METHOD FOR RECOVERING AN ETHYLENE STREAM FROM A CARBON MONOXIDE RICH FEED STREAM, AND ASSOCIATED INSTALLATION

• US 20160146534A1
• Filed: 06/25/2014
• Published: 05/26/2016
• Est. Priority Date: 06/25/2013
• Status: Abandoned Application

• Current Assignee: Technip France (Technip)
• Original Assignee: Technip France (Technip)
• Inventors: DESTOUR, Bruno, SIMON, Yvon, DADOU, Aurlia
• Application Number:
  US14/900,433
• Publication Number:
  US 20160146534A1
• Time in Patent Office: Days
• US Class Current: 1/1
• CPC Class Codes: B01D 2256/24 Hydrocarbons
• CPC Class Codes: B01D 2257/304 Hydrogen sulfide
• CPC Class Codes: B01D 2257/502 Carbon monoxide
• CPC Class Codes: B01D 2257/504 Carbon dioxide
• CPC Class Codes: B01D 2257/80 Water
• CPC Class Codes: B01D 53/002 by condensation
• CPC Class Codes: B01D 53/047 Pressure swing adsorption
• CPC Class Codes: B01D 53/1456 Removing acid components
• CPC Class Codes: C07C 7/005 Processes comprising at least two steps in series
• CPC Class Codes: C07C 7/04 by distillation
• CPC Class Codes: C10G 70/043 by fractional condensation
• CPC Class Codes: F25J 2200/02 in a single pressure main column system
• CPC Class Codes: F25J 2200/40 Features relating to the provision of boil-up in the bottom of a column
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2205/40 using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
• CPC Class Codes: F25J 2205/60 using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
• CPC Class Codes: F25J 2210/04 Mixing or blending of fluids with the feed stream
• CPC Class Codes: F25J 2210/12 Refinery or petrochemical off-gas
• CPC Class Codes: F25J 2215/62 Ethane or ethylene
• CPC Class Codes: F25J 2230/30 : Compression of the feed stream
• CPC Class Codes: F25J 2245/02 : Recycle of a stream in general, e.g. a by-pass stream
• CPC Class Codes: F25J 2270/04 : Internal refrigeration with work-producing gas expansion loop
• 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 3/0219 : Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
• 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 3/0252 : separation of hydrogen production of hydrogen containing gas in general C01B3/00, e.g. separation of hydrogen or hydrogen containing gases form gaseous mixtures at low temperatures C01B3/506
• CPC Class Codes: F25J 3/0261 : separation of carbon monoxide production of carbon monoxide containing gas in general C01B32/40, C10J, C10K

Abstract

This method comprises the following steps:

• • treating a feed stream (12) to obtain a treated gas stream (60);
  • cooling the treated gas stream (60) in a heat exchanger (34) to form at least one column feed fraction;
  • feeding each column feed fraction into a distillation column (50);
  • heating at least one downstream flow (106) derived from the column head stream (104) in the heat exchanger (34).

The treatment step comprises the forming of an intermediate stream (20) containing at least 20 mole % ethylene and at least 20 mole % carbon monoxide, the method comprising a step to remove the carbon monoxide contained in the intermediate stream (20).

Claims

1. A method to recover an ethylene stream from a feed stream, comprising the following steps:

treating a feed stream to obtain a treated gas stream;

at least partly cooling and condensing the treated gas stream in at least one heat exchanger to form at least one column feed fraction;

feeding the at least one column feed fraction into a distillation column to recover an ethylene stream at the foot of the distillation column and, at the head, a head stream depleted of ethylene;

heating at least one downstream flow derived from the head stream in the heat exchanger;

forming an intermediate stream containing at least 20 mole % ethylene and at least 20 mole % carbon monoxide; and

removing the carbon monoxide contained in the intermediate stream.

2. The method according to claim 1, wherein the pressure of the treated gas stream circulating in the at least one heat exchanger is lower than 40 kgf/cm².

3. The method according to claim 2, wherein the pressure of the treated gas stream circulating in the at least one heat exchanger is strictly lower than 30 kgf/cm².

4. The method according to claim 1, wherein the ethylene stream has an ethylene weight content higher than 99.5%, the method comprising obtaining the ethylene stream at the foot of the distillation column without passing through another distillation column.

5. The method according to claim 1, wherein the ethylene stream contains more than 99 weight % of the ethylene contained in the feed stream, the method comprising obtaining the ethylene stream at the foot of the distillation column without passing through another distillation column.

6. The method according to claim 1, comprising leading the intermediate stream into a device to remove carbon monoxide without distillation to form a carbon monoxide-rich stream and a carbon monoxide-depleted stream.

7. The method according to claim 6, wherein the carbon monoxide removing device comprises a pressure swing adsorber producing the carbon monoxide-rich stream and the carbon monoxide-depleted stream.

8. The method according to claim 6, comprising compressing the carbon monoxide-depleted stream to a recompression pressure in a compression equipment to form the treated gas stream.

9. The method according to claim 6, comprising placing at least one fraction of the treated gas stream under heat exchange with the downstream flow in an upstream heat exchanger, to obtain a partly condensed upstream stream, and

leading the upstream stream into an upstream separator and

leading at least one liquid fraction output from the upstream separator into the distillation column.

10. The method according to claim 1, comprising directly forming the intermediate stream by the treated gas stream and then leading said intermediate stream into a condensation and fractionating assembly comprising a plurality of heat exchangers operating at decreasing temperatures to produce a plurality of feed fractions for the distillation column fed into the distillation column the head stream output from the distillation column comprising more than 10 weight % of the carbon monoxide contained in the intermediate stream.

11. The method according to claim 10, comprising:

leading the treated gas stream into at least one first upstream heat exchanger to obtain a cooled and partly condensed upstream stream, and separating the upstream stream into an upstream column feed liquid fraction and an upstream gas fraction;

leading the upstream gas fraction into at least one intermediate heat exchanger to obtain at least one cooled and partly condensed intermediate stream, and separating the at least one cooled intermediate stream into an intermediate column feed liquid fraction and an intermediate gas fraction;

leading at least one intermediate gas fraction into a downstream heat exchanger to obtain a cooled and partly condensed downstream stream, and separating the downstream stream into a downstream column feed liquid fraction and a downstream gas fraction, the upstream, downstream and intermediate liquid fractions being fed into the distillation column.

12. The method according to claim 11, comprising passing at least part of the downstream gas fraction through the downstream heat exchanger and/or through the intermediate heat exchanger and/or through the upstream heat exchanger to be heated therein, the method comprising expanding the heated downstream gas fraction in a dynamic expansion turbine or static pressure-reducing valve before sending back the downstream gas to the downstream heat exchanger and/or intermediate heat exchanger and/or upstream heat exchanger.

13. The method according to claim 11, comprising circulating the downstream flow derived from the head stream in the upstream heat exchanger and/or in the intermediate heat exchanger and/or in the downstream heat exchanger.

14. The method according to claim 1, comprising feeding back, after compression into the feed stream upstream of the treatment, at least one recirculation flow derived from the downstream flow after heating the downstream flow in the heat exchanger.

15. The method according to claim 1, comprising feeding back, after compression into the feed stream upstream of the treatment, at least one recirculation flow derived from the downstream flow after heating the downstream flow in the heat exchanger into the treated gas stream, downstream of the treatment step to form the intermediate stream.

19. The method according to claim 6, wherein the pressure of the carbon monoxide depleted stream is lower than 5 kgf/cm².

20. The method according to claim 11, wherein the cooled and partly condensed upstream stream is at a temperature lower than −

50°

C., the at least one cooled and partly condensed intermediate stream being at a temperature lower than −

90°

C., the cooled and partly condensed downstream stream being at a temperature lower than −

110°

C.

16. An installation to recover an ethylene stream from a feed stream the installation comprising:

an assembly to treat a feed stream to obtain a treated gas stream;

an assembly to cool and at least partly condense the treated gas stream comprising at least one heat exchanger to form at least one column feed fraction;

a distillation assembly comprising a distillation column and an arrangement to feed the at least one column feed fraction into the distillation column to recover an ethylene stream at the foot of the distillation column and an ethylene-depleted head stream at the head of the distillation column;

an assembly to heat at least one downstream flow derived from the head stream in the heat exchanger;

an arrangement to form an intermediate stream containing at least 20 mole % ethylene and at least 20 mole % carbon monoxide;

an assembly to remove the carbon monoxide contained in the intermediate stream;

the removing assembly being configured to remove at least part of the carbon monoxide contained in the intermediate stream.

17. The installation according to claim 16, wherein the removing assembly comprises a device to remove carbon monoxide without distillation, to form a carbon monoxide-rich stream and a carbon monoxide-depleted stream.

18. The installation according to claim 16, wherein the removing assembly is formed by the distillation assembly.