CN109399853B - Ammonia nitrogen wastewater treatment device - Google Patents
Ammonia nitrogen wastewater treatment device Download PDFInfo
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- CN109399853B CN109399853B CN201811497162.5A CN201811497162A CN109399853B CN 109399853 B CN109399853 B CN 109399853B CN 201811497162 A CN201811497162 A CN 201811497162A CN 109399853 B CN109399853 B CN 109399853B
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- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 52
- 238000004065 wastewater treatment Methods 0.000 title claims description 11
- 239000007788 liquid Substances 0.000 claims abstract description 122
- 238000001704 evaporation Methods 0.000 claims abstract description 54
- 230000008020 evaporation Effects 0.000 claims abstract description 52
- 238000000926 separation method Methods 0.000 claims abstract description 44
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000002351 wastewater Substances 0.000 claims abstract description 39
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 37
- 238000002203 pretreatment Methods 0.000 claims abstract description 29
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000012545 processing Methods 0.000 claims abstract description 10
- 238000005406 washing Methods 0.000 claims description 21
- 238000004891 communication Methods 0.000 claims description 19
- 239000002562 thickening agent Substances 0.000 claims description 15
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 239000012141 concentrate Substances 0.000 claims description 11
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 10
- 239000006228 supernatant Substances 0.000 claims description 8
- 239000013078 crystal Substances 0.000 claims description 7
- 239000000706 filtrate Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 4
- 238000010979 pH adjustment Methods 0.000 claims description 3
- 230000008719 thickening Effects 0.000 claims description 2
- 229910021529 ammonia Inorganic materials 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 238000009833 condensation Methods 0.000 abstract description 5
- 230000005494 condensation Effects 0.000 abstract description 5
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 22
- 230000008569 process Effects 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- -1 ammonium ions Chemical class 0.000 description 5
- 230000003750 conditioning effect Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000009388 chemical precipitation Methods 0.000 description 3
- 208000028659 discharge Diseases 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000008267 milk Substances 0.000 description 1
- 210000004080 milk Anatomy 0.000 description 1
- 235000013336 milk Nutrition 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002455 scale inhibitor Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012546 transfer Methods 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
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention provides a treatment device for ammonia nitrogen wastewater. The processing device comprises: the pH value adjusting component is used for adjusting the pH value of the introduced ammonia nitrogen wastewater to obtain an adjusting solution; the solid-liquid separation component is communicated with the outlet of the pH value adjusting component and is used for carrying out solid-liquid separation on the adjusting liquid to obtain a pre-treatment liquid; and the evaporation assembly is communicated with the outlet of the solid-liquid separation assembly and is used for carrying out evaporation treatment on the pre-treatment liquid to obtain ammonia water and treated liquid. Because a large amount of volatile ammonia monohydrate exists in the pretreatment liquid, most ammonia nitrogen in the liquid can form ammonia after evaporation, so that the treated liquid obtained after evaporation has lower ammonia nitrogen content and heavy metal content and can meet the emission standard, and the device has the advantages of simple structure, low energy consumption, high treatment efficiency, low heat energy consumption and low running cost; the ammonia gas generated by the evaporation is easy to collect after final condensation, so that the pollution to the environment caused by direct discharge is avoided.
Description
Technical Field
The invention relates to the technical field of industrial wastewater treatment, in particular to a treatment device for ammonia nitrogen wastewater.
Background
With the increasing severity of water eutrophication problems, ammonia nitrogen removal in industrial wastewater treatment becomes a bottleneck in treatment of such wastewater. The ammonia nitrogen treatment device commonly used at present comprises an air stripping method, a stripping rectification method, an ammonia distillation method, a biological method and the like, and the common method for treating high-concentration ammonia nitrogen wastewater in domestic and foreign production practice is as follows: firstly, ammonia nitrogen in the high-concentration ammonia nitrogen wastewater is reduced to below 200mg/L through steam stripping or stripping, and then, the subsequent treatment is carried out by an A/O method or a chemical precipitation method (an ammonium magnesium phosphate method). But has several fatal drawbacks:
1) The A/O method has high investment, large occupied area and severe requirements on pretreatment effluent;
2) The chemical precipitation method has the disadvantages that the consumption of the chemical precipitation method is too large, the cost for treating the chemical is too high, and the effluent can not reach the national primary or secondary discharge standard;
3) The ammonia stripping treatment process has the stripping efficiency of only 85-90%, and ammonia gas is blown into the atmosphere to cause secondary pollution;
4) The domestic mature ammonia nitrogen wastewater treatment process mostly adopts a stripping deamination process, equipment mostly adopts a tower, and the steam unit consumption of a stripping tower for treating ammonia nitrogen wastewater under the traditional process condition is higher, and the steam consumption of each ton of wastewater is often up to 200-300 kg.
The problems seriously obstruct the popularization and application of the technology, and the low energy consumption and difficult scaling become important breakthrough points of the technical popularization.
Disclosure of Invention
The invention mainly aims to provide an ammonia nitrogen wastewater treatment device, which aims to solve the problems that the ammonia nitrogen wastewater treatment device in the prior art is easy to cause pollution and has high energy consumption.
In order to achieve the above object, there is provided a treatment apparatus for ammonia nitrogen wastewater, comprising: the pH value adjusting component is used for adjusting the pH value of the introduced ammonia nitrogen wastewater to obtain an adjusting solution; the solid-liquid separation component is communicated with the outlet of the pH value adjusting component and is used for carrying out solid-liquid separation on the adjusting liquid to obtain a pre-treatment liquid; and the evaporation assembly is communicated with the outlet of the solid-liquid separation assembly and is used for carrying out evaporation treatment on the pre-treatment liquid to obtain ammonia water and treated liquid.
Further, the pH adjustment assembly includes: the reaction tank is used for introducing ammonia nitrogen wastewater; and the regulator conveying pipeline is communicated with the reaction tank and is used for introducing the pH value regulator into the reaction tank.
Further, the solid-liquid separation assembly comprises a solid-liquid separation device, the solid-liquid separation device comprises a washing machine and a thickener, the washing machine is a filter press washing machine or a centrifugal filtration washing machine, the thickener is communicated with an outlet of the pH value adjusting assembly and used for carrying out dense sedimentation on the adjusting liquid to obtain supernatant and underflow dense liquid, the thickener is provided with a first outlet and a second outlet, the washing machine is communicated with the first outlet and used for carrying out hydraulic filtration washing on part of the underflow dense liquid to obtain filtrate and filter residues, and the outlet of the washing machine and the second outlet are respectively communicated with an inlet of the evaporation assembly and used for enabling mixed liquid of the supernatant and the filtrate to be used as a pre-treatment liquid which is introduced into the evaporation assembly.
Further, the solid-liquid separation assembly further includes: the first feeding groove is communicated with the outlet of the pH value adjusting component; and the first feeding pump is respectively communicated with the outlet of the first feeding groove and the inlet of the solid-liquid separation equipment.
Further, the evaporation assembly includes: the evaporator is communicated with the outlet of the solid-liquid separation component and comprises a heat exchange tube, and the heat exchange tube is used for exchanging heat between the pre-treatment liquid and primary steam to obtain treated liquid and secondary steam containing ammonia gas; the condenser is communicated with the evaporator and is used for condensing the secondary steam to obtain ammonia water; and the steam delivery pipeline is communicated with the evaporator and is used for delivering primary steam into the evaporator.
Further, the evaporation assembly further comprises: the second feeding groove is communicated with the outlet of the solid-liquid separation component; and the second feeding pump is communicated with the outlet of the second feeding groove and the inlet of the evaporator.
Further, the thickener is also provided with a third outlet, the evaporation assembly further comprises a concentrated solution conveying pipeline, the concentrated solution conveying pipeline is respectively communicated with the third outlet and the second feeding groove and used for conveying part of the underflow concentrated solution to the second feeding groove to be mixed with the pre-treatment solution and the calcium sulfate seed crystal so as to obtain a pre-evaporation solution, and the evaporator is used for exchanging heat between the pre-evaporation solution and the primary steam.
Further, the evaporation assembly further comprises: the condensation water pump is communicated with the evaporator and is used for discharging condensation water formed by primary steam after heat exchange; the concentrated water pump is communicated with the evaporator and is used for discharging the treated liquid; and the concentrated ammonia water pump is communicated with the evaporator and is used for discharging ammonia water.
Further, the processing device further includes: an ammonia water storage tank communicated with the ammonia water pump; and the ammonia water conveying pump is communicated with the outlet of the ammonia water storage tank.
Further, the processing device further includes: the regulating tank is communicated with the inlet of the pH value regulating assembly; and the wastewater lifting pump is respectively communicated with the outlet of the regulating tank and the inlet of the pH value regulating assembly.
By applying the technical scheme of the invention, the invention provides the ammonia nitrogen wastewater treatment device, the pH value of the ammonia nitrogen wastewater can be regulated to be alkaline by the pH value regulating component in the treatment device, so that ammonium ions in the ammonia nitrogen wastewater are easy to be converted into ammonia monohydrate, the obtained regulating liquid can be subjected to solid-liquid separation by the solid-liquid separating component so as to remove impurities such as heavy metals in the ammonia nitrogen wastewater and improve the purity of the ammonia nitrogen to obtain pre-treatment liquid, the pre-treatment liquid can be subjected to evaporation treatment by the evaporating component, and most of ammonia nitrogen in the liquid can form ammonia after evaporation due to the fact that a large amount of volatile ammonia monohydrate exists in the pre-treatment liquid, so that the post-treatment liquid obtained after evaporation has lower ammonia nitrogen content and heavy metal content and can meet emission standards.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention. In the drawings:
Fig. 1 shows a schematic structural diagram of an ammonia nitrogen wastewater treatment device provided by the invention.
Wherein the above figures include the following reference numerals:
10. An adjusting tank; 20. a waste water lifting pump; 30. a pH adjustment assembly; 40. a solid-liquid separation assembly; 410. a first feed trough; 420. a first feed pump; 430. a solid-liquid separation device; 50. an evaporation assembly; 510. a second feed trough; 520. a second feed pump; 530. an evaporator; 540. a condensate pump; 550. a concentrate pump; 560. a concentrated ammonia water pump; 60. an ammonia water storage tank; 70. ammonia water delivery pump.
Detailed Description
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other. The invention will be described in detail below with reference to the drawings in connection with embodiments.
In order that those skilled in the art will better understand the present invention, a technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in which it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, shall fall within the scope of the present invention.
It should be noted that the terms "first," "second," and the like in the description and the claims of the present invention and the above figures are used for distinguishing between similar objects and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used may be interchanged where appropriate in order to describe the embodiments of the invention herein. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
As known from the background technology, the treatment method of ammonia nitrogen wastewater in the prior art is easy to cause pollution and high in energy consumption, seriously hinders the popularization and application of the technology, and becomes an important breakthrough point of the technology popularization because of low energy consumption and difficult scaling. The inventor of the present invention studied the above problems and provided a treatment device for ammonia nitrogen wastewater, as shown in fig. 1, comprising a pH adjusting assembly 30, a solid-liquid separation assembly 40 and an evaporation assembly 50, wherein the pH adjusting assembly 30 is used for adjusting the pH value of the introduced ammonia nitrogen wastewater to obtain an adjusting solution; the solid-liquid separation assembly 40 is communicated with the outlet of the pH value adjusting assembly 30 and is used for carrying out solid-liquid separation on the adjusting liquid to obtain a pre-treatment liquid; the evaporation assembly 50 is communicated with the outlet of the solid-liquid separation assembly 40 and is used for evaporating the pre-treatment liquid to obtain ammonia water and the post-treatment liquid.
The pH value adjusting component in the treatment device can adjust the pH value of the ammonia nitrogen wastewater to be alkaline so that ammonium ions in the ammonia nitrogen wastewater are easy to be converted into ammonia monohydrate, the solid-liquid separation component can carry out solid-liquid separation on the obtained adjusting liquid so as to remove impurities such as heavy metals in the ammonia nitrogen wastewater and improve the purity of the ammonia nitrogen to obtain a pretreatment liquid, and the evaporation component can carry out evaporation treatment on the pretreatment liquid.
The ammonia nitrogen concentration of the ammonia nitrogen wastewater as the treatment object can be 1-100 g/L. Because ammonia nitrogen in the ammonia nitrogen wastewater mainly exists in the form of free ammonia (NH 3) and ammonium ions (NH 4 +), the ammonia nitrogen concentration of the ammonia nitrogen wastewater refers to the sum of the concentrations of free ammonia (NH 3) and ammonium ions (NH 4 +) in the ammonia nitrogen wastewater.
In the above-described treatment apparatus of the present invention, it is preferable that the treatment apparatus further comprises an adjusting tank 10 and a wastewater lift pump 20, the adjusting tank 10 being in communication with an inlet of the pH adjusting assembly 30; the wastewater lift pump 20 is in communication with the outlet of the conditioning tank 10 and the inlet of the pH adjusting assembly 30, respectively, as shown in fig. 1. After the conditioning liquid is added to the first feed tank 410, the conditioning liquid can be pumped into the reaction tank by the wastewater lift pump 20 to adjust the pH of the ammonia nitrogen wastewater.
In the above treatment apparatus of the present invention, preferably, the pH adjusting assembly 30 includes a reaction tank for introducing ammonia nitrogen wastewater and a regulator delivery pipe; the regulator conveying pipeline is communicated with the reaction tank and is used for introducing the pH value regulator into the reaction tank. Ammonia nitrogen wastewater can be added into the reaction tank, and a pH value regulator is added into the reaction tank through a regulator conveying pipeline to regulate the pH value of the ammonia nitrogen wastewater, and a person skilled in the art can adopt a pH value regulator such as lime milk or sodium hydroxide which is conventional in the prior art; more preferably, the pH of the ammonia-nitrogen wastewater is adjusted to 11.5-12 to enable more ammonium ions (NH 4 +) in the ammonia-nitrogen wastewater to be converted to ammonia monohydrate.
In the above treatment apparatus of the present invention, the solid-liquid separation unit 40 may include a solid-liquid separation unit 430, and preferably, the above solid-liquid separation unit 430 includes a thickener and a washer (not shown in the drawing), the washer is a filter press washer or a centrifugal filter washer, the thickener is in communication with an outlet of the pH adjusting unit 30 for thickening the adjusting liquid to obtain supernatant and underflow thick liquid, the thickener has a first outlet and a second outlet, the washer is in communication with the first outlet for washing a part of the underflow thick liquid to obtain filtrate and filter residue, and the outlet and the second outlet of the washer are respectively in communication with an inlet of the evaporation unit 50 for mixing the supernatant and the filtrate as a pre-treatment liquid passing into the evaporation unit 50.
Specifically, introducing regulating solution into a thickener for solid-liquid separation under the action of gravity sedimentation, concentrating the regulating solution into underflow slurry with higher solid content (namely underflow thickener) after gravity sedimentation, generating cleaner overflow solution (namely supernatant) at the upper part of the thickener, and adopting the overflow solution as part of the pretreatment liquid for subsequent evaporation treatment; and then, carrying out solid-liquid separation on part of the underflow dense liquid by adopting a washing machine, taking a filter press washing machine as an example, introducing part of the underflow dense liquid into the filter press washing machine, realizing solid-liquid separation through a filter medium, washing filter residues on the filter medium (such as filter cloth) to form washing liquid, then discharging the washing liquid, and taking the filtrate and the supernatant as the treatment front liquid together for subsequent evaporation treatment.
In the above-described treatment apparatus of the present invention, it is preferable that the solid-liquid separation module 40 further includes a first feed tank 410 and a first feed pump 420, the first feed tank 410 being in communication with the outlet of the pH adjusting module 30; the first feed pump 420 is in communication with the outlet of the first feed tank 410 and the inlet of the solid-liquid separation device 430, respectively. After the conditioning liquid is added to the first feed tank 410, the conditioning liquid can be pumped by the first feed pump 420 to the solid-liquid separation device 430 for solid-liquid separation to obtain a pre-treatment liquid.
In the above-described treatment apparatus of the present invention, preferably, the evaporation module 50 includes an evaporator 530, a condenser, and a vapor transfer line, the evaporator 530 being in communication with the outlet of the solid-liquid separation module 40, the evaporator 530 including a heat exchange pipe for exchanging the pre-treatment liquid with the primary vapor to obtain the above-described post-treatment liquid and the secondary vapor including the above-described ammonia gas; the condenser is in communication with the evaporator 530 for condensing the secondary steam to obtain ammonia water. As shown in fig. 1, the condenser is respectively communicated with a cooling water supply pipeline and a cooling water return pipeline, and in operation, the circulating cooling water supply is introduced into the condenser to exchange heat with the secondary steam, so that the secondary steam is condensed to obtain ammonia water, and the ammonia water is discharged from the condenser as circulating cooling water return after heat exchange; a steam delivery line communicates with the evaporator 530 for delivering primary steam into the evaporator 530. And introducing the pre-treatment liquid and the primary steam into an evaporator for heat exchange so as to evaporate the pre-treatment liquid to form secondary steam, wherein the evaporated concentrated liquid is the post-treatment liquid, and the secondary steam can also be used as the primary steam for heat exchange with the pre-treatment liquid and introduced into the evaporator.
The evaporator 530 may be a single-effect evaporator or a multi-effect evaporator, and the secondary steam of the previous effect may be used as the primary steam of the heat exchange between the next effect and the pre-treatment liquid. The single-effect or multi-effect evaporator 530 can be a falling film evaporator, mixed steam in the evaporator 530 flows in a heat exchange tube, liquid is sprayed on the outer wall of the tube to form a film, the effect number of the multi-effect evaporator is determined according to the actual water quality condition, the effect-to-effect temperature difference is about 4 ℃, the temperature difference of 30 ℃ can be arranged to be 6-7, and the energy utilization efficiency is greatly increased by adopting the multi-effect evaporator.
The evaporation assembly 50 may further include a second feed tank 510 and a second feed pump 520, where the second feed tank 510 is in communication with the outlet of the solid-liquid separation assembly 40; the second feed pump 520 is in communication with the outlet of the second feed tank 510 and the inlet of the evaporator 530. After the pre-treatment liquid is added into the second feeding groove 510, the pre-treatment liquid can be pumped into the evaporator 530 through the second feeding pump 520 for evaporation treatment so as to remove most of ammonia nitrogen, thereby obtaining the post-treatment liquid.
In a preferred embodiment, the thickener also has a third outlet, the evaporation assembly 50 further comprises a concentrate delivery line in communication with the third outlet and the second feed tank 510, respectively, for delivering a portion of the underflow concentrate to the second feed tank 510 for mixing with the pre-treatment liquor and the calcium sulfate seed crystals to obtain a pre-evaporation liquor, and the evaporator 530 is for exchanging heat of the pre-evaporation liquor with the primary steam.
In the above preferred embodiment, part of the underflow concentrate, the pre-treatment concentrate and the calcium sulfate seed crystals can be mixed in the second feed tank 510 through the concentrate delivery line to be used as the pre-evaporation concentrate for subsequent evaporation treatment, and the scale inhibition mechanism is mainly that the calcium sulfate seed crystal surface has an adsorption effect on the scale inhibitor molecules, so that the crystal growth of CaCO 3、CaSO4 is inhibited, and the scale formation in the subsequent evaporation treatment process can be effectively avoided; and compared with the traditional process that sodium hydroxide is required to be used as the pH regulator for avoiding scaling, the pH regulator can adopt calcium hydroxide, so that the cost of the wastewater treatment medicament is reduced.
In the above-described treatment apparatus of the present invention, it is preferable that the evaporation assembly 50 further includes a condensate pump 540, a concentrate pump 550, and a concentrate pump 560, the condensate pump 540 being in communication with the evaporator 530 for discharging condensate formed by the primary steam after heat exchange; the concentrate pump 550 communicates with the evaporator 530 for discharging the treated liquid; the ammonia water pump 560 is communicated with the evaporator 530 for discharging ammonia water formed by condensing ammonia in the secondary steam. The condensed water formed by the primary steam after heat exchange can be recycled through the condensed water pump 540, and the evaporated concentrated solution can meet the discharge standard, so that the primary steam is discharged through the concentrated water pump 550, and the ammonia water formed by ammonia condensation in the secondary steam can be discharged through the concentrated ammonia water pump 560, so that the secondary steam is further recycled.
In order to recycle the ammonia water formed by condensing the ammonia gas, more preferably, the treatment device further comprises an ammonia water storage tank 60 and an ammonia water delivery pump 70, wherein the ammonia water storage tank 60 is communicated with a concentrated ammonia water pump 560; the ammonia water delivery pump 70 communicates with the outlet of the ammonia water reservoir 60. The ammonia water entering the ammonia water storage tank 60 can be pumped into the desulfurization system for recycling through the ammonia water delivery pump 70.
From the above description, it can be seen that the above embodiments of the present invention achieve the following technical effects:
1. By adopting the treatment device, ammonia nitrogen wastewater can be treated to form secondary steam containing ammonia, and the evaporated concentrated solution can meet the industrial emission standard;
2. the device has the advantages of simple structure, low energy consumption, high treatment efficiency, low heat energy consumption and low operation cost, and ammonia generated after evaporation is easy to collect after condensation, so that the pollution to the environment caused by direct discharge is avoided;
3. The evaporation component further comprises a concentrated solution conveying pipeline, and part of the underflow concentrated solution, the pre-treatment solution and the calcium sulfate seed crystal can be mixed through the concentrated solution conveying pipeline to be used as the pre-evaporation solution for subsequent evaporation treatment, so that scaling in the subsequent evaporation treatment process can be effectively avoided.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. An ammonia nitrogen wastewater treatment device, which is characterized by comprising:
The pH value adjusting component (30) is used for adjusting the pH value of the introduced ammonia nitrogen wastewater to obtain an adjusting solution;
the solid-liquid separation assembly (40) is communicated with the outlet of the pH value adjusting assembly (30) and is used for carrying out solid-liquid separation on the adjusting liquid to obtain a pre-treatment liquid; and
The evaporation assembly (50) is communicated with the outlet of the solid-liquid separation assembly (40) and is used for carrying out evaporation treatment on the pre-treatment liquid to obtain ammonia water and treated liquid;
The solid-liquid separation assembly (40) comprises a solid-liquid separation device (430), the solid-liquid separation device (430) comprises a washing machine and a thickener, the washing machine is a filter press washing machine or a centrifugal filtration washing machine, the thickener is communicated with an outlet of the pH value adjusting assembly (30) and is used for thickening and settling the adjusting liquid to obtain supernatant and underflow thick liquid, the thickener is provided with a first outlet and a second outlet, the washing machine is communicated with the first outlet and is used for hydraulically filtering and washing part of the underflow thick liquid to obtain filtrate and filter residues, the outlet of the washing machine and the second outlet are respectively communicated with an inlet of the evaporation assembly (50) and are used for enabling mixed liquid of the supernatant and the filtrate to be used as the pre-treatment liquid which is introduced into the evaporation assembly (50);
the evaporation assembly (50) comprises:
An evaporator (530) in communication with the outlet of the solid-liquid separation assembly (40), the evaporator (530) comprising a heat exchange tube for exchanging heat of the pre-treatment liquid with primary steam to obtain the post-treatment liquid and a secondary steam comprising ammonia gas;
the evaporation assembly (50) further comprises:
a second feed trough (510) in communication with an outlet of the solid-liquid separation assembly (40);
A second feed pump (520) in communication with an outlet of the second feed tank (510) and an inlet of the evaporator (530);
the thickener is also provided with a third outlet, the evaporation assembly (50) further comprises a concentrated liquid conveying pipeline which is respectively communicated with the third outlet and the second feeding trough (510) and is used for conveying part of the underflow concentrated liquid into the second feeding trough (510) to be mixed with the pre-treatment liquid and the calcium sulfate seed crystal so as to obtain a pre-evaporation liquid, and the evaporator (530) is used for exchanging heat between the pre-evaporation liquid and the primary steam.
2. The processing apparatus according to claim 1, wherein the pH adjusting assembly (30) comprises:
The reaction tank is used for introducing the ammonia nitrogen wastewater;
And the regulator conveying pipeline is communicated with the reaction tank and is used for introducing a pH value regulator into the reaction tank.
3. The processing apparatus according to claim 1, wherein the solid-liquid separation assembly (40) further comprises:
A first feed trough (410) in communication with an outlet of the pH adjustment assembly (30);
And a first feed pump (420) which is respectively communicated with the outlet of the first feed trough (410) and the inlet of the solid-liquid separation equipment (430).
4. The processing apparatus according to claim 1, wherein the evaporation assembly (50) further comprises:
a condensate pump (540) communicated with the evaporator (530) and used for discharging condensate formed by the primary steam after heat exchange;
A concentrate pump (550) in communication with the evaporator (530) for discharging the treated liquid;
And a concentrated ammonia water pump (560) communicated with the evaporator (530) for discharging the ammonia water.
5. The processing device of claim 4, wherein the processing device further comprises:
an ammonia water tank (60) in communication with the ammonia water pump (560);
and an ammonia water delivery pump (70) communicated with the outlet of the ammonia water storage tank (60).
6. The processing apparatus of claim 1, wherein the processing apparatus further comprises:
an adjusting tank (10) communicated with an inlet of the pH adjusting assembly (30);
And the wastewater lifting pump (20) is respectively communicated with the outlet of the regulating tank (10) and the inlet of the pH value regulating assembly (30).
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