CN116983831A - Forward osmosis membrane separation equipment and method for high-pressure gas-driven negative pressure separation - Google Patents
Forward osmosis membrane separation equipment and method for high-pressure gas-driven negative pressure separation Download PDFInfo
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0022—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0023—Accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0024—Controlling or regulating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/005—Osmotic agents; Draw solutions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/08—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/10—Accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/10—Temperature control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/14—Pressure control
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Nanotechnology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to the technical field of water separation, and provides a positive-osmosis membrane separation device and a method for high-pressure air-driven negative-pressure separation, wherein the positive-osmosis membrane separation device comprises a positive-osmosis membrane system, a concentrated water storage tank, a high-pressure tank, a negative-pressure tank, a water source heat pump unit, an air pump and a water pump; the forward osmosis membrane system comprises a sewage inlet, a concentrated water outlet, a dilute draw solution outlet, a draw solution inlet and a sewage circulating pump; the concentrated water outlet of the forward osmosis membrane system is communicated with the concentrated water storage tank, the dilute draw solution outlet of the forward osmosis membrane system is communicated with the negative pressure tank, and the draw solution inlet of the forward osmosis membrane system is communicated with the high pressure tank; the water source heat pump unit is respectively connected with the high-pressure tank and the negative-pressure tank; the negative pressure tank is provided with a gas outlet and a liquid outlet; the gas outlet of the negative pressure tank is connected with a gas pump and leads to the high pressure tank; and the liquid outlet of the negative pressure tank is connected with a water pump. The implementation of the invention can solve the problems of the regeneration of the drawing liquid and the separation of water molecules under the condition of extremely low energy consumption.
Description
Technical Field
The invention belongs to the technical field of regeneration of a drawing liquid in a forward osmosis membrane separation technology and separation of pure water in the drawing liquid, and particularly relates to equipment and a method for high-pressure regeneration and negative-pressure separation of pure water of the drawing liquid of a forward osmosis membrane.
Background
The pollution control standards (manuscripts) for landfill sites, published by the institute of ecological environment and national marketplace administration 2022, 2, 28, prescribe that the concentrate produced by treating the leachate should be disposed of alone and not be recycled to the landfill site. The treatment of the percolate membrane filtration concentrated solution mainly comprises the technologies of evaporation, advanced oxidation, a back-spraying incinerator and the like, the back-spraying incinerator needs to be provided with the precondition that a landfill site is close to an incinerator factory, the application is less, and most of the percolate membrane filtration concentrated solution is treated by adopting the evaporation or advanced oxidation technology, but the cost of treating the concentrated solution by adopting the technology is higher, and if the concentrated solution is firstly reduced and then treated, the treatment cost can be reduced. Forward Osmosis (FO) is to drive the osmotic pressure difference between low-salt wastewater and high-salt drawing liquid (DS) on two sides of semi-permeable membrane to make H in high-water chemical potential waste liquid 2 Spontaneous diffusion of OIn DS with low water chemical potential, the process does not need external pressure and energy, and then salt and pure water are separated by combining reverse osmosis and other technologies, so that the aim of extracting pure water from sewage is fulfilled. The FO relies on the osmotic pressure difference across the membrane to effect mass transfer without the application of external pressure, so both energy consumption and membrane fouling are lower than in pressure driven membrane processes, membrane fouling is reversible and the compactness of the fouling layer is lower than in pressure driven processes.
A water treatment device and a water treatment method for coupling bioelectrochemistry and a forward osmosis membrane bioreactor (patent number is CN 109704452B) apply an electric potential to a membrane to enrich salt ions on the surface of the forward osmosis membrane, and increase the salt concentration on the surface of the membrane, so that the osmotic pressure difference on two sides of the membrane is increased, but the solution cannot accurately control electrochemical control, which may cause generation of strong oxidizing chemicals such as hydroxyl free radicals or hypochlorous acid, damage the forward osmosis membrane and endanger the survival of microorganisms, and in addition, the existence of the electric potential can more easily enrich and subside calcium and magnesium plasma on the surface of the membrane, so that the membrane is blocked. A garbage percolate concentrate reduction system (patent No. CN 214270480U) uses a high-concentration sodium chloride solution as a drawing liquid, sodium chloride and feed liquid to be treated respectively pass through two sides of a forward osmosis membrane, water molecules of the feed liquid are drawn into the high-concentration sodium chloride solution by using chemical potential difference of the two solutions, then the sodium chloride solution coming out of a forward osmosis membrane unit is treated by a nanofiltration system, and as the interception rate of nanofiltration on salinity is not high, the osmotic pressure difference of the concentrated water measurement side and the water production side of the nanofiltration is smaller, the dilute drawing liquid can be treated under the condition of lower water supply pressure, the produced water of the nanofiltration system enters a high-salt reverse osmosis system, the salt concentration of the produced water of the nanofiltration is already reduced, and therefore, the sodium chloride regenerated drawing liquid can be recovered under lower energy consumption by the high-salt reverse osmosis and the quality of produced water is further improved. According to the method, feed liquid is concentrated step by utilizing a multistage forward osmosis unit, water molecules in the feed liquid enter a high-concentration sodium chloride drawing liquid and then are concentrated by nanofiltration and reverse osmosis, and the water molecules are separated, and although the method can reduce part of energy consumption, the nanofiltration and the reverse osmosis still need to overcome the osmotic pressure of the high-concentration sodium chloride solution to separate the water molecules, so that the energy consumption is still higher, the process chain is longer, and the process is complex. In the forward osmosis separation process, a photo-thermal film is introduced at the interface between the drawing liquid and the air, and irradiated by a light source, so that light energy is converted into heat energy on the surface of the photo-thermal film, and the heat energy is concentrated by photo-thermal evaporation of the drawing liquid, thereby maintaining stable osmotic pressure difference between the forward osmosis raw material liquid and the drawing liquid in the forward osmosis process, and continuously realizing high-efficiency separation of the raw materials. The method is to evaporate and concentrate the water in the dilute drawing liquid by converting light into heat, but the method is slow in water evaporation and is difficult to apply in practical engineering. The invention discloses an anaerobic self-driven membrane reactor (patent number CN 113651420A) suitable for high COD wastewater treatment and regeneration, which is characterized in that a forward osmosis membrane is arranged in an anaerobic tank, water quality is improved after anaerobic treatment, methane is generated, water molecules in an anaerobic system enter a drawing liquid through the forward osmosis membrane, methane generated by anaerobism is utilized as an energy source to introduce the drawing liquid into a membrane distillation unit, and methane heating distillation is adopted to separate the water molecules from the system. A near zero discharge device and process for waste water using anaerobic MBR and forward osmosis as core (patent number is CN 114853284A) adopts anaerobic unit to degrade most COD, then uses forward osmosis to extract water molecules in the anaerobic unit, uses by-product methane of the anaerobic unit to evaporate the concentrated water discharged from the forward osmosis unit, does not mention how to achieve standard treatment after the forward osmosis extracts water molecules in the anaerobic unit, and in fact, only produces water after forward osmosis treatment (namely dilute extract) still contains a large amount of salt, and the produced water is difficult to reach standard. A forward osmosis zero-emission system using ammonium bicarbonate as a drawing liquid and an operation process thereof (patent number is CN 114605012A) use an ammonia distillation process to prepare ammonia water, further react with carbon dioxide to prepare ammonium bicarbonate, use ammonium bicarbonate as the drawing liquid to draw water molecules in wastewater, and then concentrate the diluted drawing liquid and separate the water molecules by adopting a reverse osmosis or electrodialysis mode. A membrane treatment system (patent number is CN 217051834U) applied to landfill leachate treatment adopts a forward osmosis membrane to concentrate sewage in high power, the concentrated wastewater enters an evaporation treatment system, and dilute drawing liquid of the forward osmosis system separates water molecules in a membrane distillation mode and realizes the regeneration of the drawing liquid. A FO device (patent No. CN 216303525U) for treating the percolate of a transfer station and a forward osmosis-reverse osmosis combined milk concentration device and a treatment method thereof (patent No. CN 113457452A) are characterized in that water molecules in wastewater are firstly drawn into the drawing liquid by utilizing the drawing liquid through forward osmosis in a forward osmosis-reverse osmosis coupling mode, and then the water molecules in the dilute drawing liquid are separated through reverse osmosis, so that the purposes of recycling the drawing liquid and discharging standard water are achieved.
Summary of the prior art finds that the process taking the forward osmosis membrane filtration technology as the core is basically consistent in the forward osmosis filtration unit, namely, the concentrated drawing liquid is taken as an intermediate, and water molecules in the feed liquid to be treated are extracted into the concentrated drawing liquid, so that the concentrated drawing liquid is changed into the dilute drawing liquid. The difference of each patent technology is that different methods are adopted for regenerating the extracting solution, and the methods can be roughly classified into a heating evaporation method for concentrating the extracting solution, a membrane distillation method for concentrating the extracting solution and a reverse osmosis method for concentrating the extracting solution. The evaporation method is used for concentrating the drawing liquid, and the solar energy is used for converting heat energy for concentration, so that the method is difficult to apply in engineering due to low photo-thermal conversion efficiency and weather influence; methane gas generated by a landfill site or anaerobism is used as a heat source to evaporate the dilute drawing liquid for regeneration, the amount of the methane gas cannot ensure that the drawing liquid can be evaporated to the required concentration, and the energy consumption for concentrating the drawing liquid by adopting an MVR evaporation method is relatively high; the method adopts a high-pressure reverse osmosis method to concentrate the dilute draw solution, and overcomes the defect that the osmotic pressure of the dilute draw solution is high, so that the method needs to concentrate stepwise by adopting sectional multistage reverse osmosis, and the required pressure is high and the energy consumption is high; the electrodialysis method is adopted to concentrate the draw solution, and the desalination efficiency of the method is low, so that the salt loss is serious, and industrial salt or other draw solution solutes need to be frequently replenished.
Disclosure of Invention
The invention aims to provide a forward osmosis membrane separation device and a forward osmosis membrane separation method for high-pressure gas-driven negative pressure separation, so as to solve the problems of drawing liquid regeneration and water molecule separation under the condition of extremely low energy consumption. The invention provides a forward osmosis membrane separation device for high-pressure air-driven negative pressure separation, which comprises a forward osmosis membrane system, a concentrated water storage tank, a high-pressure tank, a negative pressure tank, a water source heat pump unit, an air pump and a water pump; the forward osmosis membrane system comprises a sewage inlet, a concentrated water outlet, a dilute draw solution outlet, a draw solution inlet and a sewage circulating pump; the concentrated water outlet of the forward osmosis membrane system is communicated with the concentrated water storage tank, the dilute draw solution outlet of the forward osmosis membrane system is communicated with the negative pressure tank, and the draw solution inlet of the forward osmosis membrane system is communicated with the high pressure tank; the water source heat pump unit is respectively connected with the high-pressure tank and the negative-pressure tank; the negative pressure tank is provided with a gas outlet and a liquid outlet; the gas outlet of the negative pressure tank is connected with a gas pump and leads to the high pressure tank; and the liquid outlet of the negative pressure tank is connected with a water pump.
Furthermore, the high-pressure gas-driven negative pressure separation positive-osmosis membrane separation equipment also comprises a reverse osmosis system and a standard water tank, wherein a liquid outlet of the negative pressure tank is connected with a water pump and then is respectively connected with the reverse osmosis system and the standard water tank; the reverse osmosis system comprises a water production outlet and a trapped fluid outlet, the water production outlet of the reverse osmosis system is led to a standard water tank, the outlet of the standard water tank is connected with a water pump, and the trapped fluid outlet of the reverse osmosis system is led to a negative pressure tank or a high pressure tank through valve control.
Furthermore, the high-pressure air-driven negative pressure separation positive-osmosis membrane separation equipment also comprises a cooling water tank, wherein the cooling water tank is respectively connected with the negative pressure tank and the reverse osmosis system, a water pump is arranged between the cooling water tank and the reverse osmosis system, and the water source heat pump unit is respectively connected with the high-pressure tank, the negative pressure tank and the reverse osmosis system.
Specifically, the inside packing layer and the atomizer of setting up of negative pressure jar, the negative pressure jar outside sets up the circulating pump. The packing layer is used for increasing the surface area inside the tower, the circulating pump is used for continuously pumping the dilute drawing liquid at the bottom of the negative pressure tank to the top of the tower and spraying the dilute drawing liquid through the sprayer, the gas-liquid contact area of the dilute drawing liquid is increased under the negative pressure condition, and the gas volatilization speed is accelerated.
Specifically, the air pump connected with the air outlet of the negative pressure tank is a vacuum air pump and a high-pressure air pump in sequence.
The invention provides a forward osmosis membrane separation method for high-pressure air-driven negative pressure separation, which is characterized by comprising the following steps of:
(1) Dissolving soluble pressure-sensitive gas in water to obtain a drawing liquid, dissolving the soluble gas in water to form a salt solution, and filling the salt solution into a high-pressure tank, wherein the high-pressure driving drawing liquid enters a forward osmosis membrane system to draw water molecules in the feed liquid to be treated;
(2) When the feed liquid to be treated passes through the forward osmosis membrane system, water molecules diffuse into the drawing liquid with lower water chemical potential;
(3) The method comprises the steps that after water molecules enter into the extracting solution, the extracting solution is diluted into diluted extracting solution, the diluted extracting solution enters into a negative pressure tank, heat energy of the extracting solution in a high pressure tank is transferred into the extracting solution in the negative pressure tank through a water source heat pump, the temperature of the extracting solution in the negative pressure tank is increased, the temperature of the extracting solution in the high pressure tank is reduced, meanwhile, an air pump pumps air from the negative pressure tank to the high pressure tank, the pressure in the negative pressure tank is reduced, the temperature is increased, a large amount of dissolved gas in the diluted extracting solution is separated out, and the dissolved gas is pressed into the high pressure tank by the air pump to be dissolved again; thereby realizing the separation of solute and product water in the negative pressure tank and the regeneration of the drawing liquid in the high pressure tank at the same time;
(4) Discharging water in the negative pressure tank.
Aiming at the situation that the water quality to be treated is more seriously polluted, the forward osmosis membrane separation method for the negative pressure separation of the high-pressure gas drive is provided, and is characterized by comprising the following steps:
(1) Dissolving gas which is easy to dissolve in water to form drawing liquid, filling the drawing liquid into a high-pressure tank, and driving the drawing liquid to enter a forward osmosis membrane system to draw water molecules in feed liquid to be treated by high pressure;
(2) When the feed liquid to be treated passes through the forward osmosis membrane system, water molecules diffuse into the drawing liquid with lower water chemical potential;
(3) The method comprises the steps that after water molecules enter into the extracting solution, the extracting solution is diluted into diluted extracting solution, the diluted extracting solution enters into a negative pressure tank, heat energy of the extracting solution in a high pressure tank is transferred into the extracting solution in the negative pressure tank through a water source heat pump, the temperature of the extracting solution in the negative pressure tank is increased, the temperature of the extracting solution in the high pressure tank is reduced, meanwhile, an air pump pumps air from the negative pressure tank to the high pressure tank, the pressure in the negative pressure tank is reduced, the temperature is increased, a large amount of dissolved gas in the diluted extracting solution is separated out, and the dissolved gas is pressed into the high pressure tank by the air pump to be dissolved again; thereby realizing the separation of solute and product water in the negative pressure tank and the regeneration of the drawing liquid in the high pressure tank at the same time;
(4) Detecting water in the negative pressure tank, and directly discharging if the water reaches the standard; if the water does not reach the standard, the water discharged from the negative pressure tank is connected into the cooling water tank for cooling, the cooling mode is carried out by adopting a water source heat pump set, the heat of the water in the cooling water tank is conveyed into the negative pressure tank, the water produced after the water is treated by the reverse osmosis system is discharged after reaching the standard, and part of the concentrated water in the reverse osmosis system flows back to the negative pressure tank and the other part flows back to the high pressure tank.
The purpose of the concentrated water in the reverse osmosis system flowing back to the high-pressure tank is to supplement the water flowing out of the drawing liquid, and the purpose of the concentrated water flowing back to the negative-pressure tank is to reprocess in the negative-pressure tank, so that the gas is separated out again.
Preferably, in the above method, the dilute drawing liquid at the bottom of the negative pressure tank is continuously pumped to the top of the negative pressure tank by a circulating pump and sprayed by a sprayer.
The forward osmosis membrane system comprises a feed water pump, a circulating pump, a forward osmosis membrane, a drawing liquid, a pressure gauge, an electric conductivity on-line instrument and the like for feed liquid to be treated, and mainly realizes the function of extracting water molecules in the feed liquid to be treated into the drawing liquid; the high-pressure tank is mainly used for regenerating or concentrating the extracting solution and providing water supply driving force for the extracting solution side of the forward osmosis membrane component, the extracting solution is mainly prepared by dissolving soluble pressure-sensitive gas in water, the gas which is easy to dissolve in water is used for dissolving in water to form salt solution, then the pressure in the high-pressure tank is increased, so that the solubility of the gas is increased, the concentration of the salt solution is increased, the pressure in the tank is increased, the driving force can be provided for the salt solution (the salt solution at the moment is also called as concentrated extracting solution) at the same time, the extracting solution is driven to enter the forward osmosis membrane to extract water molecules in the feed solution to be treated, the extracting solution after the water molecules enter the extracting solution is diluted, the diluted extracting solution enters the negative pressure tank, the solubility of the gas is reduced along with the reduction of the pressure, the solubility of the gas is reduced along with the reduction of the temperature, and the negative pressure tank is internally provided, the heat energy of the drawing liquid in the high-pressure tank is transferred to the drawing liquid in the negative-pressure tank through the water source heat pump, so that the temperature of the drawing liquid in the negative-pressure tank is increased, the temperature of the drawing liquid in the high-pressure tank is reduced, meanwhile, the air pump pumps air from the negative-pressure tank to the high-pressure tank, thus the pressure in the negative-pressure tank is reduced, the temperature is increased, the soluble gas in the dilute drawing liquid is greatly separated out, the air pump is pressed into the high-pressure tank, if the water in the negative-pressure tank reaches the standard, the water can be discharged, if the water does not reach the standard, the outlet water after the negative-pressure tank can be connected into the middle water tank for cooling (if the water temperature does not exceed 40 ℃ according to the actual water temperature, the cooling is not needed), the water source heat pump is adopted for cooling, the heat of the water in the middle water tank is transferred into the negative-pressure tank, the water produced after the middle water is properly treated by reverse osmosis under the condition of the rear end of the middle water tank reaches the standard, and is discharged, part of the concentrated water flows back to the negative pressure tank, and the other part flows back to the high pressure tank, so that the water flowing out of the drawing liquid is supplemented, and the purpose of the return to the negative pressure tank is to reprocess in the negative pressure tank, so that the gas is separated out again. It should be noted that when the dilute draw solution of the forward osmosis membrane enters the negative pressure tank, the external environment of the draw solution is suddenly changed from positive pressure to negative pressure, flash evaporation occurs, that is, the draw solution suddenly becomes a part of saturated steam and saturated solution under the pressure of the container due to sudden pressure reduction, which is more beneficial to release of the dissolved gas. Thus, the re-concentration of the feed liquid to be treated is realized through the process.
In the process, the high-pressure tank and the negative-pressure tank are used in a combined way, the problems of regeneration of the drawing liquid and separation of water molecules are solved under the condition of extremely low energy consumption, the water source heat pump simultaneously gives consideration to the problem of temperature control required by each process unit, and the working principle of the water source heat pump is that the heat is not directly generated by utilizing electric energy, but the heat of the water in the high-pressure tank (or the middle water tank) needing to be cooled is conveyed into the negative-pressure tank needing to be heated by heat conveying, so that the purpose of 'one machine for two purposes' is achieved, and the electric energy is saved. Because the water in the middle water tank is water after the dissolved gas is extracted, the water can reach the standard in practice, for the sake of safety, if the water does not reach the standard, the dissolved gas in the water is extremely low, so that the tail end can be connected into a low-pressure reverse osmosis system for advanced treatment, and for the drainage water quality maintenance and navigation, the scheme of the invention has relatively low energy consumption as a whole because of low-pressure reverse osmosis and can not be used.
The terms involved in the creation of the present invention are explained as follows:
high pressure gas drive: the device is characterized in that in a closed pressure tank, gas is continuously filled into the top of the tank body so as to increase the pressure in the closed tank body, liquid is arranged at the middle lower part of the pressure tank, a liquid outlet is arranged at the bottom of the closed pressure tank, and after a liquid outlet valve is opened, the liquid can be pressed out of the closed tank by virtue of the atmospheric pressure due to the fact that the inside of the tank body has larger atmospheric pressure. High pressure gas driving means that liquid is driven to flow by high pressure gas.
Negative pressure separation: the method is characterized in that after the gas is dissolved into the liquid, the gas is heated and pumped in a closed container, so that the temperature in the closed container is increased and the pressure is reduced, the solubility of the gas in the solution is rapidly reduced, and the gas is separated from the solution, wherein the process comprises a flash evaporation process of the solution suddenly entering a high-temperature negative pressure tank.
Forward osmosis: forward osmosis refers to the process of water flowing from a higher water chemical potential (or lower osmotic pressure) side region through a selectively permeable membrane to a lower water chemical potential (or higher osmotic pressure) -side region. Two solutions with different osmotic pressures are respectively placed on two sides of the selective permeable membrane, one is a raw material solution with lower osmotic pressure, the other is a driving solution with higher osmotic pressure, and forward osmosis is to apply the osmotic pressure difference of the solutions on two sides of the membrane as driving force, so that water can spontaneously permeate the selective permeable membrane from one side of the raw material solution to the driving solution side. When an applied pressure less than the osmotic pressure difference is applied to the solution on the high side of the osmotic pressure, water will still flow from the feed hydraulic to the side to the drive liquid-side, a process called pressure damped osmosis. The driving force for pressure damped permeation is still the osmotic pressure and therefore it is also a forward osmosis process.
Drawing liquid: a salt solution is disposed in the forward osmosis membrane, and the salt concentration of the solution is generally many times higher than the salt content of wastewater on the wastewater side, so that the water chemical potential difference on the two sides of the forward osmosis membrane is high, water molecules in the wastewater spontaneously cross the forward osmosis membrane to enter the draw solution, in the process, the draw solution after the water in the wastewater enters the draw solution is called as a dilute draw solution, and the process of concentrating the dilute draw solution through other units is called as draw solution regeneration.
Reverse osmosis: reverse osmosis, also known as reverse osmosis, is a membrane separation operation that separates solvent from solution using pressure differential as the driving force. The feed liquid on one side of the membrane is pressurized and when the pressure exceeds its osmotic pressure, the solvent will reverse permeate against the natural direction of permeation. Thereby obtaining a permeate solvent, i.e., permeate, on the low pressure side of the membrane; the high pressure side gives a concentrated solution, i.e. a concentrate.
The invention is characterized in that:
1. the temperature-sensitive and pressure-sensitive solutes are dissolved into water to prepare the drawing liquid, when the temperature is increased and the pressure is reduced, the solutes in the drawing liquid are decomposed and desorbed, so that the water in the dilute drawing liquid and the solutes are separated, the separated solutes are pumped into a high-pressure tank again to cool and boost the pressure, and the solutes are dissolved into the water by combining reaction again to realize the regeneration of the drawing liquid in the high-pressure tank.
2. The high-pressure tank and the negative-pressure tank are combined to replace a traditional water supply pump at the side of the drawing liquid, so that the process of leading the drawing liquid into the forward osmosis membrane and leading the drawing liquid out of the forward osmosis membrane can be completed under the condition of extremely low energy consumption, two conditions of temperature-sensitive and pressure-sensitive solute separation and regeneration are provided, and the work of drawing liquid regeneration and pure water separation is synchronously completed.
3. The water source heat pump simultaneously gives consideration to the problem of temperature control required by each process unit, and because the working principle of the water source heat pump does not directly utilize electric energy to generate heat, the heat of reclaimed water in a high-pressure tank (or an intermediate water tank) needing cooling is conveyed into a negative-pressure tank needing heating through heat conveying, the purpose of 'one machine for two purposes' is achieved, and electric energy is saved. Because the water in the middle water tank is water after the dissolved gas is extracted, the water can reach the standard in practice, for the sake of safety, if the water does not reach the standard, the solute concentration in the water is extremely low, so that the tail end can be connected into a low-pressure reverse osmosis system for advanced treatment, and for the drainage water quality protection navigation, the scheme of the invention has relatively low energy consumption as a whole because of low-pressure reverse osmosis.
The beneficial effects of the invention are as follows:
1. because the water source heat pump is introduced in solute separation and concentration, heat energy in the drawing liquid regeneration tank is directly transferred to the drawing liquid solute separation tank, electric energy is not directly adopted to convert the heat energy in the process, and only electric energy is utilized to transfer the heat energy, so that compared with other technologies, the scheme is more energy-saving in adopting a heating evaporation mode to recover the solute.
2. Vacuum pump, air compressor or similar air pump are adopted to pump vacuum from the dilute drawing liquid storage tank, and the pumped air is pumped into the drawing liquid regeneration tank, so that the following three purposes are synchronously achieved: the first and the second liquid extraction regeneration tanks are filled with a large amount of ammonia gas, carbon dioxide, water vapor and other gases, so that the pressure in the tank body is increased, the generation and the solubility increase of ammonia carbonate, ammonium bicarbonate and the like are facilitated, and the liquid extraction regeneration is realized; secondly, the dilute draw solution storage tank is continuously vacuumized by a vacuum pump to form negative pressure, the draw solution which is diluted in the forward osmosis membrane is pumped into the tank body, the environment where the draw solution is located is suddenly changed into negative pressure and hotter environment at the moment when the dilute draw solution enters the tank body, so that the dilute draw solution is partially flashed, the purpose of separating ammonia and carbon dioxide from the dilute draw solution is achieved, and the solubility of various gases is extremely low because the tank body environment is a negative pressure high temperature environment, and ammonia and carbon dioxide are automatically separated from the dilute draw solution, thereby realizing the separation of solute and purified water; thirdly, under the combined action of the negative pressure environment of the dilute drawing liquid storage tank and the positive pressure environment of the drawing liquid storage tank, drawing liquid is pressed into the membrane by positive pressure at the inlet of the forward osmosis membrane, and drawing liquid is drawn out by negative pressure suction at the outlet, so that the side pressure of the drawing liquid of the forward osmosis membrane is extremely small, and the reverse osmosis degree is reduced to the greatest extent.
3. The water inlet pump of the drawing liquid in the forward osmosis is removed, a large amount of ammonia gas and carbon dioxide gas are introduced into the drawing liquid storage tank to be dissolved into water to prepare (regenerate) the concentrated drawing liquid, meanwhile, the pressure of the sealed storage tank is high due to the large air inlet amount, and the drawing liquid is driven to enter the forward osmosis membrane by utilizing air pressure, so that the energy is saved again.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings that are required in the embodiments or the description of the prior art will be briefly described, it being obvious that the drawings in the following description are only some embodiments of the invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of the structure and process of a forward osmosis membrane separation device for high pressure gas-driven negative pressure separation in an embodiment of the invention;
FIG. 2 is a schematic diagram of the structure and process of a forward osmosis membrane separation device (including a reverse osmosis system) for high pressure gas driven negative pressure separation in an embodiment of the invention;
FIG. 3 is a schematic diagram of the structure and process of a positive osmosis membrane separation device for high pressure gas-driven negative pressure separation (negative pressure tank containing sprayer) in an embodiment of the invention;
FIG. 4 is a schematic diagram of the structure and process of a positive osmosis membrane separation device (including a reverse osmosis system, a negative pressure tank including a sprayer) for high pressure gas-driven negative pressure separation in an embodiment of the invention;
FIG. 5 is a graph showing the relationship between the temperature of the drawing liquid in the high-pressure tank and the temperature of the dilute drawing liquid in the negative-pressure reaction tower.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
1. Specific examples of forward osmosis membrane separation devices for high pressure gas driven negative pressure separation
In one embodiment of the invention, as shown in FIG. 1, the forward osmosis membrane separation device for high-pressure air-driven negative pressure separation comprises a forward osmosis membrane system 1, a concentrated water storage tank 7, a high-pressure tank 2, a negative pressure tank 3, a water source heat pump unit 4, an air pump 5 and a water pump (61, 62, 63); the forward osmosis membrane system includes a sewage inlet, a concentrate outlet, a dilute draw solution outlet, a draw solution inlet, and a sewage circulation pump 62; the sewage inlet is connected with a water pump 63; the concentrated water outlet of the forward osmosis membrane system 1 is communicated with a concentrated water storage tank 7, the dilute draw solution outlet of the forward osmosis membrane system 1 is communicated with a negative pressure tank 3, and the draw solution inlet of the forward osmosis membrane system 1 is communicated with a high pressure tank 2; the water source heat pump unit 4 is respectively connected with the high-pressure tank 2 and the negative-pressure tank 3; the negative pressure tank 3 is provided with a gas outlet and a liquid outlet; the gas outlet of the negative pressure tank 3 is connected with a gas pump 5 and is led to the high pressure tank 2; the liquid outlet of the negative pressure tank 3 is connected with a water pump 61. The gas outlet of the negative pressure tank 3 is sequentially connected with a vacuum gas pump 51 and a high-pressure gas pump 52.
In another embodiment of the invention, as shown in fig. 2 and 4, the high-pressure air-driven negative pressure separation forward osmosis membrane separation device further comprises a reverse osmosis system 8 and a standard water tank 9, wherein a liquid outlet of the negative pressure tank 3 is connected with a water pump (64, 65) and then is respectively connected with the reverse osmosis system 8 and the standard water tank 9; the reverse osmosis system 8 comprises a water production outlet and a trapped fluid outlet, the water production outlet of the reverse osmosis system 8 is led to a standard water tank 9, the outlet of the standard water tank 9 is connected with a water pump 61, and the trapped fluid outlet of the reverse osmosis system 8 is led to the negative pressure tank 3 or the high pressure tank 2 through valve control.
In another embodiment of the present invention, as shown in fig. 2 and 4, the forward osmosis membrane separation device for high-pressure air-driven negative pressure separation further comprises a cooling water tank 10, the cooling water tank 10 is respectively connected with the negative pressure tank 3 and the reverse osmosis system 8, a water pump 65 is arranged between the cooling water tank 10 and the reverse osmosis system 8, and the water source heat pump unit 4 is respectively connected with the high-pressure tank 2, the negative pressure tank 3 and the reverse osmosis system 10.
In another embodiment of the present invention, as shown in fig. 3 and 4, a packing layer 31 and a sprayer 32 are disposed inside the negative pressure tank 3, and a circulation pump 33 is disposed outside the negative pressure tank 3. The packing layer 31 is used for increasing the surface area inside the negative pressure tank, the circulating pump 33 is used for continuously pumping the dilute drawing liquid at the bottom of the negative pressure tank to the top and spraying the dilute drawing liquid through the sprayer 32, the gas-liquid contact area of the dilute drawing liquid is increased under the negative pressure condition, and the gas volatilization speed is accelerated.
In particular, the forward osmosis membrane system can be designed into a multi-stage forward osmosis membrane assembly according to the actual sewage quality and needs.
2. Specific examples of the forward osmosis membrane separation method of the high pressure gas-driven negative pressure separation
The forward osmosis membrane separation method for high-pressure air-drive negative pressure separation provided in the specific embodiment of the invention comprises the following steps:
(1) Dissolving soluble pressure-sensitive gas in water to obtain a drawing liquid, dissolving the soluble gas in water to form a salt solution, and filling the salt solution into a high-pressure tank, wherein the high-pressure driving drawing liquid enters a forward osmosis membrane system to draw water molecules in the feed liquid to be treated;
(2) When the feed liquid to be treated passes through the forward osmosis membrane system, water molecules diffuse into the drawing liquid with lower water chemical potential;
(3) The method comprises the steps that after water molecules enter into the extracting solution, the extracting solution is diluted into diluted extracting solution, the diluted extracting solution enters into a negative pressure tank, heat energy of the extracting solution in a high pressure tank is transferred into the extracting solution in the negative pressure tank through a water source heat pump, the temperature of the extracting solution in the negative pressure tank is increased, the temperature of the extracting solution in the high pressure tank is reduced, meanwhile, an air pump pumps air from the negative pressure tank to the high pressure tank, the pressure in the negative pressure tank is reduced, the temperature is increased, a large amount of dissolved gas in the diluted extracting solution is separated out, and the dissolved gas is pressed into the high pressure tank by the air pump to be dissolved again; thereby realizing the separation of solute and product water in the negative pressure tank and the regeneration of the drawing liquid in the high pressure tank at the same time;
(4) Discharging water in the negative pressure tank.
Aiming at the situation that the water quality to be treated is more seriously polluted, the forward osmosis membrane separation method for the high-pressure air-drive negative pressure separation provided in the specific embodiment comprises the following steps:
(1) Dissolving gas which is easy to dissolve in water to form drawing liquid, filling the drawing liquid into a high-pressure tank, and driving the drawing liquid to enter a forward osmosis membrane system to draw water molecules in feed liquid to be treated by high pressure;
(2) When the feed liquid to be treated passes through the forward osmosis membrane system, water molecules diffuse into the drawing liquid with lower water chemical potential;
(3) The method comprises the steps that after water molecules enter into the extracting solution, the extracting solution is diluted into diluted extracting solution, the diluted extracting solution enters into a negative pressure tank, heat energy of the extracting solution in a high pressure tank is transferred into the extracting solution in the negative pressure tank through a water source heat pump, the temperature of the extracting solution in the negative pressure tank is increased, the temperature of the extracting solution in the high pressure tank is reduced, meanwhile, an air pump pumps air from the negative pressure tank to the high pressure tank, the pressure in the negative pressure tank is reduced, the temperature is increased, a large amount of dissolved gas in the diluted extracting solution is separated out, and the dissolved gas is pressed into the high pressure tank by the air pump to be dissolved again; thereby realizing the separation of solute and product water in the negative pressure tank and the regeneration of the drawing liquid in the high pressure tank at the same time;
(4) Detecting water in the negative pressure tank, and directly discharging if the water reaches the standard; if the water does not reach the standard, the water discharged from the negative pressure tank is connected into the cooling water tank for cooling, the cooling mode is carried out by adopting a water source heat pump set, the heat of the water in the cooling water tank is conveyed into the negative pressure tank, the water produced after the water is treated by the reverse osmosis system is discharged after reaching the standard, and part of the concentrated water in the reverse osmosis system flows back to the negative pressure tank and the other part flows back to the high pressure tank.
In an optimized embodiment, in the method, the dilute drawing liquid at the bottom of the negative pressure tank is continuously pumped to the top of the negative pressure tank through a circulating pump and sprayed by a sprayer.
In the specific implementation, sewage enters a forward osmosis membrane system through a sewage feed pump, the sewage circulates at a high speed on one side of a forward osmosis membrane unit through a sewage circulating pump, the flow velocity of the sewage on the surface of the membrane is kept to be about 4m/s, the sewage has a higher cross flow velocity on the surface of the membrane, concentration polarization is reduced, and pollutants are prevented from being deposited on the surface of the forward osmosis membrane; the concentrated drawing liquid is pressed into the positive osmosis membrane system by the top air pressure in the high-pressure tank, the air pressure of the high-pressure tank is 0.5-1 bar, the concentrated drawing liquid is pushed to enter the positive osmosis membrane system, the negative pressure tank (or the negative pressure reaction tower, -0.5-1 bar) is connected to the outlet of the positive osmosis membrane drawing liquid, the diluted drawing liquid is pumped into the negative pressure reaction tower through the negative pressure pumping action, the drawing liquid enters the negative pressure reaction tower and can be sprayed into the negative pressure tank through the spray header, the separation of solutes in the drawing liquid is facilitated, further, the middle part of the negative pressure reaction tower can be provided with a filler, the bottom of the negative pressure reaction tower is provided with a circulating pump to pump the feed liquid at the bottom of the negative pressure reaction tower to spray downwards, the specific surface area of the liquid is increased, and the desorption speed of the drawing liquid is accelerated. Meanwhile, the water source heat pump is connected between the high-pressure tank and the negative pressure tank (or the negative pressure reaction tower), and the heat of the water in the high-pressure tank is conveyed to the negative pressure tank (or the negative pressure reaction tower) through the water source heat pump, so that the temperature reduction (temperature reduction to 10-30 ℃) of the high-pressure tank and the temperature increase (temperature increase to 40-70 ℃ and proper conditions can be increased to 100 ℃) of the negative pressure tank synchronously occur. The method is favorable for decomposing and separating solutes in the negative pressure tank and regenerating and dissolving the solutes in the high pressure tank, at the moment, if the liquid in the negative pressure tank reaches the set standard, the solutes can be directly discharged, and if the liquid in the negative pressure tank does not reach the standard yet, the effluent of the negative pressure tank (or the negative pressure reaction tower) is connected into a cooling water tank, the heat of the water in the cooling water tank is conveyed to the negative pressure tank (or the negative pressure reaction tower) through a water source heat pump to be cooled, and then the effluent reaches the standard after the low-pressure reverse osmosis treatment.
Selection and formulation of three-embodiment draw solution
The concentrated drawing liquid adopted in the embodiment is the drawing liquid formed by dissolving ammonia in water, and the purposes of drawing liquid preparation, drawing liquid regeneration and drawing liquid separation are achieved by utilizing the property of different solubility of ammonia in water under a certain pressure condition.
The data in the prior art show that at a pressure of 1.01bar, the mass solubility of ammonia in water at 20℃is 33.95%, the solubility of ammonia in water at 40℃is 23.3%, the solubility of ammonia in water at 60℃is 13.65%, and the solubility of ammonia in water at 100℃is 0. Converted to volume concentration, then:
ammonia concentration at 100 ℃ is 0mg/L;
the ammonia concentration at 20℃was 339.5g/L, i.e.19.97 mol/L.
Assuming that the system solution is an ideal solution, the osmotic pressure of the solution is calculated using the Fan Tehe f formula, which is shown below:
pi=nCRT type (1)
In the formula (1):
pi is the osmotic pressure of the dilute solution, and the unit is KPa;
n is Fan Tehe f coefficient;
c is the molar concentration of the solution, and the unit is mol/L;
r is the gas constant of 8.31 kPa.L.K-1.mol-1;
t is absolute temperature.
The osmotic pressure of the solution was calculated by substituting ammonia solution at 20℃into the above formula, and the osmotic pressure generated under each condition was 97296.90Kpa (972.97 bar).
In a specific implementation method, ammonia solution is used as a drawing liquid, the temperature of a negative pressure tank is increased to 100 ℃ through a water source heat pump, and the temperature of a high pressure tank is reduced to 20 ℃. The natural osmotic pressure of 927.97bar can be generated after the drawing liquid enters the forward osmosis membrane, water molecules in sewage enter the drawing liquid after passing through the forward osmosis membrane, then the drawing liquid enters the negative pressure reaction tower to be heated to 100 ℃, ammonia is desorbed from the dilute drawing liquid and is pressed into the high-pressure tank by the high-pressure air pump to be redissolved to obtain the drawing liquid for regeneration, the ammonia concentration of the water at the bottom of the negative pressure reaction tower is reduced to 0, and the water can be directly discharged up to the standard.
In another specific implementation method, the concentrated drawing liquid is the drawing liquid formed by dissolving ammonium bicarbonate in water, and the characteristic that ammonium bicarbonate is easy to decompose by heating is utilized to decompose the ammonium bicarbonate in a high-temperature negative pressure reaction tower and synthesize the ammonium bicarbonate in a low-temperature high-pressure tank respectively, so that the regeneration of the drawing liquid and the separation of pure water are realized.
The drawing liquid is prepared by using ammonium bicarbonate (NH 4HCO 3), and the ammonium bicarbonate has the following properties: stable at normal temperature and pressure, has thermal instability, and the solid is decomposed at 58 ℃ and 70 ℃ with water solubility of 14% (10 ℃) and 17.4% (20 ℃) and 21.3% (30 ℃). The aqueous solution was alkaline and had a pH of 0.1 mol.L-1 at 25℃of 7.8. The ammonium bicarbonate has unstable chemical property and is easy to decompose when heated. When heated to about 60 ℃, it breaks down into white fumes consisting of 21.5% NH3, 55.7% CO2, and 22.8% H2O. Can be decomposed by hot water. Under normal pressure, moisture exists, and the slow decomposition starts at the temperature of more than 36 ℃ to generate ammonia, carbon dioxide and water.
According to the physicochemical property of ammonium bicarbonate, 2mol/L ammonium bicarbonate solution is configured at 30 ℃ to serve as a drawing liquid, the osmotic pressure generated by the drawing liquid is 10081.56kPa (100.82 bar), the osmotic pressure is extremely high, sewage is pumped into a forward osmosis membrane by a low-pressure water supply pump, the drawing liquid enters a forward osmosis membrane system from the other side of the forward osmosis membrane under the dual actions of pneumatic driving in a high-pressure storage tank and negative pressure extraction of a negative pressure storage tank, the drawing liquid extracts water molecules in the sewage and then enters a negative pressure reaction tank, a water source heat pump extracts heat in the high-pressure tank and carries the heat into the negative pressure reaction tank, so that the temperature of the high-pressure tank is lowered, the temperature of the negative pressure tank is raised, and the temperature of the high-pressure tank is maintained at 30 ℃ through an automatic control system of the water source heat pump, and the negative pressure reaction tank is maintained at 60 ℃. At the moment, the ammonium bicarbonate solution in the negative pressure reaction tank is decomposed into ammonia, carbon dioxide and water, the ammonia, the carbon dioxide and the water vapor are pumped and compressed into the high-pressure storage tank by the vacuum pump, and the ammonium bicarbonate is combined into the ammonium bicarbonate after the temperature is reduced and the pressure is increased in the high-pressure storage tank, so that the regeneration of the concentrated drawing liquid and the separation of the solute and the water of the diluted drawing liquid are realized. And determining whether a reverse osmosis system is needed to be added at the rear end according to the concentration of the ammonium bicarbonate solution in the negative pressure reaction tank. In the embodiment, ammonium bicarbonate in the negative pressure reaction tower is fully decomposed, so that the ammonium bicarbonate can be directly discharged after reaching standards without reverse osmosis. If the decomposition of ammonium bicarbonate in the negative pressure reaction tower is insufficient, the concentrated solution can be fed into a high-pressure storage tank after reverse osmosis and secondary filtration, and the produced water is discharged after reaching the standard. Even if the decomposition of ammonium bicarbonate is insufficient, the concentration of the ammonium bicarbonate remained in water is low, the generated osmotic pressure is small, so that the separation of solute solvents can be realized at the rear end through common low-pressure reverse osmosis. Thereby saving energy consumption.
4. Effects of the invention
The method is characterized in that 1.7mol/L ammonium bicarbonate solution is used as a drawing liquid, concentrated liquid generated after the garbage leachate is subjected to biochemical treatment, ultrafiltration, nanofiltration and reverse osmosis is used as a material liquid to be treated, the material liquid to be treated is treated by adopting a method for high-pressure regeneration and negative pressure separation of pure water of a forward osmosis membrane drawing liquid, and the method mainly comprises three parts of a forward osmosis membrane separation unit, a pure water and solute separation (desorption) unit in the dilute drawing liquid and a drawing liquid concentration regeneration unit.
Forward osmosis membrane separation unit: the main device of the forward osmosis membrane separation unit comprises a forward osmosis membrane component, a feed liquid feeding pump, a feed liquid circulating pump and the like. Wherein, the forward osmosis membrane only allows water in the feed liquid to pass through, and other components cannot pass through the forward osmosis membrane. In the embodiment, the forward osmosis membrane is composed of a membrane element and a membrane shell, wherein the membrane element adopts a TFC membrane (the thickness of a runner is 85mil, the effective area of a single membrane is 3 square meters, 2 membranes are used), the membrane active layer is made of a polyamide material, and the membrane shell adopts a glass fiber reinforced plastic membrane shell with the pressure level of 4 inches and 20 bar.
A unit for separating (desorbing) pure water from solute in the dilute draw solution: desorption separation is a process of separating dissolved gas (or solute) from pure water by heating, vacuumizing and the like. The ammonium bicarbonate drawing liquid is easy to decompose by heating, so that in the embodiment, the ammonium bicarbonate is separated from the pure water by vacuumizing and heating (non-electric direct heating) modes. The main device comprises a negative pressure reaction tower (the tower is filled with filler, the filler adopts silk screen corrugated plate filler, the filler is thin in material and large in specific surface area, the liquid can form a stable thin liquid layer on a net body, gas-liquid two phases are fully mixed, no liquid accumulation dead angle exists), a water source heat pump (shared with a high-pressure tank and a cooling water tank, and the purpose is to transfer heat in the high-pressure tank and the cooling water tank into the negative pressure reaction tower), a circulating pump, a sprayer, a vacuum pump, a drainage pump, related detection instruments and the like.
And a drawing liquid concentration regeneration unit: gas produced by decomposition, separation and desorption in negative pressure reaction tower(NH 3 、CO 2 ) Solubility in water is high in order to make NH 3 、CO 2 The device is designed into a high-pressure storage tank, a high-pressure air pump, a water source heat pump (shared by a negative pressure reaction tower, and the purpose is to convey the heat in the high-pressure tank into the negative pressure reaction tower, maintain the temperature in the high-pressure tank below 20 ℃, ensure that the drawing liquid enters the forward osmosis membrane and does not damage the forward osmosis membrane), a related detection instrument and the like.
The water quality of the feed liquid to be treated is as follows:
TABLE 2 main physicochemical index of feed liquid to be treated
Description of the embodiment implementation process: the feed liquid to be treated is 2.4m 3 The flow rate of/h enters the feed liquid side of the forward osmosis membrane, a circulating pump is arranged on the feed liquid side, and the flow rate of each part on the feed liquid side of the forward osmosis membrane is 2.4m 3 And/h, the liquid is 0.3m 3 The flow rate/h enters the draw solution side of the forward osmosis membrane.
After the feed liquid to be treated is subjected to forward osmosis treatment, the membrane outlet flow (concentrate flow) is 2.33m 3 And/h, the flow rate of the dilute drawing liquid before entering the negative pressure reaction tower is 0.37m 3 And/h. I.e. the water molecules in the feed liquid to be treated are 0.07m per hour 3 The ammonium bicarbonate of the drawing liquid is diluted to be 1.378mol/L and the molar concentration of the drawing liquid after the drawing liquid passes through the forward osmosis membrane is 1.378mol/L through the estimation.
The forward osmosis process is a process of extracting water molecules in the feed liquid to be treated by passing the extract through a forward osmosis membrane, and the process requires that the concentration of the extract is high (the generated osmotic pressure is high), so that the water molecules in the dilute extract are required to be separated from ammonium bicarbonate and discharged for 0.07m per hour 3 Pure water and ammonium bicarbonate are separated and then transferred to a high-pressure storage tank to be dissolved and regenerated into 1.7mol/L drawing liquid for reuse.
Because the forward osmosis process is a convection process of sewage and the drawing liquid at two sides of the forward osmosis membrane, heat exchange similar to a heat exchanger exists between the drawing liquid and the sewage, and if a temperature difference exists between the drawing liquid and the feed liquid to be treated, the heat exchange can be spontaneously performed between the sewage and the drawing liquid. The initial temperature of the drawing liquid and the sewage is 20 ℃, and the configuration quantity of the drawing liquid is 1m 3 (stored in a high-pressure tank), the initial state in the negative pressure reaction tower is also 1m 3 Drawing liquid, after the equipment is operated, the liquid to be treated is 2.4m 3 The flow rate of/h enters the feed liquid side of the forward osmosis membrane, a circulating pump is arranged on the feed liquid side, and the flow rate of each part on the feed liquid side of the forward osmosis membrane is 2.4m 3 And/h, the liquid is 0.3m 3 The flow rate/h enters one side of the forward osmosis membrane drawing liquid, and after the liquid to be treated is subjected to forward osmosis treatment, the membrane outlet flow (concentrate flow) is 2.33m 3 And/h, the flow rate of the dilute drawing liquid before entering the negative pressure reaction tower is 0.37m 3 And/h, the product water (pure water) outlet flow of the negative pressure reaction tower is 0.07m 3 And/h. In the process, the water source heat pump carries heat energy from the high-pressure storage tank to the negative pressure reaction tower, hot gas and water vapor pumped from the negative pressure reaction tower enter the high-pressure tank to release heat and reform drawing liquid, meanwhile, the heat of the drawing liquid in the high-pressure storage tank is continuously transferred to the negative pressure reaction tower to reduce the temperature, and the drawing liquid enters the forward osmosis membrane and exchanges heat with the liquid to be treated to raise the temperature, so that the heat energy source of the water source heat pump is provided with the drawing liquid in the high-pressure storage tank, the liquid to be treated and high-temperature gas and water vapor pumped from the negative pressure reaction tower (the heat transfer energy of air at the periphery of equipment is ignored).
In the forward osmosis process, heat exchange occurs between the liquid to be treated and the liquid to be treated through the forward osmosis membrane, heat transfer occurs between the negative pressure reaction tower and the high pressure tank through the water source heat pump, the energy efficiency ratio of the water source heat pump is 3, the temperature of the dilute liquid to be treated in the negative pressure reaction tower is gradually increased, and the temperature of the liquid to be treated in the high pressure tank is gradually reduced. When the temperature of the negative pressure reaction tower rises to 95 ℃, the temperature of the liquid drawn by the high-pressure storage tank is reduced to 3.12 ℃ (the relationship between the temperature of the liquid drawn by the high-pressure tank and the temperature of the liquid drawn by the thin liquid drawn by the negative pressure reaction tower is shown in figure 5). At this time, the ammonia nitrogen concentration of the dilute drawing liquid of the negative pressure reaction tower is 23.2mg/L, which is smaller than the standard limit value (25 mg/L) of Table 2 in the domestic garbage landfill pollution control standard, and the desorption rate of ammonium bicarbonate is 99.91%.
In the process, the water source heat pump with the energy efficiency ratio of 3 is adopted to heat the negative pressure reaction tower by 1m 3 The temperature of the dilute draw solution is raised from 20 ℃ to 95 ℃ and the transfer is required to be 3.15X10 8 J energy and power consumption of 1.05X10 8 J (29.17 degree electricity); if the traditional electric boiler direct heating mode is adopted, the heat energy conversion efficiency is 90 percent, 1m 3 The temperature of the dilute drawing liquid is increased from 20 ℃ to 95 ℃ and the consumption is 3.5x10 8 J energy and power consumption are 97.22 DEG electricity. The embodiment adopts a water source heat pump, and compared with an electric boiler heating method, the energy is saved by about 70 percent.
In this specification, each embodiment is described in a related manner, and identical and similar parts of each embodiment are all referred to each other, and each embodiment mainly describes differences from other embodiments. In particular, for system embodiments, since they are substantially similar to method embodiments, the description is relatively simple, as relevant to see a section of the description of method embodiments.
The foregoing description is only of the preferred embodiments of the present invention and is not intended to limit the scope of the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention are included in the protection scope of the present invention.
Claims (7)
1. The utility model provides a positive osmotic membrane separation equipment of high pressure gas drive negative pressure separation which characterized in that: the device comprises a forward osmosis membrane system, a concentrated water storage tank, a high-pressure tank, a negative pressure tank, a water source heat pump unit, an air pump and a water pump; the forward osmosis membrane system comprises a sewage inlet, a concentrated water outlet, a dilute draw solution outlet, a draw solution inlet and a sewage circulating pump; the concentrated water outlet of the forward osmosis membrane system is communicated with the concentrated water storage tank, the dilute draw solution outlet of the forward osmosis membrane system is communicated with the negative pressure tank, and the draw solution inlet of the forward osmosis membrane system is communicated with the high pressure tank; the water source heat pump unit is respectively connected with the high-pressure tank and the negative-pressure tank; the negative pressure tank is provided with a gas outlet and a liquid outlet; the gas outlet of the negative pressure tank is connected with a gas pump and leads to the high pressure tank; and the liquid outlet of the negative pressure tank is connected with a water pump.
2. The high pressure gas driven negative pressure separation forward osmosis membrane separation device according to claim 1, wherein: the separation equipment also comprises a reverse osmosis system and a standard reaching water tank, wherein a liquid outlet of the negative pressure tank is connected with the water pump and then is respectively connected with the reverse osmosis system and the standard reaching water tank; the reverse osmosis system comprises a water production outlet and a trapped fluid outlet, the water production outlet of the reverse osmosis system is led to a standard water tank, the outlet of the standard water tank is connected with a water pump, and the trapped fluid outlet of the reverse osmosis system is led to the negative pressure tank or the high pressure tank through valve control.
3. The high pressure gas driven negative pressure separation forward osmosis membrane separation device according to claim 2, wherein: the separation equipment further comprises a cooling water tank, the cooling water tank is respectively connected with the negative pressure tank and the reverse osmosis system, a water pump is arranged between the cooling water tank and the reverse osmosis system, and the water source heat pump unit is respectively connected with the high pressure tank, the negative pressure tank and the reverse osmosis system.
4. The high pressure gas driven negative pressure separation forward osmosis membrane separation device according to claim 1, wherein: the negative pressure tank is internally provided with a packing layer and a sprayer, and the negative pressure tank is externally provided with a circulating pump.
5. The high pressure gas driven negative pressure separation forward osmosis membrane separation device according to claim 1, wherein: the air pump connected with the air outlet of the negative pressure tank is a vacuum air pump and a high-pressure air pump in sequence.
6. The positive osmosis membrane separation method for high-pressure gas-driven negative pressure separation is characterized by comprising the following steps of: a forward osmosis membrane separation device employing the high pressure gas-driven negative pressure separation as claimed in claim 1 or 4, comprising the steps of:
(1) Dissolving soluble pressure-sensitive gas in water to obtain a drawing liquid, dissolving the soluble gas in water to form a salt solution, and filling the salt solution into a high-pressure tank, wherein the high-pressure driving drawing liquid enters a forward osmosis membrane system to draw water molecules in the feed liquid to be treated;
(2) When the feed liquid to be treated passes through the forward osmosis membrane system, water molecules diffuse into the drawing liquid with lower water chemical potential;
(3) The method comprises the steps that after water molecules enter into the extracting solution, the extracting solution is diluted into diluted extracting solution, the diluted extracting solution enters into a negative pressure tank, heat energy of the extracting solution in a high pressure tank is transferred into the extracting solution in the negative pressure tank through a water source heat pump, the temperature of the extracting solution in the negative pressure tank is increased, the temperature of the extracting solution in the high pressure tank is reduced, meanwhile, an air pump pumps air from the negative pressure tank to the high pressure tank, the pressure in the negative pressure tank is reduced, the temperature is increased, a large amount of dissolved gas in the diluted extracting solution is separated out, and the dissolved gas is pressed into the high pressure tank by the air pump to be dissolved again; thereby realizing the separation of solute and product water in the negative pressure tank and the regeneration of the drawing liquid in the high pressure tank at the same time;
(4) Discharging water in the negative pressure tank.
7. The positive osmosis membrane separation method for high-pressure gas-driven negative pressure separation is characterized by comprising the following steps of: a forward osmosis membrane separation device employing the high pressure gas driven negative pressure separation of claim 3, comprising the steps of:
(1) Dissolving gas which is easy to dissolve in water to form drawing liquid, filling the drawing liquid into a high-pressure tank, and driving the drawing liquid to enter a forward osmosis membrane system to draw water molecules in feed liquid to be treated by high pressure;
(2) When the feed liquid to be treated passes through the forward osmosis membrane system, water molecules diffuse into the drawing liquid with lower water chemical potential;
(3) The method comprises the steps that after water molecules enter into the extracting solution, the extracting solution is diluted into diluted extracting solution, the diluted extracting solution enters into a negative pressure tank, heat energy of the extracting solution in a high pressure tank is transferred into the extracting solution in the negative pressure tank through a water source heat pump, the temperature of the extracting solution in the negative pressure tank is increased, the temperature of the extracting solution in the high pressure tank is reduced, meanwhile, an air pump pumps air from the negative pressure tank to the high pressure tank, the pressure in the negative pressure tank is reduced, the temperature is increased, a large amount of dissolved gas in the diluted extracting solution is separated out, and the dissolved gas is pressed into the high pressure tank by the air pump to be dissolved again; thereby realizing the separation of solute and product water in the negative pressure tank and the regeneration of the drawing liquid in the high pressure tank at the same time;
(4) Detecting water in the negative pressure tank, and directly discharging if the water reaches the standard; if the water does not reach the standard, the water discharged from the negative pressure tank is connected into the cooling water tank for cooling, the cooling mode is carried out by adopting a water source heat pump set, the heat of the water in the cooling water tank is conveyed into the negative pressure tank, the water produced after the water is treated by the reverse osmosis system is discharged after reaching the standard, and part of the concentrated water in the reverse osmosis system flows back to the negative pressure tank and the other part flows back to the high pressure tank.
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