Processing facilities heat exchangers

Condensable hydrocarbon components are usually removed from gas to avoid liquid drop out in pipelines, or to recover valuable natural gas liquids where there is no facility for gas export. Cooling to ambient conditions can be achieved by air or water heat exchange, or to sub zero temperatures by gas expansion or refrigeration. Many other processes such as compression and absorption also work more efficiently at low temperatures. 

Most heat transfer processes used in production facilities involve combinations of conduction and convection ti ansfer processes. For example, in heat exchangers the transfer of heat energy from the hot fluid to the coLl fluid involves tliree steps. First, the heat energy is transferred from the luH fluid to the exchanger tube, then through the exchanger tube wall, ctud finally from the tube wall to the cold fluid. The first and third steps are convection transfer processes, while the second step is conduction process. 

The crude separation facilities for a possible Troll oil development are shown In Fiq. 6. The crude stream from subsea wells with an expected platform arrival temperature of circa 5°C will be warmed by heat exchange with the export crude free water is knocked out In a 1st stage separator and the crude 1s then heated to the desired process temperature (> 40°C), prior to entering the second stage separator. Provision for the injection of demulsifier is required at the wellhead and upstream of the crude heater. 

In principle, the flowsheet of an industrial facility is similar to those of the different hydrotreating processes (Figure 5.2-42) [61]. The feedstock C4 cut rid of water is pressurized to about 15 to 20 bar by pumping, injected with a hydrogen-rich gas and then, preheated by heat exchange with the reaction effluent and by steam. In a downflow stream, it then enters the reactor, which operates in a gas-liquid mixed phase with one or more catalyst beds (palladium, rhodium on inert alumina). After cooling, the isomerization products are flashed... 

Major equipment factor estimates. Major equipment factor estimates are made by applying multipliers to the costs of all major equipment required for the plant or process facility. Different factors are applicable to different types of equipment, such as pumps, heat exchangers, and pressure vessels. Equipment size also has an effect on the factors. 

Versatile, i.e. capable of testing different types of components (heat exchangers, electrolysers, thermochemical cycles) and/or sub and integrated processes in a view of demonstration. This versatility criterion also denotes the capability for PROHYTEC to be a plug and play like facility. 

Power or thermal transients initiated in nuclear reactor SSC, stress on heat exchanger or other component in contact with balance of plant Transient causes stress on SSC induces possible transient in process facility... 

JAEA conducted an improvement of the RELAP5 MOD3 code (US NRC, 1995), the system analysis code originally developed for LWR systems, to extend its applicability to VHTR systems (Takamatsu, 2004). Also, a chemistry model for the IS process was incorporated into the code to evaluate the dynamic characteristics of process heat exchangers in the IS process (Sato, 2007). The code covers reactor power behaviour, thermal-hydraulics of helium gases, thermal-hydraulics of the two-phase steam-water mixture, chemical reactions in the process heat exchangers and control system characteristics. Field equations consist of mass continuity, momentum conservation and energy conservation with a two-fluid model and reactor power is calculated by point reactor kinetics equations. The code was validated by the experimental data obtained by the HTTR operations and mock-up test facility (Takamatsu, 2004 Ohashi, 2006). 

A, 5A, and 13X zeolites are the predominant adsorbents for CO 2 removal by7 temperature-swing processes. The air fed to an air separation plant must be H20- and C02-free to prevent fouling of heat exchangers at cryogenic temperatures 13X is typically7 used here. Another application for 4A-type zeolite is for CO2 removal from baseload and peak-shaving natural gas liquefaction facilities. 

FIGURE 10.1 Flowsheet for the electric furnace process for the production of elemental phosphorus. Phossy water from the phosphorus phase separator (sump) is normally maintained in a closed-circuit holding pond system which also provides the feedwater for the phosphorus direct contact condenser. Some facilities have a further indirect, heat exchange condenser for the carbon monoxide stream, after the direct contact condenser. 

Table 4 presents the direct construction costs for the two plants. Equipment costs must be adjusted to account for hydrogen production these costs include the intermediate heat exchanger ( 56 M), reactor-process piping ( 38 M), primary helium circulator ( 33 M), and intermediate loop circulator ( 22 M) (for a total of 149 M). These costs are added to Account 22. On the other hand, 84% of the Fixed Capital Investment of the S-I hydrogen production facility ( 571.53 IM x 0.84 = 480 M) in account 23 (Chemical Facility) replaces account 23 (Turbine-Generator). Also, the initial chemical inventory (primarily iodine) is equal to 114.8 M x 0.84 = 96 M. (Although there is an implicit assumption in [13] that all iodine is recycled, this assumption is challenged in [14].)... 

Air-cooled condensers are especially attractive at locations where water is scarce or expensive to treat. Even when water is plentiful, air coolers are frequently the more economical alternative. Elimination of the problems associated with the water side of water-cooled equipment, such as fouling, stress-corrosion cracking, and water leaks into the process, is an important advantage of air-cooled equipment. In many cases, carbon steel tubes can be employed in air-cooled condensers when more expensive alloy tubes would otherwise have been necessary. The use of air-cooled heat exchangers may eliminate the need for additional investment in plant cooling water facilities. 

Some processes (e.g., water and wastewater treatment facilities) include concrete vessels plus traditional pumps, heat exchangers, and mixers. To cost such facilities, it is more realistic to report the sum of the L + M module costs and the delivery, taxes, and duties. We refer to this cost as the physical module (PM) cost. 

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