Hydrocarbon gas processing

• US 9,927,171 B2
• Filed: 03/22/2017
• Issued: 03/27/2018
• Est. Priority Date: 09/11/2013
• Status: Active Grant

• Current Assignee: UOP Llc (Honeywell International Inc.), SME Products LP
• Original Assignee: Ortloff Enigneers, Ltd., SME Products LP
• Inventors: Hudson, Hank M., Wilkinson, John D., Lynch, Joe T., Miller, Scott A., Cuellar, Kyle T., Johnke, Andrew F., Lewis, W. Larry
• Primary Examiner(s): Nguyen, Tam M
• Application Number:
  US15/466,366
• Publication Number:
  US 20170191751A1
• Time in Patent Office: 370 Days
• Field of Search: None
• CPC Class Codes: C07C 7/04 by distillation
• CPC Class Codes: F25J 1/0022 Hydrocarbons, e.g. natural gas
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/70 Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2200/80 using integrated mass and heat exchange, i.e. non-adiabatic rectification in a reflux exchanger or dephlegmator
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2210/06 Splitting of the feed stream, e.g. for treating or cooling in different ways
• CPC Class Codes: F25J 2215/04 Recovery of liquid products
• CPC Class Codes: F25J 2215/60 Methane
• CPC Class Codes: F25J 2230/20 Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
• CPC Class Codes: F25J 2230/60 the fluid being hydrocarbons or a mixture of hydrocarbons
• CPC Class Codes: F25J 2235/60 the fluid being (a mixture of) hydrocarbons
• CPC Class Codes: F25J 2240/02 Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
• CPC Class Codes: F25J 2240/40 Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
• CPC Class Codes: F25J 2270/90 External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
• CPC Class Codes: F25J 2290/12 Particular process parameters like pressure, temperature, ratios
• CPC Class Codes: F25J 2290/40 Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
• CPC Class Codes: F25J 2290/80 Retrofitting, revamping or debottlenecking of existing plant
• CPC Class Codes: F25J 3/0209 Natural gas or substitute natural gas
• CPC Class Codes: F25J 3/0233 : separation of CnHm with 1 carbon atom or more
• CPC Class Codes: F25J 3/0238 : separation of CnHm with 2 carbon atoms or more
• CPC Class Codes: F25J 3/0242 : separation of CnHm with 3 carbon atoms or more

Abstract

A process and an apparatus are disclosed for a compact processing assembly to improve the recovery of C₂ (or C₃) and heavier hydrocarbon components from a hydrocarbon gas stream. The preferred method of separating a hydrocarbon gas stream generally includes producing at least a substantially condensed first stream and a cooled second stream, expanding both streams to lower pressure, and supplying the streams to a fractionation tower. In the process and apparatus disclosed, the expanded first stream is heated to form a vapor fraction and a liquid fraction. The vapor fraction is combined with the tower overhead vapor, directed to a heat and mass transfer means inside a processing assembly, and cooled and partially condensed by the expanded first stream to form a residual vapor stream and a condensed stream. The condensed stream is combined with the liquid fraction and supplied to the tower at its top feed point.

Claims

1. In an apparatus for the separation of a gas stream containing methane, C₂ components, C₃ components, and heavier hydrocarbon components into a volatile residue gas fraction and a relatively less volatile fraction containing a major portion of said C₂ components, C₃ components, and heavier hydrocarbon components or said C₃ components and heavier hydrocarbon components, in said apparatus there being

(a) one or more heat exchange means and at least one dividing means to produce at least a first stream that has been cooled under pressure to condense substantially all of it, and at least a second stream that has been cooled under pressure;

(b) a first expansion means connected to receive said substantially condensed first stream under pressure and expand it to a lower pressure, whereby said first stream is further cooled;

(c) a distillation column connected to said first expansion means to receive said expanded further cooled first stream at a top feed position, with said distillation column producing at least an overhead vapor stream and a bottom liquid stream;

(d) a second expansion means connected to receive said cooled second stream under pressure and expand it to said lower pressure;

(e) said distillation column further connected to said second expansion means to receive said expanded second stream at a mid-column feed position; and

(f) said distillation column adapted to fractionate at least said expanded further cooled first stream and said expanded second stream at said lower pressure whereby the components of said relatively less volatile fraction are recovered in said bottom liquid stream and said volatile residue gas fraction is discharged as said overhead vapor stream;

the improvement wherein said apparatus includes

(1) a heat and mass transfer means housed in a processing assembly and connected to said first expansion means to receive said expanded further cooled first stream and heat it, and thereafter discharging said heated expanded first stream as a vapor fraction and a liquid fraction;

(2) a first combining means housed in said processing assembly connected to said distillation column and to said heat and mass transfer means to receive said overhead vapor stream and said vapor fraction and form a combined vapor stream;

(3) said heat and mass transfer means being further connected to said first combining means to receive said combined vapor stream and cool it, thereby to supply at least a portion of the heating of element (1) while simultaneously condensing the less volatile components from said combined vapor stream, thereby forming a condensed stream and a residual vapor stream, and thereafter discharging said residual vapor stream from said processing assembly as said volatile residue gas fraction;

(4) a second combining means housed in said processing assembly connected to said heat and mass transfer means to receive said condensed stream and said liquid fraction and form a combined liquid stream;

(5) said second combining means being further connected to said distillation column to supply said combined liquid stream to said top feed position of said distillation column; and

(6) control means adapted to regulate the quantity and temperature of said combined liquid stream to said distillation column to maintain the overhead temperature of said distillation column at a temperature whereby the major portions of the components in said relatively less volatile fraction are recovered in said bottom liquid stream.

2. The apparatus according to claim 1 wherein

(1) a pumping means is connected to said second combining means to receive said combined liquid stream and pump it to higher pressure;

and

(2) said pumping means is further connected to said distillation column to supply said combined liquid stream to said top feed position of said distillation column.

3. The apparatus according to claim 2 wherein said pumping means is housed in said processing assembly.

4. The apparatus according to claim 1 wherein

(1) said one or more heat exchange means is adapted to cool said gas stream under pressure sufficiently to partially condense it;

(2) a separating means is connected to said one or more heat exchange means to receive said partially condensed gas stream and separate it into a vapor stream and at least one liquid stream;

(3) said at least one dividing means is connected to said separating means and adapted to receive said vapor stream and divide it into at least a first vapor stream and a second vapor stream;

(4) said one or more heat exchange means is connected to said at least one dividing means and adapted to receive said first vapor stream and cool it sufficiently to substantially condense it and thereby form said substantially condensed first stream;

(5) said second expansion means is connected to said at least one dividing means and adapted to receive said second vapor stream and expand it to said lower pressure, thereby forming said expanded second stream;

(6) a third expansion means is connected to said separating means to receive at least a portion of said at least one liquid stream and expand it to said lower pressure, said third expansion means being further connected to said distillation column to supply said expanded liquid stream to said distillation column at a lower mid-column feed position below said mid-column feed position; and

(7) said distillation column is adapted to fractionate at least said expanded further cooled first stream, said expanded second stream, and said expanded liquid stream at said lower pressure whereby the components of said relatively less volatile fraction are recovered in said bottom liquid stream.

5. The apparatus according to claim 4 wherein

(1) a third combining means is connected to said at least one dividing means and said separating means to receive said first vapor stream and at least a portion of said at least one liquid stream and form a combined stream;

(2) said one or more heat exchange means is connected to said third combining means and adapted to receive said combined stream and cool it sufficiently to substantially condense it;

(3) said first expansion means is connected to said one or more heat exchange means and adapted to receive said substantially condensed combined stream and expand it to said lower pressure whereby it is further cooled;

(4) said heat and mass transfer means is adapted to receive said expanded further cooled combined stream and heat it, thereafter discharging said heated expanded combined stream as said vapor fraction and said liquid fraction; and

(5) said third expansion means is adapted to receive any remaining portion of said at least one liquid stream and expand it to said lower pressure, whereupon said expanded liquid stream is supplied to said distillation column at said lower mid-column feed position.

6. The apparatus according to claim 2 wherein

(1) said one or more heat exchange means is adapted to cool said gas stream under pressure sufficiently to partially condense it;

(2) a separating means is connected to said one or more heat exchange means to receive said partially condensed gas stream and separate it into a vapor stream and at least one liquid stream;

(3) said at least one dividing means is connected to said separating means and adapted to receive said vapor stream and divide it into at least a first vapor stream and a second vapor stream;

(4) said one or more heat exchange means is connected to said at least one dividing means and adapted to receive said first vapor stream and cool it sufficiently to substantially condense it and thereby form said substantially condensed first stream;

(5) said second expansion means is connected to said at least one dividing means and adapted to receive said second vapor stream and expand it to said lower pressure, thereby forming said expanded second stream;

(6) a third expansion means is connected to said separating means to receive at least a portion of said at least one liquid stream and expand it to said lower pressure, said third expansion means being further connected to said distillation column to supply said expanded liquid stream to said distillation column at a lower mid-column feed position below said mid-column feed position; and

(7) said distillation column is adapted to fractionate at least said expanded further cooled first stream, said expanded second stream, and said expanded liquid stream at said lower pressure whereby the components of said relatively less volatile fraction are recovered in said bottom liquid stream.

7. The apparatus according to claim 3 wherein

(1) said one or more heat exchange means is adapted to cool said gas stream under pressure sufficiently to partially condense it;

(2) a separating means is connected to said one or more heat exchange means to receive said partially condensed gas stream and separate it into a vapor stream and at least one liquid stream;

(3) said at least one dividing means is connected to said separating means and adapted to receive said vapor stream and divide it into at least a first vapor stream and a second vapor stream;

(4) said one or more heat exchange means is connected to said at least one dividing means and adapted to receive said first vapor stream and cool it sufficiently to substantially condense it and thereby form said substantially condensed first stream;

(5) said second expansion means is connected to said at least one dividing means and adapted to receive said second vapor stream and expand it to said lower pressure, thereby forming said expanded second stream;

(6) a third expansion means is connected to said separating means to receive at least a portion of said at least one liquid stream and expand it to said lower pressure, said third expansion means being further connected to said distillation column to supply said expanded liquid stream to said distillation column at a lower mid-column feed position below said mid-column feed position; and

(7) said distillation column is adapted to fractionate at least said expanded further cooled first stream, said expanded second stream, and said expanded liquid stream at said lower pressure whereby the components of said relatively less volatile fraction are recovered in said bottom liquid stream.