JPH07294055A - Rotary absorption heat pump - Google Patents

Abstract

(57) [Summary] [Purpose] To provide a rotary absorption heat pump assembly. [Structure] The assembly includes a generator (2), a condenser (3),
Evaporator (4), absorbent cooler (5), and absorber (1)
The functional absorber (1) is arranged in end-to-end relationship with the generator (2) as a constituent element of an absorption heat pump having high efficiency and excellent operating characteristics. It is in communication with this generator. The condenser (3) and the evaporator (4) are end-to-end outside the absorber (1) and the absorber cooler (5) and are concentric with the absorber and the absorber cooler and have a radius Are spaced apart in the direction.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION Absorption chillers used as chillers and ice makers, by the good part of this century, make vapor compressors of similar capacity faster than date. Although vapor compressors have replaced it since electricity has become commonplace and with the introduction of chlorofluorocarbon refrigerants, absorption refrigerators have not been completely removed from the market. Since the 1950s, vapor compressors manufactured to perform indoor air conditioning not only cool in the summer,
It heats up in the winter months, which gives it the character of a true heat pump. Thus, heat pumps are classified into two types, rotary absorption heat pumps (RAHPs) and vapor compression heat pumps (VCHPs).

[0002]

The reputation of VCHP, which was initially very high in the market, has changed over time. The world has become more sincere in its efforts to conserve energy, especially since the huge rise in energy prices that occurred in the mid-1970s. Nowadays, the absorption refrigeration process is highly evaluated from the viewpoint of economic balance.
This is because lower waste heat efficiency can be used.

Further, chlorofluorocarbon (CFC)
With the recognition of the destructive behavior of terrestrial ozone on the earth's ozone layer, the traditional position of refrigerants for use in VCHP has been lost, thus increasing the appreciation for absorption refrigeration processes. .

RAHP differs from conventional VCHP both in terms of cycle of operation and its structure. RAHP
And VCHP have common components, the evaporator and the condenser, but no other similar components. VCHP
Then, the pressure of the vapor generated in the evaporator is increased by a mechanical pump, and the condenser is cooled and liquefied at a higher pressure.
It is then returned to the evaporator to complete the cycle.
In RAHP, the refrigerant vapor generated in the evaporator is absorbed by the deliquescent material located in a component called the absorber. The diluted deliquescent material is then transferred to a component termed a generator in which it separates the refrigerant vapor from the material and adds heat to increase the pressure of the refrigerant vapor. The high pressure vapor is then directed to a condenser where it is cooled and liquefied before being returned to the evaporator to complete the cycle.

In essence, the RAHP absorber, generator,
And deliquescent materials or absorbents replace VCHP mechanical compressors. Instead of the mechanical energy required to drive the VCHP's compressor, RAHP uses low-grade heat to separate the refrigerant from the absorbent, with the concomitant increase in refrigerant vapor pressure within the generator. Let

To take advantage of the benefits of rotation, a rotary VCHP was constructed and tested. It has been found that these devices are smaller and operate quieter than static VCHP. However, rotary seals that compromise hermeticity and market acceptance have not been obtained.

In order to maintain the tightness of the object and at the same time to use the waste heat, the structure of the rotary VCHP disclosed in Donner US Pat. No. 3,863,454 was advocated. However, with the Donner design,
In addition to requiring high temperature heat sources for its operation, chlorofluorocarbons are still used as refrigerants and as boiler working fluids.

[0008]

SUMMARY OF THE INVENTION It is an object of the present invention to apply the process of an absorption heat pump to an integral rotating structure, which provides a small and mechanically simple heat pump installation. The nature of rotation is used to simplify the process of heat pumps, thereby increasing the popularity of absorption refrigeration units on the market.

Another important object of the present invention is to save energy, primarily by avoiding the wasteful process of converting the energy of the fuel into mechanical or electrical energy for operating the cooling equipment. is there.

Yet another object of the present invention is to accommodate changes in air temperature, rotational operating speed, and generator temperature, which may result in undesired crystallization of the absorbent solution during operation or shutdown of the heat pump unit. SUMMARY OF THE INVENTION It is an object of the present invention to provide a rotary absorption type heat pump unit having a small size and an integral structure, which minimizes the occurrence of deterioration.

Another object of the present invention is to construct RAHP evaporator and condenser components concentrically and coaxially with the absorber, with these components generally located radially outside of the absorber. This reduces the physical size of RAHP.

Yet another object of the present invention is to improve the efficiency of RAHP by making a very thin membrane of absorbent in the absorber with a thickness and residence time such that the absorption refrigeration process is performed at optimal completion. And to improve capacity.

[0013]

SUMMARY OF THE INVENTION The rotary absorption heat pump of the present invention comprises a plurality of enclosed interconnected components, namely an evaporator and a condenser, radially outside the absorber and the absorbent cooler. And a chamber mounted to rotate as a group so as to be arranged concentrically with the absorber and the absorber cooler. These elements are combined with the generator to form an airtight and liquidtight group.

Evaporation and condensation are added to the refrigerant working fluid used. These processes are carried out at two pressure levels. However, in order to obtain different pressure levels, instead of using a mechanically driven compressor, a thermally actuated generator is used in combination with a tapered absorber. Therefore, the heat, rather than the mechanically or electrically driven compressor, provides most of the energy required for rotation.

The invention is obtained in particular by burning heated effluents from industrial processes, heat of radiators, hot exhaust gases from internal combustion engines, solar heat or cheap hydrocarbons or other fuels. Waste heat such as heat that can be generated is used.

The interconnected components or chambers are
A generator that separates the refrigerant from the absorbent by changing it to a refrigerant vapor and a concentrated liquid absorbent fraction by applying heat, and condenses and liquefies the refrigerant vapor at a predetermined pressure, thereby releasing the heat of condensation. A condenser, an evaporator that evaporates the liquefied refrigerant vapor to absorb the heat of evaporation and cool the evaporator walls and associated fins, and a concentrated absorbent that moves very thin along the tapered, cooled inner walls. And the tapered absorber described above arranged in a thin film. This allows the refrigerant vapor from the evaporator to be absorbed completely and efficiently, thereby creating the original diluted absorbent from which the refrigerant vapor is again separated at the generator to complete the cycle. To do.

As will become more apparent in the following description, the capacity of a rotary absorption heat pump is primarily determined by the capacity of that absorber, which can be considered a high efficiency chemical contactor.

The parameters that determine the capacity of the absorber include:
It includes its axial length, average radius, taper angle, and its rotational speed. For a given capacity of the absorber, it is better to change any one of these parameters, in order to keep the capacity of the absorber constant,
The rules that disclose the required changes in one or more of the other parameters are provided below. The absorber is RAHP
Alternatively, its shape can be modified within the rules described below to accommodate the intended use of other applications.

[0019]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT Referring to FIGS. 1 and 2, these figures show an absorber 1, a generator 2, a condenser 3, an evaporator 4 and an absorbent cooler 5.

Structurally, the absorber 1, the absorbent cooler 5,
And the generator 2 constitutes a first subassembly. The condenser 3, the evaporator 4, the absorber end plate 30, the absorber bearing shaft 31, and the absorber external bearing 32 form a second subassembly. Absorber heat insulation barrier 26, absorbent transfer pipe 2
0, the generator insulation barrier 21, the refrigerant vapor pipe 67, and the support flange 68 constitute a third subassembly. Pitot tube pump 17, generator end plate 12, generator bearing shaft 1
3. The generator outboard bearing 14 constitutes a fourth subassembly. The preferred order of final assembly is the first, second, third, and fourth order, although any other order is also possible.

The interior of the absorber 1 is bounded by an absorber insulation barrier 26, an absorbent transfer tube 20, a generator insulation barrier 21, and a tapered wall 7 of the absorber. The absorber, roughly speaking, constitutes a true frustoconical hollow truncated body that tapers outward in the downstream direction.

The refrigerant vapor created by boiling the refrigerant in the evaporator 4 is supplied to the absorber through a typical exhaust pipe 44 of the evaporator which penetrates the heat insulating barrier 26 of the absorber. The concentrated liquid absorbent is used as an insulating barrier 26 for the absorber.
The absorber cooler 5 enters the absorber 1 through a typical vacuum slot 33 cut around the periphery of the absorber. The liquid absorbent is 0.076 mm (0.006 mm) on the tapered wall 7 of the absorber.
Form a very thin film "d", on the order of 3 inches). The very thin film of absorbent absorbs the refrigerant vapor as it moves under the action of rotation from the adiabatic barrier 26 of the absorber towards the adiabatic barrier 21 of the generator and at the same time is diluted during this process. Release absorbed heat.

If this process is continued, the absorbed heat has to be removed. In the illustrated embodiment, the heat of absorption is
Removed by typical fins 8 of the absorber. A large number of fins are attached to the outer surface of the tapered wall 7 of the absorber and cover the entire wall both axially and circumferentially. The diluted, very thin absorbent film “d” is shown in FIG. 7 and FIG.
An annular passage 52 to and from the generator flange 10, leaves the absorber 1 by a typical radial slot 53 and enters the generator 2 through a typical circumferential slot 54.

The ambient vapor pressure in absorber 1 is less than or equal to the ambient vapor pressure in generator 2 and absorbent cooler 5. The concentrated liquid absorbent in the cooler 5 must be depressurized at the junction of the adiabatic barrier 26 of the absorber and the tapered wall 7 of the absorber and distributed evenly around the perimeter. As we all know,
There is a pressure drop on the liquid flowing through the tube or conduit.
Thus, a thin film vacuum slot 33 is formed around the adiabatic barrier 26 of the absorber so that an axial closed passage is formed when the adiabatic barrier 26 of the absorber is positioned with respect to the tapered wall 7 of the absorber. It is cut. Each of a number of vacuum slots 33 disposed around the adiabatic barrier 26 reduces the ambient pressure of the concentrated liquid absorbent from the ambient pressure in the absorbent cooler 5 to the ambient pressure in the absorber 1. Has width and depth. Concomitant with this, the slots are distributed around the circumference so that the concentrated liquid absorbent is evenly distributed on the tapered wall 7 of the absorber.

The liquid absorbent is diluted with the absorbed refrigerant vapor as it traverses the axial length of the tapered wall 7 of the absorber,
The adiabatic barrier 21 of the generator has to pump it to the generator 2 which has a higher pressure than the absorber. This is done by a large number of radial slots 53 distributed circumferentially between the generator's insulating barrier 21 and the absorber-generator flange 10. The radial slots 53 are formed in a manner similar to the vacuum slots 33, except that these slots cut into the absorber-generator flange 10. As is well known, the acceleration force generated by the action of rotational momentum,
Pushes the liquid absorbent radially outward. In the present case, this effect is somewhat balanced by the high pressure present in the generator 2. The radial length of the radial slots 53 is such that centrifugal forces exert a pressure on the liquid absorbent that is greater than the high counterbalancing pressure in the generator 2, which causes a flow from the absorber 1 to the generator 2. It is such a length. For an average RAHP unit, the optimum thickness of thin film "d" is from about 0.00254 mm to about 0.
It is in the range of 127 mm (0.1 mil to 5.0 mil).

Means are provided for keeping the thickness of the thin film of liquid absorbent in the absorber 1 essentially constant during operation of the device.

The heat pump capacity of RAHP is maximum when the thickness of the absorbent thin film is uniform at each axial position and everywhere. For this reason, the absorber wall 7 must be concentric with the axis of rotation 51 along its entire surface. actually,
It is not reasonable to expect mechanical perfection. The consequences of imperfections are terrible. If the centerline of the tapered wall 7 of the absorber is offset from the unit axis of rotation 51 by 0.0254 mm (1 mil), the capacity is reduced by about 10%.

Accordingly, the tapered wall of the absorber is provided with a partition or baffle 85 extending axially from the absorber thermal barrier 26 to the generator thermal barrier 21. These baffles have a thickness of about 2 of the thin film flowing on the inner surface of the absorber wall.
It doubles from the tapered wall 7 of the absorber.

As shown in FIG. 6, the surface of the absorber wall 7 is divided into four quadrants, with the liquid absorbent in each quadrant being separated from the liquid absorbent in the other quadrants by a partition 85. .
Therefore, even if there is no liquid flow between the quadrants and the centerline of the tapered wall 7 of the absorber is eccentric with respect to the rotational axis direction 51, the thin film thickness remains essentially constant.

Typical dimensions for bulkhead 85 are 0.152 mm (6 mils) high and 0.254 mm wide.
(10 mil) and has the same length as the tapered wall of the absorber. The partition wall may be formed in a portion of the wall 7 using various suitable means such as electroplating, electroless plating, etching, plasma spraying and the like. The septum may be inserted into the absorber 1 as a separate subassembly, in which case the septum may be made of plastic or other suitable material.

The taper angle θ of the absorber wall is a design variable that varies depending on the capacity and other properties of the equipment, which is about 0.1 ° (0.001745 radians) for normal equipment.
The taper angle from to the arctangent of twice the average radius of the absorber divided by its axial length is suitable. Suitable values for θ are in the range of about 2.0 ° (0.0349 radians) to about 7.0 ° (0.1222 radians).

The inside of the generator 2 is the adiabatic barrier 2 of the generator.
1, bounded by a generator shell 11 and a generator end plate 12. The diluted liquid absorbent enters the generator 2 from the absorber 1 at the end of a peripheral lip 23, which is an annular extension of the insulating barrier 21 of the generator. The diluted liquid absorbent is heated and thereby separated from the refrigerant. At that time, a relatively thin layer “C” is formed along the inner surface of the generator shell 11 from the peripheral lip 23 to the pitot tube reservoir 5.
When moving axially up to 5, the liquid absorbent is converted into a concentrate. The momentum for moving the thin film of liquid absorbent in the axial direction is such that the thickness of the thin film at the location of the peripheral lip 23 is slightly thicker than the thickness of the thin film near the position of the Pitot tube reservoir 55, which results in liquid absorption. It results from creating a slight taper in the film of agent. This effect is exactly the same as the effect produced by the mechanical taper of the tapered wall 7 of the absorber 1. Alternatively, the inner surface of the generator shell 11 may be mechanically tapered.

The generator 2 takes in the diluted liquid absorbent and withdraws part of the refrigerant by boiling with the heat applied to the outer surface of the shell 11 of the generator, thereby forming a superheated refrigerant vapor, which is then , Superheated refrigerant vapor, refrigerant vapor inlet 3
Discharge into 5. The concentrated liquid absorbent moves axially within the inner surface of the generator shell 11 before entering the pitot tube reservoir 55. A predetermined constant flow rate of absorbent is pumped from the pitot tube reservoir 55 into the absorbent transfer tube 20 by the pitot tube pump 17.

Correspondingly, the generator 2 produces two effluents during its operation, since the absorber 1 requires two influents for proper operation. These classify themselves into vapor and liquid cycles. The liquid absorbent is
From the transfer pipe 20, along with the absorbent cooler 5 for removing excess heat, into the absorber 1 which receives the absorbent in a concentrated state and dilutes it, and receives the absorbent in a diluted state. It circulates only through the path to the generator 2 which delivers it in concentrated form.

The refrigerant vapor is generated from a generator 2 for separating the refrigerant vapor from the diluted liquid absorbent, to a condenser 3 for cooling and liquefying the refrigerant vapor, to an evaporator 4 for further vaporizing the refrigerant, and for the refrigerant to be a liquid. It is circulated through the path to the absorber 1 which absorbs with the concentrated absorbent, and then into the diluted liquid absorbent and goes further back into the generator 2 to complete the cycle.

The condenser 3 is internally bounded by a refrigerant vapor inlet 35, a heat insulating plug 39, and a condenser / evaporator tube 37. The superheated refrigerant vapor enters the refrigerant vapor pipe 67 arranged in the generator 2 at the refrigerant vapor inlet 35. The refrigerant vapor pipe 67 is connected to an extension 87 of the pipe that penetrates the heat insulating barrier 21 of the generator and is made liquid-tight by the refrigerant vapor pipe seal 70.

Superheated refrigerant vapor is introduced into the radial holes 86 provided in the absorber-generator flange 10. As shown in FIGS. 2 and 6, a connection pipe 36 is attached to the radial hole 86 of the connection pipe 36. The other end of the cross connection pipe 36 is joined to the header 40 of the condenser. The union fitting 80 allows the first and second assemblies to be attached and detached as defined above.

A condenser fin 81 is attached to the condenser / evaporator tube 37 at the position of the condenser 3. The condenser fin 81 is made of a highly heat conductive material such as copper or aluminum and is a continuous thin annular disk to provide radial constraint to the centrifugal force exerted on the condenser / evaporator tube 37. Is.

The condenser 3 has an annular cylindrical shape consisting of a number of condenser fins 81 and condenser / evaporator tubes 37.
Each of the plurality of condenser / evaporator tubes 37 is connected to the condenser header 40, but only a few condenser / evaporator tubes are connected to the evaporator 4 in the liquid trap 38 and the remaining The condenser / evaporator tube is isolated and insulated from the evaporator portion of the condenser / evaporator tube 37 by an insulating plug 39.

The condenser 3 has two functions, the first of which is
Function is to liquefy the superheated refrigerant vapor exiting the generator 2, and the second function is to create an air flow through the multiple fins 8 of the absorber and then through the multiple fins 81 of the condenser. It is a function. To remove the absorbed heat, the heat must be removed from the absorber 1 and to remove the heat of condensation, the heat must be removed from the condenser 3, the sum of these heats being sent to the generator. Greater than heat input.

The evaporator 4 comprises the condenser 3, the adiabatic plug 39 and the liquid trap 38 described above, the evaporator portion of the continuous condenser / evaporator tube 37, the evaporator header 42 with all tubes attached, the evaporator. The interior is bounded by a radial hole 65 intersecting the annular space in the header 42 and an evaporator exhaust pipe 44 extending from the radial hole 65 and terminating in the absorber 1.

The evaporator 4 receives the liquefied refrigerant from the condenser 3 via the liquid trap 38. These liquid traps are provided at equal intervals in the circumferential direction. The function of the liquid trap 38 is to isolate the vapor volume of the evaporator 4 from the high pressure vapor volume of the condenser 3 while at the same time allowing liquefied refrigerant to flow from the condenser 3 to the evaporator 4. It is not necessary to have a liquid trap on each of the condenser / evaporator tubes 37. This is because, of all the pipes connected to the condenser and the evaporator, the condenser header 40 redistributes the liquefied refrigerant into the condenser 3, and the evaporator header 42 liquefies inside the evaporator 4. This is for redistributing the refrigerant.

The vapor pressure in the condenser section of the condenser / evaporator tube 37 is determined by the generator 2, whereas the vapor pressure in the evaporator section of the condenser / evaporator tube 37 is determined by the absorber. 1
Determined by The vapor pressure in the evaporator is much lower than the vapor pressure in the condenser, and depending on the design, the liquefied refrigerant “b” occupies about half the internal volume of the evaporator portion of the condenser / evaporator tube 37. However, in contrast, the liquefied refrigerant occupies only a few percent of the internal volume of the condenser portion of the condenser / evaporator tube 37.

It is known that the refrigerant contained in the evaporator is vaporized by evaporation from the free surface when a large centrifugal force acts on the condenser / evaporator tube 37 during operation. Heat transfer from the tube wall to the liquid is caused by convection. At the same time, heat transfer occurs only where the liquid refrigerant wets the inner wall of the tube. This is the condenser / evaporator tube 37
This is in contrast to the heat transfer method in the condenser part of the. Maximum heat transfer during liquefaction occurs when the inner wall of the tube is not wet.

The liquid refrigerant in the condenser / evaporator tube 37 is cooled by vaporizing the refrigerant. This cools the tube walls and the evaporator fins 72 attached to them, thereby cooling or removing heat passing through the air near the fins. The process can proceed only if the vaporized refrigerant in the evaporator adds to the residual amount of vapor in the absorber and the absorber continuously discharges the excess residual amount of vapor.

As shown in FIGS. 1, 3 and 4, the inside of the absorber cooler 5 includes a flange 6 of the absorber, an end plate 30 of the absorber, a tapered wall 7 of the absorber, a heat insulating sleeve 34, and It is bounded by an absorbent transfer tube 20 and an adiabatic barrier 26 of the absorber. The absorbent cooler 5 comprises a pitot tube pump 17 and an absorbent packed absorbent transfer tube 20 from the generator 2.
It receives a design mass flow rate of hot concentrated liquid absorbent delivered through. In the present invention, the vapor pressure in the absorbent cooler 5 is the same as the vapor pressure in the generator 2, but it does not necessarily have to be the same.

Concentrated liquid absorbent "a" in absorbent cooler 5
Is cooled to a temperature somewhat higher than the temperature of the condenser.
The refrigerant vapor arriving from the generator 2 in a superheated state is cooled and releases a very small amount of heat contained in the superheated state, but since the heat removal capacity of the absorbent cooler 5 is not sufficient, the refrigerant is Does not condense. As mentioned above, the adiabatic barrier 26 of the absorber
A number of vacuum slots 33 arranged around the
It serves to reduce the overhead pressure exerted on the concentrated liquid absorbent and to form a very thin film "d" on the tapered wall 7 of the absorber.

The insulating sleeve 34 prevents vapor from condensing in the evaporator exhaust line 44 during operation. In the area of the absorber cooler 5, the absorber tapered wall 7 is cooled by air passing through a number of absorber fins 8 mounted on the outer surface of the absorber tapered wall.

The superheated refrigerant vapor generated in the generator 2 by heating the diluted liquid absorbent is condensed in the condenser 3 and thereby generates heat of condensation at a temperature lower than the temperature of the generator 2. , The liquefied refrigerant is transferred to the evaporator 4,
Here, the refrigerant is evaporated at a low temperature to remove the heat of vaporization, and the vapor thus created is absorbed by the very thin moving film "d" in the absorber 1 made of the concentrated liquid absorbent, and the temperature of the condenser is increased. Release heat of absorption at a temperature between and the temperature of the evaporator. To increase the efficiency of the absorber 1, the unconcentrated liquid absorbent from the generator 2 is removed from the absorbent cooler 5 by releasing heat at an intermediate temperature before the liquid absorbent enters the absorber.
Pre-cool with.

In other lossless systems operating in steady state, the heat dissipated by generator 2 and evaporator 4 is absorbed by absorber 1, condenser 3 and absorbent cooling, as required by the energy conservation law. It must equal the energy released by vessel 5. In the cooling mode, the coefficient of performance of the cycle is given by the ratio of the heat absorbed by the evaporator divided by the heat consumed by the generator, ignoring rotational energy. In the heating mode, the coefficient of operation of the cycle is given by the heat released by the absorber, the absorber chiller, and the condenser divided by the heat consumed by the generator, ignoring rotational energy. When the coefficient of operation in the cooling mode is 0.5, the coefficient of operation in the heating mode is 1.5, which means that the fuel energy is 1
Every time 055J (1 BTU) is consumed, 1583J (1.5
It means that the heat energy of BTU) can be released to heat the building. In countries where air conditioning is not important, the heat multiplication factor provided by heat pumps has proved to be an attractive energy storage method.

The thermal energy that must be applied to and exhausted from the various components of the RAHP to enable the cycle to proceed efficiently can be any one of several forms. It should take one form. In the illustrated embodiment, hot gases and air are energy carriers. Since gas and air are relatively poor heat transfer media, an increased surface area is typically used to enhance heat transfer from a cylindrical or annular surface.

FIG. 7 shows the arrangement of the generator fins 79 provided on the outer surface of the generator shell 11. The generator fins 79 are surrounded by a metallic sheath 78. As shown in FIG. 2, the fins 79 of the generator are oriented axially and intentionally extend all the way up to the absorber-generator flange 10 to provide space for the circumferential gas flow. It does not seem to extend. by this,
A return gas flow can occur near the diametrically opposite generator fin 79. Hot gas from the selected heat source is directed axially through the 180 ° (3.142 radian) annular nozzle 83 into the annular space between the generator endplate 12 and the metallic sheath 78. Gas is
It is ejected by a 180 ° (3.142 radians) annular nozzle 84 which is a mirror image.

During the process of traversing the generator fins 79 axially, first in the direction towards the absorber 1 and then in the direction away from the absorber 1, the hot gases heat the fins with which they come into contact. This heats the generator shell 11 by conduction. Finally, a relatively thin layer "C" of diluted liquid absorbent in generator 2 receives the heat and releases the refrigerant vapor by the static evaporation process.

1 and 4 show an absorber fin 8 provided in the absorber 1, an evaporator fin 72 provided in the evaporator 4 and a condenser provided in the condenser 3 as a similar one. The arrangement of the fins 81 is shown. The condenser fins 81 and the evaporator fins 72 are hydraulically or mechanically expanded by expanding the tubes into compression contact with the fins.
It is fixed to the evaporator tube 37. The density of the fins is smaller in the condenser 3 than in the evaporator 4, but in any case should not be so great that the array of fins acts as a filter against common air pollutants,
If the density is high enough to act as a filter, the heat exchange function will be impaired.

The air side design of the condenser removes the condenser heat in the condenser, provides the airflow necessary to remove the absorbed heat in the absorber, and provides cooling in the absorber cooler. It must be suitable to provide the necessary air flow to do. The condenser airflow contains the thermal energy discharged from the absorber cooler 5, absorber 1 and condenser 3 and thus provides a useful output of the RAHP when operating in the heating mode.

The density of the array of condenser fins 81 is typically a density of 3.15 fins per cm (8 per inch) with a 2.4 mm spacing between the fins.
Configure a spacing somewhat larger than (3/32 inch).
At this interval, the viscous drag acting on the air entrained within the annular condenser fin 81 assembly during rotation will cause a particular air flow through the array of fins of the absorber cooler 5 and absorber 1 shown in cross section in FIG. It may not be sufficient to create the pressure head needed to push. In that case, vanes (not shown) may be stamped or molded on the annular surface of the condenser fins 81. The vane is a condenser /
It is arranged so that it lies between the holes provided for the passage of the evaporator tube 37.

The air flow to and from the condenser 3 is substantially radial. Airflow to the condenser 3 is typically obtained from holes 62 in the condenser section located in the plastic sheath 9. To obtain maximum pressure recovery, the condenser 3 may be surrounded by a housing (not shown) having the well-known logarithmic spiral shape.

The absorbent cooler 5 and the absorber 1 are provided with air.
From the air inlet 60 of the absorber, from the hole 62 provided in the plastic sheath 9 arranged in the section of the evaporator 4, from the hole 61 of the isolated section and from the air barrier 59 of the absorber.
From a typical air inlet hole 46 located at. The fin 8 of the absorber has many small holes. This is because it has been empirically known that the cross-channel flow created by such holes prevents the formation of very thin boundary layers. Therefore, heat transfer is greatly improved without a proportionate increase in pressure drop. Furthermore, holes are required in the above-described airflow configuration so that all spaces are in communication.

The heat insulation characteristics of the plastic sheath 9 are as follows.
This is an important requirement in the axial region between the absorber endplate 30 and the evaporator air barrier 57. In this area, holes 62
Is just as important. This is the absorbent cooler 5,
This is because the convective heat transfer between the absorber 1 and the evaporator 4 is prohibited. The negative pressure in the air space of the array of absorber fins 8 dictates the incoming airflow to the absorber cooling airflow.
The incoming air stream removes convectively or conductively heated air that would otherwise remain near the surface of the plastic sheath 9.

Only the airflow output of the evaporator 4 is used when operating the RAHP in air conditioning mode. Since the heat-driving potential of the absorber is smaller than that of the vapor compressor, the evaporator 4 must be made large in order to obtain a competitive dehumidifying performance. Evaporator fins 7
The density of the two arrays is typically 4.72 fins per cm (12 per inch). The spacing between the fins is somewhat larger than 1.6 mm (1/16 inch). As can be seen in FIG. 4, the evaporator fins 72 are also annular, but no vanes are needed here. To obtain satisfactory air-side heat transfer in the evaporator, a circular shroud (not shown), slightly spaced from the outer circumference of the evaporator, may surround the array of evaporator fins 72. A portion of the shroud is removed and replaced with a duct through which the exhaust airflow of the evaporator is directed as indicated by the arrow in FIG. The size of the duct is
Depends on desired air flow, cooling capacity 3515W (1 ton)
The airflow per hit is about 849.5 m ³ / h (about 500 SC
FM). For the shrouds and ducts thus described, the air flow in the duct is directly proportional to the volume of air contained between the fins of the annular array of sectors facing the duct times the rotational speed of the array, and It has been empirically and analytically confirmed that the ducts can be sized to provide a particular air flow at operating speeds.

The air flow to the absorber 1, the absorber cooler 5, the condenser 3 and the evaporator 4 enters the RAHP axially from the side of the absorber bearing shaft 31 and reaches the end plate 30 of the absorber. It passes through a radial opening 64, shown in section in FIG. As shown in FIG. 1, the air flow is directed by the radial openings 64 into the space surrounded by the air inlet 60 of the absorber and also the plastic sheath 9, the inner diameter of the evaporator 4 and the air barrier 57 of the evaporator. enter in. The airflow entering the absorber air inlet 60 and moving axially along the array of absorber fins 8 draws heat of absorption from the absorber tapered wall 7, thus maintaining the tapered wall at a particular temperature. , Thereby continuing the absorption process in a very thin moving membrane of absorbent on the inner surface of the absorber wall 7.

RAHP to Determine Machine Size and Feature
The components of the cycle are the absorber and the evaporator. Of course, the absorber has an even greater effect. As already mentioned, the absorber can be realized as a chemical catalytic reactor, which in the present invention removes the refrigerant vapor by means of a very thin moving membrane "d" of absorbent. When a thin film of absorbent enters the absorber 1 from the absorbent cooler 5, it does not contain a refrigerant and its temperature is sufficiently low that it actively draws refrigerant vapor.

The absorbed refrigerant vapor dilutes near the surface of the very thin film of the absorbent, and the heat of absorption raises the temperature near the surface. This temperature rise is eliminated by conduction through the thin film, the tapered wall 7 of the absorber and the fins 8 of the absorber,
It is then resolved by convection into the nearby airflow. The concentration gradient of the refrigerant within the absorbent film is overcome by the mass diffusion process. Neither the temperature diffusion process nor the mass diffusion process proceeds immediately, so in a real engineer system these are not completely done. However, the very thin membranes used in the present invention allow these processes to be performed with higher degrees of completeness than would normally be done.

Excluding the increase in absorption rate due to the addition of a uniform thin film, the absorption rate of the refrigerant vapor in the absorber of the present invention in the absence of non-condensable gas is given by the following equation:

[0065]

[Equation 1] Here, M = absorption rate C = system constant Ω = absorber constant D = absorber diffusion coefficient ρ = absorbent density μ = absorbent viscosity L = absorber length R = absorber average radius N = Rotation speed of the absorber θ = taper angle of the absorber wall.

The system constant C is an inverse function of the amount of absorbent processed divided by the absorption rate (that is, the pumping rate of the pitot tube pump 17). The absorbent throughput divided by the absorption rate is called the circulation ratio. A large circulation ratio means that the concentration of absorbent entering the generator and the concentration of absorbent leaving the generator are very different, and vice versa for small circulation ratios. For RAHP of the present invention using lithium bromide as the absorbent and water as the refrigerant, a circulation ratio of 8.3 is preferred, but a value of C of 7.60 to 1.14 is used. Values are possible. For other absorbent-refrigerant combinations, such as aqueous lithium bromide and aqueous lithium iodide solutions, where crystallization is less likely to occur, a circulation ratio of 7 or less is preferred.

The absorber constant Ω is a complex inverse function of completion efficiency. The preferred completion efficiency for the present invention is 92%, in which case the value of Ω is 0.9652, but the value of the completion efficiency is between 95% (Ω = 0.8674) and 90% (Ω
= 1.0185). Very high completion efficiency is R
Not accepted by AHP. For example, at a completion efficiency of 99.99%, the value of Ω is 0.3789, which severely compromises the capacity of the machine. High completion efficiencies are acceptable with chemical contactors.

The diffusion coefficient, density, and viscosity are properties of the absorbent that constitutes the thin film, and must be determined at a given thin film temperature and composition. When the temperature is 51.67 ⁰ C (125
For a lithium bromide absorbent at ⁰ F) with a concentration of 62% by weight, water is the diluent and 1/4 of the formula given above is used.
The value of the property in parentheses is 1.03 × 10 ^-3 g / cm ²
-S ^1/2 (2.11 × 10 ^-3 lbm / ft ² -s ^1/2 ), combined with the preferred dimensionless values C and Ω, the absorption rate per second in pounds is On the street.

M = 2.77 × 10 ⁻³ (L ³ R ⁵ N ² sin θ) ^1/4 Typically, N is 60 revolutions per second (377 radians per second).
And θ measured with respect to the rotation axis 51 is 4.25 °
(0.0742 radian), R is 101.6 mm
(4 inches) and L is 457.2 mm (18 inches)
Then the value of M is 1.74 g / s (3.84 g / s).
× 10 ^-3 pounds). For a typical net value for the enthalpy of 2231 J / g (960 BTU / lb) for vaporizing the water in the evaporator, the total cooling capacity provided by this flow rate is 3893 W (3.69 BTU / s), This is equivalent to 1.11 tons. The average thickness of the thin film “d” on the tapered wall 7 of the absorber is 0.0 in this example.
It is 46 mm (0.046 mil).

It is clear that a given value of M can be satisfied by choosing various combinations of L, R, N and θ. For example, select the rotation speed as 10,000 rpm (1047 radians per second) and
Is selected to be 457.2 mm (18 inches), and θ is 4.25.
If you select ° (0.0742 radians), R
Must be 67.56 mm (0.221 feet or 2.66 inches) for an absorption rate of 1.74 g / s (3.84 x 10 ^-3 pounds per second). The average thickness of the film "d" on the absorber tapered wall 7 is 0.031 mm (1.21 mils) at this relatively high speed. RAH
For P applications, the values of L, R, N, and θ are limited by actual design considerations. 100,000 rpm if the device is used purely as a chemical contactor
A rate of (10472 radians per second) or higher should be chosen, in which case liquids of high viscosity can be used in devices of small physical size.

The preferred ratio of average radius to absorber length (L / R) for stationary applications is about 3, while for mobile applications the preferred ratio is about 7. Stationary RA
HP is designed to enhance energy performance,
It is designed to operate at speeds below 2400 rpm (251 rad / s), but the mobile RAHP is designed to be large in size, at 3600 rpm (3 / s).
It operates at speeds above 77 radians). Examination of the absorption rate equation reveals that the absorption rate approaches zero as the theta sine approaches zero as the value of the absorber wall taper angle θ approaches zero. Therefore, it is desirable to make θ as large as possible unless it contradicts a good design. However, θ is 2
Do not exceed R / L. This is because when θ exceeds 2R / L, the absorbent cooler 5 is eliminated for a simple geometrical reason. When the value of L / R is 2, θ cannot exceed 45.0 ° (0.785 radians), and when L / R = 3, θ is 33.7 °.
(0.588 radians) cannot be exceeded and L / R
= 7, θ cannot exceed 15.9 ° (0.278 radians), and L / R = 10,
θ cannot exceed 11.3 ° (0.197 radians). The consequences of these limits on the capacity of RAHP are not as great. Because 1
At a minimum angle of 1.3 ° (0.197 radians), the machine capacity is 66.5% of the theoretical maximum capacity when the value of θ is 90 ° (1.571 radians). .
For the cited example with θ of 4.25 ° (0.0742 °), the machine capacity is 52.2% of theory.

The absorption rate equation necessarily includes a very thin film "d" thickness. The very thin film thickness "d" is inversely proportional to the square root of the absorber's rotational speed N, L
It is directly proportional to the value obtained by dividing the 1/4 power of the / R ratio by the sine of θ.
Therefore, when the value of θ is about 0.1 ° (1.745 × 10 ⁻³ radian), the thickness “d” of the thin film is
A value of L / R = 3 at an operating speed of 2400 rpm (251 radians per second) or less representing the state of AHP, and
Approximately 3600 rpm (3 per second
For a value of L / R = 7 at a rotation speed of 77 radians),
It is at least 0.127 mm (5 mils). 0.127 mm (5
Thin film thickness'd 'of mils or greater is not very thin when considered in the context of RAHP technology. θ is at the limit value,
When the rotation speed of the absorber is 3600 rpm (377 radians per second), for L / R = 2, θ = 45.0 °
(0.785 radians) and "d" is 0.021 mm
(0.84 mil) and for L / R = 3 θ = 3
3.7 ° (0.588 radians) and "d" is 0.
025 mm (0.99 mils) and for L / R = 4.5 θ = 24.0 ° (0.418 radians),
"D" is 0.030 mm (1.19 mil), L / R
For = 7, θ = 15.9 ° (0.278 radians)
And “d” is 0.037 mm (1.46 mils) and for L / R = 10 θ = 11.3 ° (0.19 mils)
7 radians) and "d" is 0.044 mm (1.74 mm).
Mil). If the speed of rotation of the absorber is 1200 rpm (125.7 radians per second), the value of "d" must be multiplied by 1.732, and the speed of rotation of the absorber is 1
At 0800 rpm (1031.0 radians per second), the value of "d" must be divided by 1.732. All values of "d" are given for absorbent / refrigerant systems using lithium bromide and water at concentrations and temperatures typical of RAHP.

In the present invention, since the evaporator is concentric with and coextensive with the absorber, the vapor generating function and the cooling function must be satisfied within the dimensional limits of the absorber. The greatest limitation is the vaporization of the liquid refrigerant in the condenser / evaporator tube 37 under the action of a very large centrifugal field. As disclosed in Applicant's US Pat. No. 5,123,479, evaporator heat transfer in a large force field occurs only where the liquid slicks the inner wall of the tube.

In the RAHP of the present invention, heat transfer is performed by convection, and about 50% of the internal volume is filled with the refrigerant,
63.050 W / cm ² (20,000 BTU / hr-ft ² )
The values for the tubes with the following heat flux are given by the following equations by the test:

N _Nu = 0.1891 (N _Gr N _Pr ) ^0.32 where N _Nu is the Nusselt number, N _Gr is the Grashof number, and N _Pr is the Prandtl number. These numbers are
The operating temperature liquid refrigerant, the inner diameter of the condenser / evaporator tube 37, and the centrifugal field in which the tube is placed are determined. Typically, for water refrigerants having a low body expansion coefficient at the operating temperature of the evaporator, the internal heat transfer coefficient is about 227 for static applications.
A ^{1W / m 20 C (400BTU /} hr-ft 20 F), Dynamic apply approximately 3691W / m ²⁰ C (650BTU /
hr−ft ² − ⁰ F). In this case, cooling capacity 3515W
The internal area of the evaporator tube required per (1 ton) is about 0.929 m ² (10 square feet) for static applications and about 0.557 m ² for dynamic applications.
(6 square feet).

The required internal area of the evaporator tube cannot be provided by using several very long tubes. Another requirement is that a proper cross-sectional area must be provided in the evaporator tube for the flow of refrigerant vapor. Since the evaporator tubes do not work without liquid refrigerant, the flow area of the evaporator must be accurately counted. When using water as the refrigerant, the preferred cross-sectional area for steam flow is about 38.7 per ton of capacity 3515W.
cm ² (6 square inches). Therefore, there is a prohibition against the use of very small diameter but long absorbers and the exact limits are contingent on the selected refrigerant and capacity of RAHP.

Similarly, absorbers of very large diameter but short are also excluded. This is because the tube header occupies a large area available for heat transfer. Therefore, the preferred L / R = 3 ratio for static applications and the preferred L / R = 7 ratio for dynamic applications are suitable for water refrigerants, but these ratios may vary somewhat for other refrigerants. And generally in the range of about 2 to about 10.

To maintain performance, it is important to minimize unwanted heat flow between the components and prevent the absorbent from mixing with the refrigerant. To minimize unwanted heat flow between the components, a plastic porous sheath in preventing the hot absorber 1 and absorbent cooler 5 from preheating the incoming air to the evaporator 4. Nine roles are disclosed. The generator's adiabatic barrier 21 is made of materials with low thermal conductivity, such as tetrafluoroethylene, chlorotrifluoroethylene, polyvinylidene fluoride, and polycarbonate, which are chemically inert and heat resistant. It is a material with excellent properties. In a variant, the insulation barrier 21 of the generator may be made of a composite material whose inner space consists of an outer shell filled with insulation.

The temperature spectra of the components of the present invention are shown in the order of decreasing temperature: generator, absorber cooler, condenser,
An absorber and an evaporator. The generator temperature should be 111.1 ⁰ C (200 ⁰ F) higher than the absorber, and the pressure in the generator should be 258.6 torr (5 ps) than the pressure in the absorber.
i) More expensive. Teflon (tetrafluoroethylene)
Is the preferred material for making the insulating barrier 21 of the generator. This is due to the low thermal conductivity of Teflon and its excellent mechanical properties at the expected operating temperature of the generator.

An adiabatic-packed absorbent transfer tube 20 conveys the hot absorbent from the generator 2 through the center of the absorbent 1 into the absorbent cooler 5. The absorbent transfer tube must isolate the absorber from generator pressure in addition to minimizing heat loss from the hot absorbent as it passes through the absorber. As shown in FIG. 5, the absorbent transfer pipe 20 is
It consists of an outer tube 20a and an inner tube 20c concentric with it, and the inner annular part is formed to contain several concentric layers of reflective metal foil 20b and is evacuated to a very high vacuum. ing.

The absorber cooler 5 operates below the temperature of the generator and slightly above the temperature of the condenser, but these three components all operate at the same internal pressure. Therefore, the absorber insulation barrier 26 is less stringent, but is subject to the same requirements as the generator insulation barrier 21, and materials such as polystyrene, polyethylene, and polyamide are suitable.

The vapor of the evaporator 4 passes through the evaporator exhaust pipe 44 and then the absorbent cooler 5. Evaporator vapor is 55.6 ⁰ C (1
It is a low temperature of ⁰⁰⁰⁰ F) or more. In order to prevent the vapor of the generator from condensing on the exhaust pipe 44 of the evaporator, the insulating sleeve 3
4 are installed as shown in FIGS.

[0083] evaporator 4, 55.6 ⁰ C than the condenser 3
As low as (100 ⁰ F) or more, heat flow from the condenser to the evaporator is minimized by providing isolation sections in the region of the isolation section holes 61, as shown in FIG. Insulation plug 3
Insert 9 into condenser / evaporator tube 37 and place in isolated section. The preferred material of construction for the insulation plug is Teflon, but other materials of construction are equally satisfactory.

Due to the negative pressure (suction pressure) exerted by the action of the fan of the condenser, the air separates the separating section from the separating section hole 61.
Passing inwardly into the condenser / evaporator tube 3
The wall temperature of 7 is reduced to reduce the heat flow from the condenser 3 to the evaporator 4 during this process.

The absorbent should not enter the condenser and evaporator. This is due to the increased operating temperatures of these components. The vapor pressure of absorbents such as lithium iodide lithium bromide, melting point 449 ⁰ C (840 ⁰ F) having a melting point of 550 ⁰ C (1022 ⁰ F) is very low in the normal operating temperature of the generator Therefore, carryover of vapor phase absorbent to the condenser can be ignored. Liquid absorbent carryover during normal operation is due to the refrigerant vapor inlet 35 and the refrigerant vapor inlet 35, which are well separated from the nominal level of absorbent in the absorbent cooler 5 and generator 2 as shown in FIGS. It is prohibited by the position of the outlet pipe 44 of the evaporator.

To prevent refrigerant from exiting the array of condenser / evaporator tubes 37 during shutdown, a check valve 82 closes the evaporator exhaust tube 44 during shutdown, as shown in FIG. . As shown in FIG. 6, the check valve 82 is held in a closed state by a leaf spring when no centrifugal force is present. As a result, the liquid level described above represents a predetermined amount of absorbent that has not been increased by mixing with the refrigerant at shutdown, and the positions of the refrigerant vapor inlet 35 and the evaporator exhaust pipe 44 are such that the RAHP is not rotating. It is widely separated from the asymmetrically placed absorbent.

Another result of the provision of the check valve 82 is that the liquid concentration process that creates the liquid refrigerant residue is R
It does not have to be repeated every AHP cycle. Furthermore, the response time for effective cooling after RAHP startup is greatly reduced. Due to the uncharacteristically low residual amount of liquid absorbent (which is an inherent property of very thin membranes used in absorbers and relatively thick membranes used in generators). The working dynamics of the RAHP device are similar to the VCHP device.

Operation Referring to FIGS. 1 and 2, FIG. 3 revealing certain details.
The operation of the present invention will be described with reference to FIGS. In particular,
Lithium bromide is selected as the absorbent and water is selected as the refrigerant, but other refrigerants and other absorbents that are deliquescent with respect to the refrigerant may be selected.

For example, bromide, iodide, and I of the periodic table.
The hydroxides of the Group a metals, alone or in combination, are RAH
A preferred group of candidates for use in P. Representative examples include lithium chloride, lithium chlorate, lithium iodide, sodium hydroxide, cesium fluoride, cesium hydroxide, potassium fluoride, potassium hydroxide, rubidium fluoride, and rubidium hydroxide. Calcium chloride, calcium bromide, calcium iodide, magnesium bromide, magnesium chloride and magnesium iodide may be used.

Other liquid refrigerants that can be used as solvents for the solid absorbent include liquid anhydrous ammonia, lower aliphatic alcohols such as methanol, ethanol, propanol, ethers such as diethyl ether, acetone, methyl ethyl ketone, and higher ketones. Ketones, esters such as ethyl acetate, hydrocarbons such as ligroin, benzene, and toluene, chlorinated hydrocarbons such as chloroform, alkanoic acids such as acetic acid and propionic acid, and alkylene glycols such as ethylene glycol and glycerol. is there.

Further, US Pat. No. 3,296,814,
U.S. Pat. No. 3,524,815 and U.S. Pat.
The new absorbent / refrigerant combinations described in 475,352 can be used. Particularly suitable as the absorbent solution is an aqueous solution of lithium bromide and lithium iodide, in which lithium iodide is in accordance with the teachings of US Pat. No. 3,524,815 about 3% of the total salt content. 30% by weight
To 40% by weight.

First, all air and other non-condensable gases are evacuated from the RAHP with a vacuum pump attached to the exhaust / charge opening 50 located in the absorber bearing shaft 31. A dilute solution consisting of a predetermined concentration of lithium bromide and gas-free water is then evacuated / charged, for example, as illustrated in FIG. 8 of US Pat. No. 3,740,966. Charge the machine through the opening 50. Next, the opening is hermetically sealed.

The machine is rotatably mounted on the external bearing 32 of the absorber and the external bearing 14 of the generator, and the rotational speed of the RAHP unit is set to, for example, 500 rpm depending on the size and nature of the equipment. Through 4000 rp
It is connected to a motor capable of m (52.4 radians per second to 418.9 radians per second). Annular nozzles 83 and 84 are provided to direct hot air into the fins 79 of the generator and to expel cooled air therefrom. As mentioned above, a sheet metal shroud is provided surrounding the condenser and evaporator components to collect and direct the condenser and evaporator effluent air.

The RAHP dimensional ratios shown in FIGS. 1 and 2 represent dimensional ratios for devices designed for static use (L / R = 3). For the examples cited herein, the rotational speed selected is 1200 rpm (125.7 radians per second). For passing through the external fin passage of the generator 2, 427 ⁰ C (8 tons per cooling capacity 3515 W (1 ton))
00 ⁰ F) at 68.0m ³ / h (40SCFM) to 160 ⁰ C
1359.2 m ³ / h at (320 ⁰ F) (800 SCFM)
The hot exhaust gas of is required. Do not count irreversible losses momentarily, and further, complete efficiency of the absorber by 92%
The heat input to the generator is defined by
6719W (22940BTU / hr) per (ton)
Is decided. The temperature of the thin film of absorbent at equilibrium is 13
It is 5 ⁰ C (275 ⁰ F), and the concentration of lithium bromide in the Pitot tube reservoir 55 is 66% by weight. The equilibrium water vapor pressure in the generator at this temperature and concentration is 230.6 torr (4.46 psia).

Capacity: 15.7 per 3515 W (1 ton)
8 g / s (125.3 pounds per hour) of diluted absorbent must be placed in the generator 2 at the peripheral lip 23.
66% by weight of absorbent 14.21 g / s (112.8 per hour
Absorbent transfer ring 2 from pitot tube reservoir 55 in pounds
It must be pumped to 0 by the Pitot tube pump 17. The mass flow difference between the input to the generator and the output from the generator is 1.58 g / s (12.5 lbs / hr) of refrigerant vapor, which is introduced into the passage to the condenser 3. The generator must exit through the provided refrigerant vapor inlet 35.
The actual temperature of the steam is 135 ⁰ C (275 ⁰ F), whereas the saturation temperature at a steam pressure of 230.6 torr (4.46 psia) is 69.7 ⁰ C (157.4 ⁰ C). F),
Thus, the vapor leaving the generator, 65.3 ⁰ C (117.
6 ⁰ F) only being overheated, which only energy contained in an amount superheated steam 5.67kg (12.5 lbs) of ^{the, 7.2 × 10 5 J (684BTU} ), i.e., the condensation heat It is about 5.5%. By applying heat to the generator 2, the incoming diluted absorbent is separated into a concentrated absorbent fraction and a refrigerant vapor fraction.

The refrigerant vapor fraction enters the condenser 3 through the refrigerant vapor pipe 67, the cross connection pipe 36, and the condenser header 40. Machine capacity through the outside of the condenser fins 3
Approximately 1529 m ³ / h (900 SC per 515 W (1 ton)
An FM flow of air removes 200 W (684 BTU / hr) of superheat and 3675 W (12546 BTU / hr) of condensation heat from 5.67 kg / h (12.5 lb / hr) of superheated steam, removing refrigerant during the process. 69.7 ⁰ C (157.
4 liquefied at its saturation temperature of ⁰ F).

Due to the large centrifugal forces acting on the position of the condenser 3 during operation, a very large condensation coefficient is obtained in the condenser part of the condenser / evaporator tube 37. This is because the thin film of liquid deposited as a result of condensation and large centrifugal forces is extremely thin. A small amount of liquid refrigerant "e" is retained within the condenser portion of the condenser / evaporator tube 37. This is condenser 3
The internal pressure is more than 206.8 torr (4 psi) higher than the internal pressure of the evaporator 4, and the liquid trap 38 and the evaporator portion of the condenser / evaporator tube 37 (see liquid level "b" in FIGS. 1 and 4). It is designed to occupy up to about 50% of its volume with liquid (as indicated by ".") Under this condition, the pressure difference between condenser 3 and evaporator 4 is completely compensated. It The drainage of the condenser is performed by the liquid trap 38. This is because the liquid trap acts as a siphon during machine operation.

The liquid refrigerant is 5.67 kg / h (12.5 per hour
Enter the evaporator 4 at a speed of lbs. The liquid refrigerant evaporates at a temperature determined by the vapor pressure determined by the performance of the absorber. In the case of the illustrated apparatus, the vapor pressure is 11.4 torr (0.22psia), the temperature of the evaporator is 13.3 ⁰ C
A (56 ⁰ F), capacity for evaporator air flow at large thermal factor ^{0.76 917.5m 3 / h (540SCFM)} , a 3515W (1 tons), the air flow, the evaporator As in the case of the flow rate of the refrigerant to, the larger the capacity, the larger the capacity.

Returning to the generator, the condensed absorbent fraction is collected in the Pitot tube reservoir 55 to a liquid level "C", as shown in FIG. The absorbent fraction is pumped from this position into the absorbent transfer pipe 20 by the pitot pipe pump 17. The absorbent transfer tube 20 has a relatively large inner diameter to prevent crystallization from occurring during the transition of operating conditions. The absorbent transfer pipe 20 can pass the superheated refrigerant vapor into the absorbent cooler 5. The concentrated absorbent fraction accumulates in the absorbent cooler 5 up to the liquid level "a" shown in FIG.
The liquid level "a" is variable. This is because the value obtained by adding the pressure drop through the decompression slot 33 to the total hydrostatic head of the concentrated absorbent for the decompression slot 33 increased by the centrifugal force is between the vapor pressure of the generator and the vapor pressure of the absorber. The difference between
That is, 219.2 torr (4.46-0.22 = 4.24).
psi)). In the absorbent cooler 5, the free surface of the concentrated absorbent cut indicated by the liquid level “a” is the free surface at 135 ⁰ C (275 ⁰ F). Concentrated liquid absorbent has a low thermal conductivity, so its temperature near the cooled tapered wall 7 of the absorber is about 7
1.1 a ⁰ C (160 ⁰ F). This temperature difference is acceptable because relatively cool fluids and thus relatively dense fluids naturally move away radially during machine rotation.

The presence of a liquid residue, which is indicated by the liquid level "a", the variable liquid level and the presence of the temperature gradient mentioned above, characterize the design of the absorber cooler, which is the absorption Protects the generator from generator pressure and temperature transients. The absorbent cooler is 51.17 kg (112.
8 lbs. Of concentrated absorbent at 135 ⁰ C (2
75 ⁰ F) down to about 71.1 ⁰ C (160 ⁰ F), releasing 5.8 × 10 ⁶ J (5540 BTU) of thermal energy during this process. This heat energy comes in at about 1359 m ³ / h (800 SCFM) through the portion of the tapered wall 7 of the absorber located in the absorber cooler 5 and the array of absorber fins 8 near this portion. Conducts heat to the absorber cooling air. Heat driven potentials above 36.1 ⁰ C (65 ⁰ F) are required to transfer heat from the absorbent in the absorber cooler 5 to the incoming air stream initially at 35 ⁰ C (95 ⁰ F). More than enough.

Liquid level “a” to absorber tapered wall 7
The concentrated liquid absorbent moving toward creates a flow gradient in the direction of the vacuum slots 33 located around the insulating barrier 26 of the absorber. The adiabatic barrier 26 of the absorber is the third
The axial position is fixed by the transition pipe flange 27 and the second transition pipe flange 25. Thus, at operating temperatures, expansion of the absorber insulation barrier 26 closes the normal assembly gap around this insulation barrier. Therefore, absorbent flow can only pass through the array of vacuum slots 33. In this way, a uniform series of thin films of concentrated absorbent enters the absorber 1 and immediately spreads to form a single uniform very thin film.

66% by weight of absorbent is about 71.1 ⁰ C (160 ⁰ F) as it enters the absorber. The equilibrium vapor pressure of 66% lithium bromide at 71.1 ⁰ C (160 ⁰ F) is
12.56 Torr (0.243 psia), 58.7 surface% lithium bromide, 51.7 ⁰ C (125 ⁰ F)
The vapor pressure of the absorber (92% complete) at 11.4 torr (0.22 psia). Thus, when the concentrated absorbent enters the absorber, there will be some slight evaporation of refrigerant from the absorbent until the temperature of the absorbent equilibrates.

When the concentrated absorbent absorbs vapor, 1.7 × 10 ⁷ J (16 tons) per cooling capacity 3515 W (1 ton).
170 BTU) of energy is released. With the selected taper angle of 4.25 ° (0.0742 radians),
At a rotation speed of 1200 rpm (125.7 radians per second), the vapor is absorbed by a 0.074 mm (0.0029 inch) thick film "d". This very thin membrane travels from the absorber adiabatic barrier 26 of the absorber to the adiabatic barrier 21 of the generator at an average surface velocity of 121.9 mm / s (0.40 feet per second) on the inner surface of the absorber tapered wall 7. During this rapid transit, the very thin membrane must absorb 1.58 g / s (12.5 lbs / hr) of very low pressure refrigerant vapor, and 4736 W (16170 BT) from the very thin membrane.
The heat of U) must be released. Vapor is absorbed through a process called mass diffusion and heat is given off in a process called thermal diffusion. Both of these processes are unacceptably slow, especially for viscous liquids with very low thermal conductivity. The actual size of the absorber of the present invention is made possible only by using very thin membranes which advantageously limit the distance over which mass and heat must be spread.

The function of the absorber is the same as the function of the generator. The influent to the generator is the diluted liquid absorbent and the effluent from the generator is the concentrated liquid absorbent and pressurized refrigerant vapor. The influent to the absorber is the concentrated liquid absorbent and the low pressure refrigerant vapor, and the effluent is the diluted liquid absorbent. The heat is continuously removed by the driving stimulus.

In the absorber, as the very thin film moves from the absorber cooler 5 to the generator 2, the concentration of the absorber becomes 66.
The concentration varies from wt% to 59.5 wt%,
In the generator, as the relatively thick membrane travels from the peripheral lip 23 to the Pitot tube reservoir 55, the concentration of absorbent is 5%.
The average concentration rises from 9.5% by weight to 66% by weight.

As a result, in the absorber, the concentration and temperature of the absorber thin film decreases as the film moves from the absorber cooler toward the generator along the tapered wall 7 of the absorber. In the generator, as the thin film moves axially from the peripheral lip 23 toward the Pitot tube reservoir 55, the concentration and temperature of the thin film of absorbent increases. In both the absorber and the generator, the surface concentration of the absorbent thin film and its surface temperature must be in equilibrium with vapor pressure at any axial position. Therefore, as the concentration decreases, so does the temperature of the absorbent. The reverse is also true.

Absorbent at a temperature of about 125. ⁰ C (125 ⁰ F) and a concentration of 59.5% by weight leaves the absorber through the array of annular passages 52, radial slots 53 and leaves the film forming ambient. The generator is entered through the array of slots 54. The equilibrium vapor pressure of the mixed absorbent at the above-mentioned temperature and concentration is 10.
38 torr (0.201 psia). The mixed absorbent is
Must be preheated before exposure to high vapor pressure at the generator. If not, the vapor is condensed and further diluted. Preheating dilution absorber shell 11, which is superheated in the generator in combination with the thickness of the thin film of the absorbent in the circumferential slot 54, the temperature of 51.7 ⁰ C of absorber (125
⁰ F) from 71.7 ⁰ C (to allow thermal diffusion process which operates to raise up to 160 ⁰ F) saturation temperature or more, circumferential slot which is extended by a peripheral lip 23 to a predetermined axial length This is done by passing the absorbent through 54.

Absorbent mass flow rate for a given size of Pitot tube orifice 15 (as described above,
This determines the system constant C in combination with the absorption rate M), which is determined by the RAHP rotation rate and the Pitot tube pump 17
Determined by the difference between the rotation speed of the. In one extreme case, the Pitot tube weight 16 keeps the Pitot tube pump 17 stationary on the Pitot tube bearing 18 during rotation of the RAHP. This is the maximum mass flow condition. When the rotation speed of the pitot arm extension 49 is the same as the rotation speed of RAHP, the mass flow rate of the absorbent is zero. If the absorbent mass flow rate is zero, the machine capacity is also zero.

The rotational speed of the Pitot tube pump 17 is RAHP.
It can be shown that the mass flow rate of the sorbent is also zero when it is 50% of the rotation speed of, and both are rotating in the same direction. Therefore, the mass flow rate of the absorbent and the associated machine capacity can be controlled by controlling the torque exerted on the pitot arm extension 49. In the state described in this description of operation, the Pitot tube pump is 51.17 kg / h (112.17 h / hr) of absorbent for every 3515 W (1 ton) capacity of the machine.
It must provide a mass flow rate of 8 pounds. The true circulation ratio is 112.8 / 12.5 = 9.0, which is
A preferred value of 8.3 corrected for 92% completion efficiency, or 8.3 / 0.92 = 9.0.

The coefficient of operation in the cooling mode is the ratio of the heat input to the evaporator divided by the heat input to the generator, which is 12000 BTU / hr: 22940 for the above operation.
BTU / hr = 0.523. The coefficient of operation in heating mode is the ratio of the heat input to the absorber, the absorber cooler, and the condenser, all divided by the heat input to the generator, which is 161
70 BTU / hr + 5540 BTU / hr + 13230BT
U / hr: 22940 BTU / hr = 1.523. For the disclosed RAHP design, decreasing the circulation ratio increases the coefficient of performance in both cooling and heating modes.

The residual amount of the absorbent contained in the thin films of the absorber and the generator is 113.35 / W (1 ton).
It weighs less than or equal to 0.25 pounds. This is the minimum residual amount of lithium bromide absorbent needed to drive the absorption cycle described above. Therefore, absorbents that are too expensive for use in conventional absorption systems can be treated with RAH as described herein.
It can be applied to P devices.

The embodiment described above is a special case of the general class of rotary absorption heat pumps for use in stationary, portable and mobile applications.
Obviously, this class of heat pump can be applied in a sealed and unitized construction which is very advantageous during the manufacture, sale and installation of this appliance. However, if found to be advantageous, cooling of the absorber or condenser, or both absorber and condenser, may be left to separate parts of the appliance in a manner similar to current residential separate heat pumps. Good. Furthermore, it has been considered necessary to identify their existence for clarity. The present invention, except as limited by the claims below, describes a method for heating a generator, an absorbent and a refrigerant used, a method for rotating a machine, a method for creating a liquid trap between a condenser and an evaporator, circulation. There is no limitation on the method of controlling the ratio, selection of constituent materials, and the like.

[Brief description of drawings]

FIG. 1 shows the internal structure of one embodiment of RAHP of the present invention.
It is a longitudinal direction sectional view shown together.

FIG. 2 shows the internal structure of one embodiment of RAHP of the present invention.
It is a longitudinal direction sectional view shown together.

3 is a lateral cross-sectional view taken along the line 2-2 of FIG.

4 is a lateral cross-sectional view taken along line 3-3 of FIG.

5 is a detailed cross-sectional view taken along the line 3A-3A in FIG.

6 is a cross-sectional view taken along line 4-4 of FIG.

7 is a lateral cross-sectional view taken along line 5-5 of FIG.

FIG. 8 is an enlarged partial sectional view of FIG.

[Explanation of symbols]

 1 Absorber 2 Generator 3 Condenser 4 Evaporator 5 Absorbent cooler

Claims (17)

[Claims] 1. A generator (2), a condenser (3), an evaporator (4), an absorbent cooler (5), and an absorber (1) having an inflow end and an outflow end, which absorbs these. An absorber (1) having means operatively associated to function as a component of the mold heat pump, and further having mounting means for mounting the component of the heat pump to rotate as a unit. Is a round truncated cone of circular right circular cone tapering outwards in the downstream direction adapted to accept and process the absorbent solution in the form of a very thin membrane ("d") of approximately constant thickness. The absorber (1), the absorbent cooler (5), and the generator (2) are arranged concentrically with their ends facing each other, and the condenser (3) And said evaporator (4)
A rotary absorption heat pump assembly disposed end-to-end on an outer circumferential side of the absorber and the absorber cooler and being substantially concentric with the absorber and the absorber cooler. 2. The taper angle of the absorber measured with respect to the axis of rotation (51) of the absorber is about 0.1 ° (0.0
2. The heat pump assembly of claim 1, wherein the angle is between 0,175 radians) and less than or equal to the arc tangent of twice the average radius of the absorber divided by its axial length. 3. The taper angle of the absorber measured about the axis of rotation (51) of the absorber is about 2.0 ° (0.0
The heat pump assembly of claim 1, wherein the heat pump assembly is at an angle of 349 radians) to 7.0 degrees (0.1222 radians). 4. A very thin film thickness (“d”) of about 0.
0127 mm (0.5 mil) to about 0.1270 (5.0
A heat pump assembly according to claim 1, which is a mil). 5. A very thin film thickness ("d") of about 0.
0127 mm (0.5 mil) to about 0.1270 (5.0
Mil), the taper angle measured with respect to the axis of rotation of the absorber is between about 2.0 ° (0.0349 radians) and 7.0 ° (0.1222 radians), and the conical absorber ( The heat pump assembly according to claim 1, wherein the ratio of the length of 1) to the average radius is from about 2 to about 10. 6. The absorber (1) and the generator (2).
Are arranged in an end-to-end butt relationship, the inflow end of the absorber is closed by a first isolation / insulation barrier, the outflow end is closed by a second isolation / insulation barrier, and the first barrier is Wherein a plurality of peripheral openings (33) are provided in juxtaposed relation with the inner wall of the absorber for supplying the absorbent solution to the inner wall (7) of the absorber in a thin film forming relationship. Item 2. The heat pump assembly according to item 1. 7. The absorber (1) and the generator (2).
Are arranged in end-to-end butt relationship, the inflow end of the absorber is closed by a first isolation / insulation barrier, the outflow end is closed by a second isolation / insulation barrier, and the first isolation is / The insulating barrier is provided with a plurality of peripheral openings (33) in juxtaposed relationship with the inner wall of the absorber for supplying the absorbent solution to the inner wall (7) of the absorber in a film forming relationship. And a downstream second isolation / insulation barrier is provided with a plurality of peripheral openings (54) configured to deliver the absorbent solution in the form of a thin film to the inner peripheral surface of the generator (2). The heat pump assembly of claim 1, wherein: 8. The condenser (3) and the evaporator (4)
Comprises a plurality of elongated tubes (37) in combination with liquid trap means (38) and adiabatic plug means (39) dividing the interior of each tube into said condenser section (3) and supply section (4). The heat pump assembly according to claim 1. 9. The tapered inner surface (7) of the absorber (1) is provided with a plurality of longitudinally extending partitions or baffles (85), which are circumferentially spaced, A heat pump assembly according to claim 1, wherein the inner surface is divided into separate areas that are not in communication with each other to maintain a very thin membrane ("d") thickness uniformity during operation of the assembly. Three-dimensional. 10. The heat pump assembly of claim 9, wherein the thickness of the baffle or septum (85) is about twice the thickness of the thin film (“d”). 11. The heat pump assembly of claim 1 including a variable displacement pump for transferring a concentrated absorbent solution from the generator (2) to the absorbent cooler (5). 12. The pump means is a Pitot tube means (1).
The heat pump assembly according to claim 11, comprising 7). 13. A non-return valve means (82) operative to prevent refrigerant from flowing from the evaporator to the absorber during shutdown of the assembly, the evaporator (4) and the absorber (1). The heat pump assembly according to claim 1, wherein the heat pump assembly is installed between the heat pump assembly and the heat pump assembly. 14. The heat pump assembly according to claim 13, wherein the check valve means (82) comprises valve means that opens under the action of centrifugal force and closes under the pressure of a spring. 15. An adsorbent / refrigerant charge is included,
During operation of the assembly, the charge is loaded into the generator component, condenser component, evaporator component, absorbent solution cooler component, and absorber component of the assembly in working quantities. 3. The method of claim 1, wherein the charge is predetermined to maintain the charge.
The heat pump assembly according to. 16. The rotary heat pump assembly of claim 15, wherein the charge comprises lithium bromide and water. 17. The charge comprises a crystalline resistant mixture of lithium bromide, lithium iodide, and water, wherein the lithium iodide is from about 30 wt% to about 30% by weight of the total salt content of the charge. Four
16. The rotary heat pump assembly of claim 15, which comprises 0% by weight.