FIELD OF THE INVENTION
[0002] This application relates to systems and methods for controller
refrigeration cycles. More particularly, this application relates to cooling systems having
electronic controllers that control the recouperation time between reactor systems.
BACKGROUND
[0003] In solid-vapor sorption reaction systems, a gaseous reactant is
alternately absorbed and desorbed on a solid sorbent in one or more reaction chambers in
a sorber or reactor. Where multiple reactors are used the system can operate in
substantially opposing phases, or half-cycles, with one reactor or bank of reactors
desorbing the gaseous reactant from the solid sorbent while the other reactor or bank of
reactors is absorbing the gaseous reactant on the solid sorbent.
[0004] Once the reactant is desorbed from the solid sorbent it can be directed
to one or more condensers. After condensation, the condensate is then directed to one or
more evaporators where it is vaporized back into a gas. During this process, heat may be
rejected from the condenser and cooling may be recovered from the evaporator.
[0005] In other systems, the reactors are used instead of condensers and
evaporators for recovering energy from the refrigerant. Desorption is carried out by
heating the solid sorbent on which the gaseous reactant has been absorbed. Electric,
steam, or gas-driven heaters are typically used for heating the solid sorbent. A heat
transfer fluid can then be directed through a reactor heat exchanger to which the sorbent
is thermally exposed. To initiate absorption, a solid sorbent, from which the gaseous
reactant or refrigerant has been desorbed, is cooled to a suitable temperature whereby it
draws the gaseous refrigerant from the evaporator. The reactors may also be provided
with heat exchangers and piping for directing heat transfer fluid between the reactors so
that heat released from an absorbing reactor is directed to a desorbing reactor to provide
heating to carry out desorption. Such systems are described in, for example U.S. Patent
Nos. 5,079,928, 5,263,330, 5,477,706, 5,598,721, 5,628,205, and 6,477,856, all of which
disclosures are incorporated herein by reference in their entirety.
[0006] During a reaction cycle, a first (absorbing) reactor is at a lower
temperature than a second (desorbing) reactor. This means that the temperature of the
solid sorbent and other components within the second reactor is higher than the
temperature of the solid sorbent and all other components in the first reactor. At the end
of a half-cycle, with a majority of gaseous reactant desorbed from the sorbent in the
second reactor and a majority of gaseous reactant absorbed on the sorbent in the first
reactor, the absorption/desorption phases are reversed.
[0007] At this half-point of the cycle, the second reactor is then cooled and the
first reactor is heated. At least partial heating of the first reactor can be supplied by
directing heat from the second reactor to the first reactor. This recuperation of energy
from the second reactor can increase the overall energy efficiency of the system since less
external heating is required to heat the first reactor.
[0008] The overall efficiency can also be increased by cooling the second
reactor by transferring a portion of any condensed refrigerant to the heat exchange section
of the second reactor. Such cooling may be assisted by utilizing vaporized heat transfer
fluid or refrigerant for driving the liquid heat transfer fluid or refrigerant in the cooling
loop, such as disclosed in U.S. Patent No. 5,477,706.
SUMMARY
[0009] One embodiment is a cooling system. The cooling system may have a
first reactor system comprising one or more first reactors configured to adsorb and desorb
a gaseous reactant onto a first solid sorbent composition; a second reactor system
comprising one or more second reactors configured to adsorb and desorb the gaseous
reactant onto a second solid sorbent composition; a conduit connecting the one or more
first reactors of the first reactor system to the one or more second reactors of the second
reactor system, and comprising a controllable valve; and an electronic controller
configured to control the recouperation time between the first reactor system and the
second reactor systems by operating the controllable valve to equalize the pressure of the
reactant gas between the first reactor system and the second reactor system.
[0010] Another embodiment is a method of controlling a cooling system that
includes providing a first reactor system comprising one or more first reactors configured
to adsorb and desorb a gaseous reactant onto a first solid sorbent composition; providing
a second reactor system comprising one or more second reactors configured to adsorb and
desorb the gaseous reactant onto a second solid sorbent composition; providing a conduit
connecting the one or more first reactors of the first reactor system to the one or more
second reactors of the second reactor system, and comprising a controllable valve; and
electronically controlling the recouperation time between the one or more first reactors
and the one or more second reactors by operating the controllable valve to equalize the
pressure of the reactant gas between the first reactor system and the second reactor
system.
BRIEF DESCRIPTION OF THE DRAWINGS
[0011] Fig. 1 is a schematic illustration of two opposing banks of reactors
illustrating the piping and valve for reactor recuperation according to one aspect of the
invention; and
[0012] Fig. 2 is a schematic illustration of a two-sorber system illustrating one
aspect of the invention.
DETAILED DESCRIPTION
[0013] Embodiments of the invention relate to complex compound heating
and cooling systems and methods that efficiently manage adsorption/desorption cycles of
these systems. In use, after each half-cycle in which a first reactor has completed
absorption, and the other opposing second reactor has completed desorption, the cycles
are reversed. During this reversal in cycles, energy is recuperated by connecting the
absorber and desorber reactors together so that a portion of the remaining absorbed
gaseous reactant from the desorbing reactor is directed to the opposing reactor. As one
example, the system may include piping disposed between the opposing reaction
chambers to transfer the gaseous reactant from one reactor to the other. In one
embodiment, an electronically controllable valve is used to control the equalization time
of the recuperation between the two reactors.
[0014] During the controllable recuperation process a controllable valve can
be disposed into tubing run between the absorber and desorber to precisely control the
time that the sorbers are connected together. Opening the controllable valve results in a
mass transfer from the high-temperature sorber to the low-temperature sorber. The mass
transfer causes the temperature of the high-temperature sorber to be reduced and
temperature of the low-temperature sorber to be increased.
[0015] In one embodiment, the equalization time used in the system is
optimized to increase the overall efficiency of the system. For example, before the
discovery of the benefits and effects of cycle pressure equalization as described herein
were known, typical recovery periods of about 4 minutes were used within each system.
However, it was discovered that shorter periods between about 20 seconds and 4 minutes
were found to be advantageous. In some embodiments, it was found that periods as long
as 4 minutes rarely increased efficiency, as capacity declines in the system exceeded
gains in efficiency. This was particularly discovered when recovery times approached 4
minutes.
[0016] Increasing the time provided within a system to equalize the pressure,
and thus temperature, between an absorber and desorber will increase the cycle energy
efficiency because more heat can be transferred from one sorber to the other. However
this increased time results in an overall decrease in capacity since the system can perform
fewer cycles per unit of time. Thus, decreasing the equalization time of the sorbers will
increase the overall system refrigeration capacity over the full cycle of absorption and
desorption of each sorber. Embodiments of the invention provide the most efficient
balance between these considerations by providing a predefined equation, a
predetermined data curve or a customized lookup table that is integrated into the system
and allows for custom control of the overall efficiency of the system.
[0017] In one embodiment, each complex compound system may include a
specific electronic lookup table that allows the system to adjust the recuperation time
depending on the efficiency needs of the system. For example, an electronic controller
may be configured to detect the demand on the system and adjust the capacity of the
system accordingly by adjusting the system's recuperation times. In times when greater
capacity is required, the system may refer to the lookup table and adjust the recuperation
time downward so that the capacity of the system increases. Although this will increase
the energy demand by the system, the capacity needs may be met. However, in some
situations, such as when the product or load meets the setpoint tempertature in a shorter
period, overall efficiency can be better than when the setpoint is reached in a longer
period. Similarly, when the capacity requirements on the system are reduced, the system
can refer to the lookup table to properly adjust the recuperation time upward to increase
the energy efficiency. The determination of how long the reactors should equalize can
also be based on other considerations. For xample, this time could be based on a
combination of the setpoint, the load temperature, and/or the sorber temperatures. An
optimized algorithm may be used to reach the desired temperature at the most optimum
time and/or efficiency
[0018] The present disclosure comprises a method and apparatus for providing
recuperation between two opposing sorbers or banks of sorbers in a single or multiplestage
solid-vapor sorption system utilizing the sorption energy that exists between the
reactors. The method may utilize a mass-fraction of remaining absorbed vapor on the
sorbent in the desorbing reactor near the completion of a half-cycle, prior to reversing the
phases. The method can be carried out by utilizing piping between the reaction chambers
of the opposing reactors and one or more valves for opening and closing the pipe or pipes
whereby the timing of the recuperation may be selected and controlled to achieve the
desired energy transfer.
[0019] As used herein, the term "compound" and "solid sorbent composition"
is intended to mean any reaction product formed by absorption or adsorption and
desorption of a gaseous reactant on a solid reactant, i.e., chemisorption, within the scope
of the invention. "Absorption" and "adsorption" may be used interchangeably. A reactor
or sorber, within the scope of intended apparatus, includes a reaction chamber containing
the solid sorbent and heat exchange components including piping for directing heat
transfer fluids to and from the reactor in contact with the sorbent, as well as resistive
heating elements, and the like. Examples of such reactors are disclosed in the aforesaid
U.S. patents, particularly U.S. Patent Nos. 5,298,23 1, 5,328,671 , and 5,477,706.
[0020] In chemisorption reactions, desorption is carried out at relatively high
pressure and temperature while absorption is carried out at relatively low pressure and
temperature. Because of the high-pressure difference between opposing absorption and
desorption reactors, the time or duration required for the recuperation process is relatively
short. The initiation of the recuperation during the cycle is carried out near the
completion of the cycle where the remaining mass of gaseous reactant or refrigerant
vapor desorbed from the solids sorbent is not usually used for producing
refrigeration/cooling because of pressure and/or efficiency limitations.
[0021] In the configurable system, the recuperation is carried out near the
completion of a cycle for a predetermined time to adjust efficiency of the system. In a
chemisorption reaction process, the desorbing reaction temperature for a specific sorbent
composition is higher than the absorption temperature of the same sorbent composition.
Specific examples of absorption and desorption temperatures for a number of
ammoniated complex compounds are disclosed in the tables of U.S. patent number
5,079,928, the description of which are incorporated herein by reference. Temperature
differentials for absorbing and desorbing compositions are well known to those skilled in
the art.
[0022] The temperature differential between an absorbing and desorbing
reactant is referred to as DT. The recuperation may be carried out for a time sufficient to
yield a temperature change of at least about 70%, 60%, 50%, 40%, 30%, 20%, 10% or
5% DT. The time required to accomplish such recuperation may be between about 10
seconds to about 4 minutes. By using the recuperation process described herein, a
desorbing reactor is benefited by temperature reduction whereby less cool-down is
needed to achieve a temperature required for absorption, and an absorbing reactor is
benefited by the temperature increase thereby reducing the amount of heating required for
desorption. Thus, desorbing and absorbing reactors are respectively benefited as is the
overall efficiency of the system.
[0023] Solid reactants suitable for forming the solid sorbent compositions
useful in the present invention include absorbents such as metal oxides, sulfides, sulfates
and metal hydrides, and zeolites, activated carbon, activated alumina, and silica gel. Such
absorbents may be reacted with polar or non-polar gaseous reactants. Suitable non-polar
gaseous reactants include natural gas C1-C6 lower alkanes (e.g., methane, ethane,
propane, etc.), cryogenic refrigerants (helium, argon and hydrogen), environmental gases
(oxygen, nitrogen, hydrogen, NOx, CO2 and CO) and the fluorocarbon CFC, HCFC and
HFC refrigerants. Of the aforesaid, preferred systems use zeolites or activated carbon
with fluorocarbons or polar gas refrigerants water or ammonia, or a metal hydride with
hydrogen. However, the preferred solid sorbent compositions are the complex
compounds formed between an inorganic metal salt and a polar gas refrigerant.
Adsorption of the polar gas on the salt is carried out in a chemisorption reaction to yield
the complex compound. Preferred metal salts are selected from alkali and alkaline earth
metals, transition metals, aluminum, zinc, cadmium and tin. Preferred transition metals
are manganese, iron, nickel and cobalt. Preferred metal salts include nitrates, nitrites,
perchlorates, oxalates, sulfates, sulfites, and halides, particularly chlorides, bromides and
iodides of the metals. Preferred polar gases include ammonia, water, methylamine and
ethanol, ammonia being especially preferred. Other suitable polar refrigerants include
sulfur dioxide, lower alkanols, alkylamines, polyamines and phosphine. These as well as
other suitable and preferred reactants and resulting complex compounds are disclosed in
the aforesaid patents, particularly U.S. Patent Nos. 5,441,716 and 5,628,205, incorporated
herein by reference. Particularly preferred systems are opposing reactors or banks or
series of reactors incorporating one or more of the following complex compounds:
BaCl2»0-8(NH ), SrCl2»l-8(NH ), SrBr2»2-8(NH ), CaCl2»0-l(NH ),
CaCl2»l-2(NH ), CaCl2»2-4(NH ), CaCl2»4-8(NH ), CaBr2»2-6(NH ),
NiCl2»2-6(NH ), FeCl2»2-6(NH ), FeBr2»2-6(NH ), CoCl2»2-6(NH ),
CoBr2»2-6(NH ), MgCl2»2-6(NH ), MgBr2»2-6(NH ), MnCl2»2-6(NH ),
MnBr2»2-6(NH ), CuS0 2»2-6(NH ), ZnCl2»l-4(NH ), NaBF4»0-3(NH ) and
LiCl»l-3(NH ) .
[0024] A system of opposing and alternately absorbing and desorbing gaseous
reactants on the solid sorbent compositions may also include staged reactors such as
described in U.S. Patent Nos. 5,079,928 and 5,263,330. In addition, pairs or banks of
opposing stage reactors may also be used. In such multiple-staged compound systems, as
well as the single-staged systems, it is advantageous to include heat exchange loop
plumbing for directing heat transfer fluid or fluids between the reactors to take advantage
of the DT between absorbing and desorbing reactors using such staging for cooling a
desorbed reactor to a lower temperature in order to initiate absorption, and to assist in
heating an absorbed reactor prior to initiating desorption, further increases the efficiency
of the system. However, the present invention may substitute, complement, or replace
heating and cooling heat exchange hardware and components used in the previously
described systems and known in the art and which use pumped flow or phase-change
fluids and require complex piping and other components, whereby the size and cost of the
absorption system and its operation may be significantly reduced.
[0025] An example of one embodiment of a system 10 according to the
invention is schematically illustrated in Fig. 1. The illustrated apparatus includes a first
solid phase reactor 22 and a second solid phase reactor 24. The reactors 22, 24 are
connected with one another through recuperation line conduits 23 and 25, and an
electronically controllable valve 30. The valve 30 may be a solenoid valve or any other
type of electronically controllable valve known to those of skill in the art. The valve 30
communicates with a control system 31 that opens and closes the valve to control fluid or
gas flow between the reactors 22, 24.
[0026] A flow meter 2 1 is located along conduit 25 and measures the flow of
fluid or gas between the reactors 22, 24. In addition, a pressure transducer 26 is located
along conduit 23 and configured to measure the pressure existing in the line between the
reactors 22, 24. The flow meter 2 1 and the pressure transducer 26 are in electrical
communication with the control system 31 to provide pressure and flow readings to the
control system.
[0027] As will be explained in more detail below, the control system 31 is
programmed to receive pressure and flow readings from within the conduits 23 and 25
and operate the valve 30 when required to increase the efficiency of the system 10.
[0028] A heat transfer fluid is directed into the heat exchange component of
reactor 24 via a pipe 34 and out from the reactor via a pipe 31. Similarly, heat transfer
fluid is directed into reactor 22 from a pipe 32 and out from a pipe 33. Pipe 27
communicates with reactor 22 and directs refrigerant vapor desorbed from reactor 22 to a
system condenser or energy recovering reactor (not shown) and may be used for returning
refrigerant vapor from a system evaporator or reactor (not shown) to the reactor 22.
Similarly, pipe 28 communicates with reactor 24 and is used for directing refrigerant
vapor to and from reactor 24.
[0029] During the controllable recuperation process the control system 31
causes the valve 30 to control the time that the reactors 22 and 24 are connected together.
Opening the valve 30 results in a mass transfer from whichever is the higher-temperature
reactor to the lower-temperature reactor, which results in reducing the temperature of the
higher-temperature reactor and increasing the temperature of the lower-temperature
reactor. This results in an increased efficiency in the overall operation of the system 10
because of the thermal transfer from the higher temperature reactor to the lower
temperature reactor, which reduces the energy required to heat the lower temperature
reactor during each half-cycle.
[0030] Figure 2 shows more details of the control system 31. As indicated,
the control system 31 includes a processor 101 linked to a lookup table 105, a valve
control module 110, a thermal sensor interface 115, and a demand analysis module 120.
The demand analysis module senses the current demand on the system, and allows the
controller 31 to adjust capacity when the demand is below a predetermined threshold in
order to increase efficiency.
[0031] For example, the demand analysis module may continually sense the
thermal demand for cooling on the systems, and continually adjust the equalization time
between the two reactors by reference to the lookup table 105. One example of a lookup
table is shown below as Table 1. Of course, aspects of the invention are not limited to
referencing a lookup table. The system may reference a pre-stored or predetermined data
curve of equalization times and refrigerator demands. The system may also refer to a
particular equation to calculate the proper amount of equalization time given a particular
cooling/refrigeration demand. However, it should be realized that each type of system
may have a different table, equation or curve based on the system's capacity and overall
features.
Table 1
Example System Lookup Table
Equalization Time Coolina/Refri aeration
mins DemandiBtu/hr)
0.5 18000
0.75 17700
1 17500
1.5 17300
2 17 160
3 17000
4 16850
[0032] The system may being the equalization process at any time during each
cycle. However in some embodiments, the system will begin the equalization process
when the absorber and desorber pressures are within a certain bar of pressure in
comparison to the system's condenser. In one embodiment, the condenser is within two
or three bars of pressure within the absorber and the desorber. In this example, the
condenser may have a pressure of 20 bar, while the absorber has a pressure of 17 bar and
the desorber has a pressure of 23 bar. When the demand analysis module determines that
the absorber and desorber are within this pressure range with the condenser, then the
system can be placed into an energy efficiency optimization mode wherein the cycle
pressure equalization time between the absorber and the desorber is controlled to
maximize the efficiency of the system.
[0033] It should be realized that the system is not limited to this particular set
of pressures to begin optimizing the efficiency of the system 31. For example, the demand
analysis module may determine that a pressure difference of 2, 3, 4, 5, 6, 7, 8, 9, 10 or
more bars of pressure between the absorber, desorber and condenser is the proper trigger
for optimizing the efficiency of the system 31.
[0034] In one embodiment, the equalization time used in the system is
optimized to increase the overall efficiency of the system. For example, before the
discovery of the benefits and effects of cycle pressure equalization as described herein
were known, typical recovery periods of about 4 minutes were used within each system.
However, it was discovered that shorter periods between about 20 seconds and 4 minutes
were found to be advantageous. In some embodiments, it was found that periods as long
as 4 minutes rarely increased efficiency, as capacity declines in the system exceeded
gains in efficiency. This was particularly discovered when recovery times approached 4
minutes. For this reason, providing the system with an intelligent means for adjusting the
equalization time provided a system that could run with greater efficiency during times of
reduced demand and yet still be flexible enough to provide greater capacity when demand
was high.
[0035] In some embodiments, the two reactors can be supplied with CaBr2,
with ammonia adsorbed on the salt to provide a complex compound for adsorption and
desorption between the coordination steps CaBr2»2-6. Both reactors can be heated and
cooled, respectively, using Syltherm XLT™ heat transfer fluid. The system is run for
half-cycle absorption/desorption periods and between each half-cycle the valve can be
controlled to provide a variable-length equilibrium time between each half cycle.
[0036] Typically, chemisorption reaction cycles are carried out with
absorption and desorption reactions running substantially concurrently. However, the
process of the invention may also be used in systems having multiple reactors or multiple
banks of reactors which are intentionally programmed to operate out of phase. Such
operation may be especially useful in a system designed for continuous cooling and/or
freezing wherein desorption is desirably carried out more rapidly than absorption, such as
described in U.S. Patent No. 5,628,205. In such applications, any desorbing reactor in
which desorption is almost completed may be coupled with an absorbing reactor
benefiting from such gaseous refrigerant transfer and/or an almost completed absorbing
reactor may be coupled with a benefiting desorbing reactor.
[0037] Those having skill in the art will further appreciate that the various
illustrative logical blocks, modules, circuits, and process steps described in connection
with the implementations disclosed herein may be implemented as electronic hardware,
computer software, or combinations of both. To clearly illustrate this interchangeability
of hardware and software, various illustrative components, blocks, modules, circuits, and
steps have been described above generally in terms of their functionality. Whether such
functionality is implemented as hardware or software depends upon the particular
application and design constraints imposed on the overall system. Skilled artisans may
implement the described functionality in varying ways for each particular application, but
such implementation decisions should not be interpreted as causing a departure from the
scope of the present invention. One skilled in the art will recognize that a portion, or a
part, may comprise something less than, or equal to, a whole. For example, a portion of a
collection of pixels may refer to a sub-collection of those pixels.
[0038] The various illustrative logical blocks, modules, and circuits described
in connection with the implementations disclosed herein may be implemented or
performed with a general purpose processor, a digital signal processor (DSP), an
application specific integrated circuit (ASIC), a field programmable gate array (FPGA) or
other programmable logic device, discrete gate or transistor logic, discrete hardware
components, or any combination thereof designed to perform the functions described
herein. A general purpose processor may be a microprocessor, but in the altemative, the
processor may be any conventional processor, controller, microcontroller, or state
machine. A processor may also be implemented as a combination of computing devices,
e.g., a combination of a DSP and a microprocessor, a plurality of microprocessors, one or
more microprocessors in conjunction with a DSP core, or any other such configuration.
[0039] The steps of a method or process described in connection with the
implementations disclosed herein may be embodied directly in hardware, in a software
module executed by a processor, or in a combination of the two. A software module may
reside in RAM memory, flash memory, ROM memory, EPROM memory, EEPROM
memory, registers, hard disk, a removable disk, a CD-ROM, or any other form of nontransitory
storage medium known in the art. An exemplary computer-readable storage
medium is coupled to the processor such the processor can read information from, and
write information to, the computer-readable storage medium. In the alternative, the
storage medium may be integral to the processor. The processor and the storage medium
may reside in an ASIC. The ASIC may reside in a user terminal, camera, or other device.
In the alternative, the processor and the storage medium may reside as discrete
components in a user terminal, camera, or other device.
[0040] Headings are included herein for reference and to aid in locating
various sections. These headings are not intended to limit the scope of the concepts
described with respect thereto. Such concepts may have applicability throughout the
entire specification.
[0041] The previous description of the disclosed implementations is provided
to enable any person skilled in the art to make or use the present invention. Various
modifications to these implementations will be readily apparent to those skilled in the art,
and the generic principles defined herein may be applied to other implementations
without departing from the spirit or scope of the invention. Thus, the present invention is
not intended to be limited to the implementations shown herein but is to be accorded the
widest scope consistent with the principles and novel features disclosed herein.

WHAT IS CLAIMED IS:
1. A cooling system, comprising:
a first reactor system comprising one or more first reactors configured to
adsorb and desorb a gaseous reactant onto a first solid sorbent composition;
a second reactor system comprising one or more second reactors
configured to adsorb and desorb the gaseous reactant onto a second solid sorbent
composition;
a conduit connecting the one or more first reactors of the first reactor
system to the one or more second reactors of the second reactor system, and
comprising a controllable valve; and
an electronic controller configured to control the recouperation time
between the first reactor system and the second reactor systems by operating the
controllable valve to equalize the pressure of the reactant gas between the first
reactor system and the second reactor system.
2 . The cooling system of Claim 1, wherein the electronic controller is
configured to control the recouperation time by detecting the external demand on the
cooling system and altering the amount of time the valve is opened based on the external
demand.
3 . The cooling system of any one of Claims 1-2, wherein the electronic
controller controls the recouperation time by reference to a stored equation, a predefined
data curve, or a lookup table to alter the amount of time the valve is opened.
4 . The cooling system of any one of Claims 1-2, wherein the cooling system
further comprises a temperature sensor configured to detect the temperature of the gas
reactant in the conduit.
5 . The cooling system of any one of Claims 1-2, wherein the cooling system
further comprises a pressure sensor configured to determine the pressure of the gas
reactant in the conduit.
6 . The cooling system of Claim 5, wherein the electronic controller is
configured to determine the pressure of the reactant gas in the conduit before equalizing
the pressure of the reactant gas.
7 . The cooling system of any one of Claims 1-2, wherein the one or more
first reactors comprises a complex compound formed by absorbing ammonia on a metal
salt.
8. The cooling system of Claim 7, wherein the one or more second reactors
comprises a complex compound formed by absorbing ammonia on a metal salt.
9 . The cooling system of any one of Claims 1-2, wherein the one or more
first reactors or the one or more second reactors comprises a solid sorbent having a
zeolite, activated carbon, activated alumina or silica gel.
10. The cooling system of any one of Claims 1-2, wherein the one or more
first reactors and the one or more second reactors comprise the same sorbent composition.
11. A method of controlling a cooling system, comprising:
providing a first reactor system comprising one or more first reactors
configured to adsorb and desorb a gaseous reactant onto a first solid sorbent
composition;
providing a second reactor system comprising one or more second reactors
configured to adsorb and desorb the gaseous reactant onto a second solid sorbent
composition;
providing a conduit connecting the one or more first reactors of the first
reactor system to the one or more second reactors of the second reactor system,
and comprising a controllable valve; and
electronically controlling the recouperation time between the one or more
first reactors and the one or more second reactors by operating the controllable
valve to equalize the pressure of the reactant gas between the first reactor system
and the second reactor system.
12. The method of Claim 11, wherein electronically controlling the
recouperation time comprises:
detecting the external demand on the cooling system; and
altering the amount of time the valve is opened to equalize the pressure
based on the detected external demand.
13. The method of Claim 12, wherein altering the amount of time the valve is
opened is based on reference to a stored equation, a predefined data curve, or a lookup
table.
14. The method of any one of Claims 11-1 3, further comprising measuring the
temperature of the gas reactant in the conduit.
15. The method of any one of Claims 11-1 3, further comprising measuring the
pressure of the gas reactant in the conduit.
16. The method of Claim 15, wherein measuring the pressure of the gas
comprises determine the pressure of the reactant gas in the conduit before equalizing the
pressure of the reactant gas.
17. The method of any one of Claims 11-13, wherein the one or more first
reactors comprises a complex compound formed by absorbing ammonia on a metal salt.
18. The method of Claim 17, wherein the one or more second reactors
comprises a complex compound formed by absorbing ammonia on a metal salt.
19. The method of any one of Claims 11-13, wherein the one or more first
reactors or the one or more second reactors comprises a solid sorbent having a zeolite,
activated carbon, activated alumina or silica gel.
20. The method of any one of Claims 11-13, wherein the one or more first
reactors and the one or more second reactors comprise the same sorbent composition.