Experimental System of Solar Adsorption Refrigeration with Concentrated Collector

Z.X. Yuan; Y.X. Li; C.X. Du

doi:10.3791/55925

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Experimental System of Solar Adsorption Refrigeration with Concentrated Collector

Published: October 18, 2017

doi:

10.3791/55925

Z.X. Yuan¹, Y.X. Li¹, C.X. Du¹

¹College of Environmental and Energy Engineering,Beijing University of Technology

Summary

With solar energy as the driving force, a novel adsorption refrigeration system has been developed and experimentally investigated. Water vapor and zeolite formed the working pair of the adsorption system. This manuscript describes the setup of the experimental rig, the operation procedure, and the important results.

Abstract

To improve the performance of solar adsorption refrigeration, an experimental system with a solar concentration collector was set up and investigated. The main components of the system were the adsorbent bed, the condenser, the evaporator, the cooling sub-system, and the solar collector. In the first step of the experiment, the vapor-saturated bed was heated by the solar radiation under closed conditions, which caused the bed temperature and pressure to increase. When the bed pressure became high enough, the bed was switched to connect to the condenser, thus water vapor flowed continually from the bed to the condenser to be liquefied. Next, the bed needed to cool down after the desorption. In the solar-shielded condition, achieved by aluminum foil, the circulating water loop was opened to the bed. With the water continually circulating in the bed, the stored heat in the bed was took out and the bed pressure decreased accordingly. When the bed pressure dropped below the saturation pressure at the evaporation temperature, the valve to the evaporator was opened. A mass of water vapor rushed into the bed and was adsorbed by the zeolite material. With the massive vaporization of the water in the evaporator, the refrigeration effect was generated finally. The experimental result has revealed that both the COP (coefficient of the performance of the system) and the SCP (specific cooling power of the system) of the SAPO-34 zeolite was greater than that of the ZSM-5 zeolite, no matter whether the adsorption time was longer or shorter. The system of the SAPO-34 zeolite generated a maximum COP of 0.169.

Introduction

With the ozone-depletion problem of traditional vapor compressed refrigeration growing more serious, substituting traditional refrigeration with green technology has become a hot topic in recent years. Among those green technologies, the solar adsorption refrigeration has attracted much of the attention of researchers. Driven by low-grade thermal energy, the adsorption refrigeration system has the advantages of being environmentally friendly, small, and flexible. This adsorption system can also be driven with non-solar energy, for instance by waste heat discharged from thermal equipment or by engine exhaust gases from vehicles, as mentioned by Hu et al.¹

In an adsorption cooling system, the adsorption bed is the key component. Its work directly affects the performance of the whole system. Therefore, the design of the adsorption bed is the most important issue as pointed out by Sutuki.² A decade ago, the flat bed was mostly used in the adsorption cooling system.³^,⁴^,⁵ Without any solar concentrating device, the flat bed temperature was usually low and hence the COP of the system was unsatisfactory. In contrast, the tubular adsorption bed improved the COP. It was reported that the COP could reach 0.21 in sub-Sahara region by Hadj Ammar et al.⁶ Furthermore, Wang et al.⁷ developed a spiral plate adsorber that was distinguished by the characteristic of continuous heat regeneration. The novel design of the adsorption bed shortened the cycle time of the system. Abu-Hamdeh et al.⁸ reported their study on the solar adsorption refrigeration system with a parabolic trough collector. Their test results showed the COP of the system varied from 0.18 to 0.20. El Fadar et al.⁹ studied an adsorption refrigeration system that was coupled with a heat pipe and powered by parabolic trough collector, which showed an optimum COP of 0.18.

To enhance the heat transfer of the tubular bed, some finned tube adsorbers were considered and the effect of the enhancement was examined. An innovative bed that took the form of the shell and tube heat exchanger was presented by Restuccia et al.¹⁰. The internal finned tube was coated with a zeolite layer so that the contact transfer resistance of heat/mass between the metal surface and the adsorbent material could be reduced. The system produced an output of 30-60 W/kg of specific cooling power in the cycling time of 15-20 s. Al Mers et al.¹¹demonstrated that the enhanced adsorber with 5-6 fins could significantly reduce the heat loss of the adsorber to ambiance and thereby improving the COP by 45%. The effect of a finned tube adsorber on the performance of the solar driven system was also studied by Louajari et al.¹². Using activated carbon-ammonia as the working pair, they showed that the cycling mass transfer in the adsorber with fins was greater than the one without fins.

In the current study, we experimentally studied an improved solar adsorption refrigeration system, in which a solar tracking parabolic trough collector was applied and an internal cooling tunnel was deployed. With the SAPO-34/ZSM-5 zeolite and the water vapor as the working pair, the system showed interesting characteristics in terms of thermodynamics and refrigeration. The experimental methodology as well as the typical test results will be presented and discussed in this report.

Protocol

1. Experimental Setup

NOTE: The adsorption refrigeration system was composed of the adsorption bed, the evaporator, the condenser, the vacuum pump, and the solar trough collector (Figure 1). An automatic solar tracking device with a parabolic trough was manufactured and applied in the system to improve the efficiency of the solar collector. The automatic solar tracking trough was driven by the worm-gear device as shown in Figure 2. The device consisted of the stepper motor, the worm, the gear, the moving limit block, and the manual wheel. The dimensions of the worm-gear device were 21 x 80 cm². The trough collector concentrated the solar rays onto the adsorbent bed, which was located along the focus line of the parabolic trough.

Figure 1: Experimental system for solar adsorption refrigeration. (Top) Schematic of the system; (bottom) Photograph of the experimental setup. The top panel presents the components of the experimental system, which involves the evaporator, the condenser, the vacuum pump, etc. The bottom panel displays the photograph of the assembled adsorption refrigeration system. In the system, the evaporator and the condenser is of the fin-tube structure, a kind of compact heat exchanger. The adsorption bed is reformed from a vacuum solar collector, which can capture solar energy effectively. Please click here to view a larger version of this figure.

Figure 2: The structure of the worm gear box. The worm gear box is the device that transforms the rotation of the stepper motor into the solar tracking movement of the parabolic trough. In addition to the stepper motor, the worm gear box also involves the reducer, the manual wheel, the worm shaft, etc. Pulling the manual/automatic switch handle to the left, gears 5a and 5b are disengaged. Thus, the trough can be manually controlled by rotating the hand wheel. Pulling the manual/automatic switch handle to the right, gears 5a and 5b are engaged together. Thus, it is controlled automatically by the stepper motor.

Connect the tracking solar collector to the worm-wheel shaft by a welding method. Pass the rotation of the stepper motor to the solar collector by matching the gear and the worm. Fix the tubular adsorption bed together with the collector with a pair of pipe collars.
NOTE: Driven by the stepper motor, the system rotates daily from the east to the west to follow the solar movement automatically.
Adjust the tilting angle of the trough to ground level, according to the variation of the solar altitude in different seasons. Determine the tilting angle β of the trough by the local latitude Φ and the solar declination δ, and the formula β = Φ - δ. Manually rotate the little wheel that is located at the bottom of the angle adjustment lever to regulate the tilting angle of the trough (the part of No. 13, Figure 1).
NOTE: In this way, the solar radiation is as normal as possible on the trough. The experimental system was located in the campus of Beijing University of Technology, at the latitude 39.89 °N and longitude 116.38 °E. The adsorption bed took a cylindrical form. It was reformed from a vacuum solar receiver of a tube (Figure 3).

Figure 3: Structure of the adsorption bed and the deployment of the temperature probe. (Top) Schematic of the bed structure; (bottom) The temperature probes and the mass transfer channel in the bed. The top panel shows the basic structure of the bed. The adsorbent material is put into the annular cavity between the solar-absorbing tube and the copper cooling channel. The solar rays penetrate the glass tube and fall onto the surface of the solar-absorbing tube. Then, by heat conduction, the solar energy is transferred to the adsorbent material inside the bed. The bottom panel shows the location of the temperature probes. These probes are used to monitor the temperature change of the bed during the adsorption/desorption process. Please click here to view a larger version of this figure.

To promote the capture of the solar energy, coat the solar-absorbing tube of the bed, (made of stainless steel with d = 64.5 mm) with a layer of black chrome deposit by the vacuum coating method. Please refer to the previously published literature about selective coating for more information about this technique¹³. Ensure that the solar absorption rate of the coating layer is 0.95, the infrared emissivity is 0.15, and the thickness of the coating layer is 0.08 mm.
NOTE: This coating layer helps to catch the solar radiation effectively but emits very slightly itself. As a result, the solar energy gets into the adsorption bed easily and is transformed to thermal enthalpy of the adsorbent effectively.
Insert a copper tube (d = 20 mm) along the axis of the adsorption bed. Fix the copper tube to the bed with the flange (see Figure 3, top panel). The copper tube functions as the cooling channel of the bed during the adsorption process.
Fill the adsorbent material in the annular cavity in the bed that is formed by the bed tube and the copper cooling channel. Use SAPO-34 zeolite as the adsorbent material, and water as the refrigerant. Put 3.171 kg of the SAPO-34 zeolite into the bed. The granular SAPO-34 zeolite is 5.7 mm in diameter.
Deploy nine temperature probes in three cross-sections of the bed to monitor the temperature change of the bed during the adsorption/desorption process (Figure 3, bottom panel). Fix a probe at each small supporter that is seated on the copper cooling channel.
Put probes 1 and 2 in section A-A near the inlet of the adsorption bed. Put probes 8 and 9 near the dead end of the bed. Fix the other probes at the middle B-B section (see Figure 3).
Insert axially a mass-transferring channel of d = 10 mm into the bed. Ensure that the mass channel has the form of reticular tube, and is the same length of the adsorption bed (d_bed = 64.5 mm). Extend the channel downwards from the inlet and make it stand in the right position with the extrusion force of the adsorbent material. The reticular tube helps the water vapor to enter the deep region of the bed quickly.

2. Experimental Method

NOTE: Adsorption refrigeration is based on the principle that the solid adsorbent material adsorbs the refrigerant vapor strongly at low temperature, while it desorbs the vapor at a higher temperature. Using heat as the driving impetus, the purpose of refrigeration is reached. The refrigeration cycle of the adsorption system involves mainly four steps, i.e., the solar heating-up process, the desorption process, the bed-cooling process, and the adsorption process. The desorption process starts once again after the adsorption process is completed. All the steps of the experiment are equally important because they are interrelated and influence each other interactively.

Regulate the experimental setup by the following procedures to start the solar heating and desorption of the bed.
1. Turn the parabolic trough manually until it is facing due east before the experiment, so that the sunlight irradiates the parabolic trough collector normally at noon.
2. Shut off all the valves that are connected to the adsorption bed and ensure the pressure of the bed and the pipe is below 800 Pa. Make it ready for solar heating.
3. Switch on the controlling rig of the system when the sun light is parallel to the horizon line in the morning. Make the trough automatically rotate to trace the solar movement.
4. Allow the adsorption-saturated bed to be heated by solar radiation under closed conditions. As a result, the bed temperature and the bed pressure will increase gradually.
5. Monitor the bed pressure with the pressure gauge (Number 6 in Figure 1) until it is higher than the pressure value that corresponds to the condensation temperature of the environment. According to the thermodynamics, the condensation pressure of the water at 30 °C is 4,246 Pa.
Start the desorption process.
NOTE: In the desorption process, the condensation of water vapor occurs. The condensation temperature is determined by local weather conditions on the test day.
1. Open the valve that connects the bed and the condenser. Let water vapor flow into the condenser through the connecting pipe. As water vapor enters the condenser, the temperature of the condenser will rise gradually.
2. At the same time, keep the solar heating to the adsorption bed, so that the bed pressure remains high enough to cause the desorption. Do not stop the solar heating until the process is completed.
3. End the desorption process when the pressure of the bed is equal to the pressure of the condenser. Turn off the valve when the desorption process is over.
Cool down the bed before the adsorption process, as the bed is still in the state of high temperature after the desorption. The adsorbent material can largely adsorb only at low temperature.
1. To start the adsorption process, shield the adsorption bed with an aluminum foil sheet, so that the bed is cut off from the solar radiation.
2. Close all the valves that connect the evaporator and the condenser.
3. Open the circulating water-loop of the bed and cool down the adsorbent material. With the water continually circulating in the bed, the internal enthalpy is taken out and the bed pressure decreases correspondingly.
4. End the cooling process when the bed pressure drops below the saturated vapor pressure at the evaporator's temperature.
  NOTE: Be ready for the adsorption refrigeration process after the cooling down of the bed. Now the bed temperature is around the ambient air temperature, and the bed pressure has reached to the minimum level.
5. Keep the circulating water-loop in a working state during the adsorption process. The adsorption is an exothermic process, and the generated heat needs to be discharged outside as soon as possible.
6. Open the valve between the bed and the evaporator. Let the water vapor rush into the bed from the evaporator.
  NOTE: The vapor reduction of the evaporator causes more water to vaporize, which results in the drastic decrease of the evaporator temperature. Consequentially, the evaporator absorbs heat from the water tank where the evaporator is seated, and a refrigeration effect is obtained.
7. Keep the adsorption process going on, and record the change of the bed temperature and the bed pressure.
  NOTE: During the adsorption process, the vapor pressure in the evaporator becomes lower and lower, but the bed temperature increases quickly.
8. End the adsorption process when the bed pressure is equal to the evaporator pressure. Afterwards, the desorption process will follow again.

3. Data Reduction Method

Evaluate the performance of the refrigeration system based on the refrigeration capacity and the efficiency of the heat-to-cold transformation.
NOTE: For the current system, the refrigeration capacity is calculated by the mass amount of the vaporized water and the temperature change of the evaporator itself.
1. To determine the total refrigeration capacity (Q_ref) of the system, calculate the sum of the enthalpy decrement of the chilled water in the tank, the metal evaporator, and the residual water in the evaporator after the adsorption as follows:
  
  where c_p de Eq. (1) is the specific heat at constant pressure, and m denotes the mass. C is a correction factor to the refrigeration capacity of the evaporator considering the heat transfer between the water tank and the ambient environment, and it is assumed C = 1.15 according to the principle of heat transfer. The subscript w and e represents the water and the evaporator, respectively. In the equation m_w,tan and m_w,ev_a is the mass of the chilled water in the tank and the mass of the residual water in the evaporator, which corresponds to the temperature drop ΔT_w and ΔT_e, respectively.
  NOTE: The solar energy input to the bed is needed to evaluate the efficiency of the heat-to-cold transformation.
2. Determine the solar energy input Q_s as:
  
  where, I_s,i(t) is the transient solar intensity recorded by the actinometer during the desorption process. The time interval Δt of the data acquisition to the I_s,i(t) is 10 s. The aperture area of the parabolic trough A_p, the reflective efficiency of the trough surface ρ, the transmittance of the tube glass τ, and the solar absorption coefficient of the coating surface α, together with the parameters in Eq. (1), are all listed in Table 1.
3. Based on the Q_refand the_Q_s obtained above, determine the COP of the refrigeration system as¹⁴:
  
  β1 and β₂ are correction factors to the solar energy input Q_s. β₁ is the correction factor of the non-parabolic degree of the trough, which takes into account the deformation of the trough because of the limitations of the manufacturing technique, and it is assumed β₁ = 0.85. β₂ is the correction factor of the real amount of obtained heat of the bed. Due to the smaller size of the metal bed tube than the outer glass tube, the real obtained heat amount is less than that reflected onto the glass tube. β₂ is decided by the ratio of the metal bed diameter D₂ to the glass tube diameter D₁. With D₁ = 100 mm and D₂ = 64.5 mm, it is calculated that β₂ = 0.645.
4. Determine the specific cooling power of the bed by the parameters of the experiment as¹⁴:
  
  where m_a is the mass of the adsorbent material and t_ads is the time duration of the adsorption process.

Table 1: Values of the parameter in Eq. (1) and Eq. (2). The parameters that are involved in Eq. (1) and Eq. (2) are listed in this table. The parameters include c_p, A_p,α, etc.

Representative Results

Mass transfer characteristic of the bed through the adsorption process
The adsorption bed is always the most important component in an adsorption refrigeration system, and the heat and mass transfer characteristic are the main factors affecting the performance of the whole system. By analyzing the recorded temperature change in the cross sections as shown in Figure 3(bottom panel), it is possible to know the heat and mass transfer features of the bed. Figure 4 shows the dynamic change of the bed temperature during the adsorption process. The figure illustrates that the mass transfer ability of the SAPO-34 zeolite is good, for the adsorption of the points at different sections start almost the same time. If the mass transfer resistance of the bed is low, the bed may reach the adsorption equilibrium within a short time, and the adsorbent material in the bed will be fully employed. With the strongly cooling function of the circulating water convection, the temperature shooting-up was restrained effectively after about 400-600 s of the adsorption, except for time-point 9. In contrast, for a natural air cooling method, the bed temperature would decrease relatively slowly. The related experimental result has been discussed thoroughly in Du et al.¹⁴ The meager cooling effect of air flow frustrated the heat discharge of the bed, and then impacted the cycle performance of the adsorption refrigeration system. In comparison, water cooling was much better for the system.

Figure 4: Temperature change of the bed in the adsorption process for SAPO-34 zeolite. This figure presents the temperature change of the bed in the adsorption process. Through the variation of the temperature, we can analyze the characteristics of the mass transfer of the bed. The response rate of the temperature reflects the adsorption rate of the material in the bed.

Heat transfer characteristic of the bed through the desorption process
The adsorption process is a coupled heat and mass transfer phenomenon. The desorption/adsorption of the adsorbent is highly related to the temperature change of the bed. Nevertheless, the heat transfer characteristic of the bed is not only determined by the thermal properties of the adsorbent itself, but also by the bed structure. We tend to choose a material with both a strong adsorption ability and high conductivity. But unfortunately, quite often these qualities are in conflict. A porous material with good adsorption usually exhibits poor conductivity. Many factors (e.g., the molecular structure, the processing method, the particle size, etc.) can impact the thermal properties of the adsorbent¹⁵^,¹⁶. Figure 5 shows the average temperature change of the bed in the desorption process for the SAPO-34 and ZSM-5 zeolite. To facilitate the comparison, the recorded solar intensity in the test campaign is also presented. Although the solar intensity was nearly the same for the two zeolites, the increment of temperature was quite different. For the ZSM-5 zeolite, the temperature was rising over 32 °C, while for the SAPO-34 it was only 17 °C. This result revealed that the heat transfer ability of the ZSM-5 zeolite was better than that of the SAPO-34 zeolite. The mass transfer between the adsorbent and the vapor is the most important process, but only with the support of the heat transfer can a good mass transfer be realized.

Figure 5: The change of the average temperature of the bed during the desorption process. This figure shows the difference in the heat transfer between the SAPO-34 zeolite and the ZSM-5 zeolite. During the 600 s desorption time, the increment of the temperature for the ZSM-5 zeolite and SAPO-34 zeolite was quite different. For the ZSM-5 zeolite, the temperature increase was 32.52 °C, while for the SAPO-34 zeolite the increase was only 17.02 °C. At the same solar-heating condition, the larger temperature increment of the ZSM-5 zeolite indicates its superiority of heat transfer relative to SAPO-34 zeolite.

The desorption characteristic of the bed
In general, the output of the refrigeration power for an adsorption system is determined by the adsorbent characteristic and the heat transfer rate of the bed. Usually, the time for the desorption process is longer than the time for the adsorption process. It is essential to know the characteristics of the heat transfer in the bed during the desorption. Here the index of the desorption degree E(t) is used to evaluate the completeness of the desorption of the bed. E(t) is defined as the ratio between the desorbed amount of refrigerant vapor, from the beginning to time t, and the total amount of the vapor uptake in the adsorption process.

With the experimental data, the E(t) of the bed at different desorption times can be obtained. Firstly, it is shown that the desorption degree was improved to some extent as the bed temperature increased. For the SAPO-34 zeolite system, the E(t) increased from 54.9% at t = 1 h to 69.3% at t = 2 h. On the other hand, at the same desorption time, the ZSM-5 system showed a worse desorption effect than the SAPO-34 system.¹⁴ Although the bed temperature of the SAPO-34 was comparatively lower, as previously discussed regarding Figure 5, its desorption degree was better. This tells us that SAPO-34 zeolite is more suitable to use as the adsorbent material. This feature of SAPO-34 zeoilite was also emphasized by Gordeeva et al.¹⁷

The refrigeration capacity of the system
The refrigeration capacity of the adsorption system is basically reflected by the temperature decrease of the water tank. The test results for the tank temperature are presented in Figure 6. The tank temperature changed with time in a nonlinear way. It decreased quickly within the first 600 s of the adsorption time, and then the temperature decrease slowed down. In comparison to the two temperature profiles of the SAPO-34 and the ZSM-5 zeolite, it is known that the refrigeration capacity of the two zeolites was rather different. The temperature decrement of the water tank directly reflected the refrigeration capacity of the system. Obviously, the temperature drop for the SAPO-34 system was much greater than that for the ZSM-5 system. With better desorption characteristics as mentioned above, the SAPO-34 zeolite exhibited a higher refrigeration capacity than the ZSM-5 zeolite. This identification is consistent with the conclusion of Gordeeva et al.¹⁶ and Kakiuchi et al.¹⁸

Figure 6: The temperature variation of the chilled water tank. In general, the temperature variation of the chilled water in the evaporator tank was not linear. For the SAPO-34 zeolite, it declined quickly within the first 600 s and then the decline slowed down. In contrast, the temperature change of the ZSM-5 zeolite was relatively smooth. This reflected the feature that the refrigeration power output declined with time. The two curves also revealed the performance difference of SAPO-34 and ZSM-5 zeolite.

The performance of the system is evaluated by the index of COP and SCP that is determined by Eq. (3) and Eq. (4), respectively, and the results are shown in Table 2. According to the nonlinear change of the temperature in Figure 6, two sets of data for the adsorption time t_ads = 600 s and t_ads = 1,800 s are presented. For either case in the table, the Q_ref within the first 600 s takes a proportion of more than two thirds of the total refrigeration capacity of the 1,800 s adsorption time. Obviously, the SCP for t_ads = 600 s is much higher than that for t_ads = 1,800 s, however the COP results run contrary to these results. The best COP in Table 2 has reached 0.169. Error analysis was conducted and revealed the uncertainty of the COP was between 6.2–9.4% corresponding to different test campaigns. It needs to be mentioned that the maximum COP here is in the comparative range of the result by Abu-Hamdeh et al.⁸ Their system of parabolic trough collector generated a COP of 0.18-0.20. The SCP index reflects the specific power output of the refrigeration capacity of the bed. A higher SCP implies that a higher refrigeration power is generated by a unit of adsorbent mass. The analyzed results have demonstrated that both the COP and the SCP of the SAPO-34 were superior to that of the ZSM-5, no matter if the adsorption time was longer or shorter.

Table 2: Comparison of the refrigeration capacity of ZSM-5 and SAPO-34 zeolite. For comparison, here we present the comprehensive performance of the adsorption refrigeration of SAPO-34 and ZSM-5 zeolite. Either by the SCP index or by the COP index, the SAPO-34 system shows its superiority to the ZSM-5 system.

Discussion

As a thermodynamic system, the performance of a solar adsorption refrigeration device depends on the optimum design and the proper operation of the system. Both the heat supply and the cooling method of the bed are important to guarantee the system works well. Water cooling is preferred to air cooling because of the high strength of convection heat transfer of water. The poor conductivity of the adsorbent material has usually determined the limited heat transfer rate of the bed. To improve the heat transfer of the bed, many measurements were considered such as the enhancement structure of the internally-inserted fins.¹⁹ Silica gel is another kind of popular adsorbent material. If a silica gel is used in the solar adsorption system, the desorption temperature of the bed must be limited to less than 95 °C, so that the silica gel will not become dehydrated and lose activity.

Like most renewable energy systems, the current adsorption refrigeration system has some shortcomings in terms of engineering applications. The notable problem is the intermittent work of the system. With the intrinsic nature of the heating-up and cooling-down, the adsorption system can't supply cold power continually as a single bed is used. To solve this problem some researchers considered a conjugated two bed system, in which the technique of regenerative heat and mass transfer could be applied. Such systems can become rather complex but the performance improvement was often quite unsatisfactory. Another point that needs to be considered is the weather condition effect. For bad weather days, there will not enough solar energy supply to the system. In such a situation, some spare heat source needs to be ready so that the system can continue to work.

As a green energy technology, the solar adsorption refrigeration system has attracted much attention in the past decade. The use of solar energy avoids the consumption of fossil fuel and effectively reduces the air pollution. In addition, such a system has no rotating component, no noise, and can be deployed flexibly. Though the efficiency of the system is not comparable to conventional refrigeration systems that use vapor compression or ammonia absorption, the abundance of solar energy presents a potential significance for luminance in the future. For a system that consumes electricity or fuel, the efficiency of performance is very important because of operation costs. In contrast, solar energy is free and the system is still beneficial even if the COP is not very high.

We are not sure how quickly solar adsorption technologies may replace conventional refrigeration systems in large scale, because there are some aspects of this technique that need further improvement. A couple years ago, it was reported that the Tokyo Gas Corporation in Japan put forward a commercial type of adsorption refrigerator that was driven by industrial waste heat. With developments in the global economy and technology, the technique of the solar adsorption refrigeration may first find its application in the remote rural areas where the climate is hot in most time of the year.

The operation of this system involves four critical steps. According to the time sequence, they are: the pre-heating of the bed under closed conditions; the desorption process with the bed temperature increasing further; the cooling down of the bed by re-circulating water or an air stream; and the adsorption process that generates the refrigeration effect.

Declarações

The authors have nothing to disclose.

Acknowledgements

This research work was sponsored by the National Key Basic Research Program of China (No.2015CB251303), and the National Natural Science Foundation of China (No. 51276005).

Materials

evaporator	home-made		finned heat exchange
condenser	home-made		finned heat exchange
evaporator water tank	home-made		volume:9L
condenser water tank	home-made		volume:9L
vacuum pump	Beijing Jing Rui Ze Xiang Instrument Co. Ltd.		rotation speed:1400 motor pover:370W
condenser pressure sensor	Beijing Li Nuo Tian Sheng Instrument Co. Ltd.	16P2623	maximum:2200Pa
bed pressure sensor	Beijing Li Nuo Tian Sheng Instrument Co. Ltd.		maximum:2200Pa
adsorption bed	home-made		cylundrical glass tube
parabolic trough	home-made		high reflective aluminum sheet
water pump	home-made		motor pover:250W, water head:8m
water tank	home-made		volume:500L
DRT-2-2 direct solar actinometer	Beijing Tian Yu De Technology Co. Ltd.	03140132	sensitivity:13.257μV/W•m²
TBQ-2 solar pyranometer	Jinzhou Sunshine Technology Development Co., Ltd., China	209079	sensitivity:12.733μV/W•m²
SAPO-34 zeolite	Langfang Peng Cai Co., Ltd., China		20mm in length and 2.2mm in diameter
ZSM-5 zeolite	Langfang Peng Cai Co., Ltd., China		5.7mm in diameter

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Yuan, Z., Li, Y., Du, C. Experimental System of Solar Adsorption Refrigeration with Concentrated Collector. J. Vis. Exp. (128), e55925, doi:10.3791/55925 (2017).