Hydrocarbon processing diagram

FIGURE 7.1. Simplified Process Diagram Hydrocarbon Leak From Pipe (from Cullen, 1990). 

Figure 8.3.1 is a typical process diagram for tlie production of ammonia by steam reforming. Tlie first step in tlie preparation of tlie synthesis gas is desulfurization of the hydrocarbon feed. Tliis is necessary because sulfur poisons tlie nickel catalyst (albeit reversibly) in tlie reformers, even at very low concentrations. Steam reforming of hydrocarbon feedstock is carried out in tlie priiiiiiry and secondary reformers. 

Figure 14-21. Mollier diagram with expansion lines drawn for turbines with different numbers of stages. Note right vertical axis. Temperatures correspond to heavy Mollier lines and not the uniform graph paper lines. (Used by permission Althearn, F. H. Hydrocarbon Processing, p. 83, Aug. 1979. Gulf Publishing Co. All rights reserved.)...

Figure D-5 Pressure-enthalpy diagram of ethane. (From Hydrocarbon Processing 50(4) 140, 1971.)... 

Browning, R. L. Analyze Losses by Diagram. Hydrocarbon Processing, 54 253-257,1975. 

Books quickly become outdated, and many of the processes described are obsolete or at best obsolescent. More up-to-date descriptions of the processes in current use can be found in the technical journals. The journal Hydrocarbon Processing publishes an annual review of petrochemical processes, which was titled Petrochemical Developments and is now called Petrochemicals Notebook this gives flow diagrams and brief process descriptions of new process developments. 

In a first step of the process propane, butane, pentane, or hexane is used to extract vanidyl porphyrins from residual oil. The liquid extract of hydrocarbon and porphyrins is next subjected to supercritical CO2 exU action between 90and 130 °Fand 1,075 to 8,000 psi. At almost all combinations of these pressures and temperatures the C3 through C(, paraffins are miscible in CO2. With a supercritical extraction column we wonder what ratio of C02-lo-extract would result in purified oil and what happens to the vanidyl porphyrins. In the process diagram and description, the supercritical C02-liquid solvent extract is expanded to an unspecified different pressure and temperature. But, it is important to relate that pentane and hexane are miscible with CO2 at room temperature and 800 psi so that the expansion would have to be to conditions higher in temperature and lower in pressure to separate CO2 and hexane. For propane the miscibility conditions extend to much lower pressure and so the separation of propane from carbon dioxide becomes problematic. 

In Hydrocarbon Processing, 54 (11), 97-222 (1975), process flow diagrams and descriptions are given for a large number of petrochemical processes. For each of the following processes, list the separation operations in Table 1.1 that are used. 

Figure 6.17 Typical startup stability diagram. (Henry Z. Kister, Hydrocarbon Processing, February 1979. Reprinted courtesy of Hydrocarbon Processing.)...

Figure 23,2.6. GCW process diagram. Effective hydrocarbon stripping in the water column is observed in these systems using a vacuum extraction. A circulation cell is created by directional flow of water in the vertieal direetion creating a capture zone extending several meters from the well. In addition a bioreactor (high surface area baeteiial biofilm) can be used in the system to degrade low volatile contaminants [Adapted from Bemhartt et al., U.S. Patent 5,910,245,1999]...

Figure 9-29. Schematic flow diagram of Unisulf process Fenton and Gowdy, 1981). Hydrocarbon Processing, April, 1982...

Figure 9-40. Sulfint process flow diagram Mackinger et al., 1982). Courtesy of Hydrocarbon Processing, March, 1982...

Figure 15-12. Flow diagram of reformer system with membrane hydrogen recovery unit on offgas (Yamashim eta ., 1988. Reproduced withpemisskm from Hydrocarbon Processing, Februaiy 1985...

A schematic diagram of the liquid solvent extraction process is illustrated in Figure 1. Where the production of liquid hydrocarbons is the main objective an hydrogenated donor process solvent is used, whereas in the production of needle coke this is not necessary and a coal derived high boiling aromatic solvent may be used (e.g. anthracene oil). An essential economic requirement of the process is that a high extraction yield of the coal is obtained and this will depend upon the coal used and the digestion conditions. 

FIGURE 6.11 Diagram of the processing technique used to prepare Cu-Ce02-YSZ anodes for direct oxidation of hydrocarbon fuels by preparing a porous preform of YSZ and then infiltrating it with cerium nitrates to form ceria and then with copper nitrates to form metallic copper [84]. Reprinted from [84] with permission from Elsevier. 

Flow diagram of light hydrocarbon refrigeration process. 

Consecutively, the heavy paraffins are cracked into lighter hydrocarbon fractions by hydro-cracking. For example, for the Shell Middle Distillate Synthesis (SMDS) process, the liquid product stream is composed of 60% gasoil (diesel), 25% kerosene and 15% naphtha. The gaseous product mainly consists of LPG (a mixture of propane and butane) (Eilers et al., 1990). Figure 7.3 shows a simplified diagram comprising all process steps to produce synthetic hydrocarbons from biomass, natural gas and coal. 

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