WO2016079112A1 - Recycle of process condensate impurities in tigas - Google Patents

Recycle of process condensate impurities in tigas Download PDF

Info

Publication number
WO2016079112A1
WO2016079112A1 PCT/EP2015/076809 EP2015076809W WO2016079112A1 WO 2016079112 A1 WO2016079112 A1 WO 2016079112A1 EP 2015076809 W EP2015076809 W EP 2015076809W WO 2016079112 A1 WO2016079112 A1 WO 2016079112A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
feed
recycle
recycle stream
process condensate
Prior art date
Application number
PCT/EP2015/076809
Other languages
French (fr)
Inventor
Arne Knudsen
Ian MENJON
Original Assignee
Haldor Topsøe A/S
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 Topsøe A/S filed Critical Haldor Topsøe A/S
Priority to CN201580062278.4A priority Critical patent/CN107109242A/en
Priority to AU2015348631A priority patent/AU2015348631A1/en
Priority to US15/518,279 priority patent/US20170253807A1/en
Priority to MX2017006161A priority patent/MX2017006161A/en
Priority to CA2968006A priority patent/CA2968006A1/en
Priority to BR112017008676A priority patent/BR112017008676A2/en
Priority to EA201791061A priority patent/EA201791061A1/en
Publication of WO2016079112A1 publication Critical patent/WO2016079112A1/en

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
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
    • 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
    • C10G2300/4081—Recycling aspects
    • 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
    • C10G2400/02—Gasoline

Definitions

  • the invention relates to an improved process and plant for the preparation of hydrocarbons useful as gasoline com- pounds from a feed comprising methanol.
  • Gasoline can be produced by conversion of raw methanol, pure methanol and/or dimethyl ether. In the process water is formed as a by-product. The water is separated (as pro- cess condensate) from the produced raw gasoline and recycle gas in a separator and send for water treatment as it com ⁇ prises a number of impurities.
  • a conversion step converting at least a feed stream thereby obtaining a conversion effluent comprising water, hydrocarbons, unreacted, partially reacted feed and/or in- erts ,
  • a separator separating the conversion effluent into at least a recycle stream, raw gasoline and a process con ⁇ densate stream comprising water
  • the conversion effluent may comprise various hydrocarbons such as raw gasoline, higher alcohols, aldehydes, ketones, ethers, olefins and/or aromatics.
  • any convertible substances in the process condensate can be re-entered into the con- version loop whereby the output of the process may be in ⁇ creased compared to setups where the process condensate is simply sent to water treatment.
  • the present plant and process reduce the need for wa- ter treatment as the convertible substances in the water is reintroduced into the conversion step instead of being re ⁇ moved in downstream treatment of the condensate.
  • the feed to the process is preferably a methanol rich stream which also may comprise any of the following Dime ⁇ thyl Ether (DME) , higher alcohols, ketones, aldehydes, raw methanol, other alcohols, ethers and/or H2/CO mixtures.
  • DME Dime ⁇ thyl Ether
  • the process condensate from the conversion process may com- prise oxygenates of different types including alcohols, ke ⁇ tones, esters and/or aldehydes.
  • the oxygenates can be separated from the remaining process condensate which mainly consists of water.
  • the separation of the oxygenates can for example be performed by distilla ⁇ tion or stripping.
  • the stream comprising the separated oxy- genates is referred to as the recovered oxygenate stream.
  • At least part of the process condensate added to the feed stream and/or the recycle stream and/or the mixed feed-recycle stream is a recovered oxygenate stream.
  • the at least part of the process condensate stream to the feed stream, recycle stream and/or mixed feed-recycle stream may be the recovered oxygenate stream.
  • composition of the process condensate and the recovered oxygenate stream may depend on the conversion process, feed etc .
  • the conversion step is a methanol to gaso ⁇ line (MTG) process in which the produced hydrocarbons com ⁇ prises a mixture of various hydrocarbons boiling in the gasoline range, such as from C2 and higher e.g. up to C13, preferably C5+ .
  • MTG gaso ⁇ line
  • the conversion of oxygenates in the feed stream is carried out in a converter in the presence of a catalyst being active known in the art in the reaction of oxygenates to higher hydrocarbons, preferably C5+ hydrocarbons.
  • more than one conversion reactor is used. In these setups the multiple converters may be arranged in parallel allowing recovery of one or more converter while one or more reactors are still in use.
  • the recovered oxygenate stream may be added to the feed stream and/or recycle and/or the stream of mixed
  • the process provides an increased gasoline production because the unconverted oxygenates are recovered and recirculated back to the synthesis process instead of lost in the pro- cess condensate sent to water treatment.
  • the conversion of the recovered oxygenates reduce the need for treatment of the waste water as the oxygenates are utilized instead of being disposed of as part of the process conden ⁇ sate as known from existing processes.
  • Fig. 1 illustrates a process and plant 1 where feed 2 is mixed with recycle gas 3 and recovered oxygenate stream 4 is mixed into the feed/recycle gas stream at a mixing point 5.
  • the recovered oxygenate stream is mixed into the recycle stream upstream the feed mix point 5 at a sec ⁇ ond mixing point 7.
  • the mixing is preferable carried out by quenching the recovered oxygenate stream into the gas stream by means of a spray nozzle.
  • a static mixer can be used or the liquid and the gas can be mixed upstream of a heat exchanger.
  • Another alternative is to add the recovered oxygenate stream to the feed stream before the stream is evaporated or after the feed stream is evaporated as indicated by dot ⁇ ted lines 8 and 9.
  • Another alternative is to spray/mix the liquid off-stream into the gas going to the reactor as indicated by dotted line 10.
  • the ketone, aldehydes and/or alcohols in the recovered oxy- genate stream is together with the feed methanol converted to gasoline in the reactor 11.
  • the effluent 12 is
  • the recovered oxygenate stream 4 from the separation comprises ketones, aldehydes and/or alcohols.

Abstract

The present application relates to a plant and a hydrocarbon production process comprising the steps of (i) in a conversion step converting at least a feed stream thereby obtaining a conversion effluent stream comprising water, hydrocarbons such as raw gasoline, unreacted and/or partially reacted feed and/or inerts, (ii) In a separator separating the conversion effluent stream into at least a raw gasoline stream, a recycle stream and a process condensate stream comprising water and oxygenates, (iii) mixing the feed stream and the recycle stream upstream the conversion step, and (iv) adding at least part of the process condensate stream to the feed stream and/or the recycle stream and/or the mixed feed-recycle stream from step (iii).

Description

Recycle of process condensate impurities in TIGAS
The invention relates to an improved process and plant for the preparation of hydrocarbons useful as gasoline com- pounds from a feed comprising methanol.
Gasoline can be produced by conversion of raw methanol, pure methanol and/or dimethyl ether. In the process water is formed as a by-product. The water is separated (as pro- cess condensate) from the produced raw gasoline and recycle gas in a separator and send for water treatment as it com¬ prises a number of impurities.
In a first aspect of the present invention is provided a process which provides an optimized output from the gaso¬ line conversion.
In a second aspect of the present invention is provided a process which reduces the need for water treatment.
These and other advantages are achieved by a hydrocarbon production process comprising the steps of
In a conversion step converting at least a feed stream thereby obtaining a conversion effluent comprising water, hydrocarbons, unreacted, partially reacted feed and/or in- erts ,
In a separator separating the conversion effluent into at least a recycle stream, raw gasoline and a process con¬ densate stream comprising water,
- At one or more points mixing the feed stream and at least part of the recycle upstream the conversion step, and adding at least part of the process condensate stream to the feed stream, recycle stream and/or mixed feed- recycle stream. Various embodiments of the invention are disclosed and dis¬ cussed in the following. These embodiments can either be employed each alone or in combination.
The conversion effluent may comprise various hydrocarbons such as raw gasoline, higher alcohols, aldehydes, ketones, ethers, olefins and/or aromatics.
By the present process and plant any convertible substances in the process condensate can be re-entered into the con- version loop whereby the output of the process may be in¬ creased compared to setups where the process condensate is simply sent to water treatment.
Also the present plant and process reduce the need for wa- ter treatment as the convertible substances in the water is reintroduced into the conversion step instead of being re¬ moved in downstream treatment of the condensate.
The feed to the process is preferably a methanol rich stream which also may comprise any of the following Dime¬ thyl Ether (DME) , higher alcohols, ketones, aldehydes, raw methanol, other alcohols, ethers and/or H2/CO mixtures.
The process condensate from the conversion process may com- prise oxygenates of different types including alcohols, ke¬ tones, esters and/or aldehydes. The oxygenates can be separated from the remaining process condensate which mainly consists of water. The separation of the oxygenates can for example be performed by distilla¬ tion or stripping. The stream comprising the separated oxy- genates is referred to as the recovered oxygenate stream.
Preferably at least part of the process condensate added to the feed stream and/or the recycle stream and/or the mixed feed-recycle stream is a recovered oxygenate stream. I.e. the at least part of the process condensate stream to the feed stream, recycle stream and/or mixed feed-recycle stream may be the recovered oxygenate stream.
The composition of the process condensate and the recovered oxygenate stream may depend on the conversion process, feed etc .
Some exemplary compositions and ranges for pressures and temperatures are given below. The values are based on a feed of raw methanol and a conversion process based on a ZSM-5 catalyst at T = 250 - 475°C and P = 1 - 50 bar.
Process condensate :
Temperature = 75 - 105 °C, preferably 90°C
Pressure = 2 - 8 barg, preferably 5.4 barg
Composition :
Compound wtppm
Ethanol 50 wtppm
Methanol 10000 wtppm
Acetone 1100 wtppm
1-Propanol 200 wtppm Acetaldehyde 150 wtppm
Methyl Ethyl Ketone 250 wtppm
Water balance
Recovered oxygenate stream:
Temperature = 75 - 105 °C, preferably 90°C
Pressure = 15 - 40 barg, preferably 28 barg
Composition
Compound wtppm
Ethanol 2800 wtppm
Methanol 555000 wtppm
Acetone 61100 wtppm
1-Propanol 11100 wtppm
Acetaldehyde 8330 wtppm
Methyl Ethyl Ketone 13880 wtppm
Water balance
In most setups the conversion step is a methanol to gaso¬ line (MTG) process in which the produced hydrocarbons com¬ prises a mixture of various hydrocarbons boiling in the gasoline range, such as from C2 and higher e.g. up to C13, preferably C5+ . Generally speaking in the conversion pro- cess the conversion of oxygenates in the feed stream is carried out in a converter in the presence of a catalyst being active known in the art in the reaction of oxygenates to higher hydrocarbons, preferably C5+ hydrocarbons. In various setups more than one conversion reactor is used. In these setups the multiple converters may be arranged in parallel allowing recovery of one or more converter while one or more reactors are still in use. The recovered oxygenate stream may be added to the feed stream and/or recycle and/or the stream of mixed
feed/recycle in order to enter the conversion step thereby improving the output of the system compared to the case where the oxygenates are removed from the system together with the water etc. in the process condensate. I.e. the process provides an increased gasoline production because the unconverted oxygenates are recovered and recirculated back to the synthesis process instead of lost in the pro- cess condensate sent to water treatment. Furthermore the conversion of the recovered oxygenates reduce the need for treatment of the waste water as the oxygenates are utilized instead of being disposed of as part of the process conden¬ sate as known from existing processes.
Fig. 1 illustrates a process and plant 1 where feed 2 is mixed with recycle gas 3 and recovered oxygenate stream 4 is mixed into the feed/recycle gas stream at a mixing point 5.
Alternatively the recovered oxygenate stream is mixed into the recycle stream upstream the feed mix point 5 at a sec¬ ond mixing point 7. The mixing is preferable carried out by quenching the recovered oxygenate stream into the gas stream by means of a spray nozzle. Alternatively a static mixer can be used or the liquid and the gas can be mixed upstream of a heat exchanger.
Another alternative is to add the recovered oxygenate stream to the feed stream before the stream is evaporated or after the feed stream is evaporated as indicated by dot¬ ted lines 8 and 9. Another alternative is to spray/mix the liquid off-stream into the gas going to the reactor as indicated by dotted line 10.
The ketone, aldehydes and/or alcohols in the recovered oxy- genate stream is together with the feed methanol converted to gasoline in the reactor 11. The effluent 12 is
cooled/condensed in a series of heat exchangers 13 and the three phases are separated in the separator 14. The gas is recycled 15/purged 16 and the condensate 17 is sent to a distillation 18 for separation. The recovered oxygenate stream 4 from the separation comprises ketones, aldehydes and/or alcohols.

Claims

1. A hydrocarbon production process comprising the steps of
(i)in a conversion step converting at least a feed stream thereby obtaining a conversion effluent stream comprising water, hydrocarbons such as raw gasoline, unreacted and/or partially reacted feed and/or inerts,
(ii) in a separator separating the conversion effluent stream into at least a raw gasoline stream, a recycle stream and a process condensate stream comprising wa¬ ter and oxygenates,
(iii) mixing the feed stream and the recycle stream upstream the conversion step, and
(iv) adding at least part of the process condensate stream to the feed stream and/or the recycle stream and/or the mixed feed-recycle stream from step (iii) .
2. A hydrocarbon production process according to claim 1 wherein the oxygenates are separated from the process condensate and added to the feed stream and/or the re¬ cycle stream and/or the mixed feed-recycle stream as a recovered oxygenate stream. 3. A hydrocarbon production process according to any one of the preceding claims wherein the produced hydrocarbons comprise a mixture of hydrocarbons in the C2 - C13 range, preferably comprising C5+. 4. A hydrocarbon production process according to any one of the preceding claims wherein the feed comprises methanol, raw methanol, other alcohols, ketones, alde¬ hydes, ethers and/or H2/CO mixtures.
A hydrocarbon production process according to any one of the preceding claims wherein the mixing of at least part of the process condensate comprising oxygenates into the feed stream, recycle stream and/or mixed feed-recycle stream is carried out by quenching the at least part of the process condensate into the feed stream and/or the recycle stream and/or the mixed feed-recycle stream by a spray nozzle.
A hydrocarbon production process according to any one of the preceding claims wherein the process condensate is added to a stream upstream a heat exchanger.
A plant comprising a converter, means for feeding a feed stream to the converter, a separator, means for returning at least part of a recycle stream from the separator to the converter, and means for mixing at least part of a process condensate from the separator into the means for feeding the feed stream and/or into the means for returning at least part of the recycle stream upstream the converter.
. A plant according to claim 7, comprising further means for separating oxygenates from the process condensate.
9. A plant according to claim 8 wherein the means for
separating oxygenates from the process condensate com- prises a distillation unit and/or a stripper unit.
10. Raw gasoline produced by the process according to any one of the claims 1 - 6 and/or a plant according to any one of the clams 7 - 9.
PCT/EP2015/076809 2014-11-17 2015-11-17 Recycle of process condensate impurities in tigas WO2016079112A1 (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
CN201580062278.4A CN107109242A (en) 2014-11-17 2015-11-17 The recycling of process condensate thing impurity in TIGAS
AU2015348631A AU2015348631A1 (en) 2014-11-17 2015-11-17 Recycle of process condensate impurities in tigas
US15/518,279 US20170253807A1 (en) 2014-11-17 2015-11-17 Recycle of process condensate impurities in tigas
MX2017006161A MX2017006161A (en) 2014-11-17 2015-11-17 Recycle of process condensate impurities in tigas.
CA2968006A CA2968006A1 (en) 2014-11-17 2015-11-17 Recycle of process condensate impurities in tigas
BR112017008676A BR112017008676A2 (en) 2014-11-17 2015-11-17 recycling of condensed impurities in a tigas process
EA201791061A EA201791061A1 (en) 2014-11-17 2015-11-17 RECIRCULATION OF IMPURITIES CONTAINED IN TECHNOLOGICAL CONDENSATE IN THE TIGAS PROCESS (IMPROVED SYNTHESIS OF BENZINE TOPPSE)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DKPA201400670 2014-11-17
DK201400670 2014-11-17

Publications (1)

Publication Number Publication Date
WO2016079112A1 true WO2016079112A1 (en) 2016-05-26

Family

ID=54545161

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2015/076809 WO2016079112A1 (en) 2014-11-17 2015-11-17 Recycle of process condensate impurities in tigas

Country Status (1)

Country Link
WO (1) WO2016079112A1 (en)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090124841A1 (en) * 2005-10-13 2009-05-14 Martin Rothaemel Process and Plant for Producing C2-C4 Olefins from Methanol and/or Dimethyl Ether
US20120004481A1 (en) * 2010-05-06 2012-01-05 IFP Energies Nouvelles Flexible process for transformation of ethanol into middle distillates
US20120102829A1 (en) * 2009-07-14 2012-05-03 Lurgi Gmbh Method and apparatus for producing synthetic fuels
WO2014124845A1 (en) * 2013-02-18 2014-08-21 L' Air Liquide Société Anonyme Pour L' Etude Et L' Exploitation Des Procédés Georges Claude Process and plant for producing olefins from oxygenates

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090124841A1 (en) * 2005-10-13 2009-05-14 Martin Rothaemel Process and Plant for Producing C2-C4 Olefins from Methanol and/or Dimethyl Ether
US20120102829A1 (en) * 2009-07-14 2012-05-03 Lurgi Gmbh Method and apparatus for producing synthetic fuels
US20120004481A1 (en) * 2010-05-06 2012-01-05 IFP Energies Nouvelles Flexible process for transformation of ethanol into middle distillates
WO2014124845A1 (en) * 2013-02-18 2014-08-21 L' Air Liquide Société Anonyme Pour L' Etude Et L' Exploitation Des Procédés Georges Claude Process and plant for producing olefins from oxygenates

Similar Documents

Publication Publication Date Title
CN205235935U (en) A equipment for following oxygen compound produces alkene
CN105837390A (en) Process for obtaining high-purity 1-butene from c4 hydrocarbon mixtures
CN106588589B (en) The method of purification of polyoxymethylene dimethyl ethers
RU2010125246A (en) METHOD FOR PRODUCING OLEFIN PRODUCT
CN105980338B (en) By the method for the raw material production 1,3-butadiene comprising ethyl alcohol
US20140186231A1 (en) Processes for producing light olefins
US8067474B2 (en) Process for the preparationn of hydrocarbons from oxygenates
de Groot et al. The industrial production of dimethyl carbonate from methanol and carbon dioxide
CA2968006A1 (en) Recycle of process condensate impurities in tigas
WO2016079112A1 (en) Recycle of process condensate impurities in tigas
CN110452087B (en) Production method of low-carbon olefin
US10131588B2 (en) Production of C2+ olefins
RU2610277C1 (en) Method for production of methanol and hydrocarbons of gasoline range using synthetic gas
CN108698960A (en) The method of the alkene production antiknock component of origin catalytic cracking
US20110288358A1 (en) Method for producing a product containing c3h6 and c2h4
KR20220163415A (en) Method for synthesizing oxetane compound through microreactor
CN109982990A (en) Integrated MTP/MTO process flow for production of propylene
US9725390B2 (en) Integrated process for converting methane to aromatics and other chemicals
RU2005101686A (en) METHOD FOR PRODUCING DIMETHYL ETHER
RU2594564C1 (en) Catalyst and method of converting ethanol, methanol or mixture thereof
CN214270725U (en) Device for comprehensively utilizing mixed carbon four
AU2015340496B2 (en) Conversion of oxygenates in purge from raw methanol evaporator
WO2015084573A2 (en) Production of c2+ olefins
US10167361B2 (en) Production of aromatics and C2+olefins
EP2935161A1 (en) Process and plant for the production of olefins

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 15794953

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 15518279

Country of ref document: US

WWE Wipo information: entry into national phase

Ref document number: MX/A/2017/006161

Country of ref document: MX

ENP Entry into the national phase

Ref document number: 2968006

Country of ref document: CA

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2015348631

Country of ref document: AU

Date of ref document: 20151117

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: 201791061

Country of ref document: EA

122 Ep: pct application non-entry in european phase

Ref document number: 15794953

Country of ref document: EP

Kind code of ref document: A1

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112017008676

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112017008676

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20170426