DEVICE AND METHOD FOR THE CONTINUOUS THERMOCHEMICAL PRODUCTION OF COLD

Abstract

A system and a thermochemical method for the production of cold, that uses a reactive device having a reactor or a chamber for storing a reactive product that can absorb a gas. The reactive product and the gas are such that, when they are exposed to one another, they undergo a reaction resulting in absorption of the gas by the reactive product and, conversely, they undergo a reaction involving the desorption of the gas absorbed by the reactive product as a result of heat applied to the reactive product when it absorbed the gas. The system has two substantially identical reactive devices wherein when the reactor of one reactive device is operating in the absorption cycle, the reactor of the other is operating in the desorption cycle. The system has a mechanism for determining the progress rate of the thermochemical reaction.

Description

The present invention concerns a device and method for the thermochemical production of cold, and more precisely a device and method capable of producing cold in a controlled and quasi-continuous manner.

Systems are known that exploit the properties of a reversible and strongly exothermic thermochemical reaction during which a reactive product, such as certain salts and particularly calcium chloride or barium chloride, absorbs an appropriate gas such as ammonia in particular. The reversible nature of this reaction makes it possible, once the reaction is ended, to recover the initial gas by heating the salts so that the cycle can be repeated.

This property has been exploited in cold production systems in which the thermochemical system is placed in controlled communication with a reservoir containing the gas in liquid phase. When the two enclosures are placed in communication, the liquid gas contained in the reservoir is vaporized; this absorbs a certain amount of heat, cooling the reservoir, and this gas is absorbed by the reactive product thus generating the aforementioned chemical reaction, so that the reactor is the source of a release of heat. Once the reaction is ended, if the product contained in the reactor is heated, the gas absorbed in the reactive product is released and is then condensed in the reservoir.

It is understandable that devices of this type do not function continuously, because during the regeneration phase of the reagent, they are not of course in a cold producing state.

Proposed in patent applications WO 2009/153245, WO 2005/108880, and WO 97/49958 are heat pumps functioning with adsorption reactive devices, that is, without chemical reaction, which are coupled together in order to operate in opposite phases, so that when one of the reactors of one reactive device is operating in adsorption, the reactor of the other reactive device is operating in desorption. However, such systems are very different from the system according to the invention, which implements a true thermochemical reaction and which is far more efficient.

A purpose of the present invention is therefore to propose a device and a method for the thermochemical production of cold that is totally controlled and is capable of functioning continuously or quasi-continuously.

An object of the present invention is therefore a system for the thermochemical production of cold, of the type implementing at least one reactive device comprising a reactor, or enclosure for storage of a reactive product capable of absorbing a gas, the reactive product and the gas being such that, when they are placed in the presence of each other a reaction occurs resulting in the absorption of the gas by the reactive product, and in the reverse, a desorption reaction occurs of the gas absorbed by the reactive product under the effect of heat applied to the reactive product when said reactive product has absorbed the gas, said system comprising two substantially identical reactive devices disposed such as to have opposing operating cycles, so that when the reactor of one of them is operating in absorption, the reactor of the other one is operating in desorption, characterized in that it comprises means for determining the rate of progress of said thermochemical reaction.

Such a measurement is particularly advantageous in that knowing the rate of progress of the thermochemical reaction makes it possible to know the energy reserve remaining in the thermochemical system at any moment, and particularly before the end of each operating phase.

Preferably a condenser and an evaporator will be disposed between each reactor and each reservoir. According to the invention the condenser and/or the evaporator will be common to both reactors.

In order to control the rate of progress of the reaction, (i.e. the ratio of the quantity of gas absorbed in the reactor to the total quantity of gas that the reactor can absorb), the reservoirs can be provided with means suitable for measuring the quantity of liquefied gas present in each of them, particularly by measuring the quantity of gas that enters and/or leaves each of them or by measuring, by means of level sensors, the level of liquefied gas in each of them.

The system according to the invention will further comprise connection means, particularly at the end of each cycle, suitable for isolating the two reactors from the other elements of the system and to connect them to each other, so as to ensure a transfer of the gas from one reactor to the other reactor. These connection means will preferably be composed of solenoid valves controlled by programmable electronic means, particularly a microcontroller.

An object of the present invention is also a thermochemical method of producing cold of the type implementing at least one reactive device composed of a reactor containing a reactive product capable of absorbing a gas contained in the reservoir capable of being placed in communication with a condenser and an evaporator, said reactive product and the gas being such that, when they are in the presence of each other a thermochemical reaction occurs resulting in the absorption of the gas by the reactive product, and in the reverse, a desorption reaction occurs of the gas absorbed by the reactive product under the effect of heat applied to said reactive product when said reactive product has absorbed the gas, wherein two reactive devices are used that are made to operate in opposite phase so that, when the reactor of one of them is operating in absorption, the reactor of the other one is operating in desorption, characterized in that it comprises means of controlling the rate of progress of said thermochemical reaction.

The method according to the invention may advantageously comprise a step during which the quantity of liquefied gas present in the reservoirs is measured, particularly by measuring the quantity of liquefied gas that enters and/or leaves said reservoirs.

Said method may also comprise a step consisting of measuring the levels of the liquefied gas contained in the reservoirs and stopping the process when the level of liquid in the reservoir associated with the reactor during absorption reaches a lower limit and the level of liquid in the reservoir associated with the reactor during desorption reaches an upper limit.

According to the invention, the lower limit of the level sensor of one reservoir will be adjusted so that, when the liquefied gas reaches that level, the rate of progress of the reaction of the associated reactor is at its desired maximum rate of progress.

Moreover, said upper limit of the level sensor will be adjusted so that when the liquefied gas reaches that level, the rate of progress of the reaction of the associated reactor is at its desired minimum rate of progress.

According to the invention, if one of the reservoirs reaches its threshold level more quickly than the other, priority will be given to the one that has reached the lower level. More specifically, when the first threshold level reached by one reservoir is a low level, priority will be given to the reactor associated with that reservoir, and it will be isolated from the evaporator while waiting for the other reservoir to reach its upper level in order to interrupt the process by closing the valve communicating said reservoir with the condenser.

When the first threshold level reached by one reservoir is an upper level, the process will be continued until the other reservoir has reached the lower level.

Once the process has stopped, the communication of the two reactors will be controlled and maintained until the pressures therein are equalized.

Described below is a non-limiting example of one embodiment of the present invention, with reference to the appended drawing in which:

FIG. 1 is a schematic representation of a system according to the invention during the process wherein one reactor operates in absorption, the other reactor operates in desorption,

FIG. 2 is a schematic representation of the system represented in FIG. 1 after interruption of the process and in a step of placing the two reactors in communication,

FIG. 3 is a schematic representation of the system represented in FIGS. 1 and 2 in a step of placing the two reactors under operating pressure,

FIG. 4 is a graph representing the variation of the pressure in each of the two reactors during one operating cycle.

The thermochemical system that is represented schematically in FIGS. 1 to 3 essentially comprises two reactors 1a and 1b that contain a reactive product, for example in particular barium chloride or calcium chloride, and two reservoirs 3a and 3b that contain a specific liquid gas capable of reacting with the reactive product in a reaction as explained hereinafter, and which in particular can be the ammonia.

In a known manner, the reactive product and the specific gas are such that the reactive product is capable, by an exothermic thermochemical reaction, of absorbing the gas and then of restoring it by reverse thermochemical reaction, when the reactive product is heated.

The respective intakes 5a and 5b of the reactors 1a and 1b are connected to a first intake of two solenoid valves disposed in parallel, i.e. one solenoid valve 7a and one solenoid valve 7′a for the reactor 1a and one solenoid valve 7b and one solenoid valve 7′b for the reactor 1b. Moreover, a solenoid valve 11 connects the two intakes 5a and 5b.

The second intake of the solenoid valve 7a and the second intake of the solenoid valve 7b are connected to each other and to an evaporator 13, while the second intake of the solenoid valve 7′a and the second intake of the solenoid valve 7′b are connected to each other and to the intake 15a of a condenser 15. The outlet 15b of said condenser is connected to a first intake of two solenoid valves in parallel, respectively 17a and 17b, and the second intake of each of them is respectively connected to an intake of two respective reservoirs 3a and 3b. The outlet of each of the reservoirs 3a and 3b is connected, via the respective solenoid valves 21a and 21b, to the evaporator 13.

The operation of the system and particularly the opening and closing of the solenoid valves is controlled by control means, particularly a microcontroller not shown in the drawing.

The operation of the system is described in the following example in which the reactor 1a is considered to be in desorption mode (regeneration) and the reactor 1b in absorption mode (cold production). Such a process is represented in FIG. 1, in which the solenoid valves, which are placed in the closed position by the microcontroller, are represented in black.

In a known manner, to regenerate the reactive product contained in the reactor 1a, said reactor is heated for example by means of an electrical resistance, which results in the release of the gas absorbed by the reactive product, i.e. the ammonia, which passes through the solenoid valve 7′a, which is in the open position, in order to be condensed in the condenser 15, and through the solenoid valve 17a, which is in the open position, reaching the reservoir 3a in which the level increases as represented by the arrow F1.

At the same time the reactor 1b is in absorption mode (cold production) and, to that end, is connected to the evaporator 13 through the solenoid valve 7b, which is in the open position, and the reservoir 3b is connected to the evaporator through the solenoid valve 21b which is in the open position. Thus the liquid level in the reservoir 3b decreases as represented by the arrow F2.

It can be seen that the efficiency of the thermochemical system according to the invention depends on the rate of progress of the reaction X_Max at the end of absorption and of the rate of progress of the reaction X_Min at the end of desorption. It can also be seen that these rates of progress of the reaction depend on the application concerned. According to the invention, means are implemented that make it possible to control [sic] It is therefore important to be able to measure the rates of progress of the reaction X of each of the reactors.

Thus, in a first variant of embodiment these two rates of progress of the reaction are controlled by controlling the levels of liquefied gas inside the reservoirs 3a and 3b. To that end, said reservoirs are provided with liquid level measuring probes, respectively 23a and 23b, which make it possible to define for each of the reservoirs 3a, 3b an upper-level threshold N_h and a lower-level threshold N_b.

Thus, in the present embodiment, and during the phase represented in FIG. 1 in which the reactor 1b is in absorption, the sensor 23b of the reservoir 3b is adjusted so that when the level of the liquefied gas reaches its lower level N_b, the rate of progress of the reaction of the reactor 1b is equal to the maximum desired rate of progress of the reaction, i.e. X_Max.

Moreover, at the same time the reactor 1a is in desorption and the reservoir 3a is filled with liquefied gas, and the sensor 23a thereof is adjusted so that when the level of liquefied gas reaches its upper level N_h, the rate of progress of the reaction of the reactor 1a is equal to the minimum desired rate of progress of the reaction X_Min.

Under these conditions and according to the invention the operating phase is stopped when the upper threshold N_h and lower threshold N_b values are reached.

More specifically, if one of the reservoirs reaches a threshold value first (which of course occurs in most cases), the indication of the lower level is first taken into account.

Thus, if it is the reservoir that is associated with the reactor that is in absorption (i.e. the reservoir 3b in this example) that first reaches the threshold level, in this instance the lower level N_b, then the evaporator 13 is isolated by closing the solenoid valve 21b while waiting for the desorption reaction of the other reactor, here the reactor 1a, to end, which is determined when the level of the reservoir associated with it, here the reservoir 3a, reaches its threshold level, i.e. its upper level N_h. The solenoid valve 17a is then closed, and this operating phase is then ended.

However, if it is the reactor that is in desorption, here the reactor 1a, the associated reservoir of which, here the reservoir 3a, first reaches its threshold level, i.e. the upper level N_h, the desorption is allowed to continue until the other reservoir, here the reservoir 3b, associated with the reactor 1b, reaches its threshold level, here the lower threshold N_b. The solenoid valves 21b and 17a are then closed. This operating phase is then ended.

In a second variant of embodiment of the invention, the rate of progress of the reaction of each of the reactors 1a and 1b is controlled by means capable of measuring the quantity of liquefied gas that enters and/or leaves the reservoirs 3a and 3b.

In another interesting embodiment of the present invention, represented in FIGS. 2 and 4, when the aforementioned operating phase has ended, the reactors 1a and 1b of the evaporator 13 and the condenser 15 are isolated by closing the valves 7′a and 7b, then the two reactors 1a and 1b are placed in communication at the time t1 by opening the solenoid valve 11.

The two reactors 1a and 1b are left in communication until they reach a common pressure P_c at the time t2; their connection is then interrupted by closing the solenoid valve 11, as represented in FIGS. 3 and 4. To that end, each of the reactors 1a and 1b includes a pressure sensor respectively 27a, 27b, or preferably means of differential measurement of the pressures in the two reactors 1a and 1b.

As represented in FIG. 4, when the pressure in the reactor 1a reaches the low operating pressure Pb at the time t3, the operation of the system is reversed by opening the solenoid valves 7a, 7′b and 17b, so the operating phase of the system is reversed from the preceding one and now the reactor 1a operates in absorption mode (cold production) and the reactor 1b operates in desorption mode (regeneration).

Placing these two reactors in communication at the end of each of the active phases, by transferring the gas from the high-pressure reactor into the low-pressure reactor, makes it possible to shorten the time needed for the intermediate phases of increasing and decreasing pressure of these reactors.

The time lost between two half-cycles of cold production is therefore decreased and at the same time the continuous operation of the system is improved.

Claims

1. Thermochemical system for the production of cold, of the type implementing at least one reactive device comprising a reactor, containing a reactive product and a reservoir, said reactive product and said gas being such that, when they are placed in the presence of each other a reaction occurs resulting in the absorption of the gas by the reactive product, and in the reverse, a desorption reaction occurs of the gas absorbed by the reactive product under the effect of heat applied to the reactive product when said reactive product has absorbed the gas, said system comprising two reactive devices disposed such that they operate in opposite phases, so that when the reactor of one of them is operating in absorption, the reactor of the other one is operating in desorption, characterized in that it comprises means for determining the rate of progress of said thermochemical reaction.

2. Thermochemical system for the production of cold according to claim 1, characterized in that the reservoirs are provided with means capable of measuring the quantity of liquefied gas present in each of them.

3. Thermochemical system for the production of cold according to claim 2, characterized in that the reservoirs are provided with a level sensor, particularly of the capacitive type.

4. Thermochemical system for the production of cold according to claim 2, characterized in that the reservoirs are provided with means capable of measuring the quantity of liquefied gas that enters and/or leaves each of them.

5. Thermochemical system for the production of cold according to claim 1, characterized in that the reactors are provided with a pressure sensor.

6. Thermochemical system for the production of cold according to claim 1, characterized in that it comprises connection means capable of isolating the two reactors from the other elements of the system and for connecting them to each other, so as to ensure a transfer of the gas from one reactor to the other reactor.

7. Thermochemical method for the production of cold of the type implementing at least one reactive device composed of a reactor, containing a reactive product capable of absorbing a gas contained in a reservoir capable of being placed in communication with a condenser and an evaporator, said reactive product and the gas being such that, when they are placed in the presence of each other a thermochemical reaction occurs resulting in the absorption of the gas by the reactive product, and in the reverse, a desorption reaction occurs of the gas absorbed by the reactive product under the effect of heat applied to said reactive product when said reactive product has absorbed the gas, wherein two reactive devices are used that are made to operate in opposite phase so that, when the reactor of one of them is operating in absorption, the reactor of the other one is operating in desorption, characterized in that the rate of progress of said thermochemical reaction is determined during the process.

8. Thermochemical method for the production of cold according to claim 7, characterized in that the quantity of liquefied gas in the reservoirs is measured.

9. Thermochemical method for the production of cold according to claim 8, characterized in that it comprises a step comprising measuring the quantity of liquefied gas that enters and/or leaves the reservoirs.

10. Thermochemical method for the production of cold according to claim 8, characterized in that it comprises a step comprising measuring the levels of liquefied gas contained in the reservoirs.

11. Thermochemical method for the production of cold according to claim 10, characterized in that the process is stopped when the level of liquid in the reservoir associated with the reactor in the course of absorption reaches a lower limit and the level of liquid in the reservoir associated with the reactor in the course of desorption reaches an upper limit.

12. Thermochemical method for the production of cold according to claim 11, characterized in that the lower limit of the level sensor of one reservoir is adjusted so that, when the liquefied gas reaches that level, the rate of progress of the reaction of the associated reactor is at its desired maximum rate of progress.

13. Thermochemical method for the production of cold according to claim 11, characterized in that said upper limit of the level sensor is adjusted so that when the liquefied gas reaches that level, the rate of progress of the reaction of the associated reactor is at its desired minimum rate of progress.

14. Thermochemical method for the production of cold according to claim 11, characterized in that when the first threshold level reached in a reservoir is a lower level, communication of said reservoir with the evaporator is closed while waiting for the upper level to be reached in the other reservoir in order to stop the operating step by closing the communication valve of said reservoir with the condenser.

15. Thermochemical method for the production of cold according to claim 11, characterized in that when the first threshold level reached in a reservoir is an upper level the operating step is stopped by closing the communication of the reservoir with the evaporator and the communication of the other reservoir with the condenser only after the lower level is reached in the other reservoir.

16. Thermochemical method for the production of cold according to claim 15, characterized in that once said step is stopped, the communication of the two reactors is ordered.

17. Thermochemical method for the production of cold according to claim 16, characterized in that the two reactors are maintained in communication until the pressures therein are equalized.

18. Thermochemical method for the production of cold according to claim 17, characterized in that once the pressures are equalized in the two reactors, their communication is interrupted until the pressure in the reactor in regeneration reaches a floor value.