CN113952843A - Batch type MVR coupling vacuum membrane distillation concentration sulfuric acid solution recovery system and method - Google Patents
Batch type MVR coupling vacuum membrane distillation concentration sulfuric acid solution recovery system and method Download PDFInfo
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 134
- 239000012528 membrane Substances 0.000 title claims abstract description 87
- 238000004821 distillation Methods 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 21
- 238000011084 recovery Methods 0.000 title claims abstract description 13
- 230000008878 coupling Effects 0.000 title claims abstract description 8
- 238000010168 coupling process Methods 0.000 title claims abstract description 8
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 83
- 239000002994 raw material Substances 0.000 claims abstract description 32
- 239000012510 hollow fiber Substances 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 89
- 238000001704 evaporation Methods 0.000 claims description 24
- 230000008020 evaporation Effects 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 11
- 239000000498 cooling water Substances 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 238000009826 distribution Methods 0.000 claims description 4
- 230000002209 hydrophobic effect Effects 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 239000012982 microporous membrane Substances 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 239000012774 insulation material Substances 0.000 claims description 3
- -1 polytetrafluoroethylene Polymers 0.000 claims description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 3
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims 1
- 235000011149 sulphuric acid Nutrition 0.000 claims 1
- 239000001117 sulphuric acid Substances 0.000 claims 1
- 239000000243 solution Substances 0.000 description 51
- 238000005516 engineering process Methods 0.000 description 17
- 239000002699 waste material Substances 0.000 description 10
- 239000007789 gas Substances 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 6
- 238000005338 heat storage Methods 0.000 description 5
- 238000000746 purification Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000014509 gene expression Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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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
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/364—Membrane distillation
-
- 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
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/366—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
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/368—Accessories; Auxiliary operations
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A batch type MVR coupling vacuum membrane distillation concentration sulfuric acid solution recovery system and a method belong to the technical field of membrane separation. The device comprises a control valve, a raw material tank, a heat exchanger, a hollow fiber membrane tube, a vacuum membrane component, a steam compressor, a steam heat accumulator, a discharge pipe, a nozzle, a steam generator, a gas-liquid separator, a vacuum pump, a condensate tank and a circulating pump.
Description
Technical Field
The invention relates to the technical field of membrane separation, in particular to a batch type MVR coupling vacuum membrane distillation concentration sulfuric acid solution recovery system and a batch type MVR coupling vacuum membrane distillation concentration sulfuric acid solution recovery method.
Background
With the progress of society and the high-speed development of science and technology, the consumption of sulfuric acid is over 9000 ten thousand tons in China every year, and the sulfuric acid is mainly applied to the industries of petrifaction, steel, nonferrous metal, chlor-alkali, paper making and the like. However, a large amount of sulfuric acid waste liquid is generated in the production and use process, and if the sulfuric acid waste liquid is directly discharged, not only is serious resource waste caused, but also the environmental pollution is aggravated. With the increasing demand of society for energy conservation, emission reduction and clean environment development, the sulfuric acid waste liquid is listed in the national hazardous waste record at present. The country emphasizes the implementation of pollution and carbon reduction actions and accelerates the promotion of a green low-carbon technology. Obviously, the market potential of industrial sulfuric acid waste liquid treatment is huge, how to realize the resource utilization of the sulfuric acid waste liquid becomes a common problem in many industries, and an advanced and efficient sulfuric acid waste liquid resource recycling technology is urgently needed.
At present, the treatment methods for the sulfuric acid waste liquid mainly comprise neutralization, pyrolysis, single-effect evaporation, multi-effect evaporation, membrane distillation and the like. Among them, membrane distillation has been paid attention to by various tradesmen at home and abroad because of its mild operation conditions, extremely high separation efficiency and ultra-strong corrosion resistance. The membrane distillation uses a macromolecule hydrophobic microporous membrane as a barrier, water molecules in feed liquid at the hot side are evaporated on the surface of the membrane and pass through membrane holes to reach the cold side under the pushing of steam pressure difference at two sides of the membrane, and thus, the separation and purification of the feed liquid are realized. At present, membrane distillation technology shows good concentration effect aiming at different sulfuric acid solutions, but because of lack of a latent heat recovery unit, fresh steam, electric energy and the like are still used as heating heat sources in industry, key technical bottlenecks of low thermal efficiency and high energy consumption generally exist, and enterprise application cannot be completely realized.
Mechanical Vapor Recompression (MVR) is a novel efficient energy-saving technology, aims to compress and heat secondary vapor by using a vapor compressor, and then uses the secondary vapor as a heat source to heat stock solution, so that the latent heat of the secondary vapor in the vapor recompression system is recycled, the evaporation energy consumption is effectively reduced, and the vapor recompression system is widely applied to the fields of seawater desalination, wastewater treatment and the like. However, the separation efficiency of the conventional gas-liquid separator is not higher than 90%, and the secondary steam is doped with a certain sulfuric acid component, so that the secondary steam can corrode and damage a steam compressor and is not suitable for evaporation and concentration of the sulfuric acid solution. Obviously, the combination of membrane distillation technology and MVR technology to treat sulfuric acid solution such as sulfuric acid will be a development trend in the future. The invention patent CN201810628388.8 discloses a system and a method for concentrating sulfuric acid solution by MVR coupling without a liquid storage membrane module, the device comprises a membrane module, a vapor compressor, a membrane separator, a heater, a cooler, a feeding tank, a water outlet tank and other devices, the vapor compressor is mainly adopted to compress secondary vapor generated by evaporation of sulfuric acid solution in the membrane module, and then the secondary vapor is used as a heat source to heat feed liquid, the latent heat of the secondary vapor in the interior is recovered, and the evaporation energy consumption and the operation cost are effectively reduced. In fact, the initial secondary steam generation of the MVR vacuum membrane distillation system is slow, and from the start-up to the stable evaporation stage, the feed liquid cannot be heated by the latent heat of the secondary steam, and an external heat source is still required for heat compensation, so that the MVR coupled vacuum membrane distillation system has the problems of long intermittent start-up time and high energy consumption in the batch evaporation occasion.
The steam heat accumulator is an energy-saving device with wide application, can assist in adjusting the steam load changing between a boiler and a user, and ensures the energy conservation and the stability of a heating system and equipment. If the vacuum membrane distillation technology, the MVR technology and the steam heat storage technology can be combined and applied to concentration and purification of the sulfuric acid solution, the high-purity separation of the sulfuric acid solution is realized, and meanwhile, the steam heat accumulator and the latent heat of secondary steam are respectively used as heating heat sources in the intermittent starting and stable evaporation stages, so that the evaporation energy consumption of a system is reduced, the operation stability of the system is improved, and the method has important value and significance for efficient recycling of industrial sulfuric acid waste liquid.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a batch type MVR coupled vacuum membrane distillation concentration sulfuric acid solution recovery system and method with short intermittent start-up time and low energy consumption.
The technical scheme adopted by the invention is as follows: a batch type MVR coupling vacuum membrane distillation concentration sulfuric acid solution recovery system comprises a first control valve, a second control valve, a ninth control valve, a raw material tank, a first heat exchanger, a second heat exchanger, a hollow fiber membrane tube, a vacuum membrane assembly, a steam compressor, a steam heat accumulator, a discharge tube, a nozzle, a steam generator, a gas-liquid separator, a vacuum pump, a condensate tank and a circulating pump;
the solution outlet of the raw material tank is communicated with the cold side inlet of the first heat exchanger through the second control valve and the circulating pump in sequence, the cold side outlet of the first heat exchanger is communicated with the solution inlet of the vacuum membrane assembly, the steam outlet of the vacuum membrane assembly is communicated with the steam inlet of the steam heat accumulator through the steam compressor and the fourth control valve in sequence, the steam outlet of the steam heat accumulator is communicated with the hot side inlet of the first heat exchanger through the seventh control valve, the hot side outlet of the first heat exchanger is communicated with the top end inlet of the water condensing tank, the top end outlet of the water condensing tank is communicated with the hot side inlet of the second heat exchanger, the hot side outlet of the second heat exchanger is communicated with the inlet of the gas-liquid separator, the cold side of the second heat exchanger is communicated with an external cooling water system, and the bottom end outlet of the gas-liquid separator is communicated with the left side inlet of the water condensing tank;
the solution outlet of the vacuum membrane component is communicated with the solution inlet of the raw material tank;
the steam generator is communicated to a steam inlet of the steam heat accumulator through a fifth control valve;
an outlet at the top end of the gas-liquid separator is sequentially communicated with a vacuum pump and an eighth control valve;
the solution inlet of the raw material tank is communicated with a third control valve, and the liquid outlet of the raw material tank is communicated with the first control valve;
a drain outlet of the steam heat accumulator is communicated with a sixth control valve;
and the liquid outlet of the condensed water tank is communicated with a ninth control valve.
Furthermore, a plurality of hollow fiber membrane tubes are arranged in the vacuum membrane component, the hollow fiber membrane tubes are made of polytetrafluoroethylene, and the aperture of the hydrophobic microporous membrane is 0.2-0.4 mu m.
Furthermore, a plurality of calandria pipes are arranged inside the steam heat accumulator, a nozzle is installed at the tail end of each calandria pipe, and a heat insulation material with a certain thickness is laid outside the steam heat accumulator.
In the operation method of the batch type MVR coupled vacuum membrane distillation concentration sulfuric acid solution recovery system, in the initial starting stage, a sixth control valve is started to fill a certain amount of liquid water into a steam heat accumulator, then a steam generator is started to fill fresh steam into the steam heat accumulator, the liquid water in the steam heat accumulator is heated to the required temperature, and the steam generator is stopped; opening a third control valve to add the sulfuric acid solution preheated to the required temperature into the raw material tank, and closing the third control valve after the liquid level in the raw material tank meets the requirement; starting a circulating pump and a second control valve, and pressurizing the sulfuric acid solution in the raw material tank through a first heat exchanger to enter the shell side of the vacuum membrane module; starting a vacuum pump to vacuumize the system to keep the system in a certain negative pressure environment, condensing water vapor doped in non-condensable gas in the system in a second heat exchanger through external cooling water in the vacuumizing process, then introducing the condensed water into a gas-liquid separator to perform gas-liquid separation, returning liquid water to a condensed water tank to be collected and utilized, and pumping the non-condensable gas out of the system; starting a seventh control valve, evaporating liquid water with a certain temperature in the steam heat accumulator into water vapor in a negative pressure environment, and introducing the water vapor into the first heat exchanger to release heat to the sulfuric acid solution; then a steam compressor and a fourth control valve are started, water molecules of a sulfuric acid solution are vaporized into water vapor molecules on the surface of a shell side membrane of the vacuum membrane component, the water vapor molecules pass through a membrane hole under the drive of transmembrane steam pressure difference and reach a hollow fiber membrane tube, then the steam enters the steam compressor to be compressed, heated and pressurized, then the steam is sprayed out through nozzles of distribution calandria in a steam heat accumulator, the steam vapor molecules are mixed and condensed with liquid water at a certain temperature stored in the steam heat accumulator in advance and then release latent heat, the liquid water in the steam heat accumulator is heated and then is vaporized into water vapor molecules again under a certain pressure, the water vapor molecules enter a first heat exchanger through an outlet at the top end of the steam heat accumulator to exchange heat with the sulfuric acid solution, and the water vapor molecules are condensed into liquid water and collected into a water condensation tank; the sulfuric acid solution in the first heat exchanger is heated and then enters the vacuum membrane component for continuous circulating concentration, the whole system utilizes the latent heat of secondary steam produced by the vacuum membrane component as a heat source for stable evaporation, after the sulfuric acid solution in the raw material tank reaches the required concentration, a circulating pump steam compressor, a vacuum pump and various control valves are gradually closed, and a first control valve is opened for discharging;
in the intermittent starting stage, the steam heat accumulator provides an auxiliary heat source for the starting process of the system, and a third control valve is started to inject a second batch of sulfuric acid solution material into the raw material tank; starting a circulating pump and a second control valve, filling a sulfuric acid solution into a vacuum membrane component, starting a vacuum pump and an eighth control valve to vacuumize the system to a certain negative pressure environment, condensing water vapor doped in non-condensable gas in the system in a second heat exchanger through external cooling water in the vacuumizing process, then introducing the condensed water into a gas-liquid separator for gas-liquid separation, returning liquid water to a condensation tank for collection and utilization, and pumping the non-condensable gas out of the system; starting a seventh control valve, evaporating liquid water with a certain temperature in the steam heat accumulator into water vapor in a negative pressure environment, and enabling the water vapor to enter the first heat exchanger to release heat to the sulfuric acid solution; and then starting a steam compressor and a fourth control valve, enabling the vacuum membrane component to generate steam after a period of time, enabling the steam to enter the steam compressor for compression, then entering a steam heat accumulator for condensation and heat release, enabling liquid water in the steam heat accumulator to be heated and evaporated into steam, enabling the steam to enter a first heat exchanger for heating a sulfuric acid solution, and enabling the system to gradually utilize the heat energy of the steam heat accumulator to enter a stable evaporation stage from an intermittent starting stage.
The invention has the following beneficial effects: the invention combines the vacuum membrane distillation technology, the MVR technology and the steam heat storage technology to be applied to the concentration and purification of the sulfuric acid solution, the system adopts batch feeding, the steam heat storage device provides an auxiliary heat source for the intermittent starting process of the system, the starting time is reduced, the consumption of an external steam heat source is saved, the evaporation energy consumption and the operation cost are effectively reduced, and the invention can be used for batch evaporation of strong corrosive solutions such as sulfuric acid and the like.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is within the scope of the present invention for those skilled in the art to obtain other drawings based on the drawings without inventive exercise.
FIG. 1 is a schematic diagram of the system of the present invention;
in the figure, 1-1 first control valve, 1-2 second control valve, 1-3 third control valve, 1-4 fourth control valve, 1-5 fifth control valve, 1-6 sixth control valve, 1-7 seventh control valve, 1-8 eighth control valve, 1-9 ninth control valve, 2 raw material tank, 3-1 first heat exchanger, 3-2 second heat exchanger, 4 hollow fiber membrane module, 5 vacuum membrane module, 6 steam compressor, 7 steam heat accumulator, 8 distribution calandria, 9 spray nozzle, 10 steam generator, 11 gas-liquid separator, 12 vacuum pump, 13 condensate tank, 14 circulating pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in further detail with reference to the accompanying drawings.
It should be noted that all expressions using "first" and "second" in the embodiments of the present invention are used for distinguishing two entities with the same name but different names or different parameters, and it should be noted that "first" and "second" are merely for convenience of description and should not be construed as limitations of the embodiments of the present invention, and they are not described in any more detail in the following embodiments.
The terms of direction and position of the present invention, such as "up", "down", "front", "back", "left", "right", "inside", "outside", "top", "bottom", "side", etc., refer to the direction and position of the attached drawings. Accordingly, the use of directional and positional terms is intended to illustrate and understand the present invention and is not intended to limit the scope of the present invention.
As shown in fig. 1, in an embodiment of the present invention, a batch type MVR coupled vacuum membrane distillation concentration sulfuric acid solution recovery system includes a first to ninth control valves 1 to 1 … … 1 to 9, a raw material tank 2, a first heat exchanger 3 to 1, a second heat exchanger 3 to 2, a hollow fiber membrane tube 4, a vacuum membrane module 5, a vapor compressor 6, a vapor heat accumulator 7, a discharge tube 8, a nozzle 9, a vapor generator 10, a gas-liquid separator 11, a vacuum pump 12, a condensate tank 13, and a circulation pump 14;
a solution outlet of the raw material tank 2 is communicated with a cold side inlet of a first heat exchanger 3-1 through a second control valve 1-2 and a circulating pump 14 in sequence, a cold side outlet of the first heat exchanger 3-1 is communicated with a solution inlet of a vacuum membrane assembly 5, a steam outlet of the vacuum membrane assembly 5 is communicated with a steam inlet of a steam heat accumulator 7 through a steam compressor 6 and a fourth control valve 1-4 in sequence, a steam outlet of the steam heat accumulator 7 is communicated with a hot side inlet of the first heat exchanger 3-1 through a seventh control valve 1-7, a hot side outlet of the first heat exchanger 3-1 is communicated with a top end inlet of a water condensing tank 13, a top end outlet of the water condensing tank 13 is communicated with a hot side inlet of the second heat exchanger 3-2, and a hot side outlet of the second heat exchanger 3-2 is communicated with an inlet of a gas-liquid separator 11, the cold side of the second heat exchanger 3-2 is communicated with an external cooling water system, and the outlet at the bottom end of the gas-liquid separator 11 is communicated with the left inlet of the condensate tank 13;
the solution outlet of the vacuum membrane module 5 is communicated with the solution inlet of the raw material tank 2 and is used for recovering the concentrated sulfuric acid solution;
the steam generator 10 is communicated to a steam inlet of the steam heat accumulator 7 through a fifth control valve 1-5, and heat energy is provided by the steam generator 10 when the system is started for the first time;
the top outlet of the gas-liquid separator 11 is sequentially communicated with a vacuum pump 12 and eighth control valves 1-8, and the vacuum pump 12 is used for vacuumizing the system to keep the system in a certain negative pressure environment;
the solution inlet of the raw material tank 2 is communicated with a third control valve 1-3, and the liquid outlet of the raw material tank 2 is communicated with a first control valve 1-1 and is used for feeding liquid into the raw material tank 2 in batches;
a drain outlet of the steam heat accumulator 7 is communicated with a sixth control valve 1-6 and is used for discharging waste liquid and supplementing liquid water in the initial starting stage to ensure the normal operation of the system;
and a liquid outlet of the condensed water tank 13 is communicated with ninth control valves 1-9. According to the invention, the steam heat storage technology is combined into the vacuum membrane distillation technology and the MVR technology through the system structure, an auxiliary heat source is provided for the system at the interval starting stage by utilizing the steam heat storage technology, the steam generator 10 is not required to be used, the starting time of the interval starting stage is shortened, and the concentration efficiency is improved.
The vacuum membrane component 5 is internally provided with a plurality of hollow fiber membrane tubes 4, the hollow fiber membrane tubes 4 are made of polytetrafluoroethylene, the aperture of a hydrophobic microporous membrane is 0.2-0.4 mu m, and the material has the excellent characteristics of acid resistance, alkali resistance, heat resistance and cold resistance.
The steam heat accumulator 7 is internally provided with a plurality of calandria 8, the tail end of each calandria 8 is provided with a nozzle 9, and the heat insulation material with a certain thickness is laid outside the steam heat accumulator 7, so that the heat loss of steam condensate water is reduced.
In the initial starting stage, starting the sixth control valve 1-6 to fill a certain amount of liquid water into the steam heat accumulator 7, then starting the steam generator 10 to fill fresh steam into the steam heat accumulator 7, heating the liquid water in the fresh steam to a required temperature, and stopping the steam generator 10; opening a third control valve 1-3, adding the sulfuric acid solution preheated to the required temperature into the raw material tank 2, and closing the third control valve 1-3 after the liquid level in the raw material tank 2 meets the requirement; starting a circulating pump 14 and a second control valve 1-2, and pressurizing the sulfuric acid solution in the raw material tank 2 through a first heat exchanger 3-1 to enter the shell side of a vacuum membrane component 5; the vacuum pump 12 is started to vacuumize the system to keep the system in a certain negative pressure environment, in the vacuumizing process, water vapor doped in non-condensable gas in the system is condensed in the second heat exchanger 3-2 through external cooling water and then enters the gas-liquid separator 11 to be subjected to gas-liquid separation, liquid water returns to the condensed water tank 13 to be collected and utilized, the non-condensable gas is pumped out of the system, and therefore the system is guaranteed to achieve a good vacuum environment, and the non-condensable gas refers to air, hydrogen, nitrogen, lubricating oil vapor and the like mixed in the refrigerating system; opening a seventh control valve 1-7, evaporating liquid water with a certain temperature in the steam heat accumulator 7 into water vapor in a negative pressure environment, and introducing the water vapor into a first heat exchanger 3-1 to release heat to the sulfuric acid solution; then, a steam compressor 6 and a fourth control valve 1-4 are started, water molecules of a sulfuric acid solution are vaporized into water vapor molecules on the surface of a shell side membrane of a vacuum membrane component 5, the water vapor molecules pass through membrane holes under the drive of transmembrane steam pressure difference and reach a hollow fiber membrane tube 4, then steam enters the steam compressor 6 to be compressed, heated and pressurized, then the steam is sprayed out through a nozzle 9 of a distribution calandria 8 in a steam heat accumulator 7, the steam and the liquid water are mixed and condensed with liquid water at a certain temperature stored in the steam heat accumulator 7 in advance and then release latent heat, the liquid water in the steam heat accumulator 7 is heated and then is vaporized into water vapor molecules again under a certain pressure, the water vapor molecules enter a first heat exchanger 3-1 through an outlet at the top end of the steam heat accumulator 7 to exchange heat with the sulfuric acid solution, and the water vapor molecules are condensed into liquid water which is collected into a water condensing tank 13; the sulfuric acid solution in the first heat exchanger 3-1 is heated and then enters the vacuum membrane component 5 to continue to be circularly concentrated, the whole system utilizes latent heat of secondary steam produced by the vacuum membrane component 5 as a heat source to carry out stable evaporation, after the sulfuric acid solution in the raw material tank 2 reaches the required concentration, the circulating pump 14, the steam compressor 6, the vacuum pump 12 and various control valves are gradually closed, and the first control valve 1-1 is opened to discharge;
in the intermittent starting stage, the steam heat accumulator 7 provides an auxiliary heat source for the starting process of the system, and a third control valve 1-3 is opened to inject a second batch of sulfuric acid solution material into the stock tank 2; starting a circulating pump 14 and a second control valve 1-2, filling a sulfuric acid solution into a vacuum membrane component 5, starting a vacuum pump 12 and an eighth control valve 1-8 to vacuumize the system to a certain negative pressure environment, condensing water vapor doped in non-condensable gas in the system in a second heat exchanger 3-2 through external cooling water in the vacuumizing process, then introducing the condensed water into a gas-liquid separator 11 to perform gas-liquid separation, returning liquid water to a condensing tank 13 to be collected and utilized, and pumping the non-condensable gas out of the system so as to ensure that the system achieves a good vacuum environment, starting a seventh control valve 1-7, evaporating liquid water at a certain temperature in a steam heat accumulator 7 into water vapor in the negative pressure environment, and introducing the water vapor into a first heat exchanger 3-1 to release heat to the sulfuric acid solution; then a steam compressor 6 and a fourth control valve 1-4 are started, steam generated by the vacuum membrane component 5 after a period of time enters the steam compressor 6 for compression, then enters a steam heat accumulator 7 for condensation and heat release, liquid water in the steam heat accumulator 7 is heated and evaporated into steam, the steam enters a first heat exchanger 3-1 for heating a sulfuric acid solution, and the system gradually utilizes the heat energy of the steam heat accumulator 7 and enters a stable evaporation stage from an intermittent starting stage.
The above disclosure is only for the purpose of illustrating the preferred embodiments of the present invention, and it is therefore to be understood that the invention is not limited by the scope of the appended claims.
Claims (4)
1. The utility model provides a formula MVR coupling vacuum membrane distillation concentration retrieves sulphuric acid solution system of wholesale, its characterized in that: comprises a first control valve to a ninth control valve (1-1)……1-9), a raw material tank (2), a first heat exchanger (3-1), a second heat exchanger (2)3-2), a hollow fiber membrane tube (4), a vacuum membrane component (5), a steam compressor (6), a steam heat accumulator (7), a discharge pipe (8), a nozzle (9), a steam generator (10), a gas-liquid separator (11), a vacuum pump (12), a condensate tank (13) and a circulating pump (14);
a solution outlet of the raw material tank (2) is communicated with a cold side inlet of the first heat exchanger (3-1) through the second control valve (1-2) and the circulating pump (14) in sequence, a cold side outlet of the first heat exchanger (3-1) is communicated with a solution inlet of the vacuum membrane assembly (5), a steam outlet of the vacuum membrane assembly (5) is communicated with a steam inlet of the steam heat accumulator (7) through the steam compressor (6) and the fourth control valve (1-4) in sequence, a steam outlet of the steam heat accumulator (7) is communicated with a hot side inlet of the first heat exchanger (3-1) through the seventh control valve (1-7), a hot side outlet of the first heat exchanger (3-1) is communicated with a top end inlet of the condensed water tank (13), a top end outlet of the condensed water tank (13) is communicated with a hot side inlet of the second heat exchanger (3-2), the hot side outlet of the second heat exchanger (3-2) is communicated with the inlet of a gas-liquid separator (11), the cold side of the second heat exchanger (3-2) is communicated with an external cooling water system, and the bottom end outlet of the gas-liquid separator (11) is communicated with the left inlet of a water condensation tank (13);
the solution outlet of the vacuum membrane component (5) is communicated with the solution inlet of the raw material tank (2);
the steam generator (10) is communicated to a steam inlet of the steam heat accumulator (7) through a fifth control valve (1-5);
the top outlet of the gas-liquid separator (11) is communicated with a vacuum pump (12) and an eighth control valve (1-8) in sequence;
the solution inlet of the raw material tank (2) is communicated with a third control valve (1-3), and the liquid outlet of the raw material tank is communicated with a first control valve (1-1);
a drain outlet of the steam heat accumulator (7) is communicated with a sixth control valve (1-6);
and a liquid outlet of the condensed water tank (13) is communicated with a ninth control valve (1-9).
2. The batch type MVR coupled vacuum membrane distillation concentration and recovery sulfuric acid solution system as claimed in claim 1, wherein: the vacuum membrane component (5) is internally provided with a plurality of hollow fiber membrane tubes (4), the hollow fiber membrane tubes (4) are made of polytetrafluoroethylene, and the aperture of a hydrophobic microporous membrane is 0.2-0.4 mu m.
3. The batch type MVR coupled vacuum membrane distillation concentration and recovery sulfuric acid solution system as claimed in claim 1, wherein: the steam heat accumulator (7) is internally provided with a plurality of calandria (8), the tail end of each calandria (8) is provided with a nozzle (9), and the outside of the steam heat accumulator (7) is laid with a heat insulation material with a certain thickness.
4. A method of operating the batch MVR coupled vacuum membrane distillation concentration sulfuric acid solution recovery system of claim 1, wherein: in the initial starting stage, a sixth control valve (1-6) is started to fill a certain amount of liquid water into the steam heat accumulator (7), then the steam generator (10) is started to fill fresh steam into the steam heat accumulator (7), the liquid water in the fresh steam heat accumulator is heated to the required temperature, and the steam generator (10) is stopped; opening a third control valve (1-3) to add the sulfuric acid solution preheated to the required temperature into the raw material tank (2), and closing the third control valve (1-3) after the liquid level in the raw material tank (2) meets the requirement; starting a circulating pump (14) and a second control valve (1-2), and pressurizing the sulfuric acid solution in the raw material tank (2) through a first heat exchanger (3-1) to enter the shell side of a vacuum membrane component (5); the vacuum pump (12) is started to vacuumize the system, so that the system is kept in a certain negative pressure environment, in the vacuumizing process, water vapor doped in non-condensable gas in the system is condensed in the second heat exchanger (3-2) through external cooling water, then enters the gas-liquid separator (11) to be subjected to gas-liquid separation, liquid water returns to the condensation tank (13) to be collected and utilized, and the non-condensable gas is pumped out of the system; opening a seventh control valve (1-7), evaporating liquid water with a certain temperature in the steam heat accumulator (7) into water vapor in a negative pressure environment, and introducing the water vapor into a first heat exchanger (3-1) to release heat to the sulfuric acid solution; then a steam compressor (6) and a fourth control valve (1-4) are started, water molecules of the sulfuric acid solution are vaporized into water vapor molecules on the surface of a shell side membrane of the vacuum membrane component (5), driven by transmembrane steam pressure difference, the vapor passes through the membrane pores to reach the hollow fiber membrane tube (4), then the vapor enters the vapor compressor (6) to be compressed, heated and pressurized, then the steam is sprayed out through a nozzle (9) of a distribution calandria (8) in the steam heat accumulator (7), mixed with liquid water with certain temperature stored in the steam heat accumulator (7) in advance and then released latent heat after condensation, liquid water in the steam heat accumulator (7) is heated and then is evaporated into water vapor molecules under certain pressure, enters the first heat exchanger (3-1) through the outlet at the top end of the steam heat accumulator (7) to exchange heat with sulfuric acid solution, is condensed into liquid water and is collected into a water condensation tank (13); the sulfuric acid solution in the first heat exchanger (3-1) is heated and then enters the vacuum membrane component (5) for continuous circulating concentration, the whole system utilizes the latent heat of secondary steam produced by the vacuum membrane component (5) as a heat source for stable evaporation, after the sulfuric acid solution in the raw material tank (2) reaches the required concentration, the circulating pump (14) is gradually closed, the steam compressor (6), the vacuum pump (12) and various control valves are gradually closed, and the first control valve (1-1) is opened for discharging;
in the intermittent starting stage, the steam heat accumulator (7) provides an auxiliary heat source for the starting process of the system, and a third control valve (1-3) is opened to inject a second batch of sulfuric acid solution material into the raw material tank (2); starting a circulating pump (14) and a second control valve (1-2), filling a sulfuric acid solution into a vacuum membrane component (5), starting a vacuum pump (12) and an eighth control valve (1-8) to vacuumize the system to a certain negative pressure environment, condensing water vapor doped in non-condensable gas in the system in a second heat exchanger (3-2) through external cooling water in the vacuumizing process, then introducing the condensed water into a gas-liquid separator (11) to perform gas-liquid separation, returning liquid water to a condensed water tank (13) to be collected and utilized, and pumping the non-condensable gas out of the system; opening a seventh control valve (1-7), evaporating liquid water with a certain temperature in the steam heat accumulator (7) into water vapor under a negative pressure environment, and introducing the water vapor into the first heat exchanger (3-1) to release heat to the sulfuric acid solution; then a steam compressor (6) and a fourth control valve (1-4) are started, steam generated by a vacuum membrane component (5) after a period of time enters the steam compressor (6) to be compressed, then enters a steam heat accumulator (7) to be condensed and released, liquid water in the steam heat accumulator (7) is heated and evaporated into steam, the steam enters a first heat exchanger (3-1) to heat a sulfuric acid solution, and the system gradually utilizes the heat energy of the steam heat accumulator (7) to enter a stable evaporation stage from an intermittent starting stage.
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Cited By (2)
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| CN117228765A (en) * | 2023-09-07 | 2023-12-15 | 广东省和佳环保科技有限公司 | Phosphoric acid waste liquid secondary concentration MVR energy-saving evaporator |
| CN117463154A (en) * | 2023-11-20 | 2024-01-30 | 浙江环诺环保科技股份有限公司 | Multi-effect vacuum membrane distillation coupling mechanical vapor recompression evaporation system and working method thereof |
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2021
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| DONG HAN ET AL.: "Experimental investigation of a batched mechanical vapor recompression evaporation system", APPLIED THERMAL ENGINEERING, vol. 192, no. 116940 * |
| ZETIAN SI ET AL.: "Performance analysis of treating sulfuric acid solution by the combined system of vacuum membrane distillation and mechanical vapor recompression", CHEMICAL ENGINEERING & PROCESSING: PROCESS INTENSIFICATION, vol. 150, no. 107890 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117228765A (en) * | 2023-09-07 | 2023-12-15 | 广东省和佳环保科技有限公司 | Phosphoric acid waste liquid secondary concentration MVR energy-saving evaporator |
| CN117228765B (en) * | 2023-09-07 | 2024-08-27 | 广东省和佳环保科技有限公司 | Phosphoric acid waste liquid secondary concentration MVR evaporator |
| CN117463154A (en) * | 2023-11-20 | 2024-01-30 | 浙江环诺环保科技股份有限公司 | Multi-effect vacuum membrane distillation coupling mechanical vapor recompression evaporation system and working method thereof |
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