Process and apparatus for the purification of natural gas and products

• US 6,368,385 B1
• Filed: 07/26/2000
• Issued: 04/09/2002
• Est. Priority Date: 07/28/1999
• Status: Expired due to Term

• Current Assignee: Technip SA (TechnipFMC, plc)
• Original Assignee: Technip SA (TechnipFMC, plc)
• Inventors: Paradowski, Henri
• Primary Examiner(s): SMITH, DUANE
• Application Number:
  US09/626,447
• Time in Patent Office: 622 Days
• Field of Search: 951/78, 951/79, 951/80, 951/81, 951/84, 951/93, 951/94, 952/09, 952/35, 952/37
• US Class Current: 95/181
• CPC Class Codes: B01D 53/1487 Removing organic compounds
• CPC Class Codes: C10L 3/10 Working-up natural gas or synthetic natural gas
• CPC Class Codes: F25J 2200/04 in a dual pressure main column system
• CPC Class Codes: F25J 2200/72 Refluxing the column with at least a part of the totally condensed overhead gas
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2200/78 Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
• CPC Class Codes: F25J 2205/30 using a washing, e.g. "scrubbing" or bubble column for purification purposes
• CPC Class Codes: F25J 2205/50 using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
• CPC Class Codes: F25J 2215/64 Propane or propylene
• CPC Class Codes: F25J 2215/66 Butane or mixed butanes
• CPC Class Codes: F25J 2220/60 Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
• CPC Class Codes: F25J 2220/66 Separating acid gases, e.g. CO2, SO2, H2S or RSH
• CPC Class Codes: F25J 2270/12 External refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/60 Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
• 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 3/0242 separation of CnHm with 3 carbon atoms or more
• CPC Class Codes: F25J 3/0247 separation of CnHm with 4 carbon atoms or more

Abstract

A process and apparatus for the purification of a gas, in particular natural gas, in order to eliminate mercaptans without the use of gas adsorption or cryogenic expansion processes. Natural gas, dried and cooled, is supplied to an absorption column under pressure, producing a head product of a purified gas, and a base product supplied to a fractionating column which separates the most volatile compounds, free from mercaptans, from a gasoline fraction of the natural gas. The mercaptans are eliminated at the head of at least one distillation column, producing a base end product consisting of a mixture of C5 hydrocarbons, heavier than and free from volatile mercaptans, partially mixed with the most volatile recompressed compounds of the natural gas. This mixture is cooled and sent by reflux to the absorption column.

Claims

1. A process for purification of a source gas in order to eliminate volatile mercaptan sulfur compounds, comprising cooling and drying a source gas, supplying the source gas to an absorption column under pressure, the absorption column receiving a reflux fluid and producing, as a head product, a purified gas with a mercaptan level of less than 30 parts per million, and a base product supplied to a fractionating column which separates the most volatile compounds of the source gas, free from mercaptans, from a gasoline fraction withdrawn from a base and containing mercaptans, the most volatile mercaptans being eliminated at the head of at least one distillation column producing a base end product consisting of liquid gasoline with a mixture of C5 hydrocarbons and heavier hydrocarbons that, after a sweetening process so as to no longer contain volatile mercaptans, are mixed with the most volatile compounds separated at a top of the fractionating column and recompressed from the source gas, to produce a mixture, cooling the mixture, and sending the mixture by reflux to the absorption column as the reflux fluid.

2. The process according to claim 1 wherein a principal stream of source gas is subdivided into two parallel bypass streams, a first of which is cooled and supplied to a lower section of the absorption column, and a second of which is cooled and supplied to an intermediate zone of the absorption column.

3. The process according to claim 1 wherein the base product of the absorption column, containing C2 hydrocarbons and heavier hydrocarbons and mercaptans, is expanded before being supplied to the fractionating column for separation of mercaptans from the most volatile compounds of the source gas.

4. The process according to claim 3 including expanding and supplying a base product of the fractionating column, containing C3 hydrocarbons and heavier hydrocarbons and mercaptans, to a first gasoline distillation column, functioning as a depropanizer, and producing a base product containing C4 hydrocarbons and heavier hydrocarbons and mercaptans.

5. The process according to claim 1 wherein a base product of a first distillation column contains C4 hydrocarbons and heavier hydrocarbons and mercaptans, including expanding and supplying the base product of the first distillation column to a second gasoline distillation column, functioning as a debutanizer, and producing a base product containing the residual gasoline fraction consisting of C5 hydrocarbons and heavier hydrocarbons and mercaptans.

6. The process according to claim 4 including cooling a head product of said fractionating column, free from mercaptans and containing C1, C2, and C3 hydrocarbons, by partial condensation and separating the base product into a liquid phase sent to said fractionating column and a gaseous phase which is recompressed before being mixed with a distallation end product of the gasoline fraction.

7. The process according to claim 1 including cooling a head product of a first distillation column, containing C3 hydrocarbons and methylmercaptan, by complete condensation and separating the head product of the first distillation column into two partially liquid streams, one of which is sent to a head of the first distillation column and the other of which undergoes a sweetening process to eliminate methylmercaptan to obtain a mixture of C3 hydrocarbons free from mercaptans.

8. The process according to claim 1 including cooling a head product of a second distillation column, containing C4 hydrocarbons and residual volatile mercaptans, by complete condensation and separating the head product of the second distillation column into two partially liquid streams, one of which is sent to a head of the second distillation column and the other of which undergoes a sweetening process to eliminate residual volatile mercaptans to obtain a mixture of C4 hydrocarbons free from mercaptans.

9. The process according to claim 1 including cooling the stream of source gas and the reflux gas with gas emitted at a head of the absorption column and with an auxiliary cooling fluid, such as propane, including reheating the gas emitted from the absorption column by thermal exchange until close to room temperature.

10. An apparatus for the implementation of the process according to claim 1 comprising a compressor, a gasoline distillation column, a fractionating column, and an absorption column to which are successively connected supply pipes for the source and reflux gases, a main supply pipe for the source gas branching into two bypass lines, one of which, along with a reflux pipe, passes through a heat exchanger, and wherein a head of the absorption column is connected to an output pipe for the process gas passing through the heat exchanger, the absorption column having a base connected by a pipe to the fractionating column, a base of the fractionating column being connected by a pipe to the gasoline distillation column which has a base connected by an outlet pipe to a delivery pipe of the compressor connected by pipe to a head of the fractionating column, the outlet pipe and the delivery pipe joining at the reflux pipe.

11. The apparatus according to claim 10 wherein the head of the fractionating column is connected by a pipe passing through a cooler-condenser to an inlet of a phase separator having a gas phase outlet connected to the compressor and having a liquid phase outlet linked to an upper section of the fractionating column.

12. The apparatus according to claim 11 wherein the gasoline distillation comprises first and second gasoline distillation columns connected in series having respective heads each connected through a cooler-condenser to an inlet of a condensate reservoir having an outlet opening into a return pipe at an upper section of a corresponding gasoline distillation column and a header pipe.

13. The apparatus according to claim 12 wherein the header pipe, linked to the first gasoline distillation column, opens at an inlet of a sweetening apparatus having an outlet connected to a C3 hydrocarbon reservoir whilst the header pipe, linked to the second gasoline distillation column opens into a C4 hydrocarbon sweetening system.

14. The apparatus according to claim 10 including a bypass line for C5 hydrocarbons and heavier hydrocarbons connected to an outlet pipe at a base of the second gasoline distillation column.