CN105080935B - A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system - Google Patents
A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system Download PDFInfo
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Abstract
System is utilized the present invention relates to a kind of garbage flying ash cement kiln synergic processing and recycling of water resource, the washing water of incineration of refuse flyash tertiary effluent elution salt system output goes removing heavy metals system into coagulating sedimentation；Coagulating sedimentation goes the saliferous rate that removing heavy metals system is obtained to enter sodium filter and counter-infiltration preconcentration technique for 1 2% solution；Sodium filters the calcium ions and magnesium ions removed with counter-infiltration preconcentration technique in washing water, by saliferous rate for 1 2% solution be concentrated into 6% 8% dope, 6% 8% dope, which is conveyed into membrane distillation concentration system, which carries out circulation output distilled water, is used for membrane module backwash and incineration of refuse flyash washing moisturizing；The saliferous rate of membrane distillation concentration system output enters for 20% 30% nearly saturated solutions goes denier carnallite system to remove carnallite, and last nearly saturated solution is evaporated crystallization into MVR evaporation and crystallization systems.The present invention is a kind of device that cement kiln synergic processing is carried out to incineration of refuse flyash, and recycling can be achieved.
Description
Technical field：
Field, more particularly to a kind of garbage flying ash cement kiln synergic processing are disposed the present invention relates to garbage flying ash
And recycling of water resource utilizes system.
Background technology：
With the development of the social economy, Process of Urbanization is aggravated, many big and medium-sized cities of China meet with the tired of " garbage-surrounded city "
Disturb.Garbage disposal has 3 kinds of modes：Landfill, burn and compost, the garbage disposal of current China use based on landfill, compost with
Measure supplemented by burning, this will take substantial amounts of land resource.With the continuous improvement that the rising of land price, urban environment are required,
Garbage loading embeading becomes no longer economic and safety, and increasing city starts to consider incineration treatment of garbage.Burning disposal can make
The volume of municipal refuse reduces 80-90%, and its waste residue produced can make recycling.
Flying dust is the residue of waste incineration, the carcinogenic substance " bioxin that waste incineration is produced " 90% all in flying dust.Not
The flying dust of cured processing is dealt with improperly, wherein substantial amounts of heavy metal is Ji bioxin can cause serious contamination accident, harm is occupied
People's health.Before, the whole nation only has several cities and is carrying out incineration of refuse flyash processing.One side flying dust processing cost is very high.
On the other hand due to irregular marketing, not in place, the problem of there is harmful competition is supervised, " flying dust " is in " disorderly flying " state.
Flying dust can not obtain safe disposal, will be environmentally hazardous very big hidden danger.
Because flying dust contains substantial amounts of chlorion, chlorion production normal to cement kiln produces very big influence, mainly
Cement kiln skinning is shown, serious meeting produces quality accident, so, the key of cement kiln disposal flying dust is removed in flying dust
A large amount of chlorions, water wash system is the main method for removing chlorion in flying dust.
The content of the invention：
The purpose of the present invention be in view of the deficiencies of the prior art there is provided a kind of garbage flying ash cement kiln synergic processing and
Recycling of water resource utilizes system, realizes the innoxious and recycling treatment of flying dust, and flying ash can meet former used in manufacture of cement
Material standard, and water resource can realize recycling.
The technology solution of the present invention is as follows：
A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, and it includes the waste incineration being sequentially connected
Flying dust tertiary effluent elution salt system, coagulating sedimentation remove removing heavy metals system, sodium filter and counter-infiltration preconcentration technique, membrane distillation concentration
System, go denier carnallite system and MVR evaporation and crystallization systems；The incineration of refuse flyash tertiary effluent elution salt system output
Washing water goes removing heavy metals system by pipeline into coagulating sedimentation；The saliferous rate that coagulating sedimentation goes removing heavy metals system to obtain is
1-2% solution enters sodium filter and counter-infiltration preconcentration technique；The sodium filter and counter-infiltration preconcentration technique are removed in washing water
Calcium ions and magnesium ions, saliferous rate is concentrated into 6%-8% dope for 1-2% solution, 6%-8% dope is conveyed into membrane distillation
Concentration systems, which carry out circulation output distilled water, is used for membrane module backwash and incineration of refuse flyash washing moisturizing；The membrane distillation concentration
The saliferous rate of system output enters for the nearly saturated solutions of 20%-30% goes denier carnallite system to remove carnallite, last nearly saturation
Liquid is evaporated crystallization into MVR evaporation and crystallization systems.
Preferably, the incineration of refuse flyash tertiary effluent elutes salt system, it includes flying dust storage, the flying dust storage
Lower end be communicated with conveying worm a, the conveying worm a outlet be connected to the first order washing desalter, the first order
Washing desalter includes agitator tank a；Water inlet pipe a and chemical feed pipe a have been respectively communicated with the agitator tank a；In the agitator tank a
Flying dust, water with medicinal liquid agitating into mud, the mud that agitator tank a lower end is connected in slush pump a, agitator tank a passes through mud
The mud that pump a is conveyed into buffer tank a, buffer tank a is conveyed into horizontal centrifuge a by slush pump b and is dehydrated；It is described horizontal
Centrifuge a isolates mud the flying dust of chloro ion-containing solution and aqueous Ji bioxin, and chloro ion-containing solution enters coagulating sedimentation
Removing heavy metals system is gone, aqueous and bioxin flying dust enters the second level and washes desalter；The second level washing desalination dress
The flying dust that mud is isolated to chloro ion-containing solution and secondary aqueous Ji bioxin is put, chloro ion-containing solution is gone into coagulating sedimentation
Removing heavy metals system, secondary aqueous and bioxin flying dust enters the third level and washes desalter；The third level washes desalter
Chloro ion-containing solution and three aqueous and bioxin flying dusts are isolated, chloro ion-containing solution removes removing heavy metals into coagulating sedimentation
System, the flying dust of three aqueous Ji bioxin enters cement kiln, and flying dust becomes cement raw material after cement kiln is burned.
Preferably, the charging aperture of the horizontal centrifuge a is connected to slush pump b discharging opening；The horizontal centrifuge a
Slag notch be connected to conveying worm b, horizontal centrifuge a liquid outlet is connected to coagulating sedimentation by drain pipe road and removes weight
Metal system；The conveying worm b is provided with two discharging openings；The second level washing desalter includes agitator tank b, each
The slurries that conveying worm b discharging opening is connected in agitator tank a b, each agitator tank b send into buffer tank b through slush pump c,
Slurry in buffer tank b is dehydrated through slush pump d feedings horizontal centrifuge b；The slag notch of the horizontal centrifuge b is connected to
Conveying worm c, horizontal centrifuge b liquid outlet are connected to coagulative precipitation tank by drain pipe road；The conveying worm c is set
There are two discharging openings；Third level washing desalter includes agitator tank c, and each conveying worm c discharging opening is connected to one
Slurries in agitator tank c, each agitator tank c are sent into through the slush pump e slurries sent into buffer tank c, buffer tank c through slush pump f
Horizontal centrifuge c is dehydrated, and the charging aperture of the horizontal centrifuge c is connected to slush pump f discharging opening；The horizontal centrifugal
Machine c slag notch is connected to cement kiln.
Preferably, be connected on each agitator tank b on water inlet pipe b, each agitator tank c be connected into
Water pipe c, the water inlet pipe a, water inlet pipe b and water inlet pipe c are connected with inlet water tank respectively；Connect respectively on each agitator tank b
It is connected on chemical feed pipe b, each agitator tank c and is connected to chemical feed pipe c, the chemical feed pipe a, chemical feed pipe b and chemical feed pipe c connects respectively
It is connected on chemicals dosing plant；The liquid outlet parallel connection of the chemicals dosing plant has three groups of automatic control flow devices, and three groups control automatically
Flow apparatus processed controls the flow in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, and can send alarm when dose is not enough carries
Show.
Preferably, the coagulating sedimentation goes removing heavy metals system to include coagulative precipitation tank, a left side for the coagulative precipitation tank
End is connected to be communicated with liquid-feeding tube and chemical feed pipe on two agitator tank d, and each agitator tank d by delivery pump a；The chemical feed pipe
Upper be connected with by dosing pump on chemicals dosing plant, and chemicals dosing plant is connected with water pipe；The coagulative precipitation tank bottom be connected with from
Heart dewaterer, coagulative precipitation tank top is connected with buffer pool, and buffer pool is connected to delivery pump b, and delivery pump b is connected to composite bag type
Filter, and composite bag type filter lower end is connected to centrifugal dehydrator；The heavy metal precipitation thing of coagulative precipitation tank bottom is transported
Enter centrifugal dehydrator to be dehydrated, the liquid that the clear liquid on coagulative precipitation tank top is conveyed into buffer pool, buffer pool passes through conveying
Pump b is conveyed into composite bag type filter, and the heavy metal not precipitated completely and contaminant filter are fallen, obtained by composite bag type filter
Heavy metal and impurity transport into centrifugal dehydrator and are dehydrated, and obtained saliferous rate enters membrane distillation concentration for 8-15% solution
Device carries out desalting processing.
Preferably, being provided with the dosing valve of control dosing flow on the chemical feed pipe；It is provided with and adds on the liquid-feeding tube
Water valve.
Preferably, the sodium filter and counter-infiltration preconcentration technique, which include sodium, filters component, the sodium is filtered to be communicated with component
Water pipe a is connected with chemicals dosing plant a, and chemicals dosing plant a；The water inlet end of the sodium filter component is connected to filter a, sodium filter component
The condensed water of output is connected to intermediate water tank by pipeline, and the fresh water of sodium filter component output is connected to reverse osmosis water by pipeline
Case；The bottom of the intermediate water tank is connected to feeding engine a, and feeding engine a water side is connected to filter b, filter b outlet
End is connected to counter-infiltration pre-concentration device；It is communicated with the counter-infiltration pre-concentration device on chemicals dosing plant b, and chemicals dosing plant b
It is connected with water pipe b；The condensed water of the counter-infiltration pre-concentration device output is connected in membrane distillation system by water pipe, counter-infiltration
The fresh water of pre-concentration device output is connected in counter-infiltration water tank by water pipe.
Preferably, the membrane distillation concentration system includes heating water tank, the heating water tank is connected with positive displacement heat exchange
Device, the upper end of heating water tank is communicated with feed tube a, and the lower end of heating water tank is communicated with two groups of working waters by feeding engine side by side
Case；The outlet pipe of operating water tank described in every group by feeding circulating pump simultaneously be connected to distillation device hot water inlet pipe and
Concentrate and be connected with dope evacuated tube and dope return pipe, the heat of the distillation device on water tank, the operating water tank described in every group
Water outlet pipe is connected to dope return pipe；The cold water inlet tube of the distillation device is connected to connect on cooling tower, and cooling tower
CWR is connected to, the cooling water outlet pipe of distillation device is connected to CWR；The distillation device it is cold
Solidifying water pipe is connected to water producing tank；The distillation device top is connected with backwash water feed pipe, and distillation device bottom is connected with
Backwash water evacuated tube and dope evacuated tube a, backwash water feed pipe are connected to backwash water tank by backwashing pump, and backwash water tank with
Backwash water evacuated tube links together, and dope evacuated tube a links together with the dope evacuated tube on operating water tank.
Preferably, described go denier carnallite system to include concentration liquid case, the upper end of the concentration liquid case be communicated with into
Liquid pipe b, the lower end of the concentration liquid case, which is communicated with drain pipe, the drain pipe, is connected with separation feeding engine, separates feeding engine
Discharge nozzle point two-way, per road discharge nozzle on be connected to separation ball valve, for separation ball valve a and separation ball valve b, separate ball valve
A is connected to one-level carnallite release unit, and separation ball valve b is connected to two grades of carnallite release units；The one-level carnallite release unit
Lower end be connected to carnallite collecting pit, the upper end of one-level carnallite release unit is connected to separate ball valve c, and separation ball valve c passes through pipe
Road a is connected to be connected with concentration material returning valve in concentration liquid case, and pipeline a；The upper end of two grades of carnallite release units is connected to
Ball valve d is separated, separation ball valve d is connected on pipeline a and pipeline b, pipeline b be connected with crystallization and evaporation valve, crystallization and evaporation valve simultaneously
It is connected to MVR evaporation and crystallization systems.
Preferably, the MVR evaporation and crystallization systems include feeding engine d, feeding engine d is connected to evaporating chamber, the evaporation
It is communicated with storehouse on heat exchanger, heat exchanger and is connected with vapor recompression pump；The bottom of the evaporating chamber is connected with by discharging pump d
Suction filtration tank, the top of evaporating chamber is connected to Roots's vapor recompression machine by pipeline；Installed in Roots's vapor recompression machine
There is vavuum pump；The vavuum pump is connected to filtrate tank, and filtrate tank is connected with suction filtration tank, and vavuum pump is connected with vapor recompression pump
Together, the mother liquor under vacuum pumping action in filtrate tank is in negative pressure state, and the mother in filtrate tank is stored under suction function
Liquid returns evaporating chamber and continues evaporative crystallization.
The beneficial effects of the present invention are：
The chloro ion-containing solution that the tertiary effluent elution salt system of the present invention is produced enters coagulative precipitation tank, aqueous 40%-
50% and flying dust of the ion containing CL less than 1% enter sludge collecting pit and carry out a huge sum of money in microbial attack bioxin and flying dust
Category, the raw material of construction material can be directly used as by the flying dust of microbial attack bioxin.This microorganism is reusable, i.e., complete
Into flying dust water 1：8 three-level water wash systems.Three-level chemicals dosing plant is same set of chemicals dosing plant, and automatic control flow enters respectively
Row is delivered, and alarm can be sent when dose is not enough.The leaching technology of microorganism applies the direct effect of specific microorganism
Or the indirectly-acting of its metabolin is complexed acidolysis etc. by the huge sum of money in solid phase material under normal temperature and pressure conditionses by redox
Category ion-solubility discharges into the process of liquid phase.
The beam glue reinforcing of the present invention is gone in removing heavy metals system, because incineration of refuse flyash contains many kinds of metal ions, is mixed
The mass ratio that solution is added during solidifying sedimentation basin stirring is the anion active agent of one thousandth to 5/1000ths, promotes a variety of scattered
Form macromolecular to precipitate after Van der Waals force polymerization between metal ion, the overwhelming majority is treated after static half an hour to one hour
After heavy metal ion precipitation, supernatant is taken to enter composite bag type filter by the heavy metal not precipitated completely, contaminant filter falls.It is mixed
Solidifying sedimentation basin precipitation is burned after entering the pre- desiccation of sludge collecting pit progress into cement kiln, so as to solve an incineration of refuse flyash huge sum of money
The pollution of category.Precipitation is filtered out again after anion active agent is added in this system, therefore does not cause the secondary pollution of solution, to follow-up
Membranous system, evaporative crystallization etc., which is not impacted, obtains harmlessness disposing.
In the nanofiltration system of the present invention, in the washing water after being washed because of flying dust, contain substantial amounts of calcium ions and magnesium ions so that concentration
The blocking of follow-up membranous system can be caused afterwards.The separating mechanism of NF membrane is screening and dissolving diffusion and deposits, while having electric charge again
Repelling effect, can effectively remove divalence and multivalent ion, remove all kinds of materials that molecular weight is more than 200, can partly remove
Monovalention and molecular weight are less than 200 material；The separating property of NF membrane is substantially better than ultrafiltration and microfiltration, with nanofiltration first by water
Remaining calcium and magnesium in wash water is removed, and the water of the dilute side of output enters intermediate water tank, can be entered in counter-infiltration preconcentration technique.
It is that one kind isolates solvent from solution using pressure differential as motive force in the counter-infiltration preconcentration technique of the present invention
UF membrane operation because it and naturally osmotic is in opposite direction, therefore claim counter-infiltration.According to the different osmotic of various materials,
The purpose of separation, extraction, purifying and concentration can be reached to use the reverse osmosis pressure more than osmotic pressure, i.e. hyperfiltration.Through
The water for removing hardness is crossed, counter-infiltration can be directly entered, by counter-infiltration pre-concentration, 6%-8% can be concentrated into washing water.Output
Condensed water can enter membrane distillation concentration system, the fresh water of output can enter water wash system water scouring water.
The membrane distillation concentration system of the present invention carries out the chlorion of saliferous rate 6-8% in processing solution using membrane distillation, and
Make the distilled water reusable edible of generation, distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing, substantial amounts of steaming
Distilled water enters water wash system, greatly reduces the consumed water of washing, is that overall washing ratio is reduced to 1：3-1：Between 5.
The present invention's goes denier carnallite system to have removed denier carnallite and carry out the recycling of the energy, due to rubbish
The uncertainty of each supplied materials of flying ash, prevents the blocking of crystallizing evaporator, therefore denier is additionally arranged before evaporative crystallization
Carnallite system.The dope for concentrating water tank enters progress high temperature (temperature after flat ultra micro water filtration film one-level carnallite release unit
Be upgraded to 80-110 DEG C) processing removes the carnallite of high temperature section, after it is further using absorption principle by two grades of carnallite release units
Carnallite is removed, the carnallite filtered out send dangerous waste factory and office to manage, processing cost is very low.
The present invention MVR evaporation and crystallization systems because through membrane distillation system dope be concentrated into nearly saturation state water also compared with
It is small, so from forced-circulation evaporation crystallizer, dope enters evaporating chamber, and heat exchanger is passed through live steam and dope is heated, dense
Steam temperature rise can be gone successively to heat exchanger to dense by two sections of steam of output into Roots's vapor recompression machine in liquid evaporation process
Liquid heating evaporation, without it is lasting supplement original vol saturated vapor, dope be evaporated reaches hypersaturated state separate out crystal, then from
Evaporating chamber is discharged into suction filtration tank and carries out separation of solid and liquid, and mother liquor returns to evaporating chamber and continues evaporative crystallization.Because having removed a large amount of carnallites,
The salt that evaporative crystallization comes out contains sodium chloride and reaches that more than 76% can be used for papermaking, snow melting agent etc., handles this system and utilizes Roots
Steam recompression technology, greatlys save operation energy consumption.
Brief description of the drawings：
The present invention is described further below in conjunction with the accompanying drawings：
Fig. 1 is system flow chart of the invention；
Fig. 2 elutes the flow chart of salt system for the incineration of refuse flyash tertiary effluent of the present invention；
Fig. 3 removes the flow chart of removing heavy metals system for the beam glue reinforcing of the present invention；
Fig. 4 is the nanofiltration system of the present invention and the flow chart of counter-infiltration preconcentration technique；
Fig. 5 is the flow chart of the membrane distillation concentration system of the present invention；
Fig. 6 is the flow chart for going denier carnallite system of the invention；
Fig. 7 is the flow chart of the MVR evaporation and crystallization systems of the present invention.
Embodiment：
Embodiment, is shown in accompanying drawing 1~7, and a kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, and it includes
The incineration of refuse flyash tertiary effluent salt elution system I that is sequentially connected, coagulating sedimentation remove removing heavy metals system II, sodium filter III and reverse osmosis
Saturating preconcentration technique IV, membrane distillation concentration system V, go denier carnallite system VI and MVR evaporation and crystallization systems VII；The rubbish
The washing water of rubbish flying ash tertiary effluent elution salt system output goes removing heavy metals system by pipeline into coagulating sedimentation；Coagulation
Precipitation goes the saliferous rate that removing heavy metals system is obtained to enter sodium filter and counter-infiltration preconcentration technique for 1-2% solution；The sodium
Filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, and saliferous rate is concentrated into 6%-8% for 1-2% solution
Dope, 6%-8% dope, which is conveyed into membrane distillation concentration system, which carries out circulation output distilled water, is used for membrane module backwash and rubbish
Rubbish flying ash washes moisturizing；The saliferous rate of the membrane distillation concentration system output enters for the nearly saturated solutions of 20%-30% goes to pole
Micro carnallite system removes carnallite, and last nearly saturated solution is evaporated crystallization into MVR evaporation and crystallization systems.
It includes flying dust storage 1 to the incineration of refuse flyash tertiary effluent elution salt system, and the lower end of the flying dust storage connects
The outlet for being connected with conveying worm a2, the conveying worm a is connected to first order washing desalter, first order washing desalination
Device includes agitator tank a3；A certain amount of water is added, and the weight ratio of flying dust and water is 1：3, flying dust 1000kg, water 3000kg, institute
State and water inlet pipe a4 and chemical feed pipe a5 have been respectively communicated with agitator tank a；Agitator tank a volume is 1.35m3, agitator tank a power is
Add quality in 2.2kw, and whipping process to be stirred 20 minutes for 1% chaotropic agent of flying dust, flying in the agitator tank a
Ash, water and medicinal liquid agitating are connected to slush pump a6 into mud, agitator tank a lower end, and slush pump a power is 5.5kw, conveying speed
Rate is 0~50m3Mud in/h, agitator tank a is conveyed into buffer tank a7 by slush pump a, and buffer tank a power is 0.75kw,
Buffer tank a volume is 1.35m3；Mud in buffer tank a is conveyed into horizontal centrifuge a9 by slush pump b8 and is dehydrated；
The horizontal centrifuge a isolates mud the flying dust of chloro ion-containing solution and aqueous Ji bioxin, and aqueous Ji bioxin flies
The moisture content of ash is 40%-50%, and chloro ion-containing solution goes removing heavy metals system into coagulating sedimentation, and moisture content is 40%-
50% aqueous and bioxin flying dust enters the second level and washes desalter；The second level washing desalter divides mud
Chloro ion-containing solution and secondary aqueous and bioxin flying dust are separated out, chloro ion-containing solution goes to removing heavy metals system into coagulating sedimentation
System, secondary aqueous and bioxin flying dust enters the third level and washes desalter；Third level washing desalter is isolated chloride
Solion and three aqueous and bioxin flying dusts, chloro ion-containing solution go removing heavy metals system, three times into coagulating sedimentation
The flying dust of aqueous Ji bioxin enters cement kiln, and flying dust becomes cement raw material after cement kiln is burned.
The charging aperture of the horizontal centrifuge a is connected to slush pump b discharging opening；The slag notch of the horizontal centrifuge a
Conveying worm b10 is connected to, horizontal centrifuge a liquid outlet is connected to coagulating sedimentation by drain pipe road 11 and removes removing heavy metals
Washing water in agitator tank d in system, agitator tank d is handled into coagulative precipitation tank 12；The conveying worm b is provided with
Two discharging openings；The second level washing desalter includes agitator tank b13, and aqueous and bioxin flying dust is through conveying worm
B is conveyed into agitator tank b, and using the weight ratio of initial flying dust and water as 1：3 addition water, which are stirred in washing, whipping process, to be added
Quality is stirred 30 minutes for 1% chaotropic agent of initial flying dust；Secondary mud is obtained after stirring fully；Each helical feed
The power that machine b discharging opening is connected to agitator tank a b, each agitator tank b is 2.2KW, and volume is 0.8m3, after stirring fully
The slurries obtained in secondary mud, each agitator tank b send into buffer tank b15 through slush pump c14, and slush pump c power is
5.5kw, transfer rate is 0~50m3/ h, buffer tank b power are 0.75kw, and buffer tank a volume is 1.35m3, buffer tank b
Interior slurry is dehydrated through slush pump d16 feedings horizontal centrifuge b17；Slush pump d power is 1.5kw, and transfer rate is 0
~1.2m3/h。
The slag notch of the horizontal centrifuge b is connected to conveying worm c18, and horizontal centrifuge b liquid outlet is by going out
Liquid pipe road is connected to coagulating sedimentation and goes removing heavy metals system；The conveying worm c is provided with two discharging openings；Third level water elution
The discharging opening that salt device includes agitator tank c19, each conveying worm c is connected in agitator tank a c, each agitator tank c
The slurry that slurries are sent into buffer tank c21, buffer tank c through slush pump e20 is dehydrated through slush pump f feedings horizontal centrifuge c,
The charging aperture of the horizontal centrifuge c is connected to slush pump f22 discharging opening；The slag notch of the horizontal centrifuge c is connected to
Cement kiln, mud is isolated the flying dust of chloro ion-containing solution and secondary aqueous Ji bioxin, and secondary aqueous Ji bioxin flies
The moisture content of ash is 40%-50%, and chloro ion-containing solution enters coagulative precipitation tank, and the flying dust of secondary aqueous Ji bioxin, which enters, to be stirred
Mix tank c.The fly ash carry of secondary aqueous Ji bioxin is to agitator tank c, and using the weight ratio of initial flying dust and water as 1：2 add water
Addition quality in washing, whipping process is stirred to be stirred 20 minutes for 1% chaotropic agent of initial flying dust；Stirring is abundant
After obtain three mud, tri- mud and be dehydrated into horizontal centrifuge c23, horizontal centrifuge c charging aperture is connected to mud
Stock pump f discharging opening；The slag notch of the horizontal centrifuge c is connected to cement kiln 24.Mud is isolated into chloro ion-containing solution
With the flying dust of three aqueous Ji bioxin, the moisture content of the flying dust of three aqueous Ji bioxin is 40%-50%, and chloride ion-containing is molten
Liquid enters coagulative precipitation tank, and the flying dust of flying dust and chloride ion-containing less than 1% of three aqueous Ji bioxin is collected into sludge
Pond carries out the heavy metal in microbial attack bioxin and ash, and building can be directly used as by the flying dust of microbial attack bioxin
The raw material of material, this microorganism is reusable, that is, completes flying dust and water 1：8 three-level water wash system.
It is connected on each agitator tank b on water inlet pipe b, each agitator tank c and is connected to water inlet pipe c, institute
Water inlet pipe a, water inlet pipe b and water inlet pipe c is stated respectively with inlet water tank 25 to be connected；It is connected to and adds on each agitator tank b
Chemical feed pipe c is connected on pencil b, each agitator tank c, the chemical feed pipe a, chemical feed pipe b and chemical feed pipe c, which are connected to, to be added
On medicine device 26；The liquid outlet parallel connection of the chemicals dosing plant has three groups of automatic control flow devices 27, and three groups automatically control
Flow apparatus controls the flow in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, and alarm can be sent when dose is not enough.
The coagulating sedimentation goes removing heavy metals system to include coagulative precipitation tank 12, and the left end of the coagulative precipitation tank passes through defeated
Pump a28 is sent to be connected to be communicated with liquid-feeding tube 30 and chemical feed pipe 31 on two agitator tank d29, and each agitator tank d；Enter at liquid-feeding tube
Enter and anion active agent stirring is added at chloro ion-containing solution after three-level washing, chemical feed pipe, and the quality of anion active agent is accounted for
The 1 ‰ of chloro ion-containing solution quality~5 ‰, make to be formed macromolecular after a variety of dispersed metal ionic polymerizations so as to precipitate, and static 0.5
After~1 hour, precipitate 85~95% heavy metal ion；It is provided with liquid-feeding tube on priming valve 32, chemical feed pipe and control is installed
The dosing valve 33 of dosing flow processed.Chemicals dosing plant 35 is connected with by dosing pump 34 on the chemical feed pipe, the power of dosing pump is
Nearly running water at water pipe 36, water pipe is connected with 0.37KW, and chemicals dosing plant, is easy to be well mixed with decoction；The coagulation sinks
Shallow lake pond bottom is connected with centrifugal dehydrator 37, and coagulative precipitation tank top is connected with buffer pool 38, and buffer pool is connected to delivery pump
B39, delivery pump b are connected to composite bag type filter 40, and composite bag type filter has two, each composite bag type filter top
Provided with inlet, bottom is provided with liquid outlet, and lower end is provided with sewage draining exit, composite bag type filter by the heavy metal not precipitated completely and
Contaminant filter falls, and obtained heavy metal and impurity transports into centrifugal dehydrator by sewage draining exit and be dehydrated, obtained saliferous rate
Next processing system is entered by liquid outlet for 1-2% solution；The clear liquid on coagulative precipitation tank top is conveyed into buffer pool, buffering
Liquid in pond is conveyed into composite bag type filter by delivery pump b, and composite bag type filter is by the heavy metal not precipitated completely
Fall with contaminant filter.
The sodium filter and counter-infiltration preconcentration technique include sodium and filter component 41, and the sodium is filtered and is communicated with chemicals dosing plant on component
Water pipe a is connected with a, and chemicals dosing plant a；Chemicals dosing plant a enters antisludging agent, and the water inlet end of the sodium filter component is connected to filtering
Device a, the condensed water of sodium filter component output is connected to intermediate water tank 42 by pipeline, and the fresh water of sodium filter component output is connected by pipeline
Then counter-infiltration water tank；The bottom of the intermediate water tank is connected to feeding engine a, and feeding engine a water side is connected to filter b,
The filter b port of export is connected to counter-infiltration pre-concentration device 43；Chemicals dosing plant is communicated with the counter-infiltration pre-concentration device
Water pipe b is connected with b, and chemicals dosing plant b；The condensed water of the counter-infiltration pre-concentration device output is connected to film by water pipe and steamed
Evaporate in system, the fresh water of counter-infiltration pre-concentration device output is connected in counter-infiltration water tank by water pipe.The water of intermediate water tank is again
Reverse osmosis membrane assembly 43 is pumped into feeding and carries out counter-infiltration pre-concentration, while being entered in reverse osmosis membrane assembly by chemicals dosing plant c
Enter antisludging agent, water can be concentrated into 6%~8% by reverse osmosis membrane assembly, and reverse osmosis membrane assembly output fresh water enters reverse osmosis produced water
Water in case, reverse osmosis produced water tank can enter incineration of refuse flyash washing moisturizing and use
The membrane distillation concentration system includes heating water tank 44, and the volume of heating water tank is 16m3, the heating water tank company
Volumetric heat exchanger is connected to, the upper end of heating water tank, which is communicated with feed tube a, feed tube a, is provided with charging valve a；Heat water tank
Lower end be communicated with two groups of operating water tanks 45 side by side by feeding engine, the volume of operating water tank is 8m3, the power of feeding engine is
4KW, flow is 80m3Charging valve b is installed on charging line between/h, and heating water tank and operating water tank.
The outlet pipe of operating water tank described in every group is connected to the hot water of distillation device 46 by feeding circulating pump simultaneously
Inlet tube and concentration water tank 47, the volume of concentration water tank is 3m3, distillation ball valve is installed on hot water inlet pipe, concentration water tank
Filtering ball valve is installed, the power of feeding circulating pump is 4KW, and flow is 54m on water inlet pipe3/ h, the operating water tank described in every group
On be connected with dope evacuated tube and dope return pipe.Include 12 groups of membrane modules being connected in parallel in the distillation device, often
One group of membrane module is in series by 4 membrane distillers, and the temperature into the hot water of distillation device is 67 DEG C.Its membrane module is used
A kind of normal pressure anti-soil of Huzhou Sen Nuo membrane technologies Engineering Co., Ltd blocks up energy-saving membrane distiller, Patent No.
201420465882.4。
The hot water outlet pipe of the distillation device is connected to dope return pipe, and the hot water temperature of hot water outlet pipe's outflow is
57 DEG C, the hot water of hot water outlet pipe's outflow returns to operating water tank further through dope return pipe, recycles.
The cold water inlet tube of the distillation device is connected on cooling tower, and cooling tower be connected with CWR,
The cooling water outlet pipe of distillation device is connected to CWR；The cold water temperature that cold water inlet tube enters is 25 DEG C, cold water
The temperature for the water that outlet comes out is 35 DEG C, and the water that cooling water outlet pipe comes out returns to cooling tower further through CWR, cold
But tower is further continued for recycling by 35 DEG C of water cooling to 25 DEG C.
The condensate pipe of the distillation device is connected to water producing tank 48, and the volume of water producing tank is 2m3, the condensation of water producing tank
Water is used for membrane module backwash and incineration of refuse flyash washing moisturizing, and substantial amounts of distilled water recoverable saves water resource.
The distillation device top is connected with backwash water feed pipe, and distillation device bottom is connected with backwash water evacuated tube
With dope evacuated tube a, backwash water feed pipe is connected to backwash water tank 49 by backwashing pump, and the volume of backwash water tank is 3m3, and
Backwash water tank links together with backwash water evacuated tube, and dope evacuated tube a is connected to one with the dope evacuated tube on operating water tank
Rise.
Saliferous rate delivers into heating water tank for 6-8% solution, using volumetric heat exchanger using plant area's waste heat to molten
Liquid is heated, and solution temperature rise is to after 70 °, and solution enters operating water tank；Then solution is circulated into distillation device, solution warp
Cross in membrane module and undergo phase transition, vapor is by the membrane tube in membrane distiller, then passes through the high corrosion-resistant condenser pipe of thermal conductivity factor
Distilled water is condensed into, distilled water enters water producing tank, and distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing；With
The reduction of solution reclaimed water, solution concentration is increasing, and solution concentration is reached after saliferous rate 20%-30% nearly saturation state, molten
Liquid is without circulation, and nearly saturated solution is discharged into operating water tank, and operating water tank is reached at liquid level lower limit position, and self-priming pump startup is by film group
Liquid Residue is all discharged into concentration water tank in part and condensation pipe；Backwash starts after emptying, and membrane module is entered by the distilled water produced
Row backwash, backwash pipeline enters by membrane module is suitable for reading, and from the discharge of lower mouth, the micro crystalline solid adhered in distillation device is washed
Only；In backwash process, heating water tank carries out stopping fluid infusion after fluid infusion is reached at liquid level upper limit position to operating water tank, and backwash terminates
Afterwards, operating water tank carries out next circulation concentration.
The water entrance for going denier carnallite system to include the concentration water tank in concentration liquid case 50, membrane distillation concentration system
Liquid case is concentrated, the upper end of the concentration liquid case is communicated with feed tube b, and the lower end of the concentration liquid case is communicated with drain pipe, described
Be connected with separation feeding engine 51 on drain pipe, the discharge nozzle point two-way of separation feeding engine, per road discharge nozzle on be connected to point
From ball valve, for separation ball valve a52 and separation ball valve b53, separation ball valve a is connected to one-level carnallite release unit 54, separation ball valve b
It is connected to two grades of carnallite release units 55；The lower end of the one-level carnallite release unit is connected to carnallite collecting pit 56, and one-level is miscellaneous
The upper end of salt release unit is connected to separate ball valve c57, and separation ball valve c is connected to concentrate liquid case, and pipeline a58 by pipeline a
On be connected with concentration material returning valve 59；The upper end of two grades of carnallite release units is connected to separate ball valve d60, and separation ball valve d is same
When be connected on pipeline a and pipeline b61, pipeline b be connected with crystallization and evaporation valve 62, crystallization and evaporation valve is connected to MVR evaporative crystallizations
System.
The dope for concentrating water tank is entered after flat ultra micro water filtration film one-level carnallite release unit by separating feeding engine
Heated up, temperature is upgraded to 80-110 DEG C and carries out high temperature circulation processing 5~10 minutes, the carnallite of high temperature section is removed, carnallite sinks
Form sediment and enter carnallite collecting pit, obtained dope returns to concentration water tank by dope material returning valve；Then it will concentrate in water tank through one
The dope that the release unit processing of level carnallite is obtained sends into circular treatment 5~10 minutes in two grades of carnallite release units, utilizes absorption
Principle further removes carnallite, makes to be evaporated crystallization into MVR evaporation and crystallization systems except carnallite dope obtains heat heating.
The MVR evaporation and crystallization systems include feeding engine d63, and feeding engine d is connected to connect on evaporating chamber 64, the evaporating chamber
It is connected with heat exchanger 65, heat exchanger and is connected with vapor recompression pump 66；The bottom of the evaporating chamber is connected with by discharging pump d67
Suction filtration tank 68, the top of evaporating chamber is connected to Roots's vapor recompression machine 69 by pipeline；In Roots's vapor recompression machine
Vavuum pump 70 is installed；The vavuum pump is connected to filtrate tank 71, and filtrate tank is connected with suction filtration tank, and vavuum pump is pressed again with steam
Contracting pump links together, and the mother liquor under vacuum pumping action in filtrate tank is in negative pressure state, and filtrate is stored under suction function
Mother liquor in tank returns evaporating chamber and continues evaporative crystallization.
Evaporating chamber by feeding engine d is initially entered by the dope for going denier carnallite technique to obtain, heat exchanger is passed through newly
Fresh steam is heated to dope, and two sections of steam of output can enter Roots's vapor recompression machine by vapor (steam) temperature in dope evaporation process
Rise goes successively to heat exchanger to dope heating evaporation, without lasting supplement original vol saturated vapor, Roots's vapor recompression machine
The water of generation enters condensation water tank 72.Dope, which is evaporated, reaches that hypersaturated state separates out crystal, then passes through discharging from evaporating chamber
Pump d is discharged into suction filtration tank and carries out being provided with vavuum pump in separation of solid and liquid, Roots's vapor recompression machine, the connection of vavuum pump filtrate tank,
Mother liquor under vacuum pumping action in filtrate tank is in negative pressure state, and the mother liquor being stored under suction function in filtrate tank is returned
Evaporating chamber continue evaporative crystallization, the salt that evaporative crystallization comes out contain sodium chloride reach more than 76% can be used for papermaking, snow melting agent or
Chlor-alkali industry.
Above-described embodiment is the specific descriptions carried out to the present invention, simply the present invention is further described, it is impossible to manage
Solve as limiting the scope of the present invention, it is nonessential that those skilled in the art makes some according to the content of foregoing invention
Modifications and adaptations are each fallen within protection scope of the present invention.
Claims (8)
1. a kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, it is characterised in that：It includes being sequentially connected
Incineration of refuse flyash tertiary effluent elution salt system, coagulating sedimentation go removing heavy metals system, sodium filter and counter-infiltration preconcentration technique,
Membrane distillation concentration system, go denier carnallite system and MVR evaporation and crystallization systems；The incineration of refuse flyash tertiary effluent salt elution
The washing water of system output goes removing heavy metals system by pipeline into coagulating sedimentation；Coagulating sedimentation goes removing heavy metals system to obtain
Saliferous rate for 1-2% solution enter sodium filter and counter-infiltration preconcentration technique；The sodium filter and counter-infiltration preconcentration technique are removed
The calcium ions and magnesium ions gone in washing water, saliferous rate are concentrated into for 1-2% solution 6%-8% dope, and 6%-8% dope is defeated
Send into membrane distillation concentration system and carry out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing；It is described
The saliferous rate of membrane distillation concentration system output enters for the nearly saturated solutions of 20%-30% goes denier carnallite system to remove carnallite,
Last nearly saturated solution is evaporated crystallization into MVR evaporation and crystallization systems；
The membrane distillation concentration system includes heating water tank, and the heating water tank is connected with volumetric heat exchanger, heating water tank
Upper end is communicated with feed tube a, and the lower end of heating water tank is communicated with two groups of operating water tanks by feeding engine side by side；Work described in every group
Make the outlet pipe of water tank by feeding circulating pump while being connected to hot water inlet pipe and the concentration water tank of distillation device, every group of institute
It is connected with dope evacuated tube and dope return pipe on the operating water tank stated, the hot water outlet pipe of the distillation device is connected to dense
Liquid return pipe；The cold water inlet tube of the distillation device is connected on cooling tower, and cooling tower be connected with CWR,
The cooling water outlet pipe of distillation device is connected to CWR；The condensate pipe of the distillation device is connected to produce water
Case；The distillation device top is connected with backwash water feed pipe, and distillation device bottom is connected with backwash water evacuated tube and dense
Liquid evacuated tube a, backwash water feed pipe is connected to backwash water tank by backwashing pump, and backwash water tank is connected with backwash water evacuated tube
Together, dope evacuated tube a links together with the dope evacuated tube on operating water tank；
The MVR evaporation and crystallization systems include feeding engine d, and feeding engine d is connected to be communicated with heat exchange on evaporating chamber, the evaporating chamber
Vapor recompression pump is connected with device, heat exchanger；The bottom of the evaporating chamber is connected with suction filtration tank, evaporating chamber by discharging pump d
Top Roots's vapor recompression machine is connected to by pipeline；Vavuum pump is installed in Roots's vapor recompression machine；It is described
Vavuum pump is connected to filtrate tank, and filtrate tank is connected with suction filtration tank, and vavuum pump links together with vapor recompression pump, in vacuum
Mother liquor under pumping action in filtrate tank is in negative pressure state, and the mother liquor being stored under suction function in filtrate tank returns evaporating chamber
Continue evaporative crystallization.
2. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, its feature
It is：It is stored in a warehouse the incineration of refuse flyash tertiary effluent elution salt system including flying dust, and the lower end of the flying dust storage is communicated with
Conveying worm a, the conveying worm a outlet are connected to first order washing desalter, first order washing desalter
Including agitator tank a；Water inlet pipe a and chemical feed pipe a have been respectively communicated with the agitator tank a；Flying dust, water in the agitator tank a and
Medicinal liquid agitating is into mud, and the mud that agitator tank a lower end is connected in slush pump a, agitator tank a is conveyed into slow by slush pump a
Deposit the mud in tank a, buffer tank a horizontal centrifuge a is conveyed into by slush pump b and be dehydrated；The horizontal centrifuge a is by mud
Slurry isolates chloro ion-containing solution and aqueous and bioxin flying dust, and chloro ion-containing solution goes to removing heavy metals system into coagulating sedimentation
System, aqueous and bioxin flying dust enters the second level and washes desalter；The second level washing desalter separates mud
Go out chloro ion-containing solution and secondary aqueous and bioxin flying dust, chloro ion-containing solution goes to removing heavy metals system into coagulating sedimentation
System, secondary aqueous and bioxin flying dust enters the third level and washes desalter；Third level washing desalter is isolated chloride
Solion and three aqueous and bioxin flying dusts, chloro ion-containing solution go removing heavy metals system, three times into coagulating sedimentation
The flying dust of aqueous Ji bioxin enters cement kiln, and flying dust becomes cement raw material after cement kiln is burned.
3. a kind of garbage flying ash cement kiln synergic processing according to claim 2 and recycling of water resource utilize system, its feature
It is：The charging aperture of the horizontal centrifuge a is connected to slush pump b discharging opening；The slag notch connection of the horizontal centrifuge a
Conveying worm b, horizontal centrifuge a liquid outlet is connected to coagulating sedimentation by drain pipe road and goes removing heavy metals system；Institute
Conveying worm b is stated provided with two discharging openings；The second level washing desalter includes agitator tank b, each conveying worm b
Discharging opening be connected to slurries in agitator tank a b, each agitator tank b and sent into through slush pump c in buffer tank b, buffer tank b
Slurry is dehydrated through slush pump d feedings horizontal centrifuge b；The slag notch of the horizontal centrifuge b is connected to conveying worm
C, horizontal centrifuge b liquid outlet are connected to coagulative precipitation tank by drain pipe road；The conveying worm c is provided with two dischargings
Mouthful；The discharging opening that third level washing desalter includes agitator tank c, each conveying worm c is connected to an agitator tank c, often
The slurry that slurries in individual agitator tank c are sent into buffer tank c, buffer tank c through slush pump e sends into horizontal centrifuge c through slush pump f
It is dehydrated, the charging aperture of the horizontal centrifuge c is connected to slush pump f discharging opening；The slag notch of the horizontal centrifuge c
It is connected to cement kiln.
4. a kind of garbage flying ash cement kiln synergic processing according to claim 3 and recycling of water resource utilize system, its feature
It is：Be connected on each agitator tank b on water inlet pipe b, each agitator tank c and be connected to water inlet pipe c, it is described enter
Water pipe a, water inlet pipe b and water inlet pipe c are connected with inlet water tank respectively；Chemical feed pipe b is connected on each agitator tank b,
Chemical feed pipe c, the chemical feed pipe a, chemical feed pipe b and chemical feed pipe c, which are connected to, on each agitator tank c is connected to chemicals dosing plant
On；The liquid outlet parallel connection of the chemicals dosing plant has three groups of automatic control flow devices, three groups of automatic control flow devices point
Flow that Kong Zhi be in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c, alarm can be sent when dose is not enough.
5. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, its feature
It is：The coagulating sedimentation goes removing heavy metals system to include coagulative precipitation tank, and the left end of the coagulative precipitation tank passes through delivery pump a
It is connected to be communicated with liquid-feeding tube and chemical feed pipe on two agitator tank d, and each agitator tank d；Pass through dosing pump on the chemical feed pipe
It is connected with chemicals dosing plant, and chemicals dosing plant and is connected with water pipe；The coagulative precipitation tank bottom is connected with centrifugal dehydrator, coagulation
Sedimentation basin top is connected with buffer pool, and buffer pool is connected to delivery pump b, and delivery pump b is connected to composite bag type filter, and compound
Bag filter lower end is connected to centrifugal dehydrator；The heavy metal precipitation thing of coagulative precipitation tank bottom transports into centrifugal dehydrator and entered
Row dehydration, the liquid that the clear liquid on coagulative precipitation tank top is conveyed into buffer pool, buffer pool is conveyed into complex pocket by delivery pump b
Formula filter, composite bag type filter falls the heavy metal not precipitated completely and contaminant filter, obtained heavy metal and impurity fortune
Feeding centrifugal dehydrator is dehydrated, and obtained saliferous rate enters membrane distillation concentration device for 8-15% solution and carried out at desalination
Reason.
6. a kind of garbage flying ash cement kiln synergic processing according to claim 5 and recycling of water resource utilize system, its feature
It is：The dosing valve of control dosing flow is installed on the chemical feed pipe；Priming valve is installed on the liquid-feeding tube.
7. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, its feature
It is：The sodium filter and counter-infiltration preconcentration technique include sodium and filter component, and the sodium is filtered and is communicated with chemicals dosing plant a on component, and
Water pipe a is connected with chemicals dosing plant a；The water inlet end of the sodium filter component is connected to filter a, and sodium filters the condensed water of component output
Intermediate water tank is connected to by pipeline, the fresh water of sodium filter component output is connected to counter-infiltration water tank by pipeline；The middle water
The bottom of case is connected to feeding engine a, and feeding engine a water side is connected to filter b, and the filter b port of export is connected to reverse osmosis
Saturating pre-concentration device；It is communicated with the counter-infiltration pre-concentration device on chemicals dosing plant b, and chemicals dosing plant b and is connected with water pipe b；
The condensed water of the counter-infiltration pre-concentration device output is connected in membrane distillation system by water pipe, the production of counter-infiltration pre-concentration device
The fresh water gone out is connected in counter-infiltration water tank by water pipe.
8. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, its feature
It is：Described to go denier carnallite system to include concentration liquid case, the upper end of the concentration liquid case is communicated with feed tube b, described dense
The lower end of contracting liquid case, which is communicated with drain pipe, the drain pipe, is connected with separation feeding engine, and the discharge nozzle of separation feeding engine is divided to two
Separation ball valve is connected on road, every road discharge nozzle, for separation ball valve a and separation ball valve b, separation ball valve a is connected to one-level
Carnallite release unit, separation ball valve b is connected to two grades of carnallite release units；The lower end of the one-level carnallite release unit is connected to
Carnallite collecting pit, the upper end of one-level carnallite release unit is connected to separate ball valve c, and separation ball valve c is connected to concentration by pipeline a
Concentration material returning valve is connected with liquid case, and pipeline a；The upper end of two grades of carnallite release units is connected to separate ball valve d, separation
Ball valve d is connected on pipeline a and pipeline b, pipeline b be connected with crystallization and evaporation valve simultaneously, and crystallization and evaporation valve is connected to MVR evaporation knots
Crystallographic system is united.
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| CN111589837A (en) * | 2020-04-12 | 2020-08-28 | 北京锐上思环保科技有限公司 | Reinforced desalting method for water washing pretreatment of fly ash |
| CN113023989A (en) * | 2021-03-13 | 2021-06-25 | 宝钢湛江钢铁有限公司 | Method for treating silicon-containing sludge by using wastewater zero discharge system |
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Address after: 313000 Huzhou City, Huzhou Province Economic and Technological Development Zone, Hung Fung Road, No. 1366, a layer of the first floor of the 6 Applicant after: Huzhou Sano Environmental Technology Co., Ltd. Address before: 313012 Shuanglin town in Zhejiang province Huzhou city Nanxun District Zhao Dou Cun fish boat horn Applicant before: HUZHOU SENNUO MEMBRANE TECHNOLOGY ENGINEERING CO., LTD. |
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Effective date of registration: 20180524 Address after: 313000 Longquan Bay block, Miao Xi Town, Wuxing District, Huzhou, Zhejiang Patentee after: Zhejiang jinson Regenerative Resources Development Co., Ltd. Address before: 313000 6 floor, 1366 Hongfeng Road, Huzhou economic and Technological Development Zone, Huzhou, Zhejiang. Patentee before: Huzhou Sano Environmental Technology Co., Ltd. |
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Address after: 313000 Longquanwu block, Miaoxi Town, Huzhou City, Zhejiang Province Patentee after: Huzhou Jinglan Environmental Protection Technology Co.,Ltd. Address before: 313000 Longquan Bay block, Miao Xi Town, Wuxing District, Huzhou, Zhejiang Patentee before: Zhejiang jinson Regenerative Resources Development Co.,Ltd. |