WO2015089593A1 - Processo de produção de hidrocarbonetos insaturados leves - Google Patents
Processo de produção de hidrocarbonetos insaturados leves Download PDFInfo
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- WO2015089593A1 WO2015089593A1 PCT/BR2013/000569 BR2013000569W WO2015089593A1 WO 2015089593 A1 WO2015089593 A1 WO 2015089593A1 BR 2013000569 W BR2013000569 W BR 2013000569W WO 2015089593 A1 WO2015089593 A1 WO 2015089593A1
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- WIPO (PCT)
- Prior art keywords
- stream
- unsaturated hydrocarbons
- ethanol
- light
- effluent
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
- C07C1/24—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by elimination of water
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- 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
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/40—Thermal non-catalytic treatment
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/82—Phosphates
- C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
- C07C2529/85—Silicoaluminophosphates (SAPO compounds)
-
- 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
- C10G2400/22—Higher olefins
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
Definitions
- the present invention is a combined process for the production of light unsaturated hydrocarbons which allows the gradual implantation of a process based on renewable raw material using the installed capacity of petrochemical plants.
- the combined process also allows for the gradual replacement of petrochemical feedstock by replacing cracking furnaces with ethanol conversion units of renewable origin mostly in light unsaturated hydrocarbons while maintaining the entire conditioning and purification area.
- the end products of the combined process such as ethylene, propylene and C4's, have a modern carbon content that proves the lowest CO2 emissions per kilogram of product produced compared to those produced by conventional petrochemical process.
- Light unsaturated hydrocarbons such as ethylene and propylene
- ethylene and propylene are important chemical platforms for the production of a wide variety of products. Most of the production of these hydrocarbons is for polymer generation. Vinyl chloride, ethylene oxide, propylene oxide and acrylonitrile are examples of other light unsaturated hydrocarbon derivatives of major importance in the chemical industry.
- ethylene is obtained from petrochemical processes, mainly by steam cracking of petrochemical naphtha or ethane.
- Propylene is mainly obtained as a co-product of steam cracking ethylene production and gasoline production from oil refining.
- Interest in propylene production as the main product has been increasing as demand for this olefin has outpaced its supply from ethylene production and oil refining.
- bioethanol refers to ethanol produced from the fermentation of at least one organic substrate from renewable natural raw materials, such as, but not limited to, sugarcane, corn, sorghum, wheat, lignocellulosic materials, among others. Throughout the text, bioethanol will be treated as ethanol only.
- the processes for obtaining unsaturated hydrocarbons from ethanol dehydration may generate: (i) mostly ethylene with small quantities of other by-products of side reactions or;
- composition of the unsaturated hydrocarbon mixture may be further adjusted by additional serial processes: butene content may be maximized by ethylene dimerization and / or propene content may be maximized by ethane metathesis and butenes.
- the production of light unsaturated hydrocarbons from ethanol dehydration in regions such as Brazil has a number of advantages, especially the competitiveness of ethanol obtained from sugar cane associated with the low carbon footprint of the product resulting from the process ( kilograms of CO2 that are emitted into the atmosphere during the manufacture of one kilogram of product).
- the mature sugar and alcohol industry in the country provides high production of high quality anhydrous (anhydrous and hydrated) fuel ethanol, within the specifications regulated by ANP (National Agency of Petroleum, Natural Gas and Biofuels), which can be advantageously employed as a raw material for olefin production.
- ANP National Agency of Petroleum, Natural Gas and Biofuels
- the present invention presents an alternative for naphtha cracking units by replacing at least one pyrolysis furnace with at least one ethanol to olefin conversion reactor.
- the conversion routes from ethanol to light unsaturated hydrocarbons (C2, C3 and C4) have stages of separation and purification similar to those in naphtha cracking olefin plants as shown in Figure 1.
- the integration between the alcohol to light unsaturated hydrocarbon conversion route and an existing cracking unit alternative to increase the economic return of the route.
- US20110112345 discloses the integration between a preferred oxygen-to-olefin conversion system comprising methanol or dimethyl ether and a light paraffin cracking system. In order to avoid overload in the separation area and purification, cracking conditions are adjusted to ensure low severity and high ethylene selectivity.
- WO2013004544 has introduced the addition of one or more ethanol reactors to ethylene to a steam cracking plant to increase ethylene production.
- the present invention relates to reducing naphtha feed in an existing plant and replacing the petrochemical feedstock with a renewable feedstock by integrating one or more ethanol to light hydrocarbon conversion reactors. with no or slight change in the shared separation and purification areas.
- the present invention has the effect of reducing greenhouse gas emissions in the production of olefins with the lowest possible investment by leveraging existing assets.
- the present invention further permits the gradual replacement of petrochemical feedstock by renewable feedstock, increased profitability of the existing cracking plant, flexibility of feedstock and product composition according to the market, and the elimination of bottlenecks of the existing light cracking unsaturated hydrocarbon production plant.
- Figure 1 shows a comparative generic scheme of the conversion processes of ethanol to light unsaturated hydrocarbons, including some co-products, and naphtha cracking.
- Figure 2 presents a schematic of the integration between ethanol conversion processes to light unsaturated hydrocarbons and naphtha cracking with sharing of the olefin separation and purification system.
- Figure 3 shows a schematic example of the separation and purification zones of a shared petrochemical naphtha thermal cracking plant in the integration of Figure 2.
- Figure 4 presents a schematic of the integration between ethanol conversion processes to light unsaturated hydrocarbons and naphtha cracking with separation and purification, caustic washing, drying and compression system sharing.
- Figure 5 presents a schematic of the integration between ethanol conversion processes to light unsaturated hydrocarbons and naphtha cracking with the separation and purification system sharing, caustic washing, drying, compression and water quenching.
- the present invention deals with the integration between the ethanol to light unsaturated hydrocarbon conversion route and an existing naphtha cracking unit by replacing pyrolysis furnaces with ethanol to light unsaturated hydrocarbon conversion reactors.
- the integration allows the gradual replacement of cracking furnaces with ethanol conversion reactors to light unsaturated hydrocarbons and the generation of partially renewable products.
- the fossil hydrocarbon stream used as a feedstock in the production of thermal cracking olefins comprises hydrocarbons in the range of C2 to C40, preferably in the range of C2 to C30, more preferably in the range of C2 to C20 and most preferably in the range from C5 to C12 with naphtha boiling range in the range of about 36 ° C to about 195 ° C.
- Ethanol used in the present invention as a feedstock for the process of converting ethanol to light unsaturated hydrocarbons may be produced from, but not limited to, fermentation of at least one organic substrate from renewable natural raw materials, for example, but not limited to sugar cane, corn, sorghum, wheat, lignocellulosic materials among others, being preferably obtained from sugar cane. Mixtures of ethanol from different sources may also be used in the present invention.
- the ethanol used to feed the process of converting ethanol to light unsaturated hydrocarbons may be hydrous ethanol or anhydrous ethanol, with preferably hydrous fuel ethanol being used.
- the ethanol may be subjected to a purification step prior to the conversion step to light unsaturated hydrocarbons.
- the method employed to remove impurities from the ethanol filler may be a porous membrane or adsorption bed system or a system composed of ion exchange resin vessels or an assembly employing two or more of the above systems.
- the system is composed of vessels with ion exchange resins.
- the integration points between the ethanol to light unsaturated hydrocarbon conversion route and the existing naphtha cracking unit are defined according to the following:
- the present invention relates to a partially renewable light unsaturated hydrocarbon production process, wherein at least one pyrolysis furnace of a light hydrocarbon unsaturated hydrocarbon production unit is replaced by at least one reactor for converting ethanol to light unsaturated hydrocarbons in which:
- ethanol is contacted with an acid catalyst in at least one reactor under conditions suitable to form a reaction effluent stream comprising water, ethylene, propene and four carbon unsaturated hydrocarbons in addition to other by-products of side reactions;
- the stream generated in (a) is fed into a direct contact cooling unit under appropriate conditions to form a top stream containing most of the light unsaturated hydrocarbons present in the effluent stream of step (a) and a bottom stream containing most of the water present in the effluent stream of step (a);
- naphtha is contacted with steam in a pyrolysis oven under conditions suitable to form a cracking effluent stream comprising light unsaturated hydrocarbons, fuel oil, diesel and gasoline;
- the effluent generated in the cracking reaction (d) is separated into a light hydrocarbon stream containing most of the light unsaturated hydrocarbons present in the effluent from step (d), and at least one heavy hydrocarbon stream;
- step (f) the stream of light unsaturated hydrocarbons from step (e) is fed into a direct contact cooling unit under appropriate conditions to form a top stream containing most of the light unsaturated hydrocarbons present in the reaction effluent (and ), and a background stream, containing the condensed compounds and most of the water present in the reaction effluent (d);
- the present invention relates to
- step (c) a process of producing partially renewable light unsaturated hydrocarbons as described above, wherein the top stream generated in step (b) is contacted with a basic solution in a caustic washing unit under conditions suitable for removing at least part of the CO 2 from the stream before being compressed in step (c).
- the present invention relates to a process of producing light unsaturated hydrocarbons. partially renewable as described above, wherein the top stream generated in step (f) is contacted with a basic solution in a caustic wash unit under conditions suitable to remove at least part of the CO2 from the stream before being compressed in step (g). ).
- the present invention relates to a partially renewable light unsaturated hydrocarbon production process as described above, wherein the combined stream in step (h) is contacted with a basic solution in a caustic washing unit under conditions suitable for removing at least part of the CO2 from the stream before being sent to the unsaturated hydrocarbon separation and purification steps C2, C3 and C4 of the existing cracking unit.
- the present invention relates to a partially renewable light unsaturated hydrocarbon production process wherein at least one pyrolysis furnace of a hydrocarbon light unsaturated hydrocarbon production unit is replaced by at least an ethanol unsaturated hydrocarbon conversion reactor in which:
- ethanol is contacted with an acid catalyst in at least one reactor under conditions suitable to form a reaction effluent stream comprising water, ethylene, propene and four carbon unsaturated hydrocarbons in addition to other by-products of side reactions;
- naphtha is contacted with steam in a pyrolysis furnace under suitable conditions to form an effluent stream from the cracking comprising light unsaturated hydrocarbons, fuel oil, diesel and gasoline;
- the effluent generated in the cracking reaction (c) is separated into a light unsaturated hydrocarbon stream containing most of the light unsaturated hydrocarbons present in the effluent from step (c), and at least one heavy hydrocarbon stream;
- step (e) the light unsaturated hydrocarbon rich stream from step (d) is fed into a direct contact cooling unit under conditions suitable to form a top stream containing most light unsaturated hydrocarbons present in the reaction effluent (d). ), and a background stream, containing the condensed compounds and most of the water present in the reaction effluent (c);
- streams (b) and (e) are combined and contacted with a basic solution in a caustic washing unit under conditions suitable to remove at least part of the CO2 from the stream and sent to the unsaturated hydrocarbon separation and purification steps.
- the present invention relates to a partially renewable light unsaturated hydrocarbon production process wherein at least one pyrolysis furnace of a hydrocarbon light unsaturated hydrocarbon production unit is replaced by at least one reactor for converting ethanol to light unsaturated hydrocarbons in which:
- ethanol is contacted with an acid catalyst in at least one reactor under conditions suitable to form a reaction effluent stream comprising water, ethylene, propene and four carbon unsaturated hydrocarbons in addition to other by-products of side reactions;
- the integration between the ethanol to light unsaturated hydrocarbon conversion route and the existing naphtha cracking unit is done by sharing the olefin separation and purification systems, as can be seen in Figure 2. This This form is preferred when there is a pressure difference in the supply of compressors of the two processes.
- Naphtha (101) is heated, vaporized and diluted with low pressure steam (102) for the cracking reaction.
- the vapor / hydrocarbon ratio at the entrance to the pyrolysis furnaces depends on the composition of the raw material and usually ranges from 0.3 to 1.
- the reaction occurs by temperature (about 850 ° C) and naphtha is transformed into light olefins, fuel oil, diesel and gasoline (111). Part of the heat given to the furnaces for the reaction of cracking is recovered for heating and vaporization of naphtha and for the generation of steam for consumption in the plant.
- the furnace output current cooling system is optionally composed of: indirect contact cooling on heat exchangers for the generation of high pressure steam (120); then by direct contact with oil (130), where fuel oil (132), diesel (133), heavy fraction of gasoline (134) and residual coke (135) are separated as by-products; and finally, a condensation stage by direct contact with water or air (140), where light fraction of gasoline (142) and aqueous effluent (143) are generated as byproducts.
- Gas from the quench tower (141) is compressed through multistage compressors (150) at a pressure suitable for cryogenic distillation, where a stream of condensate (152) is generated as a byproduct.
- the pressure of the condensate stream is preferably between 1500 and 3000 kPa (15 and 30 bar) and even more preferably between 1800 and 2600 kPa (18 and 26 bar).
- acidic gases H2S, CO2, COS, CS2
- a basic solution (162) and process water (161) in a caustic wash unit (160) where aqueous effluent ( 164) is generated as a byproduct.
- some compression stages may occur after the caustic washing step.
- Residual water is removed by contacting desiccant adsorption beds (170) prior to the separation and purification step by fractionation.
- ethanol (301) is heated, vaporized and overheated in multiple ovens (310) by integrating with the dehydration reaction output stream.
- the reaction system is optionally composed of multiple reactors (320) and multiple forams (310).
- the process may be conducted in isothermal or adiabatic modes.
- an amount of steam or water or other high calorific inert material 302 may optionally be added to reduce the temperature drop in the reactor.
- the inert material is water, its total mass concentration at the reactor inlet may range from 5 to 80%, preferably from 25 to 70% and more preferably from 45 to 65%.
- the catalyst employed in the ethanol conversion reaction to light unsaturated hydrocarbons may be any acid catalyst capable of converting the ethanol mainly to a composition comprising C2, C3 and C4 unsaturated hydrocarbons.
- C4 unsaturated hydrocarbons may comprise 1,3-butadiene in addition to
- 2-butenes 2-butenes being a mixture of the e and trans isomers.
- Examples may include zeolites, silica alumina, silicoaluminium phosphates, aluminosilicates in addition to other metal oxides and variations of the catalysts modified with metal and / or phosphorus, as well as the mixture of two or more thereof.
- the products obtained (321) are similar to those produced by naphtha cracking: ethylene, propene, four-carbon hydrocarbon mixture, aromatic and others (including heavy hydrocarbons containing 5 or more carbon atoms).
- Reaction products from the conversion of ethanol to unsaturated hydrocarbons must have in their composition (on a dry basis) 15 to 60% mol of ethylene, 5 to 40% mol of propylene and 3 to 35% mol of C4.
- C4 is a mixture of 1 and 2-butenes and optionally 1,3-butadiene.
- the reaction of converting ethanol to unsaturated hydrocarbons occurs at temperatures between 400 and 800 ° C, preferably between 400 and 600 ° C and pressures between 100 and 2000 kPa (1 and 20 bar).
- the reaction gas (321) is cooled by integrations with the inlet stream (330) and fed to a water quench tower (340) to condense most of the water present in the stream, where hydrocarbons for flaring (342) and aqueous effluent (343) are generated as by-products.
- Gas from the quench tower (341) is compressed into multi-stage compressors (350) at a pressure suitable to be fed to the purification system already present in the naphtha cracking plant, where a stream of condensate (352) ) is generated as a by-product.
- the pressure of the condensate stream is preferably between 1500 and 3000 kPa (15 and 30 bar) and even more preferably between 1800 and 2600 kPa (18 and 26 bar).
- a basic solution (362) and process water (361) in a caustic wash unit (360) the CO2 and organic acids generated in the reaction, where aqueous effluent (364) is generated. as a by-product.
- some compression stages may occur after the caustic washing step.
- Residual water is removed from the caustic wash gas, for example, by contact with adsorption beds with desiccant agents (370).
- the gases from drying the ethanol to light unsaturated hydrocarbon conversion route (371) and cracking (171) are combined and fed into an olefin separation and purification system (200).
- olefin separation and purification system There are several possible configurations for the arrangement of distillation columns for olefin separation and purification, all of which are compatible with integration.
- the system shown in Figure 3 uses the dispropaning column at the beginning of the separation and purification area.
- the bottom products of the de-companing column are fed into a debutanizing column, in which a product stream comprising a mixture of C4's and a rich stream of C5 and C6 are separated, the latter can be specified as pyrolysis gasoline.
- the distillate stream from the despraniser passes through a hydrogenation reactor (acetylene hydrogenation) and is fed into the cold area along with the despranizer top gases. In the cold area, hydrogen and part of the methane are separated and sent for burning, while the remainder of the methane is separated in the demethanizing column.
- acetylene hydrogenation acetylene hydrogenation
- the bottom of the demethanizer is fed into the deethanizer.
- the top product of the de-sanitizer is fed to the ethylene fractionator column from which the ethylene product is obtained, and the bottom product of the de-sanitizer is fed to the propene fractionator column from which the propene product is obtained.
- integration is accomplished by sharing the olefin separation and purification, caustic washing, drying and compression system as shown in Figure 4. This configuration is preferred when there is a neck in the quench tower due to excess water at the exit from the process of converting ethanol to unsaturated hydrocarbons in relation to cracking.
- integration is accomplished by sharing the olefin separation and purification system, caustic washing, drying, compression and water quenching, as shown in Figure 5.
- This configuration uses as few equipment as possible and Because it requires the least investment, it is preferred when none of the equipment is the bottleneck.
- a typical ethanol-to-olefin conversion plant was evaluated in terms of the investment required for its construction including units required for the storage of raw materials and products, as well as utility supply and wastewater treatment units.
- the investment distribution is shown in Table.
- Table 1 Investment distribution for the construction of a typical ethanol to olefin conversion plant
- Table 2 presents a typical product composition for naphtha cracking and ethanol to unsaturated hydrocarbon conversion compositions obtained experimentally with three different catalysts. From these compositions, the mass contents of renewable ethylene and propylene produced from the substitution of 10% of the petrochemical feedstock (naphtha) feedstock for renewable feedstock (ethanol) for three conversion reactor effluent compositions were calculated. of ethanol corresponding to the three catalysts considering a naphtha cracking plant with a production capacity of 870 kta of light olefins (ethylene and propene). Table 2: Typical naphtha cracking furnace outlet compositions and ethanol to unsaturated hydrocarbon conversion reactor outlet compositions using three different catalysts.
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- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
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Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP13899431.4A EP3085754B1 (en) | 2013-12-17 | 2013-12-17 | Method for producing light unsaturated hydrocarbons |
PCT/BR2013/000569 WO2015089593A1 (pt) | 2013-12-17 | 2013-12-17 | Processo de produção de hidrocarbonetos insaturados leves |
BR112016013092-8A BR112016013092B1 (pt) | 2013-12-17 | 2013-12-17 | processo de produção de hidrocarbonetos insaturados leves |
US15/105,398 US9751816B2 (en) | 2013-12-17 | 2013-12-17 | Method for producing light unsaturated hydrocarbons |
Applications Claiming Priority (1)
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PCT/BR2013/000569 WO2015089593A1 (pt) | 2013-12-17 | 2013-12-17 | Processo de produção de hidrocarbonetos insaturados leves |
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WO2015089593A1 true WO2015089593A1 (pt) | 2015-06-25 |
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PCT/BR2013/000569 WO2015089593A1 (pt) | 2013-12-17 | 2013-12-17 | Processo de produção de hidrocarbonetos insaturados leves |
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US (1) | US9751816B2 (pt) |
EP (1) | EP3085754B1 (pt) |
BR (1) | BR112016013092B1 (pt) |
WO (1) | WO2015089593A1 (pt) |
Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20050038304A1 (en) | 2003-08-15 | 2005-02-17 | Van Egmond Cor F. | Integrating a methanol to olefin reaction system with a steam cracking system |
US20100206771A1 (en) | 2007-09-21 | 2010-08-19 | Lurgi Gmbh | Process and plant for producing hydrocarbons |
US20110112345A1 (en) | 2009-11-10 | 2011-05-12 | Leslie Andrew Chewter | Process for the preparation of a lower olefin product |
US20110112314A1 (en) | 2009-11-10 | 2011-05-12 | Leslie Andrew Chewter | Process for producing olefins |
WO2012021345A2 (en) * | 2010-08-10 | 2012-02-16 | Uop Llc | Integration of a methanol-to-olefin reaction system with a hydrocarbon pyrolysis system |
BRPI0717043A2 (pt) * | 2006-09-28 | 2013-01-01 | Uop Llc | processo para produzir olefinas leves a partir de uma carga de alimentação que contém oxigenados, e, sistema para converter oxigenados em olefinas leves |
WO2013004544A1 (en) | 2011-07-07 | 2013-01-10 | Ineos Europe Ag | Process and apparatus for producing olefins with heat transfer from steam cracking to alcohol dehydration process. |
-
2013
- 2013-12-17 EP EP13899431.4A patent/EP3085754B1/en active Active
- 2013-12-17 WO PCT/BR2013/000569 patent/WO2015089593A1/pt active Application Filing
- 2013-12-17 US US15/105,398 patent/US9751816B2/en active Active
- 2013-12-17 BR BR112016013092-8A patent/BR112016013092B1/pt active IP Right Grant
Patent Citations (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20050038304A1 (en) | 2003-08-15 | 2005-02-17 | Van Egmond Cor F. | Integrating a methanol to olefin reaction system with a steam cracking system |
BRPI0717043A2 (pt) * | 2006-09-28 | 2013-01-01 | Uop Llc | processo para produzir olefinas leves a partir de uma carga de alimentação que contém oxigenados, e, sistema para converter oxigenados em olefinas leves |
US20100206771A1 (en) | 2007-09-21 | 2010-08-19 | Lurgi Gmbh | Process and plant for producing hydrocarbons |
US20110112345A1 (en) | 2009-11-10 | 2011-05-12 | Leslie Andrew Chewter | Process for the preparation of a lower olefin product |
US20110112314A1 (en) | 2009-11-10 | 2011-05-12 | Leslie Andrew Chewter | Process for producing olefins |
WO2012021345A2 (en) * | 2010-08-10 | 2012-02-16 | Uop Llc | Integration of a methanol-to-olefin reaction system with a hydrocarbon pyrolysis system |
WO2013004544A1 (en) | 2011-07-07 | 2013-01-10 | Ineos Europe Ag | Process and apparatus for producing olefins with heat transfer from steam cracking to alcohol dehydration process. |
Non-Patent Citations (1)
Title |
---|
CRELL'S CHEM. ANN., vol. 2, pages 195 - 205,310-316,430-440 |
Also Published As
Publication number | Publication date |
---|---|
EP3085754A1 (en) | 2016-10-26 |
EP3085754B1 (en) | 2019-10-23 |
US9751816B2 (en) | 2017-09-05 |
BR112016013092B1 (pt) | 2018-12-11 |
EP3085754A4 (en) | 2017-06-14 |
US20160318825A1 (en) | 2016-11-03 |
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