EP3137578A1 - Verfahren und anlage zur gewinnung von rohölprodukten - Google Patents
Verfahren und anlage zur gewinnung von rohölproduktenInfo
- Publication number
- EP3137578A1 EP3137578A1 EP15721173.1A EP15721173A EP3137578A1 EP 3137578 A1 EP3137578 A1 EP 3137578A1 EP 15721173 A EP15721173 A EP 15721173A EP 3137578 A1 EP3137578 A1 EP 3137578A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- stream
- crude oil
- hydrocarbons
- distillation
- quench
- 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.)
- Granted
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
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
-
- 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
-
- 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
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
-
- 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
- C10G9/002—Cooling of cracked gases
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
-
- 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 invention relates to a method and a plant for the production of
- Crude oil is first desalinated in known refinery processes and after heating a fractional distillation at atmospheric pressure (hereinafter referred to as
- each cracking furnace is therefore a structural unit used for steam cracking in which identical or comparable reaction conditions are present.
- a steam cracking plant may comprise one or more cracking furnaces.
- a fission gas stream is understood here to mean a gaseous stream which is formed from the effluent of one or more cracking furnaces.
- the cracked gas stream also referred to as cracker effluent
- a quench gas cooler for example a linear cooler (transfer line
- the first cooling step i. the cooling of the quenching gas with cooling water, for example in the quench cooler, referred to as quenching.
- quenching the cooling of the quenching gas with cooling water
- the cracked gas is cooled only indirectly and not, as in the second cooling step, with a liquid
- the second cooling step may therefore also be referred to as oil quench for better distinctness.
- the stream formed by combining the cracked gas stream with the liquid stream used for quenching is referred to herein as quench effluent.
- quench effluent stream comprises all of the liquid stream used for quenching and compounds derived from the cracked gas stream which may at most be equivalent
- the mass flow of the quench effluent corresponds to the sum of the mass flow of the liquid stream used for quenching and the mass flow of the cracked gas stream, It is therefore explicitly not the product of a separation or deposition process.
- the Quenchabstrom is immediately after the union of the quenching
- the invention proposes a method for recovering crude oil products in which a gaseous stream is formed from a first crude oil stream and the gaseous stream is at least partially subjected to a steam cracking process. In the steam cracking process, a split gas flow is generated.
- one or more cracking furnaces are supplied. If several cracking furnaces are present, they can also be charged with different currents. As is generally known, the charging of the cracking furnaces takes place in each case after the addition of water vapor. The resulting cleavage gas stream is at least partially to obtain a
- the present invention proposes to use at least part of the quench effluent to form a separation insert and to separate the separation insert together with a second crude oil stream to obtain distillate effluents by distillation.
- the separation insert may be formed from the quench effluent in any manner, but always contains within the quench effluent
- Hydrocarbons having one, two, three, four or more carbon atoms and / or from such hydrocarbons, for example by hydrogenating or
- hydrocarbons for example, methane, ethane, ethylene, acetylene, propane, propylene and
- the separation insert advantageously contains hydrocarbons previously contained in the quench liquid hydrocarbon stream and / or compounds formed from such hydrocarbons. These are typically hydrocarbons with more than ten or twenty and more
- the present invention achieves full integration into a refinery by, for example, feeding the quench effluent or separation feedstock entirely to atmospheric distillation in a correspondingly configured distillation column along with the second crude stream.
- This makes it possible to dispense with separate separation means for hydrocarbons in the steam gap stream or the Quenchabstrom.
- the compounds contained in the liquid hydrocarbon stream used for quenching pass into the respective fractions, for example the vacuum gas oil or the atmospheric gas oil, according to their boiling point. A separate separation of the liquid used in the quenching
- Hydrocarbon Ström compounds contained in the manner of a conventional oil column is not required.
- a water quench is also eliminated since pyrolysis gasoline also passes into the corresponding fractions of the crude oil distillation, namely the gasoline fractions.
- a separate compression of Quenchabstroms is also not required in the invention.
- the inventive method can therefore be with significantly less
- US 2010/03201 19 A1 discloses a method in which a quench effluent is fed to a primary fractionation to obtain different streams.
- US 2010/03201 19 A1 explicitly teaches to prepare a tar stream from the primary fractionation and to use it in a quench oil cycle, the introduction of a second crude oil stream into the primary fractionation is prohibited since this would make it impossible to obtain the tar stream by the additionally fed crude oil components .
- the Quenchabstrom contains a considerable proportion of finely divided oil droplets from the quenching liquid stream and heavy components (oils, tars and the like), it is first freed in conventional vapor cracking process in a so-called oil column of corresponding components. Only downstream of the oil column, a corresponding stream of the known separation stages for recovering the hydrocarbon products from the cracking gas can be supplied.
- Quenchabstrom is subjected together with the second crude oil stream, removed and go into the appropriate (s) fraction (s).
- a particularly advantageous embodiment of the invention provides to form said gaseous stream by evaporation from the first crude oil stream, wherein a portion of the crude oil stream remaining liquid during the evaporation is used at least in part to form the liquid hydrocarbon stream used for quenching. It is particularly advantageous if the liquid hydrocarbon stream used for quenching is poor or free of components which have been separated off from the quench waste stream or a stream formed from the quench waste stream. In other words, in the context of the present invention, the liquid hydrocarbon stream used for quenching is advantageously not submerged Use of a recycle stream formed and there is no Quenchniklauf used, as it is known from conventional methods.
- a so-called oil column with two sections arranged one above the other is used.
- the quench oil is given up at the top of the lower section.
- a lower portion of the lower portion of the cracked gas stream is fed and sent towards the Quenchöl.
- the gap gas stream contained heavy compounds are dissolved or suspended in the quench oil and the gap gas stream is cooled simultaneously.
- the quench oil with the optionally dissolved or suspended therein compounds is withdrawn from the bottom of the oil column, optionally treated, and returned to the head of the lower portion of the oil column again.
- pyrolysis gasoline is abandoned, which is separated in a downstream water quench and also partially circulated.
- the disadvantage of conventional quench circuits is the aging of the
- quench oil Due to the frequent contacts with the hot cleavage gas stream, the initially low-viscosity compounds are polymerized and the formation of soot and tar or other tough, high-boiling compounds occurs. The quench oil must therefore be replaced regularly and replaced by fresh
- Quench oil be replaced.
- the aged quench oil is practically worthless.
- the liquid hydrocarbon stream used according to the preferred embodiment for quenching is poor in or free of components separated from the quench effluent stream or a stream formed from the quench effluent, with little or no aging process because it is lean or free from components contained, not recycled compounds only once with the
- Spaltgasstrom come into contact. This one-time contact does not lead to aging reactions and the corresponding compounds can in
- the split gas stream leaves the radiation zone of the cracking furnace (s) at a temperature of typically 750 to 875 ⁇ .
- the splashing gas flow should be for
- the cracked gas stream conventionally enters the oil column at a temperature of about 230 ° C. and leaves it at a temperature of about 100 ° C. The majority of the heat is dissipated by the quench oil.
- the temperature of the quenching gas is reduced from a temperature value in a first temperature range to a temperature value in a second temperature range, wherein the temperature value in the second temperature range by about 130 ⁇ I ⁇ lower than the temperature value in the first temperature range .
- the temperature difference between the temperature values is significantly higher.
- a method is known in which a non-vaporized portion of a crude oil stream is used for a pre-quench of a cracked gas stream obtained by steam cracking a vaporized portion of the crude oil stream.
- the pre-quench is made to cleave, but still cleavable components contained in the non-evaporated portion by the heat of the cracked gas stream.
- the addition of the unevaporated fraction to the cracked gas stream in the course of the pre-quenching therefore takes place at a still high temperature of the cracked gas stream.
- the temperature of the quenching gas in the preamble is reduced from a temperature value in a first temperature range to a temperature value in a second temperature range, wherein the temperature value in the second temperature range is at most 1 1 1 ⁇ lower than the
- Temperature value in the first temperature range is at least 649 ⁇ C.
- Hydrocarbon ström the Quenchabstrom obtained at a temperature which is in a temperature range of 0 to 250 ⁇ , in particular from 50 to 200 ⁇ or from 50 to 150 ⁇ , ie at a temperature which is also achieved in a conventional oil column, and the a direct further processing of Quenchabstroms allows.
- the cracked gas stream, before it is quenched with the liquid hydrocarbon Ström has already been cooled to a temperature which is 50 to 200 ⁇ , for example 100 to 150 ⁇ , above the temperature of Quenchabstroms and for example the typical
- Incoming temperatures corresponds to an oil column in a conventional method.
- the invention makes it possible in this particularly preferred embodiment to dispense with the use of further quench oil, in particular an oil circuit.
- Another advantage that results from not using an oil circuit, is that, for example, the conventionally provided heat recovery from the cracking gas by consuming
- Heat exchanger in the oil circuit is eliminated and the heat through the Quenchabstrom directly can be supplied to another consumer.
- the heat can be used, for example, for (pre) heating the streams used in the atmospheric distillation.
- the separating insert is formed from at least part of the quenching flow, which, together with the second
- Crude oil is separated by distillation to obtain distillation effluents.
- This distillative separation is advantageously carried out initially in a distillation column for fractional distillation at atmospheric distillation, as it is also used in a conventional refinery.
- the atmospheric pressure is advantageously carried out initially in a distillation column for fractional distillation at atmospheric distillation, as it is also used in a conventional refinery.
- Distillation may be a vacuum distillation set up in a dedicated
- distillation effluents All streams (cuts, fractions) formed in the distillation (for example, atmospheric distillation and / or vacuum distillation) are referred to herein as distillation effluents.
- the present invention proposes in an advantageous
- the separation insert such as conventional crude oil streams also, together with the second crude oil stream initially in an atmospheric
- Refinery process used distillation column for atmospheric distillation functionally merged.
- the products of the steam cracking process withdrawn from the top or from the top of the atmospheric distillation column may be subjected, together with corresponding light products from the crude oil stream, if present, to the post-cracking gas separation steps usually following the oil column of a steam cracking process.
- a water wash can be used, in which, if necessary, the naphtha still present in a corresponding stream in liquid form is deposited. After washing with water, hydrocarbons having one to four carbon atoms typically remain in the gas phase. These can then be subjected to known separation sequences (Demethanizer First, Deethanizer First, etc., for details, see the cited technical literature).
- Distillation effluents are composed of heavier hydrocarbons, predominantly from the uncleaved crude oil or for quenching
- recycle streams Such streams subjected to the steam cracking process are referred to as recycle streams. Recycled streams may be combined and together or separately, optionally together with
- Fresh inserts the same or different cracking furnaces are supplied.
- the already explained, formed in the evaporation of the crude oil stream gaseous stream is used, but it can also be used other, supplied from the plant boundary streams.
- the separation of the fractions provided as recycle streams can be carried out, for example, in the customary separation devices which are provided in the context of the present invention, similar to conventional steam-splitting processes. Separate separation of corresponding light fractions, as conventionally carried out in a refinery, can therefore be dispensed with. Such light fractions, because they can be supplied to the steam cracking process as recycle streams, need not be stored in tanks as in conventional refinery plants. As also explained below, the compounds contained in corresponding streams can also be at least partially further implemented.
- the result of the inventive measures the advantage that can be dispensed with an oil column, and that no pyrolysis oil and no
- the process according to the invention can also be configured by recycling all distillation effluents which are not desired as products such that they are no longer used for the production of typical refinery products such as gasoline, diesel, heating oil, etc.
- the said components may be used, for example after appropriate treatment such as hydrotreats or (mild) hydrocracking, together or separately, as an insert for the steam cracking process.
- appropriate treatment such as hydrotreats or (mild) hydrocracking
- ethylene, propylene, butadiene, aromatics and high-pressure steam or electricity can be obtained from the crude oil used.
- This variant proves to be extremely economical.
- the method according to the invention can be flexibly adapted to the respective requirements of corresponding compounds.
- the present invention further enables a particularly effective utilization of the waste heat generated in a steam cracking process. This can first for
- the vaporized portion is then subjected to the steam cracking process.
- Further waste heat may, for example, also be used to heat the further stream of crude oil, which is then fed to the distillation column for atmospheric distillation.
- the quench cooler can be integrated into a corresponding heat recovery circuit, for example, by steam generated there is used to heat the crude oil stream.
- Crude oil is, as explained, advantageously initially at atmospheric pressure and then in vacuo, so that can be used for distillation on known methods of refinery technology and appropriate methods for the treatment of the distillation effluents can be used.
- the distillation effluents or streams derived therefrom may also be at least partially subjected to the steam cracking process.
- diverted streams can each be derived by branching off a partial stream, combining with other streams, chemical or physical
- Reacting at least some components in corresponding streams, heating, cooling, evaporation, condensation, etc. are formed.
- the recycle streams may be, in particular, atmospheric hydro (ATO) treated by hydrotreatment and / or hydrocracking, and vacuum gas oil treated by hydrotreatment and / or hydrocracking (Vacuum Gasoil, VGO), ie distillation residues from the
- Suitable recycling streams are also unsaturated hydrocarbons having two to four carbon atoms and / or hydrocarbons having five to eight carbon atoms in question. Naphtha can also be used again in corresponding steam cracking processes. In the separation by distillation downstream separation stages, which
- Vacuum distillation resulting and not further usable vacuum residue and / or the methane formed can be fired to produce energy.
- a plant for the production of crude oil products which is adapted to form a gaseous stream from a first stream of crude oil and to subject the gaseous stream at least in part a vapor cracking process, is also Subject of the present invention.
- the plant is arranged such that in the steam cracking process a split gas stream is generated which is used to form a separation insert contained in the quench effluent
- means are provided which are set up to separate at least part of the quench waste stream together with a second crude oil stream to obtain distillate effluents by distillation.
- Such a system has all the means that enable it to carry out a method according to the invention.
- means are furthermore provided which are set up to at least partially subject the distillation effluents or streams derived therefrom formed in this distillation column to the steam cracking process.
- Figure 1 shows a plant for the production of crude oil products according to a
- Embodiment of the invention in partial view.
- Figure 2 shows a plant for the production of crude oil products according to a
- Plant components simultaneously correspond to steps of a process.
- FIG. 1 is a plant for the production of crude oil products according to a
- Embodiment of the invention shown schematically in a partial view and designated 100 in total.
- the plant 100 supplied crude oil a is divided into two crude oil streams b and c.
- the crude oil stream b is preheated in a convection zone of one or more cracking furnaces 1 and transferred to an evaporation tank 2.
- Vaporization tank 2 vaporizing fraction of the crude oil stream b is passed as stream d after mixing with steam through the radiation zone of the cracking furnace or 1, wherein a cleavage gas e is obtained.
- the cracked gas e is cooled in a quench cooler 3 and then quenched in a quench device 4 with a portion of the crude oil stream b remaining liquid in the evaporation tank 2, here illustrated with stream f.
- a separating insert formed from the quenching stream g (without a separate name) is transferred to a distillation column 5 for fractional atmospheric distillation, into which the crude oil stream c is also fed.
- the distillation column 5 is operated in a conventional manner, so that in this
- an atmospheric residue h and an atmospheric gas oil i can be obtained.
- a stream k is withdrawn containing light products from the cracking furnace (s) 1 and the crude oil stream c.
- a water scrubber 6 By mixing water (not shown) in a water scrubber 6, a water-naphtha mixture is separated from the stream k and transferred as stream I into a decanter 7. In this a water flow m and a naphtha flow n is obtained.
- the system 100 is illustrated in an expanded view, ie as an expanded section of an overall system 100, and designated as a whole by 200.
- a correspondingly processed current s can in the
- Steam splitting method can be returned. From a stream u, which contains substantially hydrocarbons having five to eight carbon atoms, aromatics can be separated in an aromatic extraction unit 12 and carried out as stream v from the plant. A remaining portion can be used as power w the
- stream o which predominantly has hydrocarbons having one to four carbon atoms
- stream o which predominantly has hydrocarbons having one to four carbon atoms
- product streams indicated here overall with x for example ethylene, propylene and butadiene
- a methane stream y can be carried out from the plant and / or used for heating.
- Hydrocarbons not recovered as product streams x can be recycled as stream z into the steam cracking process.
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)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102014006327.5A DE102014006327A1 (de) | 2014-04-30 | 2014-04-30 | Verfahren und Anlage zur Gewinnung von Rohölprodukten |
EP14003150 | 2014-09-11 | ||
PCT/EP2015/059250 WO2015165921A1 (de) | 2014-04-30 | 2015-04-28 | Verfahren und anlage zur gewinnung von rohölprodukten |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3137578A1 true EP3137578A1 (de) | 2017-03-08 |
EP3137578B1 EP3137578B1 (de) | 2018-06-20 |
Family
ID=53059070
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP15721173.1A Active EP3137578B1 (de) | 2014-04-30 | 2015-04-28 | Verfahren zur gewinnung von rohölprodukten |
Country Status (11)
Country | Link |
---|---|
US (1) | US10000711B2 (de) |
EP (1) | EP3137578B1 (de) |
JP (1) | JP2017516893A (de) |
KR (1) | KR20160146766A (de) |
CN (1) | CN106232779B (de) |
AU (1) | AU2015254695A1 (de) |
BR (1) | BR112016025290A2 (de) |
HU (1) | HUE039134T2 (de) |
PH (1) | PH12016501940A1 (de) |
RU (1) | RU2016142702A (de) |
WO (1) | WO2015165921A1 (de) |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7374664B2 (en) * | 2005-09-02 | 2008-05-20 | Equistar Chemicals, Lp | Olefin production utilizing whole crude oil feedstock |
US7550642B2 (en) * | 2006-10-20 | 2009-06-23 | Equistar Chemicals, Lp | Olefin production utilizing whole crude oil/condensate feedstock with enhanced distillate production |
US8118996B2 (en) | 2007-03-09 | 2012-02-21 | Exxonmobil Chemical Patents Inc. | Apparatus and process for cracking hydrocarbonaceous feed utilizing a pre-quenching oil containing crackable components |
US20090050523A1 (en) * | 2007-08-20 | 2009-02-26 | Halsey Richard B | Olefin production utilizing whole crude oil/condensate feedstock and selective hydrocracking |
US8105479B2 (en) | 2009-06-18 | 2012-01-31 | Exxonmobil Chemical Patents Inc. | Process and apparatus for upgrading steam cracker tar-containing effluent using steam |
-
2015
- 2015-04-28 WO PCT/EP2015/059250 patent/WO2015165921A1/de active Application Filing
- 2015-04-28 EP EP15721173.1A patent/EP3137578B1/de active Active
- 2015-04-28 BR BR112016025290A patent/BR112016025290A2/pt not_active IP Right Cessation
- 2015-04-28 KR KR1020167030315A patent/KR20160146766A/ko unknown
- 2015-04-28 RU RU2016142702A patent/RU2016142702A/ru not_active Application Discontinuation
- 2015-04-28 US US15/307,531 patent/US10000711B2/en active Active
- 2015-04-28 HU HUE15721173A patent/HUE039134T2/hu unknown
- 2015-04-28 CN CN201580021667.2A patent/CN106232779B/zh active Active
- 2015-04-28 AU AU2015254695A patent/AU2015254695A1/en not_active Abandoned
- 2015-04-28 JP JP2016565499A patent/JP2017516893A/ja not_active Withdrawn
-
2016
- 2016-09-30 PH PH12016501940A patent/PH12016501940A1/en unknown
Also Published As
Publication number | Publication date |
---|---|
HUE039134T2 (hu) | 2018-12-28 |
US10000711B2 (en) | 2018-06-19 |
RU2016142702A (ru) | 2018-05-30 |
KR20160146766A (ko) | 2016-12-21 |
CN106232779B (zh) | 2018-09-21 |
CN106232779A (zh) | 2016-12-14 |
EP3137578B1 (de) | 2018-06-20 |
US20170058215A1 (en) | 2017-03-02 |
BR112016025290A2 (pt) | 2017-08-15 |
AU2015254695A1 (en) | 2016-10-20 |
JP2017516893A (ja) | 2017-06-22 |
WO2015165921A1 (de) | 2015-11-05 |
RU2016142702A3 (de) | 2018-08-29 |
PH12016501940A1 (en) | 2017-01-09 |
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