CN209835693U

CN209835693U - Leachate treatment device

Info

Publication number: CN209835693U
Application number: CN201920587006.1U
Authority: CN
Inventors: 徐永华
Original assignee: Zhongchuang Water Science And Technology Environmental Protection (guangdong) Co Ltd
Current assignee: Zhongchuang Water Science And Technology Environmental Protection (guangdong) Co Ltd
Priority date: 2019-04-26
Filing date: 2019-04-26
Publication date: 2019-12-24
Anticipated expiration: 2029-04-26

Abstract

The utility model aims at providing a leachate treatment device with low energy consumption, low cost and high efficiency of ammonia nitrogen removal. The utility model discloses a preprocessing unit, MVR evaporimeter, compressor and second grade ammonia nitrogen advanced treatment unit, preprocessing unit with the MVR evaporimeter is connected, the steam outlet of MVR evaporimeter with the compressor is connected, second grade ammonia nitrogen advanced treatment unit includes gaseous state membrane treater, gaseous state membrane treater includes the absorption sap cavity, the inside ammonia nitrogen material sap cavity that still is equipped with of absorption sap cavity, the absorption sap cavity with be provided with the hollow fiber microporous membrane between the ammonia nitrogen material sap cavity, ammonia nitrogen material sap cavity with the output of compressor is connected, absorption sap cavity top is provided with steam outlet, steam outlet with the heat exchange assembly of MVR evaporimeter is connected. The utility model discloses be applied to the technical field that landfill leachate handled.

Description

Leachate treatment device

Technical Field

The utility model relates to a leachate treatment device.

Background

The prior art can not thoroughly solve the problem of stable standard discharge of the percolate. The system has unstable operation, long process chain, complex operation and high treatment cost per ton of water. Too many equipment units and high maintenance cost.

Because the leachate has complex components and high pollutant concentration, if a biochemical treatment process is adopted, the sludge culture needs a long time. The activated sludge is easy to die due to the fluctuation of the quality and the quantity of the incoming water, and the recovery is difficult. Especially in winter in northern cold areas, the activated sludge system cannot normally operate at all due to small water amount and low temperature, and the effluent cannot reach the standard. Once the biochemical system is disrupted, it takes a long time to re-incubate the acclimatized sludge because the temperature is too low. The direct back-spraying incineration is carried out, and the adding amount of the percolate is not too large, so that the operation of the incinerator is influenced. This results in a large portion of the percolate not being treated effectively and requiring the addition of further process units. If the reverse osmosis process is adopted, the permeable membrane is easy to block, the recovery rate is low, and the membrane replacement cost is high. The process has higher requirements on the pretreatment process and the water quality index entering the membrane working section has stricter requirements. The ton water consumption and the like increase with the increase of the operation time due to the membrane clogging. During winter operation, the water yield is greatly reduced due to low temperature.

SUMMERY OF THE UTILITY MODEL

The utility model aims to solve the technical problem that overcome prior art not enough, provide a filtration liquid processing apparatus that the energy consumption is low, with low costs, the ammonia nitrogen is deviate from efficiently.

The utility model adopts the technical proposal that: it includes preprocessing unit, MVR evaporimeter, compressor and second grade ammonia nitrogen advanced treatment unit, preprocessing unit with the MVR evaporimeter is connected, the steam outlet of MVR evaporimeter with the compressor is connected, second grade ammonia nitrogen advanced treatment unit includes gaseous state membrane treater, gaseous state membrane treater includes the absorption sap cavity, the inside ammonia nitrogen material sap cavity that still is equipped with of absorption sap cavity, the absorption sap cavity with be provided with the hollow fiber microporous membrane between the ammonia nitrogen material sap cavity, ammonia nitrogen material sap cavity with the output of compressor is connected, the top in absorption sap cavity is provided with steam outlet, steam outlet with the heat exchange assembly of MVR evaporimeter is connected.

According to the scheme, the leachate is pretreated through the pretreatment unit, the MVR evaporator is used for achieving evaporation concentration of the leachate, the vapor discharged from the MVR evaporator is compressed into a high-temperature high-pressure solution through the compressor, ammonia nitrogen components in the high-temperature high-pressure solution are absorbed through the gaseous membrane processor, and then the distilled water meeting the discharge standard is obtained through condensation treatment. The hollow fiber microporous membrane is used for isolating a barrier which is used for containing ammonia feed liquid and absorption liquid, and free NH in the feed liquid₃Diffusion to the hydrophobic microporous membrane surface through a concentration boundary layer on the wastewater side followed by NH on both sides of the membrane₃Driven by a partial pressure difference, NH₃The waste water and the microporous membrane interface are gasified and enter the membrane pores, and then are diffused to enter the absorption liquid side to perform rapid irreversible reaction with the acidic absorption liquid, so that the aim of removing/recycling the ammonia nitrogen is fulfilled. The MVR evaporator has the characteristic of low energy consumption.

According to a preferable scheme, the secondary ammonia nitrogen advanced treatment unit further comprises a washing purifier, the washing purifier is positioned between a steam outlet of the MVR evaporator and the compressor, and the washing purifier comprises a gas washing unit and a gas alkali washing unit which are sequentially connected.

According to the scheme, the steam is preliminarily purified by the washing purifier, and most of ammonia nitrogen components and organic matters contained in the steam are removed.

According to a preferable scheme, the pretreatment unit further comprises a stock solution tank, a mixer, a reaction tank, a sedimentation tank and an intermediate tank which are sequentially connected, the intermediate tank is connected with the MVR evaporator, the leachate treatment device further comprises a sludge concentration tank and a filter press which are connected, the sludge concentration tank is connected with the sedimentation tank, and the water outlet end of the filter press is connected with the intermediate tank.

As can be seen from the scheme, the percolate gas is firstly treated in the mixer and is output to the reaction tank, so that the acid consumption and part of VOC of the subsequent process are reduced. And after the requirement of the retention time required by aeration is met, sending the percolate in the reaction tank to the sedimentation tank for removing sludge sediments in the aerated percolate, sending the precipitated supernatant into an intermediate tank, directly discharging the sludge into a sludge concentration tank, dehydrating the sludge through a filter press, sending the pressed liquid back to the intermediate tank, and transporting the sludge blocks to be treated. And adding acid to the percolate in the intermediate tank to adjust the pH value, stirring by using a jet system, and generally controlling the pH value of the feed liquid to 4-6.

One preferred scheme is, the MVR evaporimeter still includes evaporation chamber and circulating pump, heat exchange assembly link up the evaporation chamber, the input port of circulating pump with the bottom in evaporation chamber is connected, the delivery outlet of circulating pump with the top in evaporation chamber is connected.

According to the scheme, the MVR evaporator adopts the principle of falling film evaporation and condensation, a continuous and stable evaporation process is realized under an automatic control unit, percolate stock solution to be treated enters the MVR evaporator after being preheated and is mixed with concentrated percolate, the percolate flows back to the upper part of the evaporation cavity through the circulating pump, the percolate is uniformly distributed on the heat exchange assembly, the percolate boils on the outer surface of the heat exchange assembly and is partially vaporized in the downward flowing process of the heat exchange assembly, and the residual part is collected at the lower part of the evaporator, namely concentrated solution.

One preferred scheme is, leachate treatment device still includes exhaust condenser, distilled water jar and the pond of keeping in that goes out water, the steam of second grade ammonia nitrogen advanced treatment unit output gets into condensation behind the heat exchange assembly is the distilled water, exhaust condenser's air inlet with the heat exchange assembly is linked together, the delivery port of heat exchange assembly the delivery port of exhaust condenser all with the distilled water jar is connected, the delivery port of distilled water jar with the pond of keeping in that goes out water is connected.

In a preferred embodiment, the hollow fiber microporous membrane is a hydrophobic membrane.

Drawings

Fig. 1 is a schematic connection diagram of the present invention;

FIG. 2 is a simplified flow diagram of the present invention;

FIG. 3 is a schematic diagram of the configuration of the gaseous membrane processor.

Detailed Description

As shown in fig. 1, fig. 2 and fig. 3, in this embodiment, the utility model discloses a pretreatment unit 1, MVR evaporimeter 2, compressor 3 and second grade ammonia nitrogen deep treatment unit 4, pretreatment unit 1 with MVR evaporimeter 2 is connected, MVR evaporimeter 2's steam outlet with compressor 3 is connected, second grade ammonia nitrogen deep treatment unit 4 includes the gaseous state membrane treater, the gaseous state membrane treater includes absorption liquid chamber 41, absorption liquid chamber 41 is inside still to be equipped with ammonia nitrogen material liquid chamber 42, absorption liquid chamber 41 with be provided with hollow fiber microporous membrane 43 between the ammonia nitrogen material liquid chamber 42, ammonia nitrogen material liquid chamber 42 with the output of compressor 3 is connected, the top of absorption liquid chamber 41 is provided with steam outlet 44, steam outlet 44 with MVR evaporimeter 2's heat exchange component 21 is connected.

In this embodiment, second grade ammonia nitrogen advanced treatment unit 4 still includes the scrubber, the scrubber is located the steam outlet of MVR evaporimeter 2 with between the compressor 3, the scrubber is including the gaseous pickling unit and the gaseous alkaline washing unit that connect gradually.

In this embodiment, the pretreatment unit 1 further includes a raw liquid tank 11, a mixer 12, a reaction tank 13, a sedimentation tank 14, and an intermediate tank 15, which are connected in sequence, the intermediate tank 15 is connected to the MVR evaporator 2, the leachate treatment apparatus further includes a sludge concentration tank 5 and a filter press 6, which are connected to each other, the sludge concentration tank 5 is connected to the sedimentation tank 14, and a water outlet end of the filter press 6 is connected to the intermediate tank 15.

In this embodiment, the pretreatment unit 1 further includes a plurality of pretreatment agent tanks for storing various pretreatment agents, and the plurality of pretreatment tanks are connected to the mixer 12.

In this embodiment, the MVR evaporator 2 further includes an evaporation cavity 22 and a circulation pump 23, the heat exchange assembly 21 penetrates through the evaporation cavity 22, an input port of the circulation pump 23 is connected with the bottom of the evaporation cavity 22, and an output port of the circulation pump 23 is connected with the top of the evaporation cavity 22.

Leachate treatment device still includes exhaust condenser 7, distilled water jar 8 and goes out water and keeps in pond 9, the steam of second grade ammonia nitrogen advanced treatment unit 4 output gets into condensation is the distilled water behind the heat exchange assembly 21, exhaust condenser 7 the air inlet with heat exchange assembly 21 is linked together, heat exchange assembly 21 the delivery port exhaust condenser 7 the delivery port all with distilled water jar 8 is connected, distilled water jar 8 the delivery port with go out water and keep in pond 9 and connect.

In the present embodiment, the hollow fiber microporous membrane 43 is a hydrophobic membrane.

The utility model discloses a work flow includes following step:

a. sending the percolate to be treated to the pretreatment unit 1 for pretreatment;

b. sending the pretreated percolate into the MVR evaporator 2, storing the percolate at the bottom of the evaporation cavity 22 after entering the evaporation cavity 22, vaporizing the water in the percolate under the action of the temperature of the evaporation cavity 22, volatilizing ammonia nitrogen gas, and pumping the concentrated percolate out of an external concentrated solution tank for backfilling;

c. the circulating pump 23 pumps the percolate at the bottom of the evaporation cavity 22 to the upper part of the heat exchange assembly 21, and the percolate is uniformly sprayed on the outer surface of the heat exchange assembly 21 through a plurality of nozzles to form a film and is subjected to secondary evaporation;

d. the steam formed after the leachate is evaporated sequentially passes through a gas acid washing unit and a gas alkali washing unit so as to remove 99% of ammonia nitrogen and 99% of CODcr in the steam;

e. then the steam enters the compressor 3 and is compressed into a high-temperature and high-pressure solution, the high-temperature and high-pressure solution enters the ammonia nitrogen material liquid cavity 42 from the bottom, and the NH3 in the solution is absorbed by the absorption liquid in the absorption liquid cavity 41 through the hollow fiber microporous membrane 43;

f. when the solution reaches the top, the solution is converted into NH 3-removed steam under the action of temperature and air pressure, the steam enters the inside of the heat exchange assembly 21 from the steam outlet 44, at the moment, the steam exchanges heat with percolate on the outer surface of the heat exchange assembly 21 and is further condensed into distilled water to flow into the distilled water tank 8, gas which is not condensed in the heat exchange assembly 21 enters the exhaust condenser 7 to be secondarily condensed, and the distilled water obtained by secondary condensation flows into the distilled water tank 8;

g. distilled water in the distilled water tank 8 is sent to the temporary effluent storage tank 9, and the water in the temporary effluent storage tank 9 can be discharged when the water quality reaches the standard and is used as cooling water or discharged in a system.

The absorption liquid is sulfuric acid or hydrochloric acid or a renewable absorbent.

Sulfuric acid is stored in the gas acid washing unit, ammonia nitrogen in the steam reacts with the sulfuric acid to form ammonium sulfate when the steam passes through the gas acid washing unit, sodium hydroxide is stored in the gas alkali washing unit, and organic matters in the steam react with the sodium hydroxide when the steam passes through the gas alkali washing unit.

The utility model discloses be applied to the technical field that landfill leachate handled.

While the embodiments of the present invention have been described in terms of practical embodiments, they are not intended to limit the scope of the invention, and modifications of the embodiments and combinations with other embodiments will be apparent to those skilled in the art in light of the present description.

Claims

1. A leachate treatment device, which is characterized in that: it comprises a pretreatment unit (1), an MVR evaporator (2), a compressor (3) and a secondary ammonia nitrogen deep treatment unit (4), the pretreatment unit (1) is connected with the MVR evaporator (2), a steam outlet of the MVR evaporator (2) is connected with the compressor (3), the secondary ammonia nitrogen advanced treatment unit (4) comprises a gaseous film processor which comprises an absorption liquid cavity (41), an ammonia nitrogen material liquid cavity (42) is also arranged in the absorption liquid cavity (41), a hollow fiber microporous membrane (43) is arranged between the absorption liquid cavity (41) and the ammonia nitrogen material liquid cavity (42), the ammonia nitrogen liquid cavity (42) is connected with the output end of the compressor (3), the top of the absorption liquid cavity (41) is provided with a vapor outlet (44), and the vapor outlet (44) is connected with a heat exchange component (21) of the MVR evaporator (2).

2. The leachate treatment plant of claim 1, wherein: the secondary ammonia nitrogen advanced treatment unit (4) further comprises a washing purifier, the washing purifier is located between a steam outlet of the MVR evaporator (2) and the compressor (3), and the washing purifier comprises a gas washing unit and a gas alkali washing unit which are sequentially connected.

3. The leachate treatment plant of claim 1, wherein: the pretreatment unit (1) further comprises a stock solution tank (11), a mixer (12), a reaction tank (13), a sedimentation tank (14) and an intermediate tank (15) which are sequentially connected, the intermediate tank (15) is connected with the MVR evaporator (2), the percolate treatment device further comprises a sludge concentration tank (5) and a filter press (6) which are connected, the sludge concentration tank (5) is connected with the sedimentation tank (14), and the water outlet end of the filter press (6) is connected with the intermediate tank (15).

4. The leachate treatment plant of claim 1, wherein: MVR evaporimeter (2) still include evaporation chamber (22) and circulating pump (23), heat exchange assembly (21) link up evaporation chamber (22), the input port of circulating pump (23) with the bottom in evaporation chamber (22) is connected, the delivery outlet of circulating pump (23) with the top in evaporation chamber (22) is connected.

5. The leachate treatment plant of claim 1, wherein: leachate treatment device still includes exhaust condenser (7), distilled water jar (8) and goes out water and keeps in pond (9), the steam of second grade ammonia nitrogen advanced treatment unit (4) output gets into heat exchange assemblies (21) back condensation is the distilled water, the air inlet of exhaust condenser (7) with heat exchange assemblies (21) are linked together, the delivery port of heat exchange assemblies (21) the delivery port of exhaust condenser (7) all with distilled water jar (8) are connected, the delivery port of distilled water jar (8) with go out water and keep in pond (9) and connect.

6. The leachate treatment plant of claim 1, wherein: the hollow fiber microporous membrane (43) is a hydrophobic membrane.