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Flash Desalination Processes
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E-type shells in shell-and-tube heat exchangers: Ebert and Panchal equation, for crude oil fouling, Eckert number, Eddy viscosity: Eddy diffusivity, of heat, Edge, D, Edwards, D K EEC code for thermal design of heat exchangers, Effective diffusivity, Effective thermal conductivity of fixed beds, Effective tube length in shell-and-tube heat exchangers, Effectiveness of a heat exchanger: Efficiency of fins, Eicosane: Eicosene: Ejectors, in flash distillation plant, EJMA (Expansion Joint Manufacturers Association), standards for expansion bellows Elastic properties of solids: El-Dessouky, H,
Flash Desalination Processes
Electrical enhancement processes, in heat transfer augmentation, Electric fields, effect on properties of rheologically complex materials, Electric fields, in augmentation of condensation, Electrical process heater, specification of, Electrokinetics, for heat transfer augmentation in microfluidic systems, Electromagnetic theory of radiation, Electrostatic fields in augmentation of heat transfer, Elements: Elhadidy relation between heat and momentum transfer, Embedding methods for radiative heat transfer in nonisothermal gases, Embittlement, of stainless steels, Emission of thermal radiation, in solids, Emissivity: Emitting media, interaction phenomena with, Emulsions, viscosity of, EN13445 (European Pressure Vessel Codes), design of heat exchangers to, Enclosures: Energy equation: Energy recovery, maximum, in heat exchanger network design, Enhanced surfaces, fouling in, Enhancement devices: Enlargements in pipes: Enthalpy: Entrainment in annular gas-liquid flow Entrance effects in heat and mass transfer: Entrance lengths, hydrodynamic in pipe flow, Entrance losses for tube inlet in shell-and-tube heat exchanger, Entry losses in plate heat exchangers, Entropy generation and minimisation Environmental impact, of fouling, Eotvos number: Epstein, N, Epstein matrix, for fouling, Equalizing rings, for expansion bellows, Equilibrium interphase: Equilibrium vapor nucleus, Equivalent sand roughness, Ergun equation, for pressure drop in fixed beds ESDU correlations: Esters: Ethane: Ethanol: Ethers: Ethyl acetate: Ethylacetylene: Ethylacrylate: Ethylamine: Ethylbenzene: Ethyl benzoate: Ethyl butanoate: Ethylcyclohexane: Ethylcyclopentane: Ethyl formate: Ethylene: Ethylene diamine: Ethylene glycol: Ethylene oxide: Ethylmercaptan: 1-Ethylnaphthalene: 2-Ethylnaphthalene: Ethyl proprionate: Ethyl propylether: Ettouney, H, Euler number: Eutectic mixtures, condensation of forming immiscible liquids, Evaporation: Evaporative crystallisers, Evaporators: Exergy, definition of, Exergy analysis, Exit losses for tubes in shell-and-tube exchanger, Expansion bellows, for shell-and-tube heat exchangers: EJMA (Expansion Joint Manufacturers Association), standards for Expansion joints, mechanical design of: Expansion of tubes into tube sheets: Expansion turbine, lost work in, Explosively clad plate, Explosive welding of tubes into tube sheets Explosive expansion joints, Extended surfaces (see also Fins) Externally induced convection, in kettle reboilers, Extinction coefficient, Extinction efficiency, Eyring fluid (non-Newtonian),
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E El-Dessouky, H,
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Flash Desalination Processes

DOI 10.1615/hedhme.a.000384

3.22 FLASH EVAPORATION
3.22.2 Flash desalination processes

H. El-Dessouky and H. Ettouney

On an industrial scale the flash desalination process has a multistage configuration for flash evaporation. The main elements of the process include the brine heater and the flashing stages. Other process units include the feed intake, brine disposal lines, deaerator, chemical dosing, pumping station, vacuum ejectors, and the control room. The most common industrial process is the multistage flashing process with brine circulation (MSF). On the other hand, the once through multistage flashing process (MSF-OT) is found on a very limited scale. Also, it should be noted that the single stage flashing system (SSF) combined with a brine heater is not used on industrial scale because of its low performance. However, discussion of the SSF process and development of a mathematical model for it are necessary to have better understanding of the more complex processes found in the multistage flashing systems.

The most characteristic feature of the flash desalination process is that vapor formation takes place within the liquid bulk instead of the surface of hot tubes. The hot brine is allowed to flow freely and flash in a series of chambers; this feature keeps the hot and concentrated brine from the inside or outside surfaces of heating tubes. This is a major advantage over the original and simple concept of thermal evaporation, where submerged tubes of heating steam are used to perform fresh water evaporation. The performance of submerged tubes was far from satisfactory, where salt scale is formed progressively on the outside surface of the tubes. The formed scale has a low thermal conductivity and acts as an insulating layer between the heating steam and the boiling seawater. Consequently, the evaporation rate is drastically reduced and cleaning becomes essential to restore the process efficiency.

Earlier designs of the flash desalination process were developed on commercial scale in the early 1950’s. Silver (1970) modified these earlier designs and devised the MSF process, where the number of flashing stages was much larger than the thermal performance ratio. The development optimized the system heat transfer area and the number of flashing stages. Since the establishment of the process in the late fifties, a huge amount of field experience has been accumulating in process technology, system design, construction practice, operation, and maintenance. Developments addressed several operational problems that include scale formation, foaming, fouling, and corrosion. The experience gained has led to use of inexpensive construction material capable of withstanding the harsh conditions at high seawater salinity. The MSF system does not include moving parts, other than conventional pumps. Construction of the MSF plants is simple and contains a small number of connections, which limits leakage problems and simplifies maintenance work. It is believed that the MSF system has remained the optimum choice for large capacity plants for desalination of seawater for the following reasons:

  • The conservative nature of the desalination owner.

  • The product is a strategic life-supporting element.

  • Extensive experience in construction and operation.

  • Process reliability.

  • Limited experience, small database, and unknown risks with new technologies.

Since inception, several developments have been achieved in system design and operation. These developments include the following:

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