Desalination Trends and Technologies Part 9 doc

New Trend in the Development of ME-TVC Desalination System 189 increase the feed seawater temperature and consequently decrease the energy added for evaporation. T f1 T f2 T fj D s D r +D s P d P j D r F 1 F 2 F j D 1 T v1 T v2 T vj T 1 T 2 T j D j-1 D j P s B 1 B j B 2 2D f B n D n T n T vn T j+2 T vj+2 T vj +1 D s D r F T f M c T c B j+1 B j+2 T f T fj+2 T fj+1 D M c -F T f1 T f2 T fj D s D r +D s P d P j D r F 1 F 2 F j D 1 T v1 T v2 T vj T 1 T 2 T j D j B 1 B j B 2 D s D r ME-TVC 1 ME-TVC 2 MED D j-1 D j+2 D j+1 D r y D r y T j+1 Fig. 2. A schematic diagram of two ME-TVC units combined with a conventional MED unit. 4. Thermal analysis of ME-TVC desalination system First and Second Laws analysis are used in this section to develop a mathematical model of the ME-TVC desalination system. The model is developed by applying mass and energy conservation laws to the thermo-compressor, evaporators, feed heaters and end condenser. The following assumption were used to simplify the analysis: steady state operation, negligible heat losses to the surrounding, equal temperature difference across feed heaters, salt free distillate from all effects and variations of specific heat as well as boiling point elevation with the temperature and salinity are negligible. The brine temperature in each effect is less than that of the previous one by ∆T. So, if the brine temperature in the effect i is assumed to be T i , then the brine temperature in the next effect i+1 and so on up to the last effect n and can be calculated as follow: 1 ,1,2, ii TTT i n + = −Δ = (1) Desalination, Trends and Technologies 190 The temperature of the vapor generated in the effect i, T vi is lower than the brine temperature by the boiling point elevation plus non equilibrium allowance, where T vi is a saturation temperature corresponding to the pressure in the effect P i . (),1,2, ii T T BPE NEA i n ν =− + = … (2) The temperature difference between the effects is assumed to be the same in this analysis and can be calculated as follows: 1 1 n TT T n − Δ= − (3) The feed seawater temperature flowing into each effect (T fi ) can be calculated as follows: [ ( 1)] 1,2,3 fi f TT ni T i n = +−+ ⋅Δ = (4) 4.1 Mass and Energy Balance The feed seawater flow rate F is distributed equally to all effects at a rate equal to F i which can be calculated as follows: , 2 i Fn Fj nj == + (5) The brine leaving the first effect enters into the second effect and so on up to the last effect n, and the brine from the last effect is rejected. The brine leaving the first, second and last effect can be calculated considering mass balance law as follows: ii i BFD = − (6) () 111 1 j iii i BFD +++ = =− ∑ (7) () () 11 11 2 j n niijj ij BFDFD ++ =+ =⋅ − + − ∑∑ (8) The salt mass conservation law is applied, assuming that the distillate is free of salt, to find brine salinity from the first, second and last effect as follows: () i f bi ii FX X FD ⋅ = − (9) () 1 1 11 1 if bi j ii i FX X FD + + ++ = ⋅ = − ∑ (10) New Trend in the Development of ME-TVC Desalination System 191 () () 11 11 2 nf bn j n ii j j ij FX X FD F D ++ =+ ⋅ = ⋅−+ − ∑∑ (11) The vapor generated in the first effect by boiling only and can be determined from the energy balance of the first effect as follows: () ( ) 11 11 11 sr dfd f DD h h TT DFC LL ⎡⎤ +⋅− − ⎛⎞ ⎣⎦ =−⋅⋅ ⎜⎟ ⎜⎟ ⎝⎠ (12) The amount of vapor released from the second up to j can be expressed respectively as follows: () ( ) 22 1 21 1 1 2 22 2 f r TT LCT DDDyFy B FC LL L − ⋅Δ =+⋅−⋅⋅+⋅ −⋅⋅ (13) ( ) 2 1 11 1 [( ( ) ( 1) )] j jfj j jj ir j j j jj j i TT L CT DD DDyj Fy B FC LL L − − −− = − ⋅Δ =++⋅−−⋅⋅⋅+⋅−⋅⋅ ∑ (14) The vapor formed in the last effect of each ME-TVC unit D j is divided into two streams; one is entrained by the thermo-compressor (D r ) and the other is directed to the MED unit. j r f DDD = + (15) The two streams of D f are used as a heat source to operate low temperature multi effect distillation unit (LT-MED). So, the vapor formed in first, second and last effect of this unit can be calculated as follows: ( ) 11 11 11 1 22 jfj j jf j j jj j TT L CT DD B FC LL L ++ ++ ++ + − ⋅Δ =⋅ ⋅ +⋅ ⋅ − ⋅⋅ (16) ( ) 22 1 21 2 1 2 22 2 1 ()() 2 j jfj j jj ir j j j jj j i TT L CT DD DDyjnFy B FC LL L ++ + ++ + + + ++ + = − ⎛⎞ ⋅Δ =++⋅−+⋅⋅⋅+⋅⋅ −⋅⋅ ⎜⎟ ⎜⎟ ⎝⎠ ∑ (17) ( ) 2 1 11 1 [( ( ) ( 1) )] 2 n n f n nn ir i n i nnn i TT L CT DD DDyjn Fy B FC LLL − − −− = − ⋅Δ = + + ⋅−+−⋅⋅ ⋅ +⋅ ⋅ −⋅⋅ ∑ (18) The total distillate output from all effects is equal to 1 11 2 , 1,2, 3 j n ij ij DDDi + =+ =⋅ + = ∑∑ (19) The energy balance of the thermo-compressor is used to calculate the enthalpy of the discharged steam as shown in equation (20), Desalination, Trends and Technologies 192 () 1 s s gj r d s r D hh D h D D ⎛⎞ ⎛⎞ ⋅+ ⎜⎟ ⎜⎟ ⎜⎟ ⎝⎠ = ⎜⎟ ⎛⎞ ⎜⎟ + ⎜⎟ ⎜⎟ ⎝⎠ ⎝⎠ (20) The most essential part in modeling the ME-TVC desalination system is to determine the ratio of motive steam to entrained vapor ( D s /D r ) in such thermo-compressors. An optimal ratio will improve the unit efficiency by reducing the amount of motive steam (Utomo et al., 2008). This ratio is a direct function of discharge pressure ( P d ), motive steam pressure (P s ) and entrained vapor pressure ( P j ) in terms of compression ratio (CR) and expansion ratio ( ER) as follows (El-Dessouky & Ettouney, 2002; Al-Najem et al., 1997): d j P CR P = (21) s j P ER P = (22) Several methods are available in the literature to evaluate entrainment ratios; most of these methods need lengthy computation procedures and use many correction factors (El-Dessouky & Ettouney, 2002). Two simple methods are used to evaluate this ratio in this chapter: (1) Power’s graphical data method (Al-Najem et al., 1997), (2) El-Dessouky and Ettouney’s semi–empirical model (El-Dessouky & Ettouney, 2002). Although Power’s method is a straightforward and the entrainment ratio can be extracted directly from Fig. 3 Ds/Dr=kg motive steam per kg load 1.6 1.7 1.8 1.9 2 2.2 2.6 3 4 5 6 8 10 15 20 30 50 10 2 5 10 4 5 10 3 6 1.05 1.06 1.07 1.08 1.09 1.10 1.12 1.14 1.16 1.20 1.4 1.3 1.5 1.6 1.7 1.8 2.0 2.2 2.4 2.6 3.0 3.5 4.0 5.0 6 7 8 10 20 15 12 2 0.3 0.25 0.4 0.5 0.6 1.2 0.8 1.0 1.5 2345 Ex p ansion ratio ( motive p ressure/suction p ressure ) Compression ratio (discharge pressure/suction pressure) Fig. 3. Entrainment ratio for different compression and expansion ratios (Power, 1994) New Trend in the Development of ME-TVC Desalination System 193 in terms of compression ratio and expansion ratio, it is too difficult to use in such optimization and simulation models. The developed semi–empirical model in method 2 is applicable only if the motive fluid is steam and the entrained fluid is water vapor (Al-Juwayhel et al., 1997). The pressure and temperature correction factors were eliminated for simplicity and the model equation is modified as shown in equation (23); results were tested and compared with that obtained by Power’s graphical method for validity in the following range of motive pressure 3000 ≥ P s ≥ 2000 (kPa). () () () 1.19 0.015 1.04 0.235 d s r j P D ER D P ⎛⎞ = ⎜⎟ ⎜⎟ ⎝⎠ (23) 4.2 Exergy balance An exergy balance is also conducted to the system to find the exergy destruction (I) in each component; in thermo-compressor, effects, condenser and the leaving streams in kJ/kg according to the following equation: in out IT SE E ο = ⋅Δ = − (24) Where Δ S is the entropy increase, E in is the input exergy and E out is the output exergy. 4.2.1 Thermo-compressor The exergy destruction in the thermo-compressor can be expressed as follows: ()() ( ) ( ) ej s s d o s d r d gj o d gj I D hh TSS D h h TS S ⎡ ⎤ ⎡⎤ =⋅ − −⋅− −⋅ − −⋅ − ⎣⎦ ⎣ ⎦ (25) 4.2.2 Effects The exergy destruction in the first, second and last effect can be expressed respectively as follows; () ()() () 1 111111 11 1 o e s r d fd o d fd f o vf T T IDDhhTSS DL FCTTTIn TT ⎡ ⎤ ⎛⎞ ⎛⎞ ⎡⎤ ⎢ ⎥ ⎜⎟ =+⋅ −−⋅− −⋅⋅− −⋅⋅ − −⋅ ⎜⎟ ⎜⎟ ⎣⎦ ⎜⎟ ⎢ ⎥ ⎝⎠ ⎝⎠ ⎣ ⎦ (26) () () 1 21 21 1 22 122 2 222 2 11 oo er o fo f TT T IDDyFyL BCTTIn DL TTT T FC T T TIn T ⎡⎤ ⎛⎞ ⎛⎞ ⎛⎞ = + − ⋅⋅− +⋅⋅Δ−⋅ − ⋅⋅− ⎢⎥ ⎜⎟ ⎜⎟ ⎜⎟ ⎜⎟ ⎜⎟ ⎜⎟ ⎢⎥ ⎝⎠ ⎝⎠ ⎝⎠ ⎣⎦ ⎡⎤ ⎛⎞ ⎢⎥ ⎜⎟ −⋅⋅ − −⋅ ⎜⎟ ⎢⎥ ⎝⎠ ⎣ ⎦ (27) () () () 2 1 111 1 1 112 1ln n on en n i r i n n o nn i on nn i n f o nf TT ID DDyjnFyL BCTTIn TT TT DL FC T T T TT − − −−− − = ⎡ ⎤ ⎡⎤ ⎛⎞ ⎛⎞ =+ +⋅−+−⋅⋅⋅−+⋅⋅⋅Δ−⋅ ⎢ ⎥ ⎜⎟ ⎜⎟ ⎢⎥ ⎜⎟ ⎜⎟ ⎢ ⎥ ⎝⎠ ⎝⎠ ⎣⎦ ⎣ ⎦ ⎡⎤ ⎛⎞ ⎛⎞ ⎢⎥ ⎜⎟ −⋅⋅− −⋅⋅ − −⋅ ⎜⎟ ⎜⎟ ⎜⎟ ⎢⎥ ⎝⎠ ⎝⎠ ⎣⎦ ∑ (28) Desalination, Trends and Technologies 194 4.2.3 Condenser and leaving streams The exergy destruction in the condenser, and in the leaving streams, D r ,D f and B n can be expressed using the following equations respectively: () 1ln f o cnn c fc o nc T T IDL MCTT T TT ⎡ ⎤ ⎛⎞ ⎛⎞ =⋅⋅− − ⋅⋅ −−⋅ ⎢ ⎥ ⎜⎟ ⎜⎟ ⎜⎟ ⎜⎟ ⎢ ⎥ ⎝⎠ ⎝⎠ ⎣ ⎦ (29) () ln vj Dr r vj c o c T IDCTTT T ⎡ ⎤ ⎛⎞ =⋅⋅ −−⋅ ⎢ ⎥ ⎜⎟ ⎜⎟ ⎢ ⎥ ⎝⎠ ⎣ ⎦ (30) () ln vj Df f vj c o c T IDCTTT T ⎡ ⎤ ⎛⎞ =⋅⋅ −−⋅ ⎢ ⎥ ⎜⎟ ⎜⎟ ⎢ ⎥ ⎝⎠ ⎣ ⎦ (31) () ln n Bn n n c o c T IDCTTT T ⎡ ⎤ ⎛⎞ =⋅⋅ −−⋅ ⎢ ⎥ ⎜⎟ ⎜⎟ ⎢ ⎥ ⎝⎠ ⎣ ⎦ (32) 4.3 Thermal load The heat transfer area of an effect can be obtained from the latent heat of condensation (thermal load) of each effect as shown in equation (33), where ∆T e is the temperature difference across the heat transfer surface. ee e QUA T = ⋅⋅Δ (33) Therefore, the heat transfer area for the first, second and last effect can be obtained as follows: () () 1 11 sr d f d e ed DD h h A UTT ⎡ ⎤ +⋅− ⎣ ⎦ = ⋅− (34) () 111 2 212 () r e ev DD y F y L A UTT + ⋅− ⋅ ⋅ = ⋅− (35) () 2 11 1 1 [( ( ) ( 1) ] n nir in i n en vn n DDDyjnFyL A UT T − − − = − ++⋅−+−⋅⋅⋅ = ⋅− ∑ (36) The overall heat transfer coefficient (U e ) depends mainly on the type, design and material of the tubes (El-Dessoukey et al., 2000), and for simplicity it can be calculated as follows (El-Dessouky & Ettouney, 2002): () () ( ) 23 1939.4 1.40562 0.0207525 0.0023186 1000 ii i ei TT T U +⋅− ⋅+ ⋅ = (37) New Trend in the Development of ME-TVC Desalination System 195 The cooling seawater flow rate can be obtained by applying the energy conservation law on the condenser as shown below: () fn c f c DL M CT T ⋅ = ⋅− (38) The latent heat of condensation of the un-entrained vapor D f flowing to the condenser is used to increase cooling seawater temperature to feed seawater temperature. The thermal load of the condenser is used to calculate the condenser heat transfer area as follows: () fn c c c DL A ULMTD ⋅ = ⋅ (39) The logarithmic mean temperature difference and the overall heat transfer coefficient of the condenser can be obtained from equations (40) and (41) respectively (El-Dessouky & Ettouney, 2002). () ( ) () () () ln vn f vn c c vn f vn c TT TT LMTD TT TT −− − = − − (40) () () 23 25 7 1.7194 3.2063 10 1.5971 10 1.9918 10 cvnvnvn UTTT −− − =+⋅⋅−⋅⋅+⋅⋅ (41) Similarly, the heat transfer area of the feed heaters can be expressed as follow assuming that the overall heat transfer coefficient of the feed heaters are equals to that of the condenser. ( ) 1 1 () ln , 1, 2, 2 ()() if vifi fi ffifi vifi iF C T T T Ain UTT TT + + ⋅⋅Δ − = ⋅=− ⋅− − (42) 4.4 System performance The system performance of the ME-TVC model can be evaluated in terms of the following: 4.4.1 Gain output ratio, GOR The gain output ratio is one of the most commonly performance used to evaluate thermal desalination processes. It is defined as the ratio of total distilled water produced (D) to the motive steam supplied (D s ). s D GOR D = (43) 4.4.2 Specific heat consumption, Q d This is one of the most important characteristics of thermal desalination systems. It is defined as the thermal energy consumed by the system to produce 1 kg of distilled water, where L s is the motive steam latent heat in kJ/kg Desalination, Trends and Technologies 196 ss d DL Q D ⋅ = (44) 4.4.3 Specific exergy consumption, A d The specific exergy consumption is one of the best methods used to evaluate the performance of the ME-TVC based on the Second Law of thermodynamics. It considers the quantity as well as the quality of the supplied motive steam. It is defined as the exergy consumed by the motive steam to produce 1 kg of distillate when the steam is supplied as saturated vapor and leaves as saturated liquid at ambient temperature equal to T o , according to the following equation (Darwish et al., 2006): ()() s d s fd o s fd D AhhTSS D ⎡ ⎤ =⋅ − −⋅− ⎣ ⎦ (45) where h s , S s are the inlet motive steam enthalpy and entropy at saturated vapor and h fd , S fd are that of the outlet condensate at saturated liquid. 4.4.4 Specific heat transfer area, A t The specific total heat transfer area is equal to the sum of the effect, feed heaters and the condenser heat transfer areas per total distillate product (m 2 /kg/s). 2 111 2 j nn fi deiei c ii i iji A At A A A DDDDD − =+= =⋅ + + + ∑∑∑ (46) 4.4.5 Specific exergy destruction, I t This term shows the total exergy destruction due to heat transfer and in the thermo- compressor, evaporators, condenser and the leaving streams per unit of distillate water. i t I I D = ∑ (47) where I i is the exergy destruction in each component in kJ/kg. 4.5 Model validity Engineering Equation Solver (EES) software is used to evaluate the ME-TVC system performance. The validity of the model was tested against some available data of three commercial units having different unit capacities: ALBA in Bahrain (2.4 MIGD), Umm Al- Nar in UAE (3.5 MIGD) and Al-Jubail in KSA (6.5 MIGD). The results showed good agreements as shown in Table 2. It is also cleared from Table 2 that the available data of Al-Jubail unit is limited in the literature. Hence, the developed mathematical model is used to predict the missing values in order to evaluate the system performance of this plant. New Trend in the Development of ME-TVC Desalination System 197 Desalination Plant ALBA UMM Al-NAR AL-JUBAIL Number of effects, n 4 6 8 Operating and Design Parameters ModelActualModelActualModel Actual Motive pressure, bar 21 21 2.8 2.8 2.7 2.7 Top brine temperature, o C 63 63 63 62 63 NA Minimum brine temperature, o C 48 48 44 43 42 NA Feed sea water temperature, o C 43 43 40 40 40 NA Motive steam flow rate, kg/s 8.5 × 2 8.3 × 2 11×2 10.65×2 15.5×2 NA Temperature drop per effect, o C 5 5 3.8 3.8 3 NA Thermo-compressor Design Compression ratio 1.57 NA 1.7 NA 1.75 NA Expansion ratio 120 NA 18.11 NA 18.7 NA Motive to entrained vapor ratio 0.58 NA 0.885 NA 0.98 NA System Performance Distillate production, kg/s 123 127 184.2 184.38 340.4 342.22 Gain output ratio 7.23 7.5 8.37 8.6 10.9 9.8 Specific heat consumption, kJ/kg 348.4 NA 292.1 287.5 223 NA Specific exergy consumption, kJ/kg 127.7 NA 74.6 NA 56.44 NA Specific heat transfer area, m 2 /kg/s 244.2 NA 335.6 310 452.2 NA Specific exergy destruction, kJ/kg/s 94.65 NA 54.24 NA 41.16 NA Table 2. Mathematical model calculations against some commercial plants. 5. Sensitivity analysis The new trend of combining ME-TVC desalination system with a conventional Multi effect distillation (MED) unit has been used lately in different large projects and has been also discussed in a few published works (Al-Habshi, 2002), (Darwish & Alsairafi, 2004) and (Bin Amer, 2009). Thus, a sensitivity analysis will be presented in this section to investigate the system performance variations of Al-Jubail ME-TVC unit. This project belongs to Marafiq Company and it is currently considered as the largest ME-TVC desalination plants in the world, it consists of 27 units each of 6.5 MIGD as shown in Fig.4. The available data of this unit in the literature are: the gain output ratio, number of effect, motive pressure and the unit capacity. These data are used along with the model equations to evaluate the system performance of the plant. Fig.5. shows the effect of motive steam flow rate on the vapor formed in each effect of this unit, at T 1 = 63 o C and ΔT=3 o C. The total distillate production can be controlled by adjusting the motive steam flow rate. The reason is when the motive steam flow rate increases the entrained vapor also increases for constant entrainment ratio ( D s /D r ), this will lead to generate more vapor and consequently more distillate water. The variation of the gain output ratio and the distillate production as a function of top brine temperature is shown in Fig.6. It is cleared that as the top brine temperature increases the distillate output production decreases and consequently gain output ratio decreases. This is Desalination, Trends and Technologies 198 Distillate water Vapor Seawater Brine T 1 = 63 T 2 = 60 T 3 = 57 T 4 = 54 T 5 = 51 T 6 = 48 T 7 = 45 T 8 = 4 2 D 1 = 30.94 D 2 = 30.05 D 3 = 29.17 D 4 = 2 8 .3 D 5 = 26.76 D 6 = 25.96 D 7 = 25.47 D 8 = 25.29 D s =15.5 P s = 27 0 [k pa] D r = 15.73 [kg/s] M c = 1581 [kg/s] T f1 = 58 [C ] D f = 12.56 [kg/s] D = 34 0. 4 [k g/s ] B 8 = 458.9 F = 1021 [kg/s] T f2 = 55 [C] T f3 = 52 [C] n = 8 MI GD = 6 .46 5 GR = 10.98 Q d = 222.9 [kJ/kg] A d =56.44 [kJ/kg] I t =41.16[kJ/kg/s] A t =452.2 T 1 = 63 T 2 = 60 T 3 = 57 T 4 = 54 D 1 = 3 0 .9 4 D 2 = 30.05 D 3 = 29.17 D 4 = 28.3 D r = 15.73 [kg/s] D s =15.5 P s = 27 0 [ kpa ] B 4 = 22 1.9 Fig. 4. Schematic diagram similar to Al-Jubail (MARAFIQ) ME-TVC unit, 6.5 MIGD. [...]... availability analysis of single and multi-effect systems Desalination, Vol 110 ( 199 7) 223 – 238 Al-Shammiri, M & Safar, M ( 199 9) Multi-effect desalination plants: state of the art Desalination, Vol 126 ( 199 9) 45- 59 Ashour, M (2002) Steady state analysis of the Tripoli West LT-HT-MED plant Desalination, Vol 152 (2002) 191 - 194 Bejan, A.; Michael, J & George, T ( 199 6) Thermal design and optimization, John Wiley... Gendel, A ( 198 5) Ashdod multi-effect low temperature desalination plant report on year of operation Desalination, Vol 55 ( 198 5) 13-32 Hamed, O.; Zamamiri, A.; Aly, S & lior, N ( 199 6) Thermal performance and exergy analysis of a thermal vapor compression desalination system Energy Conversion Mgmt, Vol 37 ( 199 6) 3 79- 387 Michels, T ( 199 3) Recent achievements of low temperature multiple effect desalination. .. pressure of 25 bars (Michels, 199 3) The next unit capacity was 2 MIGD which started up in 199 5 in Sicily (Italy) It consisted of four identical units; each had 12 effects, with a gain output ratio of 16 The steam was supplied from two boilers at 45 bars to the plant (Temstet, 199 6) More units of 1, 1.5 and 2 MIGD were also ordered and commissioned in UAE between 199 6 – 199 9 due to excellent performance... 0.756 2 49. 6 93 .15 699 .8 10.27 10.26 6 56 45.8 2.04 1.82 263 0.734 240.1 89. 5 94 7.8 10.67 11.72 7 56 45.3 1.78 1.85 270 0.744 216.3 80.67 1150 11.87 13.28 8 56 43.3 1.81 2 300 0.831 202 75.3 1016.8 12.7 14.57 9 57 42.8 1.77 2.2 307 0 .90 2 187 69. 82 98 2 13.7 15.8 10 59 42.8 1.8 2.43 307 1 174.8 65.42 8 79 14.61 16 .93 11 60.5 42.8 1.77 2.6 307 1.01 161.5 60.5 851.5 15.78 18.1 12 62.5 42.8 1. 79 2.85 307 1.22... Simulation and economic study of the MED-TVC units at Umm AlNar desalination plant Thesis report, (2002) UAE Al-Juwayhel, F.; El-Dessouky, H & Ettouney, H ( 199 7) Analysis of single-effect evaporator desalination systems combined with vapor compression heat pumps Desalination, Vol 114 ( 199 7) 253-275 Al-Najem, N.; Darwish, M & Youssef, F ( 199 7) Thermo-vapor compression desalination: energy and availability... (20 09) Development and optimization of ME-TVC desalination system Desalination, Vol 2 49 (20 09) 1315-1331 Choi, H.; Lee, T.; Kim, Y & Song, S (2005) Performance improvement of multiple-effect distiller with thermal vapor compression system by exergy analysis Desalination, Vol 182 (2005) 2 39- 2 49 Cipollina, A.; Micale, G & Rizzuit, L (2005) A critical assessment of desalination operation in Sicily Desalination, ... TVC/MEB and MSF Desalination, Vol 170 (2004) 223-2 39 Darwish, M.; Alasfour, F & Al-Najem, N (2002) Energy consumption in equivalent work by different desalting methods case study for Kuwait Desalination, Vol 152 (2000) 83 -92 Darwish, M.; Al-Juwayhel, F & Abdulraheim, H (2006) Multi–effect boiling systems from an energy viewpoint Desalination, Vol 194 (2006) 22- 39 El-Dessouky, H & Ettouney, H ( 199 9) Multiple-effect... as shown in Fig 15 206 Desalination, Trends and Technologies 11.5 Ras Laffan Gain Output Ratio 11.0 10.5 10.0 Al-Jubail Fujairah 9. 5 9. 0 Al-Hidd 8.5 Sharjah 8.0 2004 2005 2006 2007 2008 20 09 2010 Year Fig 14 The increase in the gain output ratio of new ME- TVC projects 1.6 Ras Al-Khaimah Water cost, US $/m3 1.4 1.2 1.0 Al-Jubail 0.8 Al-Fujairah 0.6 0.4 199 6 Al-Tawelah A1 199 8 2000 2002 2004 2006 2008... F (2005) Advanced MED process for most economical sea water desalination Desalination, Vol 182 (2005) 187- 198 Peultier, J.; Baudu, V.; Boillot, P & Gagnepain, J (20 09) New trends in selection of metallic material for desalination industry Proceeding of IDA world congress on desalination and water reuse Dubai, November, 20 09, UAE Power, R ( 199 4) Steam Jet Ejectors for the Process Industries, McGraw-Hill,... destruction in the effects, thermo-compressor, condenser and leaving streams of Al-Jubail unit 202 Desalination, Trends and Technologies Fig 12 The exergy destruction in the effects of ALBA, Umm Al-Nar and Al-Jubail units 6 Development of ME-TVC desalination system The first ME-TVC desalination unit of 1 MIGD capacity was commissioned in 199 1 in the UAE It has four effects with a gain output ratio . two boilers at 45 bars to the plant (Temstet, 199 6). More units of 1, 1.5 and 2 MIGD were also ordered and commissioned in UAE between 199 6 – 199 9 due to excellent performance of the previous. −⋅ ⎜⎟ ⎜⎟ ⎜⎟ ⎢⎥ ⎝⎠ ⎝⎠ ⎣⎦ ∑ (28) Desalination, Trends and Technologies 194 4.2.3 Condenser and leaving streams The exergy destruction in the condenser, and in the leaving streams, D r ,D f and B n can be. in the next effect i+1 and so on up to the last effect n and can be calculated as follow: 1 ,1,2, ii TTT i n + = −Δ = (1) Desalination, Trends and Technologies 190 The temperature of