EP0130908B1 - Heat transfer process with a three-phase monovariant reaction - Google Patents
Heat transfer process with a three-phase monovariant reaction Download PDFInfo
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- EP0130908B1 EP0130908B1 EP84401360A EP84401360A EP0130908B1 EP 0130908 B1 EP0130908 B1 EP 0130908B1 EP 84401360 A EP84401360 A EP 84401360A EP 84401360 A EP84401360 A EP 84401360A EP 0130908 B1 EP0130908 B1 EP 0130908B1
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- 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
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
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- 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
- F25B17/00—Sorption machines, plants or systems, operating intermittently, e.g. absorption or adsorption type
Definitions
- the present invention relates to a thermochemical process for carrying out calorie transfers between a first source of calories and a second source of calories.
- the process is implemented according to an intermittent cycle of heat storage and destocking.
- thermochemical processes having either continuous operation or intermittent operation, which can operate to supply calories - heating or to take off - cooling.
- the invention provides, on the contrary, a method which implements a monovariant system, that is to say a system for which the relationship between the logarithm of the pressure and I / T is unique and almost linear.
- thermochemical heat pumps a process implementing a three-phase monovariant system for which the absorption of gas by a saturated solution corresponds to a single equilibrium, c that is to say that one has only one reaction, whereas Mar considered that the heat exchange takes place during two distinct reactions each concerning a different solid compound.
- the invention provides a thermochemical process for transferring calories from a first heat source to a second heat source by using a reaction medium.
- This process is characterized in that the exchange of calories between one of the two sources and the said reaction medium takes place during a reaction between a gas and a liquid phase constituted by a solution saturated with solid whereas the exchange of calories between the second source and the reaction medium takes place during a gas-liquid phase change reaction of said gas or of absorption of the gas on a solid, the two reactions taking place in a closed medium and being monovariant.
- the gas may consist of water vapor or ammonia, or alternatively chosen from methanol, ethanol, butanol, methylamine, dimethylamine, trimethylamine, ethylamine, diethylamine, fluoroalkanes , chlorinated fluoroalkanes, difluoromethylsilane, chlorodifluorosilane, disiloxane, propane, butane, acetone and acetaldehyde, the fluoroalkanes themselves being chosen from CC1 3 F, CCl 2 F 2 , CHCI 2 F, CHCIF 2 , C1 3 C 2 F 3 , C1 2 C 2 F 4 , C 2 HCIF 4 , C 2 H 2 CIF 3 , CH 2 CIF and C 2 H 2 F 4 .
- the heat pump comprises a saturated solution, in the liquefied gas, of a solid chosen from CaCI 2 , KOH, LiCI, LiBr, ZnCl 2 , ZnBr 2 and the gas, in these cases, is H 2 0.
- a solid chosen from CaCI 2 , KOH, LiCI, LiBr, ZnCl 2 , ZnBr 2 and the gas, in these cases, is H 2 0.
- the heat pump comprises a reactor (1) and a reactor (2), interconnected by the pipe (3).
- Each reactor is provided with a heat exchanger (4) to (5) allowing the exchange of calories between the reaction medium and the external sources of calories.
- the reactor (1) contains the liquid in equilibrium with its vapor phase
- the reactor (2) contains the saturated solid solution.
- the gas coming from the reactor (1) condenses at the saturated solution and releases its latent heat of condensation ⁇ H while diluting the solution.
- the differential heat of dilution of the saturated solution is ⁇ H D , it is an exothermic reaction.
- excess solid dissolves to maintain the concentration at saturation, with a heat ⁇ H S of dissolution of the salt in the saturated solution.
- the gas evaporates from the solution contained in the reactor (2) to go to the reactor (1) which then plays the role of condenser.
- the solution is concentrated and the solid must crystallize.
- the enthalpies involved are the same as before, in opposite sign.
- FIG. 4 shows a heating installation allowing the implementation of the method according to the invention, and in which the heating period corresponds only to the destocking phase. It is understood that, as mentioned above, the installation could also be used for heating during the storage period.
- Part A of Figure 4 represents the storage phase while part B represents the destocking phase.
- the heat pump is symbolized by its two reactors (1) and (2) and by the gas line (3).
- the reactor (1) is connected to a hot source constituted, in the installation shown, by a solar collector (12).
- the calories given up in the reactor (2) during the condensation of the gas are released into the atmosphere, but they could as well be used for heating or even be stored.
- the reactor (2) is supplied with calories by a cold source, symbolized by the arrow (11). The calories are recovered in the reactor (1) and used for heating.
- the three-phase system used was the saturated solution of lithium chloride, water vapor and lithium chloride monohydrate.
- the range of existence of the hydrate in solid form with the saturated solution is between 19 and 95 ° C.
- the mass storage capacity, measured between a storage operation at 90 ° C and a destocking operation at 45 ° C, was 146 Wh / kg.
- a temperature rise of approximately 41 ° C. (AT) was obtained.
- phase rule shows that the system is monovariant.
- FIG. 3 shows the LiCI / LiCI H 2 0 absorption curve, referenced by the reference (9). This curve is located to the right of the curve corresponding to the saturated solution.
- the assembly works as in the previous example, with a storage phase and a destocking phase and gives identical results.
- a compressor can be provided on the tube (3) so as to improve the reaction kinetics or else to place a stirring device inside the reactor (1).
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Sorption Type Refrigeration Machines (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Compression-Type Refrigeration Machines With Reversible Cycles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
La présente invention concerne un procédé thermochimique permettant de réaliser des transferts de calories entre une première source de calories et une deuxième source de calories.The present invention relates to a thermochemical process for carrying out calorie transfers between a first source of calories and a second source of calories.
Le procédé est mis en œuvre selon un cycle intermittent de stockage de chaleur et de déstockage.The process is implemented according to an intermittent cycle of heat storage and destocking.
On a déjà proposé plusieurs types de procédés thermochimiques ayant soit un fonctionnement continu, soit un fonctionnement intermittent et qui peuvent fonctionner pour fournir des calories- chauffage ou en prélever-refroidissement.Several types of thermochemical processes have already been proposed, having either continuous operation or intermittent operation, which can operate to supply calories - heating or to take off - cooling.
Pour obtenir de bons échanges de chaleur entre le milieu réactionnel et la source de calories, on a essayé de réaliser des systèmes pour lesquels le milieu réactionnel comporte une phase liquide, c'est ce qui est. par exemple, réalisé dans les systèmes à absorption gaz liquide. Malheureusement, ces systèmes présentent l'inconvénient d'être divariants, c'est-à-dire que les échanges de chaleur ne se font pas à température constante, ce qui soulève de nombreux problèmes lorsque l'on veut prévoir une gestion efficace de l'énergie. Un tel système est par exemple décrit dans le brevet US-A-4.332.139 relatif à une méthode de stockage et de déstockage de l'énergie thermique.To obtain good heat exchanges between the reaction medium and the source of calories, we have tried to make systems for which the reaction medium comprises a liquid phase, this is what is. for example, produced in liquid gas absorption systems. Unfortunately, these systems have the drawback of being divariant, that is to say that the heat exchanges do not take place at constant temperature, which raises many problems when it is wished to plan an effective management of the 'energy. Such a system is for example described in patent US-A-4,332,139 relating to a method of storage and release of thermal energy.
On peut aussi se reporter à la publication faite par Jaeger F. A. et Hall C. A. « Ammoniated salt heat pump, thermal storage system », International Seminar on Thermo-chemical energy storage, Stockholm, 1980, p.339. Ces auteurs ont étudié l'ammoniacation de NH4CI, NH4SCN et ne se sont intéressés qu'aux domaines de composition présentant une phase liquide unique pour lesquels la variance est deux.We can also refer to the publication by Jaeger FA and Hall CA "Ammoniated salt heat pump, thermal storage system", International Seminar on Thermo-chemical energy storage, Stockholm, 1980, p.339. These authors studied the ammoniacation of NH 4 CI, NH 4 SCN and were only interested in the areas of composition presenting a single liquid phase for which the variance is two.
L'invention prévoit, au contraire, un procédé qui met en oeuvre un système monovariant, c'est-à-dire un système pour lequel la relation entre le logarithme de la pression et I/T est unique et quasi linéaire.The invention provides, on the contrary, a method which implements a monovariant system, that is to say a system for which the relationship between the logarithm of the pressure and I / T is unique and almost linear.
Des essais dans ce sens ont été effectués par R. W. Mar qui, dans son article « Chemical heat pump reactions above the solidus. A feasibility study »‾ Rapport S. A. N. D. 79-8036, indique que des systèmes basés sur la réaction de CaCI2 et de l'eau, au-dessus de la courbe de solidus ne peuvent pas être utilisés pour réaliser des pompes à chaleur thermochimiques, car ils présentent des vitesses de réactions très faibles. Au contraire, les demandeurs se sont aperçus qu'il était possible d'utiliser dans des pompes à chaleur thermochimiques, un procédé mettant en oeuvre un système triphasique monovariant pour lequel l'absorption du gaz par une solution saturée correspond à un seul équilibre, c'est-à-dire que l'on a une seule réaction, alors que Mar a considéré que l'échange thermique se faisait au cours de deux réactions distinctes concernant chacune un composé solide différent.Tests in this direction were carried out by RW Mar who, in his article "Chemical heat pump reactions above the solidus. A feasibility study ” ‾ Report SAND 79-8036, indicates that systems based on the reaction of CaCI 2 and water, above the solidus curve cannot be used to carry out thermochemical heat pumps, because they have very low reaction rates. On the contrary, the applicants have realized that it is possible to use in thermochemical heat pumps, a process implementing a three-phase monovariant system for which the absorption of gas by a saturated solution corresponds to a single equilibrium, c that is to say that one has only one reaction, whereas Mar considered that the heat exchange takes place during two distinct reactions each concerning a different solid compound.
Pour cela, l'invention prévoit un procédé thermochimique permettant de transférer des calories d'une première source de chaleur vers une deuxième source de chaleur par utilisation d'un milieu réactionnel. Ce procédé est caractérisé en ce que l'échange de calories entre une des deux sources et ledit milieu réactionnel a lieu lors d'une réaction entre un gaz et une phase liquide constituée par une solution saturée en solide alors que l'échange de calories entre la deuxième source et le milieu réactionnel se fait lors d'une réaction de changement de phase gaz-liquide dudit gaz ou d'absorption du gaz sur un solide, les deux réactions se faisant en milieu fermé et étant monovariantes.For this, the invention provides a thermochemical process for transferring calories from a first heat source to a second heat source by using a reaction medium. This process is characterized in that the exchange of calories between one of the two sources and the said reaction medium takes place during a reaction between a gas and a liquid phase constituted by a solution saturated with solid whereas the exchange of calories between the second source and the reaction medium takes place during a gas-liquid phase change reaction of said gas or of absorption of the gas on a solid, the two reactions taking place in a closed medium and being monovariant.
Le gaz peut être constitué par de la vapeur d'eau ou de l'ammoniac, ou encore choisi parmi le méthanol, l'éthanol, le butanol, la méthylamine, la diméthylamine, la triméthylamine, l'éthylamine, la diéthylamine, les fluoroalcanes, les fluoroalcanes chlorés, le difluorométhylsilane, le chlorodifluorosilane, le disiloxane, le propane, le butane, l'acétone et l'acétaldéhyde, les fluoroalcanes étant eux-mêmes choisis parmi CC13F, CCl2F2, CHCI2F, CHCIF2, C13C2F3, C12C2F4, C2HCIF4, C2H2CIF3, CH2CIF et C2H2F4.The gas may consist of water vapor or ammonia, or alternatively chosen from methanol, ethanol, butanol, methylamine, dimethylamine, trimethylamine, ethylamine, diethylamine, fluoroalkanes , chlorinated fluoroalkanes, difluoromethylsilane, chlorodifluorosilane, disiloxane, propane, butane, acetone and acetaldehyde, the fluoroalkanes themselves being chosen from CC1 3 F, CCl 2 F 2 , CHCI 2 F, CHCIF 2 , C1 3 C 2 F 3 , C1 2 C 2 F 4 , C 2 HCIF 4 , C 2 H 2 CIF 3 , CH 2 CIF and C 2 H 2 F 4 .
De préférence, la pompe à chaleur comporte une solution saturée, dans le gaz liquéfié, d'un solide choisi parmi CaCI2, KOH, LiCI, LiBr, ZnCl2, ZnBr2 et le gaz, dans ces cas-là, est H20.Preferably, the heat pump comprises a saturated solution, in the liquefied gas, of a solid chosen from CaCI 2 , KOH, LiCI, LiBr, ZnCl 2 , ZnBr 2 and the gas, in these cases, is H 2 0.
Les avantages et les caractéristiques du procédé, selon l'invention, apparaîtront plus clairement à la lecture de la description suivante faite d'une manière non limitative en référence aux dessins dans lequels :
- la figure 1 représente une pompe permettant la mise en ceuvre du procédé selon l'invention pendant la phase de stockage,
- la figure 2 représente la même pompe pendant la phase de déstockage,
- la figure 3 est un diagramme de Clapeyron,
- la figure 4 est une installation de chauffage pour la mise en oeuvre du procédé selon l'invention.
- FIG. 1 represents a pump allowing the implementation of the method according to the invention during the storage phase,
- FIG. 2 represents the same pump during the destocking phase,
- FIG. 3 is a Clapeyron diagram,
- Figure 4 is a heating installation for the implementation of the method according to the invention.
On a représenté sur la figure 1, d'une manière schématique, une pompe à chaleur pendant la phase de stockage de l'énergie, sur la figure 2 la même pompe pendant la phase de déstockage et sur la figure 3 le diagramme de Clapeyron correspondant.There is shown in Figure 1, schematically, a heat pump during the energy storage phase, in Figure 2 the same pump during the destocking phase and in Figure 3 the corresponding Clapeyron diagram .
La pompe à chaleur comporte un réacteur (1) et un réacteur (2), reliés entre eux par la conduite (3). Chaque réacteur est muni d'un échangeur de chaleur (4) à (5) permettant l'échange de calories entre le milieu réactionnel et les sources extérieures de calories.The heat pump comprises a reactor (1) and a reactor (2), interconnected by the pipe (3). Each reactor is provided with a heat exchanger (4) to (5) allowing the exchange of calories between the reaction medium and the external sources of calories.
Le réacteur (1) contient le liquide en équilibre avec sa phase vapeur, le réacteur (2) contient la solution saturée de solide.The reactor (1) contains the liquid in equilibrium with its vapor phase, the reactor (2) contains the saturated solid solution.
Dans cet exemple, les réactifs et les réactions mises en jeu sont les suivantes :
- -
réacteur 1. Le liquide est de l'eau, de sorte que l'on a la réaction
- -
réacteur 2. Le solide est du chlorure de lithium monohydraté. Il est en solution dans l'eau.
- -
reactor 1. The liquid is water, so we have the reaction - -
reactor 2. The solid is lithium chloride monohydrate. It is in solution in water.
Lors de la phase de déstockage, le gaz provenant du réacteur (1) se condense au niveau de la solution saturée et libère sa chaleur latente de condensation ΔH tout en diluant la solution. La chaleur différentielle de dilution de la solution saturée est ΔHD, c'est une réaction exothermique. Parallèlement, du solide en excès se dissout pour maintenir la concentration à la saturation, avec une chaleur ΔHS de dissolution du sel dans la solution saturée.During the destocking phase, the gas coming from the reactor (1) condenses at the saturated solution and releases its latent heat of condensation ΔH while diluting the solution. The differential heat of dilution of the saturated solution is ΔH D , it is an exothermic reaction. At the same time, excess solid dissolves to maintain the concentration at saturation, with a heat ΔH S of dissolution of the salt in the saturated solution.
Lors de phase de stockage, le gaz s'évapore à partir de la solution contenue dans le réacteur (2) pour aller dans le réacteur (1) qui joue alors le rôle de condenseur. La solution se concentre et le solide doit cristalliser. Les enthalpies mises en jeu sont les mêmes que précédemment, en signe opposé.During the storage phase, the gas evaporates from the solution contained in the reactor (2) to go to the reactor (1) which then plays the role of condenser. The solution is concentrated and the solid must crystallize. The enthalpies involved are the same as before, in opposite sign.
En principe, on néglige les enthalpies ΔHD et ΔHS qui sont d'un ordre de grandeur très inférieur à ΔH1 et généralement de signe opposé.In principle, we neglect the enthalpies ΔH D and ΔH S which are of an order of magnitude much less than ΔH 1 and generally of opposite sign.
Si on se reporte à la figure 3, qui est un diagramme de Clapeyron des réactions mises en jeu dans lequel la courbe (7) correspond à l'équilibre liquide-vapeur et la courbe (8) correspond à l'équilibre solide + gaz - solution saturée, on voit que si on fournit une quantité de calories H1 à une température Th, on récupère H2 à une température Tu qui est inférieure à Th.If we refer to Figure 3, which is a Clapeyron diagram of the reactions involved in which the curve (7) corresponds to the liquid-vapor equilibrium and the curve (8) corresponds to the solid + gas equilibrium - saturated solution, we see that if we supply an amount of calories H 1 at a temperature Th, we recover H 2 at a temperature Tu which is lower than Th.
De même, pendant la phase de déstockage, si on fournit OHZ à la température Tb, on va récupérer ΔH1 à la température T'u, qui est supérieure à Tb.Similarly, during the destocking phase, if OH Z is supplied at the temperature Tb, we will recover ΔH 1 at the temperature T'u, which is higher than Tb.
Dans un but de simplification, on considérera que Tu et Tu sont identiques.For the sake of simplification, we will consider that You and You are identical.
On comprend donc que pendant les deux étapes du cycle, stockage et déstockage, de la chaleur est délivrée à la température Tu qui correspond à la température utile pour le chauffage.It is therefore understood that during the two stages of the cycle, storage and destocking, heat is delivered at the temperature Tu which corresponds to the temperature useful for heating.
L'intérêt de ce système réside dans le fait qu'il est monovariant dans les deux réactions et que, alors, la température Tu est constante. De plus, les échanges de calories sont facilités par la présence d'une phase liquide dans chaque réacteur.The interest of this system lies in the fact that it is monovariant in the two reactions and that, then, the temperature Tu is constant. In addition, the exchange of calories is facilitated by the presence of a liquid phase in each reactor.
On représente sur la figure 4 une installation de chauffage permettant la mise en oeuvre du procédé selon l'invention, et dans laquelle la période de chauffage correspond uniquement à la phase de déstockage. Il est bien entendu que, comme il a été mentionné plus haut, l'installation pourrait aussi être utilisée en chauffage pendant la période de stockage.FIG. 4 shows a heating installation allowing the implementation of the method according to the invention, and in which the heating period corresponds only to the destocking phase. It is understood that, as mentioned above, the installation could also be used for heating during the storage period.
La partie A de la figure 4 représente la phase de stockage alors que la partie B représente la phase de déstockage.Part A of Figure 4 represents the storage phase while part B represents the destocking phase.
La pompe à chaleur est symbolisée par ses deux réacteurs (1) et (2) et par la conduite de gaz (3).The heat pump is symbolized by its two reactors (1) and (2) and by the gas line (3).
Pendant la phase de stockage, le réacteur (1) est relié à une source chaude constituée, dans l'installation représentée, par un capteur solaire (12). Les calories cédées dans le réacteur (2) lors de la condensation du gaz sont rejetées dans l'atmosphère, mais elles pourraient aussi bien être utilisées pour le chauffage ou encore être stockées.During the storage phase, the reactor (1) is connected to a hot source constituted, in the installation shown, by a solar collector (12). The calories given up in the reactor (2) during the condensation of the gas are released into the atmosphere, but they could as well be used for heating or even be stored.
Pendant la phase de déstockage, le réacteur (2) est alimenté en calories par une source froide, symbolisée par la flèche (11). Les calories sont récupérées dans le réacteur (1) et utilisées pour le chauffage.During the destocking phase, the reactor (2) is supplied with calories by a cold source, symbolized by the arrow (11). The calories are recovered in the reactor (1) and used for heating.
Dans cet exemple de réalisation, les résultats énergétiques suivants ont été obtenus.In this exemplary embodiment, the following energy results have been obtained.
Le système triphasique utilisé était la solution saturée de chlorure de lithium, la vapeur d'eau et le chlorure de lithium monohydraté. Pour ce système, le domaine d'existence de l'hydrate sous forme solide avec la solution saturée est compris entre 19 et 95 °C. La capacité de stockage massique, mesurée entre une opération de stockage à 90 °C et une opération de déstockage à 45 °C, était de 146 Wh/kg. Enfin, on a obtenu, pendant le déstockage, une remontée de température d'environ 41 °C (AT).The three-phase system used was the saturated solution of lithium chloride, water vapor and lithium chloride monohydrate. For this system, the range of existence of the hydrate in solid form with the saturated solution is between 19 and 95 ° C. The mass storage capacity, measured between a storage operation at 90 ° C and a destocking operation at 45 ° C, was 146 Wh / kg. Finally, during the destocking, a temperature rise of approximately 41 ° C. (AT) was obtained.
Le tableau ci-après donne les résultats obtenus avec d'autres sels.
Pour cela, on a pris le même dispositif que précédemment. Dans le premier réacteur, on a placé la solution liquide saturée de solide LiCI, H20.For this, we took the same device as before. In the first reactor, the saturated liquid solution of solid LiCI, H 2 0 was placed.
Dans l'autre réacteur, on a placé le solide constitué par du chlorure de lithium anhydre qui est susceptible d'absorber de t'eau vapeur pour donner LiCI H20 qui est solide.In the other reactor, the solid consisting of anhydrous lithium chloride which is capable of absorbing steam water was placed to give LiCl H 2 O which is solid.
La règle des phases montre que le système est monovariant.The phase rule shows that the system is monovariant.
On a représenté sur la figure 3 la courbe d'absorption LiCI/LiCI H20, référencée par le repère (9). Cette courbe se situe à droite de la courbe correspondant à la solution saturée. L'ensemble fonctionne comme dans l'exemple précédent, avec une phase de stockage et une phase de déstockage et donne des résultats identiques.FIG. 3 shows the LiCI / LiCI H 2 0 absorption curve, referenced by the reference (9). This curve is located to the right of the curve corresponding to the saturated solution. The assembly works as in the previous example, with a storage phase and a destocking phase and gives identical results.
En variante, on peut prévoir un compresseur sur la tubulure (3) de façon à améliorer la cinétique de réaction ou encore de placer un dispositif d'agitation à l'intérieur du réacteur (1).As a variant, a compressor can be provided on the tube (3) so as to improve the reaction kinetics or else to place a stirring device inside the reactor (1).
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT84401360T ATE29578T1 (en) | 1983-07-01 | 1984-06-26 | HEAT TRANSFER METHOD USING A MONOVARIAN THREE-PHASE REACTION. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8310955A FR2548340B1 (en) | 1983-07-01 | 1983-07-01 | THREE-PHASE HEAT PUMP |
| FR8310955 | 1983-07-01 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0130908A1 EP0130908A1 (en) | 1985-01-09 |
| EP0130908B1 true EP0130908B1 (en) | 1987-09-09 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP84401360A Expired EP0130908B1 (en) | 1983-07-01 | 1984-06-26 | Heat transfer process with a three-phase monovariant reaction |
Country Status (7)
| Country | Link |
|---|---|
| US (2) | US4682476A (en) |
| EP (1) | EP0130908B1 (en) |
| JP (1) | JPS6026261A (en) |
| AT (1) | ATE29578T1 (en) |
| CA (1) | CA1236312A (en) |
| DE (1) | DE3466059D1 (en) |
| FR (1) | FR2548340B1 (en) |
Families Citing this family (27)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2548340B1 (en) * | 1983-07-01 | 1986-03-21 | Elf Aquitaine | THREE-PHASE HEAT PUMP |
| FR2582790B1 (en) * | 1985-06-04 | 1987-07-24 | Elf Aquitaine | THERMOCHEMICAL PROCESS AND DEVICE FOR STORING AND CLEARING HEAT |
| ES2036677T3 (en) * | 1987-04-14 | 1993-06-01 | Uwe Rockenfeller | CHEMICAL ENERGY ACCUMULATION SYSTEM. |
| US4759191A (en) * | 1987-07-07 | 1988-07-26 | Liquid Co2 Engineering, Inc. | Miniaturized cooling device and method of use |
| US4901535A (en) * | 1987-07-07 | 1990-02-20 | Sabin Cullen M | Temperature changing device improved evaporation characteristics |
| US4949549A (en) * | 1987-07-07 | 1990-08-21 | International Thermal Packaging, Inc. | Cooling device with improved waste-heat handling capability |
| US4974419A (en) * | 1988-03-17 | 1990-12-04 | Liquid Co2 Engineering Inc. | Apparatus and method for simultaneously heating and cooling separate zones |
| US4993239A (en) * | 1987-07-07 | 1991-02-19 | International Thermal Packaging, Inc. | Cooling device with improved waste-heat handling capability |
| IN171470B (en) * | 1987-07-07 | 1992-10-24 | Int Thermal Packaging Inc | |
| US4744224A (en) * | 1987-07-27 | 1988-05-17 | Erickson Donald C | Intermittent solar ammonia absorption cycle refrigerator |
| FR2629575A1 (en) * | 1988-03-30 | 1989-10-06 | Elf Aquitaine | CHEMICAL PIPE, METHOD FOR REGENERATING SUCH A PIPE AND USE OF THE SAME |
| DE3837880A1 (en) * | 1988-11-08 | 1990-05-10 | Zeolith Tech | REFRIGERATED TANK FOR A SORPTION APPARATUS |
| US5197302A (en) * | 1989-01-05 | 1993-03-30 | International Thermal Packaging, Inc. | Vacuum insulated sorbent-driven refrigeration device |
| US5048301A (en) * | 1989-01-05 | 1991-09-17 | International Thermal Packaging | Vacuum insulated sorbent driven refrigeration device |
| US5018368A (en) * | 1989-10-12 | 1991-05-28 | International Thermal Packaging, Inc. | Multi-staged desiccant refrigeration device |
| US5490398A (en) * | 1993-03-15 | 1996-02-13 | Airex Research And Development, Inc. | High efficiency absorption cooling and heating apparatus and method |
| FR2723438B1 (en) | 1994-08-02 | 1996-09-20 | Lorraine Carbone | IMPROVED POWER CHEMICAL HEAT PUMP REACTOR |
| AUPM835894A0 (en) * | 1994-09-22 | 1994-10-13 | Thermal Energy Accumulator Products Pty Ltd | A temperature control system for liquids |
| FR2748093B1 (en) * | 1996-04-25 | 1998-06-12 | Elf Aquitaine | THERMOCHEMICAL DEVICE TO PRODUCE COLD AND / OR HEAT |
| SE515688C2 (en) * | 1998-12-18 | 2001-09-24 | Suncool Ab | Chemical heat pump and process for cooling and / or heating |
| CN1322286C (en) * | 2002-12-13 | 2007-06-20 | 东京电力株式会社 | Heat pump using gas hydrate, and heat utilizing apparatus |
| SE527721C2 (en) * | 2003-12-08 | 2006-05-23 | Climatewell Ab | Chemical heat pump operating according to the hybrid principle |
| FR2878940A1 (en) * | 2004-12-06 | 2006-06-09 | Guy Karsenti | AIR CONDITIONING DEVICE OF THE ABSORPTION HEAT PUMP TYPE, ESPECIALLY FOR LOW VOLUME SPEAKERS, AND SPEAKER HAVING THE SAME |
| CN101737996B (en) * | 2008-11-17 | 2012-02-01 | 苏庆泉 | Heat pump circulating system and cooling/heating united supply method |
| EP2759679A1 (en) * | 2013-01-23 | 2014-07-30 | Siemens Aktiengesellschaft | Thermal storage device for the utilisation of low temperature heat |
| US20210325092A1 (en) * | 2018-02-06 | 2021-10-21 | John Saavedra | Heat Transfer Device |
| CN113025281A (en) * | 2021-03-18 | 2021-06-25 | 天津大学 | Refrigerant containing organic silicon |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE380828A (en) * | ||||
| US2144441A (en) * | 1932-10-27 | 1939-01-17 | Schlumbohm Peter | Method of conditioning an absorption refrigerating system |
| US2138686A (en) * | 1933-02-28 | 1938-11-29 | Altenkirch Edmund | Intermittent absorption refrigerating apparatus |
| US2182453A (en) * | 1936-01-18 | 1939-12-05 | William H Sellew | Heat transfer process and apparatus |
| FR2172754A1 (en) * | 1972-02-21 | 1973-10-05 | Greiner Leonard | Heating and cooling apparatus with absorption chemical - and fluid to be absorbed |
| US3828566A (en) * | 1973-02-05 | 1974-08-13 | C Wetzel | Dry adsorption refrigeration system |
| US4005584A (en) * | 1975-04-10 | 1977-02-01 | Allied Chemical Corporation | Composition, method and apparatus for absorption heating |
| US4319626A (en) * | 1976-07-06 | 1982-03-16 | Martin Marietta Corp. | Chemical storage of energy |
| SE7706357L (en) * | 1977-05-31 | 1978-12-01 | Brunberg Ernst Ake | KIT FOR COOLING A SPACE AND DEVICE FOR PERFORMING THE KIT |
| JPS5589379A (en) * | 1978-12-27 | 1980-07-05 | Agency Of Ind Science & Technol | Energy storing medium |
| DE2923480A1 (en) * | 1979-06-09 | 1980-12-18 | Erno Raumfahrttechnik Gmbh | METHOD FOR STORAGE, IN PARTICULAR, LOW TEMPERATURE HEAT |
| US4532778A (en) * | 1979-11-16 | 1985-08-06 | Rocket Research Company | Chemical heat pump and chemical energy storage system |
| US4309980A (en) * | 1980-03-07 | 1982-01-12 | Thermal Energy Storage, Inc. | Closed vaporization heat transfer system |
| US4411384A (en) * | 1980-08-29 | 1983-10-25 | The United States Of America As Represented By The Secretary Of The Navy | Heat driven heat pump using paired ammoniated salts |
| US4386501A (en) * | 1981-07-29 | 1983-06-07 | Martin Marietta Corporation | Heat pump using liquid ammoniated ammonium chloride, and thermal storage system |
| FR2548340B1 (en) * | 1983-07-01 | 1986-03-21 | Elf Aquitaine | THREE-PHASE HEAT PUMP |
-
1983
- 1983-07-01 FR FR8310955A patent/FR2548340B1/en not_active Expired
-
1984
- 1984-06-25 US US06/623,964 patent/US4682476A/en not_active Expired - Fee Related
- 1984-06-26 DE DE8484401360T patent/DE3466059D1/en not_active Expired
- 1984-06-26 EP EP84401360A patent/EP0130908B1/en not_active Expired
- 1984-06-26 AT AT84401360T patent/ATE29578T1/en active
- 1984-06-29 CA CA000457892A patent/CA1236312A/en not_active Expired
- 1984-06-29 JP JP59133450A patent/JPS6026261A/en active Pending
-
1987
- 1987-07-28 US US07/078,591 patent/US4873842A/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| FR2548340A1 (en) | 1985-01-04 |
| JPS6026261A (en) | 1985-02-09 |
| US4873842A (en) | 1989-10-17 |
| US4682476A (en) | 1987-07-28 |
| DE3466059D1 (en) | 1987-10-15 |
| EP0130908A1 (en) | 1985-01-09 |
| CA1236312A (en) | 1988-05-10 |
| ATE29578T1 (en) | 1987-09-15 |
| FR2548340B1 (en) | 1986-03-21 |
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