CN106186127B - Thermal evaporation concentration device for treating membrane concentrated solution - Google Patents
Thermal evaporation concentration device for treating membrane concentrated solution Download PDFInfo
- Publication number
- CN106186127B CN106186127B CN201610556652.2A CN201610556652A CN106186127B CN 106186127 B CN106186127 B CN 106186127B CN 201610556652 A CN201610556652 A CN 201610556652A CN 106186127 B CN106186127 B CN 106186127B
- Authority
- CN
- China
- Prior art keywords
- flue gas
- membrane
- concentrated solution
- concentrate
- evaporation tank
- 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.)
- Active
Links
Images
Classifications
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention belongs to the technical field of pollutant treatment, and provides a thermal evaporation concentration device for treating membrane concentrated solution, which comprises: the evaporation tank is provided with a flue gas pipeline mounting hole and a liquid inlet on the side wall, an air outlet is arranged at the top, and a liquid outlet is arranged at the bottom end of the side wall; the hot flue gas inlet pipeline penetrates through a flue gas pipeline mounting hole on the side wall of the evaporation tank to enter the evaporation tank, and an air hole is formed in the pipe wall of the flue gas inlet pipeline in the evaporation tank; the membrane concentrated solution enters a pipeline, the membrane concentrated solution enters the pipeline and passes through a liquid inlet on the side wall of the evaporation tank to enter the evaporation tank, and holes are formed in the pipe wall of the membrane concentrated solution entering the pipeline, which is positioned in the evaporation tank; and the discharge pipeline is connected with a liquid outlet arranged at the bottom end of the side wall of the evaporation pool. The invention can fully utilize waste heat of exhausted smoke, thereby reducing energy consumption, recovering valuable water resources and reducing the membrane concentrated solution.
Description
Technical Field
The invention belongs to the technical field of pollutant treatment, and particularly relates to a thermal evaporation concentration device for treating membrane concentrated solution.
Background
Leachate refers to a high-concentration organic or inorganic liquid generated by biochemical degradation of garbage due to compaction, fermentation and the like in the stacking and landfill processes and under the seepage action of precipitation and groundwater, and almost all garbage leachate is from garbage landfill sites and incineration plants at present.
The landfill leachate contains various toxic and harmful inorganic matters and organic matters due to complex components, and also contains non-chlorinated aromatic compounds such as naphthalene and phenanthrene, chlorinated aromatic compounds, phosphoric acid vinegar, phenolic compounds, aniline compounds and the like which are difficult to biodegrade. The highest concentration of CODcr and BOD5 in the landfill leachate can reach thousands to tens of thousands, and compared with municipal sewage, the concentration is much higher, so the leachate can not be directly discharged into a municipal sewage treatment pipeline without strict treatment and disposal. In general, CODcr, BOD5, BOD5/CODcr decrease with "age" of the landfill and alkalinity levels increase. Therefore, the landfill leachate can be discharged after being treated.
At present, landfill sites and incineration plant leachate are treated in a plurality of comprehensive ways, and the landfill sites and the incineration plant leachate are generally pretreated in the early stage, then treated in the anaerobic stage and then treated in the aerobic stage, and then subjected to ultrafiltration, nanofiltration and reverse osmosis. The ultrafiltration can filter out macromolecules and suspended matters, and the main components of the ultrafiltration membrane are humic acid, various micromolecules and Ca 2+ 、Mg 2+ 、Na + 、Cl - 、CO 2- 、SO 4 2- Plasma, which needs to enter nanofiltration for further treatment; almost all humic acid and bivalent and above ions are separated out by the nanofiltration membrane, and the separated concentrated solution accounts for about 20 percent of that entering the nanofiltration. The nanofiltration concentrate is not easy to store or bury due to high salinity and organic matter concentration, and needs further treatment. The solution penetrating the nanofiltration membrane contains high Na + 、Cl - Plasma, which does not meet emission standards, still requires further treatment and therefore a reverse osmosis process. The clear liquid after reverse osmosis treatment can be discharged or used for irrigation of public utilities after reaching the discharge standard, the reverse osmosis concentrated solution accounts for about 25 percent of the total amount entering the reverse osmosis system, and the main component is Na + 、Cl - A solution of monovalent ions.
For the reverse osmosis concentrated solution, because the pollution is low, a natural air drying and then landfill mode can be adopted, but the efficiency is low by the natural air drying, and the occupied area is large; the industrial salt can also be processed by the process, but the cost is higher; evaporation can be promoted in a heat treatment concentration mode, but the heat exchange contact surface is easy to crystallize due to improper heat treatment process, so that uneven heat conduction of the heating surface and reduced heat exchange effect are caused.
For the treatment of nanofiltration concentrated solution, some processes adopt reflux to enter a percolate treatment system again, and although the total amount of humic acid can be reduced by adopting the way, Ca can be added along with the increase of the circulation times 2+ 、Mg 2+ 、 CO 2- 、SO 4 2- The concentration of the plasma is increased to influence a percolate treatment system before nanofiltration, so that the reflux cannot finally solve the problem of nanofiltration concentrationLiquid condensation; spraying the waste incineration furnace hearth can cause corrosion and scaling damage to the heating surface; the leachate is finally re-introduced into the landfill. Therefore, various researches have been made to solve the problems of the treatment method and the treatment process of the nanofiltration concentrated solution.
Nanofiltration concentrate and reverse osmosis concentrate are collectively referred to as membrane concentrate.
At present, typical methods for treating membrane concentrated solution at home and abroad comprise recharging, membrane distillation, evaporation, advanced oxidation and the like. But some problems have been found in practical applications.
And (4) recharging. The recycling rate can be improved by recharging, and the washing flow rate of the membrane surface is increased; however, the drawback of recharge gradually appears over time, and domestic refuse landfills have the problems of pollutant accumulation, leachate conductivity increase, membrane water yield decrease, and even membrane filtration failure caused by conductivity increase.
The membrane distillation method, i.e. submerged combustion evaporation technology, is an evaporation mode without fixed heat transfer surface, and is characterized by that the fuel and air are fed into the combustion chamber close to liquid surface or submerged under the liquid surface to make complete combustion, then the high-temp. smoke gas is directly sprayed into the liquid to heat the liquid. The high-temperature flue gas enters the liquid and then rises in the form of a large number of small bubbles, the mixing and stirring of the flue gas and the liquid are very strong, so that the heat transfer process is greatly enhanced, the temperature of the tail gas is reduced to a temperature which is not much different from that of the liquid before the tail gas is discharged, and the heat transfer efficiency can reach more than 95%.
Evaporation is a process of separating out relatively volatile components of a mixed solution at a certain temperature and pressure. The evaporation treatment process can concentrate the volume of the solution to be treated to be less than 2-10% of the volume of the stock solution.
Advanced oxidation processes. At present, compared with the above technologies, the advanced oxidation technology is a better choice for treating landfill leachate and membrane concentrated solution, and has the following main points: the high efficiency, the high speed of degrading organic matter by advanced oxidation technology is very fast, which is incomparable with other technologies. Secondly, the products are harmless, and intermediate products in the oxidation process of the advanced oxidation method can continuously react with hydroxyl radicals until the intermediate products are completely oxidized into carbon dioxide and water, so that the aim of thoroughly removing TOC and COD is fulfilled. And thirdly, as the process is a physical and chemical process, the process is easy to control so as to meet the treatment requirement.
The methods are adopted in the treatment of the membrane concentrated solution, but no device for evaporating the membrane concentrated solution by utilizing waste heat is involved, so that the waste heat of the flue gas cannot be effectively utilized.
Disclosure of Invention
The invention aims to provide a thermal evaporation concentration device for treating membrane concentrated solution, which at least solves the technical problem of resource waste in the prior art and can solve the technical problem that the membrane concentrated solution cannot be recycled in the prior art.
The invention provides a thermal evaporation concentration device for treating membrane concentrated solution, which comprises:
the side wall of the evaporation tank is provided with a flue gas pipeline mounting hole and a liquid inlet, the top of the evaporation tank is provided with a gas outlet, and the bottom end of the side wall is provided with a liquid outlet;
the hot flue gas inlet pipeline penetrates through a flue gas pipeline mounting hole on the side wall of the evaporation tank to enter the evaporation tank, and the pipe wall of the hot flue gas inlet pipeline in the evaporation tank is provided with air holes for discharging hot flue gas into the evaporation tank;
the membrane concentrated solution enters a pipeline, the membrane concentrated solution enters the evaporation tank through a liquid inlet on the side wall of the evaporation tank through the pipeline, and holes are formed in the pipe wall of the membrane concentrated solution entering pipeline, which is positioned in the evaporation tank, and used for discharging the membrane concentrated solution into the evaporation tank;
and the discharge pipeline is connected with a liquid outlet arranged at the bottom end of the side wall of the evaporation pool and is used for discharging the concentrated solution of the membrane concentrated solution.
Preferably, the flue gas duct mounting hole provided on the side wall of the evaporation tank is higher than the liquid inlet, so that the hot flue gas inlet duct is located higher than the membrane concentrate inlet duct.
Preferably, the hot flue gas inlet pipe passes through the flue gas pipe mounting hole on the side wall of the evaporation pool and extends to the opposite side wall of the evaporation pool.
Preferably, the hot flue gas inlet pipeline is provided with air holes at the bottom and/or the lower side surface of the evaporation pool, so that the hot flue gas is sprayed out from the bottom and/or the lower side surface.
Preferably, the hot flue gas inlet pipeline is one or more; one or more inlet pipelines for the membrane concentrated solution; a plurality of liquid outlets are formed in the bottom end of the side wall of the evaporation pool, and each liquid outlet is connected with a discharge pipeline; further preferably, a pump is further disposed on each of the discharge pipes to pump out the concentrated membrane concentrate.
Preferably, the method further comprises the following steps: the anti-disturbance pore plate is arranged on the lower portion of the smoke pipeline mounting hole of the evaporation tank and is a flat plate, and a plurality of holes are formed in the flat plate.
Preferably, the method further comprises the following steps: and the anti-disturbance distribution plate is arranged below the pipe orifice of the membrane concentrated solution inlet pipeline.
Preferably, the anti-disturbance distribution plate is a flat plate, and the distance between the anti-disturbance distribution plate and the pipe orifice of the membrane concentrated solution inlet pipeline is 2 mm.
Preferably, the method further comprises the following steps: and the condenser is connected with the air outlet and is used for receiving a mixture of water vapor formed by evaporating the membrane concentrated solution and cold flue gas formed by heat exchange of hot flue gas, cooling the mixture and condensing gaseous water in the mixture into liquid water.
Preferably, the membrane concentrate includes a nanofiltration concentrate and a reverse osmosis concentrate, and when the membrane concentrate is a nanofiltration concentrate, the apparatus further includes:
the pre-treatment device is used for pre-treating the nanofiltration concentrated solution; the preprocessing device comprises:
a regulating container for containing the nanofiltration concentrate, NaOH is added into the regulating container for reducing Ca in the nanofiltration concentrate 2+ 、Mg 2+ The nanofiltration concentrate forms a supernatant in the conditioning vesselA layer and a lower concentrated liquid layer, the lower concentrated liquid layer entering the evaporator; and
a humic acid membrane extraction system for absorbing the upper supernatant layer.
The thermal evaporation concentration device for treating the membrane concentrated solution can fully utilize waste exhaust gas waste heat, thereby reducing energy consumption, recovering precious water resources and reducing the quantity of the membrane concentrated solution.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
Fig. 1 is a schematic structural view of a thermal evaporation concentration apparatus for treating a membrane concentrate according to a preferred embodiment of the present invention.
Wherein the reference numerals in the figures are explained as follows:
1-an evaporation tank; 11-gas outlet; 2-hot flue gas inlet duct; 3-the membrane concentrate enters a pipeline; 4-anti-disturbance orifice plate; 5-anti-disturbance distribution plate; 6-discharge pipe.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, embodiments of the present invention will be described in detail with reference to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
In the present invention, the membrane concentrate refers to nanofiltration concentrate and reverse osmosis concentrate.
As shown in fig. 1, one embodiment of the present invention provides a thermal evaporative concentration apparatus for processing a membrane concentrate, comprising:
and the evaporation tank 1 is used for carrying out heat exchange between hot flue gas and the membrane concentrated solution. The side wall of the evaporation tank 1 is provided with a flue gas pipeline mounting hole and a liquid inlet, the top of the evaporation tank is provided with a gas outlet 11, and the bottom end of the side wall is provided with a liquid outlet.
And the hot flue gas inlet pipeline 2 is used for providing hot flue gas for the evaporation pool 1. The hot flue gas inlet pipeline 2 passes through a flue gas pipeline mounting hole on the side wall of the evaporation pool 1 and enters the evaporation pool 1. The pipe wall of the hot flue gas inlet pipe 2 in the evaporation tank 1 is provided with air holes for discharging hot flue gas into the evaporation tank 1.
The membrane concentrate enters line 3 for feeding the membrane concentrate into the evaporation tank 1. The membrane concentrate inlet pipe 3 enters the evaporation tank 1 through a liquid inlet on the side wall of the evaporation tank 1. The pipe wall or the end part of the membrane concentrated solution inlet pipe 3 in the evaporation tank 1 is provided with a hole for discharging the membrane concentrated solution into the evaporation tank 1.
And the discharge pipeline 6 is connected with a liquid outlet arranged at the bottom end of the side wall of the evaporation pool 1, and is used for discharging the concentrated solution of the membrane concentrated solution.
In the invention, the used hot flue gas can be hot flue gas discharged by a garbage incinerator. Under the conventional condition, the temperature of hot flue gas discharged by the garbage incinerator is about 240 ℃, which accounts for about 18 percent of the total heat value of garbage, the temperature of hot flue gas after deacidification treatment is about 190 ℃, and the temperature of hot flue gas after bag-type dust removal is about 185 ℃. Because the hot flue gas before deacidification treatment contains NO X 、SO X The components of the membrane concentrate are complex and corrosive, such as HCl, escaping ammonia and ash, and the like, so that the invention preferably uses relatively pure hot flue gas after deacidification and bag dedusting to remove the components for thermal evaporation concentration of the membrane concentrate. Because the adopted hot flue gas is the purer hot flue gas, the problem of secondary pollution of the flue gas is not needed to be considered, and the condensate obtained by discharging the water vapor formed after the evaporation of the membrane concentrated solution and the cold flue gas formed after the heat exchange of the hot flue gas from the gas outlet 11 and then performing condensation treatment only contains a small amount of ions and micromolecule organic matters and can be recycled as reclaimed water. Based on this, the apparatus of the present invention may further comprise a condenser (condensing means), connected to the gas outlet 11, for receiving a mixture of water vapor formed by evaporation of the membrane concentrate and cold flue gas formed by heat exchange of the hot flue gas, and cooling the mixture to condense gaseous water therein into liquid water.
When the thermal evaporation concentration device for treating the membrane concentrated solution provided by the above embodiment of the present invention is used, the membrane concentrated solution is discharged into the evaporation tank 1 from the membrane concentrated solution inlet pipe 3, and is separated into two layers after standing and precipitating in the evaporation tank 1, wherein the upper layer is a membrane concentrated solution clear solution (upper clear solution), and the lower layer is a membrane concentrated solution (lower concentrated solution). Hot flue gas passes through hot flue gas admission line 2 and gets into in evaporation pond 1 to carry out the heat exchange with membrane concentrate clear liquid in evaporation pond 1, thereby give membrane concentrate clear liquid with the heat energy transfer that hot flue gas carried, make membrane concentrate clear liquid evaporation form vapor, vapor upward movement, and the cold flue gas that forms after the heat exchange with hot flue gas is discharged from gas outlet 11 together, and membrane concentrate dense liquid is then discharged from discharge tube 6. Therefore, the device can effectively utilize the waste heat of the hot flue gas to heat the clear liquid of the concentrated membrane concentrated solution, not only utilizes the energy of the waste heat of the hot flue gas of the waste gas, reduces the water consumption, but also reduces the quantity of the concentrated membrane solution.
According to a preferred embodiment of the present invention, the flue gas duct installation hole provided on the side wall of the evaporation tank 1 is higher than the liquid inlet, so that the position of the hot flue gas inlet duct 2 is higher than the position of the membrane concentrate inlet duct 3, which can reduce the disturbance of flue gas to the membrane concentrate, reduce the attachment of crystals or sticky substances on the surface of the hot flue gas inlet duct 2 (the crystallized substances or sticky substances mostly come from the membrane concentrate), and facilitate the discharge of cold flue gas formed after heat exchange of hot flue gas and water vapor evaporated from the membrane concentrate from the gas outlet 11.
According to a preferred embodiment of the present invention, the hot flue gas inlet pipe 2 extends to the opposite side wall of the evaporation tank 1 after passing through the flue gas pipe mounting hole on the side wall of the evaporation tank 1, so as to facilitate sufficient heat exchange between the hot flue gas and the membrane concentrate clear liquid. Further preferably, the bottom and/or the lower side of the hot flue gas inlet pipe 2 extending into the evaporation tank 1 is/are provided with air holes, so that hot flue gas can be sprayed out from the lower side, thereby facilitating heat exchange with the membrane concentrate clear liquid. The number of the hot flue gas inlet pipes 2 can be one or more, and the number of the hot flue gas inlet pipes 2 can be determined according to the evaporation output. The size and the distance of the air holes on the flue gas inlet pipeline 2 can be determined according to the flow velocity, the flow and the evaporation output of hot flue gas. In the invention, the evaporation output refers to the evaporation capacity of hot flue gas in unit time or the evaporation speed of the hot flue gas to the clear liquid of the membrane concentrated solution.
According to a preferred embodiment of the invention, the membrane concentrate inlet line 3 may be one or more. The plurality of membrane concentrated solution inlet pipelines 3 are arranged to directly feed the membrane concentrated solution into different positions in the evaporation tank 1, so that the treatment speed of the membrane concentrated solution is increased, and the working efficiency of the device is improved.
According to a preferred embodiment of the present invention, in order to prevent the bottom end of the evaporation tank 1 from silting up and causing the concentrated membrane concentrate to be discharged out smoothly, a plurality of liquid outlets are provided at the bottom end of the side wall of the evaporation tank 1; each liquid outlet can be connected with a discharge pipeline 6, some discharge pipelines 6 are arranged on the side wall of the evaporation pool 1, and some discharge pipelines 6 extend into the middle of the bottom end of the evaporation pool 1; further, a pump can be arranged on each discharge pipeline 6 to pump and discharge the membrane concentrated solution, so that the bottom sedimentation of the evaporation tank 1 is further reduced.
In order to further reduce the disturbance of the membrane concentrate by the hot flue gas in the evaporation tank 1 (when the disturbance is serious, the membrane concentrate which is already layered is remixed into the membrane concentrate with consistent concentration), as shown in fig. 1, in a preferred embodiment of the invention, a disturbance-preventing orifice plate 4 is further included. The anti-disturbance orifice plate 4 may be a flat plate with a plurality of holes. The anti-disturbance pore plate 4 is arranged at the lower part of the flue gas pipeline mounting hole of the evaporation tank 1, and can be supported on the side wall or the bottom of the evaporation tank 1 through a bracket (such as a steel frame) as shown in fig. 1. The anti-disturbance pore plate 4 is arranged according to the mode, so that the clear liquid of the membrane concentrated solution can reach the upper part of the anti-disturbance pore plate 4 through the holes on the anti-disturbance pore plate 4 to exchange heat with hot flue gas, the disturbance of the flue gas to the membrane concentrated solution is further reduced, and the treatment efficiency is improved.
In order to allow the membrane concentrate to settle and settle out of layers as quickly as possible, in a preferred embodiment of the invention, an anti-disturbance distribution plate 5 is also included, as shown in fig. 1. The disturbance prevention distribution plate 5 may be a flat plate, and the flat plate may be a reinforced concrete structure. The anti-disturbance distribution plate 5 is arranged below, preferably immediately adjacent to, the mouth of the membrane concentrate inlet pipe 3, and the distance between them may be, for example, 2 mm. As shown in fig. 1, the evaporation tank 1 may be supported on the side wall or the bottom of the evaporation tank by a bracket (e.g., a steel frame). The anti-disturbance distribution plate 5 is arranged according to the mode, and the membrane concentrated solution discharged into the evaporation tank 1 from the membrane concentrated solution inlet pipeline 3 has a certain initial speed, and the membrane concentrated solution is firstly distributed on the anti-disturbance distribution plate 5 after entering the evaporation tank 1, so that the kinetic energy of the membrane concentrated solution is reduced, the disturbance of the newly discharged membrane concentrated solution on the previously discharged membrane concentrated solution is reduced, and the time required for the precipitation and delamination of the membrane concentrated solution is reduced.
Preferably, the invention further comprises a pre-treatment device (not shown) for pre-treating the nanofiltration concentrate, the pre-treatment device comprising a conditioning vessel and a humic acid membrane extraction system. Wherein the conditioning vessel is adapted to contain a nanofiltration concentrate. NaOH is added into the adjusting container to reduce Ca in the nanofiltration concentrated solution 2+ 、Mg 2+ The nanofiltration concentrate is divided into an upper supernatant layer and a lower concentrate layer in the conditioning vessel. The humic acid membrane extraction system is used for absorbing the upper supernatant layer. The pretreatment of the nanofiltration concentrate using the pretreatment apparatus described above may be: firstly adding NaOH into nanofiltration concentrated solution, adjusting pH value to 12, and then standing for precipitation to reduce Ca in the nanofiltration concentrated solution 2+ 、Mg 2+ . And adjusting the pH value of the upper clear liquid after precipitation to 7, and then feeding the upper clear liquid into a humic acid membrane extraction system. Reducing Ca in nanofiltration concentrate in a conditioning vessel 2+ 、Mg 2+ The nanofiltration concentrated solution after being treated and treated by the humic acid membrane extraction system enters the treatment device. The reverse osmosis concentrated solution does not need the pre-treatment and can be directly sent into the evaporation tank 1 for treatment.
As shown in FIG. 1, the following description will be made in detail with respect to the operation of the present invention by taking nanofiltration concentrate as an example:
the nanofiltration concentrate is first pre-treated before entering the evaporation tank 1, and the treatment process is as follows:
firstly, NaOH is added into nanofiltration concentrated solution, the pH value is adjusted to 12, and then the solution is statically precipitated to reduce nanofiltration concentrationCa in the concentrate 2+ 、Mg 2+ . And adjusting the pH value of the upper clear liquid after precipitation to 7, and then feeding the upper clear liquid into a humic acid membrane extraction system. Reducing Ca in nanofiltration concentrate in a conditioning vessel 2+ 、Mg 2+ The nanofiltration concentrated solution after being treated by the humic acid membrane extraction system is the membrane concentrated solution, and the process of treating the membrane concentrated solution by using the thermal evaporation concentration treatment device for treating the membrane concentrated solution comprises the following steps:
the membrane concentrated solution enters the pipeline 3 from the membrane concentrated solution and is discharged into the evaporation tank 1, and the anti-disturbance distribution plate 5 (the distance between the two is 2mm) is arranged below the pipe orifice of the membrane concentrated solution entering the pipeline 3, so that the membrane concentrated solution is firstly distributed on the anti-disturbance distribution plate 5, and the kinetic energy of the membrane concentrated solution is reduced. The membrane concentrated solution enters the pipeline 3 and is discharged into the membrane concentrated solution of the evaporation tank 1, standing is carried out, under the action of gravity, the membrane concentrated solution is divided into an upper membrane concentrated solution clear solution layer (an upper clear solution layer) and a lower membrane concentrated solution layer (a lower concentrated solution layer) in the evaporation tank 1, when the upper clear solution is close to the hot flue gas inlet pipeline 2 (for example, when the upper clear solution is close to the disturbance prevention pore plate 4) or after the hot flue gas inlet pipeline 2 is immersed (at the moment, the membrane concentrated solution is stopped to be input), pure hot flue gas after deacidification treatment and cloth bag dedusting treatment is introduced into the hot flue gas inlet pipeline 2, the hot flue gas enters the membrane concentrated solution clear solution from air holes formed in the pipe wall of the hot flue gas inlet pipeline 2 and exchanges heat with the membrane concentrated solution clear solution, so that the membrane concentrated solution clear solution is heated and evaporated to generate steam, the steam moves upwards and is discharged from the air outlet 11 together with cold flue gas formed after the hot flue gas is subjected to heat exchange, the membrane concentrate that has settled on the lower layer after standing is discharged from the discharge line 6 (if necessary, a pump for pumping the lower concentrate is turned on). The mixture of the water vapor and the cold flue gas formed after the hot flue gas is subjected to heat exchange can be cooled by a condenser, the gaseous water in the mixture is condensed to become liquid water, and the liquid water can be collected to be used as reclaimed water. Because the anti-disturbance pore plate 4 arranged at the lower part of the smoke pipeline mounting hole of the evaporation pool 1 exists, not only can the clear liquid of the membrane concentrated solution penetrate through the anti-disturbance pore plate 4 to perform sufficient heat exchange with the hot smoke, but also can greatly reduce the disturbance of the hot smoke to the layered membrane concentrated solution.
The reverse osmosis concentrated solution does not need the pre-treatment and can be directly sent into the evaporation tank 1 for treatment.
The heat evaporation and concentration device for treating the membrane concentrated solution can directly heat, evaporate and concentrate the membrane concentrated solution by using waste hot flue gas (such as hot flue gas exhausted by a garbage incinerator), namely, the hot flue gas transfers heat energy to the membrane concentrated solution through direct heat exchange, the membrane concentrated solution is evaporated and concentrated to form the membrane concentrated solution and water vapor, the water vapor and the concentrated membrane concentrated solution can be separately treated, the water vapor can be recycled, and the membrane concentrated solution can be fully concentrated.
The air holes on the hot flue gas inlet pipeline 2 can ensure that the hot flue gas and the membrane concentrated solution can be subjected to sufficient heat exchange, so that the utilization rate of energy is improved.
The invention can greatly reduce the disturbance of the hot flue gas to the membrane concentrated solution by arranging the disturbance-preventing pore plate 4.
The invention can greatly reduce the disturbance between the membrane concentrated solution and the concentrated membrane concentrated solution by arranging the disturbance-proof distribution plate 5, thereby ensuring the good concentration effect of the membrane concentrated solution.
It will be appreciated by those skilled in the art that the invention may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. The embodiments disclosed above are therefore to be considered in all respects as illustrative and not restrictive. All changes which come within the scope of or equivalence to the invention are intended to be embraced therein.
Claims (10)
1. A thermal evaporative concentration apparatus for processing membrane concentrate, comprising:
the side wall of the evaporation tank is provided with a flue gas pipeline mounting hole and a liquid inlet, the top of the evaporation tank is provided with a gas outlet, and the bottom end of the side wall is provided with a liquid outlet;
the hot flue gas inlet pipeline penetrates through a flue gas pipeline mounting hole on the side wall of the evaporation tank to enter the evaporation tank, and the pipe wall of the hot flue gas inlet pipeline in the evaporation tank is provided with air holes for discharging hot flue gas into the evaporation tank; and
the side wall of the evaporation pool is provided with a flue gas pipeline mounting hole which is higher than the liquid inlet, so that the position of the hot flue gas inlet pipeline is higher than that of the membrane concentrated solution inlet pipeline;
the anti-disturbance pore plate is arranged at the lower part of a flue gas pipeline mounting hole of the evaporation tank, and a plurality of holes are formed in the anti-disturbance pore plate;
the membrane concentrated solution enters a pipeline, the membrane concentrated solution enters the evaporation tank through a liquid inlet on the side wall of the evaporation tank through the pipeline, and holes are formed in the pipe wall of the membrane concentrated solution entering pipeline, which is positioned in the evaporation tank, and used for discharging the membrane concentrated solution into the evaporation tank;
and the discharge pipeline is connected with a liquid outlet arranged at the bottom end of the side wall of the evaporation pool and is used for discharging the concentrated solution of the membrane concentrated solution.
2. A thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 1 wherein the hot flue gas inlet duct extends through the flue gas duct mounting holes in the side walls of the evaporative basin to the opposite side wall of the evaporative basin.
3. A thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 2 wherein the hot flue gas inlet duct has air holes formed in the bottom and/or lower side of the evaporation tank to allow hot flue gas to be ejected from the bottom and/or lower side.
4. The thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 3, wherein the hot flue gas inlet duct is one or more;
one or more inlet pipelines for the membrane concentrated solution;
the liquid outlet that the lateral wall bottom of evaporation pond set up is a plurality of, every a discharge line is all connected to the liquid outlet.
5. A thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 4 wherein a pump is further provided on each of the discharge lines for pumping the concentrated membrane concentrate.
6. A thermal evaporative concentration apparatus for processing membrane concentrates as recited in claim 1 wherein the anti-disturbance orifice plate is a flat plate.
7. A thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 1 or 6, further comprising:
and the anti-disturbance distribution plate is arranged below a pipe orifice of the membrane concentrated solution inlet pipeline.
8. The thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 7, wherein the disturbance prevention distribution plate is a flat plate, and the disturbance prevention distribution plate is 2mm away from the pipe orifice of the membrane concentrate inlet pipe.
9. A thermal evaporative concentration apparatus for processing membrane concentrate as recited in claim 1, further comprising:
and the condenser is connected with the air outlet and is used for receiving a mixture of water vapor formed by evaporating the membrane concentrated solution and cold flue gas formed by heat exchange of hot flue gas, cooling the mixture and condensing gaseous water in the mixture into liquid water.
10. The thermal evaporative concentration apparatus for processing membrane concentrate of claim 1, wherein the membrane concentrate includes nanofiltration concentrate and reverse osmosis concentrate, and when the membrane concentrate is nanofiltration concentrate, the apparatus further comprises:
the pre-treatment device is used for pre-treating the nanofiltration concentrated solution; the preprocessing device comprises:
a regulating container for containing the nanofiltration concentrate, NaOH is added into the regulating container for reducing Ca in the nanofiltration concentrate 2+ 、Mg 2+ The nanofiltration concentrate forms an upper clear liquid layer and a lower concentrated liquid layer in the conditioning vessel, and the lower concentrated liquid layer enters the evaporator; and
a humic acid membrane extraction system for absorbing the upper supernatant layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610556652.2A CN106186127B (en) | 2016-07-14 | 2016-07-14 | Thermal evaporation concentration device for treating membrane concentrated solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610556652.2A CN106186127B (en) | 2016-07-14 | 2016-07-14 | Thermal evaporation concentration device for treating membrane concentrated solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106186127A CN106186127A (en) | 2016-12-07 |
| CN106186127B true CN106186127B (en) | 2022-08-26 |
Family
ID=57475000
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610556652.2A Active CN106186127B (en) | 2016-07-14 | 2016-07-14 | Thermal evaporation concentration device for treating membrane concentrated solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106186127B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1410359A (en) * | 2002-11-28 | 2003-04-16 | 清华大学 | Side stand immersion combustion evaporator for concentrating filtrate |
| CN1583205A (en) * | 2004-05-28 | 2005-02-23 | 清华大学 | Unitary immersed burning evaporator of concentrated percolate |
| CN102503012A (en) * | 2011-11-04 | 2012-06-20 | 北京中科通用能源环保有限责任公司 | Method for treating membrane concentrated liquor of landfill leachate |
| CN203170069U (en) * | 2013-03-27 | 2013-09-04 | 嘉兴职业技术学院 | Sedimentation pool in domestic sewage treatment device |
| CN205294987U (en) * | 2015-12-14 | 2016-06-08 | 新昌县泰兴纺织有限公司 | Novel waste water storage water tank |
| CN205838604U (en) * | 2016-07-14 | 2016-12-28 | 中国城市建设研究院有限公司 | A kind of thermal evaporation enrichment facility for processing membrance concentration liquid |
-
2016
- 2016-07-14 CN CN201610556652.2A patent/CN106186127B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1410359A (en) * | 2002-11-28 | 2003-04-16 | 清华大学 | Side stand immersion combustion evaporator for concentrating filtrate |
| CN1583205A (en) * | 2004-05-28 | 2005-02-23 | 清华大学 | Unitary immersed burning evaporator of concentrated percolate |
| CN102503012A (en) * | 2011-11-04 | 2012-06-20 | 北京中科通用能源环保有限责任公司 | Method for treating membrane concentrated liquor of landfill leachate |
| CN203170069U (en) * | 2013-03-27 | 2013-09-04 | 嘉兴职业技术学院 | Sedimentation pool in domestic sewage treatment device |
| CN205294987U (en) * | 2015-12-14 | 2016-06-08 | 新昌县泰兴纺织有限公司 | Novel waste water storage water tank |
| CN205838604U (en) * | 2016-07-14 | 2016-12-28 | 中国城市建设研究院有限公司 | A kind of thermal evaporation enrichment facility for processing membrance concentration liquid |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106186127A (en) | 2016-12-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102583862A (en) | Method and system for treating saline wastewater to zero discharge and recycling | |
| CN101209881A (en) | Method and system for processing leachate of garbage burning factory | |
| CN104230124B (en) | Coal chemical industry wastewater zero emission technique and specific equipment thereof | |
| CN104926011B (en) | The evaporative crystallization zero-discharge treatment system and processing method of a kind of high-COD waste water | |
| CN103922543A (en) | Garbage leaching liquor treatment method | |
| CN105585197A (en) | Desulfurization wastewater concentration treatment device and method | |
| CN111704301A (en) | Landfill leachate treatment process based on PMVR-ZLD | |
| CN104085933A (en) | High-salinity and high organic matter wastewater treatment process | |
| CN104828887A (en) | Method for evaporative purifying treatment of wastewater by adopting solar combination heating, and system thereof | |
| CN212269507U (en) | High-concentration wastewater zero discharge system for blast furnace slag flushing cleaning production and waste heat method in steel plant | |
| WO2018045708A1 (en) | Indirect air-cooling unit heat recovery and water treatment device and method | |
| CN104628065A (en) | Chemical pharmaceutical wastewater treatment system and method | |
| CN111875151A (en) | System and method for co-processing garbage leachate and incineration fly ash | |
| CN103265090A (en) | Zero-emission device for concentrated saline water evaporated liquid and process method | |
| CN212293240U (en) | Zero-emission treatment system for leachate of waste incineration plant | |
| CN211226804U (en) | Membrane concentrate minimizing processing system | |
| CN112320876A (en) | Salt-containing wastewater evaporation and concentration process and system | |
| CN205635216U (en) | Concentrated processing apparatus of desulfurization waste water | |
| CN106186127B (en) | Thermal evaporation concentration device for treating membrane concentrated solution | |
| CN202465443U (en) | System for processing brine waste to zero emission and recycling | |
| CN115259518A (en) | System and method for treating percolate concentrated solution | |
| CN206051603U (en) | A kind of thermal evaporation concentration systems of membrance concentration liquid | |
| CN204737747U (en) | System for adopt solar energy combination heating to make waste water evaporation purification treatment | |
| CN205838604U (en) | A kind of thermal evaporation enrichment facility for processing membrance concentration liquid | |
| CN204237642U (en) | A kind of special purpose device of Coal Chemical Industry haline water purification process technique |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |