CN112897786A - Ammonia distillation system - Google Patents

Ammonia distillation system Download PDF

Info

Publication number
CN112897786A
CN112897786A CN202110289019.2A CN202110289019A CN112897786A CN 112897786 A CN112897786 A CN 112897786A CN 202110289019 A CN202110289019 A CN 202110289019A CN 112897786 A CN112897786 A CN 112897786A
Authority
CN
China
Prior art keywords
communicated
pipeline
deamination
tower
pump
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.)
Pending
Application number
CN202110289019.2A
Other languages
Chinese (zh)
Inventor
陈卫华
田弘毅
华银锋
张海涛
唐聪
乔磊
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shanghai Liming Resources Reuse Co ltd
Original Assignee
Shanghai Liming Resources Reuse Co ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Shanghai Liming Resources Reuse Co ltd filed Critical Shanghai Liming Resources Reuse Co ltd
Priority to CN202110289019.2A priority Critical patent/CN112897786A/en
Publication of CN112897786A publication Critical patent/CN112897786A/en
Pending legal-status Critical Current

Links

Images

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
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/26—Carbonates or bicarbonates of ammonium
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C02F5/06—Softening water by precipitation of the hardness using calcium compounds
    • 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
    • C02F1/048—Purification of waste water by 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
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
    • 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
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • 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
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/06—Contaminated groundwater or leachate
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/05—Conductivity or salinity
    • C02F2209/055—Hardness
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/07—Alkalinity
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/16—Total nitrogen (tkN-N)

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Physical Water Treatments (AREA)
  • Degasification And Air Bubble Elimination (AREA)

Abstract

The invention discloses an ammonia distillation system, and belongs to the technical field of organic solid waste treatment. The ammonia distillation system comprises a raw water tank, a heat exchanger, a negative pressure desorption tower, a deamination tower, a condenser, a gas-liquid separator, an absorption tower, an alkali liquor storage tank and a pH adjusting device; the top of the raw water tank is provided with a feed inlet for introducing raw water and a defoaming agent into the raw water tank, and the bottom of the raw water tank is communicated with the heat exchanger through a No. one conveying assembly; the bottom of the deamination tower is communicated with the heat exchanger through a two-grade conveying assembly. This device operation is normal, stable, and is very showing to the removal effect of ammonia nitrogen, and the clearance is stable more than 90%, and the basicity is lower comparatively obvious, so along with a large amount of ammonium carbonate and ammonium bicarbonate generate, hardness reduction to the conductivity reduces comparatively showing, provides the advantage to subsequent membrane processing system, can effectively reduce good oxygen section operating load, need not add the carbon source again, reduces fan load simultaneously.

Description

Ammonia distillation system
Technical Field
The invention relates to an ammonia distillation system, and belongs to the technical field of organic solid waste treatment.
Background
The landfill leachate has complex water quality, and particularly has the characteristics of high COD, high ammonia nitrogen, high SS, high hardness, high alkalinity, large peculiar smell and the like, so that the treatment difficulty of the existing leachate is greatly improved. Meanwhile, the national requirements for the discharge of percolate are increasingly strict, particularly in the aspects of ammonia nitrogen and total nitrogen.
The existing ammonia distillation pilot plant needs to be capable of efficiently removing ammonia nitrogen in water aiming at complex water quality of kitchen waste after anaerobic fermentation. However, the ammonia distillation system has the following problems:
1. the efficiency of removing ammonia nitrogen in the sewage is low;
2. the COD removal effect is not good;
3. the conductivity reduction is not significant;
4. the alkalinity is not obviously reduced;
therefore, in order to solve the problems, it is necessary to design an ammonia distillation system.
Disclosure of Invention
The present invention is implemented by the following technical solutions in view of the technical problems mentioned in the background art:
the ammonia distillation system comprises a raw water tank, a heat exchanger, a negative pressure desorption tower, a deamination tower, a condenser, a gas-liquid separator, an absorption tower, an alkali liquor storage tank and a PH adjusting device;
the top of the raw water tank is provided with a feed inlet for introducing raw water and a defoaming agent into the raw water tank, and the bottom of the raw water tank is communicated with the heat exchanger through a No. one conveying assembly;
the bottom of the deamination tower is communicated with a heat exchanger through a two-type conveying assembly, and one output end of the heat exchanger is communicated with the top side wall of the negative pressure desorption tower through a pipeline;
the other output end of the heat exchanger is communicated with the bottom side wall of the PH adjusting device through a pipeline;
the bottom of the negative pressure analysis tower is communicated with the deamination tower through a three-way conveying assembly, the top of the negative pressure analysis tower is communicated with the top of the condenser through a one-way gas conveying pipe, and the side wall of one side of the negative pressure analysis tower is also communicated with the top of the deamination tower through a one-way gas conveying pipe;
one end of the condenser is also communicated with the gas-liquid separator through a pipeline;
the gas-liquid separator is communicated with the negative pressure analysis tower through a four-number conveying assembly;
the gas-liquid separator is also communicated with the top of the absorption tower through a pipeline;
the bottom of the absorption tower is communicated with an output pipe, the bottom of the alkali liquor storage tank is also communicated with the output pipe through a pipeline, and the other end of the output pipe is communicated with a four-number conveying assembly;
a vacuum input assembly is communicated between the top and the bottom of the absorption tower;
the top of the absorption tower is also communicated with the bottom of the PH adjusting device through an aeration component.
It should be noted that: the PH adjusting device refers to a carbon dioxide PH adjusting device and is mainly used for adjusting the PH of the effluent of the ammonia distillation system, namely the effluent of sewage.
It should also be noted that: the gas-liquid separator is used for separating high-purity ammonia gas from water and absorbing and utilizing the ammonia gas in an external recovery tower.
It should be noted that the antifoaming agent is a T350 antifoaming agent.
As a preferable example, the one-size conveying assembly comprises a water inlet pump, the input end of the water inlet pump is communicated with the bottom of the raw water tank through a pipeline, and the water outlet end of the water inlet pump is communicated with one side wall of the bottom of the heat exchanger through a pipeline.
As a preferred example, the secondary conveying assembly comprises a deamination water pump, an input end of the deamination water pump is communicated with the bottom of the deamination tower through a pipeline, and an output end of the deamination water pump is communicated with the other side wall of the bottom of the heat exchanger through one pipeline;
the output end of the deamination water pump is communicated with the communicated pipeline through another pipeline and is communicated with one side of the bottom of the deamination tower.
As a preferred example, the three-way conveying assembly comprises a deamination lifting pump, the input end of the deamination lifting pump is communicated with the bottom of the negative pressure analysis tower through a pipeline, and the output end of the deamination lifting pump is communicated with the bottom of one side of the negative pressure analysis tower through one pipeline;
the pipeline that the output of deamination elevator pump communicates still is linked together with the deamination tower through another pipeline.
As a preferred example, the top of one side of the condenser is also communicated with a first water outlet pipe and a first water inlet pipe, and the first water outlet pipe is positioned above the first water inlet pipe.
As a preferred example, the four-number conveying assembly comprises a deamination reflux pump, the bottom of the gas-liquid separator is communicated with the deamination reflux pump through a pipeline, and the output end of the deamination reflux pump is communicated with the top side wall of the negative pressure desorption tower through a pipeline;
the pipeline connected to the output end of the deamination reflux pump is also communicated with a branch pipe, the other end of the branch pipe is communicated with one side wall of the gas-liquid separator, and the other end of the gas-liquid separator is connected with a pipe for discharging ammonia water;
the other end of the output pipe is communicated with a pipeline communicated between the gas-liquid separator and the deamination reflux pump.
As a preferred example, the vacuum input assembly comprises a vacuum pump, an input end of the vacuum pump is communicated with the bottom of the absorption tower through a pipeline, and an output end of the vacuum pump is communicated with the top of the absorption tower through a pipeline;
and a second water inlet pipe and a second water outlet pipe are respectively communicated on a pipeline communicated between the vacuum pump and the absorption tower, and the second water outlet pipe is positioned above the second water inlet pipe.
As a preferable example, the aeration assembly comprises an aeration pump and a second air conveying pipe, the input end of the aeration pump is communicated with the top of the absorption tower through the second air conveying pipe, and the output end of the aeration pump is communicated with the bottom of the PH adjusting device through the second air conveying pipe.
As a preferable example, the top of the PH adjusting device is communicated with an air inlet pipe for communicating with an external CO steel cylinder, and the top of one side of the PH adjusting device is also communicated with a sewage discharge pipe.
It should be noted that: the gas in the secondary gas pipe is air and CO2，The gas in the gas delivery pipe A is CO2And NH3The cooling water flows in the first water outlet pipe, the first water inlet pipe, the second water outlet pipe and the second water inlet pipe, and the sewage flows in the other pipelines.
The invention has the beneficial effects that: this device operation is normal, stable, and is very showing to the removal effect of ammonia nitrogen, and the clearance is stable more than 90%, and the basicity is lower comparatively obvious, so along with a large amount of ammonium carbonate and ammonium bicarbonate generate, hardness reduction to the conductivity reduces comparatively showing, provides the advantage to subsequent membrane processing system, can effectively reduce good oxygen section operating load, need not add the carbon source again, reduces fan load simultaneously.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
In the figure: the device comprises a raw water tank 1, a heat exchanger 2, a negative pressure analysis tower 3, a deamination tower 4, a condenser 5, a gas-liquid separator 6, an absorption tower 7, an alkali liquor storage tank 8, a PH adjusting device 9, a water inlet pump 10, a deamination water pump 11, a deamination lift pump 12, a deamination reflux pump 13, a vacuum pump 14 and an aeration pump 15.
Detailed Description
In order to make the technical means, the original characteristics, the achieved purpose and the efficacy of the invention easy to understand, the invention is further described with reference to the specific drawings.
As shown in fig. 1, the ammonia distillation system comprises a raw water tank 1, a heat exchanger 2, a negative pressure desorption tower 3, a deamination tower 4, a condenser 5, a gas-liquid separator 6, an absorption tower 7, an alkali liquor storage tank 8 and a PH adjusting device 9;
the top of the raw water tank 1 is provided with a feed inlet for introducing raw water and a defoaming agent into the raw water tank 1, and the bottom of the raw water tank 1 is communicated with the heat exchanger 2 through a No. one conveying assembly;
the bottom of the deamination tower 4 is communicated with the heat exchanger 2 through a two-type conveying assembly, and one output end of the heat exchanger 2 is communicated with the top side wall of the negative pressure desorption tower 3 through a pipeline;
the other output end of the heat exchanger 2 is communicated with the side wall of the bottom of the PH adjusting device 9 through a pipeline;
the bottom of the negative pressure analysis tower 3 is communicated with the deamination tower 4 through a three-way conveying assembly, the top of the negative pressure analysis tower 3 is communicated with the top of the condenser 5 through a one-way gas conveying pipe, and the side wall of one side of the negative pressure analysis tower 3 is also communicated with the top of the deamination tower 4 through a one-way gas conveying pipe;
one end of the condenser 5 is also communicated with a gas-liquid separator 6 through a pipeline;
the gas-liquid separator 6 is communicated with the negative pressure analysis tower 3 through a four-number conveying assembly;
the gas-liquid separator 6 is also communicated with the top of the absorption tower 7 through a pipeline;
the bottom of the absorption tower 7 is communicated with an output pipe, the bottom of the alkali liquor storage tank 8 is also communicated with the output pipe through a pipeline, and the other end of the output pipe is communicated with a No. four conveying assembly;
a vacuum input assembly is communicated between the top and the bottom of the absorption tower 7;
the top of the absorption tower 7 is also communicated with the bottom of the PH adjusting device 9 through an aeration component.
The first conveying component comprises a water inlet pump 10, the input end of the water inlet pump 10 is communicated with the bottom of the raw water tank 1 through a pipeline, and the water outlet end of the water inlet pump 10 is communicated with one side wall of the bottom of the heat exchanger 2 through a pipeline.
The second conveying assembly comprises a deamination water pump 11, the input end of the deamination water pump 11 is communicated with the bottom of the deamination tower 4 through a pipeline, and the output end of the deamination water pump 11 is communicated with the other side wall of the bottom of the heat exchanger 2 through one pipeline;
the pipeline communicated with the output end of the deamination water pump 11 is also communicated with one side of the bottom of the deamination tower 4 through another pipeline.
The third conveying assembly comprises a deamination lifting pump 12, the input end of the deamination lifting pump 12 is communicated with the bottom of the negative pressure analysis tower 3 through a pipeline, and the output end of the deamination lifting pump 12 is communicated with the bottom of one side of the negative pressure analysis tower 3 through one pipeline;
the pipeline communicated with the output end of the deamination lift pump 12 is also communicated with the deamination tower 4 through another pipeline.
The top of one side of condenser 5 still communicates No. one outlet pipe and No. one inlet tube, and No. one outlet pipe is located the top of inlet tube of No. one.
The four-number conveying assembly comprises a deamination reflux pump 13, the bottom of the gas-liquid separator 6 is communicated with the deamination reflux pump 13 through a pipeline, and the output end of the deamination reflux pump 13 is communicated with the top side wall of the negative pressure desorption tower 3 through a pipeline;
a pipeline connected to the output end of the deamination reflux pump 13 is also communicated with a branch pipe, the other end of the branch pipe is communicated with one side wall of the gas-liquid separator 6, and the other end of the gas-liquid separator 6 is connected with a pipe for discharging ammonia water;
the other end of the output pipe is communicated with a pipeline communicated between the gas-liquid separator 6 and the deamination reflux pump 13.
The vacuum input assembly comprises a vacuum pump 14, the input end of the vacuum pump 14 is communicated with the bottom of the absorption tower 7 through a pipeline, and the output end of the vacuum pump 14 is communicated with the top of the absorption tower 7 through a pipeline;
a second water inlet pipe and a second water outlet pipe are respectively communicated on a pipeline communicated between the vacuum pump 14 and the absorption tower 7, and the second water outlet pipe is positioned above the second water inlet pipe.
The aeration component comprises an aeration pump 15 and a double-type gas pipe, the input end of the aeration pump 15 is communicated with the top of the absorption tower 7 through the double-type gas pipe, and the output end of the aeration pump 15 is communicated with the bottom of the PH adjusting device through the double-type gas pipe.
The top of the PH adjusting device 9 is communicated with an air inlet pipe for communicating external CO2The top of one side of the steel cylinder and the PH adjusting device 9 is also communicated with a sewage discharge pipe.
The working principle is as follows: in the operation process of the device, water after high-temperature deamination at the bottom of the deamination tower 4 is adopted to preheat an ammonia distillation system, and then the water enters the negative pressure desorption tower 3 and the deamination tower 4 in sequence, the flow directions of percolate in the negative pressure desorption tower 3 and the deamination tower 4 are both from top to bottom, and steam is opposite to the flow directions of percolate in the negative pressure desorption tower 3 and the deamination tower 4 so as to improve the mass transfer efficiency of gas and liquid and ensure good deamination effect;
the negative pressure analysis tower 3 mainly has the functions of percolating by steam heating aiming at the characteristics of high hardness, high alkalinity and easy scaling of percolate; the alkalinity such as HCO 3-in the leachate is decomposed into CO32-, CO2 and the like, and then the alkalinity is combined with hardness ions such as Ca2+ and Mg2+ in the leachate to generate calcium carbonate and other small particles, so that the hardness is reduced, and then the calcium carbonate and the small particles enter a deamination tower along with the leachate;
ammonia nitrogen in the percolate rises to the top of the deamination tower 4 under the action of steam stripping, is cooled by a condenser 5, enters an absorption tower 7 and finally enters an alkali liquor storage tank 8; the ammonia nitrogen is recovered in the form of ammonia water and then is used for denitration of flue gas of a surface incineration plant and a biogas power plant.
In addition, the device is added with a vacuumizing input assembly, so that the vacuumizing speed and the upper limit of the vacuum degree are improved; the ammonia water recovery position is changed from the previous absorption tower 7 to the current gas-liquid separator 6.
The following table is statistical data for PH, alkalinity, hardness, conductivity, COD and total nitrogen for an ammonia distillation system:
Figure BDA0002981676180000071
Figure BDA0002981676180000081
Figure BDA0002981676180000091
Figure BDA0002981676180000101
through last table, to organic matter sewage system intake carry out ammonia distillation and handle and can discover:
1. the ammonia nitrogen removal effect is obvious, and the ammonia nitrogen removal rate is over 90 percent;
2. the COD removal rate is about 20 percent;
3. the conductivity reduction is obvious, and the conductivity of the effluent is basically less than 10000 mus/cm;
4. the alkalinity is obviously reduced from more than 10000mg/L of inlet water to about 2000mg/L, and simultaneously, the PH is increased from about 8.5 of inlet water to about 9.7.
The foregoing shows and describes the general principles and broad features of the present invention and advantages thereof. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that various changes and modifications may be made without departing from the spirit and scope of the invention as defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.

Claims (9)

1. Ammonia distillation system, its characterized in that: comprises a raw water tank (1), a heat exchanger (2), a negative pressure desorption tower (3), a deamination tower (4), a condenser (5), a gas-liquid separator (6), an absorption tower (7), an alkali liquor storage tank (8) and a PH adjusting device (9);
the top of the raw water tank (1) is provided with a feeding hole for feeding raw water and a defoaming agent into the raw water tank (1), and the bottom of the raw water tank (1) is communicated with the heat exchanger (2) through a No. one conveying assembly;
the bottom of the deamination tower (4) is communicated with the heat exchanger (2) through a two-type conveying assembly, and one output end of the heat exchanger (2) is communicated with the top side wall of the negative pressure desorption tower (3) through a pipeline;
the other output end of the heat exchanger (2) is communicated with the side wall of the bottom of the PH adjusting device (9) through a pipeline;
the bottom of the negative pressure analysis tower (3) is communicated with the deamination tower (4) through a three-way conveying assembly, the top of the negative pressure analysis tower (3) is communicated with the top of the condenser (5) through a one-way gas conveying pipe, and the side wall of one side of the negative pressure analysis tower (3) is also communicated with the top of the deamination tower (4) through a one-way gas conveying pipe;
one end of the condenser (5) is also communicated with the gas-liquid separator (6) through a pipeline;
the gas-liquid separator (6) is communicated with the negative pressure analysis tower (3) through a four-number conveying assembly;
the gas-liquid separator (6) is also communicated with the top of the absorption tower (7) through a pipeline;
the bottom of the absorption tower (7) is communicated with an output pipe, the bottom of the alkali liquor storage tank (8) is also communicated with the output pipe through a pipeline, and the other end of the output pipe is communicated with a Sida conveying assembly;
a vacuum input assembly is communicated between the top and the bottom of the absorption tower (7);
the top of the absorption tower (7) is also communicated with the bottom of the PH adjusting device (9) through an aeration component.
2. The ammonia distillation system of claim 1, wherein: the No. one conveying assembly comprises a water inlet pump (10), the input end of the water inlet pump (10) is communicated with the bottom of the raw water tank (1) through a pipeline, and the water outlet end of the water inlet pump (10) is communicated with one side wall of the bottom of the heat exchanger (2) through a pipeline.
3. The ammonia distillation system of claim 1, wherein: the conveying assembly II comprises a deamination water pump (11), the input end of the deamination water pump (11) is communicated with the bottom of the deamination tower (4) through a pipeline, and the output end of the deamination water pump (11) is communicated with the other side wall of the bottom of the heat exchanger (2) through one pipeline;
the output end of the deamination water pump (11) is communicated with the communicated pipeline through another pipeline and is communicated with one side of the bottom of the deamination tower (4).
4. The ammonia distillation system of claim 1, wherein: the third conveying assembly comprises a deamination lifting pump (12), the input end of the deamination lifting pump (12) is communicated with the bottom of the negative pressure analysis tower (3) through a pipeline, and the output end of the deamination lifting pump (12) is communicated with the bottom of one side of the negative pressure analysis tower (3) through one pipeline;
the pipeline communicated with the output end of the deamination lifting pump (12) is also communicated with the deamination tower (4) through another pipeline.
5. The ammonia distillation system of claim 1, wherein: the top of one side of condenser (5) still communicates No. one outlet pipe and No. one inlet tube, just No. one outlet pipe is located the top of the inlet tube of No. one.
6. The ammonia distillation system of claim 1, wherein: the four-number conveying assembly comprises a deamination reflux pump (13), the bottom of the gas-liquid separator (6) is communicated with the deamination reflux pump (13) through a pipeline, and the output end of the deamination reflux pump (13) is communicated with the top side wall of the negative pressure analysis tower (3) through a pipeline;
a pipeline connected to the output end of the deamination reflux pump (13) is also communicated with a branch pipe, the other end of the branch pipe is communicated with one side wall of the gas-liquid separator (6), and the other end of the gas-liquid separator (6) is connected with a pipe for discharging ammonia water;
the other end of the output pipe is communicated with a pipeline communicated between the gas-liquid separator (6) and the deamination reflux pump (13).
7. The ammonia distillation system of claim 1, wherein: the vacuum input assembly comprises a vacuum pump (14), the input end of the vacuum pump (14) is communicated with the bottom of the absorption tower (7) through a pipeline, and the output end of the vacuum pump (14) is communicated with the top of the absorption tower (7) through a pipeline;
a second water inlet pipe and a second water outlet pipe are respectively communicated with a pipeline communicated between the vacuum pump (14) and the absorption tower (7), and the second water outlet pipe is positioned above the second water inlet pipe.
8. The ammonia distillation system of claim 1, wherein: the aeration component comprises an aeration pump (15) and a secondary gas pipe, the input end of the aeration pump (15) is communicated with the top of the absorption tower (7) through the secondary gas pipe, and the output end of the aeration pump (15) is communicated with the bottom of the PH adjusting device through the secondary gas pipe.
9. The ammonia distillation system of claim 1, wherein: the top of the PH adjusting device (9) is communicated with an air inlet pipe for communicating external CO2The top of one side of the PH adjusting device (9) is also communicated with a sewage discharge pipe.
CN202110289019.2A 2021-03-18 2021-03-18 Ammonia distillation system Pending CN112897786A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202110289019.2A CN112897786A (en) 2021-03-18 2021-03-18 Ammonia distillation system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202110289019.2A CN112897786A (en) 2021-03-18 2021-03-18 Ammonia distillation system

Publications (1)

Publication Number Publication Date
CN112897786A true CN112897786A (en) 2021-06-04

Family

ID=76105326

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202110289019.2A Pending CN112897786A (en) 2021-03-18 2021-03-18 Ammonia distillation system

Country Status (1)

Country Link
CN (1) CN112897786A (en)

Similar Documents

Publication Publication Date Title
CN107399876B (en) A kind of processing method of high ammonia-nitrogen wastewater
CN101659451A (en) Method for treating high-salt water by air stripping type membrane distillation
CN214936748U (en) Ammonia distillation system
CN211226612U (en) Integrated treatment device for removing hydrogen sulfide in landfill leachate
CN212609636U (en) Evaporation device with direct contact heat transfer and indirect contact heat transfer coupling
CN212222702U (en) High-efficient low temperature negative pressure ammonia nitrogen waste water strip system
CN112707504A (en) Method and device for improving treatment efficiency of anaerobic reactor in pharmaceutical wastewater treatment process
CN117164037A (en) Concentrated crystallization of high salt wastewater contains salt desalination water processing apparatus through heat pump
CN112897786A (en) Ammonia distillation system
CN217077289U (en) Anaerobic system capable of tolerating high-concentration ammonia nitrogen
CN111285493A (en) Integrated device for source separation urine treatment by using supergravity technology
CN216073129U (en) High-concentration landfill leachate treatment device
CN214115259U (en) Treatment system for realizing zero discharge of landfill leachate and fermented biogas slurry
CN215886992U (en) Carbon dioxide internal circulation biogas fermentation carbon reduction system
CN112142264B (en) Treatment system and method for realizing zero emission of landfill leachate and fermented biogas slurry
CN211712738U (en) Water treatment system based on split type anaerobic membrane bioreactor
CN112624520B (en) Resource treatment method based on nitrogen balance of waste incineration power plant
CN212334746U (en) Anaerobic reactor for wastewater treatment
CN113816549A (en) Ammonia nitrogen recovery method in kitchen waste treatment process
CN113880166A (en) High-concentration landfill leachate treatment process and device
CN210656543U (en) Materialization deamination processing system of landfill leachate anaerobism play water
CN111099723A (en) Water treatment system and method based on split type anaerobic membrane bioreactor
CN113502210A (en) Carbon dioxide internal circulation biogas fermentation carbon reduction method
CN220618504U (en) High-efficient denitrification negative pressure low temperature evaporation plant
CN111777126A (en) Device and method for treating salt-containing wastewater by using flue gas waste heat

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