EP3382306A1 - Procédé de recyclage de surdébit, appareil et procédé de traitement de recyclage de surdébit d'hydrocarbures - Google Patents

Procédé de recyclage de surdébit, appareil et procédé de traitement de recyclage de surdébit d'hydrocarbures Download PDF

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Publication number
EP3382306A1
EP3382306A1 EP17164141.8A EP17164141A EP3382306A1 EP 3382306 A1 EP3382306 A1 EP 3382306A1 EP 17164141 A EP17164141 A EP 17164141A EP 3382306 A1 EP3382306 A1 EP 3382306A1
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EP
European Patent Office
Prior art keywords
ethaniser
outlet port
reflux
inlet port
ethane
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP17164141.8A
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German (de)
English (en)
Inventor
Heinz Bauer
Andreas Bub
Lisa KÖPPL
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
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Linde GmbH
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Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP17164141.8A priority Critical patent/EP3382306A1/fr
Priority to US16/499,652 priority patent/US20200116427A1/en
Priority to PCT/EP2018/057272 priority patent/WO2018177874A1/fr
Priority to AU2018246973A priority patent/AU2018246973A1/en
Publication of EP3382306A1 publication Critical patent/EP3382306A1/fr
Withdrawn legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/32—Processes or apparatus using separation by rectification using a side column fed by a stream from the high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/78—Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream

Definitions

  • the present invention relates to an overhead recycle process apparatus of the type that, for example, recovers hydrocarbon products having a molecular weight heavier than ethane from natural gas.
  • the present invention also relates to a method of overhead recycle processing of hydrocarbons, the method being of the type that recovers hydrocarbon products having a molecular weight heavier than ethane from natural gas.
  • an overhead recycle process apparatus comprising: a heat exchange arrangement; a separator in fluid communication with an absorber and a de-ethaniser, the absorber having a reflux inlet port; and an ethane rectifier in fluid communication with the de-ethaniser, the de-ethaniser being arranged to provide cooling by heat exchange to an overhead stream path of the ethane rectifier; and the ethane rectifier comprises a reflux drum having an ethane outlet port and a vapour outlet port in fluid communication with the reflux inlet port of the absorber.
  • the overhead outlet stream port of the de-ethaniser may be in fluid communication with an inlet port of the separator via the second heat exchanger.
  • the apparatus may further comprise: a light fractions compression and cooling arrangement in fluid communication at a first end thereof with the lean gas outlet port and at a second end thereof with the first heat exchanger; wherein the compression and cooling arrangement may comprise the compressor.
  • a method of overhead recycle processing of hydrocarbons comprising: drawing off ethane from a de-ethaniser; rectifying the drawn off ethane in a rectifier; generating reflux from an overhead stream path of the rectifier; and introducing the reflux into a reflux drum of the rectifier.
  • the heat exchange arrangement comprises a first heat exchanger 116, a second heat exchanger 118 and an ethane reflux heat exchanger 120.
  • An inlet fluid path 122 extends from the natural gas inlet port 102 and passes through the first heat exchanger 116 via first inlet and outlet ports of the first heat exchanger 116 and is in fluid communication with an inlet port of the first separator 108.
  • the first separator 108 has a first vapour outlet port and a first liquid outlet port, the first vapour outlet port of the first separator 108 being in fluid communication with a bottom product inlet port 124 of the absorber 104 via the expander 114.
  • the first liquid outlet port of the first separator 108 is in fluid communication with a first feed inlet port 126 of the de-ethaniser 106 via a first Joule-Thomson device, for example a first valve 128.
  • the de-ethaniser 106 also comprises a de-ethaniser primary reflux inlet port 154, and an overhead vapour outlet port 156 in fluid communication with a primary de-ethaniser reflux path 158 at a first end thereof, the primary de-ethaniser reflux path 158 being in fluid communication with the de-ethaniser primary reflux inlet port 154 at a second end thereof.
  • the primary de-ethaniser reflux path 158 extends from the overhead vapour outlet inlet port 156 to an inlet port of the second separator 110, passing through the second heat exchanger 118 via second inlet and outlet ports thereof.
  • the second vapour outlet port of the second separator 110 is in fluid communication with an absorber reflux inlet port 164 of the absorber 104 by way of an absorber reflux path 166 that is in fluid communication with the second vapour outlet port of the second separator 110 at a first end thereof.
  • the absorber reflux path 166 also passes through the second heat exchanger 118 via third inlet and outlet ports of the second heat exchanger 118.
  • the side stream outlet port 174 is located at a location along the de-ethaniser 106 corresponding to an expected presence of elevated levels of ethane content in the de-ethaniser 106, and is located below the second feed inlet port 134, although it should be appreciated that in some embodiments the side stream outlet port 174 can be disposed slightly above the second feed inlet port 134.
  • the ethane rectifier 170 comprises a reflux drum 182 having an ethane outlet port 184, an overhead vapour outlet port 185 and a reflux inlet port 186, the overhead vapour outlet port 185 being in fluid communication with the absorber reflux inlet port 164 via a fifth Joule-Thomson device, for example a fifth valve 188.
  • a rectification portion 190 of the ethane rectifier 170 comprises an overhead stream outlet port 192 in fluid communication with a first end of an overhead stream path 194, a second end of the overhead stream path 194 being in fluid communication with the reflux inlet port 186 via the ethane reflux heat exchanger 120.
  • the de-ethaniser 106 also comprises a bottom fractions reservoir 195, and a bottom fractions inlet port 196 and a bottom fractions outlet port 197 in fluid communication with the bottom fractions reservoir 195.
  • a reboiler circuit path extends from the bottom fractions outlet port 197 and returns to the bottom fractions reservoir 195 via the bottom fractions inlet port 196.
  • the reboiler circuit path passes through a reboiler heat exchanger 198.
  • the bottom fractions outlet port 197 is also in fluid communication with a heavy hydrocarbon fractions outlet port 199 at a temperature of between about 110°C and about 130°C, for example about 118°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs).
  • the heat exchange arrangement also comprises the intercooler 146, the after-cooler 150 and the reboiler heat exchanger 198.
  • natural gas is supplied at the natural gas inlet port 102.
  • the gas is at a temperature of between about 10°C and about 60°C, for example about 40°C, and a pressure of between about 4 MPa (40 bar abs) and about 8 MPa (80 bar abs), for example about 6 MPa (60 bar abs).
  • the cooled and partially liquefied natural gas then enters the first separator 108 (Step 202), the vapour fraction being between about 0.94 mol/mol and about 0.99 mol/mol, for example about 0.97 mol/mol,
  • the liquid fraction of the cooled natural gas leaves the first separator 108 and is cooled further by passage through the first valve 128 before entering (Step 204) the de-ethaniser 106 at a temperature of between about -65°C and about -45°C, for example about -56°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs).
  • the vapour fraction of the cooled liquid fraction is between about 0.15 mol/mol and about 0.3 mol/mol, for example about 0.23 mol/mol.
  • vapour fractions leaving the absorber 104 via the overhead vapour outlet port 140 do so at a temperature of between about -85°C and about -65°C, for example about -75°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.2 MPa (32 bar abs), and follow the lean gas outlet path 142 and pass through the second heat exchanger 118 and then the first heat exchanger 116.
  • the light fractions compression and cooling arrangement comprising the first and second compressors 112, 148 and the intercooler 146 and the post-cooler 150 compress and cool (Step 210) the so-called "light" fractions present in the lean gas outlet path 142, for example nitrogen, methane and ethane.
  • the light fractions have a lower molecular weight than propane and are present at the lean gas outlet port 144, and are at a temperature of between about 10°C and about 60°C, for example about 37°C, and a pressure of between about 4 MPa (40 bar abs) and about 10 MPa (100 bar abs), for example about 6 MPa (60 bar abs).
  • the lean gas outlet path 142 supports cooling in the first and second heat exchangers 116, 118.
  • the warmed liquid fractions pass through the second valve 138, resulting in the cooling of the liquid fractions in the second feed fluid path 130, and then enter the de-ethaniser 106 via the second feed inlet port 134 (Step 212) at a temperature of between about -10°C and about 30°C, for example about 10°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs).
  • the vapour fraction of the fluid entering the de-ethaniser 106 is between about 0.7 mol/mol and about 1.0 mol/mol, for example about 0.82 mol/mol.
  • An overhead vapour stream emanates from the overhead vapour port 156 of the de-ethaniser 106 at a temperature of between about -15°C and about 10°C, for example about -2°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs), and follows the primary de-ethaniser reflux path 158 and enters the second separator 110 (Step 220) at a temperature of between about -25°C and about 0°C, for example about -16°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.3 MPa (33 bar abs).
  • Liquid fractions leave the second separator 110 and are pumped (Step 226) by the second pump 160 to the de-ethaniser primary reflux inlet port 154 via the third valve 162, which serves to cool the liquid fractions passing therethrough.
  • the cooled liquid fractions then enter the de-ethaniser primary reflux inlet port 154 at a temperature of between about -25°C and about 0°C, for example about -15°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs) and serve as reflux (Step 228).
  • a portion of the liquid fractions is tapped off the primary de-ethaniser reflux path 158 so as to follow the secondary de-ethaniser reflux path 159, the tapped off liquid fractions pass (Step 230) through the ethane reflux heat exchanger 120 to support cooling by the ethane reflux heat exchanger 120, before entering (Step 232) the de-ethaniser 106 via the secondary reflux inlet port 161 a temperature of between about 0°C and about 20°C, for example about 12°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.3 MPa (33 bar abs).
  • a proportion of the bottom fractions leaving the de-ethaniser 106 via the bottom fraction outlet port 197 follow a reboiler circuit path (Step 234) and are heated and partially vaporised in the reboiler heat exchanger 198 and reintroduced into the bottom fraction reservoir 195 of the de-ethaniser 106.
  • the remaining proportion of the bottom fractions leaving the de-ethaniser 106 via the bottom fraction outlet port 197 are drawn off (Step 236) via the heavy hydrocarbon fractions outlet port 199.
  • Ethane present in the de-ethaniser 106 is circulated (Step 240) through a side stream circuit; the ethane vapour leaves the de-ethaniser 106 via the side stream outlet port 174 at a temperature of between about 60°C and about 80°C, for example about 70°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs), and enters the bottom product reservoir 180 of the ethane rectifier 170.
  • the vapour fractions travelling up the rectification portion 190 of the ethane rectifier 170 encounter reflux originating from the reflux drum 182, which serves to rectify the vapour fractions before the vapour fractions leave the rectification portion 190 of the ethane rectifier 170 via the overhead stream outlet port 192 at a temperature of between about 5°C and about 25°C, for example about 14°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs).
  • the reflux travels down the rectification portion 190 of the ethane rectifier 170, and a proportion of the ethane in the reflux drum 182 is drawn (Step 244) from the reflux drum 182 at the ethane outlet port 184 at a temperature of between about 0°C and about 20°C, for example about 11°C, and a pressure of between about 2.5 MPa (25 bar abs) and about 4 MPa (40 bar abs), for example about 3.4 MPa (34 bar abs).

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP17164141.8A 2017-03-31 2017-03-31 Procédé de recyclage de surdébit, appareil et procédé de traitement de recyclage de surdébit d'hydrocarbures Withdrawn EP3382306A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP17164141.8A EP3382306A1 (fr) 2017-03-31 2017-03-31 Procédé de recyclage de surdébit, appareil et procédé de traitement de recyclage de surdébit d'hydrocarbures
US16/499,652 US20200116427A1 (en) 2017-03-31 2018-03-22 Overhead recycle process apparatus and method of overhead recycle processing of hydrocarbons
PCT/EP2018/057272 WO2018177874A1 (fr) 2017-03-31 2018-03-22 Appareil de traitement de recyclage de distillat de tête et procédé de traitement de recyclage de distillat de tête d'hydrocarbures
AU2018246973A AU2018246973A1 (en) 2017-03-31 2018-03-22 Overhead recycle process apparatus and method of overhead recycle processing of hydrocarbons

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP17164141.8A EP3382306A1 (fr) 2017-03-31 2017-03-31 Procédé de recyclage de surdébit, appareil et procédé de traitement de recyclage de surdébit d'hydrocarbures

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EP3382306A1 true EP3382306A1 (fr) 2018-10-03

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EP (1) EP3382306A1 (fr)
AU (1) AU2018246973A1 (fr)
WO (1) WO2018177874A1 (fr)

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US20240191941A1 (en) * 2022-12-08 2024-06-13 Uop Llc Ethane separation with overhead cryogenic heat exchanger

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2577701A (en) * 1946-05-20 1951-12-04 Shell Dev Fractionation process
US4617039A (en) 1984-11-19 1986-10-14 Pro-Quip Corporation Separating hydrocarbon gases
DE19643152A1 (de) * 1996-10-18 1998-04-23 Linde Ag Verfahren zum Umbauen einer bestehenden Anlage
US20070012072A1 (en) * 2005-07-12 2007-01-18 Wesley Qualls Lng facility with integrated ngl extraction technology for enhanced ngl recovery and product flexibility
US20100011810A1 (en) * 2005-07-07 2010-01-21 Fluor Technologies Corporation NGL Recovery Methods and Configurations
US20110048067A1 (en) * 2007-10-26 2011-03-03 Ifp Natural gas liquefaction method with high-pressure fractionation

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2577701A (en) * 1946-05-20 1951-12-04 Shell Dev Fractionation process
US4617039A (en) 1984-11-19 1986-10-14 Pro-Quip Corporation Separating hydrocarbon gases
DE19643152A1 (de) * 1996-10-18 1998-04-23 Linde Ag Verfahren zum Umbauen einer bestehenden Anlage
US20100011810A1 (en) * 2005-07-07 2010-01-21 Fluor Technologies Corporation NGL Recovery Methods and Configurations
US20070012072A1 (en) * 2005-07-12 2007-01-18 Wesley Qualls Lng facility with integrated ngl extraction technology for enhanced ngl recovery and product flexibility
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