CN107596706B - Steam condensation evaporation technology and device - Google Patents
Steam condensation evaporation technology and device Download PDFInfo
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- CN107596706B CN107596706B CN201710932988.9A CN201710932988A CN107596706B CN 107596706 B CN107596706 B CN 107596706B CN 201710932988 A CN201710932988 A CN 201710932988A CN 107596706 B CN107596706 B CN 107596706B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 106
- 239000000463 material Substances 0.000 claims abstract description 59
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Abstract
The invention relates to a steam condensing and evaporating technology and a device in the technical field of distillation, which are characterized in that steam in an evaporator is condensed into distillate and discharged out of the evaporator, and heat released when the steam is condensed into the distillate is heated by a heat pump system and heats materials in the evaporator; in the aspect of drying, a dryer shell is taken as an evaporator, a hot water tank and an annular net belt are arranged in the shell, the hot water tank is connected with a hot water storage tank and a hot end heat exchanger, and a cold end heat exchanger is connected with the right end part of the shell and a distillate storage tank; in the filter pressing industry, a van type membrane filter press is used as an evaporator, a hot end heat exchanger transfers heat to a hot water storage tank, the hot water storage tank is communicated with a heating chamber of the filter press, so that a filter cake beside the heating chamber evaporates steam, and the steam is condensed into distillate by a cold end heat exchanger; the invention utilizes the heat released by steam cooling, so that the energy consumption for producing distillate, material filter pressing and drying is only 25% -80% of that of using electric, air energy and MVR technical devices, and the energy-saving effect is remarkable.
Description
Technical Field
The invention relates to the field of distillation technology and equipment manufacturing, in particular to a steam condensation evaporation technology and a steam condensation evaporation device.
Background
It is known that a liquid absorbs a large amount of heat from a liquid phase to a gas phase, and a large amount of heat is released from the gas phase to the liquid phase. In the traditional distilled water production process, liquid water is heated to a temperature above the boiling point of the liquid water to be changed into steam, and then the steam is cooled to obtain pure distilled water. The distilled water produced by the traditional method has great energy consumption no matter the distilled water is heated by coal, fuel gas or fuel oil or by electricity, and besides the efficiency of heating the water is not high, the other reason is that the heat released when the steam is cooled into distilled water is not recycled. The distilled water produced by the resin filtration method in industry has limited application range because the purity of the water is not high.
In the prior art, air is used for controlling the temperature of heating liquid, liquid with specific boiling point such as alcohol vapor is distilled out, and then the liquid alcohol is obtained by cooling, and in the process of brewing the wine by using grains, the concentration of the wine, namely the concentration of the alcohol in the wine, is generally improved by using a distillation method, and meanwhile, the distillation energy consumption is greatly reduced. The patent publication No. CN 106267872A describes a device for distilling specific liquid by using air energy, which is divided into an upper distillation steam treatment chamber and a lower air energy heater, wherein the treatment chamber is provided with a cooling coil and a fan, and the fan takes away heat released after cooling steam into liquid, namely, the heat is discharged into the atmosphere. The heater uses an air energy heating device, the heater absorbs heat from the atmosphere, the liquid is supplied for heating warm water, and the liquid in the buffer chamber, the liquid storage chamber and the material storage chamber is heated to be changed into steam, and then the steam is cooled by the processing chamber to be changed into liquid. The energy heated by the patent is from the atmosphere, and compared with the common electric heating method, the energy is saved, the cooled heat is discharged into the atmosphere, and the energy cannot be reused, so that the energy is wasted.
The patent of integrated MVR evaporation drying system of Xin-heng-an application, bulletin No. CN 206262122U, it includes a sealed box, the inside of the box sets up the evaporation tank, the evaporation tank is below the sealed heat source channel, the heat source channel lets in the hot water; the external part of the box body is provided with a hot water storage tank and a steam-water mixer which are mutually communicated, the lower part of the hot water storage tank is communicated with the inlet of the heat source channel through a circulating pump, and the lower part of the steam-water mixer is communicated with the outlet of the heat source channel; the outside of the box body is provided with a steam compressor, and an inlet and an outlet of the steam compressor are respectively connected with a steam outlet of the box body and the lower part of the steam-water mixer. The hot water is heated by utilizing the heat of the steam discharged by the steam compressor to absorb the steam of the box body, then the hot water is led into the heat source channel, the material on the evaporation tank above the heat source channel is heated, the material is dehydrated and dried, the steam evaporated in the material drying process is absorbed and reused by the steam compressor, a large amount of steam discharged by the box body is returned to the system again for reuse, the temperature of the discharged material is reduced, and the device is energy-saving and environment-friendly. However, the patent has two disadvantages, namely, firstly, the non-condensable gas and condensed water discharged from the non-condensable gas discharge valve and the condensed water discharge valve are discharged, and the heat carried by the non-condensable gas and the condensed water is not recovered, so that the energy waste is caused; secondly, the steam evaporated in the material drying process is absorbed and compressed by the compressor and then reused, the high-temperature and high-pressure steam directly contacts with the compressor to corrode the compressor, the steam pressure at the evaporation end cannot be reduced, the evaporation temperature is higher, the high-temperature evaporation easily enables the evaporated material to react to generate byproducts, sometimes even the material is cured, foam is easily formed in the evaporator, and the evaporated material is mixed in the steam, so that the effect of effective separation cannot be achieved.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a simple and efficient steam condensation and evaporation technology and a device.
The technical scheme adopted by the invention is as follows:
a steam condensing and evaporating technology is to condense the steam evaporated from the material in the sealed evaporator into distillate, discharge the distillate out of the evaporator, reduce the steam pressure in the evaporator, heat the heat released when the steam condenses into distillate, heat the material in the evaporator through the heat pump system, maintain the evaporation process to continue, realize the evaporation and separation of the distillate with low energy consumption.
A steam condensing and evaporating device manufactured by a steam condensing and evaporating technology comprises a heat pump system, a heat pump system and a heat pump system, wherein the heat pump system comprises a compressor, a hot-end heat exchanger and a cold-end heat exchanger which are connected with each other; the cold end heat exchanger absorbs heat from steam evaporated from materials in the closed evaporator, the heat is warmed up through the compressor and is conveyed to the hot end heat exchanger, and meanwhile, the steam is condensed into distillate and discharged out of the evaporator; the hot end heat exchanger provides heat for the material to be evaporated in the closed evaporator, so that the material is evaporated to steam; the bottom of the evaporator is provided with a preheater which can be heated by any one of electricity, oil, gas and steam.
Further, a distillate outlet of the cold-end heat exchanger is connected with a distillate storage tank, and the top of the distillate storage tank is connected with a vacuum pump; the steam inlet of the cold end heat exchanger is connected with the top of the evaporator; the evaporator is connected with the hot end heat exchanger through a circulating pump.
Still further, connect a distillate pump at the bottom of said distillate storage tank; the upper part of the evaporator is connected with a mother liquor replenishing control valve, and the bottom of the evaporator is connected with a concentrated solution pumping pump.
The scheme can be used for concentrating liquid materials, evaporating and crystallizing salt solution, producing distilled water and distilling and separating wine making and oil refining. Taking distilled pure water as an example, the distilled pure water device manufactured by the invention only consumes 50 degrees of electricity per ton of pure water, which is equivalent to 0.05 degree of electricity per kilogram of water, and the cost per kilogram of water is only 0.05 yuan when the price of electricity per degree is 1 yuan. Can be used for household pure water generators and distilled water production of laboratories, medical treatment, schools and industrial and mining enterprises. Distilled pure water produced using an electric distiller has a cost of 0.20 yuan per kilogram of water. In the initial working stage after the evaporator is started, the liquid in the evaporator is required to be preheated, the preheating is stopped after the temperature reaches the set value, and the preheating is not required in the normal working process.
Another steam condensing and evaporating device manufactured by the steam condensing and evaporating technology, namely the application of the steam condensing and evaporating technology in a dryer, wherein the heat pump system comprises a compressor, a hot-end heat exchanger and a cold-end heat exchanger which are connected with each other; the evaporator is a sealed dryer shell, a hot water tank is arranged in the shell, annular mesh belts are arranged on the upper surface and the lower surface of the hot water tank, the annular mesh belts can slide on the upper surface and the lower surface of the evaporator, and materials to be dried can be placed on the annular mesh belts; the water inlet of the hot water tank is connected with a circulating pump and a hot water storage tank which are arranged outside the shell, and the water outlet of the hot water tank and the water inlet of the hot water storage tank are connected with a hot end heat exchanger; the steam inlet of the cold-end heat exchanger is connected with the right end part of the evaporator; the distillate outlet of the cold-end heat exchanger is connected with a distillate storage tank, and the top and the bottom of the distillate storage tank are respectively connected with a vacuum pump and a distillate discharge pump; the bottom of the hot water storage tank is provided with a preheater which can be heated by any one of electricity, oil, gas and steam. The annular mesh belt used in the method can be replaced by a blade type or disc type conveying mode, so that the same effect is achieved.
A further steam condensing and evaporating device manufactured by the steam condensing and evaporating technology, namely the application of the steam condensing and evaporating technology to a filter press, wherein the heat pump system comprises a compressor, a hot-end heat exchanger and a cold-end heat exchanger which are connected with each other; the evaporator is a box type membrane filter press, one of the membrane sheets of the filter press is a heating chamber, and the other membrane sheet is a filter cake generated after the filter pressing operation is completed. The hot end heat exchanger is connected with the hot water storage tank, the other hot water storage tank is communicated with the heating chamber of the evaporator through the circulating pump, hot water is provided into the heating chamber by the hot water storage tank, and the heat of the hot water enables the filter cake of the other heating chamber to evaporate steam; the vapor inlet of the cold-end heat exchanger is connected with the vapor outlet of the evaporator, the distillate outlet of the cold-end heat exchanger is connected with the distillate storage tank, and the top and the bottom of the distillate storage tank are respectively connected with the vacuum pump and the distillate discharge pump; the bottom of the hot water storage tank is provided with a preheater which can be heated by any one of electricity, oil, gas and steam.
The technical scheme is that the filter press is applied to the industry of the filter press, after the press operation of the filter press is finished, the filter cake is heated by the heat of hot water, the air in the filter chamber of the filter press is pumped by a vacuum pump, so that the filter chamber forms negative pressure, the liquid in the filter cake in the filter chamber is heated by the hot water, steam is generated in a low-pressure environment, and the steam is condensed into distillate through a cold-end heat exchanger, so that the filter chamber of the filter press is kept to be evaporated continuously under the negative pressure condition.
In the initial working stage after the hot water storage tank is started, the water in the hot water storage tank is required to be preheated, the preheating is stopped after the temperature reaches the set value, and the preheating is not required in the normal working process.
The beneficial effects of the invention are as follows:
1) In the process of producing the distillate, the heat released when the steam is cooled into liquid is reused for heating the liquid to be distilled, so that the energy consumption for producing the distillate is only 25-80% of that of using electricity, air energy and MVR technology to heat the distillation device, and the energy-saving effect is obvious;
2) The high-salt wastewater or the industrial mother liquor enters the dryer shell of the invention, and then the water and the volatile substances are directly evaporated to obtain fractions, and solids such as salts, slag and the like are separated and directly dried, and the high-salt wastewater or the industrial mother liquor does not scale in the evaporation drying process, and does not generate blockage caused by the production of crystals or slag, so that the dryer is obtained in two purposes;
3) The invention absorbs the heat of the steam and enters the evaporator to heat the liquid to be evaporated, rather than the liquid to be evaporated which is heated by the evaporator after being compressed like an MVR evaporation drying system, because the liquid with the same volume has more heat than the steam with the same volume, the evaporator can work in a relatively constant-temperature evaporation environment, the evaporation efficiency is higher, meanwhile, in the process of mixing steam and water, noncondensable gas can be discharged, and the evaporation efficiency is not influenced;
4) The flow direction of the materials to be dried, the high-salt wastewater or the industrial mother liquor above the annular mesh belt in the dryer shell is opposite to the flow direction of the hot water in the evaporator, namely the heated materials and the heated materials flow in the opposite direction, so that the heating and evaporating efficiency is improved, the temperature of the materials discharged by the system is reduced, and compared with an air energy dryer, the unit energy consumption is reduced by more than 50%;
5) The filter press is characterized in that the filter press is used for dehydrating materials to be filtered and filtered into a filter cake, then the filter cake is dried, filtrate is vaporized and condensed into distillate, and three tasks of filter pressing, filter cake drying and filtrate vaporization and condensation into distillate are realized.
Drawings
Fig. 1 is a schematic diagram of a heat pump system consisting of a compressor, a hot side heat exchanger and a cold side heat exchanger.
Fig. 2 is a schematic diagram of a vapor condensation evaporation technique.
Fig. 3 is a schematic view of a vapor condensing and evaporating apparatus.
Fig. 4 is a schematic diagram of a vapor condensing and evaporating apparatus for concentrating and crystallizing a liquid.
Fig. 5 is a schematic diagram of a vapor condensing and evaporating apparatus for drying material and extracting distillate.
Fig. 6 is a schematic diagram of a vapor condensing and evaporating apparatus for the integration of pressure filtration, drying and distillate extraction.
In the figure, 1-vacuum pump, 2-distillate storage tank, 3-cold end heat exchanger, 4-compressor, 5-hot end heat exchanger, 6-circulation pump, 7-evaporator, 8-preheater, 9-distillate discharge pump, 10-mother liquor replenishment control valve, 11-concentrate pump, 16-hot water inlet, 17-hot water storage tank, 27-hot water tank, 31-hot water outlet, 32-steam outlet, 33-diaphragm, 35-annular mesh belt, 37-material to be dried, 38-feed port, 39-discharge port, 41-steam inlet, 43-distillate outlet, 47-heating chamber, 61-circulation pump, 71-mother liquor replenishment inlet.
Detailed Description
Fig. 1 is a schematic diagram of a heat pump system consisting of a compressor, a hot side heat exchanger and a cold side heat exchanger. In the figure, the compressor is respectively connected with one ends of the cold-end heat exchanger and the hot-end heat exchanger, the other ends of the cold-end heat exchanger and the hot-end heat exchanger are mutually connected, and the heat pump system has the function of conveying heat at the cold-end heat exchanger to the hot-end heat exchanger.
Fig. 2 is a schematic diagram of a vapor condensation evaporation technique. The evaporator comprises an evaporator, a preheater at the bottom of the evaporator and a heat pump system, wherein the cold-end heat exchanger absorbs heat from steam evaporated from materials in the evaporator, the heat is heated by the compressor and is conveyed to the hot-end heat exchanger, the steam is condensed into distillate and discharged out of the evaporator, the hot-end heat exchanger provides heat for the materials in the evaporator, the materials are evaporated from the steam, and the preheater is electrically heated. By adopting the principle, the electric water distiller can be manufactured simply and practically.
Fig. 3 is a schematic view of a vapor condensing and evaporating apparatus. This is an applied optimization of fig. 2, where the cold side heat exchanger and the hot side heat exchanger are arranged outside the evaporator, the hot side heat exchanger is not in direct contact with the material to be evaporated, but the material is circulated between the evaporator and the hot side heat exchanger by the circulation pump 6, so that heat exchange is performed, i.e. heat flows from the hot side heat exchanger to the evaporator, and the use of the evaporator is greatly expanded. Meanwhile, a distillate outlet of the cold-end heat exchanger is connected with a distillate storage tank, and the top of the distillate storage tank is connected with a vacuum pump; the steam inlet of the cold end heat exchanger is connected with the top of the evaporator.
Fig. 4 is a schematic diagram of a vapor condensing and evaporating apparatus for concentrating and crystallizing a liquid. This is a further optimization of fig. 3, namely, on the basis of fig. 3, a distillate pump is connected to the bottom of the distillate storage tank, a mother liquor replenishment control valve is connected to the upper portion of the evaporator, and a concentrate pump is connected to the bottom of the evaporator. Thus, the distilled liquid and the concentrated liquid can be continuously produced by small improvement, and the mother liquid can be timely supplemented, so that continuous production is realized, and the method is suitable for the field of large-scale production.
FIG. 5 is a schematic diagram of a vapor condensing and evaporating apparatus for drying materials and extracting distillate, namely, the application of vapor condensing and evaporating technology to a dryer, wherein an evaporator 7 is a sealed dryer shell, a hot water tank 27 is arranged in the shell, annular mesh belts 35 are arranged on the upper surface and the lower surface of the hot water tank, the annular mesh belts can slide on the upper surface and the lower surface of the evaporator, and materials 37 to be dried can be placed on the annular mesh belts; the water inlet of the hot water tank is connected with a circulating pump 6 and a hot water storage tank 17 which are arranged outside the shell, and the water outlet of the hot water tank and the water inlet of the hot water storage tank are connected with a hot end heat exchanger 5; the steam inlet of the cold end heat exchanger 3 is connected with the right end part of the evaporator; the distillate outlet of the cold end heat exchanger is connected with a distillate storage tank, and the top and the bottom of the distillate storage tank are respectively connected with a vacuum pump and a distillate discharge pump; the bottom of the hot water storage tank is provided with a preheater which is heated by electricity.
Compared with the air energy dryer on the market at present, the air energy dryer is a dehumidifying dryer, which cools and dehumidifies the wet air in the drying box by the cold end heat exchanger of the heat pump system, so that part of water vapor in the air is condensed into water, the dehumidified low-temperature dry air is sent to the hot end heat exchanger of the heat pump system to be heated into high-temperature dry air, then the dry hot air is sent to the drying box, part of water in the dry hot air flow is changed into steam when passing through the material to be dried, air with higher moisture content is formed, and the air with higher moisture content is subjected to heat exchange and dehumidification with the cold end, so that circulation is realized.
In contrast, the advantages of fig. 5 of the present invention are:
1. the heat pump system does not need to repeatedly cool and heat air, directly heats and conveys the heat generated by condensing steam from the cold end heat exchanger to the hot end heat exchanger, heats the material to be evaporated, keeps continuous evaporation, reduces heat loss and improves efficiency; the heat pump system of the air energy dryer transmits most of energy which is not used for evaporation, but is consumed for cooling and heating of air, and the air energy dryer uses air as a medium, namely, adopts a vacuum mode for drying in a popular way, so that the drying efficiency is low. The invention adopts a mode of condensing and reducing vapor pressure to dry materials, and has high drying efficiency;
2. at present, the air energy dryer on the market can only evaporate 4 kg of water per degree of electricity, and the steam energy belt dryer manufactured by the technology can evaporate 8-12 kg of water per degree of electricity. The unit energy consumption is reduced by more than 50 percent.
Fig. 6 is a schematic diagram of a vapor condensing and evaporating apparatus for the integration of filter pressing, drying and distillate extraction, namely, the application of vapor condensing and evaporating technology to a filter press, wherein the evaporator 7 is a van type membrane filter press, one of the membrane sheets of the filter press is a heating chamber 47, and the other is a filter cake generated after the completion of the filter pressing operation. The hot end heat exchanger 5 is connected with the hot water storage tank 17 through the circulating pump 61, the other hot water storage tank 17 is communicated with the heating chamber 47 of the evaporator through the circulating pump 6, hot water is provided into the heating chamber by the hot water storage tank, and the heat of the hot water enables the filter cake in the other heating chamber to evaporate steam; the vapor inlet 41 of the cold-end heat exchanger is connected with the vapor outlet 32 of the evaporator, the distillate outlet of the cold-end heat exchanger is connected with a distillate storage tank, and the top and the bottom of the distillate storage tank are respectively connected with a vacuum pump and a distillate discharge pump; a preheater 8 is arranged at the bottom of the hot water storage tank and is heated by electricity.
In fig. 6, hot water circulates between the hot side heat exchanger and the hot water storage tank by means of a circulation pump 61, and heat is transferred from the hot side heat exchanger to the hot water storage tank. Through the circulating pump 6, the hot water circulates between the hot water storage tank and the heating chamber 47, heat is transferred from the hot water storage tank to the heating chamber 47, the heat of the hot water causes the filter cake of the other heating chamber to evaporate steam, the hot water returns to the hot water storage tank after being cooled, and the hot water is heated again by the hot end heat exchanger.
One of the working processes of the present invention, referring to fig. 1:
1. starting a preheater 8, preheating materials in the evaporator 7 to enable the temperature of the materials to rise to a preset temperature, starting a vacuum pump, pumping non-condensable gases such as air and the like, enabling steam in the evaporator to be in a low-pressure saturated state, and closing the vacuum pump;
2. starting the compressor 4, reducing the temperature of the cold-end heat exchanger, and increasing the temperature of the hot-end heat exchanger 5;
3. the materials in the evaporator are evaporated to generate steam, the steam rises to the periphery of the cold end heat exchanger 3 and is sucked into a steam inlet 41 of the cold end heat exchanger, and after being condensed into distillate, the distillate is discharged from a distillate outlet 43 to the outside of the evaporator 7 through a distillate discharge pump 9;
4. the heat absorbed by the cold end heat exchanger from the steam passes through the compressor 4, and the heat is conveyed to the hot end heat exchanger 5 for heating the materials in the evaporator;
5. after the heat pump system works normally, the preheater 8 can be turned off, and the distillate production can be completed only by the internal circulation of the heat pump system.
Second, the working process of the present invention is described with reference to fig. 4:
1. starting a preheater 8 to preheat the materials in the evaporator 7 to a preset temperature;
2. starting the compressor 4, starting the circulating pump 6, enabling materials in the evaporator to enter the hot-end heat exchanger 5, absorbing heat, and returning to the evaporator for evaporation;
3. the materials in the evaporator are evaporated to generate steam, the steam rises to enter a steam inlet 41 of the cold end heat exchanger 3, is condensed into distillate and then enters a distillate storage tank 2 from a distillate outlet 43, and a distillate discharge pump 9 and a vacuum pump 1 which are connected with the distillate storage tank 2 are respectively used for discharging non-condensable gases such as air and the like and the distillate;
4. the heat absorbed by the cold end heat exchanger from the steam passes through the compressor, and is conveyed to the hot end heat exchanger 5 to heat the materials in the evaporator which are continuously conveyed by the circulating pump 6;
5. the preheater 8 is turned off, and the distillate production can be completed by only the internal circulation of the heat pump system. The mother liquor replenishing control valve 10 and the concentrated solution pumping pump 11 which are connected with the evaporator are respectively used for replenishing materials in the evaporator and pumping out materials in the evaporator, namely the concentrated solution which is left after evaporation and meets the requirements.
If during the production process the material in the evaporator does not reach the temperature required for evaporation, due to the fact that the temperature of the surroundings of the invention is too low, etc., the preheater 8 may be turned on intermittently.
The invention has the energy-saving principle that:
the evaporation technology is different from the traditional evaporation in that liquid is separated by the technology, and steam is separated by the traditional technology through evaporation, and the technology recycles latent heat carried by the steam through a condensation method, so that energy conservation is realized.
According to the Nocardia theorem, the heat energy transmitted from the cold end to the hot end by the heat pump system doing work is related to the temperature difference between the two ends and the ambient temperature, and the capacity of the heat pump to do work and transmit the heat energy is called an efficiency coefficient, where the efficiency coefficient is K=the temperature of the hot end/the temperature difference between the cold end and the hot end, and the temperature refers to the thermodynamic temperature.
If the evaporation temperature is 60 ℃, the temperature difference between two ends is 30 ℃, namely the corresponding thermodynamic temperature of the hot end is 273+60=333K, and the temperature difference between the cold end and the hot end is 30K, the coefficient K=333/30=11, namely the heat pump consumes 1KW.H of electric energy, 11KW.H of heat energy can be transmitted from the cold end to the hot end, and therefore energy conservation is achieved.
Compared with the traditional air energy heater, the invention has the advantages that:
the air energy absorbs heat energy from the air, the heat energy in the air is relatively dispersed, the heat value is low, and the efficiency of absorbing heat energy is not high; the invention extracts heat energy from high-temperature steam, has moderate heat energy, high heat value and high efficiency, so the invention can also be called a steam energy utilization technical device, and is different from an air energy technical device.
Compared with MVR technology, the invention has the following advantages:
MVR is an abbreviation for vapor mechanical recompression technique (mechanical vapor recompression), which is an energy saving technique that reuses the energy of the secondary vapor generated by itself, thereby reducing the need for external energy. The MVR technology can also utilize the potential energy of steam to evaporate, and the principle is that the steam is firstly subjected to mechanical pressurization and temperature rise and then sent to a heating end, and after the heat energy of the steam at the heating end is transferred to the evaporated material, the steam is condensed into liquid and is discharged out of an evaporation system, and the MVR has the following defects:
1. the special steam compressor is needed, and steam can be in direct contact with the compressor, so that the compressor is easy to corrode;
2. the method is characterized in that steam is pressurized firstly, so that higher negative pressure cannot be formed at the evaporation end, namely the steam pressure at the evaporation end is reduced, therefore, the evaporation temperature is generally higher, the compressor, the evaporator and related pipelines are easy to cause larger corrosion, simultaneously, the evaporated materials are easy to react at high temperature to generate byproducts, sometimes even the materials are cured, foam is easy to form in the evaporator by high temperature evaporation, the evaporated materials are mixed in the steam, and the distilled liquid contains the evaporated materials, so that the effect of effective separation cannot be achieved;
3. for materials needing high vacuum evaporation, the invention is more energy-saving, the MVR can only generate negative pressure by the suction force of the compressor, and larger energy consumption is needed, while the invention generates negative pressure by vapor condensation, and the invention only has the auxiliary function of a heat pump system, and can obtain very high negative pressure without extra energy consumption, so the invention saves energy by 30% in the aspect of low-temperature vacuum evaporation compared with the MVR, and has no three defects, thereby greatly expanding the application range.
The application cases of the invention are as follows:
the high-salt water concentration and crystallization device manufactured by the invention consumes about 50-120 ℃ of electricity per ton of distillate, and has different electricity consumption basically equivalent to MVR energy consumption according to different concentrations and different boiling points of unsaturated solution, but the cost of the device and the maintenance cost of equipment in operation are 40% lower than that of the MVR device.
The high-water-content material drying device manufactured by the invention can utilize the filter chamber of the filter press as an evaporator to directly dry and dehydrate the filter cake at low temperature, is particularly suitable for materials requiring low-temperature drying such as starch, citric acid, chemical industry and the like, integrates filter pressing and drying, reduces the labor intensity of workers, reduces the process flow, saves the cost and saves the investment. The cost of evaporating one ton of water is only 120-150 ℃, and the electricity is saved by 50% compared with the common drying device.
In addition, the traditional belt type, disc type and blade type dryers can be used as the evaporator of the invention, and can be used for drying special materials such as sludge, and the blade type dryer can be used as the evaporator of the technology, so that the external steam is not consumed, the power consumption per ton of water evaporated is about 90 degrees, the drying temperature is 60 ℃, and the comprehensive energy saving is 30-40%.
The invention has the main application fields:
first, the form of the liquid-phase separator is applied to the concentration and distillation of liquid, and can use very low temperature difference;
the drying agent is applied to low-temperature drying of grains, vegetables, dried fruits, food and the like, and can also be used for drying and dewatering of sludge and the like;
thirdly, the filter press is combined, and the filter cake is directly dried.
Claims (1)
1. The vapor condensing and evaporating device condenses vapor evaporated from materials in a closed evaporator into distillate, discharges the distillate out of the evaporator, reduces vapor pressure in the evaporator, heats the materials in the evaporator through a heat pump system by heat released during vapor condensing into the distillate, maintains the continuous evaporation process, and realizes low-energy-consumption evaporation and separation of the distillate;
the heat pump system comprises a compressor, a hot-end heat exchanger and a cold-end heat exchanger which are connected with each other; the cold end heat exchanger absorbs heat from steam evaporated from materials in the closed evaporator, the heat is warmed up through the compressor and is conveyed to the hot end heat exchanger, and meanwhile, the steam is condensed into distillate and discharged out of the evaporator; the hot end heat exchanger provides heat for the material to be evaporated in the closed evaporator, so that the material is evaporated to steam; a preheater is arranged at the bottom of the evaporator, and the preheater is heated by any one of electricity, oil, gas and steam;
the distillate outlet of the cold-end heat exchanger is connected with a distillate storage tank, and the top of the distillate storage tank is connected with a vacuum pump; the steam inlet of the cold end heat exchanger is connected with the top of the evaporator; the evaporator is connected with the hot end heat exchanger through a circulating pump;
the bottom of the distillate storage tank is connected with a distillate pump; the method is characterized in that: the evaporator is a van-type membrane filter press, one of membrane sheets of the filter press is a heating chamber, and the other membrane sheet is a filter cake generated after the filter pressing operation is completed; the hot end heat exchanger is connected with the hot water storage tank, the other hot water storage tank is communicated with the heating chamber of the evaporator through the circulating pump, hot water is provided into the heating chamber by the hot water storage tank, and the heat of the hot water enables the filter cake of the other heating chamber to evaporate steam; the vapor inlet of the cold-end heat exchanger is connected with the vapor outlet of the evaporator, the distillate outlet of the cold-end heat exchanger is connected with the distillate storage tank, and the top and the bottom of the distillate storage tank are respectively connected with the vacuum pump and the distillate discharge pump; the bottom of the hot water storage tank is provided with a preheater, and the preheater is heated by any one of electricity, oil, gas and steam.
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| CN108905254B (en) * | 2018-09-25 | 2023-08-25 | 江西中医药大学 | Traditional Chinese medicine concentration device and traditional Chinese medicine concentration process |
| CN109453531A (en) * | 2019-01-06 | 2019-03-12 | 杭州安永环保科技有限公司 | A kind of high efficient cryogenic energy saving evaporator |
| CN109824105A (en) * | 2019-03-28 | 2019-05-31 | 上海济俭工业设备有限公司 | A kind of vacuum heat pump distillation and concentration system |
| IT201900007257A1 (en) * | 2019-05-27 | 2020-11-27 | Meg Srl | PROCESS OF WASHING INDUSTRIAL ITEMS IN GENERAL SUCH AS PRECISION SMALL PARTS, MECHANICAL PARTS, PRINTED CIRCUITS, LENSES, WATCHES, JEWELERY, GLASSES OR OTHER PLANT IMPLEMENTING THIS PROCESS |
| CN110339584A (en) * | 2019-08-23 | 2019-10-18 | 刘小江 | Negative pressure Low Temperature Thermal pump-type enrichment facility |
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