Experimental Study of a Bubble Mode Absorption with an Inner Vapor Distributor in a Plate Heat Exchanger-Type Absorber with NH₃-LiNO₃

Abstract

Absorption systems are a sustainable solution as solar driven air conditioning devices in places with warm climatic conditions, however, the reliability of these systems must be improved. The absorbing component has a significant effect on the cycle performance, as this process is complex and needs efficient heat exchangers. This paper presents an experimental study of a bubble mode absorption in a plate heat exchanger (PHE)-type absorber with NH₃-LiNO₃ using a vapor distributor in order to increase the mass transfer at solar cooling operating conditions. The vapor distributor had a diameter of 0.005 m with five perforations distributed uniformly along the tube. Experiments were carried out using a corrugated plate heat exchanger model NB51, with three channels, where the ammonia vapor was injected in a bubble mode into the solution in the central channel. The range of solution concentrations and mass flow rates of the dilute solution were from 35 to 50% weight and 11.69 to 35.46 × 10⁻³ kg·s⁻¹, respectively. The mass flow rate of ammonia vapor was from 0.79 to 4.92 × 10⁻³ kg·s⁻¹ and the mass flow rate of cooling water was fixed at 0.31 kg·s⁻¹. The results achieved for the absorbed flux was 0.015 to 0.024 kg m⁻²·s⁻¹ and the values obtained for the mass transfer coefficient were in the order of 0.036 to 0.059 m·s⁻¹. The solution heat transfer coefficient values were obtained from 0.9 to 1.8 kW·m⁻²·K⁻¹ under transition conditions and from 0.96 to 3.16 kW·m⁻²·K⁻¹ at turbulent conditions. Nusselt number correlations were obtained based on experimental data during the absorption process with the NH₃-LiNO₃ working pair.

1. Introduction

The increasing awareness of global warming is inspiring the population to find better solutions to the problems related to the use of clean energy. For cooling needs, industries and residential sectors use mostly mechanical vapor compression refrigeration systems driven by electricity as well as conventional refrigerants. This field generates many opportunities for research on the use of alternatives energy sources friendly to the environment [1]. The opportunity arises to develop refrigeration systems that fit into the model of the three Es (energy, economy, and ecology) [2,3].

Recently, the demand for absorption refrigeration systems has increased mainly for small capacity (5 to 20 kW) units that can be driven by low and medium temperature heat sources such as waste heat, solar, geothermal or biomass. These thermal cooling systems are an attractive option in order to reduce electric power consumption.

The design of efficient heat exchangers is vital for absorption cooling systems to compete against compression systems, since they constitute the main and most expensive components [4]. The commercial absorption systems use working pairs such as NH₃-H₂O for cooling and freezing applications; however, this system has the need for an ammonia vapor rectification component that consequently produces a rise in cost and a reduction in the coefficient of performance. However, NH₃-LiNO₃ could be an alternative working mixture, since it has a better thermodynamic properties than NH₃-H₂O and a rectifier is not necessary [5,6,7]. The absorber is a critical component of the absorption system [8] due to the complex heat and mass transfer processes during the absorption of ammonia vapor in the dilute solution. The bubbling absorption mode has been proposed as a viable option with NH₃-H₂O [9,10,11,12,13], rather than the traditional falling film absorption systems because it not only provides high heat transfer coefficients but also provides good mixing between the vapor and the liquid. However, it requires of good vapor distribution, whilst falling film transfer requires an excellent liquid distribution [11].

Plate heat exchangers (PHEs) have been used as an absorber in bubble mode because the corrugation of the channels produces high turbulence values. Lee et al. [9] analyzed an absorber using a flat plate heat exchanger with ammonia-water; they concluded that the increase of solution flow rate slightly affected mass transfer, but improved heat transfer; besides the heat transfer was improved when the vapor flow rate was increased. The authors proposed experimental correlations for the Nusselt and Sherwood numbers.

Cerezo et al. [8] presented a mathematical model to analyze the bubble absorption process using a PHE. They carried out a comparative study using different mixtures as working fluids: NH₃-H₂O, NH₃-NaSCN and NH₃-LiNO₃; the system was simulated at typical refrigeration operating conditions. The results showed that the mixtures NH₃-H₂O and NH₃-NaSCN had greater absorption heat rates and ammonia vapor mass absorption compared to the mixture NH₃-LiNO₃. The low values obtained by the last mixture were mainly caused by the high viscosity of the solution, which decreased the absorption process. On the other hand, the NH₃-LiNO₃ mixture resulted with the highest COP values. Ayub [14] presented a study of available correlations for PHE´s in only one phase in a format that is easily used by engineers to design and analyze systems of this kind. Oronel et al. [15] presented in 2012 a study of NH₃-LiNO₃ absorption in the bubbling mode with a PHE with Chevron-L type corrugation (30° from the plate vertical axis) and using a simple tube as a gas distributor with an internal diameter of 1.7 mm. The results showed empirical relationships for the Nusselt and Sherwood numbers for the NH₃-LiNO₃ solutions. Best and Rivera [16] carried out an extensive review of the theoretical and experimental thermal cooling systems. In particular, systems at small and medium size capacities operating with water/lithium bromide, and ammonia/lithium nitrate.

This paper carries out an experimental evaluation of an absorber with a type L plate heat exchanger (PHE) with NH₃-LiNO₃ using a vapor distributor with five perforations located on the bottom side of the absorber in order to increase the mass transfer. According to the literature review performed for plate heat exchangers that operate as an absorber with the NH₃-LiNO₃ working pair, the mass transfer coefficients calculated in this work reached higher values than other studies. The modified plate exchanger with an inner gas distributor will be installed as an absorber within an absorption cooling system driven by solar energy. The results of this work are presented as a good engineering option: to incorporate an efficient absorber into a compact refrigeration system by means of NH₃-LiNO₃ absorption. These results are important for the absorption refrigeration research and development.

2. Description of the Experimental System

2.1. Test Rig Description

A test rig was designed to study the absorption process in a PHE. It consisted basically of three circuits: the ammonia vapor (yellow), ammonia-lithium nitrate solution (orange) and the cooling water as can be seen in Figure 1. In the ammonia vapor circuit, liquid ammonia was stored in a tank and pumped through a micrometric expansion valve, which reduced the pressure and changed to a vapor phase, it was injected into the bottom side of the absorber using a vapor distributor as it is shown in Figure 2. The absorption process was carried out in the solution circuit. The poor in ammonia solution was stored in a container and it was pumped to the bottom side of the absorber, where ammonia vapor and solution were mixed. The concentrated solution left the absorber and was sent to a storage container. The heat generated by the absorption process was removed by the cooling water circuit, which was pumped from a cold water reservoir (15,000 L) to the side plates of the PHE, extracting the absorption heat. A needle valve regulated the cooling water mass flow. The ammonia vapor and solution circuits were made of stainless steel, whereas the cooling circuit was made of PVC. In Figure 1, we can also observe the control and measurement instruments that were placed in the experimental system (pressure, temperature, mass flows, needle valves, diaphragm pumps).

Figure 1. Schematic diagram of the device to study the bubble absorption process in a plate heat exchanger.

Figure 2. Diagram and photograph of a chevron plate heat exchanger. (a) Detailed inner main parameters; (b) the assembly of the modified PHE, with the measuring and control instruments.

2.2. Plate Heat Exchanger as Absorber

A stainless steel plate heat exchanger model T2-BFG from Alfa Laval was used as an absorber. Table 1 shows the dimension details of a plate. The PHE consisted of three channels, ammonia vapor and NH₃-LiNO₃ flowed in the central channel, and cooling water flowed into the side channels. Details of the absorber are shown in Figure 2.

Table 1. Main dimensions of a plate heat exchanger.

Parameter	Dimension
Spacing between channels, Λ [mm]	6
Inter-plate channel height, b [mm]	2.18
Effective width length, Lh [mm]	77
Pattern length, Lp [mm]	275
Effective height length, Lv [mm]	280
Inside width between gaskets edges Lw [mm]	82
Port diameter, Dp [mm]	25
Number of passes, Np	1
Chevron angle, β [degree]	30

The vapor distributor, shown in Figure 3, consisted of a 50 mm long and 5 mm inside diameter steel tube with five equidistant perforations: two of 1 mm, two of 2 mm and one of 3 mm [10,11]. Temperature, pressure, and mass flow rate sensors were placed at the inlet and outlet of the cooling water and solution flows in the plate heat exchanger as it can be seen in Figure 1. Information on the accuracy of the sensors can be seen in Table 2, and the operating parameters and their respective accuracies summary can be seen in Appendix A.

Figure 3. Inner distributor of ammonia vapor placed in the central channel of the PHE. (a) general view of the vapor distributor; (b) close up of the tube with perforations.

Table 2. Parameters of the sensors used in the experimental study and associated uncertainty values.

Sensor	Device	Operating Range	Accuracy
Temperature	RTD	−180 a 520 °C	±0.2 °C
Mass flow	Coriolis	0 a 5 kg·min−1	±0.1%
Density	Coriolis	700 a 1200 kg·m−3	±0.1%
Pressure	piezoelectric	0 a 10 bar	±0.15%
Mass flow	Turbine	0 a 30 kg·min−1	±0.2%

3. Data Reduction

The thermodynamic properties of NH₃-LiNO₃ solutions were obtained from Libotean [17], Infante Ferreira [18] and Conde [19]. The experimental data correspond to steady state conditions during at least 15 min for each experimental run. The heat transfer area (A_exch) was calculated using the surface enlargement factor (φ) defined as the proportion of increased length with respect to a plane plate length or projected length [20]. A_eff is the projected area of the plate. The heat transfer area was 0.0504 m²:

$$A_{exch}=\varnothing *A_{eff} \left[\mathrm{m}\right]$$

(1)

$$\varnothing =\frac{\mathit{increased\_length}}{\mathit{projected\_length}} \left[dimensionless\right]$$

(2)

The equivalent diameter, D_e, is defined as:

$$D_e=\frac{4b{L}_w}{2\left(b+L_w\varnothing \right)}\approx \frac{2b}{\varnothing } \left[m\right]; \mathrm{Considering} \mathrm{that}: \mathrm{b}<<\mathrm{Lw}$$

(3)

The Reynolds number (Re), channel mass velocity (Gc_sol) and the number of channels per pass (N_cp), are calculated as [21,22,23,24,25]:

$$Re=\frac{G_{Csol}{D}_e}{\mu } \left[dimensionless\right]$$

(4)

$$G{c}_{sol}=\frac{{\dot{m}}_{sol}}{N_{cp}b{L}_w} \left[{\mathrm{kg} \mathrm{m}}^{-2}{\mathrm{s}}^{-1}\right]$$

(5)

$$N_{cp}=\frac{N_t-1}{2N_p} \left[dimensionless\right]$$

(6)

G_Csol is a relationship of the solution mass flow rate with respect to the physical characteristics of the heat exchanger. D_e is equivalent diameter, b is the inter-plate channel height, µ is the dynamic viscosity, ṁ_sol is the mass flow of solution, N_cp is the number of channels per pass, N_t is the total number of plates, N_p is the number of passes and, L_w is the effective height length.

The logarithmic mean temperature difference (LMTD) was used considering the inlet and outlet temperatures of the absorber [24]:

$$LMTD=\frac{\left[T_{sol,in}-T_{c,out}\right]-\left[T_{sol,out}-T_{c,in}\right]}{ln\left[\frac{\left[T_{sol,in}-T_{c,out}\right]}{\left[T_{sol,out}-T_{c,in}\right]}\right]} \left[dimensionless\right]$$

(7)

The Nusselt number is stated by Equations (8) and (9), where µ_SOL is dynamic viscosity of solution, µ_W is the dynamic viscosity of water, L_cha is the channel length:

$$N{u}_{sol}=aR{e}^{b}P{r}^c\left(\frac{{\mu }_{sol}}{{\mu }_w}\right) \left[dimensionless\right]$$

(8)

$$N{u}_{sol}=\frac{h_{sol}{L}_{cha}}{k_{sol}} \left[dimensionless\right]$$

(9)

$$P{r}_{sol}=\frac{{\mu }_{sol}C{p}_{sol}}{k_{sol}} \left[dimensionless\right]$$

(10)

The overall heat transfer coefficient, U, was calculated by Equation (11):

$$U=\frac{1}{\frac{1}{h_w}+\frac{x_{ss}}{k_{ss}}+\frac{1}{h_{sol}}} \left[kW{m}^{-2}{K}^{-1}\right]$$

(11)

Ammonia mass absorption flux, F_ABS, indicates the capacity of the solution to absorb the ammonia vapor per unit of heat transfer area. ṁ_NH3 is absorbed ammonia mass flow rate, A_exch is the heat exchange area:

$$F_{ABS}=\frac{{\dot{m}}_{NH3abs}}{A_{exch}} \left[{\mathrm{kgm}}^{-2}{\mathrm{s}}^{-1}\right]$$

(12)

The overall mass transfer coefficient, K_m, defined by Equation (13):

$$K_m=\frac{{\dot{m}}_{NH3abs}}{{\rho }_{NH3}{A}_{exch}LMCD} \left[{\mathrm{m} \mathrm{s}}^{-1}\right]$$

(13)

$$LMCD=\frac{\left[X_{sol,in}^{equi}-X_{sol,in}\right]-\left[X_{sol,out}^{equi}-X_{sol,out}\right]}{ln\left[\frac{\left[X_{sol,in}^{equi}-X_{sol,in}\right]}{\left[X_{sol,out}^{equi}-X_{sol,out}\right]}\right]} \left[dimensionless\right]$$

(14)

where, ṁ_NH3abs is the absorbed ammonia mass flow, A_exch is the exchange area, ρ_NH3 is ammonia density, LMCD is logarithmic mean concentration difference, X, is solution concentration [26,27,28,29].

4. Discussion

The absorber was characterized using water on both sides of the PHE in order to calculate a Nusselt Number correlation for cooling water. Previously, experiments were carried out introducing water in both cold and hot sides of the channels in order to calculate the cooling water heat transfer coefficient. A correlation of the Nusselt number was obtained as a function of the Reynolds and Prandtl numbers:

$$N{u}_{water}=0.3417R{e}_{water}^{0.5891} P{r}_{water}^{0.1726} \left[dimensionless\right].$$

(15)

The range of operation conditions for the experimental test started with a solution of NH₃-LiNO₃ at 35% ammonia weight and it was progressively increased in each experiment until reaching a maximum concentration of 50%. The range of the ammonia mass flow rates injected was from 0.0794 × 10⁻³ to 1.217 × 10⁻³ kg s⁻¹. The flow rates of the dilute ammonia solution flow rate were from 0.0117 to 0.035 kg s⁻¹.

In Figure 4 the x-axis represents in ascending order the experimental tests. Each test was considered valid after being kept in steady state for at least fifteen minutes; data acquisition was performed at ten-second intervals. The values of the concentrated (X_sc) and diluted (X_sd) solutions, for each test are shown on the left-y-axis. In this work, the concentration gradually increased. The experiments started from an initial diluted concentration of 35% up to a concentration of 50%. The concentrated solution also increased step by step. The difference in concentrations (ΔX) for each valid test is shown in the lower part of the graph; the average difference in concentrations was 0.011 ± 0.005%. On the other hand, the behavior presented by the Reynolds number of the solution, Re_sol, in each of the test points is also shown; it is observed that it was increasing as the concentration increased. The latter was to be expected taking into account the decrease in the viscosity of the ammonia solution as a result of the increase in the ammonia concentration. Two behaviors can be seen for the Re_sol, the transition zone that goes from 20 ≤ Re_sol ≤ 90 and the turbulent zone 90 ˂ Re_sol ˂ 400. The transition zone showed a linear behavior with a slightly steep slope. On the other hand, the turbulent zone had a polynomial behavior.

Figure 4. Experimental valid tests, their respective concentrations, concentration difference and Reynolds number of solution.

Empirical correlations for the solution Nusselt numbers were proposed on the basis of the experimental data presented here for the absorption of ammonia vapor by ammonia-lithium nitrate solution in a PHE-type absorber. The correlations were made using the experimental data. Equation (16) is valid for the transition zone and Equation (17) for the turbulent zone. These empirical relationships in conjunction with Equation (9) allowed finding the h_sol:

$$R{e}_{sol}<90 N{u}_{sol}=0.1301R{e}_{sol}^{0.3523}P{r}^{0.333}{\left(\frac{{\mu }_{sol}}{{\mu }_w}\right)}^{0.17} \left[dimensionless\right].$$

(16)

$$R{e}_{sol}\ge 90 N{u}_{sol}=0.0089R{e}_{sol}^{0.8213}P{r}^{0.333}{\left(\frac{{\mu }_{sol}}{{\mu }_w}\right)}^{0.17} \left[dimensionless\right].$$

(17)

Figure 5 shows the behavior of the solution heat transfer coefficient, h_sol, and the channel mass velocity of the solution, G_Csol, against the Reynolds solution number, Re_sol. The solution heat transfer coefficient, h_sol, increased linearly from 0.96 to 2.46 kW m⁻²K⁻¹ at Re_sol range from 20 to 90 and G_Csol shows a linear increase for the same range of Re from 40 to 130 kg m⁻² s⁻¹. Subsequently, h_sol showed a slight increase and the channel mass velocity of the solution, G_Csol remained almost constant. This behavior was caused by the increment of the ammonia concentration in the solution, which reduced the viscosity and influenced the thermodynamic behavior; these variations influence the Prandtl number as shown in Figure 5, which shows that the thermal boundary layer will increase as a result of the decrease in the viscosity of the solution. The h_sol, increased as the result of the combination of an increase in Re_sol and the decrease in G_Csol. It was observed in the range of Re_sol from 50 to 80 a compact grouping of measured points came were obtained, as a result of the variation of solution mass flow rate which were chosen for the study (which translate into mass velocities), similar results have been reported in previous studies [22,23,24,25]. Figure 6 shows the behavior of the convective heat transfer coefficient of the solution with respect to the Re_sol number. Likewise, it is shown how the Prandtl number of the solution was modified. As the concentration of ammonia increased during the experimental tests, the viscosity of the solution decreased and consequently the Reynolds number increased.

Figure 5. Solution heat transfer coefficient and the channel mass velocity of the solution, G_Csol, as a function of Reynolds Number.

Figure 6. Prandtl number as a function of the solution Reynold number.

It can be seen that as well as the change in viscosity in the solution, μ_sol, other solution properties such as the thermal conductivity, K_sol, and specific heat, Cp_sol, were also modified. It can be seen that there was a clear decrease of the Pr_sol due to the thermodynamic and thermal properties of the solution reaching lower values and with the effect that the heat begins to diffuse faster with respect to convection. This behavior results in the increase of the convective heat transfer coefficient in the transition zone with a very steep slope and later in the turbulent zone, this slope decreases.

Figure 7 shows the effect on the mass absorption flux, F_ABS, and mass velocities, G_Csol, as a function of Re_sol. It can be observed that the average value of 1.93 ± 0.23 × 10⁻² kg m⁻²s⁻¹ was obtained, for different mass velocities for all interval of Re_sol. It can be seen that, although the ammonia solution concentration increased during the experiments, the amount of absorbed ammonia was similar during the transition region [15] as well as in the turbulence zone. The ammonia flow rate was controlled during all experimental tests at different operating conditions.

Figure 7. Mass absorption flux, F_ABS to different conditions of G_Csol and both with respect to Re_sol.

The results showed that there was a larger absorption potential using higher mass velocities as there exists a larger concentration gradient. At the beginning of the experiments, there was a low concentration of ammonia; therefore, the concentration gradient was high. In addition, during the experiments it was observed that if a larger residence time was used for the ammonia mass flow inside the absorber, a better absorption was obtained although the mass velocity in the channel, G_Csol decreased. One option to maintain the higher residence time of the ammonia flow without affecting the channel mass velocity is to employ an absorber with a larger effective length (L_eff) than the one used in this work. Figure 8 shows the mass transfer coefficient (K_m), and the ammonia vapor flow rate (ṁ_NH3), with respect to the Re_sol. The mass transfer coefficient reached values that ranged from 0.009 to 0.015 m·s⁻¹ with an average of 0.011 ± 0.002 m·s⁻¹.

Figure 8. Mass transfer coefficient and vapor flow rate as a function of solution Reynolds number.

Additionally, Figure 9 shows K_m and LMTD as a function of Re_sol. The LMTD values obtained were from 6.9 to 21.6 °C. The effect on the mass transfer coefficient, K_m, with respect the logarithmic mean temperature differential, LMTD was subsequently analyzed. Oronel et al. [15] presented a comparison of K_m with respect to sub cooling temperatures of the solution. This work proposes that it is more suitable to compare the behavior of K_m, including all temperatures in the heat exchanger, which is given by the LMTD.

Figure 9. Mass transfer coefficient, K_m and LMTD as a function of Re_sol.

Figure 9 shows the K_m and LMTD variation as a function of Re_sol. It can be seen that when the LMTD increases K_m is affected positively, both, in the transition and turbulent zones. It is clear that the values of LMTD are lower in the transition than turbulent zone, 90 < Re_sol ≤ 450, K_m is increased as a result of the dominance of shear forces over the viscous forces, improving the mixing of vapor with the solution, even though it already has a higher ammonia concentration. It can be deduced that for the transition zone, 20 ≤ Re_sol ≤90, higher values of LMTD are required in order to achieve values of K_m similar to those of the turbulence zone. High viscosity and the temperatures that were registered in the transition area (more exothermic heat generation) caused higher LMTD values.

Table 3 shows h_sol and K_m values obtained from Oronel et al. [15] and the present work at similar Reynolds number. The values of h_sol were lower than those reported by Oronel et al. [15]. At higher Reynolds numbers, h_sol values reached 3.0 kW m⁻²K⁻¹. However, F_ABS values were higher than reported by Oronel et al. due to the improved mixing of vapor and solution, besides it obtained higher values of K_m than those reported in the literature related with absorption in cooling systems.

Table 3. Comparative chart of Some Mass and Convective Heat transfer coefficients K_m reported in the literature with NH₃-LiNO_3, NH₃-H₂O and H₂O-LiBr.

Parameter	Resol	hsol [kW m−2K−1]	Km·10−5 [m s−1]	Method	Solution
Oronel et al. [15]	10–70	2.5–8.0	16.7–38.9	Experimental bubble mode absorption	NH3-LiNO3
Cerezo et al. [22]	170–370	2.7–5.4	100–200	Experimental bubble mode absorption	NH3-H2O
Infante Ferreira [30]		0.115		Experimental falling film	NH3-LiNO3
Venegas et al. [31]	10–250	5.8	18.6	Numerical spray absorption	NH3-LiNO3
Zacarias et al. [32]	6–17		34–101	Experimental spray flat fan	NH3-LiNO3
Jiang J.A. et al. [33]	300–950	0.97–1.95	--	Experimental flow boiling in smooth horizontal tubes	NH3-LiNO3
Jiang J.A. et al. [34]	300–950	0.95–1.95	--	Experimental flow boiling in horizontal tubes	NH3-LiNO3
Palacios E. et al. [35]			30	Experimental spray flat fan	H2O-LiBr
This work	20–450	0.96–3.00	820–1500	Experimental bubble mode absorption	NH3-LiNO3

In this work, a review of the experimental works was carried out with the NH₃-LiNO₃, H₂O-LiBr and NH₃-H₂O mixtures and with the absorption preferably in the bubbling absorption mode. The review did not find many PHE-type absorbers and even less with the NH₃-LiNO₃ mixture. Table 3 shows a summary of results, which are interesting as a reference frame, not all of them are experimental studies of a bubble mode absorption in a PHE-type absorber with NH₃-LiNO₃. Infante Ferreira [30] reported experimental results of NH₃-LiNO₃ absorption in a falling film absorber in which upward ammonia vapor is absorbed in countercurrent by a laminar film of diluted ammonia solution; it had many technical limitations to achieve it; hence, the small value of h_sol. It does not provide more data such as k_m. Venegas et al. [31] performed a numerical study of the spray absorption mode in a very short concentration range of 36.7 to 39% in the concentrated solution. They studied a range of the Re_sol also relatively small, of 10 to 70. The cooling water temperature was 34 °C. They considered it as an improvement to the falling film system. It considered an adiabatic chamber where the diluted ammonia solution was contacted, sprayed in small drops with the ammonia vapor. Zacarias et al. [32] carried out experimentally what was stated by Venegas et al., of the spray absorption mode and managed to obtain k_m values an order of magnitude higher than what was predicted by the numerical analysis. Cerezo [22] presented an experimental work with the NH₃-H₂O mixture with cooling water temperatures of 30 °C and mass flow rate of 0.038 kg s⁻¹. He used an ammonia distributor in a PHE-type absorber with an area of 0.1 m² of a single central hole and with mass flow rate of 0.0139 kg s⁻¹ solution, varying its concentrations from 29 to 33.4% of concentration by weight. He reported h_sol and K_m values higher than other studies that used NH₃-LiNO₃. The works of Jiang et al. [33,34] served us as a reference for the values of h_sol. They used the mixture NH₃-LiNO₃ for a boiling process. They did not report values for K_m.

5. Conclusions

An experimental study was carried out of a bubble mode absorption with an internal ammonia vapor distributor in a PHE-type absorber with the NH₃-LiNO₃ solution. The following conclusions can be drawn from the present study:

• The results obtained show that h_sol increased from a value of 0.9 to 1.8 kW m⁻²K⁻¹ for Re_sol values of 20 up to 80. For values of Re_sol greater than 120 and up to 440, due to limitations in the experimental rig, h_sol increased slowly from 1.8 to 3.0 kW m⁻²K⁻¹.
• The ammonia absorption flow F_ABS in the study had an almost constant value of 0.038 ± 0.004 kg m⁻²s⁻¹, for all the mass flow velocities, G_Csol throughout the experiments. The values are in the same range as the work by Oronel et al. [15] although for low values of Re_sol the values in this work are higher. This could be due to the vapor distributor and other operating conditions such as the higher pressure.
• It was found that the value of the mass transfer coefficient, K_m, had a relatively large interval from 0.009 to 0.015 m s⁻¹ with an average of 0.011 ± 0.002 m s⁻¹. Although mass flows of ammonia and mass velocities remained almost constant, there were fluctuations in K_m, which demonstrated that an additional factor affected its behavior. The additional factor was the logarithmic mean temperature difference (LMTD). It was observed that K_m behaved inversely proportional to the LMTD.
• It was concluded that by increasing the effective height, L_p, of the modified heat exchanger, the absorption of ammonia vapor could be increased, as the residence time will be increased. In addition, the registered thermodynamic conditions of the dilute ammonia solution were suitable for a better absorption. In order to sustain the previous hypothesis, that, even by increasing the turbulence – that is increasing the mass flow of dilute ammonia solution—the vapor absorption of ammonia remained almost constant, showing a slight decrease at higher Re_sol values; and this was mainly due to the fact that there was no greater contact area between the ammonia solution and the ammonia vapor.
• A correlation for the Nusselt number governing the absorption of ammonia vapor by the NH₃-LiNO₃ solution in a PHE-type absorber was proposed at two ranges of Reynolds number.