## 1 Introduction
The membrane module was experimentally evaluated for four operation hours; after this time, the total amounts of refrigerant available, assuming a 1 m\({}^{2}\) membrane area, were 14.50, 11.59, and 7.20 kg with LiBr solution temperatures of 95.1, 85.2, and 75.1 \({}^{\circ}\)C, respectively. Based on these results, the intermittent solar absorption cooling system was calculated and sized. [PERSON] et al. [16; 17] demonstrated the applicability of the air gap membrane distillation (AGMD) process for water vapor desorption. The authors used H\({}_{2}\)O/LiBr and H\({}_{2}\)O/Carrol mixtures, and all experimental tests were conducted at atmospheric pressure. The effects of aqueous solutions temperatures and concentrations were analyzed. The experimental desorption rate was 0.30-9.70 kg/m\({}^{2}\) h with the H\({}_{2}\)O/LiBr mixture and 0.6-2.4 kg/m\({}^{2}\) h for the H\({}_{2}\)O/Carrol mixture. Two membrane pore sizes (0.22 and 0.45 \(\upmu\)m) were used, and the Carrol concentration was constant around 61% _w/w_. [PERSON] et al. [18] analyzed the effects of several operation variables on the desorption process in a membrane desorber. Based on the experimental results, the authors concluded that in direct desorption mode, the desorption rate behaves linearly with respect to the solution temperature. However, the desorption rate increases exponentially as the solution temperature increases in boiling desorption mode. The experimental results suggested that the solution pressure has no effect on the desorption process. According to [PERSON] et al. [19], the water vapor desorption process can be enhanced if the solution layer at the membrane-solution interface is renewed. The authors proposed and evaluated a membrane desorber with microstructures in the flow channel to promote a turbulent flow regime; the desorption rate was increased around 1.7 times compared with the flow channel without the microstructures under the same operating conditions. [PERSON] et al. [20] proposed a vacuum membrane distillation process to replace the conventional boiling desorbers in absorption systems. The authors evaluated a 0.3 m\({}^{2}\) hollow fiber membrane desorber at different operation conditions. The maximum desorption rate was 2.0 kg/m\({}^{2}\) h with an 88 \({}^{\circ}\)C LiBr solution and 0.01 MPa vacuum pressure. [PERSON] et al. [21] evaluated a membrane desorber with 0.00168 m\({}^{2}\) of effective area with a water/LiBr mixture. Based on the experimental data, the authors concluded that the desorption rate increased as the pressure difference increased, and the channel thickness and the LiBr concentration in the inlet stream decreased. [PERSON] and [PERSON] [22] completed an extensive literature review of the use of membrane devices for absorption systems applications. In this study, we evaluated a membrane desorber with an AGMD configuration with H\({}_{2}\)O/LiBr as the working mixture, with solution temperatures from 75 to 95 \({}^{\circ}\)C, and condensation temperatures from 14 to 25 \({}^{\circ}\)C. With the experimental data, we calculated a thermal solar system and sizing to demonstrate the feasibility of a membrane desorber powered by renewable thermal energy for absorption cooling applications.