniques of catalytic wet oxidation processing high concentrated organic wastewater, relate in particular to one kind and urge
Technique of the dampness elimination formula oxidation processes containing high concentration COD, the organic wastewater of ammonia nitrogen.
Background technique
High concentrated organic wastewater is mainly derived from the production processes such as coal chemical industry, pharmacy, papermaking, printing and dyeing, outstanding feature
It is " four is high ", i.e., high COD (oils, phenols, polycyclic aromatic hydrocarbon), high ammonia nitrogen, high chroma, high inorganic pollution (sulfide, cyaniding
Object, salt) etc..High concentrated organic wastewater contains a large amount of bio-refractory substances and noxious material, can cause seriously to rush to microorganism
It hits and poisons, microorganism is caused to lose activation capacity.The high concentrated organic wastewater dealt with improperly causes surrounding enviroment and water body
Extremely serious harm has reached very urgent stage to the improvement of this kind of organic wastewater at present.
Catalytic wet oxidation technology is a kind of advanced technology for administering high-concentration organic industrial waste water, and the technology is in certain temperature
Degree and pressure under, with air, oxygen, ozone etc. for oxidant, disposably in high concentrated organic wastewater COD, TOC, ammonia,
The pollutants such as cyanogen carry out oxygenolysis, be allowed to be changed into the harmless components such as carbon dioxide, nitrogen gas and water, and be deodorized simultaneously, decolourize and
Sterilizing, to achieve the purpose that purified treatment water.Oxidant during catalytic wet oxidation is the oxygen in air, oxygen
Gas partial pressure plays a crucial role catalyst efficiency and waste water removal efficiency.Partial pressure of oxygen represents reaction system under certain condition
Amount needed for whether oxygen meets or exceeds reaction in uniting, while partial pressure of oxygen is also motive force of the oxygen to aqueous phase dissolved, oxygen
Pressure has direct influence to oxidation rate in a certain range.Catalytic wet oxidation occurs mainly in the active site of catalyst
On, therefore organic matter is limited using the rate that oxygen molecule carries out oxidation reaction by solution-air, liquid-solid mass transfer rate.By mass transfer
Known to rule, the mass transfer rate of liquid-vapor interface can be increased by improving gaseous phase partial pressure, while gas also will in the increase of liquid concentration
Promote the mass transfer rate of liquid-solid interface.During catalytic wet oxidation organic wastewater, it need to guarantee that oxygen has enough concentration,
Guarantee that oxygen supply amount is greater than theoretical oxygen demand.Meanwhile oxygen concentration increases to the contribution after certain value to wet oxidation effect
Almost without the amount of oxygen being excessively increased will cause energy consumption increase.For the waste water of organic concentration dynamic change, guarantee oxygen
Supply and COD concentration are maintained at the strong guarantee that stable ratio is the operation of commercial plant efficient stable.Patent
CN201110257500.X uses air as oxidant and aoxidizes to coking wastewater, under identical temperature and pressure, in air
Meltage of the oxygen in waste water it is lower than meltage of the oxygen rich gas in waste water, be unfavorable for the efficient removal of organic matter, specially
COD removal efficiency is only up to 22% in sharp CN201110257500.X.This patent is higher than the oxygen rich gas of air using concentration, has
Effect improves water oxygen concentration, to improve the organic matter removal efficiency of catalyst.
Patent CN201610363957.1 uses the oxygen of concentration range 10%-99.999% as oxidant to petroleum base
Slag is aoxidized, which uses palladium-carbon catalyst, and the petroleum alkaline residue of processing is the alkaline waste water that NaOH content is 5%-15%.
Easy carbon distribution forms the polymer such as graphitic carbon and condensed-nuclei aromatics, this kind of object to organic matter at high temperature under high pressure during catalytic wet oxidation
Matter can be firmly adsorbed on catalyst surface, and blocking catalyst duct simultaneously covers activated centre, reactant is made to be difficult to be diffused into
On activated centre inside micropore, so as to cause catalyst activity reduction.The method of catalyst inactivation is inhibited mainly to be catalyzed
Anti-carbon auxiliary agent is added in agent, anti-carbon auxiliary agent mainly includes alkali metal promoter and precious metals ag auxiliary agent [[Santiago A F
J,Sousa J F,Guedes R C,et al.Kinetic and wet oxidation of phenol catalyzed by
non-promoted and potassium-promoted manganese/cerium oxide[J].Journal of
Hazardous Materials,2006,138(2):325-330；Hamoudi S,Sayari A,Belkacemi K,et
al.Catalytic wet oxidation of phenol over PtxAg1-xMnO2/CeO2 catalysts[J]
.Catalysis Today, 2000,62 (4): 379-388.], the petroleum alkaline residue of patent CN201610363957.1 processing is alkali
Property waste water, catalyst is in always in the environment of alkali metal containing, to can avoid catalyst carbon deposition.Of the invention matched catalysis
Agent has very high carbon accumulation resisting ability using Ag as one of active metal, and therefore, the waste water that the present invention is handled is not limited by raw water
System, can handle the high concentration hard-degraded organic waste water in a variety of sources.The report of the prior art is not found through retrieval.
Summary of the invention
The object of the present invention is to provide a kind of catalysis that can effectively remove acid or alkaline organic wastewater middle and high concentration COD is wet
The technique of formula oxidation treated high concentration organic wastewater.
The present invention aoxidizes the COD in waste water using oxygen-nitrogen mixed gas as oxidant.To keep gas-liquid equal
Even mixing simultaneously makes device stable operation, and wastewater liquid air speed and oxygen rich gas air speed is made to keep certain proportionate relationship, oxygen rich air
Body air speed is between 34 times to 39 times of wastewater liquid air speed；Meanwhile in order to improve oxygen utilization rate, holding oxygen offer amount is
1.1-1.2 times of theoretical requirement.Auto-associating technique is adjusted using COD concentration on-line checking and oxygen concentration, according to waste water
COD concentration and air speed variation automatic adjustment oxygen concentration.Waste water COD concentration (S1), wastewater liquid air speed (H1), oxygen rich gas are dense
Spend (S2), oxygen rich gas air speed (H2), the ratio (V) between oxygen supply amount/theoretical oxygen demand, formula 1 are as follows:
H2/H1=0.07*V*S1/S2, wherein 34≤H2/H1≤39,1.1≤V≤1.2 (formula 1)
The variation range for setting V and H2/H1, when inlet effluent fluctuation of operating conditions, wastewater liquid air speed and the variation of COD concentration
When, oxygenerator is automatically adjusted the oxygen volumetric concentration of oxygen rich gas by formula 1.
The technique of catalytic wet oxidation processing high concentrated organic wastewater of the invention, includes the following steps:
The present invention using COD concentration on-line checking and with oxygen concentration adjusting device auto-associating, be by COD content
10000-50000mg/L, wastewater liquid air speed are 0.5-2.5h-1Organic wastewater mixed with oxygen rich gas.Oxygen rich gas is empty
Speed is 34-39 times of wastewater liquid air speed, 1.1-1.2 times that oxygen supply amount is theoretical oxygen demand, according to formula 1, device from
The dynamic oxygen volumetric concentration that adjusts is 25%-99%, to meet formula 1, to improve oxygen utilization rate and improve waste water removing effect
Rate enters heat exchanger after gas-liquid mixed and exchanges heat with the steam after oxidation reaction, then after the heating of preheated device, is sent into and fills
There is the waste water reactor of catalyst, is reacted under the conditions of 150-250 DEG C, 2.0-6.0MPa；Water after oxidation reaction
Vapour first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation, treated, and water is direct
Outlet is sent into next processing section, and the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere.
Catalyst noble metal load capacity 0.3-0.5wt%, Ag load capacity 0.5-2.0wt% as described above, metal promoter
Load capacity is 0.05-0.5wt%, and surplus is carrier.Specific preparation method is shown in that number of patent application is 201810389974.1, hair
The content of bright entitled " a kind of catalyst and preparation method and application for handling high concentrated organic wastewater ".
The determination of reaction condition needs association reaction feature and catalyst performance to comprehensively consider.Catalytic wet oxidation need to be appropriate
Reaction pressure under carry out, to guarantee the solubility of oxygen in water, sufficient oxidant, reaction pressure are provided for oxidation reaction
When lower than 2.0MPa, concentration of oxygen gas is too low, is unfavorable for the oxidation of COD, and when reaction pressure is higher than 6.0MPa, organic matter is being changed
Polymerization, carbon distribution easily occur in hot device pipeline, thus blocking device, the present invention reacts under the conditions of 2.0-6.0MPa.When anti-
It when answering temperature lower than 150 DEG C, reacts by dynamics Controlling, the oxidation rate of COD is slower, COD removal efficiency is influenced, when reaction temperature
When degree is higher than 250 DEG C, the saturated vapour pressure that will cause water in reaction system is increased, and large amount of organic enters gas phase, organic matter
The rate for diffusing into catalyst duct is slack-off, and COD removal efficiency reduces, and the present invention reacts under the conditions of 150-250 DEG C.
When oxygen content is lower than 1.1 times of theoretical requirement, all COD cannot be made to touch oxygen, COD removal efficiency is not high, and oxygen contains
When amount is higher than 1.2 times of theoretical oxygen demand, oxygen-supplying amount is excessively increased, the increase of organic matter removal efficiency is not contributed, and invalid oxygen
The increase of tolerance will increase the power of air or oxygen compressor, while extra oxygen can take away reaction heat, reduce reaction system
The heat utilization ratio of system, the present invention make 1.1-1.2 times of oxygen content theoretical requirement.
COD removal efficiency > 94.15% of technique and catalyst as described above.
Catalytic wet oxidation organic wastewater process route provided by the invention has the advantage that
When waste strength and liquid air speed change, pass through association waterwater entrance COD concentration and inlet wastewater liquid
Air speed automatically adjusts oxygen rich gas gas space velocity and oxygen volumetric concentration, controls practical oxygen supply, is remarkably improved waste water
Treatment effeciency simultaneously reaches being optimal of oxygen utilization rate, reduces process energy consumption.The COD of technique as described above and catalyst is de-
Except rate > 94.15%.The organic wastewater for being 10000~50000mg/L for COD concentration, effluent COD concentration is in 40-
Between 1855mg/L.Wherein COD concentration meets the national 1 grade of direct outlet of discharge standard of waste water in the waste water of 40-50mg/L,
COD concentration enters subsequent processing workshop section in the waste water of 50-2925mg/L.
Detailed description of the invention
Fig. 1 is catalytic wet oxidation organic wastewater process flow diagram.
Specific embodiment
For a better understanding of the present invention, be given below several illustratives rather than restrictive embodiment.
Embodiment 1:
By the catalyst (Pd-Ag-Zn/TiO of embodiment 3 in CN201810389974.12, wherein Pd accounts for 0.44wt%,
Ag accounts for 1.5wt%, and Zn accounts for 0.35wt%, TiO2Accounting for 97.71wt%) 4ml is loaded in fixed bed reactors.The COD of waste water contains
Amount is 10000mg/L, air speed 0.5h-1, giving oxygen rich gas air speed is 34 times of (16.8h of waste water air speed-1), oxygen concentration be
1.2 times of theoretical oxygen demand, it is 25% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchange after mixing with oxygen rich gas
Device, gas-liquid mixture is sent into waste water reactor after heat exchange, is reacted under the conditions of 250 DEG C, 6.0MPa；After oxidation reaction
Steam first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation, treated, and water is straight
Outlet is connect, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 2:
By the catalyst of embodiment 5 in CN201810389974.1 (Ru-Ag-La/ molecular sieve, wherein Ru accounts for 0.3wt%,
Ag accounts for 0.9wt%, and La accounts for 0.05wt%, and molecular sieve accounts for 98.75wt%) 4ml is loaded in fixed bed reactors.The COD of waste water
Content is 30000mg/L, air speed 1h-1, giving oxygen rich gas air speed is 35 times of (35h of waste water air speed-1), oxygen concentration be reason
By 1.15 times of oxygen demand, it is 69% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchange after mixing with oxygen rich gas
Device, gas-liquid mixture is sent into waste water reactor after heat exchange, is reacted under the conditions of 200 DEG C, 5.0MPa；After oxidation reaction
Steam first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation；Treated, and water is sent
Enter next processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 3:
By the catalyst (Au-Ag-Mo/ZrO of embodiment 7 in CN201810389974.12, wherein Au accounts for 0.4wt%, Ag
1.2wt% is accounted for, Mo accounts for 0.5wt%, ZrO2Accounting for 97.9wt%) 4ml is loaded in fixed bed reactors.The COD content of waste water is
20000mg/L, air speed 1.5h-1, giving oxygen rich gas air speed is 36 times of (54h of waste water air speed-1), oxygen concentration be theoretical need
1.2 times of oxygen amount, it is 47% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchanger after mixing with oxygen rich gas, changes
Gas-liquid mixture is sent into waste water reactor after heat, is reacted under the conditions of 210 DEG C, 4.0MPa；Steam after oxidation reaction
Heat exchanger is first passed through, is cooled down using water cooler, knockout drum is sent into later and carries out gas-liquid separation；Under water feeding that treated
One processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour are directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 4:
By the catalyst (Rh-Ag-Mn/CeO of embodiment 1 in CN201810389974.12, wherein Rh accounts for 0.32wt%,
Ag accounts for 0.5wt%, and Mn accounts for 0.25wt%, CeO2Accounting for 98.93wt%) 4ml is loaded in fixed bed reactors.The COD of waste water contains
Amount is 40000mg/L, air speed 2h-1, giving oxygen rich gas air speed is 37 times of (74h of waste water air speed-1), oxygen concentration be theory
1.2 times of oxygen demand, it is 91% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchanger after mixing with oxygen rich gas,
Gas-liquid mixture is sent into waste water reactor after heat exchange, is reacted under the conditions of 150 DEG C, 5.0MPa；Water after oxidation reaction
Vapour first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation；Treated, and water is sent into
Next processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour are directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 5:
By the catalyst (Pd-Ag-Sn/ZrO of embodiment 4 in CN201810389974.12, wherein Pd accounts for 0.35wt%,
Ag accounts for 0.2wt%, and Sn accounts for 0.45wt%, ZrO2Accounting for 97.2wt%) 4ml is loaded in fixed bed reactors.The COD content of waste water
For 50000mg/L, air speed 2.5h-1, giving oxygen rich gas air speed is 39 times of (97.25h of waste water air speed-1), oxygen concentration be reason
By 1.1 times of oxygen demand, it is 99% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchange after mixing with oxygen rich gas
Device, gas-liquid mixture is sent into waste water reactor after heat exchange, is reacted under the conditions of 250 DEG C, 3.0MPa；After oxidation reaction
Steam first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation；Treated, and water is sent
Enter next processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 6:
By the catalyst (Rh-Ag-Fe/Al of embodiment 2 in CN201810389974.12O3, wherein Rh accounts for 0.38wt%,
Ag accounts for 0.8wt%, and Fe accounts for 0.5wt%, Al2O3Accounting for 98.32wt%) 4ml is loaded in fixed bed reactors.The COD content of waste water
For 30000mg/L, air speed 1h-1, giving oxygen rich gas air speed is 38 times of (38h of waste water air speed-1), oxygen concentration be theoretical need
1.15 times of oxygen amount, it is 64% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchanger after mixing with oxygen rich gas, changes
Gas-liquid mixture is sent into waste water reactor after heat, is reacted under the conditions of 190 DEG C, 2.0MPa；Steam after oxidation reaction
Heat exchanger is first passed through, is cooled down using water cooler, knockout drum is sent into later and carries out gas-liquid separation；Under water feeding that treated
One processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour are directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 7:
By the catalyst (Ru-Ag-Co/TiO of embodiment 6 in CN201810389974.12, wherein Ru accounts for 0.45wt%,
Ag accounts for 1.8wt%, and Co accounts for 0.28wt%, TiO2Accounting for 97.47wt%) 4ml is loaded in fixed bed reactors.The COD of waste water contains
Amount is 20000mg/L, air speed 1.5h-1, giving oxygen rich gas air speed is 34 times of (51h of waste water air speed-1), oxygen concentration be reason
By 1.15 times of oxygen demand, it is 47% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchange after mixing with oxygen rich gas
Device, gas-liquid mixture is sent into waste water reactor after heat exchange, is reacted under the conditions of 180 DEG C, 6.0MPa；After oxidation reaction
Steam first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation；Treated, and water is sent
Enter next processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere.Reaction result is shown in Table 1.
Embodiment 8:
By the catalyst of embodiment 5 in CN201810389974.1 (Ru-Ag-La/ molecular sieve, wherein Ru accounts for 0.3wt%,
Ag accounts for 0.9wt%, and La accounts for 0.05wt%, and molecular sieve accounts for 98.75wt%) 4ml is loaded in fixed bed reactors.The COD of waste water
Content is 40000mg/L, air speed 2h-1, giving oxygen rich gas air speed is 35 times of (70h of waste water air speed-1), oxygen concentration be reason
By 1.1 times of oxygen demand, it is 99% that oxygenerator, which automatically adjusts oxygen concentration,.Waste water enters heat exchange after mixing with oxygen rich gas
Device, gas-liquid mixture is sent into waste water reactor after heat exchange, is reacted under the conditions of 160 DEG C, 3.0MPa；After oxidation reaction
Steam first passes through heat exchanger, cools down using water cooler, is sent into knockout drum later and carries out gas-liquid separation；Treated, and water is sent
Enter next processing section, the tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere.Reaction result is shown in Table 1.
The waste water COD removal efficiency of each embodiment of table 1
| Embodiment | COD concentration (mg/L) in waste water | COD concentration (mg/L) in processed waste water | Removal efficiency (%) |
| 1 | 10000 | 40 | 99.6 |
| 2 | 30000 | 1137 | 96.21 |
| 3 | 20000 | 170 | 99.15 |
| 4 | 40000 | 1144 | 97.14 |
| 5 | 50000 | 2925 | 94.15 |
| 6 | 30000 | 795 | 97.35 |
| 7 | 20000 | 770 | 96.15 |
| 8 | 40000 | 968 | 97.58 |
Claims (2)
1. a kind of technique of catalytic wet oxidation processing high concentrated organic wastewater, it is characterised in that include the following steps
Using COD concentration on-line checking and with oxygen concentration adjusting device auto-associating, by COD content be 10000-50000
Mg/L, wastewater liquid air speed are 0.5-2.5 h-1Organic wastewater mixed with oxygen rich gas；
Oxygen rich gas air speed is 34-39 times of wastewater liquid air speed, oxygen supply amount is theoretical oxygen demand 1.1-1.2 times,
According to formula 1, it is 25%-99% that device, which automatically adjusts oxygen volumetric concentration, to meet formula 1, enters heat exchanger and warp after gas-liquid mixed
Steam after oxidation reaction exchanges heat, then after the heating of preheated device, is sent into the waste water reactor that catalyst is housed,
150-250 DEG C, reacted under the conditions of 2.0-6.0 MPa；Steam after oxidation reaction first passes through heat exchanger, using water
Cooler cooling is sent into knockout drum later and carries out gas-liquid separation, the direct outlet of water that treated or the next processing section of feeding,
Tail gas containing nitrogen, oxygen, carbon dioxide, water vapour is directly discharged into atmosphere；
Wherein formula 1 are as follows:
H2/H1=0.07*V*S1/S2, wherein 34≤H2/H1≤39,1.1≤V≤1.2；
S1 is waste water COD concentration, and H1 is wastewater liquid air speed, and S2 is oxygen rich gas concentration, and rich H2 is carrier of oxygen air speed, and V is oxygen
Ratio between gas supply/theoretical oxygen demand.
2. a kind of technique of catalytic wet oxidation processing high concentrated organic wastewater as described in claim 1, it is characterised in that institute
Catalyst noble metal load capacity 0.3-0.5wt%, Ag load capacity 0.5-2.0wt% is stated, the load capacity of metal promoter is 0.05-
0.5wt%, surplus are carrier.
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| CN201811459079.9A CN109455808A (en) | 2018-11-30 | 2018-11-30 | A kind of technique of catalytic wet oxidation processing high concentrated organic wastewater |
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| CN201811459079.9A CN109455808A (en) | 2018-11-30 | 2018-11-30 | A kind of technique of catalytic wet oxidation processing high concentrated organic wastewater |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110386692A (en) * | 2019-07-26 | 2019-10-29 | 宜兴国际环保城科技发展有限公司 | A kind of auxiliary agent waste water treatment process |
| CN111573964A (en) * | 2020-03-24 | 2020-08-25 | 南京延长反应技术研究院有限公司 | Built-in micro-interface papermaking wastewater treatment system and treatment method |
| CN112254557A (en) * | 2020-09-24 | 2021-01-22 | 万华化学集团股份有限公司 | Plate-shell type heat exchanger integrated with gas-liquid mixer and method and device system for treating organic wastewater by using plate-shell type heat exchanger |
| CN113716674A (en) * | 2021-09-27 | 2021-11-30 | 格瑞环保科技(深圳)有限公司 | Kitchen waste sewage treatment system |
-
2018
- 2018-11-30 CN CN201811459079.9A patent/CN109455808A/en not_active Withdrawn
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110386692A (en) * | 2019-07-26 | 2019-10-29 | 宜兴国际环保城科技发展有限公司 | A kind of auxiliary agent waste water treatment process |
| CN110386692B (en) * | 2019-07-26 | 2022-03-22 | 福泉环保城发展有限公司 | Auxiliary agent wastewater treatment process |
| CN111573964A (en) * | 2020-03-24 | 2020-08-25 | 南京延长反应技术研究院有限公司 | Built-in micro-interface papermaking wastewater treatment system and treatment method |
| CN111573964B (en) * | 2020-03-24 | 2021-07-09 | 南京延长反应技术研究院有限公司 | Built-in micro-interface papermaking wastewater treatment system and treatment method |
| CN112254557A (en) * | 2020-09-24 | 2021-01-22 | 万华化学集团股份有限公司 | Plate-shell type heat exchanger integrated with gas-liquid mixer and method and device system for treating organic wastewater by using plate-shell type heat exchanger |
| CN113716674A (en) * | 2021-09-27 | 2021-11-30 | 格瑞环保科技(深圳)有限公司 | Kitchen waste sewage treatment system |
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Application publication date: 20190312 |
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