Method and system for obtaining hydrogen from a feed mixture which contains hydrogen and hydrocarbons

Patent metadata

Field	Value
Publication number	US-10464810-B2
Application number	US-201615741187-A
Country	US
Kind code	B2
Filing date	Jun 29, 2016
Priority date	Jun 29, 2015
Publication date	Nov 5, 2019
Grant date	Nov 5, 2019

Abstract

To obtain hydrogen from a gaseous C2minus feed, it is cooled from a first to a second temperature level at a first pressure level forming one or more condensates. A gaseous remainder is cooled to a third temperature level and subjected to a counterflow absorption at the first pressure level, obtaining a top gas rich in hydrogen and methane and a sump liquid. The former is heated and subjected to pressure swing adsorption at the first pressure level, forming a product stream rich in hydrogen and depleted in or free from methane. The condensate(s) and/or the sump liquid is/are expanded to and fed into a low pressure demethanizer at the second pressure level. The counterflow absorption is carried out using fluid taken from the demethanizer at the second pressure level, compressed in gaseous form to the first pressure level and cooled to the third temperature level.

First claim

The invention claimed is:

1. Method ( 100 , 200 ) for obtaining hydrogen from a feed mixture containing hydrogen, methane and hydrocarbons with two carbon atoms and low in or free from other hydrocarbons, wherein
fluid of the feed mixture is cooled from a first temperature level to a second temperature level at a first pressure level, while one or more condensates are precipitated out of the fluid of the feed mixture, leaving a residual gas,
fluid of the residual gas is further cooled to a third temperature level and subjected to a counterflow absorption, thereby obtaining a top gas rich in hydrogen and methane and a sump liquid,
fluid of the top gas is heated and subjected to pressure swing adsorption ( 9 ) at the first pressure level, to form a product stream which is rich in hydrogen and depleted in or free from methane, and
fluid of the condensate or condensates and/or of the sump liquid is expanded from the first pressure level to a second pressure level and is fed into a low pressure demethanizer at the second pressure level,

characterised in that
the counterflow absorption is carried out at the first pressure level using fluid which has been taken from the low pressure demethanizer at the second pressure level, compressed in gaseous form to the first pressure level and cooled to the third temperature level.

2. Method ( 100 , 200 ) according to claim 1 , wherein the feed mixture contains 55 to 90, particularly 60 to 90, mol % of methane.

3. Method ( 100 , 200 ) according to claim 2 , wherein the fluid taken from the low pressure demethanizer and used in the counterflow absorption predominantly or exclusively contains methane and is used as liquid reflux in the counterflow absorption.

4. Method ( 100 , 200 ) according to claim 1 , wherein the feed mixture contains 30 to 55, particularly 30 to 40, mol % of methane.

5. Method ( 100 , 200 ) according to claim 4 , wherein the fluid taken from the low pressure demethanizer and used in the counterflow absorption contains methane and ethylene and is at least partly freed from the ethylene in the counterflow absorption.

6. Method ( 100 , 200 ) according to claim 4 , wherein an ethane-rich reflux is used in the counterflow absorption, by means of which hydrocarbons with two carbon atoms are washed out both from the fluid of the residual gas and from the fluid taken from the low pressure demethanizer and used in the counterflow absorption.

7. Method ( 100 , 200 ) according to claim 6 , wherein the counterflow absorption is carried out using a two-part separating unit having a first absorption section and a second absorption section, in which the fluid of the residual gas is fed into a lower region of the first absorption section and the fluid taken from the low pressure demethanizer is fed into an upper region of the first absorption section, a gas is transferred from an upper region of the first absorption section into a lower region of the second absorption section and the ethane-rich reflux is fed into an upper region of the second absorption section.

8. Method ( 100 , 200 ) according to claim 7 , wherein the two-part separating unit is configured as a two-part absorption column ( 5 ) in which the first absorption section is arranged underneath the second absorption section in a common outer casing.

9. Method ( 100 , 200 ) according to claim 1 , wherein the fluid of the residual gas is enriched in hydrogen and depleted in methane before the pressure swing adsorption ( 9 ).

10. Method ( 100 , 200 ) according to claim 9 , wherein the fluid of the residual gas is enriched in hydrogen and depleted in methane by further cooling and precipitation of a liquid containing more methane than hydrogen from the fluid of the residual gas.

11. Method ( 100 , 200 ) according to claim 1 , wherein the first temperature level is at 35 to −57° C. and/or the second temperature level is at −60 to −80° C. and/or the third temperature level is at −95 to −100° C., particularly at −97 to −99° C.

12. Method ( 100 , 200 ) according to claim 1 , wherein the first pressure level is at 20 to 35 bar, particularly at 27 to 29 bar, and/or the second pressure level is at 10 to 25 bar, particularly at 12 to 15 bar.

13. Apparatus for obtaining hydrogen from a feed mixture containing hydrogen, methane and hydrocarbons with two carbon atoms and low in or free from other hydrocarbons, with means that are configured:
to cool fluid of the feed mixture from a first temperature level to a second temperature level at a first pressure level, so that one or more condensates are precipitated out of the fluid of the feed mixture, leaving a residual gas,
to further cool fluid of the residual gas to a third temperature level and subject it to counterflow absorption, thereby obtaining a top gas rich in hydrogen and methane and a sump liquid,
to heat fluid of the top gas and to subject it to pressure swing adsorption ( 9 ) at the first pressure level, thereby forming a product stream which is rich in hydrogen and depleted in or free from methane, and
to expand fluid of the condensate or condensates and/or of the sump liquid from the first pressure level to a second pressure level and to feed it into a low pressure demethanizer at the second pressure level,

characterised by
means which are configured to carry out the counterflow absorption at the first pressure level using fluid which is taken from the low pressure demethanizer at the second pressure level, compressed in gaseous form to the first pressure level and cooled to the third temperature level.

14. Apparatus according to claim 13 which, for the purpose of carrying out the counterflow absorption, comprises a two-part separating unit having a first absorption section and a second absorption section, means being provided which are configured to feed the fluid of the residual gas into a lower region of the first absorption section and to feed the fluid taken from the low pressure demethanizer into an upper region of the first absorption section, to transfer gas from an upper region of the first absorption section into a lower region of the second absorption section and to feed an ethane-rich reflux into an upper region of the second absorption section.

Assignees

• Linde Ag

Inventors

• Pham Duc Tuat
• Kuhn Paul

Classifications

• C01B2203/043

  Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration · CPC title

• F25J2205/04

  in the feed line, i.e. upstream of the fractionation step · CPC title

• F25J2205/02

  using simple phase separation in a vessel or drum · CPC title

• F25J3/0219

  Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature · CPC title

• F25J2200/70

  Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified · CPC title