Shell flow scheme

The Sulfinol process from Shell Development Company is a good example of the physical/chemical type of process. It blends a physical solvent and an amine to obtain the advantages of both. The physical solvent is Sulfolane (tetrahydrothiophene dioxide) and the amine is usually DIPA (diisopropanol amine). The flow scheme is the same as for an amine plant. ... 

The Shell Sulfinol Process is used for removal of acidic constituents such as H2S, CO2, COS, etc. from a gas stream. Improved performance over other processes is due to the use of an organic solvent, Sulfolane (tetrahydrothiophene dioxide), mixed with an aqueous alkanolamine. Relative proportions of Sulfolane, alkanolamine, and water, as well as the operating conditions, are tailored for each specific application. Simultaneous physical and chemical absorption under feed gas conditions is provided by this Sulfinol solvent. Regeneration is accomplished by release of the acidic constituents at near atmospheric pressure and a somewhat elevated temperature. The flow scheme (Figure 4) is very similar to that of an aqueous alkanolamine system since it involves only absorption, regeneration and heat exchange under typical alkanolamine treater conditions. 

Shell also offers for license a -selective version of the Shell ADIP Process. The ADIP process, which has a flow scheme very similar to Sulfinol, can be used to treat the Sulfinol acid gas to raise the H2S concentration by selectively rejecting the CO2. Some integration of the SCOT process with the ADIP process is often possible thus, reducing overall equipment and operating costs. Costs for the Claus plant are substantially reduced when "selective" ADIP is applied. Two selective ADIP plants are scheduled to come on stream in the first half of 1979. 

Figure 3. Flow scheme of the Shell higher olefin process (SHOP). AO = a-olefin c.w. = cooling water.

SHELL MIDDLE DISTILLATE SYNTHESIS SIMPLIFIED FLOW SCHEME... 

The flow scheme of the miniplant installation is shown in Fig. 2. The reactor consists of a cylindrical stainless steel shell H and an internal tube 12 which contains the catalyst bed. 

When the required product is syngas, Texaco uses a special heat exchanger in place of the direct quench to cool the raw syngas [17]. Shell utilizes a heat exchanger in either case. The Shell process flow scheme is illustrated in Figure 14 [18]. 

Figures Flow scheme of the Shell higher-alkene process (SHOP).

Shell has been involved in syngas chemistry for many years, giving special attention to the options for the conversion of natural gas into more easily transportable liquid hydrocarbons. The first result of this effort has been the Shell Middle Distillate Synthesis (SMDS) plant commissioned in Malaysia in 1993. This plant makes use of cobalt FT catalyst and tubular reactors in the Heavy Paraffin Synthesis unit (HPS). A simplified flow scheme of this plant is presented in Figure 7. 

Figure 7 - Simplified Flow Scheme of the Shell SMDS plant in Malaysia...

An important technique used in the bioartiflcial liver is based on the immobilization of the cells on the inner or outer surface of hollow fibers made of porous material. This configuration allows oxygen and other nutrients to be supplied to cells by means of a liquid stream different from the blood or plasma stream. The nutrient stream flows in the membrane side where cells are fixed, whereas blood plasma flows in the other side. The flow scheme can be co-current or counter current but usually the co-current scheme is adopted. The module is a bundle of hollow fibers contained in a cylindrical shell. A main problem to study is the level of O2 concentration in the cells at the outlet of the feed stream actually, this section is the most critical, owing to oxygen consumption along the fiber from the inlet to the outlet section. 

Shell Coal Gasification Process-Typical Flow Scheme. 5-47... 

Figure 3. Shell Middle Distillate Synthesis — simplified flow scheme.

Operation at very low temperatures with very sharp separations results in relatively complex flow schemes. This, combined with the need for low level refrigeration, leads to high plant costs. As a result, most applications of the Rectisol process represent relatively difficult gas treating conditions where other gas treating processes are not suitable for one reason or another. Typical applications are the purification of gas streams in the heavy oil partial oxidation processes of Shell and Texaco and the Lurgi coal gasification process, as used at the Sasol plants in South Africa. 

For the fixed-bed tubular reactor, the reaction exotherm is controlled by placing the catalyst in a series of tubes. The heat generated by reaction in the tubes is removed by circulating cooling water on the shell side of the reactor. The effluent from this reactor passes to a second packed-bed reactor for further conversion. Product recovery follows the same flow scheme as for the packed-bed reactor with recycle [130]. 

FIGURE 38.7 Scheme of a tube-in-shell configuration with shell side flow parallel to the lumen side one. (a) Module and (b) un-uniform packing/section view. 

The heat exchanger is of shell-and-tube type, where the combustion gases flow in tubes and the heated air in the shell. This construction was selected because of the easy removal of deposits. The principle scheme is shown in Fig 4. 

Loop seal. In some low-pressure steam reboilers the condensate pot is replaced by a loop seal (Fig. 17.Ih). In this arrangement, increasing the flow to the reboiler raises the pressure in the reboiler shell, which in turn lowers the liquid level in the reboiler and exposes more tube area. The dynamics of this system are similar to that of the condensate outlet scheme. The height of liquid in the loop is typically 5 to 10 ft. The system can be troublesome when the reboiler heat load or the steam mains pressure tend to fluctuate, and it is usually best avoided. 

In Figure 25.22, the scheme of experimental setup used for membrane extraction experiments was presented. The setup consisted of membrane contactor with aqueous and organic circuits, two pumps, and the control equipment flowmeters, pressure gauges, and valves. Two phases aqueous and organic solutions circulated countercurrently. Membrane contactor X50 2.5 x 8 Liqui-Cel Extra-Flow, Celgard, was used in the system. The characteristics of the membrane were shown in Table 25.17. The small volume module houses 11,000 capillaries with 1.9 m inner surface area. The module possesses the central baffle, which enables uniform flow inside the shell. 

A schematic representation of these two possibilities is shown in Fig. 1.1. The reaction chamber is the inner tube where a fixed bed of catalyst is assumed to be present. The permeate chamber is the annular region between the inner tube and the shell. In the permeate region, the sweep gas flows in co-current mode in the case (a) and in counter-current mode in the case (b). One or more products of the reaction are shown to flow through the membrane from the catalytic-fixed bed toward the permeate region. However, in co-current scheme an inversion of the flux is theoretically possible at some distance from the inlet section since the flux... 

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