GB2088548A - Thermal storage heating system - Google Patents
Thermal storage heating system Download PDFInfo
- Publication number
- GB2088548A GB2088548A GB8111392A GB8111392A GB2088548A GB 2088548 A GB2088548 A GB 2088548A GB 8111392 A GB8111392 A GB 8111392A GB 8111392 A GB8111392 A GB 8111392A GB 2088548 A GB2088548 A GB 2088548A
- Authority
- GB
- United Kingdom
- Prior art keywords
- heat
- evaporator
- fusion
- store
- adsorber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000010438 heat treatment Methods 0.000 title claims abstract description 6
- 230000004927 fusion Effects 0.000 claims abstract description 49
- 239000002156 adsorbate Substances 0.000 claims abstract description 39
- 239000003463 adsorbent Substances 0.000 claims abstract description 19
- 238000009833 condensation Methods 0.000 claims abstract description 10
- 230000005494 condensation Effects 0.000 claims abstract description 10
- 238000009736 wetting Methods 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 35
- 239000007788 liquid Substances 0.000 claims description 19
- 229910021536 Zeolite Inorganic materials 0.000 claims description 11
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 11
- 239000010457 zeolite Substances 0.000 claims description 11
- 238000000034 method Methods 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 10
- 235000021355 Stearic acid Nutrition 0.000 claims description 8
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 claims description 8
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 claims description 8
- 239000008117 stearic acid Substances 0.000 claims description 8
- 230000005855 radiation Effects 0.000 claims description 7
- 238000001179 sorption measurement Methods 0.000 claims description 7
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- 108010053481 Antifreeze Proteins Proteins 0.000 claims description 3
- 230000002528 anti-freeze Effects 0.000 claims description 3
- 230000008018 melting Effects 0.000 claims description 2
- 238000002844 melting Methods 0.000 claims description 2
- 238000012986 modification Methods 0.000 claims 1
- 230000004048 modification Effects 0.000 claims 1
- 230000003134 recirculating effect Effects 0.000 claims 1
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 230000005611 electricity Effects 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 238000007710 freezing Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 229910001628 calcium chloride Inorganic materials 0.000 description 2
- 239000001110 calcium chloride Substances 0.000 description 2
- IPCSVZSSVZVIGE-UHFFFAOYSA-N hexadecanoic acid Chemical compound CCCCCCCCCCCCCCCC(O)=O IPCSVZSSVZVIGE-UHFFFAOYSA-N 0.000 description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 2
- 239000000155 melt Substances 0.000 description 2
- 235000021314 Palmitic acid Nutrition 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- XMBWDFGMSWQBCA-UHFFFAOYSA-N hydrogen iodide Chemical compound I XMBWDFGMSWQBCA-UHFFFAOYSA-N 0.000 description 1
- 229910000043 hydrogen iodide Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- WQEPLUUGTLDZJY-UHFFFAOYSA-N n-Pentadecanoic acid Natural products CCCCCCCCCCCCCCC(O)=O WQEPLUUGTLDZJY-UHFFFAOYSA-N 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- OLTHARGIAFTREU-UHFFFAOYSA-N triacontane Natural products CCCCCCCCCCCCCCCCCCCCC(C)CCCCCCCC OLTHARGIAFTREU-UHFFFAOYSA-N 0.000 description 1
- YNJBWRMUSHSURL-UHFFFAOYSA-N trichloroacetic acid Chemical compound OC(=O)C(Cl)(Cl)Cl YNJBWRMUSHSURL-UHFFFAOYSA-N 0.000 description 1
- SUJUOAZFECLBOA-UHFFFAOYSA-N tritriacontane Chemical compound CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCCC SUJUOAZFECLBOA-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B29/00—Combined heating and refrigeration systems, e.g. operating alternately or simultaneously
- F25B29/006—Combined heating and refrigeration systems, e.g. operating alternately or simultaneously of the sorption type system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24D—DOMESTIC- OR SPACE-HEATING SYSTEMS, e.g. CENTRAL HEATING SYSTEMS; DOMESTIC HOT-WATER SUPPLY SYSTEMS; ELEMENTS OR COMPONENTS THEREFOR
- F24D11/00—Central heating systems using heat accumulated in storage masses
- F24D11/02—Central heating systems using heat accumulated in storage masses using heat pumps
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D20/00—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00
- F28D20/003—Heat storage plants or apparatus in general; Regenerative heat-exchange apparatus not covered by groups F28D17/00 or F28D19/00 using thermochemical reactions
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/14—Thermal energy storage
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
A heating system comprises an evaporator (10) housing an adsorbate (15) and a heat exchanger (36), an adsorber (1) in communication with the evaporator (10) and housing adsorbent (17), a heat of fusion heat store (22) in communication with the adsorber (1) and with the evaporator (10), means (2) for supplying heat to the adsorbent in the adsorber e.g. a resistive heater, means (11) for extracting heat from the adsorber, e.g. a heat exchanger, means (8) for extracting heat from the heat of fusion heat store e.g. a heat exchanger, means (27) for wetting the heat exchanger housed in the evaporator (e.g. a sprinkler) and means (20) for assisting the condensation of vapour passing from the adsorber to the heat of fusion heat store, e.g. a sprinkler. <IMAGE>
Description
SPECIFICATION
Adsorption heat pump
This invention relates to an adsorption heat pump used in conjunction with a heat of fusion heat store.
Various systems involving a solar radiation collector and a vapour-compression heat pump have been proposed, but one problem which may impede the adoption of such systems is the relatively high cost of suitable motor/compressor sets. It is also possible to construct an absorption heat pump using methanol and mixed LiBr, ZnBr salts which will pump het from -5 C to 60+"C with a coefficient of performance (COP) in the region of 1.5. If provided with a suitable 60+"C heat store such a heat pump could be operated by off-peak electricity and couid replace the boiler in an existing piped hot water central heating system. Unfortunately, however, methanol is both toxic and highly flammable. It is classified as a group 3 refrigerant and is restricted in Britain to industrial use.We have now devised a relatively cheap adsorption heat pump system which does not need to use toxic substances for domestic pumps and which can operate at a coefficient of performance (C.O.P.) of about 1.74 using off-peak power.
According to this invention a heating system comprises an evaporator housing adsorbate and a heat exchanger. There is an adsorber housing adsorbent in communication with the evaporator and a heat of fusion heat store in communication with the adsorber and with the evaporator. There are means for supplying heat to the adsorbent in the adsorber, means for extracting heat from the adsorber and means for extracting heat from the heat of fusion heat store. There are also means for wetting the heat exchanger housed in the evaporator with liquid and means for assisting the condensation of vapour passing from the adsorber to the heat of fusion heat store.
The evaporator houses a heat exchanger. This heat exchanger is preferably an extended surface heat exchanger and may be an air blown heat exchanger or it may have liquid circulated therethrough. In the latter case the heated liquid may be obtained from a solar radiation collector.
The solar radiation collector can take various forms and may for example comprise a simple unglazed receiver through which an ethylene glycol solution circulates. Usually the temperature of the fluid, e.g. water or ethylene glycol solution, extracting heat from the solar radiation collector will be fairly low, e.g. from -5" to 15"C.
Preferably the solar energy is delivered to a low temperature heat store before it is delivered to the adsorbate housed in the evaporator by for example, heat exchange. A suitable low temperature heat store is described in our copending patent application 8038284 which claims and describes a heat store comprising a tank containing a liquid having a freezing point of below 0 C in which is immersed at least one liquid-tight and heat conducting container housing a plurality of different substances each of freezing point between -5 C and +18"C and with a latent heat of fusion of above 125 kJ/kg, a solar radiation collector associated with the tank so that heat obtained from the collector can be transmitted to the liquid in the tank and means for extracting heat from said liquid.
In any case it will be desirable to accept heat from the heat exchanger housed within the evaporator at temperatures as low as -8 C. It is desirable therefore that the adsorbate within the evaporator and elsewhere be a liquid with a relatively low freezing point.
Suitable liquids include a solution of water and a suitable low vapour pressure anti-freeze such as calcium chloride or ethylene glycol.
Communicating with the evaporator e.g. by a valved conduit, is an adsorber which houses adsorbent. There are also means for supplying heat to the adorbent in the adsorber and this may be an electrical resistive heater, run for example by offpeak electricity.
It is desirable that the adsorber should be able to be recharged at very low vapour pressures and consequently the preferred adsorbent/adsorbate system is a 4A zeolite molecular sieve/water. However it would be possible to use an activated charcoal/ hydrogen iodide system or other zeolite molecular sieves with water e.g. 1 3x zeolite molecular sieve.
There are means for extracting heat from the adsorber and this is preferably a heat exchanger.
Thus for example, a pipework in which adsorbate, e.g. water, circulates communicating with the heat of fusion heat store, may be provided with a coiled section which is surrounded by the adsorbent housed in the adsorber. This pipework should preferably have a circulation pump therein. One preferred form of heat exchanger is that claimed in ourcopending application 8036901. This is a heat exchanger comprising a structure supporting a continuous pipeworkthrough which liquid can pass and ducts with pervious walls spaced from and adjacent to the pipework, the structure and pipework being made of heat conducting material. There are also means capable of housing solid material adjacent to, but external of the ducts.
Communication with the adsorber is a heat of fusion heat store, e.g. by means of a valved conduit.
This heat store comprises a container in which there are one or more liquid-tight heat conducting receptacles, for example plastic or elastomeric bags, each of which houses a substance with a relatively high heat of fusion i.e. above 150 joules/gm. These receptacles are preferably made of flexible material to cope with expansion and contraction of the substance housed therein. For the purpose of this invention this substance must melt at a temperature of between 40"C and 80"C. A particularly preferred substance is stearic acid which melts at 64"C and has a latent heat of 199 joules/gm.Other suitable substances are trichloroacetic acid (m.p. 57.5"C, latent heat 360
J/gm) tritriacontane (C33H68) (m.p.71.1 C, latent heat 226 J/gm) and palmitic acid (m.p. 61.8"C, latent heat 166 J/gm). When the system is in use there will also be adsorbate in this heat store surrounding the receptacles.
There are means for extracting heat from the heat of fusion heat store. This may be by heat exchange, wherein a pipework in which a liquid such as water, circulates, is in heat exchange relationship with the liquid, i.e. adsorbate in the heat of fusion heat store.
However, when the adsorbate comprises water, the most convenient means for extracting heat is the circulation of the adsorbate in the heat of fusion heat store through a pipeworkwhich delivers heattothe load or to a heat exchanger in circuit with the load.
There are means for wetting the heat exchanger housed in the evaporator with liquid. These means are preferably a sprinkler located in the evaporator above the heat exchanger. The liquid which will be adsorbate is preferably collected from the bottom of the evaporator and recirculated by means of a circulation pump to the sprinkler. Alternative means for wetting the heat exchanger comprises the use of water absorbent coatings which displace evaporated water by capillary action.
There are also means for assisting the condensation of vapour passing from the adsorberto the heat of fusion heat store, preferablytothetop region thereof. This is conveniently a circulating system comprising a circulation pump and a sprinkler wherein liquid from the bottom of the heat of fusion heat store is recirculated to the top of the heat of fusion heat store where it emerges through the sprinkler. This sprinkler is located at the top of the heat of fusion heat store near where it is preferred that vapour from the adsorber enters the heat of fusion heat store. There are preferably two valves in this recirculation system so that condensed adsorbate can be apportioned to the sprinkler and a heat exchanger designed to supply heat to the load, i.e.
the means for extracting heat from the heat of fusion heat store. In this way not all the heat produced need be stored in the heat of fusion heat store, but some can be used to supply domestic hot water for example.
There are also preferably means for transferring liquid from the heat of fusion heat store to the evaporator. This is preferably by means of a valved conduit connecting the heat of fusion heat store with the evaporator.
The system operates as follows:
The system receives heat from an external source by way of the heat exchanger in the evaporator. This may be a solar radiation collector or the heat exchanger may be air blown. The heat supplied causes adsorbate to be evaporated from the evaporator and this vapour passes to the adsorber where it is adsorbed, the heat of adsorption being transferred to the heat offusion heat store and thence to the load. This transfer of heat is achieved by use of the means for extracting heat from the adsorber. Adsorbate, e.g. water, is circulated through the heat exchanger in the adsorber and hot adsorbate is delivered to the heat of fusion heat store where it melts the substance of relatively high heat of fusion, e.g. stearic acid, housed in the receptacles, e.g.
plastic bags. Some of the hot adsorbate may be circulated through the pipeworkwhich delivers heat to the load.
When the adsorber is full charged with adsorbate it may be stripped. This is achieved by supplying heat to the adsorbent, e.g. by a resistive heater, operated by cheap off peak electricity at night time.
The desorbed adsorbate vapour thereafter passes to the heat of fusion heat store where it gives up its latent heat of condensation thereby melting the substance of relatively high heat of fusion housed in the liquid-tight receptacles in the heat store.
Atthecompletion of the stripping process (when no more heat is supplied) the temperature of the adsorbent will be high and it can be quenched back to a lower temperature by intermittently circulating adsorbate from the heat of fusion heat store through the heat exchanger associated with the adsorber.
This operation is controlled by the vapour pressure within the heat of fusion heat store and the excess sensible heat is thus transferred to the heat store.
When the desired lower temperature is achieved, the adsorbate which was transferred to the heat of fusion heat store from the adsorber during the stripping (desorption) process can be transferred to the evaporator by means of opening the valve in the valved conduit connecting the heat of fusion heat store with the evaporator. This valve should be closed when the vapour pressure of adsorbate in the heat of fusion heat store falls below the saturated vapour pressure of adsorbate at the desired lower temperature. Heat can be obtained from the heat store by circulating the liquid contained therein, i.e.
adsorbate, through the pipework delivering heat to the load. As the temperature in heat store cools the molten substance e.g. stearic acid housed in the receptacles will condense, giving up its heat of condensation to the adsorbate housed in the heat of fusion heat store.
The two steps of evaporating adsorbate from the evaporator and stripping adsorbate from the adsorbent can of course be reversed. In practice however, these steps will be repeated indefinitely as long as heat is required to be delivered to the load.
A preferred form of heating system is now described with reference to the accompanying drawing.
The evaporator 10 houses water containing calcium chloride anti-freeze 15 as the adsorbate. Heat is transmitted to the water 10 from the coils of an extended surface heat exchanger 36 which in turn receives its heat from an air blown heat exchanger (not shown).
Connected to the evaporator 10 by means of a conduit 16 containing a valve 3 is an adsorber 1. This adsorber 1 houses 4A zeolite molecular sieve 17 and is heated by a resistive heater 2 operated by off-peak electricity at night.
A conduit 18 is provided with a heat exchanger coil 11 located in the zeolite 17 and a pump 19. This conduit 18 contains water and connects to both the top and the bottom of a heat of fusion heat store 22.
Connected to the top of the adsorber 17 is a conduit 21 having a valve 4 which is also connected to the top of the heat of fusion heat store 22. The heat store 22 contains liquid adsorbate (water) 24 and a series of plastic bags 7. Each bag contains stearic acid (m.p. 65"C, latent heat of fusion 199 joules/gm). The bottom of the heat store 22 is connected by conduit 12, having pump 13 and also valve 14tothe heatexchanger8which supplies heat to the load. There is a branch conduit 9 having valve 5 which connects conduit 12 with a conduit 6, this conduit 6 connecting the heat exchanger 8 with a sprinkler 20 located in the top of the heat store 22.
There is a conduit 28 having valve 29 connecting the upper region of heat store 22 with the upper region of the evaporator 10. Finally there is a pump around system for the evaporator 10 consisting of a conduit 25 having a pump 26 connecting the bottom of the evaporator 10 with a sprinkler 27 located in the top of the evaporator 10.
In operation the evaporator 10 receives heat from the extended surface heat exchanger 36, but the temperature can be as low as -8 C. The heat exchanger 36 is wetted by the pump around system comprising pump 26 and sprinkler 27. Water vaporised at low temperature and pressure passes through valve 3 and is adsorbed by the zeolite 17 in the adsorber 1. In this particular embodiment up to 179 of water per 100 g of zeolite may be adsorbed at about 70"C and at a pressure corresponding to the vapour pressure of water at -50C. The heat of adsorption which is thereby produced is transferred to the heat store 22 via the heat exchanger 11 using pump 19 and conduit 18. Heat is provided to the load by circulating adsorbate through heat exchanger 8 by means of pump 13, valve 14 being open.
When the adsorber 1 is fully charged it may then be discharged. To do this resistive heater 2 is operated, e.g. at night using cheap off-peak electricity, with valve 3 shut and valve 4 open and water vapour is desorbed from the zeolite 17 passing through conduit 21 and valve 4 to the top of the heat store 22. Here the water vapour condenses giving up its latent heat of condensation in order to melt the stearic acid in the bags 7. During this stripping or discharging operation pump 19 is stopped and the water in heat exchanger 11 is allowed to drain to heat store 22. Water circulation through the heat store 22 and jet condensation are achieved by the pump around system comprising circulating pump 13, conduits 12,9 and 6 and sprinkler 20.The valves 5 and 14 allow the flow of hot adsorbate (water) by pump 13 to be apportioned between the sprinkler 20 and the heat exchanger 8 which supplies heat to the load.
At the saturated vapour pressure of water at 700C and at a temperature of 300"C the zeolite will lose water until it contains about 4 grams of water per 100 grams so that its working capacity is about 13 grams/100 grams. The stripped water vapour will condense in heat store 22 and melt the stearic acid in bags 7 so that its heat of condensation is stored at 65"C. At the completion of the stripping operation the adsorbent 17 will be at a temperature of 300"C. It is then quenched back to 70"C by starting pump 19 in intermittent operation controlled by the vapour pressure within the heat store 22 and the excess sensible heat is thus transferred to the heat store 22.
When the temperature in adsorber 1 reaches 70"C valve 29 is opened and the water which was transferred from adsorber 1 to heat store 22 is allowed to return to evaporator 10, valve 19 being shut when the vapour pressure within heat store 22 falls below the saturated vapour pressure of water at 70"C.
When the stripping operation is completed, charging of the adsorber 1 by evaporating water from the evaporator 10 re-commences as described above.
The latent heat of evaporation of water at 70"C is about 1000 BthU/1 b whilst the heat of adsorption will be about 1400 BthU/1 b. When allowance is made for the sensible heat accumulated between 70"C and 300"C by the zeolite then the heat required to strip it will be about 1900 BthU/1b,thereforethe expected
COP will be 2900/1900 = 1.526 which is about the same as that for a methanol absorption heat pump working over the same temperature range. Each 100 pounds of adsorbent will itself store 18,200 BthU and associated with this will be a further 19,500 BthU in the heat of fusion heat store. This will require 228 pounds of stearic acid suitably encapsulated.
Claims (19)
1. A heating system comprising an evaporator housing an adsorbate and a heat exchanger, an adsorber in communication with the evaporator and housing adsorbent, a heat of fusion heat store in communication with the adsorber and with the evaporator, means for supplying heat to the adsorbent in the adsorber, means for extracting heat from the adsorber, means for extracting heat from the heat of fusion heat store, means for wetting the heat exchanger housed in the evaporator and means for assisting the condensation of vapour passing from the adsorberto the heat of fusion heat store.
2. A system according to claim 1 which includes an air blown heat exchanger for transferring heat to the evaporator.
3. A system according to either of claims 1 and 2 wherein the adsorbent is 4A zeolite molecular sieve and the adsorbate is water.
4. A system according to any one of the preceding claims wherein the adsorbate housed in the evaporator is an aqueous anti-freeze solution.
5. A system according to any one of the preceding claims wherein the means for extracting heat from the adsorber is a heat exchanger.
6. A system according to any one of the preceding claims wherein the heat of fusion heat store comprises receptacles containing stearic acid.
7. A system according to any one of the preceding claims wherein the adsorbate is water and the means for extracting heat from the heat of fusion heat store comprises a pipework through which said water circulates, delivering heat to the load our a heat exchanger in circuit with the load.
8. A system according to any one of the preceding claims wherein the means for wetting the heat exchanger located in the evaporator comprises a sprinkler located above the heat exchanger, said means being capable of circulating adsorbate from the bottom of the evaporator to the sprinkler.
9. A system according to any one of the preceding claims wherein the means for assisting the condensation of vapour passing from the adsorber comprises a circulation pump and a sprinkler capable of recirculating liquid from the bottom of the heat of fusion heat store to the sprinkler which is located in the upper region of the heat store.
10. A system according to any one ofthe preceding claims which includes means for transferring liquid from the heat of fusion heat store to the evaporator.
11. Asystem according to claim 1 substantially as hereinbefore described with reference to the drawing.
12. A method of obtaining heatwherein (a) a source of heat is used to evaporate adsorbate from an evaporator which is thereafter adsorbed by an adsorbent in an adsorber, the latent heat of adsorption thereby produced providing heattothe load, and (b) a source of heat is used to desorb the adsorbate from the adsorbent in the adsorber which thereafter condenses in a heat of fusion heat store, melting a substance with a relatively high latent heat of fusion which thereafter solidifies, the resulting latent heat of fusion providing heat to the load.
13. A modification of the method according to claim 11 wherein steps (a) and (b) are reversed.
14. A method according to either of claims 12 and 13 wherein the source of heat in step (a) is a solar radiation collector
15. A method according to either of claims 12 and 13 wherein the source of heat in step (a) is an air blowm heat exchanger.
16. A method according to any one of claims 12 to 15 wherein the source of heat in step (b) is electrical resistive heat.
17. A method according to any one of claims 12 to 16 wherein atthecompletion of steps (b) adsorbent is cooled by intermittently circulating adsorbate from the heat of fusion heat store through a heat exchanger associated with the adsorber.
18. A method according to claim 17 wherein when the adsorbent has been cooled adsorbate is transferred from the heat of fusion heat store to the evaporator.
19. A method according to claim 12 wherein heat is obtained from the system according to any one of claims 1 to 11.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8111392A GB2088548B (en) | 1980-11-28 | 1981-04-10 | Thermal storage heating system |
| DE19813146902 DE3146902A1 (en) | 1980-11-28 | 1981-11-26 | HEATING SYSTEM |
| FR8122378A FR2495294A1 (en) | 1980-11-28 | 1981-11-30 | ADSORPTION PUMP HEATING INSTALLATION AND METHOD OF USE |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB8038285 | 1980-11-28 | ||
| GB8111392A GB2088548B (en) | 1980-11-28 | 1981-04-10 | Thermal storage heating system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2088548A true GB2088548A (en) | 1982-06-09 |
| GB2088548B GB2088548B (en) | 1984-10-03 |
Family
ID=26277664
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8111392A Expired GB2088548B (en) | 1980-11-28 | 1981-04-10 | Thermal storage heating system |
Country Status (3)
| Country | Link |
|---|---|
| DE (1) | DE3146902A1 (en) |
| FR (1) | FR2495294A1 (en) |
| GB (1) | GB2088548B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0085525A2 (en) * | 1982-01-29 | 1983-08-10 | Exxon Research And Engineering Company | A process of adsorption |
| EP0086383A2 (en) * | 1982-02-15 | 1983-08-24 | Hieronimi, Ulrich-M. | Sorption apparatuses and method of operating the same |
| FR2536514A1 (en) * | 1982-11-23 | 1984-05-25 | Exxon Research Engineering Co | METHOD FOR OPERATING A SORPTION HEAT PUMP AND APPARATUS FOR CARRYING OUT SAID METHOD |
| EP0386003A1 (en) * | 1987-07-07 | 1990-09-12 | International Thermal Packaging, Inc. | Self-contained cooling apparatus |
| EP0505381A1 (en) * | 1989-10-12 | 1992-09-30 | International Thermal Packaging, Inc. | Cooling device with improved waste-heat handling capability |
| US20140053577A1 (en) * | 2012-08-22 | 2014-02-27 | Kabushiki Kaisha Toyota Chuo Kenkyusho | Adsorption heat pump system and method of generating cooling power |
| EP2808640A3 (en) * | 2013-05-21 | 2015-04-08 | European Thermodynamics Limited | Energy storage |
| US20230075850A1 (en) * | 2021-08-27 | 2023-03-09 | City University Of Hong Kong | Compact membrane-based thermochemical energy storage system |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE337608A (en) * | ||||
| US1729081A (en) * | 1924-10-25 | 1929-09-24 | Silica Gel Corp | Refrigeration |
| US1826436A (en) * | 1926-11-15 | 1931-10-06 | Edmund E Allyne | Refrigerating system |
| FR663153A (en) * | 1927-10-31 | 1929-08-17 | Condenser refrigeration machine | |
| GB388352A (en) * | 1930-05-14 | 1933-02-23 | Wulff Berzelius Normelli | Process for the carrying away of waste heat developed in absorption refrigerators |
| US2166677A (en) * | 1937-03-10 | 1939-07-18 | Crosley Corp | Refrigerating apparatus |
| FR988886A (en) * | 1944-01-26 | 1951-09-03 | Water heater combined with a refrigerator | |
| DE2629441A1 (en) * | 1976-06-30 | 1978-01-05 | Linde Ag | Heat pump for power station waste heat - has ammonia soln. strengths in absorber and desorber maintained by circuit with pump, throttle and heat exchanger |
| GB1572737A (en) * | 1977-01-17 | 1980-08-06 | Exxon France | Heat pump |
| DE2808464A1 (en) * | 1977-03-01 | 1978-09-21 | Pro Elektra Ag Baden | Storage of heat for subsequent use - using reversible chemical reaction with greatly reduced ambient losses |
| US4138861A (en) * | 1977-03-24 | 1979-02-13 | Institute Of Gas Technology, A Nonprofit Corporation | Solid adsorption air conditioning apparatus and method |
| CH635415A5 (en) * | 1978-09-13 | 1983-03-31 | Sulzer Ag | ABSORPTION HEAT PUMP SYSTEM. |
-
1981
- 1981-04-10 GB GB8111392A patent/GB2088548B/en not_active Expired
- 1981-11-26 DE DE19813146902 patent/DE3146902A1/en not_active Withdrawn
- 1981-11-30 FR FR8122378A patent/FR2495294A1/en active Granted
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0085525A2 (en) * | 1982-01-29 | 1983-08-10 | Exxon Research And Engineering Company | A process of adsorption |
| EP0085525A3 (en) * | 1982-01-29 | 1986-01-22 | Exxon Research And Engineering Company | A process of adsorption |
| EP0086383A2 (en) * | 1982-02-15 | 1983-08-24 | Hieronimi, Ulrich-M. | Sorption apparatuses and method of operating the same |
| EP0086383A3 (en) * | 1982-02-15 | 1983-11-16 | Hieronimi, Ulrich-M. | Sorption apparatuses and method of operating the same |
| FR2536514A1 (en) * | 1982-11-23 | 1984-05-25 | Exxon Research Engineering Co | METHOD FOR OPERATING A SORPTION HEAT PUMP AND APPARATUS FOR CARRYING OUT SAID METHOD |
| EP0386003A4 (en) * | 1987-07-07 | 1991-11-06 | International Thermal Packaging, Inc. | Self-contained cooling apparatus |
| EP0386003A1 (en) * | 1987-07-07 | 1990-09-12 | International Thermal Packaging, Inc. | Self-contained cooling apparatus |
| EP0505381A1 (en) * | 1989-10-12 | 1992-09-30 | International Thermal Packaging, Inc. | Cooling device with improved waste-heat handling capability |
| EP0505381A4 (en) * | 1989-10-12 | 1993-05-19 | International Thermal Packaging, Inc. | Cooling device with improved waste-heat handling capability |
| US20140053577A1 (en) * | 2012-08-22 | 2014-02-27 | Kabushiki Kaisha Toyota Chuo Kenkyusho | Adsorption heat pump system and method of generating cooling power |
| US9863673B2 (en) * | 2012-08-22 | 2018-01-09 | Kabushiki Kaisha Toyota Chuo Kenkyusho | Adsorption heat pump system and method of generating cooling power |
| EP2808640A3 (en) * | 2013-05-21 | 2015-04-08 | European Thermodynamics Limited | Energy storage |
| US20230075850A1 (en) * | 2021-08-27 | 2023-03-09 | City University Of Hong Kong | Compact membrane-based thermochemical energy storage system |
| US11988454B2 (en) * | 2021-08-27 | 2024-05-21 | City University Of Hong Kong | Compact membrane-based thermochemical energy storage system |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2495294A1 (en) | 1982-06-04 |
| FR2495294B1 (en) | 1984-01-13 |
| GB2088548B (en) | 1984-10-03 |
| DE3146902A1 (en) | 1982-08-05 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |