Method for fractionating a stream of cracked gas, using an intermediate recirculation current, and related plant

• US 10,458,701 B2
• Filed: 10/23/2014
• Issued: 10/29/2019
• Est. Priority Date: 10/23/2013
• Status: Active Grant

• Current Assignee: Technip France (Technip)
• Original Assignee: Technip France (Technip)
• Inventors: Destour, Bruno, Simon, Yvon, Dadou, Aurelia, Chazallet, David
• Primary Examiner(s): Alosh, Tareq
• Application Number:
  US15/030,913
• Publication Number:
  US 20160258676A1
• Time in Patent Office: 1,832 Days
• CPC Class Codes: C07C 11/04 Ethylene
• CPC Class Codes: C07C 5/327 Formation of non-aromatic carbon-to-carbon double bonds only
• CPC Class Codes: C07C 7/005 Processes comprising at least two steps in series
• CPC Class Codes: C07C 7/09 by fractional condensation
• CPC Class Codes: C10G 2400/20 C2-C4 olefins
• CPC Class Codes: C10G 2400/26 Fuel gas
• CPC Class Codes: C10G 5/06 by cooling or compressing
• CPC Class Codes: C10G 70/041 by distillation
• CPC Class Codes: C10G 70/043 by fractional condensation
• CPC Class Codes: C10G 9/002 Cooling of cracked gases
• CPC Class Codes: C10L 2290/06 Heat exchange, direct or indirect
• CPC Class Codes: C10L 2290/10 Recycling of a stream within the process or apparatus to reuse elsewhere therein
• CPC Class Codes: C10L 2290/46 Compressors or pumps
• CPC Class Codes: C10L 2290/543 Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
• CPC Class Codes: C10L 3/00 Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
• 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 2205/04 in the feed line, i.e. upstream of the fractionation step
• CPC Class Codes: F25J 2210/04 Mixing or blending of fluids with the feed stream
• CPC Class Codes: F25J 2210/06 Splitting of the feed stream, e.g. for treating or cooling in different ways
• 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 2270/02 : Internal refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/06 : with multiple gas expansion loops
• 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 3/0271 : separation of H2/CO mixtures, i.e. of synthesis gas production of carbon monoxide containing gas in general C01B32/40, C10J, C10K, production of hydrogen containing gas C01B3/00
• CPC Class Codes: Y02P 30/40 : Ethylene production

Abstract

This method comprises:

• • forming an expanded intermediate recirculation stream (170) from a liquid (112, 128) obtained during an upstream cooling and/or intermediate cooling step, upstream from the downstream cooling step;
  • circulating the intermediate recirculation stream (170) at least in an upstream heat exchanger (42) to cool an upstream stream of cracked gas (102);
  • reintroducing the reheated intermediate recirculation stream (170) in a raw cracked gas (20) upstream from at least one compressor (36, 38) of a cooling and compression stage (24).

The upstream, intermediate and downstream cooling steps is carried out without a heat exchanger respectively of an upstream stream of cracked gas (102), an intermediate stream of cracked gas (114) and a downstream stream of cracked gas (140) with an external refrigeration cycle.

Claims

1. A method for fractionating a stream of cracked gas from a hydrocarbon pyrolysis plant to obtain an ethylene-rich cut and a C2+ hydrocarbon-lean fuel stream, the method comprising:

compressing the stream of raw cracked gas in at least one compressor of a cooling and compression stage to form a compressed cracked gas stream;

upstream cooling and partial condensing, in at least one an upstream heat exchanger, of an upstream stream of cracked gas, obtained from the compressed cracked gas stream, and separation of an upstream liquid in at least one upstream balloon to form an intermediate stream of cracked gas pre-cooled at a first temperature;

intermediate cooling and partial condensing of the intermediate stream of cracked gas in an intermediate heat exchanger and separation of an intermediate liquid in an intermediate separating balloon to form a downstream stream of cracked gas cooled to a second temperature lower than the first temperature;

downstream cooling and partial condensing of the downstream stream of cracked gas in at least one downstream heat exchanger to a third temperature lower than the second temperature;

introducing the downstream stream of partially condensed cracked gas from the downstream heat exchanger in a downstream separator;

recovering, at the head of the downstream separator a gas stream of high-pressure fuel, lean in C2+ hydrocarbons, and recovering, at the bottom of the downstream separator, a downstream liquid, rich in C2+ hydrocarbons;

passing of the stream of high-pressure fuel through the downstream exchanger and the intermediate exchanger to form a heated high-pressure fuel stream;

expanding the heated high-pressure fuel stream in at least one first dynamic expansion device to obtain a stream of partially expanded fuel;

heating of the stream of partially expanded fuel through the downstream exchanger and the intermediate exchanger;

treating at least one liquid stream obtained during the upstream cooling, intermediate cooling and downstream cooling to form the ethylene-rich cut;

forming an expanded intermediate recirculation stream from a liquid obtained during the upstream cooling and/or intermediate cooling, upstream from the downstream cooling;

circulating the expanded intermediate recirculation stream at least in the upstream heat exchanger to cool the upstream stream of cracked gas;

reintroducing the reheated intermediate recirculation stream in the raw cracked gas upstream from at least one compressor of the at least one compressor of the cooling and compression stage, the upstream, intermediate and downstream cooling being carried out without heat exchange respectively of the upstream stream of cracked gas, the intermediate stream of cracked gas and the downstream stream of cracked gas with an external refrigeration cycle, wherein passing the stream of high-pressure fuel through the downstream exchanger and the intermediate exchanger includes passing the stream of high-pressure fuel through the downstream exchanger and the intermediate exchanger without passing the stream of high-pressure fuel through the upstream heat exchanger between the head of the downstream separator and the at least one first dynamic expansion turbine.

2. The method according to claim 1, wherein the pressure of the expanded intermediate recirculation stream is greater than 15% of the pressure of the compressed cracked gas stream.

3. The method according to claim 1, wherein the pressure of the expanded intermediate recirculation stream is greater than 5 bars.

4. The method according to claim 1, wherein the molar flow rate of the expanded intermediate recirculation stream is greater than 25% of the molar flow rate of the stream of raw cracked gas.

5. The method according to claim 1, wherein the molar ethylene content in the expanded intermediate recirculation stream is greater than 50%.

6. The method according to claim 5, wherein the molar content level of ethane in the expanded intermediate recirculation stream is comprised between 15% and 30%, the molar content level of methane in the expanded intermediate recirculation stream being comprised between 10% and 20%.

7. The method according to claim 1, wherein the ratio of the molar ethylene content to the molar hydrogen content in the compressed raw cracked gas stream, after reintroduction of the expanded intermediate recirculation stream, is greater than 1.3 times the ratio of the molar ethylene content to the molar hydrogen content in the raw cracked gas stream, before the reintroduction of the expanded intermediate recirculation stream in the raw cracked gas stream.

8. The method according to claim 1, wherein the temperature of the intermediate recirculation stream is comprised between −

75°

C. and −

95°

C., after expansion, and before introduction in the upstream heat exchanger.

9. The method according to claim 1, comprising forming an expanded recirculation stream from at least one fraction of the intermediate liquid and/or at least one fraction of the downstream liquid, and introducing the expanded recirculation stream into the downstream heat exchanger, and/or into the intermediate heat exchanger, before mixing the expanded recirculation stream with the raw cracked gas stream before the passage of the raw cracked gas stream in at least one compressor of the at least one compressor of the cooling and compression stage, the pressure of the expanded recirculation stream being lower than the pressure of the expanded intermediate recirculation stream.

10. The method according to claim 9, comprising injection of at least one fraction taken from the high-pressure fuel gas stream into the expanded recirculation stream.

11. The method according to claim 1, comprising withdrawing a bypass stream from the intermediate cracked gas stream, upstream from the intermediate heat exchanger injecting the bypass stream, after expansion, in the expanded intermediate recirculation stream.

12. The method according to claim 1, comprising forming the at least one intermediate recirculation stream from the upstream liquid coming from the upstream separator balloon and forming at least one additional intermediate recirculation stream from the intermediate liquid-from the intermediate separator balloon.

13. The method according to claim 1, comprising providing a heat exchange relationship between at least one fraction of the compressed cracked gas stream and a refrigerant circulating in an outside refrigeration cycle, introducing said at least one fraction into the upstream separator balloon to form the upstream stream of cracked gas.

15. The method according to claim 2, wherein the pressure of the expanded intermediate recirculation stream is comprised between 20% and 50% of the pressure of the compressed cracked gas stream.

16. The method according to claim 3, wherein the pressure of the expanded intermediate recirculation flow is comprised between 5 bars and 20 bars.

17. The method according to claim 4, wherein said molar flow rate is comprised between 30% and 60% of the molar flow rate of the stream of raw cracked gas.

18. The method according to claim 5, wherein said molar ethylene content is comprised between 55% and 65%.

19. The method according to claim 1, wherein the first temperature of the intermediate stream of cracked gas is between −

63°

C. and −

78°

C.

20. The method according to claim 1, wherein the compressing of the stream of raw cracked gas is done in at least a first compressor and a second compressor of the at least one compressor of the cooling and compression stage to form the compressed cracked gas stream, the reintroducing of the reheated intermediate recirculation stream in the raw cracked gas being done upstream from the second compressor and downstream from the first compressor.

14. A fractionating plant for a first stream of cracked gas coming from a hydrocarbon pyrolysis plant to obtain an ethylene-rich cut and a C2+ hydrocarbon-lean fuel stream, the fractionating plant comprising:

a cooling and compression stage for the stream of raw cracked gas comprising at least one compressor, to form a stream of compressed cracked gas;

an upstream cooling and partial condensation stage for an upstream stream of cracked gas, obtained from the stream of compressed cracked gas, the upstream stage comprising an upstream heat exchanger, and at least one upstream separator balloon for an upstream liquid to form an intermediate stream of cracked gas pre-cooled to a first temperature;

an intermediate cooling and partial condensation stage for the intermediate stream of cracked gas, the intermediate stage comprising an intermediate heat exchanger and an intermediate separating balloon for an intermediate liquid to form a downstream stream of cracked gas cooled to a second temperature below the first temperature;

a downstream cooling and partial condensation stage for the downstream stream of cracked gas to cool the downstream stream of cracked gas to a third temperature below the second temperature, the downstream stage comprising at least one downstream heat exchanger;

a downstream separator and an introducer for introducing the downstream stream of partially condensed cracked gas coming from the downstream heat exchanger into the downstream separator;

a recovery stage, at the head of the downstream separator, for recovering a gaseous stream-of high-pressure fuel, lean in C2+ hydrocarbons, and recovering, at the bottom of the downstream separator, a downstream liquid, rich in C2+ hydrocarbons;

a passage assembly for the stream of high-pressure fuel through the downstream exchanger and the intermediate exchanger to form a stream of reheated high-pressure fuel;

at least first one dynamic expansion device for the stream of reheated high-pressure fuel to obtain a partially expanded fuel stream;

a passage for the stream of partially expanded fuel through the downstream exchanger and the intermediate exchanger to reheat the stream of partially expanded fuel;

a treatment stage for at least one liquid stream obtained in at least one of the upstream cooling, intermediate cooling, and downstream cooling stages to form the ethylene-rich cut;

a former for forming an expanded intermediate recirculation stream from a liquid obtained in at least one of the upstream cooling and/or intermediate cooling stages, upstream from the downstream cooling stage;

a circulator for circulating the expanded intermediate recirculation stream at least in the upstream heat exchanger to cool the upstream stream of cracked gas;

a reintroducer for reintroducing the heated intermediate recirculation stream into the raw cracked gas upstream from at least one compressor of the at least one compressor of the cooling and compression stage, the upstream, intermediate and downstream stages assemblies being configured

to respectively cool the upstream stream of cracked gas, the intermediate stream of cracked gas- and the downstream stream of cracked gas without heat exchange with an outside refrigeration cycle, wherein a flow path between the head of the downstream separator and the at least one first dynamic expansion turbine passes through the downstream exchanger and the intermediate exchanger without passing through the upstream heat exchanger.

21. A method for fractionating a stream of cracked gas from a hydrocarbon pyrolysis plant to obtain an ethylene-rich cut and a C₂⁺ hydrocarbon-lean fuel stream, the method comprising:

compressing the stream of raw cracked gas in at least one compressor of a cooling and compression stage to form a compressed cracked gas stream;

upstream cooling and partial condensing, in at least one upstream heat exchanger, of an upstream stream of cracked gas, obtained from the compressed cracked gas stream, and separation of an upstream liquid in at least one upstream balloon to form an intermediate stream of cracked gas pre-cooled at a first temperature;

intermediate cooling and partial condensing of the intermediate stream of cracked gas in an intermediate heat exchanger and separation of an intermediate liquid in an intermediate separating balloon to form a downstream stream of cracked gas cooled to a second temperature lower than the first temperature;

downstream cooling and partial condensing of the downstream stream of cracked gas in at least one downstream heat exchanger to a third temperature lower than the second temperature;

introducing the downstream stream of partially condensed cracked gas from the downstream heat exchanger in a downstream separator;

recovering, at the head of the downstream separator a gas stream of high-pressure fuel, lean in C₂⁺ hydrocarbons, and recovering, at the bottom of the downstream separator, a downstream liquid, rich in C₂⁺ hydrocarbons;

passing of the stream of high-pressure fuel through the downstream exchanger and the intermediate exchanger to form a heated high-pressure fuel stream;

expanding the heated high-pressure fuel stream in at least one first dynamic expansion device to obtain a stream of partially expanded fuel;

heating of the stream of partially expanded fuel through the downstream exchanger and the intermediate exchanger;

treating at least one liquid stream obtained during the upstream cooling, intermediate cooling and downstream cooling to form the ethylene-rich cut;

forming an expanded intermediate recirculation stream from a liquid obtained during the upstream cooling and/or intermediate cooling, upstream from the downstream cooling;

circulating the expanded intermediate recirculation stream at least in the upstream heat exchanger to cool the upstream stream of cracked gas;

reintroducing the reheated intermediate recirculation stream in the raw cracked gas upstream from at least one compressor of the at least one compressor of the cooling and compression stage, the upstream, intermediate and downstream cooling being carried out without heat exchange respectively of the upstream stream of cracked gas, the intermediate stream of cracked gas and the downstream stream of cracked gas with an external refrigeration cycle; and

forming an expanded recirculation stream from at least one fraction of the intermediate liquid and/or at least one fraction of the downstream liquid, and introducing the expanded recirculation stream into the downstream heat exchanger, and/or into the intermediate heat exchanger, before mixing the expanded recirculation stream with the raw cracked gas stream before the passage of the raw cracked gas stream in at least one compressor of the at least one compressor of the cooling and compression stage, the pressure of the expanded recirculation stream being lower than the pressure of the expanded intermediate recirculation stream.