DE102014005935A1 - Process for separating heavy hydrocarbons - Google Patents
Process for separating heavy hydrocarbons Download PDFInfo
- Publication number
- DE102014005935A1 DE102014005935A1 DE102014005935.9A DE102014005935A DE102014005935A1 DE 102014005935 A1 DE102014005935 A1 DE 102014005935A1 DE 102014005935 A DE102014005935 A DE 102014005935A DE 102014005935 A1 DE102014005935 A1 DE 102014005935A1
- Authority
- DE
- Germany
- Prior art keywords
- hydrocarbon
- fraction
- heavy hydrocarbons
- rich fraction
- liquefied
- 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.)
- Withdrawn
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 92
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 90
- 238000000034 method Methods 0.000 title claims abstract description 55
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 50
- 239000007789 gas Substances 0.000 claims abstract description 26
- 230000008929 regeneration Effects 0.000 claims abstract description 26
- 238000011069 regeneration method Methods 0.000 claims abstract description 26
- 238000001179 sorption measurement Methods 0.000 claims abstract description 24
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000000926 separation method Methods 0.000 claims abstract description 13
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000003345 natural gas Substances 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 239000003949 liquefied natural gas Substances 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 206010016352 Feeling of relaxation Diseases 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- MXRIRQGCELJRSN-UHFFFAOYSA-N O.O.O.[Al] Chemical compound O.O.O.[Al] MXRIRQGCELJRSN-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- -1 hydrocarbons hydrocarbon Chemical class 0.000 description 1
- 230000007257 malfunction Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/0231—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the working-up of the hydrocarbon feed, e.g. reinjection of heavier hydrocarbons into the liquefied gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/104—Alumina
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/116—Molecular sieves other than zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- 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
-
- 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
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- 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
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
-
- 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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
Es wird ein Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, insbesondere von Erdgas, beschrieben, wobei die zu verflüssigende Kohlenwasserstoff-reiche Fraktion einer Abtrennung von schweren Kohlenwasserstoffen, insbesondere von Benzol, unterworfen wird. Erfindungsgemäß wird a) die zu verflüssigende Kohlenwasserstoff-reiche Fraktion (1, 2) vor ihrer Verflüssigung (L) adsorptiv von schweren Kohlenwasserstoffen befreit (A), b) das bei der Regenerierung des Adsorptionsprozesses (A) anfallende, mit schweren Kohlenwasserstoffen beladene Regeneriergas (5) abgekühlt und teilkondensiert (E1, E2, E3), c) das teilkondensierte Regeneriergas (5) in eine an schweren Kohlenwasserstoffen angereicherte Fraktion (6) und eine an schweren Kohlenwasserstoffen abgereicherte Fraktion (7, 7') aufgetrennt (D) und d) letztere der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion (1, 2) zugemischt.The invention relates to a process for liquefying a hydrocarbon-rich fraction, in particular natural gas, wherein the hydrocarbon-rich fraction to be liquefied is subjected to separation of heavy hydrocarbons, in particular benzene. According to the invention, a) the hydrocarbon-rich fraction (1, 2) to be liquefied is freed from heavy hydrocarbons before its liquefaction (L). (B) the regeneration gas charged in the regeneration of the adsorption process (A) is charged with heavy hydrocarbons (US Pat. 5) cooled and partially condensed (E1, E2, E3), c) the partially condensed regeneration gas (5) into a heavy hydrocarbons enriched fraction (6) and a heavy hydrocarbon depleted fraction (7, 7 ') separated (D) and d ) the latter of the liquefied hydrocarbon-rich fraction (1, 2) admixed.
Description
Die Erfindung betrifft ein Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, insbesondere von Erdgas, wobei die zu verflüssigende Kohlenwasserstoff-reiche Fraktion einer Abtrennung von schweren Kohlenwasserstoffen, insbesondere von Benzol und anderen Aromaten, unterworfen wird.The invention relates to a process for liquefying a hydrocarbon-rich fraction, in particular of natural gas, wherein the hydrocarbon-rich fraction to be liquefied, a separation of heavy hydrocarbons, in particular of benzene and other aromatics subjected.
Das Verflüssigen einer Kohlenwasserstoff-reichen Fraktion erfolgt üblicherweise gegen wenigstens einen Kältemittelkreislauf und/oder wenigstens einen Kältemittelgemischkreislauf.The liquefaction of a hydrocarbon-rich fraction is usually carried out against at least one refrigerant circuit and / or at least one refrigerant mixture cycle.
Beim Verflüssigen Kohlenwasserstoff-reicher Fraktionen, insbesondere Erdgas, besteht eine wichtige Aufgabe darin, Betriebsstörungen durch Ausfrieren bestimmter Komponenten der zu verflüssigenden Fraktion zu verhindern. Wasser und Kohlendioxid werden üblicherweise zu Beginn der Verfahrensabfolge bei Umgebungstemperatur durch eine chemische Wäsche (z. B. Aminwäsche) und/oder adsorptive Verfahren soweit abgetrennt, dass sie bei der Verflüssigung der Kohlenwasserstoff-reichen Fraktion keine unerwünschte Feststoffbildung verursachen.When liquefying hydrocarbon-rich fractions, in particular natural gas, an important task is to prevent malfunctions by freezing certain components of the fraction to be liquefied. Water and carbon dioxide are usually separated off at the beginning of the process sequence at ambient temperature by a chemical scrubbing (eg, amine scrubbing) and / or adsorptive processes to the extent that they do not cause unwanted solids formation in the liquefaction of the hydrocarbon-rich fraction.
Gefriergefährdete, schwere Kohlenwasserstoffe (SKW) – der Begriff ”schwere Kohlenwasserstoffe” umfasse nachfolgend C6+-Kohlenwasserstoffe –, insbesondere Benzol und Toluol, lassen sich nur mit hohem Aufwand aus der zu verflüssigenden Fraktion bei Umgebungsbedingungen abtrennen.Freezing-endangered, heavy hydrocarbons (SKW) - the term "heavy hydrocarbons" in the following include C 6+ -hydrocarbons -, in particular benzene and toluene, can be separated from the fraction to be liquefied at ambient conditions only with great effort.
Üblicherweise erfolgt die Abtrennung schwerer Kohlenwasserstoffe im kalten Teil eines Verflüssigungsprozesses, wozu die abgekühlte und teilkondensierte Kohlenwasserstoff-reiche Fraktion einer Waschkolonne zugeführt wird. Aus deren Sumpf wird eine an schweren Kohlenwasserstoffen angereicherte Flüssigfraktion abgezogen. Als Rücklaufmedium dient üblicherweise ein Teilstrom der verflüssigten Kohlenwasserstoff-reichen Fraktion, im Falle einer Erdgasverflüssigung folglich ein Teilstrom des verflüssigten Erdgases (LNG). Diese Verfahrensweise erfordert jedoch einen sog. LNG-Kreislauf, der wiederum Energie und Heizfläche in den sog. kalten Wärmetauschern des Verflüssigungsprozesses kostet bzw. erfordert. Zudem ist eine vergleichsweise kostenintensive LNG-Pumpe vorzusehen. Alternativ hierzu kann der Rücklauf auf die Waschkolonne auch durch eine Teilkondensation des Kopfprodukts dieser Kolonne gegen einen Kältemittelstrom gebildet werden; die so entstandene Flüssigkeit wird als Rücklauf genutzt. Auch diese Verfahrensführung benötigt zusätzliche Kälte um den Rücklauf zu erzeugen und Heizfläche für den Kondensator.Usually, the separation of heavy hydrocarbons takes place in the cold part of a liquefaction process, for which purpose the cooled and partially condensed hydrocarbon-rich fraction is fed to a wash column. From the bottom of a heavy hydrocarbons enriched liquid fraction is withdrawn. The reflux medium is usually a partial flow of the liquefied hydrocarbon-rich fraction, in the case of natural gas liquefaction consequently a partial flow of liquefied natural gas (LNG). However, this procedure requires a so-called. LNG cycle, which in turn costs or requires energy and heating surface in the so-called. Cold heat exchangers of the liquefaction process. In addition, a comparatively cost-intensive LNG pump is to be provided. Alternatively, the reflux to the wash column may also be formed by partial condensation of the overhead of this column with a refrigerant stream; the resulting liquid is used as reflux. Also, this process requires additional cooling to produce the return and heating surface for the capacitor.
Aufgabe der vorliegenden Erfindung ist es, ein gattungsgemäßes Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, insbesondere von Erdgas, anzugeben, das die vorbeschriebenen Nachteile vermeidet.The object of the present invention is to provide a generic method for liquefying a hydrocarbon-rich fraction, in particular of natural gas, which avoids the disadvantages described above.
Zur Lösung dieser Aufgabe wird ein Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, insbesondere von Erdgas, vorgeschlagen, das dadurch gekennzeichnet ist, dass
- a) die zu verflüssigende Kohlenwasserstoff-reiche Fraktion vor ihrer Verflüssigung adsorptiv von schweren Kohlenwasserstoffen befreit,
- b) das bei der Regenerierung des Adsorptionsprozesses anfallende, mit schweren Kohlenwasserstoffen beladene Regeneriergas abgekühlt und teilkondensiert,
- c) das teilkondensierte Regeneriergas in eine an schweren Kohlenwasserstoffen angereicherte Fraktion und eine an schweren Kohlenwasserstoffen abgereicherte Fraktion aufgetrennt und
- d) letztere der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion zugemischt wird.
- a) frees the hydrocarbon-rich fraction to be liquefied before adsorption of heavy hydrocarbons,
- b) cooling and partially condensing the regeneration gas charged in the regeneration of the adsorption process and laden with heavy hydrocarbons,
- c) the partially condensed regeneration gas is separated into a fraction enriched in heavy hydrocarbons and a fraction depleted in heavy hydrocarbons, and
- d) the latter is added to the hydrocarbon-rich fraction to be liquefied.
Weitere vorteilhafte Ausgestaltungen des erfindungsgemäßen Verfahrens zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion, die Gegenstände der abhängigen Ansprüche darstellen, sind dadurch gekennzeichnet, dass
- – das bei der Regenerierung des Adsorptionsprozesses anfallende, mit schweren Kohlenwasserstoffen beladene Regeneriergas auf eine Temperatur von wenigstens 30°C, vorzugsweise wenigstens 10°C, insbesondere wenigstens 0°C abgekühlt wird,
- – der Adsorptionsprozess als TSA-, PSA- und/oder VPSA-Prozess ausgeführt ist,
- – der Adsorptionsprozess derart ausgelegt ist, dass er zusätzlich der Abtrennung von Wasser aus der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion dient,
- – das Regeneriergas zumindest teilweise durch einen Teilstrom der in dem Adsorptionsprozess gereinigten Kohlenwasserstoff-reichen Fraktion gebildet wird,
- – sofern die zu verflüssigende Kohlenwasserstoff-reiche Fraktion vor der Zuführung in den Adsorptionsprozess verdichtet wird, die an schweren Kohlenwasserstoffen abgereicherte Fraktion der zu verdichtenden Kohlenwasserstoff-reichen Fraktion zugemischt wird,
- – die Abkühlung des mit schweren Kohlenwasserstoffen beladenen Regeneriergases unterhalb der Umgebungstemperatur erfolgt, indem dieses vor der Auftrennung in eine an schweren Kohlenwasserstoffen angereicherte Fraktion und eine an schweren Kohlenwasserstoffen abgereicherte Fraktion entspannt wird und/oder indem die an schweren Kohlenwasserstoffen abgereicherte Fraktion entspannt wird, und
- – die an schweren Kohlenwasserstoffen angereicherte Flüssigfraktion einem Deethanizer mit Sumpfheizung zugeführt und in diesem stabilisiert wird.
- The regeneration gas charged in the regeneration of the adsorption process and laden with heavy hydrocarbons is cooled to a temperature of at least 30 ° C., preferably at least 10 ° C., in particular at least 0 ° C.,
- The adsorption process is carried out as a TSA, PSA and / or VPSA process,
- The adsorption process is designed such that it additionally serves for the separation of water from the hydrocarbon-rich fraction to be liquefied,
- The regeneration gas is at least partially formed by a partial flow of the hydrocarbon-rich fraction purified in the adsorption process,
- - if the hydrocarbon-rich fraction to be liquefied is compressed prior to its introduction into the adsorption process, the heavy hydrocarbon-depleted fraction of the hydrocarbon-rich fraction to be compressed is blended,
- - the cooling of the regenerated gas laden with heavy hydrocarbons below ambient temperature by this is relaxed before separation into a fraction enriched in heavy hydrocarbons and a heavy hydrocarbon depleted fraction and / or by the heavy-hydrocarbon depleted fraction is relaxed, and
- - The heavy fraction enriched liquid fraction is fed to a deethanizer with sump heating and stabilized in this.
Das erfindungsgemäße Verfahren zum Verflüssigen einer Kohlenwasserstoff-reichen Fraktion sowie weitere Ausgestaltungen desselben seien nachfolgend anhand der in den
Die zu verflüssigende Kohlenwasserstoff-reiche Fraktion
Die aus dem Adsorptionsprozess A abgezogene, von schweren Kohlenwasserstoffen befreite Kohlenwasserstoff-reiche Fraktion
Ein Teilstrom
Die vorbeschriebene Abkühlung, Teilkondensation und Auftrennung stellt eine Kältefalle für das mit schweren Kohlenwasserstoffen beladene Regeneriergas
Das mit schweren Kohlenwasserstoffen beladene Regeneriergas wird auf eine Temperatur von wenigstens 30°C, vorzugsweise wenigstens 10°C, insbesondere wenigstens 0°C abgekühlt. Als Abscheidegüte des erfindungsgemäßen Verfahrens gilt hierbei die beim Abkühlen des mit schweren Kohlenwasserstoffen beladenen Regeneriergases erreichte Temperatur, da durch sie die Menge an Kondensat im Abscheider D beeinflusst wird. Je mehr Kondensat abgeschieden wird, umso kleiner kann der Adsorptionsprozess A ausgelegt werden.The regenerated gas laden with heavy hydrocarbons is cooled to a temperature of at least 30 ° C, preferably at least 10 ° C, especially at least 0 ° C. The separation efficiency of the process according to the invention in this case is the temperature reached during cooling of the regeneration gas laden with heavy hydrocarbons, because it affects the amount of condensate in the separator D. The more condensate is deposited, the smaller the adsorption process A can be designed.
Die im Abscheider D anfallende an schweren Kohlenwasserstoffen abgereicherte Gasfraktion
Das Regeneriergas, in dem sich die schweren Kohlenwasserstoffe aufkonzentrieren, wird üblicherweise im Kreislauf gefahren, da die Regeneriergasmenge zu groß ist, um sie als Brenngas verwenden zu können. Zudem ist es im Regelfall nicht zulässig, dieses Gas aufgrund seines schwankenden Taupunktes und Heizwertes in eine Pipeline abzugeben.The regeneration gas, in which the heavy hydrocarbons concentrate, is usually driven in the circulation, since the Regeneriergasmenge is too large to use them as fuel gas can. In addition, it is usually not allowed to deliver this gas due to its fluctuating dew point and calorific value in a pipeline.
Die vorbeschriebene, an schweren Kohlenwasserstoffen angereicherte Flüssigfraktion
Bei der in der
Die
Mittels der erfindungsgemäßen Verfahrensweise ist eine sichere Abtrennung der kritischen, schweren Kohlenwasserstoffe möglich, so dass deren Ausfrieren im kalten Teil des nachgeschalteten Verflüssigungsprozesses verhindert werden kann. Das erfindungsgemäße Verfahren ist für unterschiedlichste Zusammensetzungen von Kohlenwasserstoff-reichen Fraktionen anwendbar.By means of the procedure according to the invention, a reliable separation of the critical, heavy hydrocarbons is possible, so that their freezing in the cold part of the downstream liquefaction process can be prevented. The process of the invention is applicable to a wide variety of hydrocarbon-rich fractions compositions.
Bei niedrigen Kohlendioxid-Gehalten in der zu verflüssigenden Kohlenwasserstoff-reichen Fraktion kann die Entfernung von Kohlendioxid und Wasser in einer gemeinsamen Adsorberstation erfolgen. Bei der Anwendung der vorliegenden Schaltungen ist dann darauf zu achten, dass nach der Abkühlung ein sicherer Abstand zur Hydratbildungstemperatur eingehalten ist.At low carbon dioxide levels in the hydrocarbon-rich fraction to be liquified, the removal of carbon dioxide and water may occur in a common adsorber station. When using the present circuits is then to ensure that after cooling a safe distance to the hydrate formation temperature is maintained.
Claims (8)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102014005935.9A DE102014005935A1 (en) | 2014-04-24 | 2014-04-24 | Process for separating heavy hydrocarbons |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102014005935.9A DE102014005935A1 (en) | 2014-04-24 | 2014-04-24 | Process for separating heavy hydrocarbons |
Publications (1)
Publication Number | Publication Date |
---|---|
DE102014005935A1 true DE102014005935A1 (en) | 2015-10-29 |
Family
ID=54261446
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE102014005935.9A Withdrawn DE102014005935A1 (en) | 2014-04-24 | 2014-04-24 | Process for separating heavy hydrocarbons |
Country Status (1)
Country | Link |
---|---|
DE (1) | DE102014005935A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114856528A (en) * | 2022-05-11 | 2022-08-05 | 大庆市中瑞燃气有限公司 | Method for recovering waste heat of heavy hydrocarbon removal of wellhead gas |
CN115461129A (en) * | 2020-04-17 | 2022-12-09 | 环球油品有限责任公司 | Method and apparatus for recovering catalyst from product stream |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10140585A1 (en) * | 2001-08-18 | 2003-02-27 | Linde Ag | Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval |
US6610124B1 (en) * | 2002-03-12 | 2003-08-26 | Engelhard Corporation | Heavy hydrocarbon recovery from pressure swing adsorption unit tail gas |
US20070267328A1 (en) * | 2003-10-30 | 2007-11-22 | Neumann Klaus D K | Process and System for Removing Contaminants from a Natural Gas Stream |
US8273153B2 (en) * | 2007-09-24 | 2012-09-25 | IFP Energies Nouvelles | Dry natural gas liquefaction method |
CA2851064A1 (en) * | 2011-09-30 | 2013-04-04 | Xindi Energy Engineering Technology Co., Ltd. | Water removal and heavy-hydrocarbon removal process in liquefied natural gas production from mixed gas rich in methane |
US20130192299A1 (en) * | 2012-02-01 | 2013-08-01 | Basf Corporation | Heavy Hydrocarbon Removal Process |
US20140033762A1 (en) * | 2012-08-03 | 2014-02-06 | Air Products And Chemicals, Inc. | Heavy Hydrocarbon Removal From A Natural Gas Stream |
-
2014
- 2014-04-24 DE DE102014005935.9A patent/DE102014005935A1/en not_active Withdrawn
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10140585A1 (en) * | 2001-08-18 | 2003-02-27 | Linde Ag | Separation of lower hydrocarbons comprises operating de-ethanizer at no less than de-methanizer pressure and combines head fractions for at least an interval |
US6610124B1 (en) * | 2002-03-12 | 2003-08-26 | Engelhard Corporation | Heavy hydrocarbon recovery from pressure swing adsorption unit tail gas |
US20070267328A1 (en) * | 2003-10-30 | 2007-11-22 | Neumann Klaus D K | Process and System for Removing Contaminants from a Natural Gas Stream |
US8273153B2 (en) * | 2007-09-24 | 2012-09-25 | IFP Energies Nouvelles | Dry natural gas liquefaction method |
CA2851064A1 (en) * | 2011-09-30 | 2013-04-04 | Xindi Energy Engineering Technology Co., Ltd. | Water removal and heavy-hydrocarbon removal process in liquefied natural gas production from mixed gas rich in methane |
US20130192299A1 (en) * | 2012-02-01 | 2013-08-01 | Basf Corporation | Heavy Hydrocarbon Removal Process |
US20140033762A1 (en) * | 2012-08-03 | 2014-02-06 | Air Products And Chemicals, Inc. | Heavy Hydrocarbon Removal From A Natural Gas Stream |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN115461129A (en) * | 2020-04-17 | 2022-12-09 | 环球油品有限责任公司 | Method and apparatus for recovering catalyst from product stream |
CN114856528A (en) * | 2022-05-11 | 2022-08-05 | 大庆市中瑞燃气有限公司 | Method for recovering waste heat of heavy hydrocarbon removal of wellhead gas |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE102010044646A1 (en) | Process for separating nitrogen and hydrogen from natural gas | |
CN104204159A (en) | Heavy hydrocarbon removal process | |
DE102006005822A1 (en) | Process for the refrigeration supply of the cryogenic separation stage of an olefin plant | |
EP0711969A2 (en) | Process for liquefying natural gas | |
DE2337055C2 (en) | Method and device for recovering the hydrocarbons contained in a gasoline-air mixture | |
DE102014005936A1 (en) | Process for liquefying a hydrocarbon-rich fraction | |
DE1619858A1 (en) | Method and device for component concentration in the vapor phase | |
EP3932522A1 (en) | Process and plant for removing interfering components from crude synthesis gas | |
DE102012021478A1 (en) | Method and apparatus for removing absorbable gases from pressurized, gas-contaminated industrial gases without supplying cooling energy | |
DE102013011640A1 (en) | Process for separating sour gases from natural gas | |
DE2005634A1 (en) | ||
DE2460515A1 (en) | METHOD AND APPARATUS FOR REMOVING CONTAMINATION FROM LOW-BOILING GASES CONTAINING SUCH | |
CN112292189B (en) | Temperature swing adsorption process for heavy hydrocarbon removal | |
DE102014005935A1 (en) | Process for separating heavy hydrocarbons | |
DE10324694A1 (en) | Process for the removal of acid gases from pressurized natural gas contaminated with acid gas compounds and recovery of the removed acid gases at an elevated pressure level | |
WO2010069431A1 (en) | Method for purifying gases and obtaining acid gases | |
DE102012017485A1 (en) | Process for separating C2 + hydrocarbons or C3 + hydrocarbons from a hydrocarbon-rich fraction | |
DE102013012656A1 (en) | A method of separating unwanted components from a helium stream | |
DE102013008535A1 (en) | Plant for reducing a carbon dioxide content of a carbon dioxide-rich and hydrocarbon-rich gas stream and corresponding method | |
DE3805157C1 (en) | Process for the recovery of light hydrocarbons | |
DE19622692C1 (en) | Liquefaction of hydrocarbon-rich gas stream containing aromatic and heavy hydrocarbon(s) | |
DE102004046342A1 (en) | Removal of unwanted components (e.g. heavy hydrocarbon) from hydrocarbon-rich gas stream comprises adding heavy hydrocarbon-containing fraction to the gas stream; separating mixed fraction; and liquefying gas fraction | |
WO2021058130A1 (en) | Method and system for obtaining components from natural gas | |
DE102009035389A1 (en) | Process for pollutant removal from carbon dioxide and apparatus for carrying it out | |
DE10100114A1 (en) | Regenerating loaded adsorber comprises using regenerating gas heated using hot thermal oil stream |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
R163 | Identified publications notified | ||
R119 | Application deemed withdrawn, or ip right lapsed, due to non-payment of renewal fee |