CN109396163A - A kind of garbage flying ash treatment process improving chloride ion dissolution rate - Google Patents
A kind of garbage flying ash treatment process improving chloride ion dissolution rate Download PDFInfo
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- CN109396163A CN109396163A CN201811550214.0A CN201811550214A CN109396163A CN 109396163 A CN109396163 A CN 109396163A CN 201811550214 A CN201811550214 A CN 201811550214A CN 109396163 A CN109396163 A CN 109396163A
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- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 56
- 230000008569 process Effects 0.000 title claims abstract description 37
- 238000004090 dissolution Methods 0.000 title claims abstract description 32
- 239000010813 municipal solid waste Substances 0.000 title claims abstract description 25
- 239000000428 dust Substances 0.000 claims abstract description 216
- 238000005406 washing Methods 0.000 claims abstract description 186
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 184
- 239000007788 liquid Substances 0.000 claims abstract description 79
- 238000001238 wet grinding Methods 0.000 claims abstract description 61
- 238000012545 processing Methods 0.000 claims abstract description 37
- 239000007787 solid Substances 0.000 claims abstract description 35
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 33
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 31
- 239000012528 membrane Substances 0.000 claims abstract description 31
- 238000011033 desalting Methods 0.000 claims abstract description 24
- 239000002002 slurry Substances 0.000 claims abstract description 11
- 239000006210 lotion Substances 0.000 claims abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 52
- 238000002425 crystallisation Methods 0.000 claims description 30
- 230000008025 crystallization Effects 0.000 claims description 29
- 230000002411 adverse Effects 0.000 claims description 24
- 229910021529 ammonia Inorganic materials 0.000 claims description 24
- 239000004568 cement Substances 0.000 claims description 20
- 239000000706 filtrate Substances 0.000 claims description 18
- 238000003756 stirring Methods 0.000 claims description 14
- 230000002195 synergetic effect Effects 0.000 claims description 13
- 238000000227 grinding Methods 0.000 claims description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 238000011084 recovery Methods 0.000 claims description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 7
- 239000000908 ammonium hydroxide Substances 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 7
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 6
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 6
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 6
- 229960002089 ferrous chloride Drugs 0.000 claims description 6
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 claims description 6
- 239000012153 distilled water Substances 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 4
- 230000033116 oxidation-reduction process Effects 0.000 claims description 4
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 4
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 3
- 235000011152 sodium sulphate Nutrition 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- 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 description 2
- 230000036961 partial effect Effects 0.000 claims description 2
- 239000011734 sodium Substances 0.000 claims description 2
- 229910052708 sodium Inorganic materials 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- 239000002956 ash Substances 0.000 description 16
- 238000005265 energy consumption Methods 0.000 description 7
- 230000002829 reductive effect Effects 0.000 description 7
- 239000010881 fly ash Substances 0.000 description 6
- 238000004056 waste incineration Methods 0.000 description 6
- 230000007423 decrease Effects 0.000 description 5
- 238000010612 desalination reaction Methods 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 239000003480 eluent Substances 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- 241000372132 Hydrometridae Species 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000003672 processing method Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 238000005054 agglomeration Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- 229920000832 Cutin Polymers 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000006298 dechlorination reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/80—Destroying solid waste or transforming solid waste into something useful or harmless involving an extraction step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B5/00—Operations not covered by a single other subclass or by a single other group in this subclass
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B2101/00—Type of solid waste
- B09B2101/30—Incineration ashes
Landscapes
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a kind of garbage flying ash treatment process for improving chloride ion dissolution rate, before flying dust water-washing step, wet grinding is carried out to flying dust, the slurry formed after wet grinding enters back into flying dust water-washing step, the flying dust washing is that multi-stage countercurrent is washed, reverse osmosis membrane desalting processing is carried out to the water lotion of the afterbody washing of multi-stage countercurrent washing, the water source reuse that the clear water that reverse osmosis membrane desalting processing generates is washed as afterbody, the water source that the concentrated water that reverse osmosis membrane desalting processing generates is washed as upper level, the sum of water consumption+flying dust wet grinding water consumption of first order washing and flying dust mass ratio=1 ~ 1.1:1, it is separated by solid-liquid separation after first order washing, solid enters next stage after crushing and washes, liquid enters removing heavy-metal step.The present invention can effectively improve chloride ion dissolution rate in flying dust.
Description
Technical field
The present invention relates to environmental technology field, in particular to a kind of garbage flying ash for improving chloride ion dissolution rate handles work
Skill.
Background technique
With the rapid development of urbanization, China's domestic waste yield increases year by year, from 1.89 hundred million in 2013, on
2.06 hundred million tons of 2015 are raised to, since waste incineration has many advantages, such as volume reduction, decrement and energy recovery, so China's rubbish
Incineration disposal amount accounting increases year by year.Flying dust is the inevitable outcome of waste incineration, accounts about the 3 ~ 5% of the amount of burning away the refuse.Based on this
It calculates, the whole nation is since the flying dust of waste incineration generation is at 10000-20000 ton/days from now on.So a large amount of flying dust generates, so that such as
Safely and effectively disposition flying ash becomes environment urgently to be solved and social concern for what.
Flying dust is the thin particulate matter obtained by flue gas purification system collection, including with Chemical treatment flue gas when generates
Flying dust, 10%~20% is accounted for about in lime-ash.Generally in canescence or Dark grey, partial size is largely flying dust less than 300 μm
1.0 μm~30 μm, moisture content 10%~23%, clinker ignition loss 34%~51%, easy frost heave, hardly possible compacting, particle shape is in rodlike, more more
The irregular shapes such as cutin shape, flocculence, spherical.Meanwhile flying ash contains the nuisances such as dioxin and heavy metal, according to
" consumer waste incineration contamination control standard " (GB18485-2014) regulation: " domestic garbage incineration flyash should be by hazardous waste pipe
Reason ".Therefore, flying dust must be collected separately, and must not mix with house refuse, incineration residue etc., also must not be with other hazardous wastes
Mixing.
Currently, the main processing technique of incineration of refuse flyash has: cement solidification method, chemical agent stabilisation, melting and solidification
Method and cement kiln synergic processing method etc..Consider from economy, ease for operation and utilization of area etc., cement kiln synergic processing method
It is one of most suitable processing method.Since flying dust comes from waste incineration, flying dust will form a certain proportion of difficulty during generating
With the particle that gathers to scatter, flying dust directly carries out solid-liquid mixing in water, mixes and uneven, the chloride ion in fly ash granule is difficult to
Dissolution, meanwhile, when flying dust is washed, agglomeration of reuniting is easy between fly ash granule while agitating, chloride ion is also resulted in and is difficult to
Dissolution, therefore, flying dust are often further added by washing series after what washing, and the chloride ion content in flying dust can't be into
One step reduces, and also larger impact flying dust enters cement kiln synergic processing for this.
In addition, the high concentration chloride contained in flying dust, the presence of villaumite can seriously limit the harmlessness disposing and money of flying dust
Sourceization utilizes.In order to which the villaumite removal in flying dust to be met to the requirement of cement kiln synergic processing, multi-stage countercurrent washing is generallyd use
Mode, if three-level adverse current is washed, conventional three-level adverse current washing process is only suitable for the relatively low flying dust of chloride ion content and removes
Chlorine, if the higher flying dust of chloride ion content is faced, in order to reduce the chloride ion content in flying dust to meet cement kiln synergic processing
Requirement, in the case where not changing existing equipment, can only increase afterbody washing water consumption, cause to have a large amount of washing in this way
Eluent enters evaporative crystallization steps, and the energy consumption that such evaporative crystallization forms clear water reuse will greatly increase.If changing
Existing equipment then needs to increase washing series, and equipment and technique require to adjust, and operation difficulty is larger.
Summary of the invention
It is an object of the invention to solve existing energy consumption during flying dust dechlorinates to wash chlorine in flying dust greatly and repeatedly
The problem of ion can not further decrease provides a kind of garbage flying ash treatment process for improving chloride ion dissolution rate, can effectively mention
Multi-stage water wash can not be reduced chloride ion content lower limit in flying dust and further decreased by chloride ion dissolution rate in high flying dust.
The technical solution adopted by the present invention to solve the technical problems is:
It is a kind of improve chloride ion dissolution rate garbage flying ash treatment process, including flying dust washing, removing heavy-metal, decoloration, deliming and
Evaporative crystallization steps, the flying dust washing is that multi-stage countercurrent is washed, and before flying dust water-washing step, carries out wet grinding to flying dust,
The slurry formed after wet grinding enters back into flying dust water-washing step, when flying dust carries out wet grinding, controls the quality of flying dust and water
Than=1:0.3-0.5, the sum of water consumption+flying dust wet grinding water consumption of first order washing of multi-stage countercurrent washing and flying dust
Mass ratio=1 ~ 1.1:1 is separated by solid-liquid separation after first order washing, and solid enters next stage after crushing and washes, and liquid enters de- weight
Metal step.
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1 ~ 1.1:1；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:1 ~ 1.1 of flying dust and water are washed in mass ratio=1:0.3-0.5, the second level；
It being separated by solid-liquid separation after third level washing, solid send the water source washed to cement kiln synergic processing, liquid as the second level,
Mass ratio=1:1 ~ 1.1 of the third level washing flying dust and water.
Flying dust is often further added by washing series, the chloride ion content in flying dust can't be into one after what washing
Step reduces, and also larger impact flying dust enters cement kiln synergic processing for this.How to solve the problems, such as that this becomes difficult point, inventor passes through
Research, develops solution, the present invention by introducing wet grinding before the first order is washed, first flying dust is ground to be formed it is even
Slurry can sufficiently scatter the particle that gathers for being difficult to scatter in flying dust during wet grinding, dissolve out convenient for chloride ion, and wet process is ground
It grinds the homogenate formed and is entering washing, more evenly, water-washing process is prevented from caking for mixing, can effectively improve chloride ion dissolution in this way
Multi-stage water wash can not be reduced chloride ion content lower limit in flying dust and further decreased by rate.
A kind of garbage flying ash treatment process improving chloride ion dissolution rate, including flying dust washing, removing heavy-metal, decoloration, remove
Calcium and evaporative crystallization steps, or including flying dust washing, removing heavy-metal, decoloration and evaporative crystallization steps, in flying dust water-washing step
Before, wet grinding is carried out to flying dust, the slurry formed after wet grinding enters back into flying dust water-washing step, and flying dust carries out wet grinding
When, mass ratio=1:0.3-0.5 of flying dust and water is controlled, the flying dust washing is that multi-stage countercurrent is washed, to multi-stage countercurrent washing
The water lotion of afterbody washing carries out reverse osmosis membrane desalting processing, and the clear water that reverse osmosis membrane desalting processing generates is as last
The water source reuse of grade washing, the water source that the concentrated water that reverse osmosis membrane desalting processing generates is washed as upper level, first order washing
The sum of water consumption+flying dust wet grinding water consumption and flying dust mass ratio=1 ~ 1.1:1 are separated by solid-liquid separation after first order washing,
Solid enters next stage after crushing and washes, and liquid enters removing heavy-metal step.
Since flying dust comes from waste incineration, flying dust will form during generating it is a certain proportion of be difficult to scatter gather
Grain, flying dust directly carry out solid-liquid mixing in water, mix and uneven, and the chloride ion in fly ash granule is difficult to dissolve out, meanwhile, flying dust
When washing, agglomeration of reuniting is easy between fly ash granule while agitating, chloride ion is also resulted in and is difficult to dissolve out, therefore, flying dust
By what washing after, be often further added by washing series, the chloride ion content in flying dust can't further decrease, this also compared with
The big flying dust that influences enters cement kiln synergic processing.How to solve the problems, such as that this becomes difficult point, after study, exploitation understands inventor
Certainly scheme, the present invention first grind flying dust to form homogenate, wet grinding process by introducing wet grinding before the first order is washed
In the particle that gathers for being difficult to scatter in flying dust can sufficiently be scattered, convenient for chloride ion dissolve out, wet grinding formed homogenate exist
Into washing, more evenly, water-washing process is prevented from caking, can effectively improve chloride ion dissolution rate in this way for mixing.
Multi-stage water wash is passed through for flying dust, after washing such as three-level adverse current, chloride ion content is unable to satisfy at cement kiln collaboration
The requirement set causes to have so a large amount of therefore, it is necessary to increase the dosage of water scouring water to reduce the chloride ion content in flying dust
Washing eluent enter evaporative crystallization steps, the energy consumption that such evaporative crystallization forms clear water reuse will greatly increase,
Under the premise of not changing existing equipment, this field does not have effective solution scheme.Although can be by increasing washing series drop
Chloride ion content in low flight ash, still, equipment and technique require adjustment and increase, and operation difficulty is larger.Inventor is through too long
The research of phase explores an effective solution approach, under the premise of not increasing washing series, water consumption is increased, last
Increase reverse osmosis membrane desalination scheme when one-stage water wash, by reverse osmosis membrane desalination, most of clear water can reuse, and reuse cost
Low energy consumption is low, and realizing not will increase while reducing the chloride ion content in flying dust and meeting cement kiln synergic processing requirement
Into the eluent of evaporative crystallization steps, to reduce the effect of energy consumption.Increase reverse osmosis membrane desalination in afterbody washing
Scheme, the salt content being primarily due to when afterbody washing in flying dust is lower, increases under water consumption, containing in eluent
Salt amount is low, and reverse osmosis membrane can preferably be born, and be used.The form of thinking of those skilled in the art's routine only can simply be thought
To before reverse osmosis membrane is used evaporative crystallization operation, however, the liquid before evaporative crystallization operation is excessively high because of salt content, basic nothing
Method uses reverse osmosis membrane, and therefore, reverse osmosis membrane desalination scheme is never considered to use in garbage flying ash processing.
The scheme that chloride ion content can be made to meet cement kiln synergic processing requirement is washed for conventional three-level adverse current,
Using solution of the invention, reach identical requirement and 1-2 grades of washings then only needed to can be solved, can also effectively shorten technique,
Reduce cost of equipment maintenance.
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1 ~ 1.1:1；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:0.3-0.5；
It being separated by solid-liquid separation after third level washing, solid is sent to cement kiln synergic processing, and liquid uses reverse osmosis membrane desalting processing,
The water source that the concentrated water that reverse osmosis membrane desalting processing generates is washed as the second level, the clear water conduct that reverse osmosis membrane desalting processing generates
The water source reuse of third level washing, the third level wash mass ratio=1:2.5 ~ 4 of flying dust and water.
Mass ratio=1 ~ 1.1:1 of total Water and flying dust when the first order of the present invention is washed, wherein 0.3-0.5 parts of water come from
The water of wet grinding, first order washing addition only needs to complement to 1 ~ 1.1 part of water on the basis of 0.3-0.5 parts of water.It is wet
The liquid part that the water of method grinding is separated by solid-liquid separation after the washing of the second level, recycles, without additional addition, energy-saving and emission-reduction.
Mass ratio=1:1 ~ 1.1 of the washing of the strict control first order flying dust and water (total Water) of the present invention, enter evaporation in this way
The water of crystallization, which maintains always, to be reached flying dust and can stir the minimum requirements of washing, will not be increased burden to subsequent evaporation crystallization.The
Three-level washes mass ratio=1:2.5 ~ 4 of flying dust and water, and the quality of flying dust and water when the first order is washed is met by technique fine tuning
It smooth can be run than=1:1 ~ 1.1.
Aeration stirring is carried out in multi-stage countercurrent water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is all provided with
There is Ammonia recovery mouth, is absorbed to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
The water source reuse that the distilled water that evaporative crystallization steps generate is washed as afterbody.
The removing heavy-metal step are as follows: under stirring condition, is washed in gained filtrate to flying dust and be slowly added to sodium sulfide solution,
Until the oxidation-reduction potential of system reaches 0 ~ -50mV, solution of ferrous chloride is then added, until the redox of system
Until current potential reaches -100 ~ -150mV.
The mass concentration of sodium sulfide solution is 2-5%；The mass concentration of solution of ferrous chloride is 3-10%.
The decoloration to add active carbon into the filtrate after removing heavy-metal, activated carbon dosage be filtrate weight thousand/
5/1000ths to thousand, 3-10min is stirred, filtering is collected filter residue and stored as dangerous waste, and filtrate enters to be handled in next step.
The deliming is, to sodium carbonate or sodium sulphate is added in gained filtrate after decoloration, stirs 10-20min, filters, collection
The calcium carbonate or calcium sulfate of solid portion, filtrate enters to be handled in next step.
The beneficial effects of the present invention are:
1, the present invention can substantially reduce the energy consumption when evaporative crystallization under the premise of not increasing washing series, reduce production
Cost；2, reach water washing effect same as the prior art, washing series can be reduced, effectively shorten technique, reduce equipment dimension
Protect cost；3, chloride ion dissolution rate in flying dust can be effectively improved, multi-stage water wash can not be reduced into chloride ion content lower limit in flying dust
It further decreases.
Detailed description of the invention
Fig. 1 is the first process flow chart of the invention.
Fig. 2 is second of process flow chart of the invention.
Fig. 3 is the third process flow chart of the invention.
Specific embodiment
Below by specific embodiment, technical scheme of the present invention will be further explained in detail.
In the present invention, if not refering in particular to, used raw material and equipment etc. are commercially available or commonly used in the art.
Method in following embodiments is unless otherwise instructed the conventional method of this field.
Embodiment 1:
A kind of garbage flying ash treatment process (Fig. 1) improving chloride ion dissolution rate, including wet grinding, flying dust washing, a de- huge sum of money
Category, decoloration, deliming and evaporative crystallization steps form slurry and enter back into flying dust water-washing step after flying dust wet grinding；
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1:1, i.e. flying dust and the first order are washed
Water consumption mass ratio=1:0.7；
It is separated by solid-liquid separation after the washing of the second level, mass ratio=1:1 of flying dust and water is washed in the second level, and solid enters the after crushing
Three-level washing, water source of the liquid a part as flying dust wet grinding, the water source that liquid residual part is washed as the first order,
When the middle water source as flying dust wet grinding, the dosage of water is the mass ratio=1:0.3 for controlling flying dust and water；
It is separated by solid-liquid separation after third level washing, solid (chloride ion content about 1.2% or so, in terms of dry weight) send to cement kiln and assists
With disposition, the water source that liquid is washed as the second level, the third level washes mass ratio=1:1 of flying dust and water.
Aeration stirring is carried out in three-level adverse current water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is all provided with
There is Ammonia recovery mouth, is absorbed to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
Embodiment 2:
A kind of garbage flying ash treatment process (Fig. 1) improving chloride ion dissolution rate, including wet grinding, flying dust washing, a de- huge sum of money
Category, decoloration, deliming and evaporative crystallization steps form slurry and enter back into flying dust water-washing step after flying dust wet grinding；
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1.1:1, i.e. flying dust and first order water
Mass ratio=the 1:0.6 for the water consumption washed；
It is separated by solid-liquid separation after the washing of the second level, mass ratio=1:1.1 of flying dust and water is washed in the second level, and solid enters after crushing
Third level washing, water source of the liquid a part as flying dust wet grinding, the water source that liquid residual part is washed as the first order,
Wherein when water source as flying dust wet grinding, the dosage of water is the mass ratio=1:0.5 for controlling flying dust and water；
It is separated by solid-liquid separation after third level washing, solid (chloride ion content about 1.2% or so, in terms of dry weight) send to cement kiln and assists
With disposition, the water source that liquid is washed as the second level, the third level washes mass ratio=1:1.1 of flying dust and water.
Aeration stirring is carried out in three-level adverse current water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is all provided with
There is Ammonia recovery mouth, is absorbed to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
Embodiment 3:
A kind of garbage flying ash treatment process (Fig. 2) improving chloride ion dissolution rate, including flying dust washing, removing heavy-metal, decoloration, remove
Calcium and evaporative crystallization steps, the water source reuse that the distilled water that evaporative crystallization steps generate is washed as the third level；It is washed in flying dust
Before step, wet grinding is carried out to flying dust, the slurry formed after wet grinding enters back into flying dust water-washing step；
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1:1, i.e. flying dust and the first order are washed
Water consumption mass ratio=1:0.7；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:0.3；30% of liquid i.e. after the washing of the second level is used for wet grinding, and 70% washes for the first order；
It is separated by solid-liquid separation after third level washing, solid (chloride ion content about 0.9% or so, in terms of dry weight) send to cement kiln and assists
With disposition, liquid uses reverse osmosis membrane desalting processing, the water that the concentrated water that reverse osmosis membrane desalting processing generates is washed as the second level
Source, the water source reuse that the clear water that reverse osmosis membrane desalting processing generates is washed as the third level, the third level wash the matter of flying dust and water
Measure ratio=1:2.5；
Aeration stirring is carried out in three-level adverse current water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is equipped with ammonia
Gas recovery port absorbs to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
Embodiment 4:
A kind of garbage flying ash treatment process (Fig. 2) improving chloride ion dissolution rate, including flying dust washing, removing heavy-metal, decoloration, remove
Calcium and evaporative crystallization steps, the water source reuse that the distilled water that evaporative crystallization steps generate is washed as the third level；It is washed in flying dust
Before step, wet grinding is carried out to flying dust, the slurry formed after wet grinding enters back into flying dust water-washing step；
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1.1:1, i.e. flying dust and first order water
Mass ratio=the 1:0.6 for the water consumption washed；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:0.5；
It is separated by solid-liquid separation after third level washing, solid (chloride ion content about 0.8% or so, in terms of dry weight) send to cement kiln and assists
With disposition, liquid uses reverse osmosis membrane desalting processing, the water that the concentrated water that reverse osmosis membrane desalting processing generates is washed as the second level
Source, the water source reuse that the clear water that reverse osmosis membrane desalting processing generates is washed as the third level, the third level wash the matter of flying dust and water
Measure ratio=1:3；
Aeration stirring is carried out in three-level adverse current water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is equipped with ammonia
Gas recovery port absorbs to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
Embodiment 5:
It is a kind of improve chloride ion dissolution rate garbage flying ash treatment process (Fig. 3), including flying dust washing, removing heavy-metal, decoloration and
Evaporative crystallization steps, the water source reuse that the distilled water that evaporative crystallization steps generate is washed as the third level；In flying dust water-washing step
Before, wet grinding is carried out to flying dust, the slurry formed after wet grinding enters back into flying dust water-washing step；
The flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1:1, i.e. flying dust and the first order are washed
Water consumption mass ratio=1:0.6；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:0.4；
It is separated by solid-liquid separation after third level washing, solid (chloride ion content about 0.75% or so, in terms of dry weight) send to cement kiln and assists
With disposition, liquid uses reverse osmosis membrane desalting processing, the water that the concentrated water that reverse osmosis membrane desalting processing generates is washed as the second level
Source, the water source reuse that the clear water that reverse osmosis membrane desalting processing generates is washed as the third level, the third level wash the matter of flying dust and water
Measure ratio=1:4；
Aeration stirring is carried out in three-level adverse current water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is equipped with ammonia
Gas recovery port absorbs to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
Removing heavy-metal step of the invention are as follows: under stirring condition, washed in gained filtrate to flying dust and be slowly added to vulcanized sodium
Solution then adds solution of ferrous chloride until the oxidation-reduction potential of system reaches 0 ~ -50mV, until the oxygen of system
Until change reduction potential reaches -100 ~ -150mV.The mass concentration of sodium sulfide solution is 2-5%.The quality of solution of ferrous chloride is dense
Degree is 3-10%.
Decoloration of the invention is that active carbon is added into the filtrate after removing heavy-metal, and activated carbon dosage is the thousand of filtrate weight
5/1 mono- to thousand, 3-10min is stirred, filtering is collected filter residue and stored as dangerous waste, and filtrate enters to be handled in next step.
Deliming of the invention is to stir 10-20min to adding sodium carbonate or sodium sulphate in gained filtrate after decoloration, filtering,
The calcium carbonate or calcium sulfate of solid portion are collected, filtrate enters to be handled in next step.
Removing heavy-metal, decoloration, deliming, evaporative crystallization steps are not core inventive points of the present invention in the present invention, removing heavy-metal,
Decoloration, deliming, evaporative crystallization steps particular content can also refer to 108607870 A of inventor's earlier application CN detailed note
It carries, this will not be repeated here.
By taking three-level adverse current is washed as an example, reach identical dechlorination ion effect, third level washing uses the matter of flying dust and water
Ratio=1:3 is measured, (third level, which is washed, is not used reverse osmosis deaslination, therefore first order washing flies using existing three-level adverse current hydraulic art
The mass ratio of ash and water is also in 1:3 or so), (third level washing uses reverse osmosis deaslination, does not use compared with technique of the invention
Electrodialysis desalination, the first order wash the mass ratio of flying dust and water in 1:1 or so), the present invention enters the water of evaporative crystallization about
For the one third of existing three-level adverse current hydraulic art, therefore, for realization Treated sewage reusing purpose, existing three-level adverse current hydraulic art is being steamed
The evaporation capacity of hair crystallisation step is the three times or so of evaporation capacity of the present invention, and therefore, energy consumption of the invention is only the three of the prior art
/ mono- or so.
Comparative example 1:
By taking three-level adverse current is washed as an example, third level washing uses mass ratio=1:1 of flying dust and water, certain flying dust sample is through non-wet process
The technique (wet grinding steps not being added, the first order washes the quality 1:1 of flying dust and water, the other the same as in Example 1 technique) of grinding,
Chloride ion content about 1.4%(is in terms of dry weight in flying dust after washing), being further added by washing series can not also reduce.It is wet using being added
The same process of the present invention of method grinding, chloride ion content about 0.9%(is with dry weight in the flying dust after the washing of same flying dust sample
Meter), chloride ion content reduces 0.5 percentage point, significantly improves the dissolution rate of chloride ion in flying dust, can not by multi-stage water wash
Chloride ion content lower limit in flying dust is reduced to further decrease.
Comparative example 2:
By taking three-level adverse current is washed as an example, third level washing uses mass ratio=1:3 of flying dust and water, certain flying dust sample is through non-wet process
The technique (wet grinding not being added, the first order washes the quality 1:1 of flying dust and water, the other the same as in Example 4) of grinding, after washing
Chloride ion content about 1.1%(is in terms of dry weight in flying dust), being further added by washing series can not also reduce.Using addition wet grinding
Same process of the present invention, chloride ion content about 0.8%(is in terms of dry weight in the flying dust after the washing of same flying dust sample), chloride ion
Content reduces 0.3 percentage point, significantly improves the dissolution rate of chloride ion in flying dust, and multi-stage water wash can not be reduced in flying dust
Chloride ion content lower limit further decreases.
For different flying dust raw materials, the technique that wet grinding is added is compared with the technique that wet grinding is not added, can be shown
The dissolution rate for improving chloride ion in flying dust is write, multi-stage water wash can not be reduced into chloride ion content lower limit in flying dust and further decreased,
The chloride ion content in flying dust after washing can reduce by 0.2 ~ 0.5 percentage point.
Above-mentioned embodiment is only a preferred solution of the present invention, not the present invention is made in any form
Limitation, there are also other variations and modifications on the premise of not exceeding the technical scheme recorded in the claims.
Claims (10)
1. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate, including flying dust washing, removing heavy-metal, decoloration, deliming
And evaporative crystallization steps, the flying dust washing are that multi-stage countercurrent is washed, which is characterized in that before flying dust water-washing step, to flying dust
Wet grinding is carried out, the slurry formed after wet grinding enters back into flying dust water-washing step, and when flying dust carries out wet grinding, control flies
Water consumption+flying dust wet grinding water of mass ratio=1:0.3-0.5 of ash and water, the first order washing of multi-stage countercurrent washing are used
The sum of amount and flying dust mass ratio=1 ~ 1.1:1 are separated by solid-liquid separation after first order washing, and solid enters next stage after crushing and washes,
Liquid enters removing heavy-metal step.
2. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 1, it is characterised in that: institute
Stating flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1 ~ 1.1:1；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:1 ~ 1.1 of flying dust and water are washed in mass ratio=1:0.3-0.5, the second level；
It being separated by solid-liquid separation after third level washing, solid send the water source washed to cement kiln synergic processing, liquid as the second level,
Mass ratio=1:1 ~ 1.1 of the third level washing flying dust and water.
3. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate, including flying dust washing, removing heavy-metal, decoloration, deliming
And evaporative crystallization steps, or including flying dust washing, removing heavy-metal, decoloration and evaporative crystallization steps, which is characterized in that in flying dust
Before water-washing step, wet grinding is carried out to flying dust, the slurry formed after wet grinding enters back into flying dust water-washing step, and flying dust carries out
When wet grinding, mass ratio=1:0.3-0.5 of flying dust and water is controlled, the flying dust washing is that multi-stage countercurrent is washed, to multistage inverse
The water lotion for the afterbody washing that flowing water is washed carries out reverse osmosis membrane desalting processing, and the clear water that reverse osmosis membrane desalting processing generates is made
For the water source washed as upper level of concentrated water that the water source reuse of afterbody washing, reverse osmosis membrane desalting processing generate, first
The sum of water consumption+flying dust wet grinding water consumption of grade washing and flying dust mass ratio=1 ~ 1.1:1, carry out after first order washing
It is separated by solid-liquid separation, solid enters next stage after crushing and washes, and liquid enters removing heavy-metal step.
4. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 3, it is characterised in that: institute
Stating flying dust washing is three-level adverse current washing, including first order washing, second level washing and third level washing；
It being separated by solid-liquid separation after first order washing, solid enters the second level after crushing and washes, and liquid enters removing heavy-metal step, the
The sum of the water consumption of one-stage water wash+flying dust wet grinding water consumption and flying dust mass ratio=1 ~ 1.1:1；
It is separated by solid-liquid separation after the washing of the second level, solid enters the third level after crushing and washes, and liquid a part is as flying dust wet process
The water source of grinding, water source that liquid residual part is washed as the first order, wherein flying dust carries out flying dust and water when wet grinding
Mass ratio=1:0.3-0.5；
It being separated by solid-liquid separation after third level washing, solid is sent to cement kiln synergic processing, and liquid uses reverse osmosis membrane desalting processing,
The water source that the concentrated water that reverse osmosis membrane desalting processing generates is washed as the second level, the clear water conduct that reverse osmosis membrane desalting processing generates
The water source reuse of third level washing, the third level wash mass ratio=1:2.5 ~ 4 of flying dust and water.
5. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 1 or 3, feature exist
In: aeration stirring is carried out in multi-stage countercurrent water-washing process to flying dust except ammonia, the washing pool top of every one-stage water wash is equipped with ammonia
Gas recovery port absorbs to sending ammonia to ammonia absorption tower, the ammonium hydroxide reuse of formation to power plant's denitration.
6. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 1 or 3, feature exist
In: the water source reuse that the distilled water that evaporative crystallization steps generate is washed as afterbody.
7. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 1 or 3, feature exist
In: the removing heavy-metal step are as follows: under stirring condition, is washed in gained filtrate to flying dust and be slowly added to sodium sulfide solution, until
Until the oxidation-reduction potential of system reaches 0 ~ -50mV, solution of ferrous chloride is then added, until the oxidation-reduction potential of system
Until reaching -100 ~ -150mV.
8. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 7, it is characterised in that: sulphur
The mass concentration for changing sodium solution is 2-5%；The mass concentration of solution of ferrous chloride is 3-10%.
9. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 1 or 3, feature exist
In: the decoloration to add active carbon into the filtrate after removing heavy-metal, activated carbon dosage be the one thousandth of filtrate weight extremely
5/1000ths, 3-10min is stirred, filtering is collected filter residue and stored as dangerous waste, and filtrate enters to be handled in next step.
10. a kind of garbage flying ash treatment process for improving chloride ion dissolution rate according to claim 1 or 3, feature exist
In: the deliming is, to sodium carbonate or sodium sulphate is added in gained filtrate after decoloration, stirs 10-20min, filters, collection solid
Partial calcium carbonate or calcium sulfate, filtrate enters to be handled in next step.
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| CN112605097A (en) * | 2020-11-30 | 2021-04-06 | 宝武集团环境资源科技有限公司 | Pretreatment method and harmless treatment process of incineration fly ash or sintering ash |
| CN112797419A (en) * | 2020-12-22 | 2021-05-14 | 江山市虎鼎环保科技有限公司 | High-efficiency homogeneous feeding process for fly ash generated by burning household garbage |
| CN112723768A (en) * | 2020-12-28 | 2021-04-30 | 陈磊 | Fly ash cleaning method |
| CN113413996A (en) * | 2021-06-28 | 2021-09-21 | 中国水利水电第九工程局有限公司 | Sand processing plant vertical shaft crusher sand wet method quantitative powder removal regulation and control method |
| CN114682197A (en) * | 2022-03-10 | 2022-07-01 | 内蒙古恒星化学有限公司 | Dechlorination method for dimethyl dichlorosilane hydrolysate |
| CN114682197B (en) * | 2022-03-10 | 2024-03-08 | 内蒙古恒星化学有限公司 | Method for removing chlorine from dimethyl dichlorosilane hydrolysate |
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