CN204912255U - Rubbish flying dust cement kiln is dealt with and water utilization system in coordination - Google Patents
Rubbish flying dust cement kiln is dealt with and water utilization system in coordination Download PDFInfo
- Publication number
- CN204912255U CN204912255U CN201520643657.XU CN201520643657U CN204912255U CN 204912255 U CN204912255 U CN 204912255U CN 201520643657 U CN201520643657 U CN 201520643657U CN 204912255 U CN204912255 U CN 204912255U
- Authority
- CN
- China
- Prior art keywords
- water
- tank
- pipe
- pump
- cement kiln
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 217
- 239000000428 dust Substances 0.000 title claims abstract description 66
- 239000004568 cement Substances 0.000 title claims abstract description 36
- 230000001112 coagulating effect Effects 0.000 claims abstract description 52
- 238000001704 evaporation Methods 0.000 claims abstract description 51
- PALNZFJYSCMLBK-UHFFFAOYSA-K magnesium;potassium;trichloride;hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-].[Cl-].[K+] PALNZFJYSCMLBK-UHFFFAOYSA-K 0.000 claims abstract description 51
- 239000012528 membrane Substances 0.000 claims abstract description 50
- 238000005406 washing Methods 0.000 claims abstract description 49
- 238000004821 distillation Methods 0.000 claims abstract description 46
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 46
- 238000002425 crystallisation Methods 0.000 claims abstract description 35
- 230000008025 crystallization Effects 0.000 claims abstract description 35
- 238000004094 preconcentration Methods 0.000 claims abstract description 31
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 29
- 230000008020 evaporation Effects 0.000 claims abstract description 29
- 239000011734 sodium Substances 0.000 claims abstract description 29
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 29
- 238000004062 sedimentation Methods 0.000 claims abstract description 28
- 239000010881 fly ash Substances 0.000 claims abstract description 25
- 150000003839 salts Chemical class 0.000 claims abstract description 16
- 239000012153 distilled water Substances 0.000 claims abstract description 12
- 230000003020 moisturizing effect Effects 0.000 claims abstract description 8
- 229910001425 magnesium ion Inorganic materials 0.000 claims abstract description 5
- 239000000126 substance Substances 0.000 claims description 65
- 239000000243 solution Substances 0.000 claims description 49
- 238000001764 infiltration Methods 0.000 claims description 37
- 238000000034 method Methods 0.000 claims description 32
- 238000001556 precipitation Methods 0.000 claims description 32
- 239000007788 liquid Substances 0.000 claims description 26
- -1 chloro ion Chemical class 0.000 claims description 25
- 238000007599 discharging Methods 0.000 claims description 24
- 238000012545 processing Methods 0.000 claims description 19
- 238000004064 recycling Methods 0.000 claims description 19
- 239000002956 ash Substances 0.000 claims description 18
- 239000000463 material Substances 0.000 claims description 17
- 239000008236 heating water Substances 0.000 claims description 16
- 239000002131 composite material Substances 0.000 claims description 15
- 239000000706 filtrate Substances 0.000 claims description 15
- 230000002195 synergetic effect Effects 0.000 claims description 15
- 239000012141 concentrate Substances 0.000 claims description 13
- 239000002002 slurry Substances 0.000 claims description 12
- 238000010828 elution Methods 0.000 claims description 11
- 239000002893 slag Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 239000012452 mother liquor Substances 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 239000012530 fluid Substances 0.000 claims description 8
- 239000013505 freshwater Substances 0.000 claims description 8
- 238000000967 suction filtration Methods 0.000 claims description 8
- 239000012047 saturated solution Substances 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 239000000356 contaminant Substances 0.000 claims description 5
- 239000000498 cooling water Substances 0.000 claims description 5
- 230000032258 transport Effects 0.000 claims description 5
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 4
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims description 4
- 229910001424 calcium ion Inorganic materials 0.000 claims description 4
- 230000037452 priming Effects 0.000 claims description 4
- 238000011001 backwashing Methods 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 239000000047 product Substances 0.000 claims description 3
- 238000011033 desalting Methods 0.000 claims description 2
- 238000001223 reverse osmosis Methods 0.000 abstract description 9
- 150000002500 ions Chemical class 0.000 abstract description 7
- 238000004056 waste incineration Methods 0.000 abstract description 5
- ZFXVRMSLJDYJCH-UHFFFAOYSA-N calcium magnesium Chemical compound [Mg].[Ca] ZFXVRMSLJDYJCH-UHFFFAOYSA-N 0.000 abstract description 2
- 239000011555 saturated liquid Substances 0.000 abstract 2
- 239000013078 crystal Substances 0.000 abstract 1
- 238000010612 desalination reaction Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 15
- 238000003756 stirring Methods 0.000 description 10
- 239000003795 chemical substances by application Substances 0.000 description 7
- 241000370738 Chlorion Species 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 239000013543 active substance Substances 0.000 description 4
- 150000001450 anions Chemical class 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 230000000813 microbial effect Effects 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- 230000003196 chaotropic effect Effects 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 230000003204 osmotic effect Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000002361 compost Substances 0.000 description 2
- 239000004035 construction material Substances 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000001802 infusion Methods 0.000 description 2
- 150000002605 large molecules Chemical class 0.000 description 2
- 229920002521 macromolecule Polymers 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 238000005411 Van der Waals force Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 230000000536 complexating effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012690 ionic polymerization Methods 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- DPJRMOMPQZCRJU-UHFFFAOYSA-M thiamine hydrochloride Chemical compound Cl.[Cl-].CC1=C(CCO)SC=[N+]1CC1=CN=C(C)N=C1N DPJRMOMPQZCRJU-UHFFFAOYSA-M 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model relates to a rubbish flying dust cement kiln is dealt with and water utilization system in coordination, the washing water of the tertiary washing desalination system output of waste incineration fly ash gets into coagulating sedimentation and goes to the heavy metal ion removal system, coagulating sedimentation goes that the heavy metal ion removal system obtains contain the salt rate for 1 -2%'s solution get into sodium strain with reverse osmosis pre -concentration system, the calcium magnesium ion of detaching the washing aquatic with reverse osmosis pre -concentration system is strained to sodium, will contain the salt rate and be 1 -2%'s solution concentration to 6% -8%'s dope, and 6% -8%'s dope is carried income membrane distillation concentration system to circulate output distilled water to be used for membrane module backwash and waste incineration fly ash to wash the moisturizing, the salt rate that contains of membrane distillation concentration system output goes to atomic volume carnallite system to get rid of the carnallite for the nearly saturated liquid of 20% -30% gets into, and last nearly saturated liquid gets into MVR evaporation crystal system and evaporates the crystallization. The utility model relates to a cement kiln is carried out to waste incineration fly ash and in coordination with the device of dealing with, utilization can be realized.
Description
Technical field:
The utility model relates to garbage flying ash and disposes field, relates to a kind of garbage flying ash cement kiln synergic processing in particular and recycling of water resource utilizes system.
Background technology:
Along with socioeconomic development, Process of Urbanization is aggravated, and a lot of big and medium-sized cities of China meet with the puzzlement of " garbage-surrounded city ".Garbage disposal has 3 kinds of modes: landfill, burning and compost, and the garbage disposal of current China adopts based on landfill, and compost and burning are auxiliary measure, and this will take a large amount of land resource.Along with the rising of land price, what urban environment required improves constantly, and garbage loading embeading becomes no longer economy and safety, and increasing city starts to consider incineration treatment of garbage.Burning disposal can make the volume of municipal refuse reduce 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 produces " 90% all in flying dust.The flying dust of uncured process is dealt with improperly, and wherein a large amount of heavy metals, Ji bioxin can cause serious contamination accident, endangers residents ' health.Before, the whole nation only has several cities carrying out incineration of refuse flyash process.Flying dust processing cost is very high on the one hand.On the other hand due to irregular marketing, supervise not in place, there is the problem of harmful competition, make " flying dust " be in " disorderly flying " state.Flying dust can not obtain safe disposal, will be environmentally hazardous very big hidden danger.
Because flying dust contains a large amount of chlorions, chlorion is normally produced cement kiln and is produced very large impact, be mainly manifested in cement kiln skinning, serious meeting produces quality accident, so, the key that flying dust disposed by cement kiln removes a large amount of chlorions in flying dust, and water wash system is the main method removing chlorion in flying dust.
Utility model content:
The purpose of this utility model is for the deficiencies in the prior art part, a kind of garbage flying ash cement kiln synergic processing and recycling of water resource is provided to utilize system, achieve the innoxious of flying dust and recycling treatment, flying ash can meet the raw materials used standard of manufacture of cement, and water resource can realize recycling.
Technology solution of the present utility model is as follows:
A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, it comprise connect successively incineration of refuse flyash tertiary effluent salt elution system, coagulating sedimentation removal heavy metal system, sodium filter and counter-infiltration preconcentration technique, membrane distillation concentration system, go denier carnallite system and MVR evaporation and crystallization system; The washing water of described incineration of refuse flyash tertiary effluent salt elution system produce enters coagulating sedimentation removal heavy metal system by pipeline; The saliferous rate that coagulating sedimentation removal heavy metal system obtains is that the solution of 1-2% enters sodium filter and counter-infiltration preconcentration technique; Described sodium filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, be the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into membrane distillation concentration system and carries out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing; The saliferous rate of described membrane distillation concentration system produce is that the nearly saturated solution of 20%-30% enters denier carnallite system and removed by carnallite, and last nearly saturated solution enters MVR evaporation and crystallization system and carries out evaporative crystallization.
As preferably, described incineration of refuse flyash tertiary effluent salt elution system it comprise flying dust storage, the lower end of described flying dust storage is communicated with conveying worm a, and the outlet of described conveying worm is connected to first order washing desalter, and first order washing desalter comprises agitator tank a; Described agitator tank a is communicated with respectively water inlet pipe a and chemical feed pipe a; Flying dust in described agitator tank a, water become mud with medicinal liquid agitating, the lower end of agitator tank a is connected to slush pump a, mud in agitator tank a is conveyed into buffer tank a by slush pump a, and the mud in buffer tank a is conveyed into horizontal centrifuge a by slush pump b and dewaters; Mud is isolated chloro ion-containing solution and flying dust that is moisture and bioxin by described horizontal centrifuge a, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and flying dust that is moisture and bioxin enters second level washing desalter; Chloro ion-containing solution mud isolated by described second level washing desalter and secondary is moisture and the flying dust of bioxin, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and secondary flying dust that is moisture and bioxin enters third level washing desalter; The flying dust of chloro ion-containing solution and three moisture and bioxin isolated by third level washing desalter, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, the flying dust of three moisture Ji bioxin enters cement kiln, and after cement kiln burns, flying dust becomes cement raw material.
As preferably, the charging aperture of described horizontal centrifuge a is connected to the discharging opening of slush pump b; The slag notch of described horizontal centrifuge a is connected to conveying worm b, and the liquid outlet of horizontal centrifuge a is connected to coagulating sedimentation removal heavy metal system by fluid pipeline; Described conveying worm b is provided with two discharging openings; Described second level washing desalter comprises agitator tank b, the discharging opening of each conveying worm b is connected to an agitator tank b, slurries in each agitator tank b send into buffer tank b through slush pump c, and the slurry in buffer tank b is sent into horizontal centrifuge b through slush pump d and dewatered; The slag notch of described horizontal centrifuge b is connected to conveying worm c, and the liquid outlet of horizontal centrifuge b is connected to coagulative precipitation tank by fluid pipeline; Described conveying worm c is provided with two discharging openings; Third level washing desalter comprises agitator tank c, the discharging opening of each conveying worm c is connected to an agitator tank c, slurries in each agitator tank c send into buffer tank c through slush pump e, slurry in buffer tank c is sent into horizontal centrifuge c through slush pump f and is dewatered, and the charging aperture of described horizontal centrifuge c is connected to the discharging opening of slush pump f; The slag notch of described horizontal centrifuge c is connected to cement kiln.
As preferably, described each agitator tank b is connected to water inlet pipe b, each agitator tank c is connected to water inlet pipe c, described water inlet pipe a, water inlet pipe b are connected with inlet water tank respectively with water inlet pipe c; Described each agitator tank b is connected to chemical feed pipe b, each agitator tank c is connected to chemical feed pipe c, described chemical feed pipe a, chemical feed pipe b and chemical feed pipe c are connected on chemicals dosing plant; The liquid outlet parallel join of described chemicals dosing plant has three groups of automatic control flow devices, and three groups of automatic control flow devices control the flow in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, can send alarm when dose is not enough.
As preferably, described coagulating sedimentation removal heavy metal system comprises coagulative precipitation tank, and the left end of described coagulative precipitation tank is connected to two agitator tank d by delivery pump a, and each agitator tank d is communicated with liquid-feeding tube and chemical feed pipe; Described chemical feed pipe is connected with chemicals dosing plant by dosing pump, and chemicals dosing plant is connected with water pipe; Described coagulative precipitation tank bottom is connected with centrifugal dehydrator, and 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 transports into centrifugal dehydrator and dewaters, the clear liquid on coagulative precipitation tank top is conveyed into Buffer Pool, liquid in Buffer Pool is conveyed into composite bag type filter by delivery pump b, the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter, the heavy metal obtained and impurity transport into centrifugal dehydrator and dewater, and the saliferous rate obtained is that the solution of 8-15% enters membrane distillation concentration device and carries out desalting processing.
As preferably, described chemical feed pipe is provided with the dosing valve controlling dosing flow; Described liquid-feeding tube is provided with priming valve.
As preferably, described sodium filter and counter-infiltration preconcentration technique comprise sodium filter assembly, and described sodium is filtered on assembly and is communicated with chemicals dosing plant a, and chemicals dosing plant a is connected with water pipe a; The water inlet end of described sodium filter assembly is connected to filter a, and the condensed water of sodium filter assembly output is connected to intermediate water tank by pipeline, and the fresh water of sodium filter assembly output is connected to counter-infiltration water tank by pipeline; The bottom of described intermediate water tank is connected to feeding engine a, and the water side of feeding engine a is connected to filter b, and the port of export of filter b is connected to counter-infiltration pre-concentration device; Described counter-infiltration pre-concentration device is communicated with chemicals dosing plant b, and chemicals dosing plant b is connected with water pipe b; The condensed water of described counter-infiltration pre-concentration device output is connected in Membrane Materials system by water pipe, and the fresh water of counter-infiltration pre-concentration device output is connected in counter-infiltration water tank by water pipe.
As preferably, described membrane distillation concentration system comprises heating water tank, and described heating water tank is connected with volumetric heat exchanger, and the upper end of heating water tank is communicated with feed tube, and the lower end of heating water tank is communicated with two groups of operating water tanks side by side by feeding engine; The outlet pipe often organizing described operating water tank is connected to the hot water inlet pipe of distillation device and concentrated water tank by feeding circulating pump simultaneously, often organize on described operating water tank and be connected with dope evacuated tube and dope return pipe, the hot water outlet pipe of described distillation device is connected to dope return pipe; The cold water inlet tube of described distillation device is connected to cooling tower, and cooling tower is connected with CWR, and the cooling water outlet pipe of distillation device is connected to CWR; The condensate pipe of described distillation device is connected to product water tank; Described distillation device top is connected with backwash water feed pipe, distillation device bottom is connected with backwash water evacuated tube and dope evacuated tube a, backwash water feed pipe is connected to backwash water tank by backwashing pump, and backwash water tank and backwash water evacuated tube link together, the dope evacuated tube on dope evacuated tube a and operating water tank links together.
As preferably, described denier carnallite system of going comprises concentrate case, the upper end of described concentrate case is communicated with feed tube, the lower end of described concentrate case is communicated with drain pipe, described drain pipe is connected with separation feeding engine, and the discharge nozzle being separated feeding engine divides two-way, every road discharge nozzle is connected to separation ball valve, for being separated ball valve a and being separated ball valve b, be separated ball valve a and be connected to one-level carnallite release unit, be separated ball valve b and be connected to secondary carnallite release unit; The lower end of described one-level carnallite release unit is connected to carnallite collecting pit, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a is connected with concentrated material returning valve; The upper end of described secondary carnallite release unit is connected to and is separated ball valve d, and be separated ball valve d and be connected to pipeline a and pipeline b simultaneously, pipeline b is connected with crystallization and evaporation valve, crystallization and evaporation valve is connected to MVR evaporation and crystallization system.
As preferably, described MVR evaporation and crystallization system comprises feeding engine d, and feeding engine d is connected to evaporating chamber, and described evaporating chamber is communicated with heat exchanger, heat exchanger is connected with steam recompression pump; The bottom of described evaporating chamber is connected with suction filtration tank by discharging pump d, and the top of evaporating chamber is connected to Roots's steam recompression machine by pipeline; In described Roots's steam recompression machine, vavuum pump is installed; Described vavuum pump is connected to filtrate tank, filtrate tank is connected with suction filtration tank, and vavuum pump and steam recompress pump links together, the mother liquor under vavuum pump effect in filtrate tank is negative pressure state, and the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization.
The beneficial effects of the utility model are:
The chloro ion-containing solution that tertiary effluent salt elution system of the present utility model produces enters coagulative precipitation tank, moisture 40%-50% and containing CL ion lower than 1% flying dust enter the heavy metal that mud collecting pit carries out in microbial attack bioxin and flying dust, directly can be used as the raw material of construction material through the flying dust of microbial attack bioxin.This microorganism is reusable, namely completes flying dust water yield 1:8 tertiary effluent and washes system.Three grades of chemicals dosing plants are same set of chemicals dosing plant, and automatic control flow is thrown in respectively, can send alarm when dose is not enough.The leaching technology of microorganism applies the direct effect of specific microorganism or the heavy metal ion in solid phase material is dissolved the process discharging into liquid phase by redox complexing acidolysis etc. by the indirectly-acting of its metabolin under normal temperature and pressure conditions.
In bundle glue strengthening removal heavy metal system of the present utility model, because incineration of refuse flyash contains many kinds of metal ions, coagulative precipitation tank adds solution mass ratio when stirring is the anion active agent of one thousandth to thousand/five, large molecule is formed thus precipitation after impelling the Van der Waals force polymerization between multiple dispersed metal ion, after static half an hour to one hour after most heavy metal ion precipitation, get supernatant and enter the heavy metal that composite bag type filter will not precipitate completely, contaminant filter falls.Coagulative precipitation tank precipitation enter mud collecting pit carry out pre-mummification laggard enter cement kiln burn, thus solve the pollution of incineration of refuse flyash heavy metal.In this system anion active agent after adding again sedimentation and filtration fall, therefore do not cause the secondary pollution of solution, to subsequent film system, evaporative crystallization etc. do not impact and obtain harmlessness disposing.
In nanofiltration system of the present utility model, because of in the washing water after flying dust washing, containing a large amount of calcium ions and magnesium ions, make the blocking that can cause subsequent film system after concentrating.The separating mechanism of NF membrane is for screening and dissolve and spread and deposit, while there is again electrical charge rejection effect, effectively can remove all kinds of materials that divalence and multivalent ion, removal molecular weight are greater than 200, can partly remove monovalention and molecular weight lower than 200 material; The separating property of NF membrane is obviously better than ultrafiltration and micro-filtration, and first removed by the residue calcium magnesium in washing water with nanofiltration, the water of the dilute side of output enters intermediate water tank, can enter in counter-infiltration preconcentration technique.
In counter-infiltration preconcentration technique of the present utility model, being motive force with pressure differential, is a kind of UF membrane operation of isolating solvent from solution, because it is contrary with the direction of naturally osmotic, therefore claims counter-infiltration.According to the different osmotic of various material, just can use the reverse osmosis pressure being greater than osmotic pressure, i.e. hyperfiltration, reach separation, extraction, purifying and concentrated object.Through the water of removing hardness, directly can enter counter-infiltration, by counter-infiltration pre-concentration, 6%-8% can be concentrated into washing water.The condensed water of output can enter membrane distillation concentration system, and the fresh water of output can enter water wash system water scouring water.
Membrane distillation concentration system of the present utility model adopts Membrane Materials to carry out the chlorion of saliferous rate 6-8% in Treatment Solution, and make the distilled water reusable edible of generation, distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing, a large amount of distilled water enters water wash system, reducing the water yield of washing and consuming greatly, is that totally the ratio of washing reduces between 1:3-1:5.
Of the present utility modelly go denier carnallite system can remove denier carnallite and carried out the recycling of the energy, due to the uncertainty of each supplied materials of incineration of refuse flyash, the blocking of the crystallizer that avoids evaporating, therefore set up before evaporative crystallization and go denier carnallite system.Carry out high temperature (temperature is upgraded to 80-110 DEG C) process after the dope of concentrated water tank enters flat ultra micro water filtration film one-level carnallite release unit the carnallite of high temperature section is removed, after utilize absorption principle to be removed by carnallite further through secondary carnallite release unit, the carnallite Song Weifei factory and office reason filtered out, processing cost is very low.
MVR evaporation and crystallization system of the present utility model is also less because being concentrated into the nearly saturation state water yield through Membrane Materials system dope, so select forced-circulation evaporation crystallizer, dope enters evaporating chamber, heat exchanger passes into live steam and heats dope, in dope evaporation process two sections of steam of output can enter Roots's steam recompression machine steam temperature rise is continued enter heat exchanger to dope heating evaporation, original vol saturated vapor is supplemented without the need to continuing, dope carries out evaporation and reaches hypersaturated state crystallize out, then enter suction filtration tank from evaporating chamber discharge and carry out Separation of Solid and Liquid, mother liquor is got back to evaporating chamber and is continued evaporative crystallization.Because removing a large amount of carnallite, evaporative crystallization salt out contains sodium chloride and reaches more than 76% and can be used for papermaking, snow melting agent etc., processes this system and utilizes Roots's steam recompression technology, greatly save operation energy consumption.
Accompanying drawing illustrates:
Below in conjunction with accompanying drawing, the utility model is described further:
Fig. 1 is system flow chart of the present utility model;
Fig. 2 is the flow chart of incineration of refuse flyash tertiary effluent salt elution system of the present utility model;
Fig. 3 is the flow chart of bundle glue of the present utility model strengthening removal heavy metal system;
Fig. 4 is the flow chart of nanofiltration system of the present utility model and counter-infiltration preconcentration technique;
Fig. 5 is the flow chart of membrane distillation concentration system of the present utility model;
Fig. 6 is the flow chart going denier carnallite system of the present utility model;
Fig. 7 is the flow chart of MVR evaporation and crystallization system of the present utility model.
Detailed description of the invention:
Embodiment, see accompanying drawing 1 ~ 7, a kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system, it comprise connect successively incineration of refuse flyash tertiary effluent salt elution system I, coagulating sedimentation removal heavy metal system II, sodium filter III and counter-infiltration preconcentration technique IV, membrane distillation concentration system V, go denier carnallite system VI and MVR evaporation and crystallization system VII; The washing water of described incineration of refuse flyash tertiary effluent salt elution system produce enters coagulating sedimentation removal heavy metal system by pipeline; The saliferous rate that coagulating sedimentation removal heavy metal system obtains is that the solution of 1-2% enters sodium filter and counter-infiltration preconcentration technique; Described sodium filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, be the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into membrane distillation concentration system and carries out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing; The saliferous rate of described membrane distillation concentration system produce is that the nearly saturated solution of 20%-30% enters denier carnallite system and removed by carnallite, and last nearly saturated solution enters MVR evaporation and crystallization system and carries out evaporative crystallization.
Described incineration of refuse flyash tertiary effluent salt elution system it comprise flying dust storage 1, the lower end of described flying dust storage is communicated with conveying worm a2, the outlet of described conveying worm is connected to first order washing desalter, and first order washing desalter comprises agitator tank a3; Add certain water gaging, and the weight ratio of flying dust and water is 1:3, flying dust 1000kg, water 3000kg, described agitator tank a is communicated with respectively water inlet pipe a4 and chemical feed pipe a5; The volume of agitator tank a is 1.35m
3the power of agitator tank a is 2.2kw, and to add quality in whipping process be that the chaotropic agent of 1% of flying dust carries out stirring 20 minutes, flying dust in described agitator tank a, water become mud with medicinal liquid agitating, the lower end of agitator tank a is connected to slush pump a6, the power of slush pump a is 5.5kw, and transfer rate is 0 ~ 50m
3/ h, the mud in agitator tank a is conveyed into buffer tank a7 by slush pump a, and the power of buffer tank a is 0.75kw, and the volume of buffer tank a is 1.35m
3; Mud in buffer tank a is conveyed into horizontal centrifuge a9 by slush pump b8 and dewaters; Mud is isolated the flying dust of chloro ion-containing solution and moisture Ji bioxin by described horizontal centrifuge a, the moisture content of the flying dust of moisture Ji bioxin is 40%-50%, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and moisture content is that the flying dust of the moisture of 40%-50% and bioxin enters second level washing desalter; Chloro ion-containing solution mud isolated by described second level washing desalter and secondary is moisture and the flying dust of bioxin, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and secondary flying dust that is moisture and bioxin enters third level washing desalter; The flying dust of chloro ion-containing solution and three moisture and bioxin isolated by third level washing desalter, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, the flying dust of three moisture Ji bioxin enters cement kiln, and after cement kiln burns, flying dust becomes cement raw material.
The charging aperture of described horizontal centrifuge a is connected to the discharging opening of slush pump b; The slag notch of described horizontal centrifuge a is connected to conveying worm b10, and the liquid outlet of horizontal centrifuge a is connected to the agitator tank d in coagulating sedimentation removal heavy metal system by fluid pipeline 11, the washing water in agitator tank d enters coagulative precipitation tank 12 and processes; Described conveying worm b is provided with two discharging openings; Described second level washing desalter comprises agitator tank b13, the flying dust of moisture Ji bioxin is conveyed into agitator tank b through conveying worm b, and carrying out stirring washing with the weight ratio of initial flying dust and water for 1:3 adds water, adding quality in whipping process is that the chaotropic agent of 1% of initial flying dust carries out stirring 30 minutes; Stir fully and obtain secondary mud; The discharging opening of each conveying worm b is connected to an agitator tank b, and the power of each agitator tank b is 2.2KW, and volume is 0.8m
3, stir fully and obtain secondary mud, the slurries in each agitator tank b send into buffer tank b15 through slush pump c14, and the power of slush pump c is 5.5kw, and transfer rate is 0 ~ 50m
3the power of/h, buffer tank b is 0.75kw, and the volume of buffer tank a is 1.35m
3, the slurry in buffer tank b is sent into horizontal centrifuge b17 through slush pump d16 and is dewatered; The power of slush pump d is 1.5kw, and transfer rate is 0 ~ 1.2m
3/ h.
The slag notch of described horizontal centrifuge b is connected to conveying worm c18, and the liquid outlet of horizontal centrifuge b is connected to coagulating sedimentation removal heavy metal system by fluid pipeline; Described conveying worm c is provided with two discharging openings; Third level washing desalter comprises agitator tank c19, the discharging opening of each conveying worm c is connected to an agitator tank c, slurries in each agitator tank c send into buffer tank c21 through slush pump e20, slurry in buffer tank c is sent into horizontal centrifuge c through slush pump f and is dewatered, and the charging aperture of described horizontal centrifuge c is connected to the discharging opening of slush pump f22; The slag notch of described horizontal centrifuge c is connected to cement kiln, mud is isolated the flying dust of chloro ion-containing solution and the moisture Ji bioxin of secondary, the moisture content of the flying dust of the moisture Ji bioxin of secondary is 40%-50%, chloro ion-containing solution enters coagulative precipitation tank, and the flying dust of the moisture Ji bioxin of secondary enters agitator tank c.The fly ash carry of the moisture Ji bioxin of secondary to agitator tank c, and carries out stirring washing with the weight ratio of initial flying dust and water for 1:2 adds water, and adding quality in whipping process is that the chaotropic agent of 1% of initial flying dust carries out stirring 20 minutes; Stirring fully and obtain three mud. three mud enter horizontal centrifuge c23 and dewater, and the charging aperture of horizontal centrifuge c is connected to the discharging opening of slush pump f; The slag notch of described horizontal centrifuge c is connected to cement kiln 24.Mud is isolated the flying dust of chloro ion-containing solution and three moisture Ji bioxin, the moisture content of the flying dust of three moisture Ji bioxin is 40%-50%, chloro ion-containing solution enters coagulative precipitation tank, the flying dust of three moisture Ji bioxin and chloride ion-containing enter lower than the flying dust of 1% heavy metal that mud collecting pit carries out in microbial attack bioxin and ash, flying dust through microbial attack bioxin can directly as the raw material of construction material, this microorganism is reusable, and the tertiary effluent namely completing flying dust and water yield 1:8 washes system.
Described each agitator tank b is connected to water inlet pipe b, each agitator tank c is connected to water inlet pipe c, described water inlet pipe a, water inlet pipe b are connected with inlet water tank 25 respectively with water inlet pipe c; Described each agitator tank b is connected to chemical feed pipe b, each agitator tank c is connected to chemical feed pipe c, described chemical feed pipe a, chemical feed pipe b and chemical feed pipe c are connected on chemicals dosing plant 26; The flow that the liquid outlet parallel join of described chemicals dosing plant has three groups of automatic control flow devices, 27, three groups of automatic control flow devices to control in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, can send alarm when dose is not enough.
Described coagulating sedimentation removal heavy metal system comprises coagulative precipitation tank 12, and the left end of described coagulative precipitation tank is connected to two agitator tank d29 by delivery pump a28, and each agitator tank d is communicated with liquid-feeding tube 30 and chemical feed pipe 31; Liquid-feeding tube place enters tertiary effluent and washes rear chloro ion-containing solution, chemical feed pipe place adds anion active agent and stirs, and the quality of anion active agent accounts for 1 ‰ ~ 5 ‰ of chloro ion-containing solution quality, large molecule is formed thus precipitation after making multiple dispersed metal ionic polymerization, after static 0.5 ~ 1 hour, the heavy metal ion of 85 ~ 95% is precipitated; Liquid-feeding tube is provided with priming valve 32, chemical feed pipe is provided with the dosing valve 33 controlling dosing flow.Described chemical feed pipe is connected with chemicals dosing plant 35 by dosing pump 34, and the power of dosing pump is 0.37KW, and chemicals dosing plant is connected with water pipe 36, and the nearly running water in water pipe place is convenient to mix with liquid, described coagulative precipitation tank bottom is connected with centrifugal dehydrator 37, coagulative precipitation tank top is connected with Buffer Pool 38, Buffer Pool is connected to delivery pump b39, delivery pump b is connected to composite bag type filter 40, composite bag type filter has two, each composite bag type filter top is provided with inlet, bottom is provided with liquid outlet, lower end is provided with sewage draining exit, the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter, the heavy metal obtained and impurity transport into centrifugal dehydrator by sewage draining exit and dewater, the saliferous rate obtained is that the solution of 1-2% enters next treatment system by liquid outlet, the clear liquid on coagulative precipitation tank top is conveyed into Buffer Pool, and the liquid in Buffer Pool is conveyed into composite bag type filter by delivery pump b, and the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter.
Described sodium filter and counter-infiltration preconcentration technique comprise sodium filter assembly 41, described sodium filter assembly is communicated with chemicals dosing plant a, and chemicals dosing plant a is connected with water pipe a; Chemicals dosing plant a enters antisludging agent, and the water inlet end of described sodium filter assembly is connected to filter a, and the condensed water of sodium filter assembly output is connected to intermediate water tank 42 by pipeline, and the fresh water of sodium filter assembly output is connected to counter-infiltration water tank by pipeline; The bottom of described intermediate water tank is connected to feeding engine a, and the water side of feeding engine a is connected to filter b, and the port of export of filter b is connected to counter-infiltration pre-concentration device 43; Described counter-infiltration pre-concentration device is communicated with chemicals dosing plant b, and chemicals dosing plant b is connected with water pipe b; The condensed water of described counter-infiltration pre-concentration device output is connected in Membrane Materials system by water pipe, and 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 sent into reverse osmosis membrane assembly 43 with feeding engine again and is carried out counter-infiltration pre-concentration, enter antisludging agent by chemicals dosing plant c in reverse osmosis membrane assembly simultaneously, water can be concentrated into 6% ~ 8% by reverse osmosis membrane assembly, reverse osmosis membrane assembly output fresh water enters reverse osmosis produced water tank, and the water in reverse osmosis produced water tank can enter incineration of refuse flyash washing moisturizing and use.
Described membrane distillation concentration system comprises heating water tank 44, and the volume of heating water tank is 16m
3, described heating water tank is connected with volumetric heat exchanger, and the upper end of heating water tank is communicated with feed tube, feed tube is provided with charging valve a; The lower end of heating water tank is communicated with two groups of operating water tanks 45 side by side by feeding engine, and the volume of operating water tank is 8m
3, the power of feeding engine is 4KW, and flow is 80m
3/ h, and charging line between heating water tank and operating water tank is provided with charging valve b.
The outlet pipe often organizing described operating water tank is connected to hot water inlet pipe and the concentrated water tank 47 of distillation device 46 simultaneously by feeding circulating pump, the volume of concentrated water tank is 3m
3, hot water inlet pipe is provided with distillation ball valve, the water inlet pipe of concentrated water tank is provided with Filtering ball valve, and the power of feeding circulating pump is 4KW, and flow is 54m
3/ h, often organizes on described operating water tank and is connected with dope evacuated tube and dope return pipe.Include the 12 groups of membrane modules be connected in parallel in described distillation device, each group membrane module is in series by 4 Membrane Materials devices, and the temperature entering the hot water of distillation device is 67 DEG C.Its membrane module adopts a kind of normal pressure anti-soil of Huzhou Sen Nuo membrane technology Engineering Co., Ltd to block up energy-saving Membrane Materials device, and the patent No. is 201420465882.4.
The hot water outlet pipe of described distillation device is connected to dope return pipe, and the hot water temperature that hot water outlet pipe is flowed out is 57 DEG C, and the hot water that hot water outlet pipe is flowed out gets back to operating water tank by dope return pipe again, recycles.
The cold water inlet tube of described distillation device is connected to cooling tower, and cooling tower is connected with CWR, and 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, and the temperature of cooling water outlet pipe water is out 35 DEG C, and cooling water outlet pipe water out gets back to cooling tower by CWR again, and the water cooling of 35 DEG C to 25 DEG C, then continues to recycle by cooling tower.
The condensate pipe of described distillation device is connected to and produces water tank 48, and the volume producing water tank is 2m
3, the condensed water producing water tank is used for membrane module backwash and incineration of refuse flyash washing moisturizing, and a large amount of distilled water recoverables, saves water resource.
Described 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, and backwash water feed pipe is connected to backwash water tank 49 by backwashing pump, and the volume of backwash water tank is 3m
3, and backwash water tank and backwash water evacuated tube link together, and the dope evacuated tube on dope evacuated tube a and operating water tank links together.
Saliferous rate is that the solution of 6-8% delivers into heating water tank, and use volumetric heat exchanger to utilize plant area's waste heat to heat to solution, after solution temperature rise to 70 °, solution enters operating water tank; Then solution enters distillation device and circulates, solution undergoes phase transition in membrane module, steam is by the film pipe in Membrane Materials device, distilled water is become again by the corrosion-resistant condensing tube condensation that thermal conductivity factor is high, distilled water enters product water tank, and distilled water is used for membrane module backwash and incineration of refuse flyash washing moisturizing; Along with the minimizing of water in solution, solution concentration is increasing, after solution concentration reaches the nearly saturation state of saliferous rate 20%-30%, solution does not circulate, nearly saturated solution enters operating water tank, operating water tank reaches liquid level lower limit position, and Liquid Residue in membrane module and condensation pipe is all entered concentrated water tank by self priming pump startup; Emptying rear backwash starts, and carry out backwash by the distilled water produced to membrane module, backwash pipeline enters by membrane module is suitable for reading, discharges, the micro-crystalline solid adhered to cleaned in distillation device from end opening; In backwash process, heating water tank carries out stopping fluid infusion after fluid infusion reaches liquid level upper limit position place to operating water tank, and after backwash terminates, it is concentrated that operating water tank carries out next one circulation.
Described denier carnallite system of going comprises concentrate case 50, the water of the concentrated water tank in membrane distillation concentration system enters concentrate case, the upper end of described concentrate case is communicated with feed tube, the lower end of described concentrate case is communicated with drain pipe, described drain pipe is connected with and is separated feeding engine 51, the discharge nozzle being separated feeding engine divides two-way, every road discharge nozzle is connected to separation ball valve, for being separated ball valve a52 and being separated ball valve b53, be separated ball valve a and be connected to one-level carnallite release unit 54, be separated ball valve b and be connected to secondary carnallite release unit 55; The lower end of described one-level carnallite release unit is connected to carnallite collecting pit 56, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c57, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a58 is connected with concentrated material returning valve 59; The upper end of described secondary carnallite release unit is connected to and is separated ball valve d60, and be separated ball valve d and be connected to pipeline a and pipeline b61 simultaneously, pipeline b is connected with crystallization and evaporation valve 62, crystallization and evaporation valve is connected to MVR evaporation and crystallization system.
Heat up after the dope of concentrated water tank enters flat ultra micro water filtration film one-level carnallite release unit by separation feeding engine, temperature is upgraded to 80-110 DEG C and carries out high temperature circulation process 5 ~ 10 minutes, the carnallite of high temperature section is removed, carnallite precipitation enters carnallite collecting pit, and the dope obtained turns back to concentrated water tank by dope material returning valve; Then the dope obtained through the process of one-level carnallite release unit in concentrated water tank to be sent in secondary carnallite release unit circular treatment 5 ~ 10 minutes, utilize absorption principle to be removed by carnallite further, make to heat up and enter MVR evaporation and crystallization system except carnallite dope obtains heat and carry out evaporative crystallization.
Described MVR evaporation and crystallization system comprises feeding engine d63, and feeding engine d is connected to evaporating chamber 64, described evaporating chamber is communicated with heat exchanger 65, heat exchanger is connected with steam recompression pump 66; The bottom of described evaporating chamber is connected with suction filtration tank 68 by discharging pump d67, and the top of evaporating chamber is connected to Roots's steam recompression machine 69 by pipeline; In described Roots's steam recompression machine, vavuum pump 70 is installed; Described vavuum pump is connected to filtrate tank 71, filtrate tank is connected with suction filtration tank, and vavuum pump and steam recompress pump links together, the mother liquor under vavuum pump effect in filtrate tank is negative pressure state, and the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization.
First evaporating chamber is entered by feeding engine d by the dope going denier carnallite technique to obtain, heat exchanger passes into live steam and heats dope, in dope evaporation process two sections of steam of output can enter Roots's steam recompression machine by vapor (steam) temperature raise continue to enter heat exchanger to dope heating evaporation, supplement original vol saturated vapor without the need to continuing, the water that Roots's steam recompression machine produces enters condensation water tank 72.Dope carries out evaporation and reaches hypersaturated state crystallize out, then enter suction filtration tank from evaporating chamber by discharging pump d discharge and carry out Separation of Solid and Liquid, vavuum pump is provided with in Roots's steam recompression machine, vavuum pump filtrate tank connects, mother liquor under vavuum pump effect in filtrate tank is negative pressure state, the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization, and evaporative crystallization salt out contains sodium chloride and reaches more than 76% and can be used for papermaking, snow melting agent or chlor-alkali industry.
Above-described embodiment is the specific descriptions of carrying out the utility model; just the utility model is further described; can not be interpreted as the restriction to the utility model protection domain, those skilled in the art makes some nonessential improvement according to the content of above-mentioned utility model and adjustment all falls within protection domain of the present utility model.
Claims (10)
1. garbage flying ash cement kiln synergic processing and recycling of water resource utilize a system, it is characterized in that: it comprises the incineration of refuse flyash tertiary effluent salt elution system, coagulating sedimentation removal heavy metal system, the sodium filter that connect successively and counter-infiltration preconcentration technique, membrane distillation concentration system, goes denier carnallite system and MVR evaporation and crystallization system; The washing water of described incineration of refuse flyash tertiary effluent salt elution system produce enters coagulating sedimentation removal heavy metal system by pipeline; The saliferous rate that coagulating sedimentation removal heavy metal system obtains is that the solution of 1-2% enters sodium filter and counter-infiltration preconcentration technique; Described sodium filter and counter-infiltration preconcentration technique remove the calcium ions and magnesium ions in washing water, be the dope that the solution of 1-2% is concentrated into 6%-8% by saliferous rate, the dope of 6%-8% is conveyed into membrane distillation concentration system and carries out circulation output distilled water for membrane module backwash and incineration of refuse flyash washing moisturizing; The saliferous rate of described membrane distillation concentration system produce is that the nearly saturated solution of 20%-30% enters denier carnallite system and removed by carnallite, and last nearly saturated solution enters MVR evaporation and crystallization system and carries out evaporative crystallization.
2. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described incineration of refuse flyash tertiary effluent salt elution system it comprise flying dust storage, the lower end of described flying dust storage is communicated with conveying worm a, the outlet of described conveying worm is connected to first order washing desalter, and first order washing desalter comprises agitator tank a; Described agitator tank a is communicated with respectively water inlet pipe a and chemical feed pipe a; Flying dust in described agitator tank a, water become mud with medicinal liquid agitating, the lower end of agitator tank a is connected to slush pump a, mud in agitator tank a is conveyed into buffer tank a by slush pump a, and the mud in buffer tank a is conveyed into horizontal centrifuge a by slush pump b and dewaters; Mud is isolated chloro ion-containing solution and flying dust that is moisture and bioxin by described horizontal centrifuge a, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and flying dust that is moisture and bioxin enters second level washing desalter; Chloro ion-containing solution mud isolated by described second level washing desalter and secondary is moisture and the flying dust of bioxin, and chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, and secondary flying dust that is moisture and bioxin enters third level washing desalter; The flying dust of chloro ion-containing solution and three moisture and bioxin isolated by third level washing desalter, chloro ion-containing solution enters coagulating sedimentation removal heavy metal system, the flying dust of three moisture Ji bioxin enters cement kiln, and after cement kiln burns, flying dust becomes cement raw material.
3. a kind of garbage flying ash cement kiln synergic processing according to claim 2 and recycling of water resource utilize system, it is characterized in that: the charging aperture of described horizontal centrifuge a is connected to the discharging opening of slush pump b; The slag notch of described horizontal centrifuge a is connected to conveying worm b, and the liquid outlet of horizontal centrifuge a is connected to coagulating sedimentation removal heavy metal system by fluid pipeline; Described conveying worm b is provided with two discharging openings; Described second level washing desalter comprises agitator tank b, the discharging opening of each conveying worm b is connected to an agitator tank b, slurries in each agitator tank b send into buffer tank b through slush pump c, and the slurry in buffer tank b is sent into horizontal centrifuge b through slush pump d and dewatered; The slag notch of described horizontal centrifuge b is connected to conveying worm c, and the liquid outlet of horizontal centrifuge b is connected to coagulative precipitation tank by fluid pipeline; Described conveying worm c is provided with two discharging openings; Third level washing desalter comprises agitator tank c, the discharging opening of each conveying worm c is connected to an agitator tank c, slurries in each agitator tank c send into buffer tank c through slush pump e, slurry in buffer tank c is sent into horizontal centrifuge c through slush pump f and is dewatered, and the charging aperture of described horizontal centrifuge c is connected to the discharging opening of slush pump f; The slag notch of described horizontal centrifuge c 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, it is characterized in that: described each agitator tank b is connected to water inlet pipe b, each agitator tank c is connected to water inlet pipe c, and described water inlet pipe a, water inlet pipe b are connected with inlet water tank respectively with water inlet pipe c; Described each agitator tank b is connected to chemical feed pipe b, each agitator tank c is connected to chemical feed pipe c, described chemical feed pipe a, chemical feed pipe b and chemical feed pipe c are connected on chemicals dosing plant; The liquid outlet parallel join of described chemicals dosing plant has three groups of automatic control flow devices, and three groups of automatic control flow devices control the flow in chemical feed pipe a, chemical feed pipe b and chemical feed pipe c respectively, can send alarm 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, it is characterized in that: described coagulating sedimentation removal heavy metal system comprises coagulative precipitation tank, the left end of described coagulative precipitation tank is connected to two agitator tank d by delivery pump a, and each agitator tank d is communicated with liquid-feeding tube and chemical feed pipe; Described chemical feed pipe is connected with chemicals dosing plant by dosing pump, and chemicals dosing plant is connected with water pipe; Described coagulative precipitation tank bottom is connected with centrifugal dehydrator, and 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 transports into centrifugal dehydrator and dewaters, the clear liquid on coagulative precipitation tank top is conveyed into Buffer Pool, liquid in Buffer Pool is conveyed into composite bag type filter by delivery pump b, the heavy metal do not precipitated completely and contaminant filter fall by composite bag type filter, the heavy metal obtained and impurity transport into centrifugal dehydrator and dewater, and the saliferous rate obtained is that the solution of 8-15% enters membrane distillation concentration device and carries out desalting processing.
6. a kind of garbage flying ash cement kiln synergic processing according to claim 5 and recycling of water resource utilize system, it is characterized in that: described chemical feed pipe is provided with the dosing valve controlling dosing flow; Described liquid-feeding tube is provided with priming valve.
7. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described sodium filter and counter-infiltration preconcentration technique comprise sodium filter assembly, described sodium filter assembly is communicated with chemicals dosing plant a, and chemicals dosing plant a is connected with water pipe a; The water inlet end of described sodium filter assembly is connected to filter a, and the condensed water of sodium filter assembly output is connected to intermediate water tank by pipeline, and the fresh water of sodium filter assembly output is connected to counter-infiltration water tank by pipeline; The bottom of described intermediate water tank is connected to feeding engine a, and the water side of feeding engine a is connected to filter b, and the port of export of filter b is connected to counter-infiltration pre-concentration device; Described counter-infiltration pre-concentration device is communicated with chemicals dosing plant b, and chemicals dosing plant b is connected with water pipe b; The condensed water of described counter-infiltration pre-concentration device output is connected in Membrane Materials system by water pipe, and the fresh water of counter-infiltration pre-concentration device output 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, it is characterized in that: described membrane distillation concentration system comprises heating water tank, described heating water tank is connected with volumetric heat exchanger, the upper end of heating water tank is communicated with feed tube, and the lower end of heating water tank is communicated with two groups of operating water tanks side by side by feeding engine; The outlet pipe often organizing described operating water tank is connected to the hot water inlet pipe of distillation device and concentrated water tank by feeding circulating pump simultaneously, often organize on described operating water tank and be connected with dope evacuated tube and dope return pipe, the hot water outlet pipe of described distillation device is connected to dope return pipe; The cold water inlet tube of described distillation device is connected to cooling tower, and cooling tower is connected with CWR, and the cooling water outlet pipe of distillation device is connected to CWR; The condensate pipe of described distillation device is connected to product water tank; Described distillation device top is connected with backwash water feed pipe, distillation device bottom is connected with backwash water evacuated tube and dope evacuated tube a, backwash water feed pipe is connected to backwash water tank by backwashing pump, and backwash water tank and backwash water evacuated tube link together, the dope evacuated tube on dope evacuated tube a and operating water tank links together.
9. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described in go denier carnallite system to comprise concentrate case, the upper end of described concentrate case is communicated with feed tube, the lower end of described concentrate case is communicated with drain pipe, described drain pipe is connected with separation feeding engine, the discharge nozzle being separated feeding engine divides two-way, every road discharge nozzle is connected to separation ball valve, for being separated ball valve a and being separated ball valve b, be separated ball valve a and be connected to one-level carnallite release unit, be separated ball valve b and be connected to secondary carnallite release unit, the lower end of described one-level carnallite release unit is connected to carnallite collecting pit, and the upper end of one-level carnallite release unit is connected to and is separated ball valve c, is separated ball valve c and is connected to concentrate case by pipeline a, and pipeline a is connected with concentrated material returning valve, the upper end of described secondary carnallite release unit is connected to and is separated ball valve d, and be separated ball valve d and be connected to pipeline a and pipeline b simultaneously, pipeline b is connected with crystallization and evaporation valve, crystallization and evaporation valve is connected to MVR evaporation and crystallization system.
10. a kind of garbage flying ash cement kiln synergic processing according to claim 1 and recycling of water resource utilize system, it is characterized in that: described MVR evaporation and crystallization system comprises feeding engine d, feeding engine d is connected to evaporating chamber, described evaporating chamber is communicated with heat exchanger, heat exchanger is connected with steam recompression pump; The bottom of described evaporating chamber is connected with suction filtration tank by discharging pump d, and the top of evaporating chamber is connected to Roots's steam recompression machine by pipeline; In described Roots's steam recompression machine, vavuum pump is installed; Described vavuum pump is connected to filtrate tank, filtrate tank is connected with suction filtration tank, and vavuum pump and steam recompress pump links together, the mother liquor under vavuum pump effect in filtrate tank is negative pressure state, and the mother liquor be stored under suction function in filtrate tank returns evaporating chamber and continues evaporative crystallization.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201520643657.XU CN204912255U (en) | 2015-08-25 | 2015-08-25 | Rubbish flying dust cement kiln is dealt with and water utilization system in coordination |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201520643657.XU CN204912255U (en) | 2015-08-25 | 2015-08-25 | Rubbish flying dust cement kiln is dealt with and water utilization system in coordination |
Publications (1)
Publication Number | Publication Date |
---|---|
CN204912255U true CN204912255U (en) | 2015-12-30 |
Family
ID=54961439
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN201520643657.XU Expired - Fee Related CN204912255U (en) | 2015-08-25 | 2015-08-25 | Rubbish flying dust cement kiln is dealt with and water utilization system in coordination |
Country Status (1)
Country | Link |
---|---|
CN (1) | CN204912255U (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105080935A (en) * | 2015-08-25 | 2015-11-25 | 湖州森诺膜技术工程有限公司 | Rubbish flying ash cement kiln co-treatment and water resource utilization system |
CN105537245A (en) * | 2016-01-22 | 2016-05-04 | 湖州森诺膜技术工程有限公司 | Resource utilization system for rubbish fly ash |
CN108607870A (en) * | 2018-04-26 | 2018-10-02 | 丁仲军 | A kind of garbage flying ash processing system and treatment process |
-
2015
- 2015-08-25 CN CN201520643657.XU patent/CN204912255U/en not_active Expired - Fee Related
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105080935A (en) * | 2015-08-25 | 2015-11-25 | 湖州森诺膜技术工程有限公司 | Rubbish flying ash cement kiln co-treatment and water resource utilization system |
CN105080935B (en) * | 2015-08-25 | 2017-10-20 | 湖州森诺环境科技有限公司 | A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system |
CN105537245A (en) * | 2016-01-22 | 2016-05-04 | 湖州森诺膜技术工程有限公司 | Resource utilization system for rubbish fly ash |
CN108607870A (en) * | 2018-04-26 | 2018-10-02 | 丁仲军 | A kind of garbage flying ash processing system and treatment process |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN105107821B (en) | A kind of garbage flying ash cement kiln synergic processing and recycling of water resource method of disposal | |
CN105080936B (en) | A kind of garbage flying ash cement kiln synergic processing method | |
CN105107820A (en) | Cement kiln co-processing system for waste incineration fly ash | |
CN105478438B (en) | A kind of garbage flying ash cement kiln synergic processing and innoxious resource circulation utilization method | |
CN105000737B (en) | A kind of Industrial sewage treatment system and sewage water treatment method | |
CN102139982B (en) | Water purification and regeneration device based on rotary spray evaporation and application of device | |
CN204122439U (en) | For the city garbage burning flying ash resource pretreatment system of cement producting material | |
CN105080935B (en) | A kind of garbage flying ash cement kiln synergic processing and recycling of water resource utilize system | |
CN204912255U (en) | Rubbish flying dust cement kiln is dealt with and water utilization system in coordination | |
CN107151076A (en) | A kind of processing of high-concentration waste emulsion, recovery process | |
CN114405969B (en) | Water washing desalination process for fly ash and application thereof | |
CN106966536A (en) | Strong brine zero-emission film concentration technology and equipment | |
CN103265090B (en) | Zero-emission device for concentrated saline water evaporated liquid and process method | |
CN106746129B (en) | Landfill leachate evaporation crystallization system | |
CN208684674U (en) | Processing system for garbage filter concentrate zero-emission | |
CN102633378A (en) | Method and system for recycling catalyst from coal chemical liquid waste | |
CN205974124U (en) | Coal chemical wastewater's processing system | |
CN212198888U (en) | Desulfurization waste water concentration decrement device based on film evaporation technique | |
CN204912257U (en) | Rubbish flying dust cement kiln is processing system in coordination | |
CN205710254U (en) | A kind of high slat-containing wastewater Zero emission device for coal chemical industry | |
CN115259518A (en) | System and method for treating percolate concentrated solution | |
CN206109092U (en) | Concentrated decrement processing apparatus of high salt waste water membrane | |
CN204079718U (en) | One heavy metal species chemical leaching liquid waste disposal, recycling integrated device | |
CN104230120B (en) | One heavy metal species chemical leaching liquid waste disposal, recycling integrated device and leacheate process, reuse method | |
CN209128231U (en) | A kind of flying dust leaching liquid treating system |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
C14 | Grant of patent or utility model | ||
GR01 | Patent grant | ||
C56 | Change in the name or address of the patentee | ||
CP03 | Change of name, title or address |
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 Patentee 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 Patentee before: HUZHOU SENNUO MEMBRANE TECHNOLOGY ENGINEERING Co.,Ltd. |
|
CF01 | Termination of patent right due to non-payment of annual fee | ||
CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151230 |