CN1803662A - Method and equipment for removing organic chloride from wastewater - Google Patents
Method and equipment for removing organic chloride from wastewater Download PDFInfo
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- CN1803662A CN1803662A CN 200610049204 CN200610049204A CN1803662A CN 1803662 A CN1803662 A CN 1803662A CN 200610049204 CN200610049204 CN 200610049204 CN 200610049204 A CN200610049204 A CN 200610049204A CN 1803662 A CN1803662 A CN 1803662A
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Abstract
The invention discloses a method to remove the organic chloride in sewage, which comprises: feeding the sewage circulated and tangential to form swirl flow and raise; translating sewage into rising flow to fluidizing fully the solid reducer or solid particle of supported catalyst in reactor and make them contact with water; reducing the rising flow speed after crossing main reaction zone; changing the rising flow near laminar flow when entering deposition separation area, depositing the reacted reducer or particle to remove the objective material. This invention also provides the opposite device, which fits to high-density metal particle and sewage, and is adjustable and convenient to manage.
Description
Technical field
The present invention relates to water pollution control and treatment technology, be meant a kind of method and apparatus of removing organic chloride in the waste water specifically.
Background technology
Organic chloride, also can be called chloro organic cpd, be the product after one or several hydrogen atoms are replaced by the chlorine atom in aliphatic hydrocarbon, aromatic hydrocarbon and the derivative thereof, it of a great variety comprises chlorine-containing organic compounds such as chlorinated aliphatic hydrocarbon, chlorination aromatic hydrocarbon.Organic chloride is of a great variety, be again important chemical material, intermediate, organic solvent and product, thereby be widely used in industries such as chemical industry, medicine, agricultural chemicals, process hides, machinery, wood preservation, they use by volatilization, container leakage, discharge of wastewater, agricultural chemicals and sterilant and the approach such as burning of chlorinated organics finished product enter environment, become organic chloride and pollute, severe contamination atmosphere, soil, underground water and surface water.In addition, what China extensively adopted is the method for drinking water disinfect with chlorine, also can produce deleterious organic chloride, as chloroform, chloro-alkenes, chloro nitrile, chlorinated phenol, aldehyde ketone muriate etc.
Organic chloride is a pollution substance important in the water, and common organic chloride pollution substance has the organochlorine pesticide of chlorinated aromatic hydrocarbons class in the present water body, as DDT, chlorobenzene etc., and Chemicals such as polychlorobiphenyl, the Dioxins that the chemical burning forms; The chloro fat hydro carbons is as tetracol phenixin, vinylchlorid etc.
Organic chloride pollutent majority is the artificial-synthetic compound, chemical property is relatively stable, has higher octanol/water partition ratio, in organism, soil and sedimental organic matter, accumulate easily, existence of chlorine atom has toxicity to microorganism on it, so in occurring in nature degraded slowly, the environmental hazard cycle is long, reach last 100 years as transformation period of polychlorobiphenyl.In addition, many organic chlorides are considered to have " carcinogenic, teratogenesis shape, mutagenesis " effect; Simultaneously, because a lot of organic chlorides have high volatile volatile and lipoid solubility, easily human body is caused serious harm by absorption such as skin, mucous membrane.
In 129 kinds of environment priority pollutants that the U.S. announced in 1977, it is halohydrocarbon and derivative thereof that kind more than 30 is arranged; On the pollutent Black List that the European Community announces, what rank the first also is halides and the material that can form halides in environment, mainly comprises chlorinated aliphatic hydrocarbon, chlorination aromatic hydrocarbon and derivative thereof.The extensive existence and the hazardness thereof of the pollution of organic chloride have caused national governments, academia, industry member and the public's extensive concern, become a global environmental problem.
At the characteristic of organic chloride pollutent, people have studied the method for multiple processing organo-chlorine pollutant, are broadly divided into physics method, biological process and chemical method.
One, physics method
1, charcoal absorption
Utilize the organic chloride in direct planar water of gac or the waste water, this method is mainly used in the organic chloride of removing in the tap water at present, and there is the secondary pollution problem in its processing cost height.
2, gas (vapour) formulation
This method utilizes some organic chlorides to have high-volatile characteristics, removes organic chloride with the method for gas (or steam) stripping, mainly is applicable to handle the less organic chloride of molecular weight, and it is packing tower that the normal gas (vapour) that adopts is carried device.The air stripping method simple economy, but cause secondary pollution easily.Put forward vapor liquid equilibrium concentration limit under the condition owing to be subjected to gas (vapour), the organochlorine concentration in the water outlet generally can not reach the wastewater discharge standard of national regulation.In the water pollution control of reality, gas (vapour) formulation often is used in combination with absorption method, separates organic chloride to reclaim.
3, extraction process
Organochlorine concentration is higher in waste water, and has when recycle being worth, can consider to reclaim with method of extraction, but inapplicable processing lower concentration organic chloride waste water.
Two, biological process
Found that some microorganisms have stronger degradation capability to organochlorine, laboratory study also shows, biological process is the anaerobic biological process organochlorine of can degrading especially, but in the biological wastewater treatment facility of some long-time running, because the concentration of organic chloride is higher, cause the organic degradation of microbiological degradation, thereby reduce the operating performance of treatment facility.
Three, chemical method
Chemical method is simple usually, and chemical oxidization method and chemical reduction method all have removal effect preferably to the organic chloride in the waste water.
1, burning method
Burning method can produce the incomplete combustion product when handling organic chloride, can produce the material that other thermostabilitys are higher, toxicity is bigger as the burning of tetracol phenixin, as Perchlorobenzene; Polychlorobiphenyl burns then may the bigger material of toxigenicity, as dioxins materials etc.Burning method is used for treatment capacity big, dense organic chloride waste water or waste liquid more.
2, chemical oxidization method
Some chemical oxidization methods can oxidation even the thorough organic pollutant in water of decomposition or the waste water, and the subject matter that exists is that processing cost is than higher at present.For organic chloride, many chlorinated compounds pollutent especially is because of being difficult to effectively handle with chemical oxidization method as electron acceptor(EA); And the degraded product of organic chloride---chlorion at some oxidation systems, as the supercritical oxidation system, has severe corrosive, also makes some senior chemical oxidization methods be restricted.
3, photocatalytic oxidation
It is generally acknowledged that the multiphase photocatalysis oxidation style is used for advanced treatment organic chloride waste water, be considered to one of the most promising method.The multiple organic chloride of this method in can degrading waste water, but employed catalyzer is except TiO
2Outside inexpensive relatively, other catalyzer are comparatively expensive, and have problems such as preparation complexity, recovery and activation difficulty.
4, chemical reduction method
Since the 1980s, a kind of more promising treatment process---zero-valent metal carries out dechlorination to organic chloride to be handled---becomes the research focus, for the organic chloride of removing in the waste water provides new approach.The zero-valent metal reduction method is much more superior than the micro-reduction degraded, when with the vinylchlorid in the micro-reduction degraded anoxic underground water and many vinylchlorid, conversion process is extremely slow, expend time several years sometimes, and the biological degradation of trieline and zellon may cause chlorination degree lower but the gathering of bigger chloro-alkenes (as: vinylchlorid) of toxicity, and the main carbon compound that produces in metal (as: iron) degraded vinylchlorid and the many vinylchlorid process is harmless relatively ethene, and speed of reaction is very fast relatively under conditions suitable.The degradation of organochloride advantage that possesses skills in zero-valent metal---water or the waste water system.
Chemical reduction method comprises monometallic reduction method, two or many metallic reducings method.Monometallic reduction method common metal such as iron, zinc etc., many metallic reducings method system commonly used is Pd-Te system, Pd-Ni system and Pd-Cu system.
Although obtained very promising experimental study effect aspect the organic chloride of chemical reduction method in processing environment water body and waste water, still there are many difficult points and difficulty at present, mainly contain:
(1) the metallic reducing method is handled research seldom at the trade effluent of reality to the dechlorination of organic chloride;
(2) the plant-scale processing research and the engineering construction of organic chloride waste water are few;
When (3) adopting metallic particles to be the metallic particles processing organic chloride waste water of reductive agent or supported catalyst,, can produce phenomenons such as metallic particles caking, precipitation, obstruction, cause treatment effect to reduce even disappearance when being reactor with fixed bed;
(4) when handling organic chloride waste water with agitated bed, owing to causing the solid-liquid two-phase greatly, metallic particles reductive agent density mixes inequality, and effectively the phase boundary contact area is little, and metallic particles easily is deposited in reactor bottom, causes a little less than the technology controlling and process ability.
Therefore, how to solve method and the conversion unit problem that metallic particles reduction handles organic chloride waste water and become this method engineering key in application problem.
Summary of the invention
The invention provides a kind of method of removing organic chloride in the waste water.
The present invention also provides a kind of equipment that is used for removing the waste water organic chloride, and this equipment is fit to high-density metal particle and waste water hybrid reaction, non-scaling, do not stop up, continuously-running, reduction dosage is adjustable, operational administrative is easy.
A kind of method of removing organic chloride in the waste water may further comprise the steps:
(1) make the tangential water inlet of waste water circulation form eddy flow, the scope of fluid reynolds number Re: 25000～50000;
(2) the water inlet eddy flow changes upwelling into, the solid reductant in the abundant fluidized reactor or the solid reductant particle of supported catalyst, make the abundant contact reacts of solid reductant of waste water and solid reductant or supported catalyst, fluid reynolds number Re scope: 1000～25000;
(3) upwelling reduces the upflow velocity of upwelling, the scope of fluid reynolds number Re: 1～1000 gradually by after the main reaction region;
(4) upwelling enters depositing separation area, fluid is approximately laminar flow, the effective sedimentation of solid reductant particle of reacted solid reductant or supported catalyst, in the waste water organic chloride after by separating reaction solid reductant or the solid reductant particle of supported catalyst reach effective removal, the scope of fluid reynolds number Re: 0.1～1.
The solid reductant of described solid reductant or supported catalyst adopts metallic particles or alloying pellet.
A kind of equipment that is used for removing the waste water organic chloride, comprise fluidized-bed, recycle pump and feeding device, described fluidized-bed is provided with fluidized reaction section, divergent segment and precipitating phase from bottom to up successively, and diameter increases successively, and divergent segment connects precipitating phase and fluidized reaction section; The fluidized-bed bottom is provided with water intake and recirculated water tangential water inlet, and fluidized-bed top is provided with and overflows tank and overflow port; Described feeding device comprises the dog-house of being located at the fluidized-bed top and the commissioning pipe that is connected with the dog-house lower end, and insert in the fluidized-bed commissioning pipe lower end; Described recycle pump two ends are communicated with the fluidized-bed bottom and overflow tank.
The precipitating phase of described fluidized-bed is provided with the precipitate and separate member.
Described fluidized-bed bottom is provided with hand hole.
Described precipitate and separate member is spiral swash plate or common swash plate.
Reasonably external water circulation makes waste water from the fluidized-bed bottom cycle formation eddy flow of tangentially intaking, avoided the solid reductant particle of solid reductant or supported catalyst to pile up in device bottom, fouling or obstruction, form the fluidized reaction section at the equipment hypomere, the solid reductant particle of abundant fluidisation high-density solid reductant or supported catalyst) make the solid reductant granular system of waste water and solid reductant or supported catalyst obtain maximum phase boundary contact reacts area, the solid reductant particle that helps organic chloride and solid reductant or supported catalyst forms good mixing, contact and mass transfer reaction, the solid reductant particulate contact reacts of realization waste water and solid reductant or supported catalyst.At divergent segment, the reduce upwelling gradually upflow velocity of---solid metal reductive agent system of waste water and solid metal reductive agent or supported catalyst---, during to settling section, the upwelling flow velocity drops to minimum, the solid reductant particle of solid reductant or supported catalyst sinks, and the precipitate and separate member is set in settling section, make the solid reductant particle of solid reductant or supported catalyst obtain effective sedimentation and realize separation, the solid reductant particle of solid reductant or supported catalyst returns or is retained in the fluidized reaction section or the divergent segment of equipment.
1. waste water forms eddy flow from the tangential water inlet in fluidized-bed bottom, and the solid reductant particulate settling velocity of solid reductant or supported catalyst satisfies:
2. in the fluidized reaction section, fluidised form is for turbulent flow or be called turbulent flow, 1000＜Re＜25000, and the solid reductant particulate sedimentation of solid reductant or supported catalyst meets Newton's formula:
3. at divergent segment, fluidised form is a transition state, 1＜Re＜1000, and the solid reductant particulate sedimentation of solid reductant or supported catalyst meets the A Lan formula:
4. at settling section, fluidised form is a laminar flow, Re＜1, and the solid reductant particulate sedimentation of solid reductant or supported catalyst meets Stokes'formula:
Wherein, the heavy speed of u-particle; R-particle decentering wheelbase from; u
T-particle the flow velocity of tangentially intaking; The d-grain diameter; ρ
p-pellet density; ρ
1-water-mass density; G-universal gravity constant; μ-water power viscosity.
Operational condition of the present invention is:
(1) pressure of operation operation: normal atmosphere; The temperature of operation operation: wastewater temperature is greater than freezing point, less than boiling point.
(2) the solid reductant particle of waste water and solid reductant or supported catalyst, perhaps in same equipment, carry out with the mixing of soluble catalyst, process such as react, separate, but both periodical operation, but also operate continuously, this makes that the design of waste water treatment engineering is relative simple with construction, helps to improve the stability of operation.
(3) adopt waterpower to mix, device interior need not other mechanisms.
(4), be the fluidised form of the solid-liquid system of each section in the controllable device by regulating circulating water flow according to metallic particles rerum natura and device structure parameter.
(5) by device bottom hand hole cleaning solid residue.
(6) by the solid reductant particle of dog-house interpolation solid reductant or supported catalyst, also can add catalyzer in addition if necessary.
(7) water outlet after the processing is got rid of by overflow groove and overflow port.
The present invention has following effect:
(1) is fit to engineering and uses, can avoid the solid reductant particulate of solid reductant or supported catalyst to harden, pile up, stop up;
(2) equipment adopts fluidized-bed, and is the reducing fluidized-bed, and the diameter of fluidized-bed becomes greatly successively from bottom to top, the flow velocity of upwelling from large to small, the fluidized reaction section is the high flow rate turbulent region, obtains good mass transfer effect; Divergent segment is a transition section, and fluidised form is a transition flow regime; The top settling section is provided with the precipitate and separate member, and fluidised form becomes laminar flow at this, helps particles settling;
(3) equipment (reaction) is simple in structure, easy to operate, stable;
(4) the solid reductant particle that has solved high desnity metal solid reductant or supported catalyst and waste water mixing mass transfer are removed the engineering design and construction difficult problem of organic chloride pollutent in the waste water.
Description of drawings
Fig. 1 is the structural representation of equipment of the present invention.
Embodiment
As shown in Figure 1, a kind of equipment that is used for removing the waste water organic chloride comprises fluidized-bed 1, recycle pump 2 and feeding device 3.Fluidized-bed 1 is provided with fluidized reaction section 11, divergent segment 12 and precipitating phase 13 from bottom to up successively, diameter increases successively, divergent segment 12 connects precipitating phase 13 and fluidized reaction section 11, and precipitating phase 13 is provided with precipitate and separate member 4, and precipitate and separate member 4 is spiral swash plate or common swash plate; Fluidized-bed 1 bottom is provided with water intake 15 and circulation tangential water inlet 16, and fluidized-bed 1 top is provided with and overflows tank 5 and overflow port 6, and the bottom is provided with hand hole 14; Fluidized reaction section 11 outer walls of fluidized-bed 1 can be if be provided with vision slit 17; Feeding device 3 comprises the dog-house 31 of being located at fluidized-bed 1 top and the commissioning pipe 32 that is connected with dog-house 31 lower ends, and insert in the fluidized-bed 1 commissioning pipe 32 lower ends; Recycle pump 2 two ends are communicated with fluidized-bed 1 bottom and overflow tank 5.
Waste water enters fluidized-bed 1 from recycle pump 2 by recirculated water tangential water inlet 16, the equipment bottom of making becomes fluidized reaction section 11, the solid reductant particle of solid reductant or supported catalyst is fluidized state, the solid-liquid system upwelling enters divergent segment 12 from fluidized reaction section 11, the upwelling flow velocity reduces gradually in divergent segment 12, the solid reductant particle of solid reductant or supported catalyst sinks gradually, be provided with precipitate and separate member 4 in the settling section 13, can be better the solid reductant particle of solid reductant or supported catalyst is carried out settlement separate, solid returns divergent segment 12 and fluidized reaction section 11; After waste water enters and overflows tank 5,, circulate by overflow pumping hole 21 water inlet of advancing to circulate by recycle pump 2 simultaneously by overflow port 6 water outlets.
The present invention is described in detail below in conjunction with embodiment.
Embodiment 1:
Reductive agent is the pure iron particle, and catalyzer is a soluble sulphate, and granularity 60 orders in order to handle organochlorine waste water, adopt the reducing fluidized-bed, 2.40 meters of fluidized reaction section 11 diameters, 7.8 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 48500; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 24500; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.79.1 ton of waste water of every processing adds 2kg iron powder, 0.2kg catalyzer, and under room temperature and the atmospheric pressure, influent waste water tetracol phenixin concentration is 20mg/L, hydraulic detention time 3h, tetracol phenixin concentration 2mg/L in the treat effluent.
Embodiment 2:
Platinum is catalyzer, loads to reductive agent iron particle surface, and granularity 40 orders in order to handle organochlorine waste water, adopt the reducing fluidized-bed, 1.40 meters of fluidized reaction section 11 diameters, 3.76 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 26500; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 6000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.37.1 ton of waste water of every processing adds the iron powder of 1-2kg supported catalyst platinum, and under room temperature and the atmospheric pressure, influent waste water tetracol phenixin concentration is 10mg/L, hydraulic detention time 2h, tetracol phenixin concentration 1.5mg/L in the treat effluent.
Embodiment 3:
Palladium is a catalyzer, loads to the iron particle surface in order to handle organochlorine waste water, and granularity 30 orders adopt the reducing fluidized-bed, 0.70 meter of fluidized reaction section 11 diameter, 2.5 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 36500; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 21000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.98.1 ton of waste water of every processing adds the iron powder of 0.5-2kg supported catalyst palladium, and under room temperature and the atmospheric pressure, influent waste water vinylchlorid concentration is 30mg/L, hydraulic detention time 2-4h, vinylchlorid concentration 5mg/L in the treat effluent.
Embodiment 4:
In order to handle organochlorine waste water, granularity 80 orders adopt the reducing fluidized-bed, 0.40 meter of fluidized reaction section 11 diameter, 1.5 meters of settling section 13 diameters to Ni to the iron powder surface.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 27500; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 20000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.7.1 ton of waste water of every processing adds the iron particle of 0.5-3kg supported catalyst nickel, and under room temperature and the atmospheric pressure, influent waste water chloroform concentration is 50mg/L, hydraulic detention time 2-6h, chloroform 7.5mg/L in the treat effluent.
Embodiment 5:
Platinum loads to the iron powder surface in order to handle organochlorine waste water, and granularity 100 orders adopt the reducing fluidized-bed, 0.50 meter of fluidized reaction section 11 diameter, 1.8 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 26000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 21000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.8.1 ton of waste water of every processing adds the iron powder of 0.5-2.5kg load platinum, and under room temperature and the atmospheric pressure, influent waste water polychlorobiphenyl concentration is 12mg/L, hydraulic detention time 4h, polychlorobiphenyl 1.8mg/L in the treat effluent.
Embodiment 6:
Copper-iron alloy powder (particle) is used in order to handle organochlorine waste water, and powder size 120 orders adopt the reducing fluidized-bed, 0.60 meter of fluidized reaction section 11 diameter, 1.84 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 26500; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 18000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.66.1 ton of waste water of every processing adds 1-2kg copper-iron alloy powder, and under room temperature and the atmospheric pressure, influent waste water ethylene dichloride concentration is 22mg/L, hydraulic detention time 3-4h, ethylene dichloride 3.4mg/L in the treat effluent.
Embodiment 7:
Aluminium powder is in order to handle organochlorine waste water, and grain graininess 80 orders adopt the reducing fluidized-bed, 0.55 meter of fluidized reaction section 11 diameter, 1.92 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 32000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 21000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.75.1 ton of waste water of every processing adds the 1.2-2.0kg aluminium powder, and under room temperature and the atmospheric pressure, influent waste water tetracol phenixin concentration is 8mg/L, hydraulic detention time 3h, tetracol phenixin concentration 1.1mg/L in the treat effluent.
Embodiment 8:
Zinc powder is in order to handle organochlorine waste water, and grain graininess 140 orders adopt the reducing fluidized-bed, 0.40 meter of fluidized reaction section 11 diameter, 1.6 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 25600; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 12000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.45.1 ton of waste water of every processing adds the 1.5-3.0kg aluminium powder, and under room temperature and the atmospheric pressure, influent waste water Pentachlorophenol concentration is 28mg/L, hydraulic detention time 4h, and Pentachlorophenol concentration is 2.1mg/L in the treat effluent.
Embodiment 9:
Palladium loads to the zinc powder surface in order to handle organochlorine waste water, powder size 120 orders, 1.75 meters of fluidized reaction section 11 diameters, 2.55 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 28500; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 9000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.36.1 ton of waste water of every processing adds the 0.6-1.5kg palladium and loads to zinc powder, and under room temperature and the atmospheric pressure, influent waste water trieline concentration is 7mg/L, hydraulic detention time 2-4h, and trieline concentration is 0.5mg/L in the treat effluent.
Embodiment 10:
In order to handle organochlorine waste water, powder size 160 orders adopt the reducing fluidized-bed, 3.00 meters of fluidized reaction section 11 diameters, 11.42 meters of settling section 13 diameters to Ni to the zinc powder surface.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 27000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 7000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.24.1 ton of waste water of every processing adds the 1.5-2.0kg Ni to zinc powder, and under room temperature and the atmospheric pressure, the influent waste water tce concentration is 5mg/L, hydraulic detention time 2-4h, and tce concentration is 0.3mg/L in the treat effluent.
Embodiment 11:
The Mg-Fe alloy powder is used in order to handle organochlorine waste water, and grain graininess 100 orders adopt the reducing fluidized-bed, 1.40 meters of fluidized reaction section 11 diameters, 4.5 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 32000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 20000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.62.1 ton of waste water of every processing adds 1.2.0-2.0kg Mg-Fe alloy powder, and under room temperature and the atmospheric pressure, the influent waste water tce concentration is 12mg/L, hydraulic detention time 4h, and tce concentration is 1.8mg/L in the treat effluent.
Embodiment 12:
The zinc-iron alloy particle is used in order to handle organochlorine waste water, and grain graininess 80 orders adopt the reducing fluidized-bed, 0.3 meter of fluidized reaction section 11 diameter, 1.45 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 40000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 24000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.80.1 ton of waste water of every processing adds 1.0-2.0kg zinc-iron alloy particle, and under room temperature and the atmospheric pressure, influent waste water chlorobenzene concentration is 5.2mg/L, hydraulic detention time 4h, and chlorobenzene concentration is 1.0mg/L in the treat effluent.
Embodiment 13:
The Al-Mg-Fe alloy particle is used in order to handle organochlorine waste water, and grain graininess 35 orders adopt the reducing fluidized-bed, 0.40 meter of fluidized reaction section 11 diameter, 1.75 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 45000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 23000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.20.1 ton of waste water of every processing adds 0.5-1.5kg Al-Mg-Fe alloy particle, under room temperature and the atmospheric pressure, and influent waste water 2,4-two chlorophenol concentration are 4.2mg/L, hydraulic detention time 4h, in the treat effluent 2,4-two chlorophenol concentration are 0.45mg/L.
Embodiment 14:
Magnalium zinc-iron alloy particle is used in order to handle organochlorine waste water, and grain graininess 70 orders adopt the reducing fluidized-bed, 1.0 meters of fluidized reaction section 11 diameters, 4.5 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 50000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 24000; Settling section 13 is provided with precipitate and separate member swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.7.1 ton of waste water of every processing adds 0.75-1.5kg magnalium zinc-iron alloy particle, and under room temperature and the atmospheric pressure, influent waste water orthodichlorobenzene concentration is 7.2mg/L, hydraulic detention time 3-5h, and orthodichlorobenzene concentration is 0.6mg/L in the treat effluent.
Embodiment 15:
The cast iron powder particle is used in order to handle organochlorine waste water, and grain graininess 70-80 order drops into solubility sulphite catalyzer, adopts the reducing fluidized-bed, 0.80 meter of fluidized reaction section 11 diameter, 2.25 meters of settling section 13 diameters.The device bottom water inlet that tangentially circulates forms eddy flow, and the fluid reynolds number Re is 28000; Fluidized reaction section 11 forms turbulent flow, and the fluid reynolds number Re is 24000; Settling section 13 is provided with precipitate and separate member spiral swash plate, and fluid is approximate laminar flow, and the fluid reynolds number Re is 0.50.1 ton of waste water of every processing adds the 1.8-3.0kg cast particle, and under room temperature and the atmospheric pressure, influent waste water tetracol phenixin concentration is 18mg/L, hydraulic detention time 3-5h, and tetracol phenixin concentration is 2.2mg/L in the treat effluent.
Claims (6)
1. method of removing organic chloride in the waste water may further comprise the steps:
(1) make the tangential water inlet of waste water circulation form eddy flow, the scope of fluid reynolds number Re: 25000～50000;
(2) the water inlet eddy flow changes upwelling into, the solid reductant in the abundant fluidized reactor or the solid reductant particle of supported catalyst, make the abundant contact reacts of solid reductant of waste water and solid reductant or supported catalyst, fluid reynolds number Re scope: 1000～25000;
(3) upwelling reduces the upflow velocity of upwelling, the scope of fluid reynolds number Re: 1～100 gradually by after the main reaction region;
(4) upwelling enters depositing separation area, fluid is approximately laminar flow, the effective sedimentation of solid reductant particle of reacted solid reductant or supported catalyst, in the waste water organic chloride after by separating reaction solid reductant or the solid reductant particle of supported catalyst reach effective removal, the scope of fluid reynolds number Re: 0.1～1.
2. the method for claim 1 is characterized in that: the solid reductant employing metallic particles or the alloying pellet of described solid reductant or supported catalyst.
3. equipment that is used for removing the waste water organic chloride, comprise fluidized-bed (1), recycle pump (2) and feeding device (3), it is characterized in that: described fluidized-bed (1) is provided with fluidized reaction section (11), divergent segment (12) and precipitating phase (13) from bottom to up successively, diameter increases successively, and divergent segment (12) connects precipitating phase (13) and fluidized reaction section (11); Fluidized-bed (1) bottom is provided with water intake (15) and recirculated water tangential water inlet (16), and fluidized-bed (1) top is provided with and overflows tank (5) and overflow port (6); Described feeding device (3) comprises the dog-house (31) of being located at fluidized-bed (1) top and the commissioning pipe (32) that is connected with dog-house (31) lower end, and insert in the fluidized-bed (1) commissioning pipe (32) lower end; Described recycle pump (2) two ends are communicated with fluidized-bed (1) bottom and overflow tank (5).
4. equipment as claimed in claim 3 is characterized in that: the precipitating phase (13) of described fluidized-bed (1) is provided with precipitate and separate member (4).
5. equipment as claimed in claim 3 is characterized in that: described fluidized-bed (1) bottom is provided with hand hole (14).
6. equipment as claimed in claim 4 is characterized in that: described precipitate and separate member (4) is spiral swash plate or common swash plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200610049204XA CN100429158C (en) | 2006-01-23 | 2006-01-23 | Method and equipment for removing organic chloride from wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200610049204XA CN100429158C (en) | 2006-01-23 | 2006-01-23 | Method and equipment for removing organic chloride from wastewater |
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| Publication Number | Publication Date |
|---|---|
| CN1803662A true CN1803662A (en) | 2006-07-19 |
| CN100429158C CN100429158C (en) | 2008-10-29 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200610049204XA Expired - Fee Related CN100429158C (en) | 2006-01-23 | 2006-01-23 | Method and equipment for removing organic chloride from wastewater |
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| Country | Link |
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| CN (1) | CN100429158C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103112938A (en) * | 2013-01-29 | 2013-05-22 | 华南理工大学 | Vermiculite-loaded nano-palladium-iron repair material as well as preparation method and application thereof |
| CN105152256A (en) * | 2015-10-14 | 2015-12-16 | 山东省城市供排水水质监测中心 | Fixed filler bed aeration stripping system used for removing groundwater carbon tetrachloride and method for removing groundwater carbon tetrachloride by using fixed filler bed aeration stripping system |
| CN111875044A (en) * | 2020-07-29 | 2020-11-03 | 南京大学 | Jet-swirling biological fluidized bed reactor and operation method thereof |
| CN112154123A (en) * | 2018-05-22 | 2020-12-29 | 威立雅水务解决方案与技术支持公司 | Method for treating a fluid by means of an ascending flow through a bed of adsorptive media and corresponding device |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01151992A (en) * | 1987-12-10 | 1989-06-14 | Tokyo Metropolis | Biological process for treating waste water |
| CN1242939C (en) * | 2003-08-15 | 2006-02-22 | 浙江大学 | Process for treating chloroform and carbon tetrachloride industrial waste water by catalytic metal reduction-flocculating settling method |
-
2006
- 2006-01-23 CN CNB200610049204XA patent/CN100429158C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103112938A (en) * | 2013-01-29 | 2013-05-22 | 华南理工大学 | Vermiculite-loaded nano-palladium-iron repair material as well as preparation method and application thereof |
| CN103112938B (en) * | 2013-01-29 | 2014-05-07 | 华南理工大学 | Vermiculite-loaded nano-palladium-iron repair material as well as preparation method and application thereof |
| CN105152256A (en) * | 2015-10-14 | 2015-12-16 | 山东省城市供排水水质监测中心 | Fixed filler bed aeration stripping system used for removing groundwater carbon tetrachloride and method for removing groundwater carbon tetrachloride by using fixed filler bed aeration stripping system |
| CN112154123A (en) * | 2018-05-22 | 2020-12-29 | 威立雅水务解决方案与技术支持公司 | Method for treating a fluid by means of an ascending flow through a bed of adsorptive media and corresponding device |
| US11945733B2 (en) | 2018-05-22 | 2024-04-02 | Veolia Water Solutions & Technologies Support | Method for treating a fluid by upflow through a bed of adsorbent media |
| CN111875044A (en) * | 2020-07-29 | 2020-11-03 | 南京大学 | Jet-swirling biological fluidized bed reactor and operation method thereof |
| CN111875044B (en) * | 2020-07-29 | 2022-08-09 | 南京大学 | Jet-swirling biological fluidized bed reactor and operation method thereof |
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| Publication number | Publication date |
|---|---|
| CN100429158C (en) | 2008-10-29 |
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