JP2007519881A - Heat transfer method, heat transfer apparatus and system - Google Patents

Abstract

The first gas adsorbent material and the first gas adsorbent material are thermally relatively isolated from each other, but the second gas adsorber continuously communicates with the first gas adsorbent material. Disclosed are methods, apparatus, and systems for conducting heat using an agent material. In the first step, the first material is heated to desorb the gas adsorbed on the first material, whereby the gas passes to the second material where it is adsorbed. In the second step, the first material is cooled such that the gas desorbs from the second material and is again adsorbed to the first adsorbent material. As the gas is desorbed from the second material, the second material is thus cooled. In this way, a hot gas stream can be used to cool another gas stream.
[Selection] Figure 2

Description

  The present invention relates to a heat transfer method, and an apparatus and system for heat transfer. The present invention finds particular application as a desorption cooling device that uses the heat of one fluid (gas or liquid) to cool another fluid, but is not so limited as described in this context. . Furthermore, the present invention can be applied to enhance the cooling of heated fluids, on the contrary. In any case, the present invention finds application in a wide range of industries and contexts.

  Many industries exhaust waste gas into the atmosphere in warm and hot processes and dispose of the gas, thereby losing heat energy. This can further promote environmental warming. Warm fluids such as waste water can also be released to the environment. It is desirable that some of this wasted thermal energy be captured and used in the industry or elsewhere.

  U.S. Pat. No. 5,522,228 discloses an apparatus for generating cooling by adsorption and desorption of carbon dioxide. The device comprises two containers 10, 11, packed with activated carbon and zeolite, respectively, connected by a conduit 12 with a valve 13. The heat exchange device 14 is provided around the container 10, and the heater 15 is provided around the container 11.

  In operation, the vessel 10 is cooled to -50 ° C and the zeolite in vessel 11 is at 190 ° C. Valve 13 is opened and carbon dioxide is desorbed from the activated carbon, which warms container 10 to 0 degrees. However, when desorption extracts heat from the activated carbon, it is likely that the heated fluid passes through the heat exchanger 14 and warms the vessel 10 to 0 ° C. The desorbed carbon dioxide passes to the container 11, is adsorbed by zeolite, and is cooled to 45 ° C. Adsorption heats the zeolite, and possibly some type of cooling is used to cool the vessel 11 to 45 ° C.

  The valve is then closed and the container 10 is allowed to warm from 0 ° C. to 30 ° C. (ambient temperature). At the same time, the container 11 is heated from 45 ° C. to 70 ° C. by the heater 15.

  Thereafter, the valve is opened and the container 11 is heated by the heater 15 from 70 ° C. to 200 ° C., which desorbs carbon dioxide from the zeolite and sends the carbon dioxide to the activated carbon in the container 10 for adsorption. This causes the adsorption to heat the activated carbon, so that the activated carbon is cooled from 30 ° C. to −40 ° C. (ie, by circulating a cooling fluid in the heat exchanger 14 (ie, Thermodynamically, self-cooling to −40 ° C. is impossible due to release of heat of adsorption).

  The heating of the vessel 11 is then stopped, allowing cooling from 200 ° C. to 190 ° C. When the valve is opened, this causes a pressure drop in both vessels 10, 11, and the activated carbon drops in temperature from -40 ° C to -50 ° C to complete the cycle. This cooling can then be used by the fluid passing through the exchanger 14.

  In the apparatus described in US Pat. No. 5,522,228, valve 13 is essential because it is necessary to maintain the pressure of carbon dioxide in vessel 10 during the regeneration period of zeolite. If the valve is not closed, the carbon dioxide simply desorbs from the carbon and passes to the zeolite during pre-cooling of the vessel 10, so that little cooling is observed during the cooling phase.

  In contrast to the teachings of US Pat. No. 5,522,228, the present invention does not require the complexity of periodic valve closing / opening between the two vessels and also requires a starting temperature near −50 ° C. A method, apparatus, and system are provided.

In its first aspect, the present invention provides a method of transferring heat using first and second gas adsorbent materials. Contrary to US Pat. No. 5,522,228, in the method of the present invention, the second material is relatively thermally isolated from the first material, but is in continuous communication with the gas. This method
(I) heating the first material to desorb the gas adsorbed on the first material, whereby the gas is sent to the second material and adsorbed;
(Ii) cooling the first material so that the gas is desorbed from the second material and then adsorbed again to the first material;
Thereby, the second material includes a step of cooling by desorbing the gas therefrom.

  A hot fluid stream (eg, waste gas or process liquid) is used to heat the first material to desorb the gas adsorbed on the first material, while the hot fluid stream is cooled. be able to. Thereafter, another fluid stream that requires cooling is in thermal communication with the second material, so that the second material is cooled by desorption of gas therefrom and the other fluid stream is cooled. There is an advantage that can be. In other words, effectively the heat of one fluid stream can be used to cool another fluid stream.

  In addition, by ensuring that the second material is in continuous gas communication with the first material, particularly when compared to the device of US Pat. No. 5,522,228, a number of systems, devices, Improvements in brevity and efficiency will become apparent from the following description. For example, the device can be started at ambient temperature and does not require an external cooling source. Furthermore, due to continuous gas communication, pressure changes during operation are immediately converted and adapted, and no devices for compensation, such as valves, external heaters, etc. are required.

  As used herein, the expression “relatively thermally isolated” means that the first and second adsorbent materials are sufficiently thermally isolated so that they are needed / desired. Is intended to mean that one adsorbent material can be heated or cooled without affecting the other adsorbent material to the extent that it does not interfere with obtaining a cold desorption (or vice versa). is doing. Further, thermal isolation can be enhanced by spacing and / or insulating the first and second adsorbent materials from each other.

  Typically, in step (i), the first material is heated by heat conduction from a relatively hot fluid stream (eg, via a heat exchange structure). The hot fluid stream can be process waste gas or liquid.

  Optionally, in step (i), during the period in which the first material is heated, the second material is cooled with respect to the first material by heat conduction by the cooling fluid stream. This cooling further promotes gas adsorption to the second material. The cooling fluid stream may be, for example, an ambient air stream.

  Typically, in step (ii), the first material is cooled with respect to the second material by heat conduction to the surroundings or by heat conduction by a cooling fluid stream. Again, the cooling fluid flow may be a flow of ambient air.

  Typically, in step (ii), another fluid (gas or fluid) stream is cooled (eg, via a heat exchange structure) while the second material is cooled by desorption of gas therefrom. Used for. Typically, this other fluid is a process gas or liquid that requires or benefits from cooling, for example, it may be cooled or ambient air used in the process.

  The fluid in each fluid stream may be a gas or a liquid. For example, as described above, the hot fluid stream may be process waste gas or exhaust gas, and its heat is usually discarded. Further, heat conduction by the cooling fluid stream typically involves the first and second materials (eg, via the same or different heat exchange structures used in the hot fluid or cooled fluid stream, respectively), eg ambient air. This is achieved by allowing selective thermal communication with the flow.

  Furthermore, typically, once the desorption of the gas from the second material has been completed, the second material is allowed to be slightly heated by heat conduction from the other fluid stream, and therefore the second The material is heated to just enough temperature to restore its temperature to a level corresponding to the temperature of step (i) before the gas is adsorbed thereto, thereby completing the cycle.

  Typically, the first gas adsorbent material has an adsorption power that is different from the second gas adsorbent material. In use, this provides the driving force for the gas to move between the materials. Typically, the first gas adsorbent material is a different material than the second gas adsorbent material. In this regard, the first gas adsorbent material can include a molecular sieve and the second adsorbent material can include an activated powder. Alternatively, the first and second adsorbent materials can each be composed of molecular sieves, or can be composed of activated powders of different adsorptive power. Each molecular sieve may be zeolite, each activated powder may be activated carbon, and the gas used with the first and second adsorbent materials may be carbon dioxide. Good.

  Typically, this gas is pressurized with respect to ambient pressure. The typical operating pressure of the method for gas is about 0.5 MPa.

  Typically, prior to the start step (i) of the method, the gas and the first and second materials are typically at ambient temperature.

  According to a second aspect of the present invention, there is provided a heat transfer apparatus comprising a chamber having a first portion containing a first adsorbent material and a second portion containing a second adsorbent material, The device is characterized in that these parts are always connected to allow continuous gas communication therebetween and are relatively thermally isolated from each other.

  The inventor has found that a device having a thermally isolated portion provides a desorption cooling cycle while the first and second adsorbent materials are always maintained in continuous gas communication (ie, during that time). It has been observed that desorption cooling can be effectively realized (and vice versa) without the need for a valve or stop for the purpose). This is simplified, for example, over the device of US Pat. No. 5,522,228 which requires a valve. Furthermore, since the valve is not present or required in the device, the pressures in the first and second chamber portions are automatically balanced.

  Typically, the first and second portions minimize heat conduction between the first and second portions while allowing continuous gas communication between the portions. Are joined by a section composed of This section is typically a conduit having a relatively small width (eg, a smaller or smaller effective diameter) than the width (eg, diameter or effective diameter) of the first and second chamber portions adjacent thereto. Since the conduit has a small width, the surface area / dimension for heat conduction is small and still allows continuous gas communication between those parts.

  Typically, the first and second chamber portions and the conduit are each tubular, while typically the first and second chamber portions are approximately the same size.

  Typically, one or more heat conducting elements are disposed in the first and second chamber portions, together with the first and second adsorbent materials, respectively. Typically, each heat transfer element is comprised of a metal wire mesh that enhances thermal communication between the exterior of the chamber portion and the adsorbent material therein (through the chamber portion walls). Surprisingly and effectively, it has been discovered that the heat transfer element also increases the mass transport rate of gas (eg, carbon dioxide) through the first and second adsorbent materials.

  Typically, the first and second materials are each packed into a respective portion of the chamber. Typically, the first and second materials are materials as defined in the first aspect of the invention.

  Typically, the first and second chamber portions are configured to be located in an intermediate flow in each fluid stream to more efficiently conduct heat between each fluid and the portion.

In a third aspect of the invention, a system for continuously conducting heat from a first fluid stream and continuously cooling a second fluid stream is provided. The system includes first and second devices that can be in thermal communication with the first and second fluid streams, respectively. Each device comprises a chamber having separated first and second adsorbent materials, and each device can be operated in the following stages.
(1) The first material is heated by thermal communication with the first fluid stream so as to desorb the gas adsorbed on the first material, whereby the gas is sent to the second material and absorbed. And
(2) The first material is cooled so that the gas is desorbed from the second material and passes through it so that it is adsorbed again to the first material, from which the second material It is cooled by being desorbed and the second fluid stream is cooled by thermal communication with the second material.

This system
The first device is operated under step (1) to heat the first material of the first device using the first fluid stream, and the second device under step (2), The gas can be operated to cool the second fluid stream by desorbing from the second material of the second device, after which
The first fluid stream can be directed to the second device and operated under stage (1) of the second device, the second fluid stream is directed to the first device, and the first device It is possible to operate under the step (2).

  In this way, the system efficiently and effectively conducts continuous heat transfer from the first fluid stream and continuously cools the second fluid stream. By switching between the first and second fluid flows, the system, for example, allows the method and apparatus of the first and second features to be operated continuously rather than being interrupted by a desorption cooling process (and vice versa). Enable.

  Typically, the system comprises a plurality of first devices and a plurality of second devices, and typically the first and second devices are operated in parallel.

  Typically, the system further selectively flows the first and second fluid streams between the first device and the second device and between the second device and the first device, respectively. For maintaining a continuous conduction of heat from the first fluid stream and a continuous cooling of the second fluid stream. The valve can also be used to switch a cooling fluid flow, such as ambient air, between the first device and the second device.

  In this system, each of the first and second devices is typically defined with a second feature, and typically each device is operated using the method of the first feature.

While there are many other forms that fall within the scope of the invention, the preferred form of the invention is described by way of example only with reference to the accompanying drawings.
In a typical mode of use, the method, apparatus, and system according to the present invention provides thermal energy (eg, waste heat) from a gas or liquid stream to achieve separate cooling purposes (eg, cooling another separate fluid stream). Used to conduct.

  Referring to FIG. 1, a simple apparatus according to the present invention is shown in the form of a desorption cooler module. The module includes a sealed vessel 10 having two cylindrical chambers (eg, tubes such as stainless steel tubes) that are a regenerator chamber 12 and a desorption cooler chamber 14. The chambers are connected by a junction section in the form of a narrow (eg small diameter) conduit or neck 16 (such as a small diameter tube). To provide greater thermal isolation of the chambers 12, 14, the conduit 16 can be formed from a metal with a lower thermal conductivity (eg, stainless steel with lower thermal conductivity) than the chamber walls, typically It is welded to the chamber wall for sealing the container 10.

  The regenerator chamber 12 is typically packed with a first adsorbent material in the form of a molecular sieve (eg, a zeolite such as 13X zeolite), and the desorption chiller chamber 14 is filled with a different second adsorbent material (eg, Second adsorbent material with different activated carbon-like surface activated powder) or the same material with different adsorptive power (eg 10A, 8A, 5A zeolite with low adsorption power) Another type of zeolite or another type of 13X zeolite).

  One or more heat conducting elements in the form of a plurality of discrete metal wire mesh panels are preferably disposed in each of the chambers 12 and 14 along with the first and second adsorbent materials (ie, the panel is adsorbed). Dispersed through the agent material). The panel is typically made of a material that does not react to the gases and materials in the container 10, such as stainless steel, brass, aluminum, or copper, and that has sufficient thermal conductivity. The panel functions to increase the thermal conductivity between the adsorbent material and the walls and thus the exterior of each chamber. Furthermore, the present invention has surprisingly and effectively discovered that the panel enhances the mass transport rate of carbon dioxide through each first and second adsorbent material.

  The sealed container 10 further contains a suitably pressurized gas, typically carbon dioxide for abundance and ease of use, but refrigerant, ammonia, alcohol, water (steam), nitrogen. Other gases such as etc. can be used in combination with an adsorbent suitable for the gas.

  In accordance with the present invention, the sealed container 10 is configured such that gas can pass between the chambers 12, 14 through the conduit 16 continuously and unimpeded. There is the advantage that no valve or additional flow control is performed or required, and the sealed container has the advantage of having no moving parts.

  In addition, the sealed container 10 typically has a regenerator chamber 12 (contains the first adsorbent material) to the extent that the desorption cooler chamber 14 (contains the second adsorbent material) is at least operational. Configured to be thermally isolated from the This is optimally achieved by using a narrow conduit 16 so that it connects to the chamber but is spatially separated. However, thermal isolation is further enhanced by using appropriately positioned isolation means (eg, see the system of FIG. 2 described below) that includes an isolation barrier and baffle around and / or between chambers. be able to.

  In the first mode of use, the first adsorbent material is selected to have a higher adsorption power for the container gas than the second adsorbent material. It is observed that starting at ambient temperature, a greater proportion or bulk of the vessel gas is adsorbed with the first material.

  In the first mode of use, and in the first step, the regenerator chamber 12 is positioned at the center or midpoint of the hot gas stream to provide a relatively hot gas stream (eg, process waste gas). ), Thereby heating the first adsorbent material. The hot gas stream may be passed over or around chamber 12 (via one or more pipes / tubes extending through chamber 12). As the temperature of the first material increases, the adsorbed gas (eg, carbon dioxide) desorbs therefrom and the gas pressure in the container increases. Due to the relative thermal isolation of the desorption cooler chamber 14, carbon dioxide passes from chamber 12 to chamber 14 through conduit 16 and is adsorbed to a relatively cool second material (eg, activated carbon). There is a driving force to be used. During this adsorption period, the second material is slightly heated. The tendency of the gas to be adsorbed by the second material places the chamber 14 at the center or midpoint of the cooling gas flow (eg, ambient air flow) so that the second material is further cooled with respect to the first material. Can be strengthened by.

  The first material (eg, zeolite molecular sieve) remains relatively heated while in thermal communication with the hot gas stream, thereby driving the gas in the vessel 10 to re-adsorb there. Does not exist.

  In the first mode of use, in a second subsequent step, the regenerator chamber 12 (eg, by stopping or redirecting the hot gas flow), and more typically the cooling gas flow ( For example, it is cooled by contact with ambient air. As the chamber 12 cools, the first material cools and the carbon dioxide pressure in the container is reduced. This then provides the driving force for the gas to return to the regenerator chamber 12 and be adsorbed again by the first material. In this regard, the gas is desorbed from the second material, passes through chamber 16 from chamber 14 to chamber 12, and is adsorbed again to the first material.

  Effectively, the desorption of carbon dioxide from the second material in chamber 14 cools the second adsorbent material (ie, the gas needs to extract heat from the material during the desorption period), and thus Cool chamber 14 and its walls. In fact, the inventors have observed that as the gas desorption proceeds, the second chamber can be cooled at a temperature higher than 10 ° C. below ambient temperature.

  The same or another fluid stream can be passed over, around or through the chamber 14 (via one or more heat exchange pipes / tubes disposed through the chamber 14), thereby allowing other fluids The stream is cooled. Thus, the cooled chamber 14 can be used to pre-cool a gas stream, such as an engine or a gas turbine, or can be used to provide cooling air for air conditioning, or the like. In this way, the hot process fluid (eg, waste gas) can be used to cool another process fluid that requires or benefits from cooling.

  The optimal application of the present invention is in electricity generators, where hot waste (exhaust) gas from, for example, coal or fuel combustion is used to pre-cool the gas stream applied to the turbine or the like.

  Referring to FIG. 2, like reference numerals are used herein to indicate like or identical parts, and a desorption chiller system 20 according to the present invention is shown. This system is capable of continuous desorption cooling according to the present invention.

  The system 20 uses a plurality of sealed desorption cooler vessels 10 of FIG. 1, which are aligned in parallel in each parallel module bank A and B. Each module bank is aligned in a respective bank container 22. In addition, each bank vessel 22 has a thermal barrier wall positioned to separate each regenerator chamber 12 from its respective desorption cooler chamber 14 (except for a conduit 16 extending through the wall 24). 24. The barrier wall 24 thus further enhances the thermal isolation of the chambers 12,14. The barrier wall 24 can also be formed from and / or coated with an insulating material. In addition, the barrier wall 24 defines a regenerator chamber 26 and a desorption cooler chamber 28 in each bank vessel 22.

  At opposite ends in the system 20, four-way valves 30, 30 ′ are arranged to selectively direct fluid (eg, gas) into the bank containers 22 of module banks A and B. In this regard, the four-way valve 30 can selectively direct a hot process gas 32 (eg, a hot air stream) to one of the regenerator chambers 26 while simultaneously directing a cooling gas 34 (eg, an ambient air stream). Other regenerator chambers 26 of the regenerator chambers 26 can be directed.

  Similarly, the four-way valve 30 'can selectively direct a process gas 32 (eg, an air stream) that requires cooling to one of the desorption cooler chambers 28, while simultaneously cooling gas 36 (eg, ambient air). Stream) can be directed to another desorption cooler chamber 28 of the desorption cooler chambers 28. However, in the system of FIG. 2, the cooling gas stream 36 is split and directed to both desorption chiller chambers 28, one gas stream for cooling purposes (ie in one of the chambers 28), the other gas The stream is cooled to produce a cooled air stream 38 (ie, selectively recovered from one of the chambers 28). The cooled air stream is then selectively withdrawn from the other chambers of chamber 28 and is performed in a continuous manner.

  (I.e. when controlled by the four-way valve 30), for example, the regenerator chamber 26 of module A receives the hot process gas 32 and facilitates the desorption of gas from each first adsorbent material. The four-way valves 30, 30 'are controlled so that the chamber 26 receives the cooling gas 34 and facilitates gas adsorption of each first adsorbent material. Similarly, module A desorption cooler 28 receives cooling gas 36 there (which is controlled by four-way valve 30 ') to facilitate gas adsorption on each second adsorbent material and module B desorption. A four-way valve 30, so that when the cooling device 28 receives a gas 36 to be cooled there when gas desorption occurs from each second adsorbent material, the gas adsorbs each first adsorbent material; 30 'is controlled.

  The same predetermined time for each module (eg when hot gas heat conduction and / or gas cooling starts moving from steady state), the gas flow to each four-way valve 30, 30 ' Is switched so that subsequent processing stages can be performed in each module A and B. In this way, the system 20 effectively provides continuous heat transfer from the hot process gas 32 and continuous cooling of the gas 36. Furthermore, by switching the gas flow, the system allows continuity as opposed to interrupted desorption cooling. Instead, the system can facilitate a process that is the opposite of desorption cooling.

  Non-limiting examples of methods, apparatus, and systems are described.

[Example 1]
The desorption cooler module of FIG. 1 was tested and calculated to have a coefficient of performance (COP) of 0.22 (theoretical COP of less than 0.054 for the system of US Pat. No. 5,522,228). This calculation was made using the system of US Pat. No. 5,522,228 based on the following.

  In the system of US Pat. No. 5,522,228, it was assumed that each vessel 11 and 10 contained 100 g of zeolite and carbon, respectively. The energy required to heat the carbon from 0 ° C. to 30 ° C. was estimated to be about 2.1 kJ. The energy required to heat the zeolite from 45 ° C. to 70 ° C. and 70 ° C. to 200 ° C. was estimated to be about 1.75 kJ and 9.1 kJ, respectively. The energy removed by cooling from −40 ° C. to −50 was estimated to be about 0.7 kJ. The energy required to cool the zeolite from 190 ° C. to 45 ° C. and 200 ° C. to 190 ° C. (because energy may circulate from the cooled material to the heated material), from −50 ° C. Neglecting the energy required to heat the carbon to 0 ° C., the COP was estimated to be 0.7 / (2.1 + 1.75 + 9.1) = 0.054.

  Using a similar method, the module of FIG. 1 was calculated to have a COP of 0.22. The desorption cooling system of FIG. 2 is calculated to have a COP that is much greater than 0.22, which, due to the containment of the modules in the bank vessel 22, with each module A and B with less heat loss therefrom. This is because a fairly large uniform heating is realized.

[Example 2]
A demonstration device was developed and tested for the following evaluations.

1. Regenerator temperature optimization;
2. Cooling capacity by kJ;
3. Coefficient of performance (COP) or efficiency;
4.1 degree of temperature drop obtained in one cycle;
5). Influence on performance by time;
6). Probability of bending heating and cooling rates, or time to allow optimal time cycle design for commercial systems.

  A schematic and plan view of the demonstration device is shown in FIGS. 3a and b, where like reference numerals are used to indicate parts similar or identical to FIGS. The demonstration device 40 comprises one of the two modules A and B shown and described in FIG.

  Experiments are conducted to study and optimize one of the modules to gather relevant performance and design data, thereby allowing commercial module designs to be scaled up and down.

  The demonstration apparatus includes 102 identical cooler modules 10 (as shown in FIG. 1). The cooler module is stacked with insulated regenerators and desorption cooler chambers 26, 28, with each cooler module conduit 16 extending through a wall 24. In addition, insulated inlet 41, 42, 44 and outlet 46 ducts were provided to / from chambers 26, 28 to maximize heat transfer efficiency and minimize heat loss.

  The inlet of the regenerator chamber was connected to a hot air source and an ambient air source. The hot air source consists of an electric heater 48 that communicates the air flow with a coaxial fan 50 (fan 2) to generate hot air of various desired flow rates and temperatures. The ambient air source has another coaxial fan 52 (fan 3). A manually operated damper 54 was used between the hot air source and the ambient air source to selectively switch between the hot air and the ambient air. The desorption cooler chamber 28 was also connected to an ambient air source including a third coaxial fan 56 (fan 1).

  Appropriate thermocouples at regenerator inlet (T1, T8), regenerator outlet (T4), regenerator (T6), desorption cooler inlet (T3), regenerator outlet (T4), desorption cooler outlet (T5) Detected temperature changes during operation and recorded continuously. A data recording computer connected to a thermocouple was used to record the temperature during the test period.

[Operation]
The following steps were used to provide air flow cooling.
1. The data recording computer was turned on to record the temperature T at various locations as shown by the device 40 of FIG.
2. The damper 54 was manually switched to allow hot air to flow to the regenerator 26 via the heater 48, after which the fan 50 (fan 2) and the heater 48 were switched on.
3. Fan 56 (fan 1) was turned on to remove the heat generated by adsorption in the desorption cooler chamber 28. During the regeneration period, fan 52 (fan 3) was switched off.
4). When regenerator 26 achieved a temperature of 135 to 200 ° C and desorption cooler 28 was cooled to ambient temperature (20 to 25 ° C), heater 48 and fan 50 were switched off. The damper was then manually switched to allow ambient air from the fan 52 to enter the regenerator 26.
5). In this regard, the fan 52 was switched on while the fan 56 continued to operate to produce cool air flowing out of the desorption cooler 28.

  These steps completed one cycle of operation. For example, in a commercial system, module B generates a cooling effect while module A is regenerating, and when module B stops generating cold air, module A is energized to start generating cold air. It should be noted that. In this way, cold air can be continuously generated.

  Although the demonstration device has been tested with air, it should be noted that many other fluid streams can be used as heating and / or cooling media.

[Operating parameters and results]
During the test (eg, operation number 76 below, see Table 1), the regenerator 26 is heated with hot air (T1, T8) at 150-200 ° C. with a flow rate of about 250-300 liters / second. It was. The air flow through the desorption cooler chamber 28 was maintained at about 250 liters / second. Regeneration is considered complete when the air temperature T4 at the regenerator outlet 46 is the same as the inlet temperatures T1, T8 of 150-200 ° C and the regenerator temperature T6 reaches about 120-150 ° C. It is done. Heating is continued for a short extra time (eg, 20-30 minutes) to ensure complete regeneration.

  As shown in FIG. 4, regeneration was completed within the first 30 minutes (ie, T4 = T8). Furthermore, after 30 minutes, no significant change was observed in the regenerator temperature T6.

  After regeneration, the heater 48 and fan 50 were switched off and the position of the damper 54 was changed to allow ambient air from the fan 52 to cool the regenerator. During this time, the air flow rate by the fan 52 was maintained at about 250 to 450 liters / second.

  In most operations, the air flow to the desorption cooler 28 by the fan 56 was maintained in the range of 85 to 250 liters / second to generate cool exhaust air. As shown in FIG. 5, a temperature drop in the range of 5 ° C. to 7 ° C. (T5) is observed with desorbed cold exhaust air according to the relative humidity of the air (changed from 30% to 86%). It was. It was also observed that in the absence of air flow through the desorption cryochamber 28, the chamber temperature dropped by 11-14 ° C. according to ambient temperature.

  The cooling cycle was considered complete when the inlet (T3) and outlet (T5) temperatures were the same (ie, more than 100 minutes in FIG. 5). Further, as shown by FIG. 5, the total cooling period was about 60 minutes. In practice, however, it was noted that only 30 minute peak cooling needs to be considered consistent with a 30 minute heating cycle.

  The temperature plot of FIG. 6 records a special action consisting of a 25 minute regeneration period and a 25 minute cooling period. The operating conditions are shown in Table 2 (below). It has been discovered that reduced regeneration air temperatures of 150-170 ° C. can be used without significant loss of cooling capacity.

  Note that the inlet air temperature increased slightly during each operation. This was in particular due to the heat released from the fan motor but also due to changes in room temperature resulting from a small loss from the insulated surfaces of the heater, regenerator and associated ducts.

  The flow rate used in the commissioning is based on a heat conduction model. The air flow was estimated from the air velocity in a 1 meter long, 310 mm internal diameter duct fitted to each fan inlet. A digital anemometer (manufacturer Lutron, model YK-2001AL) was used to measure speed. The relative humidity and temperature around the demonstration device were measured with an accuracy of ± 10% using an electronic hygrometer (Manufacturer Erler & Weinkauff).

  Thermocouple calibration and accuracy were tested on a regular basis. The temperature was recorded to the second position according to the decimal system, which had an error of up to 10%.

  Based on the temperature and flow rate measured in more than 50 trial runs, the cooling capacity of the desorption cooler is estimated to be about 900-1200 kJ, and the coefficient of performance (COP) is the heat loss, humidity, regeneration efficiency, It varies between 0.07 and 0.12, depending on the measurement error. This indicates that favorable performance can be achieved with commercial scale-up. Tests were also performed to optimize operating conditions to obtain maximum cooling capacity and COP.

The performance of a single module was tested for about one year, and the demonstrator was tested for more than 6 months, with no performance degradation observed in any case.

  The foregoing descriptions of the preferred methods, apparatus, and systems, and the foregoing examples, are provided for purposes of illustration only and are not intended to limit the scope of the invention in any way. Furthermore, it should be appreciated that various other changes and modifications can be made to the embodiments in addition to those already described without departing from the basic inventive concept. All such changes and modifications should be considered within the scope of the present invention.

  It should also be understood that reference to prior art information herein does not constitute an admission that the information forms part of common general knowledge in Australia or any other country.

1 is a schematic view of a desorption cooler module according to the present invention. FIG. FIG. 2 is a schematic view of a desorption cooler system using a plurality of desorption cooler modules of FIG. 1 in accordance with the present invention. FIG. 2 is a schematic side view and plan view of a demonstration device for use in gas desorption cooling. The graph which shows the temperature change with respect to time in temperature position T8, T4, T6 of the regenerator of the apparatus of FIG. The graph which shows the temperature change with respect to time in temperature position T5, T3 of the desorption cooling device of the apparatus of FIG. The graph which shows the temperature change with respect to time in temperature position T1, T6, T4, T3, T5 of the verification apparatus of FIG.

Claims (34)

In the method of transferring heat using the first and second gas adsorbing materials, the second material is thermally relatively isolated from the first material, but the gas is continuously communicated. And
(I) heating the first material to desorb the gas adsorbed on the first material, and the gas generated thereby is sent to the second material and adsorbed;
(Ii) cooling the first material so that the gas desorbs from the second material and is adsorbed again from there onto the first material;
A method of heat transfer whereby the second material is cooled by desorbing a gas therefrom.   The method of claim 1, wherein in step (i), the first material is heated by heat conduction from a relatively hot fluid stream.   The method of claim 2 wherein the relatively hot fluid stream is a waste process gas or liquid.   4. A method according to any one of the preceding claims, wherein during the period in which the first material is heated, the second material is cooled with respect to the first material by heat conduction through a cooling fluid stream.   The method of claim 4, wherein the cooling fluid stream is an ambient air stream.   6. A method according to any one of the preceding claims, wherein in step (ii) the first material is cooled with respect to the second material by heat conduction to the surroundings or by heat conduction by a cooling fluid stream.   The method of claim 6, wherein the cooling fluid stream is an ambient air stream.   8. In step (ii), when the second material is being cooled by desorption of gas from the material, the second material is used to cool another fluid. The method according to claim 1.   9. The method of claim 8, wherein the other fluid stream is a process gas or liquid that requires cooling.   When desorption from the second material is complete, the second material is allowed to be slightly heated by heat conduction from the other fluid stream, the temperature of which is before the gas is adsorbed onto it. 10. A method according to claim 8 or 9, wherein the second material is just at a temperature sufficient to restore its temperature to a level corresponding to the temperature of step (i).   The method according to any one of claims 1 to 10, wherein the first gas adsorbent material has an adsorption power different from that of the second gas adsorbent material.   The method according to any one of claims 1 to 11, wherein the first gas adsorbent material is a material different from the second gas adsorbent material.   The method according to any one of claims 1 to 12, wherein the first gas adsorbent material is zeolite and the second gas adsorbent material is activated carbon.   The method according to any one of claims 1 to 13, wherein the gas adsorbed on the first and second materials is carbon dioxide.   15. A method according to any one of the preceding claims, wherein the gas is pressurized with respect to ambient pressure.   The method of claim 15, wherein the gas is pressurized to about 0.5 MPa.   17. A method according to any one of claims 1 to 16, wherein the gas and the first and second materials are generally at ambient temperature prior to the starting step (i).   A heat transfer method substantially as herein described with reference to the accompanying drawings and / or examples.   In a heat transfer device comprising a chamber having a first part containing a first adsorbent material and a second part containing a second adsorbent material, the first and second parts are always A heat transfer device connected in such a way as to allow continuous gas communication therebetween and is relatively thermally isolated from each other.   The first and second portions are configured to minimize conduction of conduction heat between the first portion and the second portion while allowing continuous gas communication between the portions. 20. The device of claim 19, wherein the devices are joined by sections.   21. The apparatus of claim 20, wherein the section is a conduit having a width that is small compared to a width of the first and second chamber portions adjacent thereto.   The apparatus according to any one of claims 19 to 21, wherein one or more heat conducting elements are disposed in each of the first and second chamber portions together with the first and second adsorbent materials.   Each heat transfer element includes a metal wire mesh that enhances heat communication between the exterior of the chamber portion and the adsorbent material therein, through each of the first and second adsorbent materials. 24. The device of claim 22, wherein the device increases the mass transport rate.   20. The first and second chamber portions are each configured to be located in an intermediate flow of a respective fluid flow so as to conduct heat between each fluid and those portions. 24. The apparatus according to any one of 23.   25. An apparatus according to any one of claims 19 to 24, wherein the first and second materials are each packed in a respective portion of the chamber.   25. Apparatus according to any one of claims 19 to 24, wherein the first and second materials are defined in claim 12 or 13.   A heat transfer device substantially as herein described with reference to the accompanying drawings and / or examples. In a system for continuously conducting heat from a first fluid stream and continuously cooling a second fluid stream, the system can be in thermal communication with the first and second fluid streams, respectively. First and second devices, each device comprising a chamber having separated first and second adsorbent materials, each device being operable in the following stages: Yes, that is,
(1) The first material is heated by thermal communication with the first fluid stream so as to desorb the gas adsorbed on the first material, whereby the gas is sent to the second material. And
(2) The first material is cooled so that the gas is desorbed from the second material and sent from there so that it is again adsorbed to the first material, from which the second material is gaseous Is cooled by desorption, and the second fluid stream is cooled by thermal communication with the second material;
the system,
While the first device is operated under step (1) to heat the first material of the first device using the first fluid stream, the second device is under step (2). The gas is operated to cool the second fluid stream by desorbing from the second material of the second device;
Thereafter, the first fluid flow can be directed to the second device, operated under stage (1) of the second device, the second fluid flow directed to the first device, and the first device Operated under stage (2) of the equipment of
Thereby, a system for efficiently conducting continuous conduction of heat from the first fluid stream and continuously cooling the second fluid stream.   30. The system of claim 28, comprising a plurality of first devices and a plurality of second devices.   30. The system of claim 28 or 29, wherein the first and second devices are operated in parallel.   And a valve for selectively switching the flow of the first and second fluid flows between the first device and the second device, and between the second device and the first device, respectively. 21. A system according to any one of claims 28 to 20, comprising, thereby maintaining continuous conduction of heat from the first fluid stream and continuous cooling of the second fluid stream.   The system according to any one of claims 28 to 31, wherein each of the first and second devices has a configuration defined in any one of claims 19 to 27.   33. A system according to any one of claims 28 to 32, wherein each of the first and second devices is operated using the method described in any one of claims 1 to 18.   A system for conducting heat continuously from a first fluid stream and continuously cooling a second fluid stream substantially as herein described with reference to the accompanying drawings and / or examples.

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