CN105417769A - Laboratory carbon tetrachloride separation treatment system and treatment process thereof - Google Patents
Laboratory carbon tetrachloride separation treatment system and treatment process thereof Download PDFInfo
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- CN105417769A CN105417769A CN201510778935.7A CN201510778935A CN105417769A CN 105417769 A CN105417769 A CN 105417769A CN 201510778935 A CN201510778935 A CN 201510778935A CN 105417769 A CN105417769 A CN 105417769A
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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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
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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
- C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
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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
- C02F2103/003—Wastewater from hospitals, laboratories and the like, heavily contaminated by pathogenic microorganisms
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Abstract
The invention discloses a laboratory carbon tetrachloride separation treatment system and a treatment process thereof. The laboratory carbon tetrachloride separation treatment system comprises an activated carbon filter box with S-shaped adsorption tanks and a treatment region with a nano-bubble generator. The activated carbon filter box and the treatment region are arranged in an aeration reaction box and partitioned through a partition plate and are communicated through a flow guiding pipe. The S-shaped adsorption tanks are filled with activated carbon filler and internally provided with suspension plates, and one end of each S-shaped adsorption tank is provided with a water outflow pipe. One end of the aeration reaction tank is provided with a residual liquid inflow pipe. The laboratory carbon tetrachloride separation treatment system and the treatment process thereof have the advantages that due to the adoption of an oxidation, aeration and adsorption joint treatment mode, the treatment efficiency is high, and the high removal effect is achieved for high-concentration volatile substances containing tetrachloride laboratory residual liquid; in the adsorption process of activated carbon, the activated carbon filter tank is divided into the multiple S-shaped adsorption tanks through the suspension plates, the laboratory residual liquid containing carbon tetrachloride flows in an S-shaped path, the contact time of the residual liquid and the activated carbon is prolonged, meanwhile, the contact area of the residual liquid and oxygen is increased, and treatment efficiency is improved.
Description
Technical field
The invention belongs to environmental protection treatment technology, relate to the organic process field containing tetracol phenixin laboratory raffinate of high density, particularly relate to a kind of laboratory tetracol phenixin separation process system and treatment process thereof.
Background technology
Tetracol phenixin (CCl
4) be a kind of organic hydrochloric ether of lower boiling (proportion 1.591g/cm of synthetic
3, boiling point 77 DEG C), be slightly soluble in water.Foreign study shows: tetracol phenixin belongs to typical hepatotoxic agent, during high density, is first affect central nervous system, affects liver, kidney subsequently.It has persistence, extended residual and bioconcentration in the environment, has therefore been listed in by U.S. EPA from 1979 " pollutent containing priority acccess control in tetracol phenixin underground water ", has also been listed in the 68 kinds of pollutent of priority acccess control " in the water " lists by China.
Eighties of last century the seventies is owing to manufacturing in a large number and using agricultural chemicals, cause some regional underground water by Carbon Tetrachloride Contamination, if the waterbearing stratum near the Michigan waterbearing stratum of the U.S. and Canadian Ottawa is all by the pollution (it exists mainly with nonaqueous phase (NAPL) in waterbearing stratum) of being tetracol phenixin.
The pollution that before the U.S., FortordArmy causes in military base makes CCl in the municipal water supply of Marina
4exceed standard, in August, 2000 records CCl
4concentration reaches 15 μ g/L.The groundwater monitoring in U.S. Livermore area finds that the stacking of poisonous Harmful Waste causes CCl
4the generation of pollutent, CCl in toxic substance percolate
4concentration up to 500 μ g/L.In April, 2000, underground water CCl in the MW-10 well near Hafner & Sons refuse landfill
4concentration reaches 6.3 μ g/L.
At home, the shallow ground water of Xiaoqing River, Shandong Province bank once suffered CCl
4pollution, maximum concentration reaches 380 μ g/L, and contaminated area reaches 80km
2.Xiaoqinghe River Ya Wangkou, western lock two measuring point shallow ground water CCl
4content is 16.0-380.0 μ g/L.1997, detect CCl in the tap water of Zhabei District in Shanghai
4content is 1.17 μ g/L, and Xicheng District of Beijing and Xuanwu District are then respectively 0.24 and 0.32 μ g/L.Within 2000, carry out carbon tetrachloride content monitoring to China's somewhere shallow ground water, find have 3 wells to receive pollution, May calendar year 2001 in the waterhead area of southern suburbs, existing 53 karstic ground water wells receive pollution, and area reaches 17.5km
2, in water, tetracol phenixin maximum concentration reaches 3909.2 μ g/L, exceedes national drinking water standard 1954.6 times, and the healthy of area more than 20 ten thousand people that supply water in serious threat.
Existing Treatment process
Tetracol phenixin common are organic pollutants in soil and groundwater, easily enters in soil and groundwater with rainwater or irrigation water by eluviation, cause the pollution of soil and groundwater body.The traditional method of administering about Carbon Tetrachloride Contamination in underground water at present has following several:
1. active carbon adsorption
With the tetracol phenixin in charcoal absorption water source, without the need to adding any chemical reagent, technical requirements is not high, lower concentration advantages of good adsorption effect, and some materials being difficult to degrade can directly adsorb on the activated carbon.By having investigated the factors such as gac dosage, adsorption time, temperature to the impact of removal effect.
This method technical maturity, simple to operate reliable for effect, but adsorption efficiency is unstable, effective when tetracol phenixin is in lower concentration, during high density, process is unstable, the active adsorption life-span is short, carrier needs to carry out secondary desorb just can carry out circulating use, and by the solution after solvent desorption, forms again the mixture containing tetracol phenixin, how to be isolated again, to need to study further.
2. aeration process repairing method
Pressurized air is injected underground water saturation zone by aeration process reparation, gas moves upward in process and causes volatile contaminant to enter gas phase from the soil body and underground water, make the air containing pollutent rise to unsatalation zone, then reach remove the object of pollutent by the process of gas phase extraction system.The based technique for in-situ remediation of this process underground water saturation zone volatile organic contaminant, owing to can the advantage of original position construction make it be used widely, be applied to molecular weight more, easily becomes the pollutent of gas phase from liquid phase.
But aeration process repairing method is easily subject to the factor impacts such as gas flow shape change, number of bubbles, bubble size, gas channel density, reduce processing power because treatment process is different simultaneously.Aeration process repairing method in force, if there is local low-permeability soil layer in zone of pollution, air and pollutent are difficult to fully contact, if there is structural crack or zone of fracture in underground water saturation zone, the air injected then easily forms preferential flow, cause aeration short circuit, greatly affect process range and treatment effect, zone of pollution is difficult to effectively be repaired.Simultaneously aeration process repairing method is also subject to water-soluble and volatile direct impact of soil response type, place uniformity, ground water table and flowing, pollutent, such that remediation efficiency declines, cost increase.
3. in situ chemical oxidation method
The oxygenant permanganate that in-situ chemical recovery technique adopts, Fenton reagent, hydrogen peroxide and persulphate etc.
Oxygenant is injected into underground pollution district, soil and waterbearing stratum itself are containing a large amount of virgin iron mineral, and under the effect of iron mineral catalysis, oxidizing reaction can the organic pollutant of effectively rehabilitating soil and underground water.Research shows that in-situ chemical recovery technique easily makes reparation district soil produce mineralising, makes reparation district soil compaction, bad hydraulic permeability, changes and repair district's Soil structure.
4. biological restoration
Utilize bio-inert and organic clay adsorbed bioactive bacterium, by the metabolism of biology, reduce the engineering techniques of poisonous and harmful compound in underground environment, biology in situ repairing method can process large-scale pollutent, and can complete decomposing pollutant.
Current biology in situ repairing method is an emerging technology for process underground water Organic pollutants source, the key factor of biological restoration is suitable electron acceptor(EA), and the oxygen acceptor that has been best electricity, due to this electron acceptor(EA) of deficiency of oxigen in underground environment, the simultaneously undersupply of microbial nutrition material, also makes the biological degradation of microorganism can not be lasting.
5. permeable reactive wall repairing method
Utilize and be filled with the dependent response district of Active reaction medium material, when contaminated underground water by time, pollution substance wherein and reaction medium generation physics, chemistry and biological etc. act on and be degraded, adsorb, precipitate or remove, thus sewage is purified.
But permeable coefficient tensor exists easily blocked, the its native environmental conditions such as the redox potential of underground water easily go to pot, shortcoming such as reaction wall engineering measure and running maintenance relative complex etc., add that bimetallic systems, nanotechnology cost are higher, these factors hinder further developing of permeable coefficient tensor and widely popularize.
6. original position aeration repairing method
Original position aeration process is a kind of based technique for in-situ remediation of emerging underground water volatile organic matter, below air Injection Polluted area, volatile organic compounds is resolved to airflow from underground water and causes the based technique for in-situ remediation that ground processes, enough oxygen can be provided for the aerobic microbiological in underground water to deep well injection air simultaneously, promote the Degradation of indigenous microorganism.This technology, in acceptable cost-range, can process more Polluted Groundwater, and system is easily installed and shifted, and easy and other technical combinations uses.
But because geologic framework is complicated, when injecting air and running into complete rock stratum band, loosening shatter belt or flexural deformation band, the injection air carrying volatile organic matter is difficult to penetrate above-mentioned geologic framework, when injection air runs into above-mentioned geologic framework simultaneously, atmospheric drag is large, and equipment energy consumption will be made greatly to improve.To be not only not easy volatilization but also not easily biodegradable Pollutant Treatment effect more not good.
Summary of the invention
The technical problem that the present invention solves is: provide a kind of for flowing in aerated reaction case by the raffinate containing tetracol phenixin in laboratory to overcome above the deficiencies in the prior art, the separation of tetracol phenixin is being realized after the processes such as oxidation, aeration, absorption, solve the defect that conventional processes exists, and improved.Technical scheme support is provided containing tetracol phenixin laboratory raffinate advanced treatment for follow-up.
For achieving the above object, the present invention is by the following technical solutions:
A kind of laboratory tetracol phenixin separation process system, comprise the active carbon filtration case containing S shape adsorption tank and the treatment zone with nano-bubble generator, the two is placed in aerated reaction case, is separated by dividing plate, and is communicated with through thrust-augmenting nozzle; Wherein S shape adsorption tank inside is filled active carbon filler and is provided with unsettled plate, and one end of S shape adsorption tank is provided with rising pipe; One end of aerated reaction case is provided with raffinate water inlet pipe.
Further, S shape adsorption tank is formed by unsettled plate vertical direction Heterogeneous Permutation.
Further, the quantity of unsettled plate is at least one.
Further, nano-bubble generator stretches in aerated reaction case, is divided into high-speed rotor impeller, micro porous aeration head and air access tube, and wherein micro porous aeration head is located at air access tube venting port one end, and high-speed rotor impeller is arranged on air access tube.
Further, raffinate water inlet pipe is three-way pipe structure, is communicated with hydrogen peroxide filler pipe, and is communicated with aerated reaction case by mouth at the bottom of raffinate water inlet pipe.
Further, rising pipe is divided into porous header and liquid discharge pipe, and wherein the quantity of porous header is at least one.
Further, the packing height of the inner active carbon filler of S shape adsorption tank is not less than the height of gauging line.
Further, the packing height of the inner active carbon filler of S shape adsorption tank is higher than gauging line 10 ~ 20 centimetres.
Above laboratory tetracol phenixin separation process system carries out the technique of tetracol phenixin process, flow process is as follows: tetracol phenixin raffinate enters aerated reaction case by raffinate water inlet pipe, hydrogen peroxide reaction reagent enters aerated reaction case by hydrogen peroxide filler pipe simultaneously, reacts with tetracol phenixin raffinate; Simultaneously, outside air enters nano-bubble generator by air access tube, high-speed rotor impeller rotates with the rotating speed of speed 3000 ~ 9000 revs/min, the microbubble that micro porous aeration head produces is smashed into the bubble of diameter 10 ~ 600 nanometer, be diffused into reaction box house equably, and fully react with tetracol phenixin in aerated reaction case; Solution after process enters activated carbon filtration case by thrust-augmenting nozzle, because activated carbon filtration case inside is provided with at least one unsettled plate, and Heterogeneous Permutation in the vertical direction, impel raffinate to present S path in active carbon filtration case inside and arrive porous header place, finally discharge through liquid discharge pipe; Wherein control condition is air flow is 80 liters/min, water level 80 centimetres, temperature are 60 DEG C, aeration time is 2 hours.
Technique scheme discloses based on flowing in aerated reaction case process containing tetracol phenixin laboratory raffinate, by the tetracol phenixin separation system that tetracol phenixin is separated, utilizes built-up type treatment process to remove the innoxious process for treating of tetracol phenixin in the raffinate of laboratory.The pending laboratory raffinate containing tetracol phenixin is entered aerated reaction case through raffinate water inlet pipe, and hydrogen peroxide mixes with raffinate simultaneously, is oxidized raffinate; Meanwhile, fresh air is squeezed into air access tube by air pump, forms a large amount of nano bubble, impel carbon dioxide gasification under the effect of nano-bubble generator in aerated reaction case; Raffinate after preliminary treatment flows into activated carbon filtration case through thrust-augmenting nozzle, with the flowing of S shape path in S shape adsorption tank, thus adds aeration and activated carbon adsorption time, impels tetracol phenixin to be separated from water body.
Beneficial effect
Laboratory disclosed by the invention tetracol phenixin separation process system and treatment process thereof, its advantage is:
(1) owing to have employed oxidation, aeration, absorption combination treatment mode, its processing efficiency is high, and volatile matter high density being contained to tetrachloro laboratory raffinate has higher removal effect;
(2) in charcoal adsorption process, activated carbon filtration case is divided into multiple S shape adsorption tank by unsettled plate, containing tetracol phenixin laboratory raffinate with the flowing of S shape path, adds the duration of contact of raffinate and gac, add the contact area of raffinate and oxygen simultaneously, improve processing efficiency.
Accompanying drawing explanation
Fig. 1 is laboratory of the present invention tetracol phenixin separation process system structural representation;
Fig. 2 is laboratory of the present invention tetracol phenixin separation process system vertical view;
Fig. 3 is laboratory of the present invention tetracol phenixin separation process system front view;
Fig. 4 is laboratory of the present invention tetracol phenixin separation process system schematic perspective view;
Fig. 5 is the service branch structure schematic diagram of laboratory of the present invention tetracol phenixin separation process system;
Wherein, 1 is nano-bubble generator, and 1-1 is high-speed rotor impeller, and 1-2 is micro porous aeration head, 1-3 is air access tube, and 2 is aerated reaction case, and 3 is thrust-augmenting nozzle, 4 is S shape adsorption tank, and 5 is dividing plate, and 6 is raffinate water inlet pipe, 6-1 is hydrogen peroxide filler pipe, and 7 is mouth at the bottom of raffinate water inlet pipe, and 8 is active carbon filler, 9 is unsettled plate, and 10 is rising pipe, and 10-1 is porous header, 10-2 is liquid discharge pipe, and 11 is activated carbon filtration case, and 12 is gauging line.
Embodiment
Below in conjunction with accompanying drawing, laboratory of the present invention tetracol phenixin separation process system is described in detail.
Embodiment 1
As shown in Figure 1, for laboratory of the present invention tetracol phenixin separation process system structural representation, can find out, comprise the active carbon filtration case 11 containing S shape adsorption tank 4 and the treatment zone with nano-bubble generator 1, the two is placed in aerated reaction case 2, separated by dividing plate 5, and be communicated with through thrust-augmenting nozzle 3; Wherein active carbon filler 8 is filled and the one end being provided with unsettled plate 9, S shape adsorption tank 4 is provided with rising pipe 10 in S shape adsorption tank 4 inside; One end of aerated reaction case 2 is provided with raffinate water inlet pipe 6.
As shown in Figure 3, be laboratory of the present invention tetracol phenixin separation process system front view, can find out, S shape adsorption tank 4 is formed by unsettled plate 9 vertical direction Heterogeneous Permutation, and the quantity of unsettled plate 9 is at least one.
In laboratory tetracol phenixin separation process system described in the present embodiment, nano-bubble generator 1 stretches in aerated reaction case 2, be divided into high-speed rotor impeller 1-1, micro porous aeration head 1-2 and air access tube 1-3, wherein micro porous aeration head 1-2 is located at air access tube 1-3 venting port one end, and high-speed rotor impeller 1-1 is arranged on air access tube 1-3.
As shown in Figure 4, be laboratory of the present invention tetracol phenixin separation process system schematic perspective view, raffinate water inlet pipe 6 is three-way pipe structure, is communicated with hydrogen peroxide filler pipe 6-1, and is communicated with aerated reaction case 2 by mouth 7 at the bottom of raffinate water inlet pipe.
As shown in Figure 5, be the service branch structure schematic diagram of laboratory of the present invention tetracol phenixin separation process system, can find out, rising pipe 10 is divided into porous header 10-1 and liquid discharge pipe 10-2, and wherein the quantity of porous header 10-1 is at least one.
In the present embodiment, the packing height of the inner active carbon filler 8 of S shape adsorption tank 4 is not less than the height of gauging line, and in figure, 12 are expressed as the gauging line in tetracol phenixin separating treatment process.
Embodiment 2
Above-mentioned separation system is utilized to process the laboratory raffinate containing tetracol phenixin, first, tetracol phenixin raffinate enters aerated reaction case 2 by raffinate water inlet pipe 6, and hydrogen peroxide reaction reagent enters aerated reaction case 2 by hydrogen peroxide filler pipe 6-1 simultaneously, reacts with tetracol phenixin raffinate; Simultaneously, outside air enters nano-bubble generator 1 by air access tube 1-3, high-speed rotor impeller 1-1 rotates with the rotating speed of speed 3000 ~ 9000 revs/min, the microbubble that micro porous aeration head 1-2 produces is smashed into the bubble of diameter 10 ~ 600 nanometer, be diffused into reaction box house equably, and fully react with tetracol phenixin in aerated reaction case 2.
Solution after process enters activated carbon filtration case 11 by thrust-augmenting nozzle 3, because activated carbon filtration case 11 inside is provided with at least one unsettled plate 9, and Heterogeneous Permutation in the vertical direction, impel raffinate to present S path in active carbon filtration case 11 inside and arrive porous header 10-1 place, finally discharge through liquid discharge pipe 10-2; Wherein control condition is air flow is 80 liters/min, water level 80 centimetres, temperature are 60 DEG C, aeration time is 2 hours.
In order to the reasonableness of test design, make it reach best treatment effect, detected by above tetracol phenixin separation system to tetracol phenixin clearance, verify the reasonableness designed and optimal operating parameter, result is as follows:
In simulation tetracol phenixin separation system, containing in the laboratory raffinate of tetracol phenixin, the concentration of tetracol phenixin is 20 μ g/L, control simulation system temperature is 60 DEG C, aeration time is 2 hours, air flow is 80 liters/min, water level 80 centimetres, high-speed rotor impeller 1-1 respectively with speed 3000 revs/min, 5000 revs/min, 7000 revs/min, 9000 revs/min rotating speed rotate, concrete detected result is as shown in the table.
Tetracol phenixin removal effect in the raffinate of laboratory
Claims (9)
1. a laboratory tetracol phenixin separation process system, it is characterized in that, comprise the active carbon filtration case (11) containing S shape adsorption tank (4) and the treatment zone with nano-bubble generator (1), the two is placed in aerated reaction case (2), separated by dividing plate (5), and be communicated with through thrust-augmenting nozzle (3); Wherein S shape adsorption tank (4) inside is filled active carbon filler (8) and is provided with unsettled plate (9), and one end of S shape adsorption tank (4) is provided with rising pipe (10); One end of aerated reaction case (2) is provided with raffinate water inlet pipe (6).
2. a kind of laboratory tetracol phenixin separation process system according to claim 1, it is characterized in that, S shape adsorption tank (4) is formed by unsettled plate (9) vertical direction Heterogeneous Permutation.
3. a kind of laboratory tetracol phenixin separation process system according to claim 1 or 2, it is characterized in that, the quantity of unsettled plate (9) is at least one.
4. a kind of laboratory tetracol phenixin separation process system according to claim 1, it is characterized in that, nano-bubble generator (1) stretches in aerated reaction case (2), be divided into high-speed rotor impeller (1-1), micro porous aeration head (1-2) and air access tube (1-3), wherein micro porous aeration head (1-2) is located at air access tube (1-3) venting port one end, and high-speed rotor impeller (1-1) is arranged on air access tube (1-3).
5. a kind of laboratory tetracol phenixin separation process system according to claim 1, it is characterized in that, raffinate water inlet pipe (6) is three-way pipe structure, is communicated with hydrogen peroxide filler pipe (6-1), and is communicated with aerated reaction case (2) by mouth (7) at the bottom of raffinate water inlet pipe.
6. a kind of laboratory tetracol phenixin separation process system according to claim 1, it is characterized in that, rising pipe (10) is divided into porous header (10-1) and liquid discharge pipe (10-2), and wherein the quantity of porous header (10-1) is at least one.
7. a kind of laboratory tetracol phenixin separation process system according to claim 1, it is characterized in that, the packing height of S shape adsorption tank (4) inner active carbon filler (8) is not less than the height of gauging line (12).
8. a kind of laboratory tetracol phenixin separation process system according to claim 1 or 7, is characterized in that, the packing height of S shape adsorption tank (4) inner active carbon filler (8) is higher than gauging line (12) 10 ~ 20 centimetres.
9. a kind of laboratory according to claim 1 tetracol phenixin separation process system carries out the technique of tetracol phenixin process, it is characterized in that, technical process is as follows: tetracol phenixin raffinate enters aerated reaction case (2) by raffinate water inlet pipe (6), hydrogen peroxide reaction reagent enters aerated reaction case (2) by hydrogen peroxide filler pipe (6-1) simultaneously, reacts with tetracol phenixin raffinate; Simultaneously, outside air enters nano-bubble generator (1) by air access tube (1-3), high-speed rotor impeller (1-1) rotates with the rotating speed of speed 3000 ~ 9000 revs/min, the microbubble that micro porous aeration head (1-2) produces is smashed into the bubble of diameter 10 ~ 600 nanometer, be diffused into reaction box house equably, and fully react with tetracol phenixin in aerated reaction case (2); Solution after process enters activated carbon filtration case (11) by thrust-augmenting nozzle (3), because activated carbon filtration case (11) inside is provided with at least one unsettled plate (9), and Heterogeneous Permutation in the vertical direction, impel raffinate to present S path in active carbon filtration case (11) inside and arrive porous header (10-1) place, finally discharge through liquid discharge pipe (10-2); Wherein control condition is air flow is 80 liters/min, water level 80 centimetres, temperature are 60 DEG C, aeration time is 2 hours.
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| CN106006908A (en) * | 2016-05-24 | 2016-10-12 | 徐州工程学院 | Vehicular underground water carbon tetrachloride treatment equipment and water purifying method thereof |
| CN106045075A (en) * | 2016-05-24 | 2016-10-26 | 徐州工程学院 | Device for treating carbon tetrachloride in groundwater with spiral-flow aeration method, and carbon tetrachloride removing method |
| CN106045075B (en) * | 2016-05-24 | 2018-11-20 | 徐州腾睿智能装备有限公司 | Carbon tetrachloride device and its minimizing technology in a kind of spiral-flow aeration method processing underground water |
| CN106006908B (en) * | 2016-05-24 | 2018-12-21 | 徐州腾睿智能装备有限公司 | A kind of vehicular underground water carbon tetrachloride processing equipment and its process for purifying water |
| CN106219803A (en) * | 2016-08-10 | 2016-12-14 | 徐州工程学院 | A kind of carbon granule double layer filter based on biological activated carbon strengthening screening system |
| CN106219803B (en) * | 2016-08-10 | 2019-04-16 | 徐州工程学院 | A kind of carbon granule double layer filter reinforcing screening system based on biological activated carbon |
| CN106157770A (en) * | 2016-09-22 | 2016-11-23 | 陕西师范大学 | Methane and chlorine substitution reaction device and method |
| CN107569985A (en) * | 2017-09-27 | 2018-01-12 | 徐州工程学院 | One kind reaction cracker |
| CN107720869A (en) * | 2017-09-27 | 2018-02-23 | 徐州工程学院 | A kind of turbulence bed |
| CN114904410A (en) * | 2021-02-07 | 2022-08-16 | 佛山市顺德区美的洗涤电器制造有限公司 | Microbubble generating device and range hood |
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