EP3999614A1 - Système et procédé de production de composés en c9+ non hydrogénés et hydrogénés - Google Patents

Système et procédé de production de composés en c9+ non hydrogénés et hydrogénés

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Publication number
EP3999614A1
EP3999614A1 EP20743352.5A EP20743352A EP3999614A1 EP 3999614 A1 EP3999614 A1 EP 3999614A1 EP 20743352 A EP20743352 A EP 20743352A EP 3999614 A1 EP3999614 A1 EP 3999614A1
Authority
EP
European Patent Office
Prior art keywords
stream
hydrogenated
compounds
produce
primarily
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.)
Pending
Application number
EP20743352.5A
Other languages
German (de)
English (en)
Inventor
Shehzada Khurram
Ernesto UEHARA
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.)
SABIC Global Technologies BV
Original Assignee
SABIC Global Technologies BV
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by SABIC Global Technologies BV filed Critical SABIC Global Technologies BV
Publication of EP3999614A1 publication Critical patent/EP3999614A1/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
    • C10G45/48—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
    • C10G45/52—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing platinum group metals or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/26—Fuel gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics

Definitions

  • the present invention generally relates to the processing of pyrolysis gasoline
  • the present invention relates to a process of processing pyrolysis gasoline to produce un-hydrogenated C 9+ hydrocarbons and hydrogenated C 9+ hydrocarbons.
  • the hydrocarbon feedstock is superheated in a reactor to temperatures as high as 750-950 °C.
  • a dilution steam generator supplies dilution steam to the reactor to reduce the partial pressure of the hydrocarbons.
  • the superheated hydrocarbons are then rapidly cooled (quenched) to stop the reactions after a certain point to optimize cracking product yield.
  • Pyrolysis gasoline is one of the products of the cracking process and may include components such as aromatics, olefins, and/or diolefins, among others.
  • the pygas is hydrogenated before further processing to produce finished products such as benzene, toluene, and xylene (BTX).
  • GHU Gasoline hydrogenation units
  • Olefins and sulfur compound are also hydrogenated to meet final product specifications.
  • different product cuts are separated based on downstream demand. For example, after hydrogenation of pyrolysis gasoline, a C 9+ cut is normally separated at a deoctanizer to produce hydrogenated wash oil and hydrogenated C 9+ residue.
  • WO 2018/002810 A1 relates to a separation system for separating a feed stream comprising C6+ hydrocarbons, the system comprising: i) a first distillation column for producing a first light stream comprising C6- hydrocarbons and a first heavy stream comprising C7+ hydrocarbons, wherein the first distillation column is operated between a lowest pressure and a highest pressure, ii) a second distillation column for producing a second light stream comprising C6- hydrocarbons and a second heavy stream comprising C7+ hydrocarbons, wherein the second distillation column is operated between a lowest pressure and a highest pressure, wherein the lowest pressure of the second distillation column is higher than the highest pressure of the highest distillation column and iii) a heat exchanger comprising a first reboiler for reboiling a part of the first heavy stream to produce a first boiled heavy stream and a second condenser for condensing the second light stream to produce a second condensed light
  • the discovered process provides the flexibility of producing (1) only un-hydrogenated C 9+ hydrocarbons (separation upstream of GHU and not further hydrogenated), (2) un-hydrogenated C 9+ hydrocarbons and hydrogenated C 9+ hydrocarbons (separation upstream of GHU and GHU operated to process only a portion of the un-hydrogenated C 9+ hydrocarbons), or (3) only hydrogenated C 9+ hydrocarbons (GHU operated to process all of the un-hydrogenated C 9+ hydrocarbons).
  • Embodiments of the invention include a method of processing pyrolysis gasoline, where the method involves separating a pyrolysis gasoline stream to produce a first stream comprising primarily un-hydrogenated C 9+ compounds. According to embodiments of the invention, the separating of the pyrolysis gasoline is carried out upstream of the hydrogenation unit.
  • Embodiments of the invention include a method of processing pyrolysis gasoline to concurrently produce a first stream comprising primarily un-hydrogenated C 9+ compounds and a second stream comprising hydrogenated C 9+ hydrogenated compounds. The method includes separating a pyrolysis gasoline stream to produce the first stream comprising primarily un-hydrogenated C 9+ compounds and further includes hydrogenating a portion of the first stream to produce the second stream comprising hydrogenated C 9+ hydrogenated compounds.
  • the terms“wt.%”,“vol.%” or“mol.%” refer to a weight, volume, or molar percentage of a component, respectively, based on the total weight, the total volume, or the total moles of material that includes the component. In a non-limiting example, 10 moles of component in 100 moles of the material is 10 mol.% of component.
  • “primarily” may include 50.1 wt.% to 100 wt.% and all values and ranges there between, 50.1 mol.% to 100 mol.% and all values and ranges there between, or 50.1 vol.% to 100 vol.% and all values and ranges there between.
  • FIG. 1 shows a system for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ compounds, according to embodiments of the invention
  • FIG. 2 shows a process for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ compounds, according to embodiments of the invention
  • FIG. 3 shows a system for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ and hydrogenated wash oil compounds, according to embodiments of the invention.
  • FIG. 4 shows a process for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ and hydrogenated wash oil compounds, according to embodiments of the invention.
  • FIG. 5 shows a system and process for processing pyrolysis gasoline to produce un-hydrogenated C 9+ and un-hydrogenated wash oil compounds, according to an embodiment of the invention.
  • GHU Gasoline hydrogenation units
  • Olefins and sulfur compounds are also hydrogenated to meet final product specifications.
  • different product cuts are separated based on downstream demand. For example, after hydrogenation of pyrolysis gasoline, a C 9+ cut is normally separated at the deoctanizer to produce hydrogenated wash oil and hydrogenated C 9+ residue. This process, however, does not contribute to meeting the demand for un-hydrogenated C 9+ products.
  • a solution to address this deficiency of the conventional process has been discovered.
  • the discovered process is premised on separating un-hydrogenated C 9+ hydrocarbons from pyrolysis gasoline upstream of a GHU so that un-hydrogenated C 9+ hydrocarbons can be recovered as a product and as hydrogenated C 9+ hydrocarbons can likewise be recovered as a product.
  • FIG. 1 shows system 10 for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ compounds (e.g., un-hydrogenated hydrocarbons), according to embodiments of the invention.
  • FIG. 2 shows process 20 for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ compounds, according to embodiments of the invention.
  • System 10 may be used to implement process 20.
  • process 20 includes, at block 200, separating pyrolysis gasoline stream 100, in separation unit 121 to produce stream 101 (C 9+ compounds/stream), which comprises primarily un-hydro genated C 9+ compounds.
  • Wash oil is used to control the build-up of polymers on cracked gas compressors, turbines, seals, and heat exchangers.
  • a good wash oil has a fairly high initial boiling point so that it won’t immediately flash to vapor, combined with a high C 9+ aromatic content for dissolving polymeric compounds.
  • the wash oil described herein is hydrogenated to saturate the dienes before using to control the build-up of polymers.
  • Stream 101 may include 10 to 100 wt.% C 9+ compounds and all ranges and values there between, including ranges of 10 to 20 wt.%, 20 to 30 wt.%, 30 to 40 wt.%, 40 to 50 wt.%, 50 to 60 wt.%, 60 to 70 wt.%, 70 to 80 wt.%, 80 to 90 wt.%, and 90 to 100 wt.%, and 0 to 90 wt.% wash oil and all ranges and values there between, including ranges of 0 to 10%, 10 to 20%, 20 to 30%, 30 to 40%, 40 to 50%, 50 to 60%, 60 to 70%, 70 to 80%, 80 to 90%, and 90 to 100%.
  • block 201 includes flowing at least a portion of stream 101 to GHU reactor 115 and hydrogenating that portion or all of stream 101 in GHU reactor 115 to produce stream 102 comprising hydrogenated C 9+ compounds (e.g., hydrogenated hydrocarbons).
  • hydrogenated C 9+ compounds e.g., hydrogenated hydrocarbons.
  • all of stream 101 may be hydrogenated or, as shown in FIG. 1, stream 101 may be separated into stream 101-1 and stream 101-2 and only stream 101-1 is hydrogenated in GHU reactor 115.
  • GHU reactor 115 is not operated and, instead, is bypassed such that stream 101 is flowed to flash drum 116 so that only un-hydrogenated C 9+ compounds are produced.
  • system 10 is adapted to have the flexibility to produce (1) only un-hydrogenated C 9+ compounds (GHU reactor 115 not operated), (2) un-hydrogenated C 9+ compounds and hydrogenated C 9+ compounds (GHU reactor 115 operated to process only a portion of the un- hydrogenated C 9+ compounds), or (3) only hydrogenated C 9+ compounds (GHU reactor 115 operated to process all of the un-hydrogenated C 9+ compounds).
  • the reaction conditions in GHU reactor 115 include a temperature in a range of 100 to 200 °C and all ranges and values there between including ranges of 100 to 110 °C, 110 to 120 °C, 120 to 130 °C, 130 to 140 °C, 140 to 150 °C, 150 to 160 °C, 160 to 170 °C, 170 to 180 °C, 180 to 190 °C, and 190 to 200 °C, a pressure in a range of 10 to 30 bar and all ranges and values there between including ranges of 10 to 12 bar, 12 to 14 bar, 14 to 16 bar, 16 to 18 bar, 18 to 20 bar, 20 to 22 bar, 22 to 24 bar, 24 to 26 bar, 26 to 28 bar, and 28 to 30 bar, a WHSV of 2 to 8 h -1 and all ranges and values there between including ranges of 2 to 3 h -1 , 3 to 4 h -1 , 4 to 5 h -1 , 5 to 6 h 1 , 6
  • stream 102 which comprises hydrogenated C 9+ compounds is flowed to flash drum 116, wherein stream 102 is separated to produce stream 103 comprising hydrogenated wash oil and stream 104 comprising hydrogenated C 9+ compounds.
  • stream 103 comprises 0 to 90 wt.% wash oil and all ranges and values there between including ranges of 0 to 10 wt.%, 10 to 20 wt.%, 20 to 30 wt.%, 30 to 40 wt.%, 40 to 50 wt.%, 50 to 60 wt.%, 60 to 70 wt.%, 70 to 80 wt.%, and 80 to 90 wt.%
  • stream 104 comprises 10 to 100 wt.% hydrogenated C 9+ compounds and all ranges and values there between including ranges of 10 to 20 wt.%, 20 to 30 wt.%, 30 to 40 wt.%, 40 to 50 wt.%, 50 to 60 wt.%, 60 to 70 wt.%, 70 to 80 wt.%, 80 to 90 wt.%, and 90 to 100 wt.%.
  • separating pyrolysis gasoline stream 100 comprises, as shown at block 201-1, distilling the pyrolysis gas stream in depentanizer column 112 to produce stream 105 as an overhead stream comprising primarily C 4 and C 5 compounds and stream 106 as a bottoms stream comprising primarily C 6+ compounds.
  • stream 105 as an overhead stream comprising primarily C 4 and C 5 compounds
  • stream 106 as a bottoms stream comprising primarily C 6+ compounds.
  • a C 4 to C 5 fraction is separated as an un-hydrogenated stream upstream of any GHU. This provides an advantage where valuable diene components can be separated from this stream.
  • separating pyrolysis gasoline stream 100 further includes, at block 201-2, flowing stream 106 from depentanizer column 112 to deoctanizer column 113 and distilling stream 106 in deoctanizer column 113 to produce stream 107 comprising primarily C 6 to C 8 compounds and un-hydrogenated C 9+ compounds/stream 101. More specifically, at deoctanizer column 113, un-hydrogenated BTX is flowed from the top for deoctanizer column 113 and un- hydrogenated C 9+ compounds are flowed from the bottom of deoctanizer column 113.
  • the un- hydrogenated C 9+ compounds can be used un-hydrogenated or, if necessary, can be hydrogenated by passing through GHU reactor 115. This is possible because system 10 has the flexibility to be operated in any mode, either hydrogenated, un-hydrogenated, or a combination of both.
  • a separation flash drum can be installed before GHU reactor 115, where an overhead un-hydrogenated wash oil and bottom un- hydrogenated C 9+ residue can be produced.
  • the separation of the un-hydrogenated C 9+ compounds/stream 101 can require the operation of deoctanizer column 113 at low temperature, for example, 70 to 100 °C and all ranges and values there between including ranges of 70 to 75 °C, 75 to 80 °C, 80 to 85 °C, 85 to 90 °C, 90 to 95 °C, and 95 to 100 °C, on the reboiler and at high vacuum, for example 0.04 to 0.9 bara and ranges and values there between including ranges of 0.04 to 0.1 bara, 0.1 to 0.2 bara, 0.2 to 0.3 bara, 0.3 to 0.4 bara, 0.4 to 0.5 bara, 0.5 to 0.6 bara, 0.6 to 0.7 bara, 0.7 to 0.8 bara, and 0.8 to 0.9 bara.
  • deoctanizer column 113 at low temperature, for example, 70 to 100 °C and all ranges and values there between including ranges of 70 to 75 °C, 75 to 80 °C,
  • TBC package 120 supplies 4-tert -Butylcatechol (TBC), an organic chemical compound, as a fouling inhibitor to depentanizer column 112 and deoctanizer column 113.
  • TBC 4-tert -Butylcatechol
  • Process 20 may further include, at block 203, flowing stream 107 from deoctanizer column 113 to GHU reactor 114 and hydrogenating stream 107 in GHU reactor 114 to produce stream 108 comprising benzene, toluene, and xylene.
  • the reaction conditions in GHU reactor 114 include a temperature in a range of 100 °C to 200 °C and all ranges and values there between including ranges of 100 to 110 °C, 110 to 120 °C, 120 to 130 °C, 130 to 140 °C, 140 to 150 °C, 150 to 160 °C, 160 to 170 °C, 170 to 180 °C, 180 to 190 °C, and 190 to 200 °C, a pressure in a range of 10 to 30 bar and all ranges and values there between including ranges of 10 to 12 bar, 12 to 14 bar, 14 to 16 bar, 16 to 18 bar, 18 to 20 bar, 20 to 22 bar, 22 to 24 bar, 24 to 26 bar, 26 to 28 bar, and 28 to 30 bar, a WHS V of 2 to 8 h -1 and all ranges and values there between including ranges of 2 to 3 h -1 , 3 to 4 h -1 , 4 to 5 h -1 , 5 to 6 h
  • process 20 includes, at block 204, flowing stream 105 from depentanizer column 112 to stabilizer 117 and processing stream 105 in stabilizer 117 to produce stream 109 comprising fuel gas and stream 110 comprising primarily C 4 and C 5 compounds.
  • Block 205 involves flowing stream 110 from stabilizer 117 to GHU reactor 118 and hydrogenating stream 110, in GHU reactor 118, to produce stream 111 comprising primarily hydrogenated C 4 and C 5 compounds, in embodiments of the invention.
  • the reaction conditions in GHU reactor 118 includes a temperature in a range of 40 to 140 °C and all ranges and values there between including ranges of 40 to 50 °C, 50 to 60 °C, 60 to 70 °C, 70 to 80 °C, 80 to 90 °C, 90 to 100 °C, 100 to 110 °C, 110 to 120 °C, 120 to 130 °C, and 130 to 240 °C, a pressure in a range of 20 to 40 bar and all ranges and values there between including ranges of 20 to 22 bar, 22 to 24 bar, 24 to 26 bar, 26 to 28 bar, 28 to 30 bar, 30 to 32 bar, 32 to 34 bar, 34 to 36 bar, 36 to 38 bar, and 38 to 40 bar, a WHSV of 10 to 16 h -1 and all ranges and values there between including ranges of 10 to 11 h -1 , 11 to 12 h -1 , 12 to 13 h -1 , 13 to 14 h -1 , 14 to 15
  • Process 20 may further include, at block 206, flowing stream 111 from GHU reactor 118 to cracker 119 and subjecting stream 111 to cracking conditions in cracker 119 to form C 2 to C 4 light olefin, LPG, and H 2 in cracker effluent stream 122.
  • FIG. 3 shows system 30 for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ compounds, according to embodiments of the invention.
  • FIG. 4 shows process 40 for processing pyrolysis gasoline to produce a stream comprising primarily un-hydrogenated C 9+ compounds, according to embodiments of the invention.
  • System 30 may be used to implement process 40.
  • System 30, according to embodiments of the invention includes the elements 100 to 122 of system 10 as well as further elements 300 to 309.
  • process 40 in embodiments of the invention, includes operating elements 100 to 122 to carry out steps of blocks 200 to 206 as described in process 20.
  • Process 40 as implemented by system 30, like process 20 implemented by system 10, includes blocks 200 to 206, in embodiments of the invention, except that GHU reactor 118 is not required as reactor 304 can hydrogenate stream 110 and GHU reactor 114 is similarly not required.
  • Process 40 further includes, at block 400, routing stream 103, stream 107, and stream 110 to feed drum 300 where they are combined to form combined stream 301. Hydrogenation of the combined stream 301 may be carried out by injecting hydrogen stream 302, as shown at block 401, to form hydrogenated combined stream 303.
  • Block 402 involves, in embodiments of the invention, flowing hydrogenated combined stream 303 to reactor 304, where hydrogenated combined stream 303 is subjected to reaction conditions sufficient to saturate diolefins and partially saturate the olefins.
  • stream 305 is used to heat hydrogenated combined stream 303 in heat exchanger 306.
  • stream 305 is separated in separator 307 to form vapor stream 308 comprising water and H 2 and stream 309.
  • stream 309 is split into two portions, stream 309-1 and stream 309-2.
  • stream 309-2 is recycled to reactor 304.
  • stream 309-1 is separated to form a BTX stream, a stream comprising primarily hydrogenated wash oil, a fuel gas stream and a stream comprising primarily C 5 compounds.
  • FIG. 1 and FIG. 3 a stream shown from a first element or apparatus to a second element or apparatus is a disclosure that the first element or apparatus is in fluid communication with the second element or apparatus in a manner such that the flow of the stream shown, or described in the specification, can take place.
  • the systems and processes described herein can also include various equipment that is not shown and is known to one of skill in the art of chemical processing. For example, some controllers, piping, computers, valves, pumps, heaters, thermocouples, pressure indicators, mixers, heat exchangers, and the like may not be shown.
  • Embodiment 1 is a method of processing pyrolysis gasoline. The method includes separating a pyrolysis gasoline stream to produce a first stream containing primarily un hydrogenated C 9+ compounds.
  • Embodiment 2 is the method of embodiment 1 wherein the first stream contains 98 to 100 wt.% C 9+ compounds.
  • Embodiment 3 is the method of embodiment 1 further including hydrogenating a portion of the first stream to produce a second stream containing hydrogenated C 9+ hydrogenated compounds.
  • Embodiment 4 is the method of embodiment 3, wherein the hydrogenating of the first portion of the first stream is carried out under reaction conditions including a temperature in a range of 100 °C to 200 °C, a pressure in a range of 10 bar to 30 bar, a WHSV of 2 h -1 to 8 h -1 , and in the presence of a catalyst containing Ni/Al 2 O 3 to Pd/Al 2 O 3 .
  • Embodiment 5 is the method of either of embodiments 3 or 4 further including separating the second stream to produce a third stream containing hydrogenated wash oil and a fourth stream containing hydrogenated C 9+ residue.
  • Embodiment 6 is the method of embodiment wherein third stream contains 0 to 90 wt.% wash oil and the fourth stream contains 10 to 100 wt.% hydrogenated C 9+ compounds.
  • Embodiment 7 is the method of either of embodiments 5 or 6, further including subjecting the third stream to reaction conditions to hydrogenate the third stream.
  • Embodiment 8 is the method of embodiment 1, wherein the separating of the pyrolysis gasoline stream includes distilling the pyrolysis gas stream in a depentanizer column to produce a fifth stream containing primarily C 4+ compounds and a sixth stream containing primarily C 6+ compounds.
  • Embodiment 9 is the method of embodiment 8 wherein the separating of the pyrolysis gasoline stream further includes distilling the sixth stream in a deoctanizer column to produce a seventh stream containing primarily C 6 to C 8 compounds and the first stream.
  • Embodiment 10 is the method of embodiment 9 including hydrogenating the seventh stream to produce an eighth stream containing benzene, toluene, and xylene.
  • Embodiment 11 is the method of embodiment 10, wherein the hydrogenating of the seventh stream is carried out under reaction conditions including a temperature in a range of 100 °C to 200 °C, a pressure in a range of 10 bar to 30 bar, a WHSV of 2 h -1 to 8 h -1 , and in presence of a catalyst containing Ni/Al 2 O 3 , to Pd/Al 2 O 3 ,.
  • Embodiment 12 is the method of embodiment 8 further including processing the fifth stream in a stabilizer to produce a ninth stream including fuel gas and a tenth stream containing primarily C 4 and C 5 compounds.
  • Embodiment 13 is the method of embodiment 12 further including hydrogenating the tenth stream to produce an eleventh stream containing primarily C 4 and C 5 compounds.
  • Embodiment 14 is the method of embodiment 13, wherein the hydrogenating of the tenth stream is carried out under reaction conditions including a temperature in a range of 40 °C to 140 °C, a pressure in a range of 20 bar to 40 bar, a WHSV of 10 h -1 to 16 h -1 , and in presence of a catalyst containing Ni/Al 2 O 3 to Pd/Al 2 O 3 .
  • Embodiment 15 is the method of either of embodiments 13 or 14 further including subjecting the eleventh stream to cracking conditions to form C 2 to C 4 light olefins, LPG, and H 2 .
  • Embodiment 16 is method of processing pyrolysis gasoline. The method includes concurrently producing (1) a first stream containing primarily un-hydro genated C 9+ compounds and (2) a second stream containing hydrogenated C 9+ hydrogenated compounds, wherein the producing includes separating a pyrolysis gasoline stream to produce the first stream containing primarily un-hydrogenated C 9+ compounds and hydrogenating a portion of the first stream to produce the second stream containing hydrogenated C 9+ hydrogenated compounds.
  • Embodiment 17 is the method of embodiment 16 further including producing a stream containing primarily un-hydrogenated C 4+ compounds.
  • Embodiment 18 is a method of processing pyrolysis gasoline.
  • the method includes separating a pyrolysis gasoline stream to produce a first stream containing primarily un- hydrogenated C 9+ compounds and hydrogenating a portion of the first stream to produce a second stream containing hydrogenated C 9+ compounds.
  • the method further includes separating the second stream to produce a third stream containing hydrogenated wash oil and a fourth stream containing hydrogenated C 9+ residue
  • the separating of the pyrolysis gasoline stream includes distilling the pyrolysis gas stream in a depentanizer column to produce a fifth stream containing primarily C 4+ compounds and a sixth stream containing primarily C 6+ compounds.
  • the method also includes distilling the sixth stream in a deoctanizer column to produce a seventh stream containing primarily C 6 to C 8 compounds and the first stream.
  • the method includes processing the fifth stream in a stabilizer to produce a ninth stream containing fuel gas and a tenth stream containing primarily C 4 and C 5 compounds.
  • the method further includes combining the third stream, the seventh stream, and the tenth stream to form a combined stream and flowing the combined stream to a reactor.
  • Embodiment 19 is the method of embodiment 18, further including subjecting the combined stream to reaction conditions sufficient to form a reactor effluent.
  • Embodiment 20 is the method of embodiment 19 further including processing the reactor effluent to produce a BTX stream, a stream containing primarily hydrogenated wash oil, a fuel gas stream and a stream containing primarily C 5 compounds.
  • a first cut model was built in Aspen-Plus V10 Software. Simulations were performed according to an embodiment of the current disclosure as shown in FIG. 5. Separated streams containing C 4 - C 5 compounds, un-hydrogenated C 6 to C 8 compounds, un- hydrogenated wash oil, un-hydrogenated C 9+ residues were obtained from a pyrolysis gasoline stream.
  • the pyrolysis gasoline stream contained C 4 compounds, C 5 compounds, benzene, toluene, xylene, styrene, indene, indane, dicyclopentadiene (DCPD), methyldicyclopentadiene (MDCPD), and others (e.g.
  • the pyrolysis gasoline stream was distilled in a depentanizer column to obtain a stream containing the C 4 and C 5 compounds from the top of the column, and a C 6+ stream containing un-hydrogenated C 6+ compounds from the bottom of the column.
  • the C 6+ stream contained benzene, toluene, xylene, styrene, indene, indane, DCPD, MDCPD and the other.
  • the C 6+ stream was distilled in a deoctanizer column to obtain a C 6-8 stream containing un-hydrogenated C 6 to C 8 compounds from the top of the column, and a C 9+ stream containing un-hydrogenated C 9+ compounds from the bottom of the column.
  • the C 6-8 stream contained benzene, toluene, xylene and a portion of other (e.g. C 6 -C 8 paraffinic and olefinic components,).
  • the C 9+ stream contained styrene, indene, indane, DCPD, MDCPD and a portion of the other (e.g. C 9+ paraffinic, olefinic, napthenic and aromatic components).
  • the C 9+ stream was separated in a separation flash drum to obtain a stream containing un- hydrogenated wash oil from the top and a stream containing un-hydrogenated C 9+ residues from the bottom.
  • the compositions, flow rate of the streams are provided in Tables 1-7.
  • TBC 4-tert -Butylcatechol

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Abstract

L'invention concerne un système et un procédé de traitement d'essence de pyrolyse. Le système et le procédé comprennent la séparation d'un flux d'essence de pyrolyse pour produire un premier flux comprenant principalement des composés C9+ non hydrogénés. La séparation de l'essence de pyrolyse se produit sans hydrogénation effectuée sur l'essence de pyrolyse avant la séparation.
EP20743352.5A 2019-07-15 2020-07-13 Système et procédé de production de composés en c9+ non hydrogénés et hydrogénés Pending EP3999614A1 (fr)

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AU2020314880B2 (en) 2023-03-09
SA522431355B1 (ar) 2024-04-03
CA3146793A1 (fr) 2021-01-21
CN114008179A (zh) 2022-02-01
AU2020314880A1 (en) 2022-01-27
US20220315847A1 (en) 2022-10-06

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