CN207671878U - High ammonia-nitrogen wastewater deamination nitrogen system - Google Patents
High ammonia-nitrogen wastewater deamination nitrogen system Download PDFInfo
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- CN207671878U CN207671878U CN201721683211.5U CN201721683211U CN207671878U CN 207671878 U CN207671878 U CN 207671878U CN 201721683211 U CN201721683211 U CN 201721683211U CN 207671878 U CN207671878 U CN 207671878U
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Abstract
The utility model discloses a kind of high ammonia-nitrogen wastewater deamination nitrogen system,It includes and the sequentially connected filter in organic waste pond and waste water degassing tank,Its bottom degassing biogas slurry pipeline is connected with the biogas slurry import of feed pump and plate heat exchanger in turn,The biogas slurry outlet of plate heat exchanger is connected to the feed inlet on stripper top,The gas outlet of stripper top is connected to the air inlet of Heat Exchanger in Circulating Water System,Liquefied ammonia outlet and the ammonia separation tower return tank inlet communication of Heat Exchanger in Circulating Water System,The outlet of ammonia separation tower return tank is connected to ammonia separation reflux pump,Ammonia separation reflux pump is connected separately with liquid ammonia storage tank and the liquefied ammonia reflux nozzle on stripper top,The hot waste water outlet of stripper bottom is connected to the high-temperature inlet water mouth of plate heat exchanger,Hot waste water outlet, which is also pumped with ammonia separation tower recuperation, to be connected,The wasted water outlet of ammonia separation bottom of tower heat exchanger is connected to the refluxing opening of stripper lower part,This system operating cost is low,Non-secondary pollution,Suitable for large-sized biogas project and landfill leachate treatment project.
Description
Technical field
The utility model is related to field of environment engineering, and in particular to a kind of high ammonia-nitrogen wastewater deamination nitrogen system is also applied for
Municipal garbage percolate deamination nitrogen system.
Background technology
After the anaerobic fermentation Biogas that it's 30 days or more pasts manure of livestock and poultry soiled ends in methane-generating pit formed sepia solid content and
Liquid is biogas residue and biogas liquid, also known as natural pond fertilizer.Biogas residue moisture 60%~80%, biogas slurry moisture 96%~99%, pH value
It is 6.5~8.0.Nitrogen, phosphorus, the potassium needed for plant are not only saved in biogas slurry, and contain abundant amino acid, various hydrolysis
Enzyme, auxin and biogas fermentation strain etc..Biogas residue and biogas liquid belongs to effect late and has both with quick-acting, quick-acting more than the organic fertilizer imitated late, it
The zoonosis germ and Activities of Some Plants pest and disease damage biological source carried in raw excrement after fermentation has largely been killed, they are
Good organic fertilizer and methane-generating pit start inoculation strain.
By-product of the biogas slurry as large-sized biogas engineering, while being also good fertilizer, the area that especially kind cultivation is concentrated
Domain, the large-sized biogas engineering using livestock and poultry feces as raw material are practically free of toxic harmful components, the value of comprehensive utilization in biogas slurry
It is higher, it is handled according to field irrigation standard currently, the biogas slurry of large-sized biogas engineering is substantially,《After biogas engineering biogas slurry and biogas residue
Treatment technology specification》(NY/T 2374-2013) is the standard of the directiveness of current domestic biogas engineering biogas slurry treatment, by agricultural
Department is leading, and returning to the field dissolves biogas slurry treatment mode nearby by the way of tank car or pipeline, but remote if building ground
From large-scale farmland, this pure broken Irrigation processing biogas slurry pattern there is problem.What on January 1st, 2014 came into effect《Poultry
Fowl breeding scale pollution prevention ordinance》, Article 20 clearly states：To the treated animal waste of environmental emission,
Pollutant emission standard and overall control index as defined in country and place should be met.Animal waste is unprocessed,
It must not be directly to environmental emission.So biogas slurry diversification processing just seems very necessary large-sized biogas engineering.
With the reinforcement of rural ecological environmental consciousness, large-sized biogas engineering is more from traditional large-scale plant that raises trend at present
Field, the building site of biogas is also from traditional northern farm, and general rural area and suburbs are moved towards in large-scale farm, biogas
Construction mode is also from traditional simple processing solid organic castoff to biogas comprehensive utilization pattern, and large-scale plant that raises gas is warm at present
Electric fertilizer coproduction pattern, large-scale plant that raises direct-furnish peasant household pattern, concentrated biogas purifying networking pattern, the vehicle-mounted gas supply of concentrated biogas
Pattern, kitchen garbage marsh gas power generation pattern.While various modes integrated treatment organic solid castoff, huge economy is generated
Benefit, the biogas under the above various modes, if building ground in rural area or suburbs far from field irrigation area, biogas slurry treatment
Do not have operability using large-scale pasture grassland returning to the field, then biogas slurry comprehensive utilization, which just becomes, restricts large-sized biogas engineering
Key factor.A large amount of biogas slurry needs stool discharge after advanced treating, and the biogas slurry generated using chicken manure as raw material has a
Typical feature is exactly that biogas slurry ammonia-nitrogen content is very high, can reach 4000ppm or more, other biochemical indicators are also higher, and biogas slurry is straight
It connects that Biochemical Treatment is undesirable, generally requires and pretreatment is carried out to biogas slurry reduce NH in biogas slurry3- N enters back into wastewater biochemical
Pond is handled, and is discharged after up to standard.
At the same time, according to the principle of China's garbage disposal " innoxious, minimizing, recycling ", there will be large quantities of lives
Garbage sanitary filling field will create.And whether landfill leachate handles qualified discharge, is to weigh whether a landfill yard is health
One of important indicator of landfill yard.One underproof refuse landfill is exactly a big pollution sources, such as not in time to its into
Row is collected, is handled, and pollution and influence on underground water, surface water and refuse landfill ambient enviroment will be caused.Especially it is right
The pollution of underground water source and soil is even more serious.Some old refuse landfills are not due to taking seepage control measure, generation to ooze
Filtrate permeates the ground in water, causes the serious pollution to underground water.It pollutes perdurabgility can be decades-long or even up to a hundred
Year.Once underground water source and surrounding soil are polluted by it, think to implement to purify again by artificial means, technically will be extremely difficult,
Expense is also extremely expensive, it is difficult to implement, to seriously threaten the life and production of people.
Landfill leachate water quality characteristics are as follows：(1) leachate quality is sufficiently complex, not only contains oxygen consumption organic pollution,
Also contain each metalloid and nutrient for plants (ammonia nitrogen etc.), if industrial department uses refuse landfill, is also had in percolate
Poisonous and harmful organic pollution；(2) COD and BOD concentration is high, reaches as high as tens of thousands of, significantly larger than municipal sewage；(3) rubbish oozes
Organic pollutant category is more in filtrate, wherein being difficult to the non-chlorinated such as biodegradable naphthalene, phenanthrene aromatic compound, chlorinated aromatic
Compounds of group, phosphate, phthalic acid ester, phenolic compound and amino benzenes compounds etc.；The states such as Polychlorinated biphenyls, polycyclic aromatic hydrocarbon
Chinese Ministry of Environmental Protection of family priority pollutants, also some endocrine disruptors substances.(4) contain 10 various metals in landfill leachate
Ion, heavy metal ion therein can generate serious inhibiting effect to biological treatment process；(5) ammonia-nitrogen content is high, and C/N ratios are lost
It adjusts, P elements lack, and certain difficulty is brought to biological treatment.
To sum up, existing biogas slurry is as discharged wastewater met the national standard treatment process, and there are two directions for the technique mainly used：One
Be by film concentrate in the way of, concentrate can be used for the foliar fertilizer production of high concentration, and the waste water COD and ammonia nitrogen after concentration be all big
Big reduction, control concentration technology can accomplish qualified discharge after qualified discharge or simple biochemical treatment；Another is exactly
By the way of traditional treatment of Organic Wastewater, using Multilevel biochemistry treatment, final qualified discharge, landfill leachate is because of ingredient
It is complicated, it is necessary to use the processing mode of qualified discharge, naturally it is also possible to using techniques such as film concentrations, but if using multistage raw
Change pond processing, in the waste water of this kind of high ammonia nitrogen, activity of traditional Biochemical Treatment bacterium in the environment of high ammonia nitrogen is bad, sternly
Ghost image rings the efficiency of wastewater treatment.Membrane separation waste water does not require ammonia nitrogen, but processing cost is relatively expensive, using more
Grade biochemical processing process processing cost is relatively low but the biogas slurry and landfill leachate of unsuitable high ammonia nitrogen, thus biochemical treatment it
Before, it needs to do biogas slurry and landfill leachate the pretreatment except ammonia nitrogen.
Currently, ammonia nitrogen waste water treatment method mainly has two major classes, i.e. physico-chemical process and bioanalysis.Common physico-chemical process and biology
Method is summarized as follows：
(1) physico-chemical process
1. blow-off method
Under alkaline condition, it is detached using the vapor-liquid equilibrium relationship between the gas phase concentration of ammonia nitrogen and liquid concentration
A kind of method, it is considered that stripping is related with temperature, PH, gas liquid ratio.
2. zeolite deamination method
Utilize the cation in zeolite and the NH in waste water4 +It swaps to achieve the purpose that denitrogenation.Using zeolite deamination
Method must take into consideration the regeneration issues of zeolite, usually there is regenerated liquid method and burning method.When using burning method, the ammonia of generation must be into
Row processing.
3. membrane separation technique
A kind of method of ammonia nitrogen removal is carried out using the selective penetrated property of film.This method is easy to operate, the ammonia nitrogen rate of recovery
Height, non-secondary pollution.There is ionic dissociation equilibriums in water for ammonia nitrogen, as PH is increased, ammonia NH in water3Form ratio increases,
Under certain temperature and pressure, NH3Gaseous state and liquid two reach balance.According to the principle of chemical balance shifting, in nature
In all balances be all opposite and temporary.Chemical balance could only be kept under certain condition, " if change balance system
One of condition of system, such as concentration, pressure or temperature, balance is just moved to the direction that can weaken this change." defer to this principle
It is high-concentration ammonia nitrogenous wastewater that following design concept, which has been carried out, in the side of film, and using pressure difference as motive force, reverse osmosis will
Water is separated from high-concentration ammonia nitrogenous wastewater, achievees the purpose that ammonia nitrogen removal.
4. the MAP precipitation method
Mainly utilize following chemical reaction：Mg2++NH4 ++PO4 3-=MgNH4PO4
Microcosmic salt and magnesium salts are added into the waste water containing ammonia nitrogen in high density with certain proportion theoretically, as [Mg2+][NH4 +][PO4 3-]>2.5×10–13When produce ammonium magnesium phosphate (MAP), remove waste water in ammonia nitrogen.
5. chemical oxidization method
Ammonia nitrogen is direct oxidation into a kind of method that nitrogen removes using strong oxidizer.Break point chlorination is using in water
In ammonia reacted with chlorine and generate nitrogen deamination, this method can also play bactericidal effect, but the chlorine residue generated can be to fish
Have an impact, therefore must set up except chlorine residue facility.
(2) biological denitrificaion method
This is a kind of traditional processing method, and principle is to carry out oxygenolysis to pollutant using bacterial micro-organism.It passes
System and denitrification process newly developed have A/O, two sections of activated sludge processes Strong oxdiative Aerobic biological process, short-cut nitrification and denitrification, to surpass
Sound stripping handles ammonia nitrogen method method etc..
(3) biochemical combination method
Physical chemistry method will not be restricted when handling high-concentration ammonia nitrogenous wastewater because ammonia nitrogen concentration is excessively high, but cannot
Ammonia nitrogen concentration is dropped to sufficiently low (such as 100mg/L or less).And biological denitrificaion can be because of high concentration free ammonia or nitrite
Nitrogen and be suppressed.Using biochemical united method in practical application, first to the waste water containing ammonia nitrogen in high density before biological treatment
Carry out materializing strategy.Biochemical treatment is carried out to low-concentration ammonia-nitrogen again, such as：Biological activated carbon fluid bed, film-bioreactor skill
Art (MBR) etc..
The weakness of the above common device for treating high-concentration ammonia：
1. either " stripping+A/O or stripping+chemical precipitation " all be unable to do without the pretreatment work of with high investment, high operating cost
Skill, " stripping " power consumption is too big, and the mixed gas that stripping obtains needs to obtain ammonium sulfate with sulfuric acid absorption, and consumption is a large amount of
Inorganic acid, cost further increases, and the leakage of stripping atmospheric pressure device is serious, ammonia penetrating odor is dense, hence it is evident that is not suitable for agriculture
This ecological, environmental protective project of village's biogas.
2. conventional biochemical method not only invests height when using continued access A/O methods, but also takes up a large area, pretreatment water inlet is wanted
Seek harshness (such as NH3- N needs to be less than 200mg/L, and blow-off method reaches the high-concentration ammonia nitrogenous wastewater more than 2000mg/L or more at all
Less than this requirement, then clear water at double can only be used to dilute).
3. although the investment of continued access chemical precipitation method and floor space are all smaller than A/O method, the consumption of its medicament is too big, N：
P：The ratio between Mg is 1：1.1~1.2, treatment agent cost is too high, and water outlet is also impossible to reach national standard level-one or two level row
Standard is put, there is secondary pollution.
Invention content
The utility model provides a kind of high ammonia-nitrogen wastewater deamination nitrogen system, this kind of system using materialization and biochemical connection and as
Starting point, using stripping rectifying method to biogas slurry class high concentrated organic wastewater pre-process, by ammonia nitrogen in organic wastewater from
4000ppm be reduced to 1000ppm hereinafter, this concentration for the traditional handicrafts such as continuous A/O or MBR relatively be suitble to, Bu Huixian
The operating load of the raising processing cost biochemistry pool of work, the indexs such as ammonia nitrogen and COD are coordinated.System solves the problem traditional A/O is continuous
There is the unconformable problem of biochemical bacterium in the wastewater treatment of this kind of high ammonia nitrogen of biochemical treatment biogas slurry, while optimizing tradition stripping and removing ammonia
Technique solves the problems, such as that conventional vapor stripping process steam consumption is big, and steam is comprehensive in pneumoelectric coproduction project in the engineerings such as solution biogas
Utilizing question is closed, to improve the stability and total energy approach of whole system.
The system is suitable at the high ammonia nitrogen biogas slurry qualified discharge biochemistry that chicken manure class anaerobic methane Cogeneration Project generates
The pretreatment system of reason.The system can also can be used for rural area livestock and poultry feces and farmland stalk comprehensive utilization production biogas engineering, city
The rubbish that biogas engineering, municipal refuse landfill and power generation by waste combustion processing generate is produced in the organic wastes integrated treatment such as city's kitchen garbage
Percolate processing and other chemical industry light industry organic wastewaters give up produces biogas engineering admittedly.
To achieve the above object, a kind of high ammonia-nitrogen wastewater deamination nitrogen system designed by the utility model, it include with it is organic
The degassing biogas slurry pipeline of the sequentially connected filter of wastewater disposal basin and waste water degassing tank, the waste water degassing pot bottom is connected in turn
The biogas slurry import of feed pump and plate heat exchanger, the escape pipe at the top of the waste water degassing tank are connected with vacuum pump and power generation in turn
Machine flue gas system.
The biogas slurry outlet of the plate heat exchanger is connected to the feed inlet on stripper top, the outlet of the stripper top
Mouth is connected to the air inlet of Heat Exchanger in Circulating Water System, and the Heat Exchanger in Circulating Water System, which is provided at both ends with, to be connected with circulating water inlet and follow
Ring water outlet pipe, liquefied ammonia outlet and the ammonia separation tower return tank inlet communication of the Heat Exchanger in Circulating Water System, the ammonia separation tower return
The outlet of stream tank is connected to the entrance of ammonia separation reflux pump, the outlet of the ammonia separation reflux pump be connected separately with liquid ammonia storage tank with
The liquefied ammonia reflux nozzle on stripper top.
The hot waste water outlet of the stripper bottom is connected to the high-temperature inlet water mouth of plate heat exchanger, the plate-type heat-exchange
The low temperature water inlet of device is connected to biochemistry pool；The hot waste water outlet is also connect with the entrance of ammonia separation tower recuperation pump,
The outlet of the ammonia separation tower recuperation pump is connected to the waste water inlet of ammonia separation bottom of tower heat exchanger, the ammonia separation bottom of tower
The wasted water outlet of heat exchanger is connected to the refluxing opening of stripper lower part, and the ammonia separation bottom of tower heat exchanger both ends are connected separately with
Vapour system and condensate system.
Further, liquid level of flux cascade controller A is provided on the pipeline between the feed pump and plate heat exchanger；
It is provided with liquid level of flux cascade controller B on pipeline between the ammonia separation reflux pump and liquefied ammonia reflux nozzle；It is described board-like
Liquid level of flux cascade controller C is provided on pipeline between heat exchanger and biochemistry pool.
Still further, the liquid level of flux cascade controller A, liquid level of flux cascade controller B and liquid level of flux tandem
Controller C includes control valve, is parallel with flowmeter on the control valve, the flowmeter is connected with liquid level gauge, the flow
In liquid level cascade controller A, liquid level of flux cascade controller B and liquid level of flux cascade controller C three liquid level gauges respectively with it is useless
Water degasification tank, stripper are connected with ammonia separation tower return tank.
Still further, being provided with flow controller on pipeline between ammonia separation bottom of tower heat exchanger and vapour system
A is provided with flow controller B, the ammonia separation reflux on the pipeline between the stripper and ammonia separation tower recuperation pump
It is provided with flow controller C on pipeline between pump and liquid ammonia storage tank.
Still further, the flow controller A, flow controller B and flow controller C include control valve, it is described
Flowmeter is parallel on control valve.
Still further, the flowmeter in the liquid level of flux cascade controller B connects with the flowmeter in flow controller A
It is logical.
The course of work of above system is：
(1) a small amount of biogas that biogas slurry enters after filter filters in waste water degassing tank abjection biogas slurry is not coagulated with other
Gas, a small amount of biogas and fixed gas are extracted into generator flue gas system 21 by vacuum pump；
(2) biogas slurry of removing exhaust gas enters plate heat exchanger by feed pump, and the purpose of heat exchanger is to utilize stripper tower
The hot waste water of the hot waste water outlet at bottom exchanges heat, and improves the temperature of biogas slurry, and the bottom of tower waste water after cooling enters biochemistry pool,
Liquid level of flux cascade controller A is set between feed pump and plate heat exchanger, passes through the liquid level and charging pump line of waste water degassing tank
Flow serials control charging on road；
(3) biogas slurry after heating up enters the feed inlet of stripper middle and upper part, and bottom of tower biogas slurry is by the few portion in hot waste water outlet again
Divide and enter above-mentioned steps, another part biogas slurry removes biochemistry pool after middle heat exchange, is connected between hot waste water outlet and biochemistry pool
Liquid level of flux cascade controller C utilizes the flow string between the liquid level of stripper, hot waste water outlet and biochemistry pool 13 on pipeline
Grade controls the unlatching of the control valve on the pipeline；
(4) most of biogas slurry of bottom of tower enters ammonia separation bottom of tower by hot waste water outlet by ammonia separation tower recuperation pump
Heat exchanger is arranged flow controller B between hot waste water outlet and ammonia separation tower recuperation pump, controls the flow of the pipeline.
(5) heat exchanger heat source is used for the high-temperature flue gas from biogas internal combustion engine generator (vapour system) or flue gas heat-exchange unit institute
Flow controller A is arranged on heat source pipeline for producing steam, is flowed back using the liquefied ammonia on ammonia separation reflux pump and refluxing opening this pipeline
Amount controls the amount of steam source, and the biogas slurry inside stripper carries out reboiling in heat exchanger and be heated to reflux, control tower top temperature
Degree and pressure, gas outlet obtain pure ammonia liquid mixture；
(6) the gas-liquid mixed material of gas outlet enters Heat Exchanger in Circulating Water System and cools down to obtain liquefied ammonia, and liquefied ammonia enters ammonia separation tower
Return tank, the liquefied ammonia in ammonia separation tower return tank are pressurizeed by ammonia separation reflux pump, most of to be returned to by the liquefied ammonia nozzle that flows back
In stripper, small part into discharging into liquid ammonia storage tank outside.Liquid level of flux is set between ammonia separation reflux pump and liquefied ammonia reflux nozzle
Cascade controller B utilizes the flow between the liquid level of ammonia separation reflux pump, ammonia separation reflux pump and liquefied ammonia reflux nozzle on pipeline
The unlatching of control valve on the serials control pipeline.It is provided with flow controller C between ammonia separation reflux pump and liquid ammonia storage tank, controls
Make the flow of the pipeline.
(7) by process above, the ammonia nitrogen concentration of biogas slurry can be reduced to 1000ppm from 4000ppm or more once, control
The reflux ratio and column plate quantity and process conditions of stripper can adjust the ammonia nitrogen concentration of outlet waste water, generally be reduced to
1000ppm or less can adapt to multistage A/O or the wastewater treatment requirement of other biochemical treatment tanks, and the concentration for exporting ammonia nitrogen is higher,
The processing load of biochemistry pool is bigger, otherwise the operating cost of the ammonia nitrogen removal device used in the utility model is higher.It can be according to natural pond
The ammonia nitrogen concentration of liquid and the treatment process of next step biochemistry pool select suitable process conditions.
The beneficial effects of the utility model：
(1) system of the utility model is compared to directly with high ammonia-nitrogen wastewater multistage A/O biochemical treatments, the utility model use
Less floor space and less investment physical chemistry method remove the free ammonia in high-concentration ammonia nitrogenous wastewater, can significantly reduce dirt
The floor space and operating cost of water process.
(2) system of the utility model removes the technique of ammonia nitrogen relative to current mainstream blow-off method, and the utility model uses
The problems such as method of operation with pressure, scene is not in ammonia leakage, a small amount of ammonia contained in the fixed gas in the utility model
It also returns to internal combustion engine high temperature to burn, is not in the secondary pollution problem in stripping process.Stripping process obtains simultaneously
Stripping tail gas must be handled by way of adding the inorganic acids chemical absorbing such as sulfuric acid, and a large amount of ammonium sulfate of by-product, concentration is not
Height, processing or big using difficulty, the utility model directly obtain liquefied ammonia, and purity height can be used as technical grade liquefied ammonia to outgoing
It sells.
(3) system of the utility model removes the technique of ammonia nitrogen relative to existing stripping rectifying at present, and current technique is adopted
It is high pressure stripping rectifying tower process with mainly having two lines, the first route, obtained product is liquefied ammonia, but strips rectifying column
High temperature and pressure operation needs a large amount of reboiler to be heated in bottom of tower to ensure to strip the operation of rectifying column, bottom of tower using combustion gas or
Coal-burning boiler is heated to reflux, and this technique certainly will burn a considerable amount of biogas for biogas project, influence Biogas Generator Set
Operation, using the tail gas desulfurization denitration of coal-burning boiler and all unsuitable large-sized biogas engineering of boiler system, on the other hand
Generator flue gas is in large-sized biogas power generation project in addition to winter is used for fermentation liquor pretreatment, spring and summer autumn most high-temperature flue gas
Directly idle discharge is put, the biogas that on the one hand needs to burn is for heating materials at bottom of tower, and one side high-temperature flue gas is to empty direct emission, originally
The high-temperature flue gas or heat system for bottom of tower by the superheated steam of flue gas heat-exchange unit that utility model generates biogas internal combustion engine
System, effective solution total energy approach problem, and also in general, biogas slurry to be treated is used in the utility model
Technique under, biogas internal combustion engine flue gas is removed heated for zymotic fluid after be the heat that can guarantee needed for the heating of stripping rectifying column bottom
's.Article 2 route uses micro-positive pressure rectifying mode, stripping rectifying to use normal pressure micro-positive pressure mode, and low energy consumption for this mode, but
The stripped product for being is 30% or so weak aqua ammonia, and the yield amount of weak aqua ammonia is this reality under the ammonia nitrogen removal amount of identical scale
More than the three times with Novel liquid ammonia yield, 4 times or so of volume, scene needs to build weak aqua ammonia storage tank, and weak aqua ammonia is to outgoing
It sells and is also not so good as high-purity liquefied ammonia, overall economic efficiency is less than process program used by the utility model.
(4) system of the utility model removes ammonia nitrogen relative to membrane separating method, and the utility model also has operating cost excellent
Gesture.
Description of the drawings
Fig. 1 is the system diagram figure of the high ammonia-nitrogen wastewater deamination nitrogen system of the utility model；
Fig. 2 is the detail view of liquid level of flux cascade controller；
Fig. 3 is the detail view of flow controller；
In figure, filter 1, waste water degassing tank 2, vacuum pump 3, feed pump 4, plate heat exchanger 5, stripper 6, feed inlet
6.1, liquefied ammonia reflux nozzle 6.2, refluxing opening 6.3, hot waste water outlet 6.4, gas outlet 6.5, ammonia separation tower recuperation pump 7,
Ammonia separation bottom of tower heat exchanger 8, Heat Exchanger in Circulating Water System 9, ammonia separation tower return tank 10, ammonia separation reflux pump 11, liquid ammonia storage tank 12,
Biochemistry pool 13, liquid level of flux cascade controller A14, liquid level of flux cascade controller B15, liquid level of flux cascade controller C16,
Flow controller A17, flow controller B18, flow controller C19, organic waste pond 20, generator flue gas system 21, cycle
Water water inlet pipe 22, circulating water outlet pipe 23, vapour system 24, condensate system 25, control valve 26, flowmeter 27, liquid level gauge 28.
Specific implementation mode
The utility model is described in further detail in the following with reference to the drawings and specific embodiments, so as to art technology
Personnel understand.
High ammonia-nitrogen wastewater deamination nitrogen system as shown in Figure 1, it includes and 20 sequentially connected filter of organic waste pond
1 and waste water degassing tank 2, the degassing biogas slurry pipeline of 2 bottom of waste water degassing tank is connected with feed pump 4 and plate heat exchanger 5 in turn
The escape pipe of biogas slurry import, 2 top of waste water degassing tank is connected with vacuum pump 3 and generator flue gas system 21 in turn.
The biogas slurry outlet of plate heat exchanger 5 is connected to the feed inlet 6.1 on 6 top of stripper, the gas outlet at 6 top of stripper
6.5 are connected to the air inlet of Heat Exchanger in Circulating Water System 9, and Heat Exchanger in Circulating Water System 9, which is provided at both ends with, is connected with 22 He of circulating water inlet
Circulating water outlet pipe 23, liquefied ammonia outlet and 10 inlet communication of ammonia separation tower return tank of Heat Exchanger in Circulating Water System 9, the reflux of ammonia separation tower
The outlet of tank 10 is connected to the entrance of ammonia separation reflux pump 11, and the outlet of ammonia separation reflux pump 11 is connected separately with liquid ammonia storage tank 12
With the liquefied ammonia reflux nozzle 6.2 on 6 top of stripper.
The hot waste water outlet 6.4 of 6 bottom of stripper is connected to the high-temperature inlet water mouth of plate heat exchanger 5, plate heat exchanger 5
Low temperature water inlet be connected to biochemistry pool 13；Hot waste water outlet 6.4 is also connect with the entrance of ammonia separation tower recuperation pump 7,
The outlet of ammonia separation tower recuperation pump 7 is connected to the waste water inlet of ammonia separation bottom of tower heat exchanger 8, the heat exchange of ammonia separation bottom of tower
The wasted water outlet of device 8 is connected to the refluxing opening 6.3 of 6 lower part of stripper, and heat exchanger 8 both ends in ammonia separation bottom of tower are connected separately with
Vapour system 24 and circulation 25.
Liquid level of flux cascade controller A14 is provided on pipeline between feed pump 4 and plate heat exchanger 5；Ammonia separation returns
It is provided with liquid level of flux cascade controller B15 on pipeline between stream pump 11 and liquefied ammonia reflux nozzle 6.2；Plate heat exchanger 5 with
Liquid level of flux cascade controller C16 is provided on pipeline between biochemistry pool 13.Liquid level of flux cascade controller A14, flow liquid
Position cascade controller B A15 and liquid level of flux cascade controller C16 include control valve 26, and flowmeter is parallel on control valve 26
27, flowmeter 27 is connected with liquid level gauge 28, in liquid level of flux cascade controller A14, liquid level of flux cascade controller B15 and C16
Three liquid level gauges 28 respectively with waste water degassing tank 2, stripper 6 and ammonia separation tower return tank 10.
Flow controller A17, stripper 6 are provided on pipeline between ammonia separation bottom of tower heat exchanger 8 and vapour system 24
It is provided with flow controller B18, ammonia separation reflux pump 11 and liquid ammonia storage tank on pipeline between ammonia separation tower recuperation pump 7
Flow controller C19 is provided on pipeline between 12.
Flow controller A17, flow controller B18 and flow controller C19 include control valve 26, on control valve 26 simultaneously
It is associated with flowmeter 27.The flowmeter 27 in flowmeter 27 and flow controller A17 in liquid level of flux cascade controller B 15 connects
It is logical.
Above-mentioned high ammonia-nitrogen wastewater ammonia nitrogen removal working-flow：
1) biogas slurry carries out vacuum flash degassing after filter 1 is filtered to remove solid suspension into waste water degassing tank 2
Processing removes fixed gas therein, and tank deck is aspirated using vacuum pump 3, and the operating pressure -0.09Mpa (G) of vacuum pump 3, maximum can
Divisible fixed gas therein；
2) vacuum pump 3 exports fixed gas (mainly air and a small amount of ammonia) to generator flue gas system 21 and burns up；Tank bottom
Waste water through feed pump 4 boosting after by the control of flow and liquid level enter plate heat exchanger 5 exchange heat, biogas slurry into system temperature be 30
DEG C or so, it heats up 200 DEG C or so and enters the separation that stripper 6 carries out NH3 and water, waste water enters heat exchanger from steam stripping ammonia-removing tower
Temperature is about 210 DEG C, enters biochemistry pool 13 for about 30~40 DEG C after heat exchange；
3) about 80 DEG C of tower top material is cooled to 50 DEG C or so into Heat Exchanger in Circulating Water System 99, into ammonia separation tower return tank
10, the tank bottom liquefied ammonia of ammonia separation tower return tank 10 is largely back to the liquid of stripper 6 by the serials control of flow and liquid level
Ammonia reflux nozzle 6.2, fraction are sent outside by flow control to liquid ammonia storage tank outside battery limit (BL) 12；
4) 190~220 DEG C or so of bottom of tower biogas slurry temperature, a part of waste water is after 7 boosting of ammonia separation tower recuperation pump, stream
It measures and stripper 6, ammonia separation bottom of tower is returned to by refluxing opening 6.3 after control is warming up to 220 DEG C or more into ammonia separation bottom of tower heat exchanger 8
8 thermal medium of heat exchanger is the steam that biogas internal combustion generator flue gas or flue gas heat-exchange unit generate, and is saturated and is steamed using 2.0Mpa
Vapour heats materials at bottom of tower, and the flow of flue gas or steam is controlled by liquefied ammonia reflux 6.2 liquefied ammonia regurgitant volume of nozzle, tower
Bottom another part waste water is cooled to 30~40 DEG C by plate heat exchanger 5, passes through the stream of flow and liquid level controlled on the pipeline
Amount, goes biochemistry pool 13 to be further processed.
Other unspecified parts are the prior art.Although above-described embodiment is made that the utility model detailed
Description, but it is only the utility model a part of the embodiment, rather than whole embodiments, people can also be according to this implementations
Example obtains other embodiment under the premise of without creativeness, these embodiments belong to scope of protection of the utility model.
Claims (6)
1. a kind of high ammonia-nitrogen wastewater deamination nitrogen system, it is characterised in that：It includes and organic waste pond (20) sequentially connected mistake
The degassing biogas slurry pipeline of filter (1) and waste water degassing tank (2), waste water degassing tank (2) bottom is connected with feed pump (4) in turn
With the biogas slurry import of plate heat exchanger (5), the escape pipe at the top of the waste water degassing tank (2) be connected in turn vacuum pump (3) and
Generator flue gas system (21),
The biogas slurry outlet of the plate heat exchanger (5) is connected to the feed inlet (6.1) on stripper (6) top, the stripper (6)
The gas outlet (6.5) at top is connected to the air inlet of Heat Exchanger in Circulating Water System (9), and the Heat Exchanger in Circulating Water System (9) is provided at both ends with
Circulating water inlet (22) and circulating water outlet pipe (23), liquefied ammonia outlet and the ammonia separation tower of the Heat Exchanger in Circulating Water System (9) return
Tank (10) inlet communication is flowed, the outlet of the ammonia separation tower return tank (10) is connected to the entrance of ammonia separation reflux pump (11), institute
The outlet for stating ammonia separation reflux pump (11) is connected separately with liquid ammonia storage tank (12) and the liquefied ammonia reflux nozzle on stripper (6) top
(6.2),
The outlet (6.4) of the hot waste water of stripper (6) bottom is connected to the high-temperature inlet water mouth of plate heat exchanger (5), institute
The low temperature water inlet for stating plate heat exchanger (5) is connected to biochemistry pool (13)；Hot waste water outlet (6.4) also with ammonia separation tower
Recuperation pumps the entrance connection of (7), the outlet of the ammonia separation tower recuperation pump (7) and ammonia separation bottom of tower heat exchanger (8)
Waste water inlet connection, the refluxing opening of the wasted water outlet and stripper (6) lower part of ammonia separation bottom of tower heat exchanger (8)
(6.3) it is connected to, the ammonia separation bottom of tower heat exchanger (8) both ends are connected separately with vapour system (24) and condensate system (25).
2. high ammonia-nitrogen wastewater deamination nitrogen system according to claim 1, it is characterised in that：It the feed pump (4) and board-like changes
It is provided with liquid level of flux cascade controller A (14) on pipeline between hot device (5)；The ammonia separation reflux pump (11) is returned with liquefied ammonia
Liquid level of flux cascade controller B (15) is provided on pipeline between flow tube mouth (6.2)；The plate heat exchanger (5) and biochemistry
Liquid level of flux cascade controller C (16) is provided on pipeline between pond (13).
3. high ammonia-nitrogen wastewater deamination nitrogen system according to claim 2, it is characterised in that：The liquid level of flux cascade controller
A (14), liquid level of flux cascade controller B (15) and liquid level of flux cascade controller C (16) include control valve (26), the control
Flowmeter (27) is parallel on valve (26) processed, the flowmeter (27) is connected with liquid level gauge (28), the liquid level of flux tandem control
Three liquid level gauges (28) point in device A (14) processed, liquid level of flux cascade controller B (15) and liquid level of flux cascade controller C (16)
It is not connect with waste water degassing tank (2), stripper (6) and ammonia separation tower return tank (10).
4. high ammonia-nitrogen wastewater deamination nitrogen system according to claim 3, it is characterised in that：Ammonia separation bottom of tower heat exchanger
(8) flow controller A (17) is provided on the pipeline between vapour system (24), the stripper (6) is returned with ammonia separation tower
It is provided with flow controller B (18), the ammonia separation reflux pump (11) and liquid ammonia storage tank on pipeline between stream heat exchange pump (7)
(12) flow controller C (19) is provided on the pipeline between.
5. high ammonia-nitrogen wastewater deamination nitrogen system according to claim 4, it is characterised in that：The flow controller A (17), stream
Amount controller B (18) and flow controller C (19) includes control valve (26), and flowmeter is parallel on the control valve (26)
(27)。
6. high ammonia-nitrogen wastewater deamination nitrogen system according to claim 5, it is characterised in that：The liquid level of flux cascade controller
Flowmeter (27) in B (15) is connected to the flowmeter (27) in flow controller A (17).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721683211.5U CN207671878U (en) | 2017-12-05 | 2017-12-05 | High ammonia-nitrogen wastewater deamination nitrogen system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109958987A (en) * | 2019-04-22 | 2019-07-02 | 湖南福瑞来环保节能科技有限公司 | Animal residue comprehensively utilizes power generator |
| CN115196807A (en) * | 2022-07-21 | 2022-10-18 | 中国科学院山西煤炭化学研究所 | Treatment method for deacidifying and deaminating coal chemical wastewater with enhanced waste heat recovery |
-
2017
- 2017-12-05 CN CN201721683211.5U patent/CN207671878U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109958987A (en) * | 2019-04-22 | 2019-07-02 | 湖南福瑞来环保节能科技有限公司 | Animal residue comprehensively utilizes power generator |
| CN109958987B (en) * | 2019-04-22 | 2024-02-20 | 湖南福瑞来环保节能科技有限公司 | Power generation device for comprehensively utilizing livestock excrement |
| CN115196807A (en) * | 2022-07-21 | 2022-10-18 | 中国科学院山西煤炭化学研究所 | Treatment method for deacidifying and deaminating coal chemical wastewater with enhanced waste heat recovery |
| CN115196807B (en) * | 2022-07-21 | 2024-05-31 | 中国科学院山西煤炭化学研究所 | Treatment method for deacidifying and deaminizing coal chemical wastewater by strengthening waste heat recovery |
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