CN110090467A

CN110090467A - A kind of vacuum sublimation evaporation is cold and hot can separation method and device

Info

Publication number: CN110090467A
Application number: CN201810949355.3A
Authority: CN
Inventors: 武伟
Original assignee: Individual
Current assignee: Individual
Priority date: 2018-06-22
Filing date: 2018-08-20
Publication date: 2019-08-06
Also published as: CN209060589U

Abstract

The present invention provides a kind of cold and hot energy separation method of vacuum sublimation evaporation, is: establishing vacuum environment in an artificial environment, enables into wherein liquid a part and be evaporated to steam, a part is solidified as solid, and a portion solid can also distil as steam；Then steam and solid are separated, solid or solidliquid mixture are exported as cold energy, and steam is exported as thermal energy, this process is carried out continuously, and realize the separation of cold energy and thermal energy.The present invention utilizes the physical property of vacuum technique and water, realizes cold energy and thermal energy separation and further stores and use, and can greatly improve system effectiveness and COP value on the basis of existing refrigeration, heating technology.The present invention also provides the devices used in the method.

Description

Vacuum sublimation evaporation cold and heat energy separation method and device

Technical Field

The invention belongs to the technical field of refrigeration and heat pumps, and provides a method for separating cold energy and heat energy by adopting a vacuum sublimation evaporation method. The invention also provides a device used in the method.

Background

The refrigeration or heating technology is a unit operation belonging to a thermodynamic process, which is to cool or heat an object or object in a certain time and a certain space by a manual method to make the temperature of the object or object lower than the ambient temperature or higher than the ambient temperature, i.e. to transfer heat from a low-temperature object to a high-temperature object by adding energy to the refrigeration or heating equipment. The refrigeration or heating technology applied in the prior art is an operation technology which utilizes a compressor to do work to enable a medium in refrigeration or heating equipment to be boosted and then decompressed, so that cold and heat energy is absorbed and released and transferred to a use place.

At present, the refrigeration and heating are based on the compressor technology to realize the transfer and use operation of cold and heat energy, and the refrigeration energy efficiency ratio (COP value for short) of the compressor refrigeration equipment is about 6 for a long time due to the limitation of the equipment principle and the working environment. Domestic air conditioners with primary energy consumption in China have COP of about 3.4, and although foreign reports show that refrigerating units with COP more than 6 and less than 8 are provided, the equipment cost is low because the actual efficiency improvement range is not large enough due to high equipment cost.

The high energy consumption of the existing refrigeration and heating technology enables the centralized air conditioner to become a large power consumer, and greatly increases the load pressure of the summer national grid peak period; and in winter, the heating only can be realized by burning coal due to relatively high electric charge, so that the air pollution is increased. In order to control the atmosphere, the nation carries out coal gas change, but the popularization has certain difficulty due to the problems of tight natural gas resource supply, higher price and the like.

The problem that energy saving and consumption reduction are needed to be achieved by seeking a low-energy-consumption technology to partially replace the traditional compressor refrigeration and heating technology is at present urgently solved.

Disclosure of Invention

The invention aims to provide a cold and heat energy separation method for vacuum sublimation evaporation, which utilizes the vacuum technology and the physical properties of water to realize the separation of cold energy and heat energy and further storage and use, and can greatly improve the system efficiency and COP value on the basis of the existing refrigeration and heating technology.

It is another object of the present invention to provide an apparatus for use in the above cold-heat energy separation method.

The purpose of the invention is realized as follows:

a cold and heat energy separation method of vacuum sublimation evaporation is carried out in a device which comprises an artificial environment, namely a sealed container, wherein the container is provided with a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet;

the separation method comprises the following steps:

step 1: establishing a vacuum environment in the artificial environment, the vacuum environment being: letting the artificial environment liquid enter from the liquid inlet:

wherein a portion evaporates and a portion solidifies as a solid, or,

wherein one part is evaporated, one part is solidified into solid, and the other part is sublimated into steam;

simultaneously and/or before and/or after, introducing a liquid into the artificial environment through the liquid inlet;

step 2: separating the steam from the solid, starting a stirring device to crush the solidified solid, discharging the solid or the mixture of the solid and the liquid from the solid or solid-liquid mixture outlet to form cold energy output, and pumping the steam from the gas outlet by a vacuum sublimation evaporation unit to form heat energy output;

and (3) alternately and/or simultaneously performing the step (1) and the step (2), so that liquid enters the container, solid or solid-liquid mixture is discharged from a solid or solid-liquid mixture outlet, steam is extracted from a gas outlet, and the process is continuously performed to realize the separation of cold energy and heat energy.

Further, the method provided by the invention also comprises the following step 3: the solids or solid-liquid mixture is discharged from the vessel to a solids storage tank at the same pressure as the vessel.

Preferably, the stirring device is started in step 1.

Specifically, the artificial environment has a pressure of 600Pa or less.

Further, the temperature in the artificial environment is 272K or less.

Preferably, the pressure of the artificial environment is 600-100 Pa.

Further, the temperature in the artificial environment becomes 272 and 253K.

Further, the stirring device arranged in the container is used for stirring in the step 2, so that the solid in the container can not seal the whole liquid level, and the solid is crushed and discharged from the solid or solid-liquid mixture outlet.

The apparatus used in the method is such that: the device comprises a sealed container, wherein a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet are formed in the container, a vacuum sublimation evaporation unit is connected to the gas outlet to provide set pressure for the sealed container, and a stirring device is arranged in the container.

Preferably, the stirring paddle in the stirring device is located at the set liquid level in the vessel or at a height within 50mm below the set liquid level.

The solid storage tank is communicated with the container to form the same pressure as the container, a solid or solid-liquid mixture outlet in the container is communicated with an inlet on the solid storage tank, and a stopping device is arranged between the solid storage tank inlet and the solid or solid-liquid mixture outlet of the container to enable the solid storage tank inlet and the solid or solid-liquid mixture outlet to be communicated or stopped; the solid storage tank is provided with a solid matter or solid-liquid mixture discharge port, and is also provided with a vent communicated with the atmosphere, and the vent is provided with a vent valve.

Furthermore, a communication pipeline is arranged between the solid storage tank and the container, and a conveying device is arranged on the communication pipeline.

The transport device is preferably a slurry pump.

Furthermore, the air suction port of the vacuum sublimation evaporation unit is respectively connected with the gas outlet of the container and the gas outlet on the solid storage tank, so that the same pressure is formed by the action of the same vacuum sublimation evaporation unit, namely a multi-stage vacuum pump unit, on the container and the solid storage tank.

Furthermore, the exhaust port of the vacuum sublimation evaporation unit is connected with a gas inlet of a steam heat exchanger for exchanging heat with the extracted steam, and the heat energy of the steam which is extracted from the container and is raised in temperature after being boosted is used for heating the low-temperature medium.

And a vacuum pump is connected to a gas outlet of the steam heat exchanger and used for pumping the steam subjected to heat exchange out of the steam heat exchanger.

The vacuum sublimation evaporation unit is a multistage vacuum pump, preferably a roots vacuum pump unit.

The container may be a crystallizer configured to: the crystallizer is a tank body, a basin-shaped clapboard which comprises a lower bottom and side walls is arranged in the tank body to form a crystallization tray, the crystallization tray divides the inner space of the tank body into an upper space and a lower space, a gas outlet is arranged on the tank wall at the top of the tank body and is connected with a vacuum sublimation evaporation unit through a pipeline; the stirring device hermetically penetrates into the crystallizing disc arranged in the upper space from the top of the tank body; a liquid conveying pipe connected with the liquid inlet is hermetically inserted into the tank body from the side wall of the lower space of the tank body and then communicated with the inside of the crystallization tray from the position below the side wall of the crystallization tray; the lower bottom of the crystallizing pan is provided with a waste water outlet which is connected with a waste water discharge pipe, and the waste water discharge pipe extends downwards and penetrates out of the tank body from the bottom of the tank body in a sealing way. The bottom of the crystallizing tank is also provided with a discharge port for discharging waste water in the lower space; the part of the crystallization plate close to the upper part of the side wall is provided with an ice outlet, and the side wall of the lower space of the tank body is provided with a solid-liquid mixture outlet.

The structure of the container can also be as follows: the container is a crystallizer and has the structure that: the crystallizer is a tank body, the gas outlet is arranged on the tank wall at the top of the tank body and is connected with the vacuum sublimation evaporation unit through a pipeline; the stirring device penetrates into the tank body from the top of the tank body in a sealing way; the liquid inlet is arranged on the side wall of the tank body, the side wall of the tank body is provided with a solid or solid-liquid mixture outlet, and the liquid inlet is lower than the solid-liquid mixture outlet; the bottom of the crystallizing tank 4 is provided with a discharge port for discharging waste water in the lower space.

The stirring paddle in the stirring device is positioned at the set liquid level in the crystallization tray or at the height within 50mm lower than the set liquid level; or the stirring paddle in the stirring device is positioned at the set liquid level in the crystallization tank or at the height within 50mm below the set liquid level.

The invention provides a cold and heat energy separation method by vacuum sublimation and evaporation, which is a technology for separating, storing and using cold energy and heat energy by utilizing a vacuum technology and the physical properties of water. Due to the adoption of the efficient vacuum sublimation evaporation technology different from the compressor technology, on the premise of not using other refrigeration media and a matched refrigeration medium circulating system, the link of energy transfer is reduced, the system efficiency is improved, the COP value can be greatly improved, and the larger the refrigeration or heating quantity is, the larger the COP value is, so that the COP value can break through 8 and even can reach more than 20. Meanwhile, the invention uses the phase-change substances (steam and ice) of the liquid as the carrier of the energy and the medium for storing and applying, so that the separation and the use of the cold and hot energy are more convenient, and the efficiency is greatly improved. Thereby greatly improving the overall efficiency of the system.

The invention is further illustrated by the figures and examples.

Drawings

Fig. 1 is a schematic structural diagram of a device used in the vacuum sublimation evaporation cold and heat energy separation method provided by the invention.

FIG. 1a is a schematic structural diagram of the crystallizer in FIG. 1.

FIG. 1b is a schematic view of a crystallizer of another construction.

Fig. 2 is a schematic diagram of a control system of the device used in the vacuum sublimation evaporation cold-heat energy separation method provided by the invention, and the flow running directions of various fluids in the device shown in fig. 1 are also shown in fig. 2.

FIG. 3 is an equilibrium phase diagram of water.

Fig. 4 is a graph showing a relationship between operating conditions and COPs, in which COP conditions in the conventional compression refrigeration or heating are shown, in which the abscissa is a state point where the temperature difference between the artificial environment and the fluid is different, and the ordinate is a COP value corresponding to each state point.

FIG. 5 is a graph of operating conditions versus COP showing the COP status of the method of the present invention during cooling or heating.

Detailed Description

As an example of the method for separating cold and heat energy by vacuum sublimation and evaporation provided by the present invention, an apparatus as shown in fig. 1 and fig. 1a is given.

The device is a sealed container called a crystallizer 4, an artificial environment is formed in the crystallizer 4, a liquid inlet 44, a gas outlet 42 and a solid-liquid mixture outlet 49 are arranged in the crystallizer 4, a vacuum sublimation evaporation unit 2 is connected to the gas outlet 42, and a stirrer 43 is also arranged in the crystallizer 4. The separation method comprises the following steps:

step 1: a vacuum artificial environment is established in the crystallizer 4, and a vacuum is pumped into the crystallizer 4 through a vacuum sublimation evaporation unit, namely a vacuum pump unit 3 connected with a gas outlet 42 on the crystallizer 4, so that the pressure in the crystallizer 4 is reduced to 600-100Pa, for example 128Pa, and raw water is input into the crystallizer 4 through a liquid inlet 44. Under the working condition of the vacuum environment, as can be seen from a water equilibrium phase diagram shown in fig. 4, water is in a triangular area formed by a gas-solid equilibrium line and b-a-o, the temperature of the crystallizer 4 is in the area, and the temperature can be reduced from 272 to 253K, namely from minus 1 ℃ to minus 20 ℃, namely in a gas-solid two-phase area and is deviated from a gas-phase area. In such an artificial environment, a part of the water will evaporate into steam, which is pumped away by the vacuum pump unit 3, a part of the water will freeze into ice, a part of the ice will also become steam by sublimation, and at the same time, a certain amount of water will remain.

Step 2: the vapor and the ice are separated, the condensed ice is broken by the stirrer 43 arranged in the crystallizer 4, the ice and part of water form ice slurry, the ice slurry is discharged from the solid-liquid mixture outlet 49 to be output as cold energy, and the vapor is pumped out of the artificial environment from the gas outlet 42 by the vacuum sublimation evaporation unit to be output as heat energy. The stirrer has two functions, one is to ensure that the ice in the container can not seal the whole liquid level to ensure the evaporation and sublimation speed of solid and liquid on the liquid level, and the other is to guide the cold energy in the artificial environment above the liquid level of the crystallizer into the liquid to accelerate the icing. For this purpose, the stirrer can be started in step 1.

At the beginning, liquid can be added into the crystallizer 4, then the vacuum pump unit 3 is started, then the liquid starts to evaporate, steam is pumped away, freezing starts, the stirrer can be started from the beginning, cold energy above the liquid level in the crystallizer 4 is led into the liquid, the condensed ice is broken by slurry of the stirrer along with the freezing of the liquid surface, the ice is discharged from the solid-liquid mixture outlet 49, and meanwhile, raw water also continuously enters the crystallizer.

Thus, the steps 1 and 2 are alternately and simultaneously carried out, water and water continuously enter the crystallizer, the vacuum pump unit 3 which is a vacuum sublimation evaporator for maintaining the ambient pressure in the crystallizer 4 continuously pumps steam out of the gas outlet 42, and ice slurry continuously discharges out of the solid-liquid mixture 49 outlet, thereby realizing the continuous separation of cold energy and heat energy.

The invention relates to a technology for separating and utilizing cold energy and heat energy by using a high-efficiency vacuum sublimation evaporation unit. Is a new technology application based on the second law of thermodynamics.

As can be seen from fig. 3, when the pressure in the artificial environment, i.e. the space in which the water is located, is reduced from 101.3KPA (atmospheric pressure) to below 128PA, the equilibrium point of the vaporization temperature of the water will move down along the gas-liquid (C-O) line, the triple point (O point), and the gas-solid (O-A) line. I.e. from 373K to below 253K (from 100 c to below-20 c).

In order to realize the separation of cold energy and heat energy and facilitate the utilization, the method of the invention is to extract heat energy in the form of steam, and separate and store cold energy in the form of ice. The process interval is as follows: temperature: 272K-253K (or below) (see lines a-b in fig. 3), pressure: 600 Pa-100 Pa (see o-a in FIG. 3). As can be seen from the water equilibrium phase diagram shown in FIG. 3, this region is a solid-gas two-phase region. And the gas phase zone is a closed triangular area of o-a-b-o. In this region, the solid form of water (ice) can sublimate directly into vapor. Since the pressure is much lower than the saturation vapor pressure of liquid water (see table 1), the surface layer of water can still exist in liquid form in non-equilibrium state and can be directly changed into vapor by evaporation. The vapor sublimed from the ice and the vapor evaporated from the water are pumped through a vacuum unit and the ice slurry is pumped through an ice slurry pump. The separation and the transmission of cold and hot energy are realized.

Table 1: temperature and saturated vapor pressure of water

The invention can break through the bottleneck that the efficiency of the heat pump and the refrigeration system based on the gas compression technology is lower at present, and the energy consumption ratio of the existing mainstream technology is lower than the limiting value of COP (coefficient of performance) less than 8, and is improved by times. The reason was analyzed as follows:

from the second law of thermodynamics, the entropy increase of an ideal refrigeration cycle is equal to zero, i.e., Qa/Ta-Q0/Tc. (Qa is an ambient heat transfer amount; Q0 is a heat transfer amount of a target fluid; Ta is an ambient temperature; Tc is a temperature of the target fluid), and Q0+ W is substituted into Qa to obtain (Q0+ W)/Ta (Q0/Tc), and Q0/W (1/(Ta/Tc-1) ═ epsilon c, epsilon c is called a refrigeration coefficient, and the coefficient is the same as an energy efficiency ratio COP known in the industry. As can be seen from the equation, the cooling capacity and the input power are only related to the target fluid temperature Tc and the ambient temperature Ta. Using the above formula, it can be found by calculation that Ta/Tc is 2 when the ambient temperature Ta is 35 ℃, Tc is-119 ℃. In this case, the cooling capacity is equal to the power, that is, ∈ c is equal to 1, or the energy efficiency ratio COP is equal to 1. When the temperature difference Ta-Tc begins to decrease, the COP value begins to be > 1. Since COP is 1/(Ta/Tc-1), the COP value shows an accelerated rising trend as the temperature difference decreases. As shown in fig. 4, a graph of COP data is cut from Ta-Tc 44 ℃, to Ta-Tc 1, starting with Ta-Tc 44 ℃.

The relationship between COP and Ta-Tc at 35 ℃ is as follows:

the COP value shows an accelerated increase with decreasing temperature difference (approximately abscissa of the point on the flat line). (the abscissa is the number of sequences and the ordinate is the COP number)

Taking the current mainstream compression technology as an example, when the ambient temperature is Ta-35 ℃ and the target temperature Tc at the refrigeration end is 0 ℃, the Ta-Tc at this time is 35 ℃, and the COP value can reach 7.8 (see the point 10 on the abscissa in the figure corresponds to the value on the ordinate). In actual use, the temperature difference requirement of heat transfer needs to be considered, the heat transfer temperature difference is set to be 5 ℃, and the temperature of the refrigerating end needs to reach minus 5 ℃ at the moment, so that the use requirement can be met. At this time, Ta-Tc is 40 ℃, and the COP value can only reach 6.7 (see the abscissa point 5 in the figure, which corresponds to the ordinate value). I.e. the temperature difference is enlarged and the COP value is reduced. Considering the problem of the system efficiency coefficient, the method is consistent with the condition that the COP of the mainstream equipment in the market is less than about 6. Therefore, the energy efficiency ratio level of the compression refrigeration technology is determined by the system structure; the limitation of the environmental temperature and the use requirement, and the large breakthrough is impossible.

Taking the embodiment of the present invention as an example, by applying the above principle and calculation formula, it can be found through calculation that when the ambient temperature Ta is 272K and the temperature difference Ta-Tc between the ambient temperature Ta and the temperature Tc of the surface of the ice water in the crystallizer, which is the target fluid, is 10 degrees, the liquid radiates heat to the environment, and ice is formed. Refrigerating capacity is greater than power. The COP value is then up to 26 (see point 30 on the ordinate). Since in the present invention the working environment, i.e. the artificial environment, is highly coincident with, i.e. in one space, the space in which the target fluid, i.e. the water in the crystallizer, is located. Therefore, the temperature difference between the ambient temperature and the target fluid can be controlled within a narrow range. According to the second law of thermodynamics, COP values can reach very high levels.

It can be understood that the compression refrigeration and heating in the prior art is a natural process of forcibly moving heat from a low temperature to a high temperature, and the method provided by the invention is a natural process of vacuumizing the environment, and the liquid in the environment can be obtained under a certain vacuum pressureNature of natureEvaporating and solidifying, and the solidified solid can be sublimated to generate vapor. The generated steam and the generated solid are respectively removed from the environment, ice is cold energy and can be used, and the temperature is increased after the steam is boosted and can be used as heat energy. The energy consumed in the process is only to form a vacuum environment with set pressure and to break the solid out. Therefore, the energy consumption is necessarily small, and the COP value is high!

Fig. 5 is a graph of COP data starting with Ta-Tc 39 ℃ (Tc 234K), COP 6, and Ta-Tc 1 ℃ when Ta is 0 ℃. The graph of COP vs. Ta-Tc at 0 ℃ is shown in fig. 5:

when Tc is 263K, i.e., -10 degrees (point 30 corresponds to a value on the ordinate), COP is 26.3.

The superiority of the present invention will be described below by calculating the data of one experiment and the mass production efficiency.

The experiment adopts a method for calculating the yield and energy consumption of industrial production scale according to a class-specific method by taking laboratory conditions and small experimental equipment data as starting points, and partially replaces a pilot plant test. But all process parameters will be based on pilot plant data.

Table 1 shows experimental data on the brine state and the final evaporation amount in relation to the icing amount (capacity) at each stage of the vacuum pumping of experiment 1.

TABLE 1

Table 2 shows experimental data on the brine state and the final evaporation amount in relation to the icing amount (energy production) at each stage of the evacuation in experiment 2.

TABLE 2

The experiment was carried out in a 4L/s vacuum apparatus, and the sublimation evaporation amounts in 2 minutes after the start-up were 39.6g and 38.65g, respectively. The ice making amounts were 263.86g and 226.23g, respectively, with an average of 245 g. The ratio of the ice making amount to the evaporation amount was 6.66 and 5.85, respectively. As the evaporation heat of water at 0 ℃ is 2501KJ/Kg, the water at 0 ℃ is formed into ice at 0 ℃, and the heat quantity to be released is as follows: 334.4KJ/Kg, the evaporation heat is about 7.48 times of the latent heat of icing. The ratio of vaporization heat absorption to freezing latent heat in the experimental result is very close to 6.25 in consideration of the loss of cold energy by the experimental equipment. Namely, every time 1Kg of water vapor is pumped away, 7.48Kg of ice can be frozen

The comparison of the energy efficiency ratio of the equipment in the prior art:

the ice making machine can make 15Kg of ice per hour according to 250g of ice making per minute by a vacuum equipment experiment of 4L/s (power of 0.55 KW). According to 1KWH 1000w 3600s 3600000J, 334400KJ (i.e. 92.89KWH) of cold energy is required for freezing 1 ton of ice. The experimental device consumes 36.67KWH per ton of ice, and the COP value reaches 2.53 (namely 92.89/36.67 is 2.53). Has energy efficiency ratio equivalent to that of the ice slurry equipment matured on the market. Taking an SF100 ice slurry machine produced by a certain factory as an example, the unit yield of the machine is 28 times that of the experimental equipment (420Kg/15Kg is 28), but the efficiency is calculated according to the installation power, and the COP is only 1.94. The COP, as calculated by the operating power, also reached only 2.76, which is close to the experimental data.

The parameters of the ice slurry machine produced by a certain plant are shown in the table 3:

TABLE 3

The parameters of the ice cube machine produced by a certain factory are shown in a table 4: (efficiency is much lower than ice slurry machine)

TABLE 4

On the basis of the two experiments, if the air extraction amount of the vacuum unit is increased by 2500 times, ice can be made by more than 37.5 tons per hour. The installation capacity of the unit is 135KW, and the following are calculated: the ice consumption per ton is 3.6 degrees, the COP value can reach at least 26, and the COP value is improved by more than 5 times compared with the prior compressor technology.

Calculating the air extraction efficiency of the vacuum unit:

the efficiency of ice production mainly depends on the air extraction efficiency of the vacuum unit. Comparison was also carried out with an extension of the vacuum unit of 4L/s (power 0.55KW) by 2500 times (power 135KW), the calculation results being shown in Table 5:

TABLE 5

The calculation method was substantially the same as the calculation method described above (COP 26). From another perspective, it is demonstrated that system efficiency can be improved by scaling up the vacuum unit. In fact, the experimental vacuum pump is different from a large-scale vacuum unit in form, so that the equipment efficiency of large-scale production is greatly improved.

One specific operation is: firstly, the vacuum degree required by the vacuum evaporation working environment is 600-100Pa in the water crystallizer. Part of low-temperature raw material water in the water crystallizer is evaporated, water vapor takes away heat, and part of residual water begins to freeze into ice. Along with the increase of the vacuum degree according to the technological requirements, the pressure in the working space of the water crystallizer is continuously reduced according to the technological parameter requirements, and the pressure enters into an ice sublimation area, namely a normal production pressure parameter area of the process. Since ice is generated on the water surface, the sublimation reaction starts. At this time, the ice is successively discharged from the space by the stirrer in the water crystallizer. The removal of a portion of the ice layer provides conditions for continued evaporation of water beneath the ice layer, which in turn provides good heat transfer conditions for sublimation of the ice layer. At the moment, the sublimation and the evaporation are simultaneously carried out in the water crystallizer, water vapor continuously overflows and takes away a large amount of heat, and low-temperature new raw material water is continuously frozen into ice in the water crystallizer. And discharging finished ice through solid-liquid separation equipment to finish the whole ice making and steam production process.

The invention utilizes the physical characteristics of the phase change principle, the steam partial pressure and the like of water, so that the refrigeration and heating processes with large energy consumption can be carried out under the condition of relatively small energy consumption. The reason for this is that the present invention uses a way to follow the natural law to make ice and liquid water sublimate and evaporate in the environment with low steam partial pressure, i.e. high vacuum degree, and then to draw out the water vapor. Thus, the cold energy and the hot energy can be separated by using less energy. The technology heats while refrigerating, separates cold energy in the form of ice (solid state) and heat energy in the form of (gaseous) steam, and utilizes the separated cold energy and heat energy.

The ice produced can be stored as cold energy. When melting, the cold energy can be supplied as the cold energy of the centralized air conditioner. Since ice is a monomineral rock which cannot be co-located with other substances, water will automatically remove impurities during crystallization to maintain its pure characteristics (e.g. sea ice). The ice making process of the invention can also provide a new technical scheme with low energy consumption for seawater desalination, so that the seawater desalination cost is greatly reduced. Can create a new technical approach in the field of seawater desalination, and realize the low-cost wide application of the seawater desalination technology.

An embodiment of the structure of a crystallizer is provided as shown in fig. 1 and 1 a.

The structure of the crystallizer 4 is: the crystallizer 4 is a tank body, a basin-shaped clapboard comprising a lower bottom and a side wall is arranged in the tank body to form a crystallization tray 41, the crystallization tray 41 divides the inner space of the tank body into an upper space and a lower space, a vacuumizing interface 42 is arranged on the tank wall at the top of the tank body, and the multi-stage Roots vacuum pump 3 is connected through a pipeline. The stirrer 43 penetrates hermetically into the crystallization tray 41 placed in the upper space from the top of the tank at a level at or below 50mm in the crystallization tray 41; a liquid feed pipe 45 connected to the liquid inlet 44 is sealingly inserted into the tank from the side wall of the lower space of the tank, and is communicated with the inside of the crystallization tray 41 from a position below the side wall of the crystallization tray 41. Introducing raw water into the crystallization tray 41; a waste water outlet 46 is arranged on the lower bottom of the crystallizing pan 41, a waste water discharge pipe 47 is connected with the waste water outlet 46, the waste water discharge pipe 47 extends downwards and penetrates out of the tank body from the bottom of the tank body in a sealing way. A drain port 47a is further provided at the bottom of the crystallization tank 4 for discharging waste water in the lower space.

An ice outlet 48 is arranged at the upper part of the side wall of the crystallizing disc 41, the crushed ice is communicated with ice slurry mixed by part of water to fall into the lower space of the tank body from the ice outlet, and the ice slurry is discharged out of the tank body from an ice slurry outlet 49 arranged on the side wall.

The tank body is also provided with a viewing hole 40.

Also included is an ice slurry reservoir 6, the ice slurry reservoir 6 being in communication with the crystallizer 4 such that the pressure in the reservoir 6 is opposed to the pressure in the crystallizer 4. A stop valve 61 is arranged on the ice slurry inlet of the ice slurry storage tank. In this embodiment, the vacuum pumping port 62 formed at the top of the ice slurry storage tank 6 is also connected to the vacuum pump unit 3 of the multi-stage roots vacuum pump, so that the pressure in the ice slurry storage tank 6 can be easily equalized to the pressure in the crystallization tank 4. And a slurry pump 5 is arranged on a pipeline arranged between the ice slurry storage tank and the crystallizer 4, and drives the ice slurry to enter the ice slurry storage tank 6 from the crystallizer 4. An air release valve 63 is also provided at the top of the ice slurry tank 6 so that the ice slurry tank can be vented to the atmosphere. The bottom of the ice slurry storage tank 6 is provided with an ice slurry discharge port 64. In practical use, the ice continuously condensed in the crystallization tray 41 in the crystallizer 4 is broken by the stirrer 43, the ice slurry falls into the lower space, the slurry pump 5 is sent into the ice slurry storage tank 6, after the ice slurry storage tank 6 is full, the stop valve 61 is closed, the emptying valve 63 is opened, so that the pressure in the ice slurry storage tank 6 is balanced with the atmospheric pressure, then the valve on the lower ice slurry discharge port 64 is opened, the ice slurry is discharged, and then the ice and the water can be separated. Solid ice was obtained. One crystallizer 4 may be connected in parallel with several ice slurry storage tanks 6, and when one ice slurry storage tank 6 discharges ice slurry, the other ice slurry storage tank is opened, so that the process of the crystallizer 4 can be continuously performed.

Of course, several crystallizers can be arranged to form a system to increase the output of the cold and heat energy separation.

The device can also comprise two heat exchangers, wherein one heat exchanger is a steam heat exchanger 2 utilizing steam heat energy, and the other heat exchanger is a raw water heat exchanger 2' for pre-cooling raw water entering the crystallization tank 4 to ensure that the temperature of the raw water is reduced to 1-4 ℃.

When the device is used, raw water passes through a raw water heat exchanger 2', ice water in the ice slurry discharged is utilized to cool the raw water to 1-4 ℃, the cooled raw water enters the lower space of the crystallization tank 4 and then enters the crystallization disc 41, ice which is formed under high vacuum degree is broken through the stirrer 43, water-containing broken ice is discharged to the lower space of the crystallization tank 4 from an ice outlet 48 on the upper side wall of the crystallization disc 41 and then is conveyed to the ice slurry storage tank 6 from an ice slurry outlet 49 through the slurry pump 5, and the ice slurry is output from the ice slurry storage tank 6 as cold energy for use. The crystallization tank obtains set pressure through the suction of the multistage Roots vacuum pump 3, meanwhile, the pumped steam is conveyed into the steam heat exchanger 2, after the pressure is increased, the temperature of the steam rises, and the steam exchanges heat with the heating water at 25 ℃ in the heat exchanger 2, so that the temperature of the heating water can be raised to about 70 ℃, and therefore heat energy is output. The steam at the outlet of the steam channel of the steam heat exchanger 2 is pumped out by another vacuum pump 1 and discharged to the atmosphere.

As shown in fig. 1b, the crystallizer may also be of a construction that eliminates the crystallization disk 41 and associated structure in the crystallizer 4 shown in fig. 1 and 1 a. The crystallizer 4 is an integral space, in the crystallizer 4' shown in fig. 1b, the liquid inlet 44 is lower than the ice slurry outlet 49, and the ice slurry outlet 49 is within 50mm below the set liquid level. The stirring blade 43 is preferably positioned such that half of it is above the liquid surface and the other half is below the liquid surface. The design can make the function of the stirrer well played.

The crystallizer shown in fig. 1b is suitable for pure water or a liquid with less impurities, because such a liquid is hard to freeze during the separation of cold and heat energy, and the ice slurry is easier to discharge in the crystallizer with such a structure. The crystallizer shown in fig. 1a is suitable for liquid with high impurity content, such liquid is soft ice, the ice slurry is generally like soft mud, and the crystallizer with a crystallizing disc is used, and the soft mud ice slurry is conveniently dropped from the crystallizing disc to the lower space, separated from the liquid and then discharged from an ice slurry outlet.

The vacuum sublimation evaporation cold and heat energy separation device provided by the invention also comprises a centralized control system, as shown in fig. 2, the centralized control system controls the operation of the following devices: 1. the vacuum sublimation evaporation unit, namely the opening and closing of a multi-stage Roots vacuum pump, controls the pressure in the crystallizer at a speed, 2, the opening and closing and the rotating speed of a stirrer in the crystallizer, and also controls the opening and closing and the opening degree of valves on each inlet and outlet, and 3, the opening and closing and the opening degree of valves on each inlet and outlet on the ice slurry storage tank. The larger arrows in fig. 2 show the control relationship of the centralized control system to each part of the plant, and the smaller arrows show the direction of logistics in the plant.

The embodiment shows that the hot water with the temperature of 60-70 ℃ can be directly produced by the output heat energy of the method, namely the steam pumped by the multi-stage Roots vacuum pump, and about 2 tons of hot water with the temperature of 60 ℃ can be produced when 1 ton of ice is produced. If only according to the actual refrigeration COP of the technology being 12, the electricity consumption is less than 7.75 degrees per 1 ton of ice produced, and the refrigeration energy consumption is reduced by at least half. With the addition of hot water produced, the total energy consumption can be reduced by 75%, namely 25% of the energy consumption when the COP is 6 (and the COP value of the ice machine sold on the market at present is generally lower than 3). Can provide centralized heating and bathing hot water in a certain range.

The invention has obvious energy-saving effect and great development potential. The COP of the equipment refrigeration can be more than 12 or even higher. In addition, the equipment cost of the invention is lower, and the equipment investment recovery period is greatly shortened.

Claims

1. A cold and heat energy separation method of vacuum sublimation evaporation is carried out in a device which comprises an artificial environment, namely a sealed container, wherein the container is provided with a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet;

the separation method comprises the following steps:

step 1: establishing a vacuum environment in the artificial environment, the vacuum environment being: letting liquid entering the artificial environment from the liquid inlet:

wherein a portion is evaporated to steam and a portion is solidified to a solid, or,

wherein a part of the vapor is evaporated into vapor, a part of the vapor is solidified into solid, and a part of the solid is sublimated into vapor;

simultaneously or before or after, introducing a liquid into the artificial environment through the liquid inlet;

step 2: separating steam and solid, starting a stirring device to crush the solidified solid, discharging the solid or the mixture of the solid and the liquid from a solid or solid-liquid mixture outlet to form cold energy output, and pumping the steam from a gas outlet by a vacuum sublimation evaporation unit to form heat energy output;

2. The method of claim 1, wherein: the pressure of the artificial environment is below 600 Pa; and/or the presence of a gas in the gas,

further comprising the step 3: discharging the solid or solid-liquid mixture from the vessel to a solids storage tank isobaric to the vessel.

3. The method of claim 2, wherein: the temperature in the artificial environment is 272K or less.

4. The method of claim 2, wherein: the pressure of the artificial environment is 600-100 Pa.

5. The method of claim 4, wherein: the temperature in the artificial environment is 272 and 253K.

6. Method according to one of claims 1 to 5, characterized in that: the stirring device arranged in the container is used for stirring in the step 2, so that the solid in the container can not seal the whole liquid level, and the solid is crushed and discharged from the solid or solid-liquid mixture outlet; and/or the presence of a gas in the gas,

the stirring device is started in step 1.

7. Apparatus for use in a method according to one of claims 1 to 6, characterized in that: the device comprises a sealed container, wherein a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet are formed in the container, a vacuum sublimation evaporation unit is connected to the gas outlet to provide set pressure for the sealed container, and a stirring device is arranged in the container.

8. The apparatus of claim 7, wherein: the solid storage tank is communicated with the container to form the pressure equal to that of the container, a solid or solid-liquid mixture outlet in the container is communicated with an inlet on the solid storage tank, and a stopping device is arranged between the solid storage tank inlet and the solid or solid-liquid mixture outlet of the container to enable the solid or solid-liquid mixture outlet and the solid storage tank to be communicated or stopped; the solid storage tank is provided with a solid matter or solid-liquid mixture discharge port, a vent port communicated with the atmosphere and a vent valve;

and/or the presence of a gas in the gas,

the stirring paddle in the stirring device is positioned at the set liquid level in the container or at the height within 50mm lower than the set liquid level; and/or the presence of a gas in the gas,

the exhaust port of the vacuum sublimation evaporation unit is connected with a gas inlet of a steam heat exchanger for exchanging heat with the extracted steam, and the heat energy of the steam extracted from the container and heated after being boosted is used for heating the low-temperature medium; and/or the presence of a gas in the gas,

the vacuum sublimation evaporation unit is a multi-stage Roots vacuum pump; and/or the presence of a gas in the gas,

the container is a crystallizer and has the structure that: the crystallizer is a tank body, a basin-shaped clapboard which comprises a lower bottom and side walls is arranged in the tank body to form a crystallization tray, the crystallization tray divides the inner space of the tank body into an upper space and a lower space, a gas outlet is arranged on the tank wall at the top of the tank body and is connected with a vacuum sublimation evaporation unit through a pipeline; the stirring device hermetically penetrates into the crystallizing disc arranged in the upper space from the top of the tank body; a liquid conveying pipe connected with the liquid inlet is hermetically inserted into the tank body from the side wall of the lower space of the tank body and then communicated with the inside of the crystallization tray from the position below the side wall of the crystallization tray; a waste water outlet is arranged on the lower bottom of the crystallization tray, a waste water discharge pipe is connected on the waste water outlet, the waste water discharge pipe extends downwards and penetrates out of the tank body from the bottom of the tank body in a sealing way; the bottom of the crystallizing tank is also provided with a discharge port for discharging waste water in the lower space; the part of the crystallization tray close to the upper part of the side wall is provided with an ice outlet, and the side wall of the lower space of the tank body is provided with a solid-liquid mixture outlet; or,

the container is a crystallizer and has the structure that: the crystallizer is a tank body, the gas outlet is arranged on the tank wall at the top of the tank body and is connected with the vacuum sublimation evaporation unit through a pipeline; the stirring device penetrates into the tank body from the top of the tank body in a sealing way; the liquid conveying pipe of the liquid inlet is hermetically inserted into the tank body from the side wall of the lower space of the tank body and then communicated with the inside of the crystallization tray from the position which is lower than the side wall of the crystallization tray; a waste water outlet is arranged on the lower bottom of the crystallization tray, a waste water discharge pipe is connected on the waste water outlet, the waste water discharge pipe extends downwards and penetrates out of the tank body from the bottom of the tank body in a sealing way; the bottom of the crystallizing tank 4 is also provided with a discharge port for discharging waste water in the lower space.

9. The apparatus of claim 8, wherein: a communicating pipeline is arranged between the solid storage tank and the container, and a conveying device is arranged on the communicating pipeline; and/or the presence of a gas in the gas,

the air suction port of the vacuum sublimation evaporation unit is respectively connected with the gas outlet of the container and the gas outlet on the solid storage tank, so that the same vacuum sublimation evaporation unit, namely a multi-stage vacuum pump unit, acts on the container and the solid storage tank to form the same pressure; and/or the presence of a gas in the gas,

the stirring paddle in the stirring device is positioned at the set liquid level in the crystallization tray or at the height within 50mm lower than the set liquid level; or the stirring paddle in the stirring device is positioned at the set liquid level in the crystallization tank or at the height within 50mm lower than the set liquid level; and/or the presence of a gas in the gas,

a connecting pipe is connected to the discharge port of the solid storage tank and is connected with a raw water heat exchanger, so that liquid in a solid-liquid mixture in the solid storage tank cools liquid entering the crystallizer; and/or the presence of a gas in the gas,

and a vacuum pump is connected to the gas outlet of the steam heat exchanger and used for pumping the gas subjected to heat exchange out of the heat exchanger.

10. The apparatus of claim 9, wherein: the conveying device is a slurry pump.