WO2016174145A1 - Heavy gasoline separation - Google Patents

Heavy gasoline separation Download PDF

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Publication number
WO2016174145A1
WO2016174145A1 PCT/EP2016/059503 EP2016059503W WO2016174145A1 WO 2016174145 A1 WO2016174145 A1 WO 2016174145A1 EP 2016059503 W EP2016059503 W EP 2016059503W WO 2016174145 A1 WO2016174145 A1 WO 2016174145A1
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WO
WIPO (PCT)
Prior art keywords
durene
rich
fraction
gasoline
splitter
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.)
Ceased
Application number
PCT/EP2016/059503
Other languages
French (fr)
Inventor
Arne Knudsen
Jan Due NIELSEN
Ian MENJON
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.)
Topsoe AS
Original Assignee
Haldor Topsoe AS
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 Haldor Topsoe AS filed Critical Haldor Topsoe AS
Publication of WO2016174145A1 publication Critical patent/WO2016174145A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • 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
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °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
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C

Definitions

  • raw gasoline, light ends, LPG and wa ⁇ ter are produced from methanol.
  • the majority of the raw gasoline is already within the gasoline range with rela ⁇ tively good product properties, but some fraction is too heavy or contains too much durene and therefore it needs to be treated.
  • Treatment of the raw gasoline may be achieved by a process for treating raw synthetic gasoline, said process compris ⁇ ing the steps of
  • a first splitter separating a raw gasoline stream into at least a first light fraction, a first durene rich fraction and a heavy gasoline fraction
  • a second splitter separating the first durene rich fraction into a second light fraction and a second durene rich fraction.
  • the first light fraction may be ready for blending in the gasoline product pool.
  • the present setup with the second splitter may advanta ⁇ geously be applied in relation to a gasoline upgrading unit (GUU) i.e. where the second durene rich gasoline fraction is sent to a gasoline upgrading unit in which the second durene rich fraction is upgraded to an upgraded product stream.
  • GUI gasoline upgrading unit
  • the second splitter and separation of the first durene rich fraction into a second durene rich fraction and second light fraction is advantageously ap- plied as it ensures that a good separation is achieved and an optimized stream (second durene rich fraction) is send to the GUU.
  • the durene content may be reduced and the octane number increased in the upgraded product stream compared to the second durene rich gasoline fraction.
  • Reduced durene content and/or increased octane number may be an advantage as durene may negatively influence cloud point and in ⁇ creased octane number may provide a better fuel.
  • the durene rich gasoline fraction is subject to isomerization, (mild) hydrotreatment and/or
  • a stabilization step (such as mild hydrocracking) may also take place in the GUU.
  • Stabilization may e.g. be carried out by stripping (e.g. with steam, N 2 , LPG) and/or by dis ⁇ tillation in the GUU.
  • the GUU may comprise at least one reaction step and at least one stabilization step.
  • the first splitter comprises a number of stages for example 5 - 50 stages, such as 10 - 30 stages, such as 15 - 20 stages. More stages provide a more refined separation and fewer stages results in a more crude separation which for example may result in more light components in the heavy fraction and/or the need to recycle more heavy components separated from the first light fraction to the first split ⁇ ter .
  • the first durene rich stream is separated from the first splitter in the rectification zone.
  • the first durene rich fraction may be separated from the first splitter in a centre zone of the splitter such as at or near one or more middle stages. If e.g. the first split ⁇ ter comprises 16 stages, the first durene rich stream may be separated near the 6 th - 10 th stage, such as by the 8 th stage.
  • first durene rich stream is separated from the first splitter in order to maximize 1 , 2 , 4-trimethylbenzene and/or durene in the second durene rich stream sent to the GUU it may be possible to optimize its operation.
  • first durene rich stream may be separated from the first splitter in order to minimize the concentration of xylenes since xylenes may de-alkylate in an isomerization reactor which entails a yield loss.
  • the present invention may advantageously be used in relation to synthetic raw gasoline as the composition of the synthetic raw gasoline may be well known whereby the specific components to be separated from the first splitter into the first durene rich stream can be selected as de ⁇ scribed above.
  • the heavy gasoline constitutes a no sulfur fuel .
  • the present application also relates to a plant for treat- ing raw gasoline comprising
  • a first splitter wherein raw gasoline is separated in ⁇ to a light fraction, a durene rich gasoline fraction and a heavy gasoline fraction
  • a second splitter wherein the durene rich gasoline fraction is separated into a second light fraction and a second durene rich stream
  • a GUU for upgrading the second durene rich stream into a upgraded product may further be arranged so that the first durene rich stream is separated from the first splitter in order to maximize 1 , 2 , 4-trimethylbenzene and/or durene and/or in order to minimize the concentration of xylenes in the second durene rich stream sent to the GUU.
  • the second durene rich fraction is sent to the gasoline upgrading unit (GUU) , thus minimizing the LPG production and allowing a better control of the final boiling point of the final product .
  • GUI gasoline upgrading unit
  • Fig. 1 illustrates the process flow and simplified plant layout .
  • Fig. 2 Illustrates Concentration curves in the first split- ter.
  • Figure 1 illustrates the process flow and plant.
  • the stabi ⁇ lized gasoline [1] is separated in a first gasoline split ⁇ ter distillation column [11] into a first light fraction (IBP ⁇ 165°C) [5] which is ready for product blending, a first durene rich fraction (138- 198°C) [8] and a heavy gasoline fraction (195 - 260°C) [9].
  • the gas phase (first light fraction) leaves the overhead [2] and is condensed [12] and recovered [13] .
  • a reflux pump [14] is typically used to return the liquid to the column [4] and/or to send the first light gasoline fraction to storage and/or blending.
  • a second splitter (side column) [15] ensures that a good separation is achieved.
  • a reboiler [17] supplies the heat input for the separation in the gasoline splitter.
  • the first durene rich fraction [6] which typically consti- tutes a -25 wt% of the stabilized gasoline, is sent to a second splitter (side column) where the gas phase [7] is returned to the first splitter and a second durene rich fraction is taken from the bottom.
  • a reboiler [16] may be used to supply the necessary heat input to drive the sepa- ration.
  • the second durene rich fraction is sent to a GUU where durene content is reduced and/or octane number (RON, MON) is increased.
  • GUU Durene may be isomerized to other types of tet- ra-methlybenzenes and/or de-alkylate to trymethyl benzenes.
  • Tri methylbenzenes may be isomerized to other types of tri- methylebenzenes and/or de-alkylate to xylenes and/or tolu- ene and/or benzene.
  • Gases may be produced as a consequence (C1-C4) .
  • the heavy gasoline fraction may e.g. be used as a no-sulfur fuel or sent to post treatment.
  • Fig 2 illustrates where the first durene rich fraction may be taken from the first separator based on the concentra ⁇ tions of various components.
  • the curves are normalised and the values on the x-axis is tray number, i.e. the present example is for a 16 tray column.
  • Concentration curves are indicated by A, B, C.
  • the first durene rich stream may advantageously be separated from the first splitter at or near (e.g.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The present relates to a plant and a process for treating raw gasoline, said process comprising the steps of (1) In a first splitter separating a raw gasoline stream into at least a first light fraction, a first durene rich fraction and a heavy gasoline fraction, and (2) In a second splitter separating the first durene rich fraction into a second light fraction and a second durene rich fraction.

Description

Title: Heavy gasoline separation
In the MTG processes, raw gasoline, light ends, LPG and wa¬ ter are produced from methanol. The majority of the raw gasoline is already within the gasoline range with rela¬ tively good product properties, but some fraction is too heavy or contains too much durene and therefore it needs to be treated. Treatment of the raw gasoline may be achieved by a process for treating raw synthetic gasoline, said process compris¬ ing the steps of
In a first splitter separating a raw gasoline stream into at least a first light fraction, a first durene rich fraction and a heavy gasoline fraction, and
In a second splitter separating the first durene rich fraction into a second light fraction and a second durene rich fraction. By splitting the first durene rich fraction in a second splitter it is possible to have detailed control of the composition of the second durene rich fraction. Depending on the use and further treatment of the second durene rich fraction in may be highly advantageous to have a reduced content of light gasoline in the second durene rich frac¬ tion.
The first light fraction may be ready for blending in the gasoline product pool.
The present setup with the second splitter may advanta¬ geously be applied in relation to a gasoline upgrading unit (GUU) i.e. where the second durene rich gasoline fraction is sent to a gasoline upgrading unit in which the second durene rich fraction is upgraded to an upgraded product stream. If light gasoline is sent to the GUU it may nega- tively contribute to a lover product yield and a higher gas/LPG yield due to cracking/de-alkylation reactions in the GUU. Therefore the second splitter and separation of the first durene rich fraction into a second durene rich fraction and second light fraction is advantageously ap- plied as it ensures that a good separation is achieved and an optimized stream (second durene rich fraction) is send to the GUU.
From the GUU an upgraded product stream and a third LPG stream is withdrawn.
In the GUU the durene content may be reduced and the octane number increased in the upgraded product stream compared to the second durene rich gasoline fraction. Reduced durene content and/or increased octane number may be an advantage as durene may negatively influence cloud point and in¬ creased octane number may provide a better fuel.
In several embodiments the durene rich gasoline fraction is subject to isomerization, (mild) hydrotreatment and/or
(mild) hydrocracking in the gasoline upgrading unit (GUU) .
A stabilization step (such as mild hydrocracking) may also take place in the GUU. Stabilization may e.g. be carried out by stripping (e.g. with steam, N2, LPG) and/or by dis¬ tillation in the GUU. I.e. the GUU may comprise at least one reaction step and at least one stabilization step.
The first splitter comprises a number of stages for example 5 - 50 stages, such as 10 - 30 stages, such as 15 - 20 stages. More stages provide a more refined separation and fewer stages results in a more crude separation which for example may result in more light components in the heavy fraction and/or the need to recycle more heavy components separated from the first light fraction to the first split¬ ter .
Preferably, the first durene rich stream is separated from the first splitter in the rectification zone. For example the first durene rich fraction may be separated from the first splitter in a centre zone of the splitter such as at or near one or more middle stages. If e.g. the first split¬ ter comprises 16 stages, the first durene rich stream may be separated near the 6th - 10th stage, such as by the 8th stage.
By selecting the point of separation from the first splitter it is possible to adjust the composition of the first durene rich fraction.
If the first durene rich stream is separated from the first splitter in order to maximize 1 , 2 , 4-trimethylbenzene and/or durene in the second durene rich stream sent to the GUU it may be possible to optimize its operation.
Also the first durene rich stream may be separated from the first splitter in order to minimize the concentration of xylenes since xylenes may de-alkylate in an isomerization reactor which entails a yield loss.
Thus, the present invention may advantageously be used in relation to synthetic raw gasoline as the composition of the synthetic raw gasoline may be well known whereby the specific components to be separated from the first splitter into the first durene rich stream can be selected as de¬ scribed above.
In some embodiments the heavy gasoline constitutes a no sulfur fuel .
The present application also relates to a plant for treat- ing raw gasoline comprising
A first splitter wherein raw gasoline is separated in¬ to a light fraction, a durene rich gasoline fraction and a heavy gasoline fraction
A second splitter wherein the durene rich gasoline fraction is separated into a second light fraction and a second durene rich stream
A GUU for upgrading the second durene rich stream into a upgraded product . The plant may further be arranged so that the first durene rich stream is separated from the first splitter in order to maximize 1 , 2 , 4-trimethylbenzene and/or durene and/or in order to minimize the concentration of xylenes in the second durene rich stream sent to the GUU.
Thus, according to the present process and plant the second durene rich fraction is sent to the gasoline upgrading unit (GUU) , thus minimizing the LPG production and allowing a better control of the final boiling point of the final product . The invention is further illustrated in the drawings
Fig. 1 illustrates the process flow and simplified plant layout .
Fig. 2 Illustrates Concentration curves in the first split- ter.
The drawings are exemplary and are not to be construed as limiting to the invention. Figure 1 illustrates the process flow and plant. The stabi¬ lized gasoline [1] is separated in a first gasoline split¬ ter distillation column [11] into a first light fraction (IBP ~ 165°C) [5] which is ready for product blending, a first durene rich fraction (138- 198°C) [8] and a heavy gasoline fraction (195 - 260°C) [9].
The gas phase (first light fraction) leaves the overhead [2] and is condensed [12] and recovered [13] . A reflux pump [14] is typically used to return the liquid to the column [4] and/or to send the first light gasoline fraction to storage and/or blending.
If light gasoline is sent to the GUU [18] it may negatively contribute to a higher gas/LPG yield due to cracking and/or de-alkylation reactions, therefore a second splitter (side column) [15] ensures that a good separation is achieved. A reboiler [17] supplies the heat input for the separation in the gasoline splitter.
The first durene rich fraction [6], which typically consti- tutes a -25 wt% of the stabilized gasoline, is sent to a second splitter (side column) where the gas phase [7] is returned to the first splitter and a second durene rich fraction is taken from the bottom. A reboiler [16] may be used to supply the necessary heat input to drive the sepa- ration.
The second durene rich fraction is sent to a GUU where durene content is reduced and/or octane number (RON, MON) is increased.
In the GUU Durene may be isomerized to other types of tet- ra-methlybenzenes and/or de-alkylate to trymethyl benzenes. Tri methylbenzenes may be isomerized to other types of tri- methylebenzenes and/or de-alkylate to xylenes and/or tolu- ene and/or benzene. Gases may be produced as a consequence (C1-C4) .
The heavy gasoline fraction may e.g. be used as a no-sulfur fuel or sent to post treatment.
Fig 2 illustrates where the first durene rich fraction may be taken from the first separator based on the concentra¬ tions of various components. The curves are normalised and the values on the x-axis is tray number, i.e. the present example is for a 16 tray column. Concentration curves are indicated by A, B, C. For example the first durene rich stream may advantageously be separated from the first splitter at or near (e.g. +/- 1 or +/- 2 ) the 8 tray, as this point may result in a first durene rich fraction which is relatively low in Xylenes (A) while containing a sub¬ stantial amount of the desired components (B, C) for exam- pie tetra-methlybenzenes (incl. durene) and 1,2,4- trimethylbenzene .

Claims

Claims
1. Process for treating raw gasoline, said process com' prising the steps of
- In a first splitter separating a raw gasoline
stream into at least a first light fraction, a first durene rich fraction and a heavy gasoline fraction, and
- In a second splitter separating the first durene rich fraction into a second light fraction and a second durene rich fraction.
. Process for treating raw gasoline according to claim wherein the first light fraction is ready for blend¬ ing .
Process for treating raw gasoline according to any of the preceding claims, wherein the second durene rich gasoline fraction is sent to a gasoline upgrading unit wherein the second durene rich fraction is upgraded to an upgraded product .
Process for treating raw gasoline according to any of the preceding claims, wherein the durene content is reduced and the octane number increased in the upgrad ed product stream compared to the second durene rich gasoline fraction.
5. Process for treating raw gasoline according to any of the preceding claims, wherein the second durene rich gasoline fraction is subject to isomerization, (mild) hydrotreatment and/or hydrocracking in the gasoline upgrading unit.
. Process for treating raw gasoline according to any of the preceding claims, wherein the first durene rich stream is separated from the first splitter in order to maximize 1 , 2 , 4-trimethylbenzene and/or durene in the second durene rich stream sent to the GUU.
Process for treating raw gasoline according to any of the preceding claims, wherein the first durene rich stream is separated from the first splitter in order to minimize the concentration of xylenes in the second durene rich stream sent to the GUU.
Process for treating raw gasoline according to any of the preceding claims, wherein the heavy gasoline constitutes a no sulfur fuel. 9. Plant for treating raw gasoline comprising
- A first splitter wherein raw gasoline is separated in¬ to a first light fraction, a first durene rich frac¬ tion and a heavy gasoline fraction
- A second splitter, wherein the first durene rich gaso- line fraction is separated into a second light frac¬ tion and a second durene rich fraction
- A GUU for upgrading the second durene rich fraction into an upgraded product.
10. A plant according to claim 9, wherein the first durene rich steam is separated from the first split- ter in order to maximize 1 , 2 , 4-trimethylbenzene and/or durene in the second durene rich stream sent to the GUU.
A plant according to claim 9 or 10, wherein the first durene rich stream is separated from the first splitter in order to minimize the concentration of xylenes in the second durene rich stream sent to the GUU .
PCT/EP2016/059503 2015-04-28 2016-04-28 Heavy gasoline separation Ceased WO2016174145A1 (en)

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Application Number Priority Date Filing Date Title
DKPA201570246 2015-04-28
DKPA201570246 2015-04-28

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Publication Number Publication Date
WO2016174145A1 true WO2016174145A1 (en) 2016-11-03

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2025021688A1 (en) * 2023-07-26 2025-01-30 Shell Internationale Research Maatschappij B.V. Gasoline fuel compositions

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2239965A (en) * 1937-08-28 1941-04-29 Universal Oil Prod Co Treatment of hydrocarbon oils
US2348815A (en) * 1939-06-20 1944-05-16 Texas Co Manufacture of motor fuel
GB1408758A (en) * 1971-12-06 1975-10-01 Shell Int Research Process for producing from gasoline starting material containing c5and hydrocarbons including normal paraffins a gasoline product of higher octane number than said gasoline starting material
US4304951A (en) * 1981-01-14 1981-12-08 Mobil Oil Corporation Hydrotreating of bottoms fractions resulting from conversion of methanol to gasoline in order to decrease durene and produce distillate
US4524227A (en) * 1983-09-29 1985-06-18 Mobil Oil Corporation Coproduction of durene and gasoline from synthesis gas and alcohols and separation of durene-gasoline mixtures
US4747933A (en) * 1987-03-27 1988-05-31 Uop Inc. Isomerization unit with integrated feed and product separation facilities
US4950387A (en) * 1988-10-21 1990-08-21 Mobil Oil Corp. Upgrading of cracking gasoline
CN103351887A (en) * 2013-07-08 2013-10-16 常熟市联邦化工有限公司 Process for preparing high temperature heat transfer oil base oil by using C10 heavy aromatic residual oil
US20150094510A1 (en) * 2012-05-29 2015-04-02 Haldor Topsøe A/S Process for synthesis of alcohols

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2239965A (en) * 1937-08-28 1941-04-29 Universal Oil Prod Co Treatment of hydrocarbon oils
US2348815A (en) * 1939-06-20 1944-05-16 Texas Co Manufacture of motor fuel
GB1408758A (en) * 1971-12-06 1975-10-01 Shell Int Research Process for producing from gasoline starting material containing c5and hydrocarbons including normal paraffins a gasoline product of higher octane number than said gasoline starting material
US4304951A (en) * 1981-01-14 1981-12-08 Mobil Oil Corporation Hydrotreating of bottoms fractions resulting from conversion of methanol to gasoline in order to decrease durene and produce distillate
US4524227A (en) * 1983-09-29 1985-06-18 Mobil Oil Corporation Coproduction of durene and gasoline from synthesis gas and alcohols and separation of durene-gasoline mixtures
US4747933A (en) * 1987-03-27 1988-05-31 Uop Inc. Isomerization unit with integrated feed and product separation facilities
US4950387A (en) * 1988-10-21 1990-08-21 Mobil Oil Corp. Upgrading of cracking gasoline
US20150094510A1 (en) * 2012-05-29 2015-04-02 Haldor Topsøe A/S Process for synthesis of alcohols
CN103351887A (en) * 2013-07-08 2013-10-16 常熟市联邦化工有限公司 Process for preparing high temperature heat transfer oil base oil by using C10 heavy aromatic residual oil

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2025021688A1 (en) * 2023-07-26 2025-01-30 Shell Internationale Research Maatschappij B.V. Gasoline fuel compositions

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