High propane recovery process and configurations
a high-efficiency, propane-based technology, applied in the direction of rectification, condensation, lighting and heating apparatus, etc., can solve the problems of increasing the pressure of the absorber while maintaining desirable propane recovery, increasing the operating cost, and increasing the operating cos
Inactive Publication Date: 2006-10-05
MAK JOHN
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Benefits of technology
This configuration achieves high propane recovery rates (at least 95%) and increased ethane recovery, while reducing CO2 levels in ethane products to below 500 ppm, thereby minimizing operating costs and improving energy efficiency.
Problems solved by technology
Consequently, Rambo's system is generally limited by the upper operating limit of the de-ethanizer pressure.
Increasing of the absorber pressure while maintaining desirable propane recovery becomes difficult, if not impossible in Rambo's process configuration.
Moreover, operating the absorber and de-ethanizer at a pressure at or below 500 psig typically necessitates higher residue gas recompression, thereby incurring relatively high operating cost.
Furthermore, ethane recovery using such known systems designed for propane recovery is normally limited to about 20% recovery.
Campbell's scheme typically requires over-stripping of the ethane product, and CO2 removal is generally limited to about 6%.
Moreover, additional CO2 removal using Campbell's process will significantly reduce ethane recovery, and increase power consumption.
Furthermore, and especially where the ethane product is used for chemical production, the product in Campbell's configuration typically requires further treatment to remove CO2 to or below a level of 500 ppmv, which often requires substantial capital and operating expenditure.
Although there are various configurations and processes for improved propane and ethane recovery known in the art, all or almost all of them, suffer from one or more disadvantage.
Method used
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[0046] Operations of gas processing plants according to FIGS. 1, 2, 3, 4, and 5 were computer simulated using process simulator HYSYS, and Tables 1, 2, 3, 4, and 5 below summarize exemplary component flow, pressures and temperatures in the configurations as shown in FIG. 1-5, respectively.
[0047] Furthermore, calculations were performed to project the heat composite curve for the heat exchanger 100 in plant configuration according to FIG. 2, the heat exchanger 100 in plant configuration according to FIG. 4, and the side heat exchanger 116 in plant configuration according to FIG. 4, and the results are depicted in FIGS. 2A, 4A, and 4B, respectively. The energy efficiencies of these inventions are very high that are demonstrated by the relatively close temperature approaches of these composite curves.
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A gas processing plant has a de-ethanizer and a refluxed absorber, wherein the absorber operates at higher pressure than the de-ethanizer, and wherein at least a portion of the absorber bottoms product is expanded to provide cooling for the absorber reflux stream and / or the distillation column feed stream. Especially contemplated gas processing plants include propane and ethane recovery plants, and where the gas processing plant is an ethane recovery plant, it is contemplated that the ethane product comprises no more than 500 ppm carbon dioxide.
Description
FIELD OF THE INVENTION [0001] The field of the invention is recovery of a gas fraction from a feed gas, and particularly relates to propane recovery. BACKGROUND OF THE INVENTION [0002] Many natural and man-made gases comprise a variety of different hydrocarbons, and numerous methods and configurations are known in the art to produce commercially relevant fractions from such gases. Among other processes, cryogenic gas separation (see e.g., U.S. Pat. No. 4,157,904 to Campbell et al., U.S. Pat. No. 4,690,702 to Paradowski et al., or U.S. Pat. No. 5,275,005 to Campbell et al.) has become a preferred method of gas separation. [0003] In a typical gas separation process, a feed gas stream under pressure is cooled by heat exchanger and as the gas cools, liquids condense from the cooled gas. The liquids are then expanded and fractionated in a distillation column (e.g., de-ethanizer or de-methanizer) to separate residual components such as methane, nitrogen and other volatile gases as overhea...
Claims
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IPC IPC(8): F25J3/00F25J3/02
CPCF25J3/0209Y02C10/12F25J3/0238F25J3/0242F25J2200/02F25J2200/04F25J2200/70F25J2200/74F25J2200/78F25J2205/04F25J2205/50F25J2220/66F25J2230/60F25J2240/02F25J2270/90F25J2290/10F25J2290/12F25J2290/40F25J3/0233Y02C20/40
InventorMAK, JOHN
OwnerMAK JOHN