EP2454218A1 - Procédé et installation de production de carburants synthétiques - Google Patents

Procédé et installation de production de carburants synthétiques

Info

Publication number
EP2454218A1
EP2454218A1 EP10737757A EP10737757A EP2454218A1 EP 2454218 A1 EP2454218 A1 EP 2454218A1 EP 10737757 A EP10737757 A EP 10737757A EP 10737757 A EP10737757 A EP 10737757A EP 2454218 A1 EP2454218 A1 EP 2454218A1
Authority
EP
European Patent Office
Prior art keywords
stream
hydrocarbons
etherification
rich
reactor
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
Application number
EP10737757A
Other languages
German (de)
English (en)
Other versions
EP2454218B1 (fr
Inventor
Martin Rothaemel
Theis Ohlhaver
Peter Trabold
Andreas Ochs
Harald KÖMPEL
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.)
Air Liquide Global E&C Solutions Germany GmbH
Original Assignee
Lurgi GmbH
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 Lurgi GmbH filed Critical Lurgi GmbH
Publication of EP2454218A1 publication Critical patent/EP2454218A1/fr
Application granted granted Critical
Publication of EP2454218B1 publication Critical patent/EP2454218B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/22—Organic compounds not containing metal atoms containing oxygen as the only hetero atom
    • 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
    • C10G2400/20—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
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/18—Organic compounds containing oxygen
    • C10L1/185—Ethers; Acetals; Ketals; Aldehydes; Ketones
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/18—Organic compounds containing oxygen
    • C10L1/185—Ethers; Acetals; Ketals; Aldehydes; Ketones
    • C10L1/1852—Ethers; Acetals; Ketals; Orthoesters
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2270/00—Specifically adapted fuels
    • C10L2270/02—Specifically adapted fuels for internal combustion engines
    • C10L2270/023—Specifically adapted fuels for internal combustion engines for gasoline engines
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/543—Distillation, fractionation or rectification for separating fractions, components or impurities during preparation or upgrading of a fuel
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/58—Control or regulation of the fuel preparation of upgrading process
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/60—Measuring or analysing fractions, components or impurities or process conditions during preparation or upgrading of a fuel
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2300/00—Mixture of two or more additives covered by the same group of C10L1/00 - C10L1/308
    • C10L2300/30—Mixture of three components

Definitions

  • the invention relates to a method and a plant for the production of synthetic fuels from a water vapor and oxygenates, such as methanol and / or dimethyl ether (DME), containing educt mixture.
  • a water vapor and oxygenates such as methanol and / or dimethyl ether (DME), containing educt mixture.
  • DME dimethyl ether
  • C 2 -C 4 -olefins in particular propylene
  • MTP dimethyl ether
  • a variety of methods are known in the art, which usually on the implementation of a steam and methanol and / or or Dimethyletherdampf-containing educt mixture based on a shape-selective zeolite catalyst. Such methods are described, for example, in DE 100 27 159 A1 or EP 0 882 692 B1.
  • the methanol is placed in an adiabatically operated prereactor, where it is converted to dimethyl ether (DME) and water (H 2 O) using a highly active and highly selective Al 2 O 3 catalyst.
  • DME dimethyl ether
  • H 2 O water
  • the methanol / water / DME stream is passed to the first of several reactor stages, in which the resulting vapor is supplied.
  • the hydrocarbon product mainly produces propylene.
  • Further reactions can be achieved in subsequent reactor stages.
  • the process conditions are selected in all stages so that similar reaction conditions and a maximum propylene yield are ensured. This results in a yield of propylene of over 60%, in addition to other olefin fractions, but also a gasoline fraction.
  • the resulting from such a plant gasoline product is high quality. Typical values compared to the specified European specifications according to EN 228 for normal gasoline show the high quality of the product:
  • the adducts must be hydrogenated, which decreases the octane number and the boiling curve is worse.
  • Obtaining the high octane number of synthetic crude gas can be achieved by alkylation, for example of i-butane with butenes.
  • the olefin content decreases with simultaneous formation of high-octane paraffinic adducts.
  • the high-acid catalyst eg sulfuric acid, hydrogen fluoride
  • the reaction would therefore require a complex and unprofitable separation of the fraction to be alkylated, such as the C 4 fraction.
  • 4,361,422 teaches a process for the treatment of an olefinic C 5 fraction by controlled hydrogenation and subsequent etherification with a C 1 -C 4 alcohol.
  • the patent US 3,902,870 reports on the reduction of the olefin content correlated bromine number of cracking benzene by olefin etherification with methanol.
  • US Pat. No. 3,482,952 also discloses a process for preparing a high-octane gasoline while simultaneously reducing the volatility and the atmospheric reactivity by etherification of the tertiary olefins with lower alcohols in the presence of an etherification catalyst.
  • CA 22 28 738 teaches a process for the preparation of light olefins by the combination of the process steps steam reforming, oxygenate production and conversion of oxygenates to olefins, wherein the propylene and butylene obtained in the latter step is converted by etherification in high-octane products, after previously were separated from the product mixture.
  • a steam and oxygenates, such as methanol and / or dimethyl ether, containing reactant mixture is reacted on a catalyst to olefins, this olefin mixture in one Separator is divided into a stream rich in d- C 4 hydrocarbons and a stream rich in C 5 + hydrocarbons, the stream rich in C 5 + hydrocarbons in one of C 5 - and Ce- hydrocarbons (pentene, hexene) range Stream and a stream rich in C 7+ hydrocarbons, the stream rich in C 5 and C 6 hydrocarbons is at least partially subjected to etherification with methanol, and the resulting ethers are admixed with the gasoline product stream rich in C 7+ hydrocarbons.
  • the octane number remains constant.
  • the C 5 and C ⁇ olefins contained in the gasoline fraction have octane numbers of 110-145, paraffins, which may also be produced by additional hydrogenation, lead to octane numbers of 85 - 100 and the methyl ether formed by the etherification have octane numbers of 115 - 125, these octane numbers each having to be understood as mixing octane numbers, so-called BONs (blending octane numbers).
  • a methanol supply is present through the previous process steps and no further substances have to be introduced into the process.
  • the LPG also produced only has a low Olefinanteil.
  • C - - According to a preferred embodiment of the invention, a partial stream of 5 to C is rich hydrocarbon stream past the etherification and blended directly with the rich in C 7 + hydrocarbons gasoline product stream. It has proved to be advantageous in this case to regulate the division between the Cs / C ⁇ stream fed to the etherification and the C 5 / C 6 stream passed past the etherification as a function of the total olefin content of the resulting gasoline product.
  • the C 4 fraction is separated off from the stream which is rich in C 1 -C 4 -hydrocarbons and at least partially subjected to etherification with methanol.
  • the amount of the valuable product can be further increased in compliance with the specifications. From the butene fraction, this produces methyl tertiary butyl ether (MTBE).
  • MTBE methyl tertiary butyl ether
  • a C 4 partial flow is always present in a MTP system, so that there are no additional costs.
  • the gasoline product according to the invention if necessary, a C 4 partial stream is added.
  • Another embodiment of the invention involves returning at least portions of the pentene and hexene fractions to the reactor of the first process stage, which further increases the flexibility of the process with respect to the product spectrum.
  • a selective hydrogenation which precedes the olefin etherification
  • Temperatures of 50 to 90 0 C and a pressure of 1 to 1, 5 MPa are particularly preferred, since then all components are liquid.
  • the invention further relates to a plant for the production of synthetic fuels, which is suitable for carrying out the method according to the invention.
  • This plant comprises a reactor for the catalytic conversion of a water vapor and oxygenates, such as methanol and / or dimethyl ether, containing educt mixture to olefins, a first separator for dividing the olefin mixture into a current rich in CiC-p hydrocarbons and a current rich in C 5+ hydrocarbons a further separator for branching off a to C 5 - and Ce-rich stream from the hydrocarbons rich in C 5 + hydrocarbons stream and a reactor for the etherification of the C 5 fraction and the C 6 fraction with methanol.
  • a water vapor and oxygenates such as methanol and / or dimethyl ether
  • butene is additionally fed to the etherification reactor via a feed line.
  • the olefin content of the resulting gasoline can be further reduced and the butene can be used to increase value.
  • a further embodiment of the system according to the invention provides a line for at least partial recycling of the pentene and hexene fraction from the further separation device to the olefin-producing reactor. This further increases the flexibility with regard to the product range generated by this system.
  • a reactor for selective hydrogenation of these compounds is provided, which is connected upstream of the reactor for etherification.
  • the etherification reactor is an ion exchanger, as a result of which an established and thus risk-minimized component is used
  • a cooler As a separator for dividing the olefin mixture in the Ci-C 4 stream and the stream rich in C 5 + hydrocarbons, preferably a cooler is used, which dispenses with the introduction of additional substances other than in a chemical separation process.
  • the single figure shows schematically a plant for carrying out the method according to the invention.
  • methanol is fed as starting material through line 1 in a DME reactor 2 and there, for example.
  • a DME reactor 2 At an Al 2 O 3 catalyst at least partially converted to dimethyl ether.
  • the methanol / DME mixture is then passed through line 3 and 4, mixed with the steam coming from line 14 and finally fed via line 5 into the reactor 6 where it is catalytically converted to hydrocarbons, in particular to propylene (MTP ).
  • Line 7 leads the product mixture into a cooler 8 designed as the first separation device in which the olefin fractions are divided into a Ci-C 4 -hydrocarbons stream and a stream rich in C 5+ hydrocarbons. Furthermore, there is water as by-product of the reaction.
  • the cooler 8 is thus a three-phase separator (liquid / liquid / gaseous).
  • the Ci-C 4 fractions are fed via line 16 into the compressor 17 and through line 18 to a second separator 19, which consists of at least one distillation column.
  • a propylene-rich stream is fed to a further separating device 50, in which a propane-rich stream is separated off.
  • the propylene-rich stream is discharged via line 20a.
  • Via line 21, the separated C- t fraction leaves the separator 19.
  • a portion of the stream via line 21a is discharged together with the propane from line 20b as liquefied petroleum gas (LPG).
  • LPG liquefied petroleum gas
  • the main part of the stream 21 is transferred via the line 21 b and 24 in line 26, in the with Line 22 and the preferably withdrawn via the top of the separator 19 ethylene-rich fraction is transferred.
  • the stream can then be returned to the line 4 in front of the reactor 6.
  • water is removed from condenser 8 via line 9, and those olefin fractions which are rich in components having a chain length of five or more carbon atoms (C 5+ stream) are withdrawn via line 15.
  • line 10 and 11 the water formed mainly by the reaction of methanol and DME is discharged from the process, wherein a partial stream of water via line 12 to an evaporator 13 and then fed via line 14 and 5 as steam into the reactor 6 can.
  • the C 5+ stream passes via line 15 into a further, third separation device 28, in which a stream rich in C 7 + hydrocarbons is removed and withdrawn from the process through lines 38, 40 and 41.
  • the C 5 -fraction and the C 6 -fraction are withdrawn via line 29 from the third separator 28.
  • this fraction can be at least partially fed into line 26 and combined with the ethylene and the butylene fraction to the reactor 6 recycled.
  • At least a subset of the C 5 / C 6 fraction from line 29 is transferred to line 30. From there, the further divided stream wholly or partially mixed through line 39 the higher olefins from line 38 and are withdrawn from the process whereby the ratio of the flow rates in line 39 to that in line 30 can be between 0 and 100%.
  • the etherification reactor 36 may be preceded by a selective hydrogenation in order to remove interfering compounds, such as dienes.
  • the division of the pentene and hexene fraction on lines 32 and 39 is regulated as a function of the olefin content of the gasoline product in line 41.
  • the higher the olefin content the greater the proportion of the C 5 / C 6 stream which exceeds the Etherification is performed, since this can be lowered, the olefin content.
  • Partial flow in an MTP system anyway exist, there are no additional costs.
  • the effect of the partial etherification according to the invention of a partial flow of the MTP gasoline for the purpose of lowering the olefin content is illustrated in the following calculation examples. In each case relative amounts are indicated. In addition, the increase in volume of the product is taken into account by the addition of methanol, for the sake of simplicity it was assumed that the proportion of olefin in the Cs / C ⁇ stream in each case split in half on pentenes and hexenes.
  • VA is the etherification fraction, ie the ratio of mass flow 32 / mass flow 30.
  • the olefin content of the streams 38 and 30 changes, for example as a result of aging of the catalyst or altered reaction conditions, a new operating point for the etherification fraction is obtained.
  • the olefin content in the effluent streams has decreased so that the operator of a plant can reduce the etherification fraction to 33% and still not exceed 18% in the gasoline product 41.

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  • 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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé de production de carburants synthétiques, procédé selon lequel, dans une première étape, un mélange de produits de départ renfermant de la vapeur d'eau et des oxygénats tels que méthanol et/ou diméthyléther est transformé, sur catalyseur, en oléfines, et ce mélange d'oléfines est réparti, dans un dispositif de séparation, en un courant riche en hydrocarbures en C1-C4- et en un courant riche en hydrocarbures en C5+-. Le courant riche en hydrocarbures en C5+- est réparti en un courant riche en hydrocarbures en C5- et C6- et en un courant riche en hydrocarbures en C7+-, le courant riche en hydrocarbures en C5- et C6- étant soumis, au moins partiellement, à une éthérification avec le méthanol. Les éthers ainsi formés sont incorporés au courant de produits de l'essence.
EP10737757.4A 2009-07-14 2010-07-03 Procédé et installation de production de carburants synthétiques Active EP2454218B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102009032915A DE102009032915A1 (de) 2009-07-14 2009-07-14 Verfahren und Anlage zur Herstellung von synthetischen Kraftstoffen
PCT/EP2010/004032 WO2011006594A1 (fr) 2009-07-14 2010-07-03 Procédé et installation de production de carburants synthétiques

Publications (2)

Publication Number Publication Date
EP2454218A1 true EP2454218A1 (fr) 2012-05-23
EP2454218B1 EP2454218B1 (fr) 2015-09-02

Family

ID=42691165

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10737757.4A Active EP2454218B1 (fr) 2009-07-14 2010-07-03 Procédé et installation de production de carburants synthétiques

Country Status (6)

Country Link
US (1) US9028567B2 (fr)
EP (1) EP2454218B1 (fr)
CN (1) CN102471179B (fr)
DE (1) DE102009032915A1 (fr)
RU (1) RU2509070C2 (fr)
WO (1) WO2011006594A1 (fr)

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DE102013101577B4 (de) * 2013-02-18 2019-01-31 L’AIR LIQUIDE Société Anonyme pour l’Etude et l’Exploitation des Procédés Georges Claude Verfahren und Anlage zur Herstellung von Olefinen aus Oxygenaten
WO2016079112A1 (fr) * 2014-11-17 2016-05-26 Haldor Topsøe A/S Recyclage d'impuretés de condensat de transformation dans tigas
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Also Published As

Publication number Publication date
RU2012104886A (ru) 2013-08-20
WO2011006594A1 (fr) 2011-01-20
RU2509070C2 (ru) 2014-03-10
US9028567B2 (en) 2015-05-12
CN102471179A (zh) 2012-05-23
DE102009032915A1 (de) 2011-03-31
CN102471179B (zh) 2015-02-25
EP2454218B1 (fr) 2015-09-02
US20120102829A1 (en) 2012-05-03

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