Refrigeration – Cryogenic treatment of gas or gas mixture – Separation of gas mixture
Reexamination Certificate
2000-01-27
2001-11-06
Doerrler, William (Department: 3744)
Refrigeration
Cryogenic treatment of gas or gas mixture
Separation of gas mixture
Reexamination Certificate
active
06311516
ABSTRACT:
BACKGROUND OF THE INVENTION
1. Field of the Invention
This invention relates to an improved process for separating a hydrocarbon-bearing feed gas which contains methane and lighter components, (not necessarily all hydrocarbon components), C
2
(ethylene and ethane), C
3
(propylene and propane), and heavier hydrocarbon components into two fractions. The first fraction contains predominantly C
2
's and lighter components and the second fraction contains the recovered desirable C
3
and heavier components. More particularly, this invention relates to a process and apparatus wherein the yield of C3's is increased.
2. The Prior Art
Hydrocarbon-bearing gas may contain lighter components (e.g., hydrogen, nitrogen, etc.) methane, ethane, and/or ethylene, and a substantial quantity of hydrocarbons of higher molecular weight, for example, propane, butane, pentane and often their unsaturated analogs. Recent changes in propylene/propane demand have created increased markets for propylene/propane and have created a need for more efficient processes which yield higher recovery levels of this product. In more recent times, the use of cryogenic processes utilizing the principle of gas expansion through a mechanical device to produce power while simultaneously extracting heat from the system have been employed. The use of such equipment depends upon the pressure of the gas source, the composition of the gas and the desired end results. In the typical cryogenic expansion-type recovery processes used in the prior art, a gas stream under pressure is cooled by heat exchange with other streams of the process and/or external sources of cooling are employed such as refrigeration systems. As the gas is cooled, liquids are condensed and are collected and separated so as to thereby obtain desired hydrocarbons. The high pressure liquid feed is typically transferred to a deethanizer column after the pressure is adjusted to the operating pressure of the deethanizer. In such fractionating column the liquid feed is fractionated to separate the residual ethylene/ethane and lighter components from the desired products of propylene/propane and heavier hydrocarbon components. In the ideal operation of such separation processes, the vapors leaving the process contain substantially all of the ethylenelethane and lighter components found in the feed gas and substantially no propylene/propane or heavier hydrocarbon components remain. The bottom fraction leaving the deethanizer typically contains substantially all of the propylene/propane and heavier hydrocarbon components with very little ethylenelethane or lighter components which is discharged in the fluid gas outlet from the deethanizer.
A patentability search was conducted on the present invention and the following references were uncovered.
Inventor
U.S. Pat. No.
Issue Date
Harandi
4,664,784
5/12/1987
Buck et al
4,895,584
1/23/1990
Campbell et al
5,771,712
9/01/1998
Wilkinson et al
5,699,507
6/30/1998
U.S. Pat. No. 4,664,784—Issued May. 12, 1987
M. N. Harandi to Mobil Oil Corporation
In a reference directed to fractionation of hydrocarbon mixtures, teachings are found on column 4, line 32 et sequitur re: a zone (81) wherein a descending liquid heavy-ends portion contacts an ascending vaporous light-ends portion so as “ . . . to aid in heat transfer between vapor and liquid.” (column 4, line 44).
U.S. Pat. No. 4,895,584—Issued Jan. 23, 1990
L. L. Buck et al to Pro-Quip Corporation
A reference that claims an improved process for hydrocarbon separation and teaches supplying of the liquids recovered from the light-ends fractionating column to the heavy ends fractionating column and directing part of the (C2 containing) liquid from a first step into intimate contact with a second residue, which liquid provides additional liquefied methane which acts with the partially condensed second residue as a direct contact refrigerant to thereby condense C2 and heavier comprising hydrocarbons while methane itself is evaporated in the light-ends fractionating column.
On column 1, lines 56-67 the following teachings are found: “ . . . feed gas is first cooled and partially condensed and delivered to a separator to provide a first residue vapor and a C2 containing liquid . . . Part of the C2 containing liquid from the separator may be directed into a heavy ends fractionating column wherein the liquid is separated into a second residue containing lighter hydrocarbons and C2 containing products. A part of the first residue vapors with at least part of the partially condensed second residue are counter currently contacted and co-mingled in a light ends fractionating column (emphasis added) . . . ”
On column 2, lines 1-10 the following teachings are found: “The liquids recovered from the light-ends fractionating column are then fed to the heavy-ends fractionating column as a liquid feed. A portion of the C2 containing liquids from the separator is fed into intimate contact with the second residue prior to discharging the co-mingled liquids and gases into the light-ends fractionating column to thereby achieve mass and heat transfer (emphasis added) to thereby liquefy a higher percent of the C2 and heavier hydrocarbon components while the methane is vaporized (column 2, lines 1-10).
The following Elcor Corporation references describe the recovery of C3 and heavier hydrocarbons via processes wherein counter-current contact of a stream drawn from a deethanizer with a stream in a separator/absorber takes place:
U.S. Pat. No. 5,799,507—Issued Sep. 1, 1998
J. D. Wilkinson et al to Elcor Corporation
See column 4, line 2 re: “. . . liquid portion of expanded stream comingles with liquids falling downward from the absorbing section . . . ” l.o.w., the stream (36) from the deethanizer (17) flows through heat exchanger (20) to become stream (36a) which flows into the upper section of separator (15) where it . . . contacts the vapors rising upward through the absorption section” (column 5, lines 3-4).
U.S. Pat. No. 5,771,712—Issued Jun. 30, 1998
R. E. Campbell et al to Elcor Corporation
This reference teaches essentially the same as Wilkinson et al.
None of the foregoing patents discussed above embody the present invention.
SUMMARY OF THE INVENTION
The present invention provides processes for increasing the propylene and propane component of the liquid discharge from the process unit at reduced energy consumption than the prior art. The foregoing advantage is achieved in the present invention by a process in which the feed gas is first cooled and partially condensed and delivered to a separator to provide a first residue vapor and a C
3
containing liquid which liquid also contains lighter hydrocarbons. Part of the C
3
containing liquid from the separator may be directed into a heavy-ends fractionation column, wherein the liquid is separated into a second residue containing lighter hydrocarbons, and a C
3
containing product. The second residue is partially or fully condensed and delivered to a separator where a C
2
containing liquid is discharged. Where the second residue is only partially condensed, a fourth residue will be discharged also. A part of the C
2
containing liquid is further cooled before being sent to the light-ends fractionating column. The portion of the C
2
containing liquid that is not cooled and sent to the light-ends fractionating column is recycled back to the heavy-ends fractionating column as reflux. A part of the first residue vapors is counter-currently contacted and co-mingled with the cooled part of the C
2
containing liquid in a light-ends fractionating column to thereby provide third residue vapors and liquids which are separately discharged. The liquids recovered from the light-ends fractionating column are then fed to the heavy-ends fractionation column as a liquid feed. A cooled portion of the C
2
containing liquids is fed into the light-ends fractionating column to thereby achieve mass and heat transfer and to thereby liquefy a higher percent of the C
3
and heavier hydrocarbon components while the ethylene/ethane is vaporized. In this manner a
Brantingham Steven C.
Key Ronald D.
Doerrler William
Dorman William S.
Drake Malik N.
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