WO2019242507A1

WO2019242507A1 - Heat and cold energy separation method and apparatus employing sublimation and evaporation in vacuum and application apparatus thereof

Info

Publication number: WO2019242507A1
Application number: PCT/CN2019/090283
Authority: WO
Inventors: 武伟
Original assignee: 武伟
Priority date: 2018-06-22
Filing date: 2019-06-06
Publication date: 2019-12-26

Abstract

Provided in the present invention is a heat and cold energy separation method for separating a sensible heat of water from a latent heat of ice employing sublimation and evaporation in a vacuum. The method comprises: establishing a vacuum environment in an artificial environment, evaporating a portion of liquid entering therein, and solidifying a portion of liquid, wherein a portion of the solid can further be sublimated; separating the vapor from the solid, wherein the solid or solid-liquid mixture becomes cold energy for output, and the vapor becomes heat energy for output. The process continues to proceed, realizing the separation of cold and heat energies. The present invention makes use of the vacuum technology and the physical properties of water to realize the heat and cold energy separation and further realize the storage and usage thereof, which can greatly improve the system efficiency and COP value on the basis of the existing refrigerating and heating technologies. Further provided in the present invention is an apparatus for implementing said method. In addition, the present invention further provides equipment for applying said apparatus in seawater desalination, low-temperature power generation, heating, and refrigeration.

Description

Vacuum sublimation evaporation cold and heat energy separation method and device and application equipment thereof

Technical field

The invention belongs to the technical field of refrigeration and heat pumps, and provides a method for separating cold energy and thermal energy by means of vacuum sublimation evaporation, which separates sensible heat and latent heat of freezing in water for use. The invention also provides a device for use in the method. The invention also provides a distributed energy supply station, a desalination device, and a heating or cooling device suitable for cooling in summer and heating in winter.

Background technique

Refrigeration or heating technology refers to the use of artificial methods to cool or heat an object or object within a certain time and space, so that its temperature drops below the ambient temperature, or rises above the ambient temperature, that is, the use of refrigeration or heating A thermal operation is a unit operation in which thermal equipment adds energy to transfer heat from a low-temperature object to a high-temperature object. The refrigeration or heating technology applied in the prior art uses the compressor to do work to increase the pressure of the medium in the refrigeration or heating equipment, and then depressurizes it to absorb and release cold and heat energy and transfer it to the place of use. An operating technique.

Current refrigeration and heating are based on compressor technology to achieve the transfer of cold and heat energy and use operations. Due to the limitations of equipment principles and the working environment, the refrigeration energy efficiency ratio (COP value) of compressor refrigeration equipment has been hovering for a long time. Around 6 (the national-level energy-consumption COP of domestic air conditioners is only about 3.4, and the heat pump system COP is also below 6). The COP of domestic air conditioners with first-level energy consumption in China is around 3.4. Although foreign countries have reported refrigeration units with COP> 6 and <8, due to the high equipment prices, the actual improvement in efficiency is not large enough, resulting in low cost performance of equipment. The existing air energy water heater belongs to a heat pump system. Although it can heat and cool at the same time, it is limited by the compressor heat pump equipment, and the system COP is still below 6.

The high energy consumption of the existing cooling and heating technology makes centralized air-conditioning a large consumer of electricity, and greatly increases the load pressure of the national grid during the peak period in summer; while heating in winter is relatively expensive, it can only burn coal, which increases air pollution. In order to control the atmosphere, the country promotes the conversion of coal to gas, but due to the tight supply of natural gas resources and high prices, there are also some difficulties in promotion.

Freshwater is a necessary resource for human survival and development. With the development of society, fresh water resources have become more and more scarce resources. China is one of the most water-starved nations in the world. The amount of water per capita is even lower. The ocean contains huge water resources. Due to cost, it has not yet been used on a large scale. Experts and scholars believe that the current price system for desalination is unreasonable, and a new price system should be rationalized and formulated. The current desalination price is about 5 yuan / ton, and the recommended price from a professional perspective is 2 yuan / ton. It can be seen that there is still a large gap between the actual cost and the expected price of use. But at present, the price of water for citizens in cities has reached more than 4 yuan / ton, and the minimum price in small cities has reached more than 2.5 yuan / ton (residents' water prices include government subsidies). Water prices for other uses are much higher. Moreover, the trend of rising water prices continues. This opens the market door for commercial applications of desalination technology from an economic perspective.

At present, the technologies used in desalination include reverse osmosis desalination, low-temperature multi-effect evaporation, low-temperature steam distillation, and multi-stage flash evaporation, etc. See Table 1 for various desalination operating costs:

工艺技术Process technology	单位造水成本(元/吨)Unit water cost (yuan / ton)	工艺技术Process technology	单位造水成本(元/吨)Unit water cost (yuan / ton)
反渗透淡化Reverse osmosis desalination	4.314.31	低温压汽蒸馏Cryogenic steam distillation	5.035.03
低温多效蒸Low-temperature multi-effect steaming	4.874.87	多级闪蒸Multi-stage flash	5.155.15

Among them, the comprehensive operating cost of reverse osmosis is the lowest. Generally, the electricity consumption per ton of water is about 4KWH, plus the cost of chemicals is about 0.5 yuan per ton of fresh water. The direct operating costs are mainly the two types mentioned above. The direct operating cost per ton of water is 2.9 yuan / ton of fresh water. Then consider the cost of labor, maintenance, and replacement of reverse osmosis membranes is 0.93. The operating cost (excluding depreciation) is generally more than 4 yuan.

Let's take a look at the cost of equipment in the current desalination technology. The unit price of domestic desalination equipment market is around 10,000 yuan (ie 10,000 yuan per ton of daily production capacity). Taking a desalination plant with a daily output of 1,000 tons as an example, it requires an investment of about 10 million yuan and an annual desalination capacity of about 350,000 tons. Based on the 20 years of equipment use (excluding interest), the equipment depreciation fee is 500,000 yuan per year. Based on an annual operation of 350 days, the daily depreciation fee is 1,428 yuan. Depreciation per tonne of water: 1.43 yuan.

Other costs: such as labor, maintenance costs, and operating costs. However, this part of the cost accounts for a relatively small total cost of about 0.5 yuan / ton of water.

Comprehensive cost analysis:

The energy cost and the cost of a single-input desalination equipment are the decisive factors affecting the cost of desalination. Taking the reverse osmosis method as an example, the cost per ton of water should be more than 4 yuan. At present, the country's water price is generally lower than the cost of desalination. From the perspective of operation only, the relatively good state is a low profit level. From the perspective of investment profitability, the industry is not attractive to capital. It is just that the government considers from a macro perspective and a long-term development perspective to do some demonstration projects. From the perspective of payback period, the payback period is longer. For example, based on a net profit of 1.5 yuan per ton of water, a unit with a daily output of 1,000 tons of water can produce 350,000 tons of fresh water per year and an annual profit of about 525,000. If the investment is only based on 10 million, the equipment investment payback period needs to be at least 20 years. Therefore, from the perspective of comprehensive operating costs and equipment depreciation costs, high investment and operating costs are the biggest obstacles to the current large-scale market desalination technology.

Approaches to reduce the cost of seawater desalination technology From the perspective of comprehensive cost analysis, reducing equipment costs and energy consumption levels is the direction of seawater desalination technology development.

Low-temperature power generation technology is mostly used for geothermal power generation, reuse of exhausted steam after power plant generation, and utilization of industrial waste heat, but in practical applications, low-cost waste heat and exhausted steam sources are not widespread, so the application of low-temperature power generation is not widespread , Especially in remote areas where the level of power development is low, there is usually no condition for developing low-temperature power generation. The vacuum sublimation evaporation cold and heat energy separation method can efficiently and cost-effectively provide a stable steam source for low-temperature power generation in areas with water sources.

In the prior art, the use of waste heat to generate electricity can be an air energy water heater, which belongs to a heat pump system, and the current mainstream technology of heat pumps is based on compressor technology to realize the transfer and use of cold and heat energy. Due to the limitation of the equipment principle and working environment, the COP value of the existing compressor equipment has hovered below 6 for a long time (the national-level energy-consumption COP of domestic air conditioners is only about 3.4, and the heat pump system COP is also below 6). Although the air energy water heater can heat and cool at the same time, it is limited by the compressor heat pump equipment, and the system COP is still below 6.

In the prior art, it is common to provide energy for underfloor heating or centralized air-conditioning by burning fuel or electric heating equipment, heating a medium such as mineral oil, and then heating the water through heat exchange. cycle. In the summer, geothermal cooling is used. The compressor of the refrigeration equipment acts on the refrigerant, and then the refrigerant cools the water. The cooled cold water is circulated in the geothermal pipe or the centralized air conditioner.

The current mainstream technology of refrigeration and heat pumps is based on compressor technology to achieve the transfer and use of cold and heat energy. Due to the limitation of equipment principle and working environment, the COP value of the existing compressor refrigeration equipment has hovered below 6 for a long time (the national-level energy-consumption COP of domestic air conditioners is only about 3.4, and the heat pump system COP is also below 6). The existing air energy water heater belongs to a heat pump system. Although it can heat and cool at the same time, it is limited by the compressor heat pump equipment, and the system COP is still below 6.

It can be known that seeking a low-energy-consumption technology to partially replace the traditional compressor cooling and heating technology to achieve energy conservation and consumption reduction is an urgent problem to be solved at present.

Summary of the Invention

The object of the present invention is to provide a method for separating cold and heat energy by vacuum sublimation evaporation. The method utilizes vacuum technology and physical properties of water to realize the separation of cold and heat energy and further storage and use, which can be used in existing refrigeration and heating. Based on technology, system efficiency and COP value are greatly improved.

Another object of the present invention is to provide a device used in the above-mentioned cold-heat energy separation method.

The invention also provides application equipment using the method and device on seawater desalination, energy supply stations and heating and cooling.

The object of the present invention is achieved as follows:

A method for separating cold and heat energy by vacuum sublimation evaporation, used to separate sensible heat and latent heat of icing in water, is performed in such a device, the device includes an artificial environment, that is, a sealed container, the container is provided with The liquid inlet, gas outlet and solid or solid-liquid mixture outlet are also provided with a stirring device in the container, and a vacuum sublimation evaporation unit or a vacuum pump unit is connected to the gas outlet;

The separation method is:

Step 1: Establish a vacuum environment in an artificial environment, the vacuum environment is: let the liquid inlet enter the artificial environment liquid:

Part of it evaporates, part of it solidifies, or,

Some of them evaporate, some of them solidify into solids, and some of them solidify into steam;

Simultaneously and / or before and / or after, the introduction of liquid into the artificial environment through the liquid inlet;

Step 2: The steam is separated from the solid, and the stirring device is started, so that the solidified solid is broken, and the solid or solid-liquid mixture is discharged from the solid or solid-liquid mixture outlet into cold energy output, and the steam is discharged from the gas outlet by the vacuum pump unit Extraction becomes thermal energy output;

Steps

1 and 2 are performed alternately and / or simultaneously, so that the liquid enters the container, the solid or solid-liquid mixture exits the solid or solid-liquid mixture outlet, and the steam is extracted from the gas outlet. This process is continuously performed to achieve the cold and thermal energy. Separation.

Further, the method provided by the present invention further includes step 3: discharging the solid or solid-liquid mixture from the container into a solid storage tank at the same pressure as the container.

Preferably, the stirring device is started in step 1.

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

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

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

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

Further, in the stirring device provided in the container, in step 2, stirring is performed to ensure that the solid in the container does not seal the entire liquid surface, and the solid is broken and discharged from the solid or solid-liquid mixture outlet.

The device used in the method is such that it contains a sealed container on which a liquid inlet, a gas outlet, and a solid or solid-liquid mixture outlet are provided. A vacuum sublimation evaporation unit is connected to the gas outlet, which is sealed. A container provides a set pressure, and a stirring device is provided in the container.

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

Further, it also includes a solid storage tank, which is in communication with the container and constitutes the same pressure as the container. The solid or solid-liquid mixture outlet in the container is in communication with the inlet on the solid storage tank. A cut-off device is provided between the tank inlet and the solid or solid-liquid mixture outlet of the container to enable the two to communicate or cut off; a solid substance or solid-liquid mixture discharge port is provided on the solid storage tank, and an emptying port and The atmosphere is connected, and a vent valve is arranged on the vent.

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

The conveying device is preferably a mud pump.

Further, the suction port of the vacuum sublimation evaporation unit is respectively connected to the gas outlet of the container and an air outlet on the solid storage tank, so that the same vacuum sublimation evaporation unit, that is, a multi-stage vacuum pump unit, The solid storage tank acts to create the same pressure.

Further, the exhaust port of the vacuum sublimation evaporation unit is connected to a gas inlet of a steam heat exchanger that exchanges the extracted steam, and the low-temperature medium is heated by using the thermal energy of the steam that is heated up after the pressure is extracted from the container. .

A vacuum pump is connected to the gas outlet of the steam heat exchanger, and the vacuum pump is used to suck out the steam after the heat exchange and exit the steam heat exchanger.

The vacuum sublimation evaporation unit is a multi-stage vacuum pump, preferably a roots vacuum pump unit.

Preferably, in the multi-stage vacuum pump, the last stage is a screw-type vacuum pump; in the vacuum pump of each stage, the exhaust port of the former vacuum pump is directly connected to the suction port of the latter vacuum pump.

Preferably, the vacuum pumps of the previous stages are Roots vacuum pumps.

Further, the multi-stage vacuum pump unit has three stages, the first two stages are roots vacuum pumps, and the third stage is a screw vacuum pump.

The container may be a crystallizer, and its structure is as follows: the crystallizer is a tank body, and a basin-shaped partition plate including a bottom and a side wall is provided in the tank body to form a crystal plate, which crystallizes the internal space of the tank body. It is divided into an upper space and a lower space, and a gas outlet is provided on a tank wall at the top of the tank, and a vacuum sublimation evaporation unit is connected through a pipeline; the stirring device penetrates from the top of the tank in a sealed manner into a crystallization tray placed in the upper space; The liquid conveying pipe connected to the liquid inlet is inserted into the tank in a sealed manner from the side wall of the lower space of the tank, and then communicates with the crystallization disc from a position lower than the side wall of the crystallization disc; a waste water outlet is provided on the bottom of the crystallization disc, and The waste water discharge pipe is connected to the waste water discharge pipe, and the waste water discharge pipe extends downward and is sealed out from the bottom of the tank. The bottom of the crystallization tank is also provided with a drain port for draining waste water from the lower space; an ice outlet is provided on the upper part of the side wall of the crystallization disc, and a solid-liquid mixture outlet is provided on the side wall of the lower space of the tank body. .

The structure of the container may also be: the container is a crystallizer, the structure is: the crystallizer is a tank body, the gas outlet is arranged on the tank wall at the top of the tank body, and the vacuum sublimation evaporation unit is connected through a pipeline; the stirring device From the top of the tank, it penetrates into the tank tightly; the liquid inlet is set on the side wall of the tank, and the solid or solid-liquid mixture outlet is set on the side wall of the tank. The liquid inlet is lower than the solid-liquid mixture outlet; The bottom of the tank is provided with a drain port for draining waste water from the lower space.

The stirring paddle in the stirring device is located at a set liquid level in the crystallization pan or at a height within 50 mm below the set liquid level; or, the stirring paddle in the stirring device is located at a set liquid level in the crystallization tank or Height below 50mm of set liquid level.

The following are equipment for several applications using the vacuum sublimation evaporation cold and heat energy separation method and equipment:

I. Desalination equipment:

A vacuum sublimation evaporation and freezing seawater desalination device for separating sensible heat and latent heat of icing in water, which is characterized in that it includes at least one desalination unit, the desalination unit includes a raw water inlet and a freshwater outlet. Including a cold and heat energy separation device,

The cold and heat energy separation device includes at least one crystallizer and a vacuum pump unit. The crystallizer is provided with the water inlet, steam outlet, ice-water mixture outlet, and high-salt wastewater discharge outlet. The water inlet and the raw water The inlet is connected, and the ice-water mixture outlet is in communication with the fresh water outlet. The steam outlet is connected to the vacuum pump unit to provide a set vacuum pressure for the crystallizer, so that raw water can appear after entering the crystallizer. :

Part of the raw water becomes steam and is extracted, and part of the raw water becomes solid ice, or,

Part of the raw water becomes steam and is extracted, part of the raw water becomes solid ice, and part of the ice rises into steam;

A stirring device is provided in the crystallizer. The stirring device breaks solid ice to form an ice-water mixture and discharges it, and then discharges through the fresh water outlet to form fresh water with reduced salt content.

The structure of the crystallizer in the cold-heat energy separation device may be various:

One of the crystallizer structures is:

A liquid supply tray is provided in the tank of the crystallizer, and the liquid supply tray is provided at the lower part of the tank. The liquid supply tray includes a cavity, and a liquid inlet is provided on the lower part or the side wall of the cavity. A hole is connected to the raw water inlet through a pipeline, and a liquid spray hole is provided on the wall of the cavity facing upward; the ice-water mixture outlet is disposed above the water inlet, so that the liquid supply tray is in use Placed below the liquid surface.

Further, the stirring device includes a paddle provided on a stirrer shaft, the stirrer shaft sealingly protruding from the tank body is connected to a power source; the paddle is located higher than the ice-water mixture outlet , Located at the set liquid level in the tank, so that half of the mixing paddle is above the liquid level and the other half is below the liquid level, or the mixing paddle is at a height within 50mm of the set liquid level to break the liquid surface The resulting ice layer.

Further, the liquid supply tray may be a shower head, the liquid spray holes are arranged upward, and the liquid inlet hole at the bottom is connected to the water inlet on the crystallizer tank through a pipeline.

Further, the crystallizer may further include a heater, and the heater is disposed in an upper space of the tank body above a set liquid level.

Furthermore, the heater is a heating coil or a plurality of heating coils arranged above and below, and the two ends of the heating coil are hermetically extended out of the tank to inject and discharge the heating medium.

Setting a heater in the crystallizer can speed up the evaporation process and help to improve the separation speed of cold and heat energy.

The heating medium inlet of the heating coil is connected with the steam outlet of the vacuum pump unit, and the steam with reduced pressure and temperature is used as the heating medium.

Another structure of the mold can be:

A pot-shaped partition plate including a lower bottom and a side wall is set in the crystallizer tank to form a crystallization disc, which divides the internal space of the tank into an upper space and a lower space; the stirring device is from the top of the tank Sealedly penetrated into the crystal plate placed in the upper space; the liquid conveying pipe connected to the water inlet is sealedly inserted into the tank from the side wall of the lower space of the tank, and then lowered from the side wall of the crystal plate Connected to the inside of the crystallization tray; a drain port is provided on the lower bottom of the crystallization tray; a waste water discharge pipe is connected to the waste water discharge pipe; the waste water discharge pipe extends downward; and is sealed out from the bottom of the tank through the high-salt waste water discharge port Tank body; a drain port is also provided on the bottom of the crystallizer for draining waste water from the lower space; an ice port is provided on the upper part of the side wall of the crystallization plate, and the side wall of the lower space of the tank body is provided with the drain port Ice water mixture outlet.

Further, the stirring paddle in the stirring device is located at a set liquid level in the crystallization plate, so that half of the paddle is above the liquid level and the other half is below the liquid level, or the paddle is below the set liquid level Height within 50mm.

Desalination can be performed using the above equipment:

The seawater is passed into a crystallizer in the cold-heat energy separation device. The crystallizer constructs an artificial environment, that is, a vacuum environment through a vacuum pump unit. The vacuum environment is such that a part of the raw water entering the crystallizer evaporates into steam, and a part solidifies Ice, or part of the seawater evaporates into steam, part of it freezes into ice, and part of the ice sublimates into steam.

The artificial environment is a high-vacuum environment where the pressure is in the three-phase diagram of water or below the three-phase point.

After the vacuum pump unit builds the artificial environment, it continues to work. The steam of the incoming raw water evaporated under high vacuum is continuously extracted from the crystallizer. The raw water in the crystallizer is quickly frozen, and the stirring device is continuously stirred to break the formed ice. When the seawater is continuously input to the artificial environment through the raw water inlet, the steam is continuously pumped away, and the remaining seawater is continuously frozen and broken by stirring. The seawater in the crystallizer becomes an ice-water mixture.

The ice-water mixture is discharged from the ice-water mixture outlet of the crystallizer, and the high-salt wastewater in the crystallizer is discharged from the high-salt wastewater discharge port provided at the bottom of the crystallizer.

The ice-water mixture outlet of the crystallizer can be connected to an ice slurry pump, or a large-diameter ice discharge port can be used, which can be closed by a sealable gate valve.

Desalination processes can be intermittent. In the above equipment, after the vacuum pump unit works for a set time, stop working, open the valve on the crystallizer to release the pressure, then open the valve on the ice slurry outlet, discharge the ice slurry, and then remove the high salt from the bottom of the crystallizer or the bottom of the crystallizing plate. The valve on the waste water discharge opening is opened to discharge the high-salt waste water. Then close each valve, re-open the vacuum sublimation evaporation unit, and put in seawater.

Desalination processes can also be continuous. At this time, the above equipment needs to be improved as follows:

Further, at least one isobaric ice slurry storage tank may be connected to the crystallizer, and the isobaric ice slurry storage tank communicates with the crystallizer to form the same pressure as the crystallizer. The ice water mixture outlet is in communication with the inlet on the ice slurry storage tank, and the pipeline between the ice slurry storage tank inlet and the ice water mixture outlet of the crystallizer is provided with a shut-off device to make the two communicate or Closing; an ice-water mixture outlet is provided on the ice-pressurized slurry storage tank, and an air vent is provided on the ice-pressed slurry storage tank to communicate with the atmosphere, and a vent valve is provided on the vent.

Preferably, the suction port of the vacuum pump unit is respectively connected to the steam outlet of the crystallizer and an air outlet on an isobaric ice slurry storage tank, so that the crystallizer is accessed by the same vacuum pump unit, that is, a multi-stage vacuum pump unit. Acts with the isobaric ice slurry storage tank to form the same pressure.

During the seawater desalination process, seawater continuously enters the crystallizer from the seawater inlet on the crystallizer, and the ice-water mixture outlet is continuously discharged from the ice-water mixture outlet into the isobaric ice slurry storage tank. When full, close the valve on the pipeline between the crystallizer and the isobaric ice slurry storage tank, vent the isobaric ice slurry storage tank to atmospheric pressure, discharge the ice-water mixture from the ice-water mixture outlet, and then close the isobaric ice The slurry storage tank is connected to a vacuum pump unit to form a set vacuum pressure, and then communicates with the crystallizer. It is also possible to set two or more isobaric ice slurry storage tanks at the same time, so as to realize an inverted tank full of isobaric ice slurry storage tanks. In this way, the desalination process can be continuously performed for a longer period of time. After a period of time, the crystallizer stops operating and the high-salt wastewater is discharged.

Preferably, a conveying device is provided in a communication pipeline between the isobaric ice slurry storage tank and the crystallizer, and the conveying device is preferably a mud pump.

The cold and heat energy separation device further includes two heat exchangers, one of which is a steam heat exchanger, which is connected to a steam exhaust port on the vacuum pump unit, so that steam with an increased pressure and an increased temperature is extracted from the crystallizer. As the heating medium of the steam heat exchanger; the second is the ice slurry heat exchanger, which is connected to the ice-water mixture outlet, so that the ice slurry serves as the cooling medium of the ice slurry heat exchanger.

A steam heat exchanger can be used to melt the ice discharged from the crystallizer, which is usually in the state of ice slurry.

The ice slurry heat exchanger can be used to cool the raw water entering the crystallizer, which is more conducive to the separation of cold and heat energy in the crystallizer.

The desalination unit may further include an ice slurry dehydrator, which is a tank body provided with an inlet and an outlet, the inlet is connected to the ice-water mixture outlet, and the outlet is provided in the ice slurry dehydration At the set liquid level of the device, the outlet is the fresh water outlet.

The desalination unit may further include an ice slurry pond on which an inlet and an outlet are provided, the inlet is connected to the ice-water mixture outlet, and the outlet is the fresh water outlet.

The desalination unit may further include an ice slurry dehydrator and an ice slurry pond,

The ice slurry dehydrator is a tank body, which is provided with an inlet and an outlet, the inlet is connected to the ice water mixture outlet, and the outlet is provided at a set liquid level of the ice slurry dehydrator,

The ice slurry pond is provided with an inlet and an outlet, the inlet is connected to the outlet of the ice slurry dehydrator, and the outlet is the fresh water outlet.

The desalination unit may further include an ice slurry dehydrator, an ice slurry pool, and an ice slurry melter,

The ice slurry dehydrator is a tank body, which is provided with an inlet and an outlet, and the inlet is connected to the ice-water mixture outlet;

The ice slurry pool is a container on which an inlet and an outlet are provided, and the inlet is connected to the outlet of the ice slurry dehydrator;

The ice-melt melter is a container provided with an inlet and an outlet, the inlet is connected to the outlet of the ice-melt pool, and the outlet is the fresh water outlet of the desalination unit, in the container of the ice-melt melter. Install a heating device.

Preferably, the number of the desalination units is n, and the raw water inlet in the first desalination unit is a seawater inlet, and the raw water inlet in the nth desalination unit is n times the raw water inlet, which is connected to the fresh water in the n-1th desalination unit. Exit, and so on.

The desalination unit is preferably 2-3.

When multiple desalination units are used, the seawater can be subjected to multiple cold and heat energy separations. The fresh water produced by the first desalination unit is used as the secondary raw water and then introduced into the crystallizer of the second desalination unit, where it is evaporated and frozen The ice slurry is discharged through the ice slurry melter to obtain fresher water of higher purity. The outlet of the ice slurry melter of the last desalination unit leads to qualified fresh water.

Second, the distributed energy supply station

A distributed energy supply station for vacuum sublimation evaporation cold and heat energy separation method, including a group of cold and heat energy separation device and a low-temperature power generation device,

The cold and heat energy separation device includes a set of separation equipment and a vacuum pump unit,

The cold and heat energy separation equipment includes a sealed container, which is provided with at least a water inlet and a steam outlet;

The suction port of the vacuum pump unit is connected to a steam outlet on the sealed container, and a high-temperature steam and / or hot water discharge port is also provided thereon;

The low-temperature power generation device includes a low-temperature generator set, and the generator set includes:

A low temperature generator;

A power-generating medium evaporator that transmits power-generating medium steam to a low-temperature generator, and

A power-generating medium condenser receiving a power-generating medium discharged from a low-temperature generator,

The power generation medium condenser and the power generation medium evaporator are both wall heat exchangers. The power generation medium flow channels in the two are connected to the low temperature generator to form a circulation system;

These are existing technologies, and specifically may be: a low-temperature power generation medium inlet and a high-temperature power generation medium steam outlet are provided on the power generation medium flow passage in the power generation medium evaporator, and a high temperature steam inlet and a low temperature exhaust steam outlet are provided on the heating medium flow passage; A high-temperature power medium inlet and a low-temperature power medium outlet are provided on the power medium passage in the power medium condenser, and a low-temperature medium inlet and a high-temperature medium outlet are provided on the cooling medium flow passage; the high-temperature power medium steam outlet on the power medium evaporator passes through The pipeline is connected to the steam inlet of the generating medium of the low-temperature generator, and the exhaust steam outlet of the low-temperature generator is connected to the high-temperature generating medium inlet of the generating medium condenser through the pipeline. The low-temperature generating medium outlet of the generating medium condenser is directly or through a storage tank. Connected to the low temperature power medium inlet on the power medium evaporator; the characteristics are:

The high-temperature steam inlet on the power generation medium evaporator in the low-temperature power generation device is connected to the high-temperature steam and / or hot water discharge port of the vacuum pump unit in the cold-heat energy separation device through a pipeline.

The mechanism of the invention is: using the steam separated from the cold and heat energy separation device at about 100 ° C or the converted hot water of more than 90 degrees to heat the power generation medium in the low temperature power generation device to vaporize it, and then use the vaporized power generation medium to push it The screw expander generates electricity by driving the generator to run; and the heat source used to heat the power generation medium is provided by the cold-heat energy separation device, which separates the sensible heat and latent heat of freezing from the raw water. It is through the vacuum pump unit to pump down the pressure of the sealed container, to create a vacuum working environment in the sealed container, so that the liquid inside the sealed container, such as water, evaporates, the water vapor takes away the heat, and the steam extracted by the vacuum pump unit passes through The stage is boosted and no cooling device is installed between the stages. The temperature of the steam discharged in the last stage can reach about 100 ° C. Such low-temperature steam or converted hot water of more than 90 degrees is used as a heat source to heat the medium used for power generation and vaporize it. And drive the low temperature generator to generate electricity.

The working process of the cold and heat energy separation device is: as the vacuum degree increases according to the process requirements, the pressure in the working space of the sealed container continues to decrease according to the process parameter requirements. The vacuum degree can be controlled so that the water in the sealed container remains liquid, and the vacuum degree can also be increased. So that the water in it enters the sublimation zone of ice, which is the normal production pressure parameter zone of the process. Since ice is formed on the water surface, the sublimation reaction starts. At this time, an ice ejector in the sealed container is used to set an ice slurry discharge port on the sealed container, and the ice is successively discharged from the space through the ice slurry discharge port. The elimination of part of the ice layer provides conditions for the water under the ice layer to continue to evaporate. The water vapor that continues to evaporate provides good heat transfer conditions for the sublimation of the ice layer. At this time, sublimation and evaporation occur simultaneously in the sealed container, and water vapor overflows continuously and is extracted by the vacuum pump unit and takes away a lot of heat, and the low-temperature new raw material water is continuously frozen into ice in the sealed container. The finished ice is then discharged through the separation equipment to complete the entire ice making and steam production process.

The cold-heat-energy separation device may include a low-temperature cold-heat energy separation device and / or a high-temperature cold-heat energy separation device with a relatively high set temperature in a sealed container, and the sealed container in the low-temperature cold-heat energy separation device. There is also an ice slurry outlet; the sealed container in the high-temperature cold-heat energy separation device is provided with at least a water inlet and a steam outlet.

The forms of the low-temperature cold-heat energy separation device and the high-temperature cold-heat energy separation device are similar, but the working pressure and temperature regions are different. The low-temperature cold-heat energy separation device is used to separate the latent heat of freezing of water. Therefore, an ice slurry outlet is provided on the sealed container. The high-temperature heat energy separation device is used to separate the sensible heat in water and efficiently and low-consumption water vapor. The working temperature of the low-temperature cold-heat energy separation device can be below 0 ° C, and the working temperature of the high-temperature unit can be above 10 ° C.

Because the evaporation efficiency of water will be greatly reduced when the temperature is low or the freezing point is reached, in order to ensure sufficient water vapor generation efficiency, this technology uses stirring, cold boiling, increasing the evaporation area, and increasing Heat exchanger or cold trap technology to achieve efficient separation of cold and heat energy.

Specifically: in the sealed container, a stirring device may be provided.

To manufacture cold boiling, preferably, a liquid supply tray is provided in the sealed container, and the liquid supply tray is arranged in the lower part of the sealed container, and the liquid supply tray is lower than a set liquid level height in the sealed container. For a shower, the liquid spray hole is set upward, and the liquid inlet at the bottom is connected to the water inlet through a pipeline.

In use, the liquid supply tray is located below the liquid surface, and water is ejected from the liquid injection hole facing upward from the liquid supply tray, thereby forming cold boiling in a sealed container.

In order to improve the evaporation efficiency of water in sealed containers, another effective measure is to increase the temperature of the incoming water. In order to increase the inlet water temperature, the following measures can be taken:

The first measure is to increase the inlet water temperature by preheating, that is:

A preheater may be provided on the pipeline of the water inlet of the sealed container, so that the water entering the sealed container is heated in advance.

And what is used as the heating medium for the preheater? The following scenarios are possible:

The first option is to use a low-temperature power generation medium as a preheating agent:

Preferably, one end of a branch pipe may be connected to the power generation medium outlet of the low temperature generator in the low temperature power generation device, and the other end of the branch pipe is connected to the heating medium of the preheater provided on the water inlet of the sealed container. An inlet for heating the water entering the sealed container from the partition wall. The heating medium outlet on the preheater is connected to one end of a power generation medium return pipe, and the other end of the power medium return pipe is connected to the power medium inlet of the power medium evaporator in the low-temperature power generation device. , Or connect to a power storage tank. The heat of the power generation medium is thereby used to raise the temperature of the water entering the sealed container.

The second option is to use the high temperature steam discharged from the vacuum pump unit connected to the sealed container as a preheating agent:

Preferably, the inlet of the heating medium of the preheater is connected to one end of a pipeline, and the other end of the branch pipeline is connected to a branch port on the high-temperature steam discharge pipeline of the vacuum pump unit, and the heating medium of the preheater The outlet can be vented or connected to the heating steam inlet on the power generation medium evaporator in the low-temperature power generation device.

The third solution is to use the cooling water for cooling the power generation medium in the low-temperature power generation device as a preheating agent:

Preferably, the inlet of the heating medium of the preheater is connected to one end of a pipe, and the other end of the branch pipe is connected to the cooling water outlet of the power generating medium condenser in the low-temperature power generation device, and the preheater The heating medium outlet can be vented or connected to a storage tank through a pipeline.

The fourth option is to use the exhaust steam that heats the power generation medium in the low temperature power generation device as a preheating agent:

Preferably, the inlet of the heating medium of the preheater is connected to one end of a pipeline, and the other end of the branch pipeline is connected to the exhaust steam outlet of the power generation medium evaporator in the low-temperature power generation device, the preheater The heating medium outlet can be vented or connected to a storage tank through a pipeline.

Further, the outlet of the heating medium of the preheater may be connected to a sewer, or may be connected to a water inlet, and water or steam may be passed into the sealed container for use.

The second measure is: hot water with a certain temperature directly used in the heating medium in the preheater is input into the sealed container, that is:

The water inlet of the sealed container is connected to one end of a pipeline, and the other end of the pipeline can be connected to at least one of the following equipment:

A cooling water outlet of the power generation medium condenser;

Exhaust steam outlet of the power generation medium evaporator;

A branch opening on the high-temperature steam discharge line of the vacuum pump unit.

The third measure is to set up a cold and heat energy separation device. The water entering the new cold and heat energy separation device comes from the hot water condensed by the high-temperature steam drawn from the elementary cold and heat energy separation device, or the incoming water comes from low temperature power generation The hot water formed by the exhaust steam from the power-generating medium evaporator or the cooling water from the power-generating medium condenser in the device, namely:

The cold-heat energy separation device is a low-temperature cold-heat energy separation device, which is used to separate sensible heat and latent heat of freezing in normal temperature water. It is called a first-level cold-heat energy separation device, and an ice slurry is also provided on the sealed container. An outlet is connected to a storage tank at the high-temperature steam discharge port of the first-stage cold-heat energy separation device; a high-temperature cold-heat energy separation device is further included between the first-stage cold-heat energy separation device and the low-temperature power generation device, It is used to separate sensible heat in hot water below 100 ° C. It is called a secondary cold-heat energy separation device. It includes a secondary sealed container. The secondary sealed container is provided with at least a high-temperature water inlet and a high-temperature steam outlet. The water inlet is connected to the storage tank connected to the high-temperature steam discharge port of the primary cold-heat energy separation device, and the high-temperature steam outlet is connected to a second-stage vacuum pump unit, and the last-stage steam discharge port of the second-stage vacuum pump unit passes a pipe. The heating steam inlet on the power generation medium evaporator in the low-temperature power generation device; or

The cold-heat energy separation device is a low-temperature cold-heat energy separation device, called a primary cold-heat energy separation device, and further includes a high-temperature cold-heat energy separation device, called a secondary cold-heat energy separation device. The separation device includes a secondary sealed container. The secondary sealed container is provided with at least a secondary water inlet and a secondary steam outlet. The secondary water inlet is connected to the power generation medium in the low-temperature power generation device through a pipeline. The waste steam outlet of the evaporator or the cooling water outlet connected to the condenser of the power generation medium; the secondary steam outlet is connected to a secondary vacuum pump unit, and the last stage steam outlet of the secondary vacuum pump unit is connected to the low temperature through a pipeline The heating steam inlet on the power generation medium evaporator in the power generation device, and / or, the heating steam inlet on the power generation medium evaporator in another low temperature power generation device; or:

The cold-heat energy separation device is a low-temperature cold-heat energy separation device, called a primary cold-heat energy separation device, and further includes a high-temperature cold-heat energy separation device, called a secondary cold-heat energy separation device. The separation device includes a secondary sealed container. The secondary sealed container is provided with at least one secondary water inlet and one secondary steam outlet. In addition, it also includes a wall-type heat exchanger with a heating agent flow channel and a water flow. The steam exhaust port of the last stage of the vacuum pump unit in the primary cold and heat energy separation device is connected to the inlet of the heating agent flow channel of the heat exchanger through a pipeline, and the seal in the secondary cold and heat energy separation device is sealed. The water inlet on the container is connected to the outlet of the water flow channel of the heat exchanger through a pipeline, and the secondary steam outlet of the secondary cold heat energy separation device is connected to the high temperature steam inlet of the power generation medium evaporator on the low temperature power generation device. .

For the hot steam and hot water condensed by the steam heated in the power generation medium evaporator, the cold and heat energy separation equipment can be used again to separate the thermal energy from the water and generate new water vapor. Since the evaporation efficiency of water at higher temperatures is several times that of water at lower temperatures, the energy spent to obtain the same amount of thermal water vapor is only a fraction of the energy at low temperatures. This part of the steam energy can be reused. therefore,

In the aforementioned hot and cold energy separation device, the water inlet of the sealed container is connected to one end of a pipeline, and the other end of the pipeline may be connected to at least one of the following equipment:

A cooling water outlet of the power generation medium condenser;

Exhaust steam outlet of the power generation medium evaporator;

A branch nozzle on a high-temperature steam discharge pipeline of the vacuum pump unit.

It is also possible to take a measure that is beneficial to the evaporation of water in the sealed container: a heater is provided in the upper part of the sealed container, which is located above the set liquid level in the sealed container.

Preferably, the heater is a heating coil, and the two ends of the heating coil are hermetically extended out of the sealed container to connect a heating medium supply device.

Preferably, the heating medium supply device connected to the heating coil may be the vacuum pump unit, and a branch pipe from the steam outlet of the vacuum pump unit is connected to the heating coil.

It may also be: the heating coil is connected to a cooling water outlet of the power generation medium condenser;

The heating coil is connected to the exhaust steam outlet of the power generation medium evaporator;

The heating coil is connected to the exhaust steam outlet of the cryogenic generator.

The installation of heating coils is conducive to the steam production efficiency of reduced pressure and temperature. The hot steam generated in the cold-heat energy separation device heats the vaporized power generation medium, and after the primary power generation, more than 80% of the energy remains unused. The thermal energy separation unit can be reused for secondary power generation or multiple power generation, so that The energy separated by cold and heat energy separation technology is fully utilized.

To this end, the low-temperature generator set includes at least two low-temperature generators, which are connected in series, that is, the exhaust steam outlet of the power generation medium of the previous low-temperature generator is connected to the power generation medium of the next low-temperature generator through a pipeline. The steam inlet and the exhaust outlet of the last low-temperature generator's power-generating medium exhaust steam are connected to the power-generating medium exhaust steam inlet of the power-generating medium condenser through a pipeline.

A water inlet is provided above the liquid level of the sealed container, and a water spray device is provided on the water inlet to make the water inlet spray into the sealed container.

One end of a water inlet connected to a water inlet is provided above the liquid level in the sealed container, and the other end of the tube is connected to the cooling water outlet of the power medium condenser and / or the exhaust steam outlet of the power medium evaporator.

That is, the water inlet above the liquid surface can be sprayed with raw water, or the raw water may not be input in a spraying manner, and hot water is preferably sprayed to increase the steam output rate. Therefore, the water jet is connected to at least one of the following devices:

Connected to a cooling water outlet of the power generation medium condenser;

The spent steam outlet of the power generation medium evaporator is connected.

Preferably, the water spraying port of the water spraying device is provided in a horizontal direction or a downwardly inclined direction.

The vacuum pump unit is a multi-stage vacuum pump, wherein the suction port of the first-stage vacuum pump is connected to the steam outlet on the sealed container, the suction port of the subsequent stage is connected to the exhaust port of the previous stage, and the vacuum pumps of each stage are from front to back The amount of air extraction is gradually reduced, so that the pressure of the extracted steam is gradually increased to atmospheric pressure, and the high-temperature steam and / or hot water discharge port is provided in the last stage.

Preferably, in the multi-stage vacuum pump, the first-stage vacuum pump and the second-stage vacuum pump are Roots vacuum pumps, and the last-stage vacuum pump is a screw vacuum pump.

Third, heating or cooling equipment

A vacuum sublimation evaporation cold-heat energy separation heating or cooling device includes a cold-heat energy separation device, a vacuum pump unit, and a steam heat exchanger.

The cold-heat energy separation device has a sealed container, which is provided with a water inlet and a steam outlet;

The vacuum pump unit is a multi-stage vacuum pump. The suction port of the first stage is connected to the steam outlet on the sealed container, and the suction port of the subsequent stage is connected to the exhaust port of the previous stage. The air volume gradually decreases, so that the pressure of the extracted steam is gradually increased to atmospheric pressure;

The steam heat exchanger is a wall-type heat exchanger, in which the inlet of the high-temperature fluid channel is connected to the exhaust port of the last stage of the vacuum pump unit, and the outlet of the high-temperature fluid channel is emptied or connected to a condensate storage tank; The inlet and outlet are connected to the heating pipe and the water inlet pipe and the return pipe of the heat source water tank of the centralized air conditioner to form heating equipment.

The process of providing floor heating or central air conditioning heating through the heating device is:

Normal temperature water enters through the water inlet on the sealed container. The vacuum pump unit is started at the same time or in advance. The sealed container is evacuated to form a high vacuum state. The minimum pressure can reach near or below the three-phase point in the three-phase diagram of water. . Part of the water entering the sealed container continuously evaporates in the high-vacuum environment and is pumped out by the vacuum pump unit. The vacuum pump unit pressurizes the steam step by step, and the temperature of the steam that increases the pressure also gradually increases; the usual vacuum pump unit is in the stage. A heat exchanger will be set to reduce the temperature of the steam, and the vacuum pump unit in this equipment cancels the interstage heat exchanger, so that the temperature of the steam discharged from the last stage of the vacuum pump unit is higher, which can reach 100 ° C; Input to the high-temperature fluid channel of the steam heat exchanger. For the heating of water in the low-temperature fluid channel, the heated water is discharged from the steam heat exchanger and sent to the floor heating heating coil or the heat source water tank of the centralized air conditioner. The heat exchanged and cooled steam generally becomes condensed water, is discharged from the outlet of the high temperature fluid channel of the steam heat exchanger, or is collected. With the continuous injection of normal temperature water, such as tap water, in the sealed container, and the continuous operation of the vacuum pump unit, high-temperature steam will continuously flow into the steam heat exchanger, which will also be able to heat the water in the heating coil or the water tank Continuous heating to meet the needs of floor heating or central air conditioning.

The utility model also provides a vacuum sublimation evaporation cold-heat energy separation heating or cooling device, which can provide ground cooling applications only in summer, including a cold-heat energy separation device, a vacuum pump unit, and an ice-water heat exchanger. And an ice slurry tank,

The cold-heat energy separation device has a sealed container, which is provided with a water inlet, a steam outlet, and an ice slurry outlet;

An inlet of the ice slurry storage tank is connected to an ice slurry outlet provided on a sealed container in the cold-heat energy separation device;

The ice-water heat exchanger is a wall-type heat exchanger, wherein the inlet of the low-temperature fluid channel is connected to the outlet of the ice slurry storage tank, and the outlet of the low-temperature fluid channel is connected to the return water port of the ice slurry storage tank or becomes a discharge port; The inlet and outlet of the high-temperature fluid channel are respectively connected to the water inlet pipe and the water return pipe of the floor heating cooling coil or the cold source water tank of the centralized air conditioner to form cooling equipment.

In the foregoing two types of equipment, preferably, a stirring device is provided in the sealed container, and the stirring blades in the stirring device are set at the set liquid level of the sealed container so as to break the ice layer formed on the liquid surface. And improve evaporation efficiency.

In the aforementioned first device, further, the vacuum sublimation evaporative freezing heating or cooling device further includes an ice slurry storage tank and an ice water heat exchanger,

The ice-water heat exchanger is a wall-type heat exchanger, wherein the inlet of the low-temperature fluid channel is connected to the outlet of the ice slurry storage tank, and the outlet of the low-temperature fluid channel is connected to the return water port of the ice slurry storage tank or becomes a discharge port; The inlet and outlet of the high-temperature fluid channel are respectively connected to the water inlet pipe and the water return pipe of the heating source cooling coil or the cold source water tank of the centralized air conditioner to form equipment that can supply heat and cold.

This kind of equipment can be used in this way: as the vacuum pump unit continues to evacuate the sealed container, the temperature of the water in the sealed container will continue to decrease and even freeze. This part of water is used in the floor heating device to provide a cool summer. Floor heating applications. Therefore, in a preferred technical solution, an ice slurry outlet is provided on the sealed container, and a connecting pipe thereon is connected to the inlet of an ice water storage tank, and the ice slurry discharged from the sealed container is melted into cold water in the ice water storage tank, Then, the cold water is input to the inlet of the low-temperature runner of the ice-water heat exchanger, and normal temperature water enters from the inlet of the high-temperature runner of the ice-water heat exchanger. The outflow is sent to the floor heating heating coil or the cold source water tank of the centralized air conditioner for use. In summer, the high-temperature steam extracted by the vacuum pump unit of the cold-heat energy separation equipment can be used to manufacture domestic hot water. Therefore, based on the foregoing technical solutions, a preferred solution can be provided, in which the vacuum pump unit The pipeline connected to the exhaust port of the last stage is connected to the inlet of a high-temperature runner of a hot water heat exchanger, and the domestic water pipeline connects the inlet and outlet of a low-temperature runner of the hot water heat exchanger.

The above-mentioned heating and cooling, as well as both heating and cooling, and the preparation of domestic hot water, these applications are all around a core device, that is, cold and heat energy separation equipment. In practical applications, A steam heat exchanger can be separately connected to the cold and heat energy separation equipment to provide hot water required for floor heating or centralized air conditioning for the floor heating heating coil or central air conditioning heat source water tank in winter, or it can be separately connected to the ice water heat exchanger. In summer, it provides cold water for underfloor heating or centralized air conditioning for cold heating coils or central air conditioning cold water tanks. It can also be connected to a hot water heat exchanger separately to produce domestic hot water. Of course, you can also combine at least two of them together.

The vacuum sublimation evaporation cold and heat energy separation method provided by the present invention is a technology that realizes the separation, storage and use of cold energy and heat energy by utilizing vacuum technology and physical properties of water.

In specific applications, it can be used for seawater desalination and cold-heat energy separation of water. The extracted steam can be used for low-temperature power generation and heating, and ice slurry can be used as a refrigerant. Due to the use of a high-efficiency vacuum sublimation evaporation technology different from the compressor technology, without using other refrigeration media and supporting refrigeration medium circulation systems, the energy transfer link is reduced, the system efficiency is improved, and the COP value can be greatly increased. The larger the cooling or heating capacity, the larger the COP value, so that it can break through 12, and even reach 20 or more. At the same time, the present invention uses liquid phase-change morphology (steam and ice) as a carrier of energy and a storage and application medium, which makes it easier to separate and use cold and heat energy, and greatly improves the efficiency. As a result, the overall efficiency of the system is greatly improved.

The invention is further described below with reference to the drawings and embodiments.

BRIEF DESCRIPTION OF THE DRAWINGS

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

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

FIG. 1b is a schematic structural diagram of a crystallizer of another structure.

FIG. 2 is a schematic diagram of a control system of a device used in the vacuum sublimation evaporation cold and heat energy separation method provided by the present invention, and FIG. 2 also shows the flow running direction of various fluids in the device described in FIG. 1.

Figure 3 is an equilibrium phase diagram of water.

Figure 4 shows the relationship between working conditions and COP, which shows the current COP conditions during compression cooling or heating, where the abscissa is the state point with different artificial environment and fluid temperature difference, and the ordinate is the COP value corresponding to each state point. .

FIG. 5 is a graph showing the relationship between working conditions and COP, showing the COP status of the method of the present invention during cooling or heating.

FIG. 6 is a process flow chart of one embodiment of seawater desalination by vacuum sublimation evaporation and freezing.

FIG. 7 is a schematic structural diagram of a crystallizer of another structure.

FIG. 8 is a schematic bottom view of the liquid supply tray in the crystallizer shown in FIG. 7.

FIG. 9 is a schematic structural diagram of a heating coil in the crystallizer shown in FIG. 7.

FIG. 10 is a schematic structural diagram of a distributed energy supply station for vacuum sublimation evaporation cold and heat energy separation method provided by the present invention.

FIG. 11 is a schematic structural diagram of an energy supply station in which a secondary cold-heat energy separation device is added on the basis of FIG. 1.

FIG. 12 is a schematic structural diagram of an energy supply station in which a secondary cold-heat energy separation device is added based on FIG. 1.

FIG. 12a is a modified embodiment of FIG. 3. FIG.

FIG. 13 is a schematic structural diagram of an energy supply station on the basis of FIG. 1, in which steam extracted from a sealed container by a vacuum pump unit is used to preheat the raw water.

FIG. 14 is a schematic structural diagram of an energy supply station in which a preheating structure for raw water is added to the raw water by using cooling water for cooling the power generating medium steam in the power generating device on the basis of FIG. 1.

FIG. 15 is a schematic structural diagram of an energy supply station in which a structure for preheating raw water by using steam after heating a vaporized power generation medium in a power generation device is added on the basis of FIG. 1.

FIG. 16 is a graph showing the evaporation of water at different temperatures and pressures.

FIG. 17 is a schematic structural diagram of an embodiment of a vacuum sublimation evaporation cold-heat energy separation floor heating device provided by the present utility model.

18 is a schematic structural diagram of another embodiment of a vacuum sublimation evaporation cold-heat energy separation floor heating device provided by the present utility model.

FIG. 19 is a schematic structural diagram of another embodiment of a vacuum sublimation evaporation cold-heat energy separation floor heating device provided by the present utility model.

detailed description

As an example of the vacuum-sublimation evaporation cold-heat energy separation method provided by the present invention, a device as shown in FIG. 1 and FIG. 1a is given.

A sealed container of the device is called a crystallizer 4. The crystallizer 4 constitutes an artificial environment. The crystallizer 4 is provided with a liquid inlet 44, a gas outlet 42, and a solid-liquid mixture outlet. A vacuum sublimation is connected to the gas outlet 42. The evaporation unit is further provided with a stirrer 43 in the crystallizer 4. The separation method is:

Step 1: Establish a vacuum artificial environment in the crystallizer 4, connect the gas outlet 42 on the crystallizer 4 through a vacuum sublimation evaporation unit, that is, a vacuum pump unit 3, and evacuate the crystallizer 4 to make the pressure in the crystallizer 4 It is reduced to 600-100Pa, for example, 128Pa. In the crystallizer 4, raw water is input through the liquid inlet 44. Under the working condition of the vacuum environment, it can be known from the water equilibrium phase diagram shown in FIG. 4 that water is in a triangle region composed of a gas-solid equilibrium line and bao, and the temperature of the crystallizer 4 is in such a region. It can be reduced from 272 to 253K, that is, from -1 ° C to -20 ° C, that is, in the gas-solid two-phase region and biased to the gaseous region. In such an artificial environment, part of the water will evaporate into steam and be pumped away by the vacuum pump unit 3, part of the water will freeze to ice, and part of the ice will be sublimated to become steam. At the same time, a certain amount of water will be stored.

Step 2: Separating the steam and ice, the stirrer 43 provided in the crystallizer 4 breaks the condensed ice, and the ice and a part of the water form an ice slurry, which is discharged from the solid-liquid mixture outlet 49 to output cold energy. The steam is extracted by the vacuum sublimation evaporation unit from the gas outlet 42 into the artificial environment and becomes heat energy output. The stirrer also has two functions. One is to ensure that the ice in the container will not seal the entire liquid surface, to ensure the evaporation and sublimation speed of the solid and liquid on the liquid surface, and the second is to be able to place the artificial environment on the liquid surface of the crystallizer. The cold energy is introduced into the liquid to accelerate icing. For this purpose, the stirrer can be started in step 1.

At the beginning, the liquid can be added to the crystallizer 4 and then the vacuum pump unit 3 is started. Then the liquid starts to evaporate, the steam is pumped away, and the icing is started. The agitator can be started from the beginning. 4 The cold energy above the inner liquid surface introduces liquid. As the liquid surface freezes, the condensed ice is broken by the slurry of the agitator and discharged from the solid-liquid mixture outlet 49. At the same time, the raw water continues to enter the crystallizer.

In this way, steps 1 and 2 are performed alternately and simultaneously. The water successively enters the crystallizer, and the vacuum sublimation evaporator that maintains the ambient pressure in the crystallizer 4, that is, the vacuum pump unit 3, continuously extracts steam from the gas outlet 42. The ice slurry successively discharges the solid-liquid mixture 49 outlet, thereby achieving continuous separation of cold energy and thermal energy.

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

It can be seen from Figure 3 that when the artificial environment, that is, the pressure of the space where the water is located is lowered from 101.3KPa (atmospheric pressure) to below 128Pa, the vaporization temperature equilibrium point of water will be along the gas-liquid (CO) line and the triple point (Point O), the gas-solid (OA) line moves down. That is, from 373K to below 253K (from 100 degrees Celsius to minus 20 degrees Celsius).

In order to realize the separation of cold and heat energy and facilitate utilization, the method of the present invention is to extract heat energy in the form of steam, and separate and store cold energy in the form of ice. The process section is placed at: temperature: 272K-253K (or below) (see line a-b in Figure 3), pressure: 600Pa-100Pa (see o-a in Figure 3). As can be seen from the water equilibrium phase diagram shown in Figure 3, this interval is a solid-gas two-phase region. The gas phase region is a closed triangle region of o-a-b-o. In this area, the solid form of water (ice) can be directly sublimated into steam. Because the pressure is much lower than the saturated vapor pressure of liquid water (see Table 1), under non-equilibrium conditions, the surface water can still exist in liquid form and can be directly converted into vapor by evaporation. The steam sublimated from the ice and the steam evaporated from the water are extracted by the vacuum unit, and the ice slurry is extracted by the ice slurry pump. The separation and transportation of cold and hot energy is realized.

Table 1: Comparison of water temperature and saturated water vapor pressure

温度(K)Temperature (K)	温度(℃)Temperature (℃)	饱和蒸汽压(Pa)Saturated vapor pressure (Pa)
253253	-20-20	128128
258258	-15-15	193193
263263	-10-10	288288
268268	-5-5	423423
270.5270.5	-2.5-2.5	498498
273273	00	611611

The reason why the present invention can break through the current bottleneck of low efficiency of heat pump and refrigeration system based on gas compression technology is to make the energy consumption ratio of the existing mainstream technology to the limit value of COP <8 doubled. The reasons are as follows:

According to the second law of thermodynamics, the entropy increase of an ideal refrigeration cycle is equal to zero, that is, Qa / Ta = Q0 / Tc. (Qa is the amount of heat transferred from the environment; Q0 is the amount of heat transferred from the target fluid; Ta is the temperature of the environment; Tc is the temperature of the target fluid), substituting Q0 + W = Qa, we get (Q0 + W) / Ta = Q0 / Tc, It is deduced that Q0 / W = 1 / (Ta / Tc-1) = εc, εc is called the cooling coefficient, which is the same as the energy efficiency ratio COP called in the industry. It can be seen from the formula that the magnitude of the cooling capacity and input power is only related to the target fluid temperature Tc and the ambient temperature Ta. Using the above formula, it can be calculated through calculation that when the ambient temperature Ta = 35 ° C and Tc = -119 ° C, Ta / Tc = 2. At this time, the cooling capacity = power, that is, εc = 1, or the energy efficiency ratio COP = 1 called in the industry. When the temperature difference Ta-Tc starts to decrease, the COP value starts to be> 1. Since COP = 1 / (Ta / Tc-1), the COP value increases rapidly as the temperature difference decreases. As shown in FIG. 4, when Ta = 35 ° C., Ta-Tc = 44 ° C., COP = 6, and COP data pattern are intercepted.

The relationship between COP and Ta-Tc at Ta = 35 ° C is as follows:

As the temperature difference decreases (approximately the point on the horizontal line), the COP value increases rapidly. (The abscissa is the sequence number and the ordinate is the COP value)

Taking the current mainstream compression technology as an example, when the ambient temperature is Ta = 35 ° C and the target temperature Tc on the cooling end is 0 ° C, the Ta-Tc = 35 ° C at this time, and the COP value can reach 7.8 (see the point on the abscissa in the figure) 10 corresponds to the value on the ordinate). In actual use, the temperature difference of heat transfer needs to be considered, and the heat transfer temperature difference is set to 5 ° C. At this time, the temperature of the cooling end must reach -5 ° C to meet the needs of use. At this time, Ta-Tc = 40 ° C, the COP value can only reach 6.7 (see point 5 on the abscissa in the figure corresponding to the value on the ordinate). That is, the temperature difference increases and the COP value decreases. Considering the efficiency factor of the system, it is consistent with the situation that the mainstream equipment on the market has a COP <6 or so. It can be known that the energy efficiency ratio of compression refrigeration technology is limited by the system structure, the ambient temperature and the requirements of use, and no major breakthrough is possible.

Taking the embodiment of the present invention as an example, the above principles and calculation formulas are also used. Through calculation, it can be obtained that when the ambient temperature Ta = 272K, the temperature difference Ta-Tc = 10 from the target fluid, that is, the ice water surface temperature Tc in the crystallizer. When the temperature is low, the liquid dissipates heat to the environment and freezes. Cooling capacity >> power. The COP value can reach 26 (see figure 30 corresponds to the value on the ordinate). Because in the present invention, the working environment, that is, the artificial environment, and the target fluid, that is, the water in the crystallizer, are highly coincident, that is, in one space. 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, forcing the heat from a low temperature to a high temperature, is an anti-natural process, and the method provided by the present invention is a natural process. vacuum environment, a certain vacuum pressure at which the fluid will naturally evaporation and solidification, the solid after solidification can also be sublimed vapor. The generated steam and solids are removed from the environment separately. Ice is cold energy and can be used. After the pressure of steam is increased, the temperature can be used as heat energy. The energy consumed in this process is only to create a vacuum environment with a set pressure and to remove the solids. Therefore, it is necessary to consume less energy and a higher COP value!

FIG. 5 shows a graph of COP data when Ta = 0 ° C (from Ta-Tc = 39 ° C (Tc = 234K)), COP = 6, and Ta-Tc = 1 ° C. The relationship between COP and Ta-Tc at Ta = 0 ° C is shown in Figure 5:

When Tc = 263K, that is, -10 degrees (point 30 corresponds to the value on the ordinate), COP = 26.3.

The superiority of the present invention is illustrated by the following experimental data and large-scale production efficiency estimates.

This experiment uses the laboratory conditions and small experimental equipment data as the starting point, and uses the analogy method to estimate the output and energy consumption of the industrial production scale, and partially replaces the pilot. However, all process parameters will be based on pilot data.

Table 2 is the experimental data of the state of the brine and the relationship between the final evaporation amount and the amount of ice formation (capacity) in each stage of vacuuming in Experiment 1.

No.1No.1	时间minTime min	样℃Sample ℃	压力PaPressure Pa	状态status
400g400g	00	4.24.2	100000100000	Zh
Zh	3030	44	18001800	剧烈沸腾Intense boiling
Zh	11	-1.1-1.1	460460	结冰Icing
Zh	1:301:30	-2.6-2.6	440440	冰封Frozen
Zh	22	-2-2	440440	停机Downtime
Zh	Zh	Zh	Zh	Zh
剩余盐水gRemaining brine g	冰gIce g	总重Gross weight	损耗(包括蒸汽)Consumption (including steam)	冰/耗Ice / consumption
96.5496.54	263.86263.86	360.4360.4	39.639.6	6.666.66

The experimental results can freeze 6.66Kg of ice per 1Kg of steam, which is basically consistent with the result of the ratio of vaporization heat to latent heat of ice.

Table 2-1: Heat of vaporization of water at different temperatures

It can be seen that 1Kg of water (0 ° C) will completely form ice, which will release 334.4KJ of icing latent heat. According to calculations, it can be known that each 1Kg of steam can absorb about 7Kg of ice.

Table 3 is the experimental data of the state of the brine and the relationship between the final evaporation amount and the amount of ice formation (capacity) in each stage of vacuuming in Experiment 2.

In a 4L / s vacuum equipment experiment, the sublimation evaporation amounts were 39.6g and 38.65g within 2 minutes of starting. The ice making capacity was 263.86g and 226.23g, with an average of 245g. The ratio of ice production to evaporation is 6.66 and 5.85, respectively. Since the heat of evaporation of 0 ° C water is 2501KJ / Kg, and the water of 0 ° C forms ice at 0 ° C, the heat to be released is 334.4KJ / Kg. It can be concluded that the heat of evaporation is about 7.48 times the latent heat of freezing. Considering the loss of cold energy by the experimental equipment, the ratio of the endothermic heat of vaporization to latent heat of ice in the experimental results is very close to 6.25. That is, for every 1Kg of water vapor pumped, 7.48Kg of ice can be frozen.

Comparison of energy efficiency ratio between the present invention and the prior art equipment:

With 4L / s (power 0.55KW) vacuum equipment experiment, calculated at 250g of ice per minute, it can make 15Kg of ice per hour. According to 1kwh = 1000w × 3600s = 3600000J, each ton of ice frozen requires 334400KJ (ie 92.89KWH) of cold energy. After calculation, the energy consumption per ton of ice of this experimental device is 36.67KWH, and the COP value has reached 2.53 (that is, 92.89 / 36.67 = 2.53). It has comparable energy efficiency with mature ice slurry equipment on the market. Take the SF100 ice maker produced by a factory as an example. The unit yield is 28 times that of the experimental equipment (420Kg / 15Kg = 28), but the efficiency is calculated according to the installed power, and the COP is only 1.94. Calculated by operating power, the COP also only reached 2.76, which is close to the experimental data.

The parameters of the ice maker produced by a factory are shown in Table 4:

The parameters of the ice cube machine produced by a factory are shown in Table 5: (the efficiency is much lower than that of the ice pulp machine)

On the basis of the above two experiments, if the vacuum pumping capacity of the vacuum unit is increased by 2500 times, more than 37.5 tons of ice can be produced per hour. The installed capacity of this unit is 135KW. It is calculated that the power consumption per ton of ice is 3.6 degrees, and the COP value can reach at least 26, which should be more than 5 times higher than the current compressor technology.

Calculated by the extraction efficiency of the vacuum unit:

Because the efficiency of ice production mainly depends on the extraction efficiency of the vacuum unit. The comparison is based on a comparison of a 4L / s (power 0.55KW) vacuum unit expanded by 2500 times (power 135KW). The calculation results are shown in Table 6:

It is basically the same as the result obtained by the above calculation method (COP = 26). From another perspective, it has been proved that the system efficiency can be improved by increasing the size of the vacuum unit. In fact, because the form of the vacuum pump used in the experiment is very different from that of large vacuum units, the efficiency of large-scale production equipment will be greatly improved.

A specific operation is as follows: first, a vacuum degree of 600-100Pa required for manufacturing a vacuum evaporation working environment in a water crystallizer. Part of the low temperature raw water in the water crystallizer is evaporated, the water vapor takes away the heat, and part of the remaining water starts to freeze into ice. With the increase of the vacuum degree according to the process requirements, the pressure in the working space of the water crystallizer continues to decrease according to the process parameter requirements, and enters the sublimation area of the ice, which is the normal production pressure parameter area of the process. Since ice is formed on the water surface, the sublimation reaction starts. At this time, the agitator in the water crystallizer is used to successively discharge the ice from the space. The elimination of part of the ice layer provides the conditions for the water below the ice layer to continue to evaporate, and the water vapor that continues to evaporate provides good heat transfer conditions for the sublimation of the ice layer. At this time, the sublimation and evaporation in the water crystallizer are performed simultaneously, water vapor overflows and takes away a lot of heat, and the low-temperature new raw material water is constantly frozen into ice in the water crystallizer. The finished ice is then discharged through the solid-liquid separation equipment to complete the entire ice making and steam production process.

The invention uses physical characteristics such as the phase change principle of water, steam partial pressure, etc., so that the refrigeration and heating processes with large energy consumption can be performed with relatively small energy consumption. The reason is that the present invention uses a method that conforms to the laws of nature, so that the ice and liquid water have a low partial pressure of steam, that is, sublimate and evaporate in an environment with a high degree of vacuum, and then water vapor is pumped away. That is, less energy can be used to complete the separation of cold and hot energy. This technology generates heat while refrigerating, and separates cold energy in the form of ice (solid state) and thermal energy in the form of (gaseous) steam and uses them.

The generated ice can be stored as cold energy. When melting, it can be used as cold energy supply for centralized air-conditioning. The use of ice is a single ore and cannot coexist with other materials. During the crystallization process of water, impurities are automatically excluded to maintain its pure characteristics (such as sea ice). The ice-making process of the present invention can also provide a new technical solution with low energy consumption for seawater desalination, which can greatly reduce the cost of seawater desalination. It can create a new technical approach in the field of seawater desalination and realize the wide application of low-cost seawater desalination technology.

As shown in FIG. 1 and FIG. 1 a, an example of the structure of a crystallizer is provided, which is also a crystallizer used in seawater desalination.

The structure of the crystallizer 4 is: the crystallizer 4 is a tank body, and a pot-shaped partition plate including a bottom and a side wall is provided in the tank body to form a crystal plate 41, which divides the internal space of the tank body into an upper space And the lower space, the vacuuming interface 42 is provided on the tank wall at the top of the tank, and is connected to the vacuum pump unit 3, that is, the multi-stage roots vacuum pump through a pipeline. The agitator 43 is hermetically penetrated from the top of the tank into the crystallization pan 41 placed in the upper space, located at the liquid level in the crystallization pan 41 or at a height within 50 mm below the liquid level; the liquid transport connected to the liquid inlet 44 The pipe 45 is hermetically inserted into the tank body from the side wall of the lower space of the tank body, and communicates with the inside of the crystal plate 41 from a position lower than the side wall of the crystal plate 41. Raw water is introduced into the crystallization pan 41; a waste water outlet 46 is provided on the lower bottom of the crystallization pan 41, and a waste water discharge pipe 47 is connected to the waste water discharge pipe 47, which extends downward and seals out from the bottom of the can body. A drain port 47a is also provided at the bottom of the crystallization tank 4 for draining waste water from the lower space.

The upper part of the side wall of the crystallization plate 41 is provided with an ice outlet 48. The crushed ice communicates with a part of the mixed water slurry and drops from the ice outlet into the lower space of the tank. From the solid-liquid mixture outlet 49 provided on the side wall, The ice slurry outlet 49 is discharged from the tank. An observation hole 40 is also provided in the tank body.

An ice slurry storage tank 6 is further included, and the ice slurry storage tank 6 communicates with the crystallizer 4 so that the pressure in the storage tank 6 is opposite to the pressure in the crystallization tank 4. A stop valve 61 is provided at the ice slurry inlet of the ice slurry storage tank. In this embodiment, the vacuuming port 62 provided on 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 and the crystallization tank 4 can be conveniently made. The pressure is equal. A slurry pump 5 is provided on a pipeline provided between the ice slurry storage tank and the crystallization tank 4 to drive the ice slurry from the crystallizer 4 into the ice slurry storage tank 6. A vent valve 63 is also provided on the top of the ice slurry storage tank 6 so that the ice slurry storage tank can communicate with the atmosphere. An ice slurry discharge port 64 is provided at the bottom of the ice slurry storage tank 6. In actual use, the continuously condensed ice in the crystallization plate 41 in the crystallizer 4 is broken by the agitator 43, and the ice slurry falls into the lower space. A slurry pump 5 sends the ice slurry to the ice slurry storage tank 6, and the ice slurry storage tank 6 is full. Then, close the shut-off valve 61 and open the vent valve 63 so that the pressure in the ice slurry storage tank 6 is balanced with the atmospheric pressure. Then, open the valve on the ice slurry discharge port 64 below, the ice slurry is discharged, and then, it can pass through ice water Separation. Obtained solid ice. One crystallization tank 4 may be connected with several ice slurry storage tanks 6 in parallel. When one ice slurry storage tank 6 discharges ice slurry, another ice slurry storage tank is opened, so that the process of the crystallization tank 4 can be continuously performed.

Of course, several crystallization tanks can also be set up to form a system to increase the output of cold and heat energy separation.

The device can also include two heat exchangers, one is the steam heat exchanger 2 using the heat energy of the steam, and the other is the pre-cooling of the raw water entering the crystallization tank 4 to cool the raw water to 1-4 degrees Celsius. Heater 2 '.

During use, the raw water passes through a raw water heat exchanger 2 ', and the ice water in the ice slurry is used for cooling. After the raw water is cooled, the temperature is reduced to 1-4 ° C. 41. The ice formed under high vacuum is broken by the agitator 43. The water-containing crushed ice is discharged from the ice outlet 48 on the upper side wall of the crystallization plate 41 to the lower space of the crystallization tank 4, and then from the ice slurry outlet 49. It is transported to the ice slurry storage tank 6 by the mud pump 5, and the ice slurry is used as cold energy output from the ice slurry storage tank 6. The crystallization tank obtains a set pressure through the suction of the multi-stage Roots vacuum pump 3, and at the same time, the extracted steam is sent to the steam heat exchanger 2. After the pressure is increased, the temperature of the steam rises. The heat exchange of the heating water at ℃ can raise the temperature of the heating water to about 70 ° C, thereby outputting thermal energy. The steam at the outlet of the steam channel of the steam heat exchanger 2 is extracted by another vacuum pump 1 and discharged into the atmosphere.

As shown in FIG. 1b, the crystallizer may also have such a structure, and the crystallizing disc 41 and related structures in the crystallizer 4 shown in FIG. 1 and FIG. 1a are eliminated. The inside of the crystallizer 4 is a whole space. In the crystallizer 4 'shown in FIG. 1b, the height of the liquid inlet 44 is lower than the ice slurry outlet 49, and the ice slurry outlet 49 is within 50 mm below the set liquid level. The position of the stirring blade 43 is preferably such that half of the stirring blade 43 is above the liquid surface and the other half is below the liquid surface. Such a design can make the role of the agitator well.

The crystallizer shown in Figure 1b is more suitable for pure water or liquids with less impurities, because such a liquid freezes harder when the cold and heat energy is separated, and the crystallizer with such a structure has a relatively easy discharge of ice slurry. The crystallizer shown in Figure 1a is suitable for liquids with higher impurity content. Such liquids have softer ice and the ice slurry is generally like soft mud. Use a crystallizer with a crystallizing plate. It is more convenient for the crystallization tray to fall into the lower space, separate from the liquid, and then discharged from the ice slurry outlet.

The vacuum sublimation evaporation cold and heat energy separation device provided by the present invention further includes a centralized control system, as shown in FIG. 2. The centralized control system controls the operation of the following devices: 1. The start of the vacuum sublimation evaporation unit, that is, the multi-stage roots vacuum pump. Close, speed to control the pressure in the crystallizer, 2. Opening and closing of the agitator in the crystallizer and the rotation speed, but also to control the opening and closing and opening of the valves on each inlet and outlet, 3. On each inlet and outlet on the ice slurry storage tank Valve opening and closing and opening degree. The larger arrow in Figure 2 shows the control relationship of the centralized control system for each part of the device, and the smaller arrow shows the direction of logistics in the device.

It can be known from the examples that the output heat energy of the method, that is, the steam extracted by the multi-stage Roots vacuum pump can directly produce hot water at 60 ° C-70 ° C. For every 1 ton of ice, about 2 tons of 60 ° C hot water can be produced. . Calculating only based on the actual refrigeration COP = 12 of this technology, for each ton of ice produced, the power consumption will be less than 7.75 degrees, and the refrigeration energy consumption will be reduced by at least half. Adding hot water produced, the total energy consumption can be reduced by 75%, that is, 25% of the energy consumption when COP = 6 (while the COP value of ice machines currently on the market is generally lower than 3). Central heating and hot water for bathing can be provided within a certain range.

FIG. 6 is a process flow chart of an embodiment of the vacuum sublimation evaporation frozen seawater desalination provided by the present utility model. In the device of this embodiment, three desalination units are included, and each desalination unit includes a cold-heat energy separation device 01, an ice slurry dehydrator 02, an ice slurry pool 03, and an ice slurry melter 04. Each cold and heat energy separation device 01 includes several crystallizers and a vacuum pump unit. A vacuum pump unit is connected to the plurality of crystallizers to reduce the pressure in each crystallizer to a set low pressure state.

Seawater enters each desalination unit in sequence. In the high vacuum environment of the crystallizer in the cold and heat energy separation device of each desalination unit, it is separated into steam and ice-water mixture. The ice-water mixture is divided into ice by an ice slurry dehydrator. And water, the ice slurry is then melted into water by an ice-melt melter, and the water obtained through the first desalination unit A1 has a reduced salt content, but has not yet reached the standard of fresh water, and requires second desalination. This is called secondary raw water. The secondary raw water enters the second desalination unit A2. It also performs cold and heat energy separation in a high vacuum environment to obtain water. The salt content continues to decrease, but it has not yet reached the fresh water standard. This water is called tertiary raw water, and the tertiary raw water passes through the third desalination unit A3, and finally meets the standard fresh water.

In each desalination unit, the key to reducing the salt content in water is to separate the cold and heat energy in a high-vacuum crystallizer.

The method for desalination of seawater using cold and heat energy separation device is:

Referring to FIG. 1 and FIG. 1 a, a vacuum artificial environment is established in the crystallizer 4. A vacuum pump unit 3 is connected to a gas outlet 42 on the crystallizer 4 as a steam outlet 42. A vacuum is applied to the crystallizer 4 so that the The pressure is reduced to 600-100Pa, for example, 128Pa. In the crystallizer 4, seawater is input through the liquid inlet 44 that is the raw water inlet 44. Under the working condition of the vacuum environment, it can be known from the water equilibrium phase diagram shown in FIG. 3 that water is in a triangular region composed of a gas-solid equilibrium line and bao, and the temperature of the crystallizer 4 is in such a region. It can be reduced from 272 to 253K, that is, from -1 ° C to -20 ° C, that is, in the gas-solid two-phase region and biased to the gaseous region. In such an artificial environment, part of the seawater will evaporate into steam and be pumped away by the vacuum pump unit 3, part of the seawater will solidify into ice, and part of the ice will be sublimated into steam, and at the same time, a certain amount of water will be stored. The condition of seawater will be different because of its composition. However, under low pressure, it still basically conforms to the nature and law of ordinary water, and under suitable low pressure, crystallization will also be achieved. According to the characteristics of ice, that is, when seawater freezes, salt is excluded from ice crystals. The longer the ice crystals form, the less salt is. Therefore, in the crystallizer 4, the seawater is frozen under a low-pressure environment, and an ice slurry with reduced salt content can be obtained.

Next, the steam and ice are separated. The stirrer 43 provided in the crystallizer 4 breaks the condensed ice, and the ice and a part of the water form an ice-water mixture, which is discharged from the solid-liquid mixture outlet 49, that is, the ice-water mixture outlet 49. As the cold energy output, the steam is extracted by the vacuum pump unit 3 from the steam outlet 42 into the artificial environment and becomes the thermal energy output. The stirrer also has two functions. One is to ensure that the ice in the crystallizer will not seal the entire liquid surface, so as to ensure the evaporation and sublimation speed of the solid and liquid on the liquid surface. Cold energy from the environment is introduced into the liquid, accelerating freezing. To this end, the stirrer can be started when raw water enters the crystallizer.

At the beginning, seawater can be added to the crystallizer 4 and then the vacuum pump unit 3 is started. Then the seawater starts to evaporate, the steam is pumped away, and ice formation begins. The agitator can be started from the beginning. After being broken, it is discharged from the ice-water mixture outlet 49, and at the same time, raw water continuously enters the crystallizer.

In this way, seawater successively enters the crystallizer, and the vacuum pump unit 3 that maintains the ambient pressure in the crystallizer 4 continuously extracts steam from the steam outlet 42 and the ice-water mixture is successively discharged from the ice-water mixture outlet 49, thereby achieving desalination and separation of seawater.

In order to increase the degree of desalination of seawater, after the first desalination unit is completed, the second desalination and third desalination are performed. The equipment of the second desalination unit and the third desalination unit may be exactly the same as the structure of the first desalination unit. . The fresh water drawn from the ice melter in the first desalination unit may also be referred to as secondary raw water, and is introduced into the crystallizer in the cold-heat energy separation device in the second desalination unit. The fresh water from the second desalination unit is also referred to as 3 times of raw water, and is then introduced into the crystallizer in the cold and heat energy separation device in the third desalination unit. Finally, fresh water that meets national standards can be obtained.

The ice slurry dehydrator 02 is a tank body on which an inlet and an outlet are provided, and the inlet is connected to the ice-water mixture outlet 49 of the crystallizer 4 in the cold-heat energy separation device 01;

The ice slurry pool 03 is a container on which an inlet and an outlet are provided, and the inlet is connected to the outlet of the ice slurry dehydrator;

The ice melter 04 is a container provided with an inlet and an outlet. The inlet is connected to the outlet of the ice slurry pool 03, and the outlet is the fresh water outlet of the desalination unit. The container of the ice melter 04 is provided with heating. Device.

The heating device may also be a coil heater, and steam or condensed hot water extracted from the crystallizer may be passed through the coil.

The key device for desalination of seawater according to the present invention is a technology for separating and utilizing cold energy and thermal energy by using a high-efficiency vacuum sublimation evaporation unit. It is a new technology application based on the second law of thermodynamics.

An embodiment of the structure of a crystallizer is provided as shown in FIG. 1a. Its structure is as described above.

The upper part of the side wall of the crystallization plate 41 is provided with an ice outlet 48. The crushed ice and a part of the ice-water mixture mixed with water fall from the ice outlet into the lower space of the tank body, and the solid-liquid mixture outlet 49 provided on the side wall Here the ice-water mixture outlet 49 is discharged from the tank.

It also includes an isobaric ice slurry storage tank 6, as shown in FIG. 1, the isobaric ice slurry storage tank 6 is in communication with the crystallizer 4, and the structure of the ice slurry storage tank 6 is as described above. In this embodiment, the vacuum extraction port 62 provided on the top of the isobaric ice slurry storage tank 6 is also connected to the vacuum pump unit 3 of the multi-stage roots vacuum pump. The pipeline provided between the isobaric ice slurry storage tank and the crystallizer 4 is provided. A slurry pump 5 drives the ice-water mixture from the crystallizer 4 into the isobaric ice slurry storage tank 6. In actual use, the continuously condensed ice in the crystallization plate 41 in the crystallizer 4 is broken by the agitator 43. The mixture of ice and water falls into the lower space of the crystallizer 4, and the ice-water mixture is discharged through the outlet. The pump 5 is sent to the isobaric ice slurry storage tank 6. After the isobaric ice slurry storage tank 6 is full, the shut-off valve 61 is closed and the vent valve 63 is opened, so that the pressure in the isobaric ice slurry storage tank 6 is balanced with the atmospheric pressure, and then Open the valve on the ice slurry discharge port 64 below, and the ice-water mixture is discharged. One crystallizer 4 may be connected with several isobaric ice slurry storage tanks 6 in parallel. When one isobaric ice slurry storage tank 6 discharges ice slurry, another isobaric ice slurry storage tank is opened, so that the process of the mold 4 can be continuously performed. The ice water mixture discharged from the isobaric ice slurry storage tank 6 enters the ice slurry dehydrator, which is a tank body provided with an inlet and an outlet. The inlet is connected to the ice water mixture outlet 49 of the crystallizer, and the outlet is provided at the At the set liquid level of the ice slurry dehydrator 02, the ice generally floats on the liquid surface and is conveniently discharged from the outlet. The discharged broken ice with some water becomes ice slurry, which is then introduced into the ice slurry pool 03 for storage. The ice slurry pool 03 is provided with an inlet and an outlet, the inlet is connected to the outlet of the ice slurry dehydrator 02, and the outlet is further connected to an ice slurry melter 04, which is a container on which an inlet and The outlet is connected to the outlet of the ice slurry pond 03, and the outlet is the fresh water outlet of the desalination unit. A heating device is provided in the container of the ice slurry melter. The heating agent in the heater may be steam or hot water which is drawn out from the vacuum pump unit 3 and is boosted and heated. If the salt water content of the fresh water discharged from the ice melter does not meet the requirements, it will be introduced into the second desalination unit.

The crystallizer in the cold and heat energy separation device may be a system composed of several crystallizers to increase the output of cold and heat energy separation.

A cold and heat energy separation device includes two heat exchangers. One is a steam heat exchanger 2 that uses steam thermal energy. As mentioned above, it is used in a subsequent ice melter, which uses the heat of steam to melt the ice slurry. . The other is a raw water heat exchanger 2 'that cools the raw water entering the crystallizer 4 in advance to reduce the temperature to 1-4 degrees Celsius.

The crystallizer for seawater desalination may also have a structure as shown in FIG. 1b. In the crystallizer 4 ′ shown in FIG. 1b, the height of the raw water inlet 44 introduced into the seawater is lower than the ice slurry outlet 49, and the ice slurry outlet 49 is set. Within 50mm below the liquid surface. The position of the stirring blade on the agitator 43 is preferably such that half of the blades are above the liquid surface and the other half is below the liquid surface. Such a design can make the role of the agitator well.

The mold shown in Fig. 7 is an improvement on the mold shown in Fig. 1b. The improvement mainly lies in the following two points. One is that a heater 4-2 is added to the space above the liquid level of the crystallizer 4-1. The heater 4-2 passes a relatively hot medium to heat the steam. This can increase the flow rate of steam, accelerate the evaporation process, and help improve the separation efficiency of cold and heat energy.

As shown in FIG. 9, the heater 4-2 is a heating coil, and the nozzles at both ends of the heating coil are hermetically extended out of the crystallizer to connect a heating medium supply device. The inlet of the heating coil can be connected to the steam outlet of the vacuum pump unit, so as to use the steam with reduced pressure and temperature as the heating medium.

The heater 4-2 may be a plurality of heating coils arranged up and down.

The second improvement point is the structure of the raw water inlet device. As shown in FIG. 7 and FIG. 8, a liquid supply tray 4-3 is set in the tank of the crystallizer 4-1, and the liquid supply tray 4-3 is set in the tank. In the lower part, the liquid supply tray is a 4-3 shower, the liquid spray holes are set upward, and the liquid inlet hole in the middle of the bottom is connected to the raw water inlet 44 on the crystallizer tank through a pipeline; the ice-water mixture outlet 49 is set above the raw water inlet 44 so that the liquid supply tray 4-3 is placed below the liquid level in use.

The stirring device 43 includes a paddle, which is arranged on a stirrer shaft, the stirrer shaft sealingly protrudes from the tank body and connected to a power source; the paddle blade is located higher than the ice-water mixture outlet 49 and is set in the tank body At the liquid level, or at a height less than 50mm below the set liquid level, the ice layer formed on the liquid surface is broken.

As shown in Figure 6, there are 3 desalination units, and the raw water inlet in the second desalination unit is the secondary raw water inlet, which is connected to the freshwater outlet in the first desalination unit, ... 3 raw water imports.

If it is extended, the vacuum sublimation evaporation and freezing seawater desalination equipment has n desalination units. The raw water inlet of the first desalination unit enters the seawater, and the raw water inlet of the nth desalination unit is the raw water inlet for n times.

It can be known from the examples that the output heat energy of the method, that is, the steam extracted by the multi-stage Roots vacuum pump can directly produce hot water at 60 ° C-70 ° C. For every 1 ton of ice, about 2 tons of 60 ° C hot water can be produced. . Calculating only based on the actual refrigeration COP = 12 of this technology, for each ton of ice produced, the power consumption will be less than 7.75 degrees, and the refrigeration energy consumption will be reduced by at least half. Adding hot water produced, the total energy consumption can be reduced by 75%, that is, 25% of the energy consumption when COP = 6 (while the COP value of ice machines currently on the market is generally lower than 3). If you do not use hot water to melt ice, you can also provide central heating and hot water for bathing in a certain range.

The energy-saving effect of the invention is very obvious, and the development potential is huge. The COP that can achieve equipment cooling is greater than 26 or even higher. In addition, the cost of the equipment of the present invention is relatively low, and the payback period of equipment investment will be greatly reduced.

The seawater desalination process that follows the existing technology has been fully developed in terms of technical maturity and operating costs. Although there is still room for reduction in operating costs and equipment costs, the reduction is unlikely to be too great. . The cold-heat energy separation of seawater using the low-pressure environment provided by the present invention, that is, the vacuum sublimation evaporation freezing seawater desalination method, provides a new method and approach for the development of seawater desalination. Since this method uses only electrical energy, it also provides new possibilities for a significant reduction in the cost of desalination.

The cost list for several desalination methods is as follows:

From the cost list of several desalination methods, it can be seen that the energy cost of the cost of the sublimation evaporative freezing method accounts for 72% of the total cost, and the other cost ratios are lower or similar to other technologies. This cost structure provides greater space for future cost reductions. The biggest technical advantage of sublimation evaporative freezing is energy saving and high efficiency. The current calculations are only conservative numbers, and there is still a lot of room for energy savings.

Using the energy separation method of seawater desalination technology, the by-products of seawater desalination will become a huge profit point for the project. This includes making sea salt, supplying cooling and heating to surrounding residents, and generating income from steam. The cost of desalination can be reduced to a secondary position. This technology will form a major impetus for the development of current technology-related industries.

Another application equipment energy supply station of the present invention is to use the stable steam flow generated by the cold and heat energy separation technology as an energy supply for low-temperature power generation. Because of the high efficiency of water vapor generation and low energy consumption, electrical and thermal energy can be provided at a very low cost, and even cold energy can be provided. At the same time, due to the use of a thermal energy separation device of a modified unit using a cold-heat energy separation device, the lower-quality thermal energy that was originally unavailable for low-temperature power generation can be well utilized, which greatly improves the energy utilization efficiency.

The power generation medium used by the generator of the invention provides steam through a cold and heat energy separation device, and the sealed container is a key part of a vacuum sublimation evaporation cold and heat energy separation device, that is, it has a high degree of vacuum inside, and the water in the Evaporation and vaporization can be performed at low temperatures, and steam with a higher temperature is extracted by the vacuum pump unit, which is used to heat the power generation medium in the low-temperature generator set. Vacuum sublimation evaporation cold and heat energy separation technology is a technology that uses vacuum technology and the physical properties of water to realize the separation, storage and use of cold and heat energy.

Due to the use of a high-efficiency vacuum sublimation evaporation technology different from the compressor technology, without using other refrigeration media and supporting refrigeration medium circulation systems, the energy transfer link is reduced, the system efficiency is improved, and the efficiency is greatly improved, so that the system The overall efficiency is greatly improved, and the COP value can reach at least 18 or more. At the same time, the use of phase change morphology of water (steam and ice) as the carrier of energy and the application medium makes the separation and use of cold and heat energy more convenient. The invention seeks a low-energy-consumption technology to partially replace the traditional compressor technology, and achieves energy saving and consumption reduction. Vacuum sublimation evaporation cold and heat energy separation technology can provide a new solution. The use of a high-efficiency vacuum sublimation evaporation unit to separate and utilize cold and thermal energy is a new technology application based on the second law of thermodynamics. Utilizing physical characteristics such as the phase change principle of water and the partial pressure of steam, the refrigeration and heating processes that consume large amounts of energy are used in a way that conforms to the laws of nature, so that ice and liquid water have a higher vacuum and lower temperature. The environment sublimes, evaporates, and immediately removes water vapor. Separate cold and hot energy with less energy. This technology generates heat while refrigerating, and separates cold energy in the form of ice (solid state) and thermal energy in the form of (gaseous) steam and uses them. For energy supply stations, the degree of vacuum in the sealed container can also be set low, that is, the water in the sealed container does not necessarily form ice, but it only needs to reach low temperature for evaporation.

Furthermore, the exhaust steam and condensed hot water after power generation are reused and enter the sealed container inlet of the original or secondary cold-heat energy separation equipment to separate the thermal energy from the water and generate new water vapor. . Since the evaporation efficiency of water at higher temperatures is several times higher than the evaporation efficiency of water at lower temperatures, the energy spent to obtain the same amount of high-quality thermal energy (water vapor) is only a fraction of that at low temperatures. This part of the new steam energy can be reused. Using hot water after power generation, if two sets of cold and heat energy separation devices are used, different vacuum degrees are set in the two sealed containers. The first one enters the sealed container of room temperature water and sets a higher vacuum degree, and the second one is twice. The sealed container can be set to a lower vacuum level because of hot water.

In the aforementioned cold and heat energy separation device, another cold and heat energy separation device of the second stage is added. The first stage cold and heat energy separation device is set to a higher vacuum degree, and the heat energy is separated by the crystallization heat of water. The secondary cold and heat energy separation device is set to a lower vacuum degree, which mainly improves the evaporation efficiency, and obtains a large amount of high-quality thermal energy steam for low-temperature power generation devices, which can also improve the power generation efficiency.

As shown in FIG. 10, an embodiment of a distributed energy supply station for a vacuum sublimation evaporation cold and heat energy separation method provided by the present invention includes a low temperature power generation device and a cold and heat energy separation device.

The low-temperature power generation device is a prior art and includes a low-temperature power generator set, which includes a low-temperature power generator 1, a power-generating medium evaporator 2 and a power-generating medium condenser 3,

The low-temperature generator 1 is a low-temperature steam generator, specifically a screw expansion generator, which has a casing, and a screw is arranged in the casing. The casing is provided with a power-generating medium steam inlet 11 and a power-generating medium exhaust steam outlet 12.

The power generation medium evaporator 2 is a partition-type heat exchanger, and a power generation medium inlet 21 and a power generation medium steam outlet 22 are provided on the power generation medium evaporation channel. The power generation medium steam outlet 22 is connected to the power generation medium steam inlet 11 of the low-temperature generator 1 to generate electricity. The medium evaporator 2 is further provided with a heating steam inlet 23 and a waste steam outlet 24 to communicate with the heating steam passage.

The power generation medium condenser 3 is a partition-wall heat exchanger, and a power generation medium exhaust steam inlet 31 and a power generation medium condensate outlet 32 are provided on the power generation medium condensation passage. The power generation medium exhaust steam inlet 31 is connected to the low temperature generator 1 The steam outlet 12 and the power generation medium condenser 3 are further provided with a cooling water inlet 33 and a cooling water outlet 34 to communicate with the cooling water channel.

The power generation medium steam outlet 12 of the low-temperature generator 1 is connected to the power generation medium depleted steam inlet 31 of the power generation medium condenser 3.

The cold and heat energy separation device includes a separation device 4 and a vacuum pump unit 5,

The separation device 4 includes a sealed container, which is equivalent to the aforementioned crystallizer 4. In FIG. 10, the sealed container includes a sealed tank 4-1, and a raw water inlet 44 is provided on the tank 4-1. A steam outlet 42 is provided on the top of the tank 4-1, and the vacuum pump unit 5 is connected to the steam outlet 42. A waste water discharge port is provided on the bottom of the tank 4-1; a liquid supply tray 4-3 and a stirrer are provided in the tank 4-1. 43 and the heater 4-2; the liquid supply tray 4-3 is set at the lower part of the tank 4-1, and is located below the set liquid level. The liquid supply tray is a 4-3 shower, with the liquid spray holes facing upwards. The liquid inlet at the bottom is connected to the raw water inlet 44 on the tank 4-1 through a pipeline; the heater 4-2 is a heating coil. Located above the set liquid level. Both ends of the heating coil 4-2 are hermetically extended out of the tank 4-1 to connect the heating medium supply device. The inlet of the heating coil can be connected to the steam outlet of the vacuum pump unit, so as to use the steam with reduced pressure and temperature as the heating medium. The installation of the heating coil 4-2 is favorable for generating more steam under reduced pressure and temperature.

The heating coil 4-2 may also be connected to the cooling water outlet of the power generation medium condenser, or to the exhaust steam outlet of the power generation medium evaporator, or to the exhaust steam outlet of the low-temperature generator.

The vacuum pump unit 5 is a multi-stage vacuum pump. The suction port 51 of the first stage is connected to the steam outlet on the sealed container, and the suction port of the subsequent stage is connected to the exhaust port of the previous stage. The air extraction volume is gradually reduced, so that the pressure of the extracted steam is gradually increased to atmospheric pressure, and a high temperature steam outlet 52 is provided in the last stage.

The high-temperature steam discharge port 52 of the vacuum pump unit 5 is connected to the heating steam inlet 23 on the power-generating medium evaporator 2 in the power generating device through a pipeline, and is extracted from the sealed container and gradually increased to a high temperature of atmospheric pressure by the vacuum pump unit 5 The steam heats the power generation medium R245fa in the medium evaporation channel in the power generation medium evaporator 2 to vaporize it.

The vacuum sublimation evaporation cold and heat energy separation method distributed energy supply station shown in FIG. 10 provided by the present invention can operate as follows:

Start the vacuum pump unit 5 so that a set vacuum is generated in the tank 4-1 of the sealed container, and at the same time, raw water is added to the tank 4-1. The raw water is vaporized at a low temperature in the tank 4-1 due to the vacuum environment. Water vapor is drawn out with the vacuum pump unit 5, and with the multi-stage vacuum pump's suction capacity gradually reduced from front to back, the steam pressure of the drawn water vapor is gradually increased to atmospheric pressure, and the temperature of the steam is increased to, for example, 100 At about ℃, the steam is passed into the power generation medium evaporator in the low-temperature power generation device, which is used as a heating medium to heat the power generation medium to vaporize it. The exhaust steam of the power generation medium is discharged from the low-temperature generator and enters the power-generation medium condenser to be cooled and liquefied, and then enters the storage tank or directly enters the power-generation medium evaporator to be vaporized and returned to the low-temperature generator. In the energy supply station, the steam used to heat the vaporized power generation medium used by the low-temperature generator uses water vapor generated by the vacuum sublimation evaporation cold and heat energy separation equipment, and the production of this water vapor uses a special cold and heat energy Separation method, so its energy consumption is small.

This energy supply station uses vacuum sublimation evaporation cold and heat energy separation technology to separate energy in water into energy that can be conveniently used and used. That is, the latent icing heat and sensible heat energy in water at normal temperature and below are separated into thermal energy (water vapor) and cold energy (ice), and the sensible heat in water at normal temperature and below 100 ° C is separated into high-quality thermal energy (water vapor). The energy supply station uses low-temperature power generation technology to generate electricity using water vapor energy, and uses an ice-water mixture as a cold source to improve the power generation efficiency of the low-temperature generator.

The following specifically analyzes the high-efficiency mechanism of the cold-heat energy separation device provided by the present invention:

This energy supply station is a technology that uses a high-efficiency vacuum sublimation evaporation unit to separate cold and heat energy and uses it in low-temperature power generation. It is a new technology application based on the second law of thermodynamics.

The reason why the present invention can break through the current bottleneck of low efficiency of heat pump and refrigeration system based on gas compression technology is to make the energy consumption ratio of the existing mainstream technology to the limit value of COP <8 doubled. The reason is as follows: Water in nature contains thermal energy, that is, it contains sensible heat and latent heat of freezing. If the thermal energy (sensible heat and latent heat of icing) contained in 1 ton of 20 ° C water is separated and used to heat 1 ton of 0 ° C water, the water temperature can be raised to 100 ° C. Vacuum sublimation evaporation cold and heat energy separation technology separates energy in water at room temperature into heat energy (water vapor) and cold energy (ice), and makes further use of these two energy forms. Steam can be used as a source of energy for low-temperature power generation (similar to a geothermal source), or as a source of heat for winter heating. It provides a cheap heat source for solving the central heating of large buildings and residential areas. Ice is the cheapest and most efficient form of storing cold energy. It can be used for the supply of cold sources in centralized air-conditioning places and residential districts. It can partially replace large and medium-sized chillers with high energy consumption. At the same time, using the physical properties of water, the seawater is subjected to the icing process during the separation of cold and heat energy, the desalination of seawater is completed, and the second water source is developed at low cost. Therefore, the emergence of vacuum sublimation evaporation cold and heat energy separation technology will provide new ways and efficient and cheap methods for solving the problems of energy and water sources. In order to further improve the production efficiency of water vapor in the sealed container, it is a good measure to stir the water in the tank by the agitator 43. In addition, the water in the tank can be cold-boiling by using a shower-type water inlet method as shown in FIG. 10. Specifically, a liquid supply tray 4-3 is provided, and the lower part in the tank body 4-1 is set lower than the set liquid level height in the sealed container. The liquid supply tray 4-3 is a shower, spray The liquid hole is set upward, and the liquid inlet hole at the bottom is connected to the water inlet 44 through a pipeline.

As shown in FIG. 16, the evaporation amount of water at different temperatures is shown. From this figure, it can be seen that the evaporation rate of water increases with increasing temperature. Moreover, in different temperature intervals, as the temperature rises, the evaporation rate of water shows an accelerated growth trend, and its growth rate is a linear relationship of non-proportional growth.

It can be seen from this that in order to further increase the extraction rate of water vapor in the sealed container, it is advantageous to heat the space on the water surface in the sealed container. For this reason, it is an effective measure to provide the heater 4-2 in the space above the water surface of the sealed container in the aforementioned embodiment.

After one generation of steam, more than 80% of the energy remains in the steam. It exists in the exhaust steam discharged from the generator. Therefore, the exhaust steam can be used again for another power generation or multiple power generation. , So that the energy separated by cold and heat energy separation technology can be fully utilized.

To this end, it can be designed as follows: the low-temperature generator set includes at least two of the low-temperature generators connected in series, that is, the exhaust outlet of the steam generation medium of the previous low-temperature generator is connected to the pipeline by a low-temperature power generation The generator ’s power generation medium steam inlet and the last low temperature generator ’s power generation medium exhaust steam outlet are connected to the power generation medium exhaust steam inlet of the power generation medium condenser through a pipeline.

Based on the low-temperature generator's primary power generation efficiency of 8% -12%, the energy utilization rate after secondary or multiple power generation will reach more than 24%. For example, from the perspective of energy conservation, the energy released by condensing one ton of water vapor to 100 ° C water is 2260000KJ, which is equal to 630KWH. Considering the loss of the power generation system, the power generation efficiency can reach 50%.

Furthermore, as shown in FIG. 16, according to the evaporation rate graphs of the still water at different temperatures, it can be seen that when the water temperature exceeds 25 ° C., the evaporation rate starts to show an accelerated growth trend. According to this property, cold and heat energy separation technology can be divided into low temperature cold and heat energy separation technology and high temperature heat energy separation technology. The goal of separating energy using low-temperature cold-heat energy separation technology is the latent heat of water crystallization. This part of the heat energy is equal to the heat energy required to heat 20 ° C water to 100 ° C. The high-temperature thermal energy separation technology can efficiently separate the sensible heat energy in water at 20 ° C to 100 ° C to generate high-quality energy steam. The energy separation products in the above different temperature intervals all have water vapor, but the water vapor generated in different temperature intervals has different efficiency. Vacuum sublimation evaporation cold and heat energy separation technology is to efficiently separate the sensible heat and latent heat of freezing in water below normal temperature, that is, to use a small amount of energy consumption to separate several times the input energy. The high-temperature energy separation is a technology that can be obtained by using the latent heat of crystallization separated by the low-temperature energy separation technology to heat the raw water and make the thermal energy (water vapor) with a small amount of energy consumption (<10KWH / ton steam). Since 1 ton of steam at 100 ° C condenses into 100 ° C water, the heat released is 2260000KJ, which is equal to 630KWH. According to the calculation of 10% power generation efficiency, the power generation capacity is 63KWH, which is much higher than the energy used to separate the 10KWH / ton of water vapor. This provides conditions for making full use of the latent heat of crystallization. Use, greatly improve the efficiency of power generation.

According to such a theory, the water added to the tank 4-1 of the sealed container can be heated, that is, a preheater is connected to the raw water inlet 44 of the sealed container, and the preheater enters the seal through hot water or hot steam. The container of water is heated. The heat source of the preheater can be an external heat source, and the heat energy of the energy supply station itself can be used.

As shown in FIG. 13, the preheating heat source can be steam extracted by a vacuum pump unit, that is, a pipe is provided on a pipeline for transmitting heating steam to the power generation medium evaporator 2 and is connected to the preheater. The water discharged from the preheater can be added to the sealed container from the raw water inlet 44. Of course, it can also be vented or vented.

As shown in FIG. 14, the preheating heat source may be cooling water for cooling the power generating medium in the power generating medium condenser 3, that is, a branch pipe is connected to the cooling water outlet 34 of the power generating medium condenser 3, and the branch pipe is connected to the preheater. The water discharged from the preheater can be added to the sealed container from the raw water inlet 44. Of course, it can also be vented or vented.

As shown in FIG. 15, the preheating heat source may also be steam or hot water after heating the power generation medium, that is, a branch pipe is connected to the waste steam outlet 24 of the power generation medium evaporator 2, and the branch pipe is connected to the preheater. The water discharged from the preheater can be added to the sealed container from the raw water inlet 44. Of course, it can also be vented or vented.

In this way, additional energy consumption is not required, and by increasing the temperature of the raw water, the water vapor output rate is greatly increased, and the energy saving efficiency of the energy supply station is further improved. The power generation medium condenser 3 is also connected to a liquid reservoir, not shown in the figure. The liquid receiver is provided with a liquid inlet and a liquid outlet, and the liquid inlet is connected to the medium condenser outlet 32 on the power generation medium condenser 3, The liquid outlet is connected to the medium evaporator inlet 21 on the power generation medium evaporator 2, and a liquid pump 6 is provided on the pipeline therebetween.

An oil separator 7 is provided on the pipeline of the medium steam outlet 12 of the low-temperature generator 1 to separate the power generation medium from the lubricating oil. The separated power generation medium is sent to the power generation medium condenser 3 through the pipeline, and the separated lubricating oil is It is returned to the generator 1 by the oil pump 8. Referring to FIG. 5, if the temperature of raw water is increased to 40-70 ° C., the amount of steam produced per hour can be increased by 2-3 times.

From this, two preferred embodiments can be produced:

One is: a pipeline connected to the cooling water outlet 34 of the power generation medium condenser 3 in the low-temperature generator set is arranged on the water inlet of the sealed container. The second is that a water inlet 44 of the sealed container is provided with a pipeline to connect the exhaust steam outlet 24 of the power generation medium evaporator 2 in the low-temperature generator set. In these two solutions, the high-temperature cooling water in the power generation device or the exhaust steam that also contains thermal energy is directly passed into a sealed container for cold-heat energy separation.

Further, as can be seen from FIG. 16, the technology and equipment for vacuum sublimation evaporation cold and heat energy separation can be subdivided into the following two types:

① Low-temperature cold-heat energy separation technology, the goal of its separation energy is the latent heat of crystallization of water.

② High-temperature thermal energy separation technology, the goal of separating energy is sensible heat in hot water. The separated latent heat is used to heat the raw material water at a temperature above normal temperature, and the thermal energy of the heated raw material water can be used to separate the water vapor with only a small amount of energy (<10KWH / ton steam), so as to adapt to the use of low temperature power need.

To this end, a cold and heat energy separation device can be added to the energy supply station:

As shown in FIG. 11, the foregoing cold-heat energy separation device is a low-temperature cold-heat energy separation device, which is used to separate sensible heat and latent heat of freezing in normal temperature water. An ice slurry outlet 4-4 is also provided on the tank body 4-1 of the sealed container, and a storage tank 53 is connected to the high-temperature steam discharge outlet of the first-stage cold-heat energy separation device; A high-temperature cold-heat energy separation device is also included between the separation device and the low-temperature power generation device, which is used to separate sensible heat in hot water below 100 ° C. It is called a secondary cold-heat energy separation device and includes a secondary sealed container. ', The secondary sealed container 4' is provided with at least one high temperature water inlet 44 'and a high temperature steam outlet 42', and the high temperature water inlet 44 'is connected to the high temperature steam outlet 52 of the primary cold and heat energy separation device A storage tank connected to the high-temperature steam outlet 42 'on the secondary sealed container 4' is connected to a secondary vacuum pump unit 5 ', and a final-stage steam exhaust port of the secondary vacuum pump unit 5' is connected to the low-temperature power generation through a pipeline. Heating and steaming on the power generation medium evaporator 2 in the device Entrance 24.

In this embodiment, a high degree of vacuum can be set in the first-stage cold-heat energy separation device, a part of the raw water is frozen, the ice slurry is discharged from the ice slurry outlet, and the latent heat released by the ice is converted into steam and pumped by a vacuum pump unit. Then the steam, or hot water, may be passed into the sealed container in the secondary cold and heat energy separation device as raw water. The vacuum degree is set low, and the hot water can quickly form a large amount of steam from the vacuum pump unit. Higher temperature steam is obtained and used to heat the power generation medium in the low temperature power generation device.

Due to the use of high-temperature energy separation technology, a low-quality energy source (such as hot water below 60 ° C.), which is difficult to use for power generation in the prior art, can be made into thermal water vapor suitable for low-temperature power generation by applying only a small amount of energy. This makes multiple uses of energy possible, and the power generation efficiency will be several times that of existing energy utilization technologies. At the same time, it opens a new path for the use of low-quality waste heat energy in other fields. That is, hot water with a lower temperature can be passed into the cold-heat energy separation device, and a higher vacuum degree can be set, thereby obtaining steam at a higher temperature for low-temperature power generation.

The equipment used in the high-temperature energy separation technology is basically the same as the equipment used in the vacuum sublimation evaporation cold and heat energy separation technology. Only 2-3 water inlets are added above the water surface in the evaporation tank, and a water spray device is set on the water inlet to make the water inlet spray into Seal the container, the spray nozzle of the water spray device is set horizontally or downwardly. The best hot water entering from the water spray device, for example, the connection pipe connected to the water inlet is connected to the condenser of the power generation medium. The cooling water outlet may also be connected to the exhaust steam outlet of the power generation medium evaporator. Hot water is sprayed horizontally or obliquely downward, which can improve the evaporation efficiency when the water temperature drops. The exhausted steam discharged from the power-generating medium evaporator and the hot-water condensed by the power-generating medium cooler after power generation can be reused. This hot water is passed into the cold-heat energy separation equipment to separate the thermal energy from the water and generate a new one. steam.

Figure 12 shows another specific embodiment:

The aforementioned cold-heat energy separation device is a low-temperature cold-heat energy separation device, called a primary cold-heat energy separation device, and further includes a high-temperature cold-heat energy separation device, called a secondary cold-heat energy separation device. The separation device includes a secondary sealed container 4 ". The secondary sealed container 4" is provided with at least a secondary water inlet 44 "and a secondary steam outlet 42". The secondary water inlet 44 "is connected to the station through a pipeline. The waste steam outlet 24 of the power generation medium evaporator 2 in the low-temperature power generation device, or the cooling water outlet 34 connected to the power generation medium condenser 3; the secondary steam outlet 42 "is connected to a secondary vacuum pump unit 5", and the secondary vacuum pump The last stage steam outlet of unit 5 "is connected to the heating steam inlet on the power generation medium evaporator in another low-temperature power generation unit through a pipeline connection. Of course, it can also be connected to the heating steam inlet of the power generation medium evaporator of the original low-temperature power generation device. Because the evaporation efficiency of water at higher temperatures will be several times higher than the evaporation efficiency of water at lower temperatures, the energy spent to obtain the same amount of thermal energy is only a fraction of that at low temperatures. This part of the new steam energy can be reused.

It can be seen from Fig. 16 that the relationship between the evaporation amount of water and the temperature is that when the water surface is stationary and reaches 60 degrees, the saturated vapor pressure reaches 19920 Pa, and the equipment suction capacity reaches 36000 m ³ / h, the water evaporation rate is 6374 Kg / h. Under the same equipment conditions, when the water surface is stationary, the temperature reaches 0 degrees, and the saturated vapor pressure reaches 610 Pa, the water evaporation rate is only 238 Kg / h, which is only one-seventh of that at 60 degrees. In practice, because the efficiency of water vapor extraction by vacuum equipment mainly depends on two factors, that is, the equipment's pumping capacity of the vacuum pump unit and the evaporation capacity of the raw material water in the space to be pumped. Under the condition that the equipment and process parameters are not changed, the evaporation capacity in the extraction space is the decisive factor affecting the steam production. According to the data obtained under the above conditions, the evaporation rate of water at 60 degrees is equivalent to 27 times that of water at 0 degrees (under water surface static conditions). Therefore, under the same vacuum unit conditions, using heated water will Greatly increase the steam production per unit time. That is, it is possible to obtain steam evaporated by using low-temperature water with only a few tenths of the energy output. According to the law of conservation of energy, the energy of the steam extracted in this part is still equal to the energy of the input heating water, and only the thermal energy is separated in the form of water vapor with very low energy consumption, which becomes a higher quality thermal energy that can be used. It can be seen that the advantages of vacuum sublimation evaporation cold and heat energy separation technology are very obvious.

Similarly, with this technology, we can perform energy separation in the ocean, summer, or the four seasons in southern China, and the efficiency should be much higher than the temperature difference power generation technology.

In addition to the above embodiments, there may be the following implementations:

1. Use multiple sets of cold and heat energy separation devices as shown in Figure 10, multiple sets of sealed containers 4 and their respective corresponding vacuum pump units 5 or multiple sets of sealed containers 4 corresponding to one vacuum pump unit, to achieve the separation of latent heat of icing in water The purpose of coming out (1 ton of water will release 1 ton of water from normal temperature to 100 degrees).

2. As shown in FIG. 12a, the high-temperature steam obtained from the primary cold-heat energy separation device 4 passes through the heating agent inlet A1 into the heating agent channel of the heat exchanger A, and is discharged from the heating agent outlet A2, and then goes to the next or next few The heat exchanger is heated in the water channel where the normal temperature water enters the heat exchanger from the normal temperature water inlet A3 of the heat exchanger, the hot water is discharged from the outlet A4, and the secondary cold and heat energy separation device 4 ”water inlet is introduced through the connection. , You can use the heat energy separated in the first step to use the heat exchanger to heat the raw water, so that at a higher temperature, the secondary cold and heat energy separation device can be used to efficiently separate high-quality water vapor and increase its pressure to It can be used above atmospheric pressure, such as low-temperature power generation, or it can be used elsewhere. According to the law of conservation of energy, the thermal energy of the steam separated from the secondary is equal to the energy separated from the primary, but the energy quality is better, that is, the temperature of the steam can be more Therefore, the use of such steam can greatly improve the power generation efficiency of low-temperature generators.

3. Low-quality thermal energy can be reused after use, which greatly improves the efficiency of separated energy utilization. Such as condensed hot water after power generation, and return water or waste water that retains waste heat.

Due to the efficient separation of cold and heat energy, ice and heating are both very efficient. With a fraction of the energy consumed by existing technologies, both cold and thermal energy can be obtained at the same time, and the quality of thermal energy can be improved and used efficiently.

The above-mentioned two-stage or two-stage cold-heat energy separation technology is used to improve the efficiency. The positioning of the one-stage or one-stage cold-heat energy separation device is to obtain higher temperature water and latent heat of freezing of water. Use normal temperature water to separate its energy, because the temperature is closer to 0 degrees, the energy is less. The secondary or secondary cold and heat energy separation device uses hot water, and the focus is on obtaining high-quality steam and improving steam production efficiency.

The cold and hot energy separation method distributed energy supply station is a new set of combined heat and heat energy separation technology to integrate and improve the original technology and equipment, make full use of the existing technology and equipment advantages to reduce construction costs. Distributed energy supply system for centralized supply of cold energy, heat energy, and electric energy. The invention creates a new form of energy supply with high efficiency, strong adaptability and short payback period. Table 8 below shows the investment and payback period estimates for several types of power generation.

It can be seen that the operation cost of the energy supply station provided by the present invention is the lowest, the recovery period is the shortest, and the investment is also the smallest. The overall performance is the best.

Further analyze the cost of using various energy sources:

Taking the cost of energy consumed by heating 1 ton of water at 20 ° C to 60 ° C as an example, Table 9. is as follows:

If normal temperature water (20 ° C) is heated to 100 ° C, the energy cost is doubled.

Table 10

According to the data in Table 9 and Table 10, heating 1 ton of hot water requires burning 16.8 kg of standard coal, and the cost is RMB 8,07. Or burning natural gas 16.8m ³ , the cost is 42 yuan. Under the condition of COP = 18, the energy consumption of cold and heat energy separation technology is only 6.45KWH, and the cost is 3.6 yuan.

Using cold and heat energy separation technology can make 1 ton of room temperature water release the heat energy equivalent to burning 16.8Kg standard coal or 16.8 cubic meters of natural gas. And the amount of water in rivers and lakes is amazing. Provides a steady stream of energy.

Using low temperature power generation technology, an energy generating unit with different steam output and different power generation efficiency can generate electricity. Table 11:

The energy supply station uses the separated thermal energy to implement the function of a distributed energy supply station. The energy supply station has high efficiency, low investment and low threshold for use.

In the prior art, low temperature generator projects can only be launched in areas with waste heat, such as in the vicinity of steel mills and power plants. Using the present invention, as long as the water source is fresh water or salt water, low temperature can be carried out. Power generation, of course, if there is waste heat, the aforementioned high-temperature cold-heat energy separation device can be used to produce more high-quality steam for low-temperature power generation. Therefore, the supply station plays a very important role in solving remote areas, islands, and areas and units that need distributed energy supply. The energy saving and emission reduction effect is very significant. Because the separated thermal energy is partially used and partially converted into electrical energy, the corresponding cold energy is relatively increased, and it has no warming effect on the environment. According to the current low-temperature power generation technology, inputting hot water with a temperature of more than 60 degrees as an energy source can generate 6% -12% of the effective energy input. With the development of technology, the efficiency of low-temperature power generation technology is likely to increase and the energy utilization efficiency will be even higher.

The invention cools at the same time as heating, and can run in four seasons on the seashore and the river banks in the south. When heating in the north in winter, ice can be stored in winter and used or sold in summer to solve the problem of ice production during winter production.

The invention uses thermal energy (sensible heat and icing latent heat) stored in seawater to generate electricity and provide electrical energy. From the data provided in Tables 1 and 2, it can be known that separating the sensible heat and latent heat of freezing from 1 ton of room temperature water is equivalent to the heat generated by burning 16.8Kg of standard coal. Based on the power generation efficiency of 20%, it can generate 18.6KWH. The energy consumed to separate the sensible and latent heat of 1 ton of room temperature water is only 5.6KWH (COP = 18).

It can be used for low-cost cooling services in summer, especially the renovation of centralized air conditioning in large buildings, hospitals, and office buildings, and the energy-saving replacement of some air conditioners in residential communities (using floor cooling technology). COP = 3.4. Compared with the lower limit of new technology, COP = 18 consumes more than 5 times more energy. Therefore, the advantages of the new technology are very obvious.

Can be used for low-cost heating services in winter. According to the principle of conservation of energy, the separated heat and cold energy are equal. The new technology unit produces ice water of equal energy while making ice. Based on the energy consumption ratio of 18, the efficiency of heat production is still very high. If it is not used to melt ice cubes, it is completely used for building heating. The heating area is basically equivalent to the summer cooling area.

The separated water vapor can be regarded as a geothermal source. The cold-heat energy separation system can provide a stable steam flow and provide a heat source for low-temperature screw generators to generate electricity. Because the low-temperature power generation efficiency is between 8% and 12%, after the steam source is used for power generation, it will still retain more than 85% of low-temperature thermal energy (hot water above 90 degrees). The hot water at this temperature completely meets the heating and bathing heat. The use of water (40-50 degrees) is required.

The functional device provided by the invention can be used for power supply of islands, fresh water supply, heating in winter and cooling in summer.

The invention can be modified on the basis of the original low-temperature power generation equipment, and a set of cold-heat energy separation device can be added. Therefore, the present invention also has the advantages of low equipment cost, small floor space, convenient reconstruction of the original equipment system, low investment for transformation, short investment recovery period, and quick results.

As shown in FIG. 17, the vacuum sublimation evaporation cold and heat energy separation heating or cooling device provided by the present invention can provide both heat and cooling, and includes a cold and heat energy separation device, a vacuum pump unit 2, and a steam exchange. Heater 3, an ice slurry storage tank 4, and an ice-water heat exchanger 5, the cold-heat energy separation equipment has a sealed container 1 whose structure is basically the same as that shown in FIG. 1b. The sealed container 1 is provided with a water inlet 11 , Steam outlet 12 and ice slurry outlet 13; the vacuum pump unit 2 is a multi-stage vacuum pump, the first-stage suction port is connected to the steam outlet 12 on the sealed container 1, and the second-stage suction port is connected to the previous stage. The exhaust port of the vacuum pump gradually decreases from front to back, so that the pressure of the extracted steam is gradually increased to atmospheric pressure; the steam heat exchanger 3 is a wall heat exchanger, in which the inlet 31 of the high-temperature fluid channel is connected to a vacuum pump The connecting pipe 21 on the exhaust port of the last stage of the unit 2 and the outlet 32 of the high-temperature fluid channel are vented, and a condensed water storage tank (not shown in the figure) can also be connected. The inlet 33 and outlet 34 of the low-temperature fluid channel in the steam heat exchanger 3 are connected to the water inlet pipe 6 and the water return pipe 7 of the floor heating heating coil, respectively.

The inlet 41 of the ice slurry storage tank 4 is connected to the ice slurry outlet 13 provided on the sealed container in the cold and heat energy separation equipment through a pipeline, and a valve is installed on the pipeline, and a mud pump can be provided as the driving power for the transportation; The heat exchanger 5 is a wall type heat exchanger, in which the inlet 51 of the low-temperature fluid channel is connected to the outlet 42 of the ice slurry tank 4, and the outlet 52 of the low-temperature fluid channel is connected to the return water port 43 of the ice slurry tank 4 or becomes a discharge port; The inlet 53 and the outlet 54 of the fluid channel are respectively connected to the water inlet pipe 8 and the water return pipe 9 of the floor heating cooling coil.

The connecting pipeline on the ice slurry outlet 13 provided on the sealed container 1 in the cold-heat energy separation equipment is connected to the inlet of an ice water storage tank 4, and the ice slurry discharged from the sealed container 1 passes through the inlet 41 of the ice slurry storage tank 4. Enter the ice water storage tank and melt into cold water, and then input the cold water from the outlet 42 of the ice slurry storage tank 4 to the inlet 51 of the low temperature runner of the ice water heat exchanger 5, and then from the outlet 52 of the low temperature runner The return water port 43 returned to the ice slurry storage tank 4 may not be returned to the ice slurry storage tank 4 but may be discharged into another pool for use as the water inlet of the sealed container. The normal-temperature water in the floor heating cooling coils flows from the return pipe 9 into the inlet 53 of the high-temperature runner of the ice-water heat exchanger 5, and the temperature-reduced normal-temperature water flows out from the outlet 54 of the high-temperature runners. The water pipe 8 is transported to a floor heating heating coil for use.

The process of providing floor heating through the device provided in this embodiment is:

In winter, the tap water enters through the water inlet 11 on the sealed container 1, and the vacuum pump unit 2 is started at the same time or in advance. The sealed container 1 is evacuated to form a high vacuum state, and the minimum pressure can reach the three-phase diagram of water ( As shown in Figure 3) near or below the triple point O. Part of the water entering the sealed container 1 continuously evaporates in the high vacuum environment, and is drawn out by the vacuum pump unit 2, which gradually pressurizes the steam step by step, and the temperature of the steam that increases the pressure also gradually increases; the usual vacuum pump The unit will set heat exchangers between stages to reduce the temperature of the steam, and the vacuum pump unit in this equipment eliminates the interstage heat exchanger, so that the temperature of the steam discharged from the last stage of the vacuum pump unit is higher, which can reach 100 ° C; The high-temperature steam is input into the high-temperature fluid channel of the steam heat exchanger 3, and for heating the water in the low-temperature fluid channel, the heated water is discharged from the steam heat exchanger 3 and sent to the geothermal heating coil for use; The steam is generally condensed and discharged from the outlet of the high temperature fluid channel of the steam heat exchanger, or collected. With the continuous injection of tap water into the sealed container 1 and the continuous operation of the vacuum pump unit 2, high-temperature steam will continuously enter the steam heat exchanger 4, which can continuously heat the water in the heating coils for the floor heating to meet the needs of floor heating. At this time, the valve on the ice slurry outlet 13 on the sealed container is closed, and the heating and cooling coil system does not work.

If the heated water in the steam heat exchanger is sent to the heat source water tank of the centralized air conditioner, a vacuum sublimation evaporation cold and heat energy separation heating and centralized air conditioning device is formed.

If you simply use the floor heating device to heat in winter, you can use the equipment shown in Figure 19. The sealed container 1 may not be provided with an ice slurry outlet. However, a water outlet 14 may be provided at the bottom of the sealed container 1.

In summer, this type of floor heating equipment can be used as follows: As the vacuum pump unit 3 continues to evacuate the sealed container 1, the temperature of the water in the sealed container 1 will continue to decrease, or even freeze, this part of the water will be discharged through the ice slurry discharge port 13 It is melted into cold water in the ice slurry storage tank 4, and the cold water is cooled by passing through the cold water heat exchanger to cool the water in the cold heating coils, which can provide an application for warming in summer.

If the cooled water in the ice-water heat exchanger is sent to the cold source water tank of the centralized air conditioner, a vacuum sublimation evaporation cold and heat energy separation and cooling centralized air conditioner will be formed.

It is also possible to make a device without a steam heat exchanger, but only for the purpose of warming and cooling the ground in summer, which is not shown in the figure.

In the equipment shown in FIG. 17, a device for preparing domestic hot water by using the high temperature steam in the vacuum pump unit 2 may be added. As shown in FIG. 18, a hot water heat exchanger 10 and a hot water heat exchanger 10 is a tank body, and a high-temperature fluid coil 101 is provided in the tank body as a high-temperature flow path, and the inlet 101a and the outlet 101b of the coil tube 101 protrude from the tank body,

The pipeline 21 connected to the exhaust port of the last stage of the vacuum pump unit 2 is connected to a branch 22, which is connected to the inlet 101a of the high temperature fluid coil 101 and the outlet of the high temperature fluid coil 101 of the hot water heat exchanger 10 101b may be vented, or may be connected to a condensed water storage tank (not shown in the figure), and the domestic water pipeline 100a is connected to the inlet 102 and the water return 103 of the low-temperature runner of the hot water heat exchanger.

If the amount of steam is sufficient, domestic hot water can also be prepared in winter.

A stirring device 1A is provided in the sealed container. The stirring paddle 1a in the stirring device 1A is set at a set liquid level of the sealed container so as to break the ice layer formed on the liquid surface. An observation hole 1B is also provided in the sealed container.

Heating or cooling systems, specifically floor heating systems or centralized air-conditioning equipment, have been widely used and recognized by the market as a mature technology. At present, many district heating districts are also equipped with floor heating. The ground cooling system, as a newer technology, has not received widespread attention due to its lagging effect of ground conduction cold energy and its insignificant advantages compared to existing air conditioning technologies. Due to the floor heating equipment provided by the present invention, the floor heating heating and cooling systems can be shared (only the temperature of the water supply changes, and the temperature difference is only about 10 degrees). Therefore, the common system will improve the use efficiency of the original floor heating system, and the cost of transformation is low, and the energy saving effect is obvious. If the centralized supply of cold and heat energy is achieved, the energy saving effect and the cost of system reconstruction will achieve satisfactory results.

In the heating or cooling equipment provided by the present invention, the vacuum state in the sealed container of the cold-heat energy separation equipment is at the three-phase point (point O) as shown in FIG. 3, and the gas-solid (O-A) line moves downward. That is, from 373K to below 253K (from 100 degrees Celsius to minus 20 degrees Celsius).

In order to realize the separation of cold and heat energy and facilitate the use, this equipment is to extract the heat energy in the form of steam, and the cold energy is separated and stored in the form of ice. The process section is placed at: temperature: 272K-253K (or below) (see line a-b in Figure 3), pressure: 600Pa-100Pa (see o-a in Figure 3).

Figure 7 shows a modification of a sealed container. The improvement lies mainly in the following two points. One is that a heating coil 4-2 is added to the space above the liquid level of the sealed container 4-1. The heating coil 4-2 is passed through a relatively hot medium. Heating, which can increase the flow rate of steam, accelerate the evaporation process, and help improve the separation efficiency of cold and heat energy.

As shown in FIG. 7 and FIG. 9, the heater 4-2 is a heating coil, and the nozzles at both ends of the heating coil are hermetically extended out of the crystallizer to connect the heating medium supply device. The inlet of the heating coil can be connected to the steam outlet of the vacuum pump unit, so as to use the steam with reduced pressure and temperature as the heating medium.

The heater 4-2 is a plurality of heating coils arranged up and down.

The second improvement point is the structure of the raw water inlet device. As shown in Figs. 7 and 8, a liquid supply tray 4-3 is provided in the tank of the sealed container 4-1, and the liquid supply tray 4-3 is provided in the tank. In the lower part, the liquid supply tray is a 4-3 shower, with the liquid spray holes facing upward. The liquid inlet hole in the middle of the bottom is connected to the raw water inlet 44 on the sealed container tank through a pipeline; the ice-water mixture outlet 49 is set to the raw water. Above the inlet 44, the liquid supply tray 4-3 is placed below the liquid level in use.

From the examples, it can be known that the output heat energy of this equipment, that is, the steam extracted by the multi-stage Roots vacuum pump can directly produce hot water at 60 ° C-70 ° C. While producing 1 ton of ice, it can produce about 2 tons of 60 ° C hot water. . Calculating only based on the actual refrigeration COP = 12 of this technology, for each ton of ice produced, the power consumption will be less than 7.75 degrees, and the refrigeration energy consumption will be reduced by at least half. Adding hot water produced, the total energy consumption can be reduced by 75%, that is, 25% of the energy consumption when COP = 6 (while the COP value of ice machines currently on the market is generally lower than 3). The prepared domestic hot water can also provide central heating and bath hot water in a certain range.

The energy-saving effect of the heating and cooling equipment provided by the invention is very obvious, and the development potential is huge. The COP that can achieve equipment cooling is greater than 18 or even higher. In addition, the cost of this equipment is low, and the payback period of equipment investment will be greatly reduced.

The energy-saving effect of the invention is very obvious, and the development potential is huge. The COP that can achieve equipment cooling is greater than 12 or even higher. In addition, the cost of the equipment of the present invention is relatively low, and the payback period of equipment investment will be greatly reduced.

Claims

A method for separating hot and cold energy by vacuum sublimation evaporation is performed in a device including an artificial environment, that is, a sealed container provided with a liquid inlet, a gas outlet, and a solid or solid-liquid mixture. The outlet is also provided with a stirring device in the container, and a vacuum sublimation evaporation unit, namely a vacuum pump unit, is connected to the gas outlet;

The separation method is:

Step 1: Establish a vacuum environment in the artificial environment, the vacuum environment is: let the liquid inlet enter the liquid in the artificial environment:

Part of it evaporates to steam and part of it solidifies, or,

Some of it evaporates into steam, some solidifies into solids, and some solids sublimate into steam;

Simultaneously or before or after, inputting liquid to the artificial environment through the liquid inlet;

Step 2: Separate the steam and solid, start the stirring device to break the solidified solid, the solid or solid-liquid mixture is discharged from the solid or solid-liquid mixture outlet into cold energy output, and the steam is vacuum pumped from the gas outlet The unit is pumped out to become heat energy output;

Steps 1 and 2 are performed alternately and / or simultaneously, so that the liquid enters the container, the solid or solid-liquid mixture exits the solid or solid-liquid mixture outlet, and the steam is extracted from the gas outlet. This process is continuously performed to achieve the cold and thermal energy. Separation.
The method according to claim 1, characterized in that: the pressure of the artificial environment is 600 Pa or less; and / or,

It also includes step 3: draining the solid or solid-liquid mixture from the container into a solid storage tank at the same pressure as the container.
The method according to claim 2, wherein the temperature in the artificial environment is 272K or less.
The method according to claim 2, wherein the pressure of the artificial environment is 600-100Pa.
The method according to claim 4, wherein the temperature in the artificial environment is 272-253K.
The method according to any one of claims 1 to 5, characterized in that: in step 2, the stirring device provided in the container is stirred to ensure that solids in the container do not seal the entire liquid surface, And the solid is broken and discharged from the solid or solid-liquid mixture outlet; and / or, the stirring device is started in step 1.
The device used in the method according to any one of claims 1 to 6, characterized in that it comprises a sealed container on which a liquid inlet, a gas outlet and a solid or solid-liquid mixture outlet are provided, on which the gas outlet A vacuum sublimation evaporation unit is connected to provide a set pressure for the sealed container, and a stirring device is arranged in the container.
The device according to claim 7, further comprising a solid storage tank which communicates with the container and constitutes the same pressure as the container, and the solid or solid-liquid mixture outlet in the container is connected to the solid. The inlet on the storage tank is connected, and a cut-off device is provided between the solid storage tank inlet and the solid or solid-liquid mixture outlet of the container to enable the two to communicate or cut off; a solid substance or solid-liquid is provided on the solid storage tank The mixture discharge port is also provided with a vent port to communicate with the atmosphere, and a vent valve is provided on the vent port; and / or,

The stirring paddle in the stirring device is located at a set liquid level in the container or at a height within 50 mm below the set liquid level; and / or,

The exhaust port of the vacuum sublimation evaporation unit is connected to a pair of gas inlets of a steam heat exchanger that extracts steam for heat exchange, and heats a low-temperature medium by using the thermal energy of the steam that is heated up after the pressure is extracted from the container; and /or,

The vacuum sublimation evaporation unit is a multi-stage Roots vacuum pump; and / or,

The container is a crystallizer, and its structure is: the crystallizer is a can body, and a pot-shaped partition plate including a bottom and a side wall is set in the can body to form a crystallization disc, and the crystallization disc divides the inner space of the can body In the upper space and the lower space, the gas outlet is arranged on the tank wall at the top of the tank, and the vacuum sublimation evaporation unit is connected through a pipeline; the stirring device penetrates from the top of the tank in a sealed manner into the crystallization tray placed in the upper space; The liquid inlet pipe of the liquid inlet is sealedly inserted into the tank body from the side wall of the lower space of the tank body, and then communicates with the crystallization tray from a position lower than the side wall of the crystallization tray; a waste water outlet is provided on the lower bottom of the crystallization tray, on which Connected to the waste water discharge pipe, the waste water discharge pipe extends downwards and seals out of the tank from the bottom of the tank; a drain port is also provided at the bottom of the crystallization tank for waste water discharge from the lower space; Part of which is provided with an ice outlet and a solid-liquid mixture outlet provided on the side wall of the lower space of the tank body; or,

The container is a crystallizer, and its structure is: the crystallizer is a tank body, the gas outlet is arranged on the tank wall at the top of the tank body, and the vacuum sublimation evaporation unit is connected through a pipeline; the stirring device is sealedly passed from the top of the tank body Into the tank; the liquid inlet pipe of the liquid inlet is sealedly inserted into the tank from the side wall of the lower space of the tank, and then communicates with the crystallization tray from a position lower than the side wall of the crystallization tray; waste water is arranged on the lower bottom of the crystallization tray The outlet is connected to a waste water discharge pipe, and the waste water discharge pipe extends downward and is sealed out from the bottom of the tank body; a drain port is further provided at the bottom of the crystallization tank 4 for draining waste water from the lower space.
The device according to claim 8, characterized in that: a communication pipeline is provided between the solid storage tank and the container, and a conveying device is provided on the communication pipeline; and / or,

The suction port of the vacuum sublimation evaporation unit is respectively connected to the gas outlet of the container and an air outlet on the solid storage tank, so that the container and the solid are passed through the same vacuum sublimation evaporation unit, that is, a multi-stage vacuum pump unit. The tank acts to create the same pressure; and / or,

The stirring paddle in the stirring device is located at a set liquid level in the crystallization pan or at a height within 50 mm below the set liquid level; or, the stirring paddle in the stirring device is located at a set liquid level in the crystallization tank or At a height within 50mm of the set liquid level; and / or,

A connection is connected to the outlet of the solid storage tank, and the connection is connected to a raw water heat exchanger, so that the liquid in the solid-liquid mixture in the solid storage tank cools the liquid entering the crystallizer; and / or,

A vacuum pump is connected to the gas outlet of the steam heat exchanger, which is used to suck the heat-exchanged gas out of the heat exchanger.
The device according to claim 9, wherein the conveying device is a mud pump.
A vacuum sublimation evaporation and freezing seawater desalination device is characterized in that it includes a desalination unit, the desalination unit includes a raw water inlet and a freshwater outlet, and the desalination unit further includes a cold and heat energy separation device.

The cold-heat energy separation device includes at least one crystallizer and a vacuum pump unit. The crystallizer is provided with a water inlet, a steam outlet, an ice-water mixture outlet, and a high-salt wastewater discharge outlet. The water inlet is in communication with the raw water inlet. The ice-water mixture outlet is in communication with the fresh water outlet, and the vacuum pump unit is connected to the steam outlet to provide a set vacuum pressure for the crystallizer, so that raw water can appear after entering the crystallizer:

Part of the raw water becomes steam and is extracted, and part of the raw water becomes solid ice, or,

Part of the raw water becomes steam and is extracted, part of the raw water becomes solid ice, and part of the ice rises into steam;

A stirring device is provided in the crystallizer. The stirring device breaks solid ice to form an ice-water mixture and discharges it, and then discharges through the fresh water outlet to form fresh water with reduced salt content.
The vacuum sublimation evaporation and freezing seawater desalination device according to claim 11, wherein the structure of the crystallizer in the cold-heat energy separation device is:

A liquid supply tray is provided in the tank of the crystallizer, and the liquid supply tray is provided at the lower part of the tank. The liquid supply tray includes a cavity, and a liquid inlet is provided on the lower part or the side wall of the cavity. A hole is connected to the raw water inlet through a pipeline, and a liquid spray hole is provided on the wall of the cavity facing upward; the ice-water mixture outlet is disposed above the water inlet, so that the liquid supply tray is in use Placed below the liquid surface; and / or,

The stirring device includes a paddle, which is arranged on a stirrer shaft, the stirrer shaft sealingly protrudes from the tank body and connected to a power source; the paddle blade is located higher than the ice-water mixture outlet and is located in the tank Set the liquid level in the body so that half of the stirring paddle is above the liquid level, and the other half is below the liquid level or the height of the stirring paddle is less than 50mm below the set liquid level, so as to break the Ice layers; and / or,

The crystallizer further includes a heater, which is disposed in an upper space of the tank body above a set liquid level.
The vacuum sublimation evaporation and freezing seawater desalination device according to claim 11, wherein the structure of the crystallizer in the cold-heat energy separation device is:

A pot-shaped partition plate including a lower bottom and a side wall is set in the crystallizer tank to form a crystallization disc, which divides the internal space of the tank into an upper space and a lower space; the stirring device is from the top of the tank Sealedly penetrated into the crystal plate placed in the upper space; the liquid conveying pipe connected to the water inlet is sealedly inserted into the tank from the side wall of the lower space of the tank, and then lowered from the side wall of the crystal plate Connected to the inside of the crystallization tray; a drain port is provided on the lower bottom of the crystallization tray; a waste water discharge pipe is connected to the waste water discharge pipe; the waste water discharge pipe extends downward; and is sealed out from the bottom of the tank through the high-salt waste water discharge port Tank body; a drain port is also provided on the bottom of the crystallizer for draining waste water from the lower space; an ice port is provided on the upper part of the side wall of the crystallization plate, and the side wall of the lower space of the tank body is provided with the drain port Ice water mixture outlet.
The vacuum sublimation evaporation and freezing seawater desalination device according to claim 12, characterized in that: the liquid supply tray is a shower, the liquid spray holes are arranged upward, and the liquid inlet hole in the middle of the bottom is connected to the pipeline through a pipeline. The water inlet on the crystallizer tank; and / or,

The heater is a heating coil or a plurality of heating coils arranged above and below, and the two ends of the heating coil are hermetically extended out of the tank body to inject and discharge the heating medium.
The vacuum sublimation evaporation and freezing seawater desalination device according to claim 14, characterized in that: the heating medium inlet of the heating coil is connected with a steam outlet of the vacuum pump unit, so as to use steam with reduced pressure and temperature as a heating medium.
The vacuum sublimation evaporation frozen seawater desalination device according to claim 13, characterized in that: the stirring paddle in the stirring device is located at a set liquid level in the crystal plate, so that the stirring paddle is half above the liquid level, The other half is below the liquid level or at a height within 50mm of the set paddle level.
The vacuum sublimation evaporation frozen seawater desalination device according to claim 12 or 13, characterized in that the crystallizer is further connected to at least one isobaric ice slurry storage tank, the isobaric ice slurry storage tank and the crystal The ice-water mixture outlet in the crystallizer is in communication with the inlet on the ice slurry storage tank, and the ice-water slurry storage tank inlet and the ice in the mold are connected. A cut-off device is provided on the pipeline between the water mixture outlets so that the two are connected or cut off; an ice-water mixture outlet is provided on the ice-pressed slurry storage tank, and an air vent and the atmosphere are provided on the ice-pressed slurry storage tank The venting port is provided with a venting valve.
The vacuum sublimation evaporation and freezing seawater desalination device according to claim 17, characterized in that: a communication pipeline between the isobaric ice slurry storage tank and the crystallizer is provided with a conveying device; and / or,

The suction port of the vacuum pump unit is respectively connected to the steam outlet of the crystallizer and an air outlet on an isobaric ice slurry storage tank, so that the crystallizer and the mold The isobaric ice slurry tank acts to create the same pressure.
The vacuum sublimation evaporation and freezing seawater desalination device according to claim 11, wherein the cold-heat energy separation device further comprises a heat exchanger, which is a steam heat exchanger connected to a steam discharge port on the vacuum pump unit So that steam with increased pressure and temperature increased is extracted from the crystallizer as the heating medium of the steam heat exchanger; and / or, it is an ice slurry heat exchanger connected to the ice-water mixture outlet so that the ice slurry serves as ice Cooling medium for a slurry heat exchanger; and / or,

The vacuum pump unit is a roots-screw vacuum pump unit; and / or,

The desalination unit further includes an ice slurry dehydrator, which is a tank body with an inlet and an outlet provided thereon, the inlet is connected to the ice water mixture outlet, and the outlet is provided in the ice slurry dehydrator. Where the liquid level is set, the outlet is the fresh water outlet; or,

The desalination unit further includes an ice slurry pond on which an inlet and an outlet are provided, the inlet is connected to the ice-water mixture outlet, and the outlet is the fresh water outlet; or,

The desalination unit further includes an ice slurry dehydrator and an ice slurry pond,

The ice slurry dehydrator is a tank body, which is provided with an inlet and an outlet, the inlet is connected to the ice water mixture outlet, and the outlet is provided at a set liquid level of the ice slurry dehydrator,

The ice slurry pond is provided with an inlet and an outlet, the inlet is connected to the outlet of the ice slurry dehydrator, and the outlet is the fresh water outlet; or,

The desalination unit further includes an ice slurry dehydrator, an ice slurry pool, and an ice slurry melter,

The ice slurry dehydrator is a tank body, which is provided with an inlet and an outlet, and the inlet is connected to the ice-water mixture outlet;

The ice slurry pool is a container on which an inlet and an outlet are provided, and the inlet is connected to the outlet of the ice slurry dehydrator;

The ice-melt melter is a container provided with an inlet and an outlet, the inlet is connected to the outlet of the ice-melt pool, and the outlet is the fresh water outlet of the desalination unit, in the container of the ice-melt melter. Install a heating device.
The vacuum sublimation evaporation and freezing seawater desalination device according to any one of claims 11 to 15 and 18 to 19, wherein the number of the desalination units is n, and the raw water inlet in the first desalination unit is a seawater inlet. The raw water inlets in the n desalination units are n raw water inlets, which are connected to the freshwater outlets in the n-1th desalination unit.
A distributed energy supply station for vacuum sublimation evaporation cold and heat energy separation method is characterized in that it includes a cold and heat energy separation device and a low temperature power generation device.

The cold and heat energy separation device includes a separation device and a vacuum pump unit,

The cold and heat energy separation equipment includes a sealed container, which is provided with at least a water inlet and a steam outlet;

The suction port of the vacuum pump unit is connected to a steam outlet on the sealed container, and a high-temperature steam and / or hot water discharge port is also provided thereon;

The low-temperature power generation device includes a low-temperature power generator, and the low-temperature power generator includes:

A low temperature generator,

A power generation medium evaporator; and

A power medium condenser;

The power-generating medium condenser and the power-generating medium evaporator are both wall heat exchangers, and the power-generating medium flow channels in the two are connected to the low-temperature generator to form a circulation system;

The high-temperature steam inlet on the power-generating medium evaporator in the low-temperature power generation device is connected to the high-temperature steam and / or hot water discharge port of the vacuum pump unit in the cold-heat energy separation device through a pipeline.
The distributed energy supply station for vacuum sublimation evaporation cold and heat energy separation method according to claim 21, characterized in that the cold and heat energy separation device is a low temperature cold and heat energy separation device, which is called a first stage cold and heat energy separation device, The sealed container is further provided with an ice slurry outlet, and a storage tank is connected to the high-temperature steam outlet of the first-stage cold-heat energy separation device; the first-stage cold-heat energy separation device and the low-temperature power generation device It also includes a high-temperature cold-heat energy separation device, called a secondary cold-heat energy separation device, which includes a secondary sealed container. The secondary sealed container is provided with at least a high-temperature water inlet and a high-temperature steam outlet. A water port is connected to a storage tank connected to the high-temperature steam discharge port of the primary cold-heat energy separation device, and the high-temperature steam outlet is connected to a secondary vacuum pump unit, and the high-temperature steam and / or heat of the secondary vacuum pump unit is connected. The water outlet is connected to the high-temperature steam inlet on the power generation medium evaporator in the low-temperature power generation device through a pipeline; or,

The cold and heat energy separation device is a low temperature cold and heat energy separation device, which is called a primary cold and heat energy separation device. The sealed container is also provided with an ice slurry outlet, and further includes a high temperature cold and heat energy separation device, called Secondary cold and heat energy separation device, the secondary cold and heat energy separation device includes a secondary sealed container, the secondary sealed container is provided with at least one secondary water inlet and a secondary steam outlet, and the secondary water inlet passes through The pipeline is connected to the waste steam outlet of the power generation medium evaporator in the low-temperature power generation device or the cooling water outlet of the power generation medium condenser; the secondary steam outlet is connected to the air inlet of a secondary vacuum pump unit, The high-temperature steam and / or hot water discharge port of the secondary vacuum pump unit is connected to a heating steam inlet on a power generation medium evaporator in the low-temperature power generation device connected to the sequential cold-heat energy separation device through a pipeline, and / Or, connect the high-temperature steam inlet on the power-generating medium evaporator in another low-temperature power generation device; or,

The cold-heat energy separation device is a low-temperature cold-heat energy separation device, called a primary cold-heat energy separation device, and further includes a high-temperature cold-heat energy separation device, called a secondary cold-heat energy separation device. The separation device includes a secondary sealed container. The secondary sealed container is provided with at least one secondary water inlet and one secondary steam outlet. In addition, it also includes a wall-type heat exchanger with a heating agent flow channel and a water flow. The high temperature steam and / or hot water discharge port of the vacuum pump unit in the primary cold and heat energy separation device is connected to the inlet of the heating agent flow path of the heat exchanger through a pipeline, and the secondary cold and heat The water inlet on the secondary sealed container in the separation device can be connected to the outlet of the water flow channel of the heat exchanger through a pipeline, and the high temperature steam and / or hot water discharge outlet of the vacuum pump unit in the secondary cold heat energy separation device is connected. A high temperature steam inlet of a power generation medium evaporator on the low temperature power generation device; or

The separation equipment includes a low-temperature cold-heat energy separation device and / or a high-temperature cold-heat energy separation device, and the sealed container in the low-temperature cold-heat energy separation device is further provided with an ice slurry outlet; the high-temperature cold-heat energy separation The sealed container in the device is provided with at least a water inlet and a steam outlet.
The vacuum sublimation evaporation cold and heat energy separation method distributed energy supply station according to claim 21, wherein:

The water inlet of the sealed container is connected to one end of a pipeline, and the other end of the pipeline is connected to at least one of the following equipment:

A cooling water outlet of the power generation medium condenser;

Exhaust steam outlet of the power generation medium evaporator;

A branch nozzle on a high-temperature steam discharge pipeline of the vacuum pump unit.
The distributed energy supply station for vacuum sublimation evaporation cold-heat-energy separation method according to claim 21 or 22 or 23, characterized in that:

A stirring device is provided in the sealed container; and / or,

A liquid supply tray is arranged in the sealed container, and the liquid supply tray is arranged in the lower part of the sealed container, which is lower than the set liquid level height in the sealed container. The liquid supply tray is a shower and sprays liquid. The holes are arranged upward, and the liquid inlet at the bottom is connected to the water inlet through a pipeline; and / or,

A heater is provided in an upper chamber in the sealed container, which is located above a set liquid level in the sealed container; and / or,

The low-temperature generator set includes at least two low-temperature generators, which are connected in series, that is, the exhaust outlet of the exhaust steam of the power generation medium of the previous low-temperature generator is connected through a pipeline to the steam inlet of the power generation medium of the low-temperature generator, The exhaust outlet of the last low-temperature generator's power-generating medium exhaust steam is connected to the power-generating medium exhaust steam inlet of the power-generating medium condenser through a pipeline; and / or,

A water inlet is provided above the liquid level of the sealed container, and a water spray device is provided on the water inlet to make the water inlet spray into the sealed container; and / or,

One end of a water inlet connected to a water inlet is arranged above the liquid level in the sealed container, and the other end of the tube is connected to the cooling water outlet of the power medium condenser and / or the exhaust steam outlet of the power medium evaporator; and / or,

The vacuum pump unit is a multi-stage vacuum pump, wherein the suction port of the first-stage vacuum pump is connected to the steam outlet on the sealed container, the suction port of the subsequent stage is connected to the exhaust port of the previous stage, and the vacuum pumps of each stage are from front to back The amount of air extraction is gradually reduced, so that the pressure of the extracted steam is gradually increased to atmospheric pressure, and the high-temperature steam and / or hot water discharge port is provided in the last stage.
The distributed energy supply station of the vacuum sublimation evaporation cold-heat energy separation method according to claim 21 or 22, characterized in that: a pipeline of a water inlet of the sealed container in the cold-heat energy separation device is provided with a The preheater preheats the water entering the sealed container.
The vacuum sublimation evaporation cold and heat energy separation method distributed energy supply station according to claim 25, wherein:

The preheater is a partition-wall heat exchange device,

The preheating medium is derived from the power generation medium of the low-temperature power generation device: one end of a branch pipe is connected to the power generation medium outlet of the low-temperature power generator in the low-temperature power generation device, and the other end of the branch pipe is connected to the water inlet of the sealed container The heating medium inlet of the preheater is used for heating the partition wall to enter the sealed container. The outlet of the heating medium on the preheater is connected to one end of a power generation medium return pipe, and the other end of the power medium return pipe is connected to a low temperature power generation device. The power medium inlet of the power medium evaporator, or connected to the power medium storage tank, thereby using the heat of the power medium to raise the temperature of the water entering the sealed container;

;and / or,

The preheating medium comes from the steam discharged from the vacuum pump unit connected to the sealed container: the inlet of the heating medium of the preheater is connected to one end of a pipe, and the other end of the branch pipe is connected to the high temperature of the vacuum pump unit A by-pass in the pipeline connected to the steam and / or hot water outlet; and / or,

The preheating medium is derived from the cooling water for cooling the power generation medium in the low temperature power generation device: the inlet of the heating medium of the preheater is connected to one end of a pipeline, and the other end of the branch line is connected to the power generation in the low temperature power generation device Cooling water outlet of the medium condenser; and / or,

The preheating medium is derived from the exhaust steam discharged after heating the power generation medium in the low-temperature power generation device: the inlet of the heating medium of the preheater is connected to one end of a pipeline, and the other end of the branch line is connected to all of the low-temperature power generation devices. The exhaust steam outlet of the power generation medium evaporator is described.
The distributed energy supply station for vacuum sublimation evaporation cold and heat energy separation method according to claim 24, wherein the heater is a heating coil, and the two ends of the heating coil are hermetically extended out of the sealed container. To connect heating medium supply equipment; and / or,

The spray nozzle of the water spray device is provided in a horizontal direction or a downwardly inclined direction; and / or,

The water jet is connected to at least one of the following devices:

Connected to a cooling water outlet of the power generation medium condenser;

An exhaust steam outlet connected to the power generation medium evaporator; and / or,

In the multi-stage vacuum pump, the first-stage vacuum pump and the second-stage vacuum pump are roots vacuum pumps, and the last-stage vacuum pump is a screw vacuum pump.
The distributed energy supply station for vacuum sublimation evaporation cold and heat energy separation method according to claim 27, characterized in that: the heating coil is connected to a steam discharge port of the vacuum pump unit; and / or,

The heating coil is connected to a cooling water outlet of the power generation medium condenser; and / or,

The heating coil is connected to the exhaust steam outlet of the power generation medium evaporator; and / or,

The heating coil is connected to the exhaust steam outlet of the cryogenic generator.
A vacuum sublimation evaporation cold and heat energy separation heating or cooling device is characterized in that it includes a cold and heat energy separation device, a vacuum pump unit and a steam heat exchanger.

The cold-heat energy separation device has a sealed container, which is provided with a water inlet and a steam outlet;

The vacuum pump unit is a multi-stage vacuum pump. The suction port of the first stage is connected to the steam outlet on the sealed container, and the suction port of the subsequent stage is connected to the exhaust port of the previous stage. The air volume gradually decreases, so that the pressure of the extracted steam is gradually increased to atmospheric pressure;

The steam heat exchanger is a wall-type heat exchanger, in which the inlet of the high-temperature fluid channel is connected to the exhaust port of the last stage of the vacuum pump unit, and the outlet of the high-temperature fluid channel is emptied or connected to a condensate storage tank; The inlet and outlet are connected to the heating pipe and the water inlet pipe and the return pipe of the heat source water tank of the centralized air conditioner to form heating equipment.
A vacuum sublimation evaporation cold and heat energy separation heating or cooling device is characterized in that it includes a cold and heat energy separation device, a vacuum pump unit, an ice-water heat exchanger, and an ice slurry storage tank.

The cold-heat energy separation device has a sealed container, which is provided with a water inlet, a steam outlet, and an ice slurry outlet;

The vacuum pump unit is a multi-stage vacuum pump. The suction port of the first stage is connected to the steam outlet on the sealed container, and the suction port of the subsequent stage is connected to the exhaust port of the previous stage. The air volume gradually decreases, so that the pressure of the extracted steam is gradually increased to atmospheric pressure;

An inlet of the ice slurry storage tank is connected to an ice slurry outlet provided on a sealed container in the cold-heat energy separation device;

The ice-water heat exchanger is a wall-type heat exchanger, wherein the inlet of the low-temperature fluid channel is connected to the outlet of the ice slurry storage tank, and the outlet of the low-temperature fluid channel is connected to the return water port of the ice slurry storage tank or becomes a discharge port; The inlet and outlet of the high-temperature fluid channel are respectively connected to the ground cooling cold coil or the water inlet pipe and the water return pipe of the cold source water tank of the centralized air conditioner to form the cooling equipment.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to claim 29, further comprising an ice slurry storage tank and an ice-water heat exchanger,

An inlet of the ice slurry storage tank is connected to an ice slurry outlet provided on a sealed container in the cold-heat energy separation device;

The ice-water heat exchanger is a wall-type heat exchanger, wherein the inlet of the low-temperature fluid channel is connected to the outlet of the ice slurry storage tank, and the outlet of the low-temperature fluid channel is connected to the return water port of the ice slurry storage tank or becomes a discharge port; The inlet and outlet of the high-temperature fluid channel are respectively connected to the ground cooling cold coil or the water inlet pipe and the return pipe of the cold source water tank of the centralized air conditioner to form equipment capable of supplying heat and cooling.
The vacuum sublimation evaporation cold heat energy separation heating or cooling equipment according to any one of claims 29 to 31, characterized in that a hot water exchange is connected to a pipeline connected to an exhaust port of the last stage of the vacuum pump unit The inlet of the high temperature runner of the heater, the domestic water pipeline connects the inlet and outlet of the low temperature runner of the hot water heat exchanger.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to any one of claims 29 to 31, wherein a stirring device is provided in the sealed container, and the stirring blades in the stirring device are arranged at The sealed container is set at the liquid level to break up the ice layer formed on the liquid surface.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to claim 32, characterized in that: a stirring device is provided in the sealed container, and the stirring paddles in the stirring device are set in the sealed container setting At the liquid level to break up the ice layer formed on the liquid surface.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to any one of claims 29 to 31, characterized in that: a liquid supply tray is provided in a tank body of the sealed container, and the liquid supply tray is provided at In the lower part of the tank body, the liquid supply tray includes a cavity. A liquid inlet is provided on the lower part or the side wall of the cavity, and is connected to the water inlet through a pipeline. The cavity faces the cavity wall facing upward. Setting a spray hole; and / or,

The tank of the sealed container further includes a heater, and the heater is disposed in an upper space of the tank and is located above a set liquid level.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to claim 32, characterized in that: a liquid supply tray is arranged in the tank body of the sealed container, and the liquid supply tray is arranged in the tank body The liquid supply tray includes a cavity. A liquid inlet is provided on the lower part or side wall of the cavity. The liquid inlet is connected to the water inlet through a pipeline. The liquid cavity is provided on the wall of the cavity facing upward. ;and / or,

The tank of the sealed container further includes a heater, and the heater is disposed in an upper space of the tank and is located above a set liquid level.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to claim 35, wherein an ice slurry outlet is provided on the sealed container, and the ice slurry outlet is disposed above the water inlet, So that the liquid supply tray is placed below the liquid surface in use; and / or,

The heater is a heating coil or a plurality of heating coils arranged above and below, and the two ends of the heating coil are hermetically protruding from the tank body to enter and discharge the heating medium.
The vacuum sublimation evaporation cold-heat energy separation heating or cooling device according to claim 36, wherein an ice slurry outlet is provided on the sealed container, and the ice slurry outlet is disposed above the water inlet, So that the liquid supply tray is placed below the liquid surface in use; and / or,

The heater is a heating coil or a plurality of heating coils arranged above and below, and the two ends of the heating coil are hermetically protruding from the tank body to enter and discharge the heating medium.