CN109399853A - The processing unit of ammonia nitrogen waste water - Google Patents
The processing unit of ammonia nitrogen waste water Download PDFInfo
- Publication number
- CN109399853A CN109399853A CN201811497162.5A CN201811497162A CN109399853A CN 109399853 A CN109399853 A CN 109399853A CN 201811497162 A CN201811497162 A CN 201811497162A CN 109399853 A CN109399853 A CN 109399853A
- Authority
- CN
- China
- Prior art keywords
- liquid
- component
- outlet
- ammonia
- processing unit
- 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.)
- Granted
Links
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 239000002351 wastewater Substances 0.000 title claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 142
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 68
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 34
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 238000001704 evaporation Methods 0.000 claims abstract description 30
- 230000008020 evaporation Effects 0.000 claims abstract description 24
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000000908 ammonium hydroxide Substances 0.000 claims abstract description 21
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 11
- 230000003750 conditioning effect Effects 0.000 claims description 8
- 239000006228 supernatant Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000000706 filtrate Substances 0.000 claims description 7
- 239000003002 pH adjusting agent Substances 0.000 claims description 7
- 239000013078 crystal Substances 0.000 claims description 5
- 238000011085 pressure filtration Methods 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 238000010025 steaming Methods 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 12
- 238000011282 treatment Methods 0.000 abstract description 9
- 230000036571 hydration Effects 0.000 abstract description 6
- 238000006703 hydration reaction Methods 0.000 abstract description 6
- 229910052751 metal Inorganic materials 0.000 abstract description 3
- 239000002184 metal Substances 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 26
- 230000008569 process Effects 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 208000028659 discharge Diseases 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 238000009388 chemical precipitation Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 230000005764 inhibitory process Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000004254 Ammonium phosphate Substances 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 229910000148 ammonium phosphate Inorganic materials 0.000 description 1
- 235000019289 ammonium phosphates Nutrition 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Substances N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
Abstract
The present invention provides a kind of processing units of ammonia nitrogen waste water.The processing unit includes: that pH value adjusts component, is adjusted for the pH value to the ammonia nitrogen waste water being passed through to obtain adjusting liquid；It is separated by solid-liquid separation component, the outlet of component is adjusted with pH value, for being separated by solid-liquid separation adjusting liquid to obtain handling preceding liquid；And evaporative component is handled with the outlet for being separated by solid-liquid separation component for being evaporated to liquid before handling to obtain liquid after ammonium hydroxide and processing.Due to there are a large amount of volatile hydration ammonia before above-mentioned processing in liquid, to which the most ammonia-nitrogen in liquid can be made to form ammonia after evaporation, and then make liquid after the processing obtained after evaporation that there is lower ammonia-nitrogen content and content of beary metal, it can satisfy discharge standard, above-mentioned apparatus structure is simple, low energy consumption, treatment effeciency is high, thermal energy consumption is low, operating cost is low；The ammonia that above-mentioned evaporation generates also is easy to be collected after end effect condenses, to avoid direct outlet pollution on the environment.
Description
Technical field
The present invention relates to industrial waste water treatments, in particular to a kind of processing unit of ammonia nitrogen waste water.
Background technique
With getting worse for Water Eutrophication problem, in the processing of industrial wastewater, the removal of ammonia nitrogen is up to standard to be become
Handle the bottleneck of this kind of wastewater treatment.Currently used ammonia nitrogen handling arrangement have air stripping method, stripping rectification method, ammonia still process method,
Bioanalysis etc., the more current way of processing high-concentration ammonia nitrogenous wastewater is in domestic and international production practices: first ammonia nitrogen in high density giving up
Ammonia nitrogen in waste water is dropped to 200mg/L hereinafter, then with A/O method or chemical precipitation method (ammonium phosphate by stripping or stripping by water
Magnesium salts method) carry out subsequent processing.But there are several critical defects:
1) A/O method not only invests height, but also takes up a large area, and the requirement to pretreatment water outlet is harsh；
2) chemical precipitation method reagent consumption amount is too big, and treatment agent cost is too high, and water outlet is also unable to reach country one
Grade or secondary discharge standard；
3) ammonia aeration treatment process, stripping efficiency can only achieve 85-90%, and ammonia stripping enters and causes two in atmosphere
Secondary pollution；
4) domestic mature Ammonia-nitrogen wastewater treatment technology mostly uses stripping deamination technique, and equipment mostly uses tower, and traditional
The stripper steam mono-consumption that ammonia nitrogen waste water is handled under process conditions is higher, and waste water per ton often reaches 200~300kg steam consumption quantity.
Problem above seriously hinders the popularization and application of technology, and low energy consumption, less scaling, becomes Technique Popularizing
Important breakthrough point.
Summary of the invention
The main purpose of the present invention is to provide a kind of processing units of ammonia nitrogen waste water, useless to solve ammonia nitrogen in the prior art
The processing unit of water easily causes pollution and the high problem of energy consumption.
To achieve the goals above, a kind of processing unit of ammonia nitrogen waste water is provided, comprising: pH value adjusts component, is used for
The pH value for the ammonia nitrogen waste water being passed through is adjusted to obtain adjusting liquid；It is separated by solid-liquid separation component, the outlet of component is adjusted with pH value
Connection, for being separated by solid-liquid separation adjusting liquid to obtain handling preceding liquid；And evaporative component, with the outlet for being separated by solid-liquid separation component
Connection, for being evaporated processing to liquid before handling to obtain liquid after ammonium hydroxide and processing.
Further, it includes: reactive tank that pH value, which adjusts component, for being passed through ammonia nitrogen waste water；Regulator conveyance conduit, and it is anti-
Slot is answered to be connected to, for being passed through pH adjusting agent into reactive tank.
Further, being separated by solid-liquid separation component includes solid-liquid separating equipment, and solid-liquid separating equipment includes rinsing maching and concentrator,
Rinsing maching is pressure filtration washing machine or centrifugal filtration rinsing maching, and concentrator and pH value adjust the outlet of component, for that will adjust
For the dense sedimentation of liquid to obtain supernatant and the dense liquid of underflow, concentrator has first outlet and second outlet, rinsing maching and first
Outlet, for underflow dense hydraulic filter washing in part to be obtained to filtrate and filter residue, the outlet and second outlet of rinsing maching
Be connected to respectively with the entrance of evaporative component, for make the mixed liquor of supernatant and filtrate as the processing of evaporative component is passed through before
Liquid.
Further, it is separated by solid-liquid separation component further include: the first feeder trough adjusts the outlet of component with pH value；First
Feed pump is connected to the entrance of the outlet of the first feeder trough and solid-liquid separating equipment respectively.
Further, evaporative component includes: evaporator, and with the outlet for being separated by solid-liquid separation component, evaporator includes heat exchange
Pipe, liquid and comprising the secondary steam of ammonia after heat exchanger tube is handled for liquid before handle and primary steam heat exchange；It is cold
Condenser is connected to evaporator, for condensing secondary steam to obtain ammonium hydroxide；Steam pipeline is connected to evaporator, is used for
Primary steam is conveyed into evaporator.
Further, evaporative component further include: the second feeder trough, with the outlet for being separated by solid-liquid separation component；Second feed
Pump, is connected to the entrance of the outlet of the second feeder trough and evaporator.
Further, concentrator also has third outlet, and evaporative component further includes dope feed-line, dope feed-line
Respectively with third outlet and the second feeder trough be connected to, for by the dense liquid of part underflow be delivered in the second feeder trough with before processing
To obtain evaporating preceding liquid, evaporator exchanges heat for liquid before evaporating and primary steam for liquid and the mixing of calcium sulfate crystal seed.
Further, evaporative component further include: condensate pump is connected to evaporator, is used for primary steam after heat exchange
The condensed water of formation is discharged；Concentrated water pump, is connected to evaporator, is discharged for liquid after handling；Concentrated ammonia liquor pump, connects with evaporator
It is logical, for ammonium hydroxide to be discharged.
Further, processing unit further include: Ammonia vessel is connected to concentrated ammonia liquor pump；Ammonium hydroxide delivery pump, with Ammonia vessel
Outlet.
Further, processing unit further include: conditioning tank, the entrance for adjusting component with pH value are connected to；Waste water lifting pump, point
The entrance for not adjusting component with the outlet of conditioning tank and pH value is connected to.
It applies the technical scheme of the present invention, provides a kind of processing unit of ammonia nitrogen waste water, the pH value in the processing unit
The pH value of ammonia nitrogen waste water can be adjusted to alkalinity by adjusting component, so that the ammonium ion in ammonia nitrogen waste water is easily converted into a hydration ammonia,
Obtained adjusting liquid can be separated by solid-liquid separation by being separated by solid-liquid separation component, to remove the impurity such as the heavy metal in ammonia nitrogen waste water, and
It improves ammonia nitrogen purity to obtain handling preceding liquid, evaporative component can be evaporated processing to liquid before the processing, due to above-mentioned processing
There are a large amount of volatile hydration ammonia in preceding liquid, so that the most ammonia-nitrogen in liquid can be made to form ammonia after evaporation,
And then make liquid after the processing obtained after evaporation that there is lower ammonia-nitrogen content and content of beary metal, it can satisfy discharge standard, on
It states that device is not only simple in structure, low energy consumption, treatment effeciency is high, thermal energy consumption is low, operating cost is low, and is generated after above-mentioned evaporation
Ammonia also be easy be collected after condensation, to avoid direct outlet pollution on the environment.
Detailed description of the invention
The Figure of description for constituting a part of the invention is used to provide further understanding of the present invention, and of the invention shows
Examples and descriptions thereof are used to explain the present invention for meaning property, does not constitute improper limitations of the present invention.In the accompanying drawings:
Fig. 1 shows a kind of structural schematic diagram of the processing unit of ammonia nitrogen waste water provided by the present invention.
Wherein, the above drawings include the following reference numerals:
10, conditioning tank；20, waste water lifting pump；30, pH value adjusts component；40, it is separated by solid-liquid separation component；410, the first feed
Slot；420, the first feed pump；430, solid-liquid separating equipment；50, evaporative component；510, the second feeder trough；520, the second feed pump；
530, evaporator；540, condensate pump；550, concentrated water pumps；560, concentrated ammonia liquor pumps；60, Ammonia vessel；70, ammonium hydroxide delivery pump.
Specific embodiment
It should be noted that in the absence of conflict, the feature in embodiment and embodiment in the present invention can phase
Mutually combination.The present invention will be described in detail below with reference to the accompanying drawings and embodiments.
In order to enable those skilled in the art to better understand the solution of the present invention, below in conjunction in the embodiment of the present invention
Attached drawing, technical scheme in the embodiment of the invention is clearly and completely described, it is clear that described embodiment is only
The embodiment of a part of the invention, instead of all the embodiments.Based on the embodiments of the present invention, ordinary skill people
The model that the present invention protects all should belong in member's every other embodiment obtained without making creative work
It encloses.
It should be noted that description and claims of this specification and term " first " in above-mentioned attached drawing, "
Two " etc. be to be used to distinguish similar objects, without being used to describe a particular order or precedence order.It should be understood that using in this way
Data be interchangeable under appropriate circumstances, so as to the embodiment of the present invention described herein.In addition, term " includes " and " tool
Have " and their any deformation, it is intended that cover it is non-exclusive include, for example, containing a series of steps or units
Process, method, system, product or equipment those of are not necessarily limited to be clearly listed step or unit, but may include without clear
Other step or units listing to Chu or intrinsic for these process, methods, product or equipment.
It can be seen from background technology that the processing method of ammonia nitrogen waste water easily causes pollution in the prior art and energy consumption is high, serious to hinder
Hinder the popularization and application of technology, and it is low energy consumption, less scaling, become the important breakthrough point of Technique Popularizing.Invention of the invention
People studies regarding to the issue above, provides a kind of processing unit of ammonia nitrogen waste water, as shown in Figure 1, including pH value adjusting group
Part 30 is separated by solid-liquid separation component 40 and evaporative component 50, and pH value adjusts component 30 and is used to carry out the pH value for the ammonia nitrogen waste water being passed through
It adjusts to obtain adjusting liquid；It is separated by solid-liquid separation component 40 and pH value adjusts the outlet of component 30, for consolidating to adjusting liquid
Liquid is separated to obtain handling preceding liquid；Evaporative component 50 and the outlet for being separated by solid-liquid separation component 40, for being carried out to liquid before handling
Evaporation process is to obtain liquid after ammonium hydroxide and processing.
PH value, which adjusts component, in above-mentioned processing unit of the invention can adjust the pH value of ammonia nitrogen waste water to alkalinity, so that
Ammonium ion in ammonia nitrogen waste water is easily converted into a hydration ammonia, and solid-liquid point can be carried out to obtained adjusting liquid by being separated by solid-liquid separation component
From to remove the impurity such as the heavy metal in ammonia nitrogen waste water, and improving ammonia nitrogen purity and obtain handling preceding liquid, evaporative component can be to place
Liquid is evaporated processing before managing, due to there are a large amount of volatile hydration ammonia before above-mentioned processing in liquid, to after evaporation can
So that most ammonia-nitrogen in liquid is formed ammonia, so make after the processing obtained after evaporation liquid have lower ammonia-nitrogen content and
Content of beary metal can satisfy discharge standard, and above-mentioned apparatus is not only simple in structure, low energy consumption, treatment effeciency is high, thermal energy consumption
It is low, operating cost is low, and the ammonia generated after above-mentioned evaporation also be easy be collected after condensation, to avoid direct outlet
Pollution on the environment.
The ammonia nitrogen concentration of the above-mentioned ammonia nitrogen waste water as process object can be 1~100g/L.Due in ammonia nitrogen waste water
Ammonia nitrogen is mainly with free ammonia (NH3) and ammonium ion (NH4 +) form exist, so the ammonia nitrogen concentration of above-mentioned ammonia nitrogen waste water is
Refer to free ammonia (NH in ammonia nitrogen waste water3) and ammonium ion (NH4 +) concentration summation.
In above-mentioned processing unit of the invention, it is preferable that processing unit further includes conditioning tank 10 and waste water lifting pump 20,
Conditioning tank 10 is connected to the entrance that pH value adjusts component 30；Waste water lifting pump 20 respectively with the outlet of conditioning tank 10 and pH value tune
The entrance connection of component 30 is saved, as shown in Figure 1.After logical liquid the first feeder trough 410 of addition by adjusting, waste water can be passed through by adjusting liquid
Elevator pump 20 is pumped to the pH value that ammonia nitrogen waste water is adjusted in reactive tank.
In above-mentioned processing unit of the invention, it is preferable that it includes that reactive tank and regulator convey that pH value, which adjusts component 30,
Pipeline, reactive tank is for being passed through ammonia nitrogen waste water；Regulator conveyance conduit is connected to reactive tank, for being passed through pH value into reactive tank
Regulator.Ammonia nitrogen waste water can be added in reactive tank, and pH value adjusting is added into reactive tank by regulator conveyance conduit
Agent, to adjust the pH value of ammonia nitrogen waste water, those skilled in the art can be using pH adjusting agent such as stone conventional in the prior art
Grey cream or sodium hydroxide；It is further preferable that the pH value of ammonia nitrogen waste water is adjusted to 11.5~12, so as to can have in ammonia nitrogen waste water
More ammonium ion (NH4 +) it is converted into a hydration ammonia.
In above-mentioned processing unit of the invention, being separated by solid-liquid separation component 40 may include solid-liquid separating equipment 430, preferably
Ground, above-mentioned solid-liquid separating equipment 430 include concentrator and rinsing maching (not shown), the rinsing maching be pressure filtration washing machine or from
Heart filtration washing machine, concentrator and pH value adjust the outlet of component 30, for that will adjust the dense sedimentation of liquid to obtain supernatant
Liquid and the dense liquid of underflow, concentrator have first outlet and second outlet, and rinsing maching is connected to first outlet, are used for part bottom
Dense liquid washing is flowed to obtain filtrate and filter residue, and the outlet of rinsing maching and second outlet connect with the entrance of evaporative component 50 respectively
It is logical, for making the mixed liquor of supernatant and filtrate as liquid before the processing for being passed through evaporative component 50.
Specifically, adjusting liquid is passed through in concentrator and is separated by solid-liquid separation by gravitational settling effect, above-mentioned adjusting liquid exists
After gravitational settling concentration be the higher bottom slurry of solid content (the i.e. above-mentioned dense liquid of underflow), while concentrator top generate compared with
For peace and quiet overflowing liquid (i.e. above-mentioned supernatant), subsequent evaporation is carried out as a part in liquid before handling using the overflowing liquid
Processing；Then, underflow dense liquid in part is separated by solid-liquid separation using rinsing maching, by taking pressure filtration washing machine as an example, by part underflow
Dense liquid, which is passed through in pressure filtration washing machine, realizes separation of solid and liquid by filter medium, and the filter residue on filter medium (such as filter cloth) is by washing
It washs and is discharged after forming cleaning solution, filtrate and above-mentioned supernatant are collectively as the subsequent evaporation process of liquid progress before handling.
In above-mentioned processing unit of the invention, it is preferable that being separated by solid-liquid separation component 40 further includes the first feeder trough 410 and the
One feed pump 420, the first feeder trough 410 adjust the outlet of component 30 with pH value；First feed pump 420 is given with first respectively
The outlet of hopper 410 and the entrance connection of solid-liquid separating equipment 430.After logical liquid the first feeder trough 410 of addition by adjusting, adjust
Liquid can be pumped in solid-liquid separating equipment 430 by the first feed pump 420 and is separated by solid-liquid separation to obtain handling preceding liquid.
In above-mentioned processing unit of the invention, it is preferable that evaporative component 50 includes evaporator 530, condenser and steam
Feed-line, evaporator 530 and the outlet for being separated by solid-liquid separation component 40, evaporator 530 include heat exchanger tube, which is used for
Liquid obtains liquid and the secondary steam comprising above-mentioned ammonia after above-mentioned processing with primary steam heat exchange before handling；Condenser
It is connected to above-mentioned evaporator 530, for condensing secondary steam to obtain ammonium hydroxide.As shown in fig. 1, above-mentioned condenser respectively with
Cooling water-supply line and the connection of cooling backwater pipeline, circulating cooling water supply is passed through in the condenser and above-mentioned secondary steaming when work
Vapour heat exchange is discharged as circulating cooling return water from the condenser after heat exchange so that secondary steam be condensed to obtain ammonium hydroxide；Steam is defeated
Pipeline is sent to be connected to evaporator 530, for conveying primary steam into evaporator 530.Liquid is passed through with primary steam before handling
It exchanges heat in evaporator, liquid evaporates to form secondary steam before handling, and the concentrate after evaporation is liquid after handling, above-mentioned
Secondary steam is also used as being passed through in evaporator with the primary steam for handling preceding liquid heat exchange.
Above-mentioned evaporator 530 can be single effect evaporator, or multi-effect evaporator, at this point, the secondary steaming of a upper effect
The primary steam of liquid heat exchange before vapour can be used as next effect and handle.The evaporator 530 of above-mentioned single-action or multiple-effect can be falling liquid film
Evaporator, mixed vapour flows in heat exchanger tube in evaporator 530, and liquid forms film, multiple-effect evaporation through spray in pipe outer wall
The effect number of device is according to depending on practical water quality situation, and about 4 DEG C of the temperature difference between effect, 30 DEG C of temperature difference can arrange 6~7 effects, using multiple-effect evaporation
Device considerably increases efficiency of energy utilization.
Above-mentioned evaporative component 50 can also include the second feeder trough 510 and the second feed pump 520, the second feeder trough 510 with
It is separated by solid-liquid separation the outlet of component 40；Second feed pump 520 and the second outlet of feeder trough 510 and entering for evaporator 530
Mouth connection.After logical the second feeder trough 510 of preceding liquid addition by processing, steaming can be pumped to by the second feed pump 520 by handling preceding liquid
Processing is evaporated in hair device 530 to remove liquid after most ammonia nitrogen is handled.
In a preferred embodiment, above-mentioned concentrator also has third outlet, and evaporative component 50 further includes dope
Feed-line, dope feed-line is connected to third outlet and the second feeder trough 510 respectively, for the dense liquid of part underflow is defeated
It send into the second feeder trough 510 and is mixed with liquid and calcium sulfate crystal seed before processing to obtain evaporating preceding liquid, evaporator 530 is used for will
Liquid and primary steam exchange heat before evaporating.
In above-mentioned preferred embodiment, by dope feed-line can will the dense liquid of the underflow of part and processing before
Liquid and calcium sulfate crystal seed mix in the second feeder trough 510, to carry out subsequent evaporation process as liquid before evaporation, scale inhibition
Mechanism is mainly that calcium sulfate seed surface has suction-operated to scale inhibition agent molecule, to inhibit CaCO3、CaSO4Crystallization it is raw
It is long, so as to the fouling being effectively prevented from subsequent evaporation treatment process；Also, in traditional handicraft in order to avoid fouling
It needs to do pH adjusting agent using sodium hydroxide and compare, the pH adjusting agent in the present invention can use calcium hydroxide, to drop
Low Waste water treatment medicament cost.
In above-mentioned processing unit of the invention, it is preferable that evaporative component 50 further includes condensate pump 540, concentrated water pump 550
With concentrated ammonia liquor pump 560, condensate pump 540 is connected to evaporator 530, the condensed water row for forming primary steam after heat exchange
Out；Concentrated water pump 550 is connected to evaporator 530, is discharged for liquid after handling；Concentrated ammonia liquor pump 560 is connected to evaporator 530, is used
It is discharged in the ammonium hydroxide for forming ammonia condensation in secondary steam.Primary steam can exchanged heat by above-mentioned condensate pump 540
The condensate-water polishing that is formed afterwards utilizes, and the concentrate after evaporation can satisfy discharge standard, thus by above-mentioned concentrated water pump 550 into
Row discharge is discharged, with further progress by the ammonium hydroxide that above-mentioned concentrated ammonia liquor pump 560 can be formed ammonia condensation in secondary steam
It recycles.
In order to realize the recycling of the ammonium hydroxide formed to above-mentioned ammonia condensation, it is further preferable that above-mentioned processing unit is also
Including Ammonia vessel 60 and ammonium hydroxide delivery pump 70, Ammonia vessel 60 is connected to concentrated ammonia liquor pump 560；Ammonium hydroxide delivery pump 70 and ammonium hydroxide store up
The outlet of slot 60.It can be pumped to above-mentioned in desulphurization system into ammonium hydroxide in Ammonia vessel 60 by ammonium hydroxide delivery pump 70
It is recycled.
It can be seen from the above description that the above embodiments of the present invention realized the following chievements:
1, ammonia nitrogen waste water can be made to form the secondary steam comprising ammonia after treatment using above-mentioned processing unit, after evaporation
Concentrate can satisfy industrial discharge standard；
2, above-mentioned apparatus is not only simple in structure, low energy consumption, treatment effeciency is high, thermal energy consumption is low, operating cost is low, Er Qieshang
It states the ammonia generated after evaporation to be also easy to be collected after condensation, to avoid direct outlet pollution on the environment；
3, evaporative component further includes dope feed-line, by dope feed-line can by the dense liquid of the underflow of part with
Liquid and the mixing of calcium sulfate crystal seed are used as liquid before evaporating to carry out subsequent evaporation process before handling, so as to be effectively prevented from
Fouling in subsequent evaporation treatment process, in traditional handicraft in order to avoid fouling needs to do pH adjusting agent using sodium hydroxide
It compares, the pH adjusting agent in the present invention can use calcium hydroxide, to reduce Waste water treatment medicament cost.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, made any to repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of processing unit of ammonia nitrogen waste water characterized by comprising
PH value adjusts component (30), is adjusted for the pH value to the ammonia nitrogen waste water being passed through to obtain adjusting liquid；
It is separated by solid-liquid separation component (40), the outlet of component (30) is adjusted with the pH value, for consolidating to the adjusting liquid
Liquid is separated to obtain handling preceding liquid；And
Evaporative component (50), the outlet with separation of solid and liquid component (40), for being evaporated to liquid before the processing
Processing is to obtain liquid after ammonium hydroxide and processing.
2. processing unit according to claim 1, which is characterized in that the pH value adjusts component (30) and includes:
Reactive tank, for being passed through the ammonia nitrogen waste water；
Regulator conveyance conduit is connected to the reactive tank, for being passed through pH adjusting agent into the reactive tank.
3. processing unit according to claim 1, which is characterized in that the separation of solid and liquid component (40) includes being separated by solid-liquid separation
Equipment (430), the solid-liquid separating equipment (430) include rinsing maching and concentrator, the rinsing maching be pressure filtration washing machine or from
Heart filtration washing machine, the concentrator and the pH value adjust the outlet of component (30), for the adjusting liquid is dense
To obtain supernatant and the dense liquid of underflow, the concentrator has first outlet and second outlet, the rinsing maching and institute for sedimentation
State first outlet connection, for by the dense hydraulic filter washing of the part underflow to obtain filtrate and filter residue, the rinsing maching
Outlet and the second outlet are connected to the entrance of the evaporative component (50) respectively, for making the supernatant and the filtrate
Mixed liquor as liquid before the processing for being passed through evaporative component (50).
4. processing unit according to claim 3, which is characterized in that the separation of solid and liquid component (40) further include:
First feeder trough (410) adjusts the outlet of component (30) with the pH value；
First feed pump (420), respectively with the outlet of first feeder trough (410) and the solid-liquid separating equipment (430)
Entrance connection.
5. processing unit according to claim 3, which is characterized in that the evaporative component (50) includes:
Evaporator (530), with the outlet for being separated by solid-liquid separation component (40), the evaporator (530) includes heat exchanger tube, institute
Heat exchanger tube is stated for liquid before the processing and primary steam heat exchange to be obtained to after the processing liquid and comprising the secondary of ammonia
Steam；
Condenser is connected to the evaporator (530), for condensing the secondary steam to obtain the ammonium hydroxide；
Steam pipeline is connected to the evaporator (530), for the conveying primary steaming into the evaporator (530)
Vapour.
6. processing unit according to claim 5, which is characterized in that the evaporative component (50) further include:
Second feeder trough (510), with the outlet for being separated by solid-liquid separation component (40)；
Second feed pump (520) is connected to the entrance of the outlet of second feeder trough (510) and the evaporator (530).
7. processing unit according to claim 6, which is characterized in that the concentrator also has third outlet, the steaming
Sending out component (50) further includes dope feed-line, and the dope feed-line is fed with third outlet and described second respectively
Slot (510) connection, for by the part dense liquid of the underflow be delivered in the second feeder trough (510) with liquid before the processing and
To obtain evaporating preceding liquid, the evaporator (530) is used for liquid before the evaporation and the primary steam mixing of calcium sulfate crystal seed
Heat exchange.
8. processing unit according to claim 5, which is characterized in that the evaporative component (50) further include:
Condensate pump (540) is connected to, the condensation for forming the primary steam after heat exchange with the evaporator (530)
Water discharge；
Concentrated water pumps (550), is connected to the evaporator (530), for liquid after the processing to be discharged；
Concentrated ammonia liquor pumps (560), is connected to the evaporator (530), for the ammonium hydroxide to be discharged.
9. processing unit according to claim 8, which is characterized in that the processing unit further include:
Ammonia vessel (60) is connected to concentrated ammonia liquor pump (560)；
Ammonium hydroxide delivery pump (70), the outlet with the Ammonia vessel (60).
10. processing unit according to claim 1, which is characterized in that the processing unit further include:
Conditioning tank (10), the entrance for adjusting component (30) with the pH value are connected to；
Waste water lifting pump (20), the entrance for adjusting component (30) with the outlet of the conditioning tank (10) and pH value respectively are connected to.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811497162.5A CN109399853B (en) | 2018-12-07 | 2018-12-07 | Ammonia nitrogen wastewater treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811497162.5A CN109399853B (en) | 2018-12-07 | 2018-12-07 | Ammonia nitrogen wastewater treatment device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109399853A true CN109399853A (en) | 2019-03-01 |
| CN109399853B CN109399853B (en) | 2024-04-16 |
Family
ID=65457983
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811497162.5A Active CN109399853B (en) | 2018-12-07 | 2018-12-07 | Ammonia nitrogen wastewater treatment device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109399853B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113680109A (en) * | 2021-08-30 | 2021-11-23 | 赣州科清环境工程有限公司 | Movable device and method for dense dehydration of sediments of medium-low ammonia nitrogen leacheate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456635A (en) * | 2008-12-17 | 2009-06-17 | 深圳市能源环保有限公司 | Process and system for treating electric power plant waste water |
| CN102923905A (en) * | 2012-10-19 | 2013-02-13 | 佛山市新泰隆环保设备制造有限公司 | Method and devices for treating rare-earth-smelting wastewater |
| CN103466870A (en) * | 2013-08-22 | 2013-12-25 | 苏州苏净环保工程有限公司 | Material recovery method of wastewater containing high-concentration ammonia-nitrogen and heavy metal ions and treatment system |
| CN209412000U (en) * | 2018-12-07 | 2019-09-20 | 中国恩菲工程技术有限公司 | The processing unit of ammonia nitrogen waste water |
-
2018
- 2018-12-07 CN CN201811497162.5A patent/CN109399853B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456635A (en) * | 2008-12-17 | 2009-06-17 | 深圳市能源环保有限公司 | Process and system for treating electric power plant waste water |
| CN102923905A (en) * | 2012-10-19 | 2013-02-13 | 佛山市新泰隆环保设备制造有限公司 | Method and devices for treating rare-earth-smelting wastewater |
| CN103466870A (en) * | 2013-08-22 | 2013-12-25 | 苏州苏净环保工程有限公司 | Material recovery method of wastewater containing high-concentration ammonia-nitrogen and heavy metal ions and treatment system |
| CN209412000U (en) * | 2018-12-07 | 2019-09-20 | 中国恩菲工程技术有限公司 | The processing unit of ammonia nitrogen waste water |
Non-Patent Citations (1)
| Title |
|---|
| 宋妙发等: "《核环境学基础》", 原子能出版社, pages: 284 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113680109A (en) * | 2021-08-30 | 2021-11-23 | 赣州科清环境工程有限公司 | Movable device and method for dense dehydration of sediments of medium-low ammonia nitrogen leacheate |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109399853B (en) | 2024-04-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105585194B (en) | One kind contains Na+、K+、NH4+、Cl‑、SO42‑、NO3‑The highly concentrated effluent brine method of comprehensive utilization of coal chemical industry | |
| CN110183025A (en) | Desulfurization wastewater recycling processing method and system | |
| CN109928560A (en) | A kind of zero emission treatment of desulfured waste water and processing unit | |
| CN102329036A (en) | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization | |
| CN109836006B (en) | Efficient concentration crystallization device and process for salt-containing wastewater | |
| CN110540332B (en) | Fluorine-containing and chlorine-containing sewage treatment process | |
| CN106145487A (en) | A kind of technique processing rare-earth trade high-concentration ammonia nitrogenous wastewater reuse | |
| CN210855652U (en) | Treatment device for zero discharge of wastewater in polycrystalline silicon production | |
| CN209412000U (en) | The processing unit of ammonia nitrogen waste water | |
| CN111003717A (en) | Device and method for preparing alkali salt by evaporating and crystallizing sea water desalination strong brine | |
| CN106587477A (en) | System and method for treating industrial waste lye | |
| CN109399853A (en) | The processing unit of ammonia nitrogen waste water | |
| CN206033465U (en) | Coal chemical wastewater preliminary treatment deamination system | |
| CN102963909A (en) | Method for recovering and reutilizing waste ammonia gas in LED (light-emitting diode) manufacturing through ammonia water method | |
| CN204939142U (en) | A kind for the treatment of facility of desulfurization wastewater of flue gas desulphurization system discharge | |
| CN109455862A (en) | The processing method of ammonia nitrogen waste water | |
| CN1214272A (en) | Continuous stirring vacuum sodium sulfate crystallization technology | |
| CN105152405A (en) | Method and device for treating desulfurization wastewater discharged by flue gas desulfurization system | |
| CN115872406A (en) | Hydrogen fluoride wastewater resource utilization system device and method in photovoltaic industry | |
| CN112919506B (en) | Device and method for continuously producing lithium chloride from salt lake lithium-rich brine | |
| CN202208671U (en) | Brine waste zero emission recovering system | |
| CN107487802A (en) | A kind of recycling processing method of high ammonia nitrogen and high salt waste water | |
| CN109455861A (en) | The processing method of ammonia nitrogen waste water | |
| CN213294703U (en) | Fly ash desalination system containing potassium chloride salt | |
| CN112194298B (en) | System and method for recycling wastewater of whole power plant |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant |