WO2007075204A2 - Procede et systeme de production de methanol - Google Patents

Procede et systeme de production de methanol Download PDF

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Publication number
WO2007075204A2
WO2007075204A2 PCT/US2006/037448 US2006037448W WO2007075204A2 WO 2007075204 A2 WO2007075204 A2 WO 2007075204A2 US 2006037448 W US2006037448 W US 2006037448W WO 2007075204 A2 WO2007075204 A2 WO 2007075204A2
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WO
WIPO (PCT)
Prior art keywords
stream
hydrocarbon
methanol
gas
containing gas
Prior art date
Application number
PCT/US2006/037448
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English (en)
Other versions
WO2007075204A3 (fr
Inventor
Nathan A. Pawlak
Walter Breidenstein
Robert W. Carr
Original Assignee
Gas Technologies Llc
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
Priority claimed from US11/319,093 external-priority patent/US8202916B2/en
Priority claimed from US11/351,532 external-priority patent/US7642293B2/en
Priority claimed from US11/432,692 external-priority patent/US8293186B2/en
Priority claimed from US11/446,371 external-priority patent/US9180426B2/en
Priority claimed from US11/526,824 external-priority patent/US7910787B2/en
Application filed by Gas Technologies Llc filed Critical Gas Technologies Llc
Priority to BRPI0621143-7A priority Critical patent/BRPI0621143A2/pt
Priority to JP2008548504A priority patent/JP5281897B2/ja
Priority to CN2006800493197A priority patent/CN101346331B/zh
Priority to EP06815449A priority patent/EP2054362A4/fr
Publication of WO2007075204A2 publication Critical patent/WO2007075204A2/fr
Publication of WO2007075204A3 publication Critical patent/WO2007075204A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/10—Mixing gases with gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3131—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit with additional mixing means other than injector mixers, e.g. screens, baffles or rotating elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3133—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit characterised by the specific design of the injector
    • B01F25/31331—Perforated, multi-opening, with a plurality of holes
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    • B01F25/45—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads
    • B01F25/452—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads characterised by elements provided with orifices or interstitial spaces
    • B01F25/4521—Mixers in which the materials to be mixed are pressed together through orifices or interstitial spaces, e.g. between beads characterised by elements provided with orifices or interstitial spaces the components being pressed through orifices in elements, e.g. flat plates or cylinders, which obstruct the whole diameter of the tube
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/1516—Multisteps
    • C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
    • C07C29/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
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Definitions

  • the present invention relates to a method of and an apparatus for producing methanol.
  • Russian Patent No. 2,162,460 includes a source of hydrocarbon-containing gas, a compressor and a heater for compression and heating of the gas, and a source of oxygen-containing gas with a compressor. It further includes successively arranged reactors with alternating mixing and reaction zones and a means to supply the hydrocarbon-containing gas into a first mixing zone of the reactor and the oxygen-containing gas into each mixing zone, a recuperative heat exchanger for cooling of the reaction mixture through a wall by a stream of cold hydrocarbon-containing gas of the heated hydrocarbon-containing gas into a heater, a cooler-condenser, a partial condenser for separation of waste gasses and liquid products with a subsequent separation of methanol, a pipeline for supply of the waste gas into the initial hydrocarbon-containing gas, and a pipeline for supply of waste oxygen- containing products into the first mixing zone of the reactor.
  • the apparatus also requires burning an additional quantity of the initial hydrocarbon-containing gas in order to provide the utility needs of a rectification of liquid products. Since it is necessary to cool the gas- liquid mixture after each reactor for separation of liquid products and subsequent heating before a next reactor, the apparatus is substantially complicated and the number of units is increased.
  • a further method and apparatus for producing methanol is disclosed in the patent document RU 2,200,731 , in which compressed heated hydrocarbon-containing gas and compressed oxygen-containing gas are introduced into mixing zones of successively arranged reactors, and the reaction is performed with a controlled heat pick-up by cooling of the reaction mixture with water condensate so that steam is obtained, and a degree of cooling of the reaction mixture is regulated by parameters of escaping steam, which is used in liquid product rectification stage.
  • a method of producing methanol which includes the steps of supplying into a reactor a hydrocarbon-containing gas stream, supplying into the reactor an oxygen containing gas; carrying out in the reactor an oxidation of the hydrocarbon- containing gas by oxygen of said oxygen-containing gas; and, after removing impurities and products of the reaction, recycling un-reacted hydrocarbon gas into the hydrocarbon-containing gas stream for further reaction.
  • Another feature of the present teachings is an apparatus for producing methanol, which has a reactor for receiving and reacting a hydrocarbon-containing gas stream from a well or other source with an oxygen- containing gas, to carry out in the reactor oxidation of the heated hydrocarbon- containing gas by oxygen of said oxygen-containing gas.
  • the apparatus also has a mechanism for supplying into the reactor a non-oxidizing coolant to be directly mixed with a mixture of said heated hydrocarbon containing gas and said oxygen containing gas at a later stage of the reaction to inhibit the further oxidation and decomposition of formaldehyde. Un-reacted hydrocarbon- containing gas is then processed to remove products and contaminants before being recycled back into the hydrocarbon-containing gas stream. Reaction byproducts, such as CO 2 , can be injected into the ground at a predetermined distance from a well to increase the output of the well.
  • a heated hydrocarbon-containing gas stream and oxygen-containing gas are supplied into a reaction zone or into a reactor, where a gas phase oxidation of the hydrocarbon-containing gas is performed at elevated temperature and pressure in the reaction zone.
  • the reaction mixture is cooled and then is separated into waste gas and liquid product.
  • the waste gas is scrubbed to remove CO 2 and formaldehyde and returned to the heated hydrocarbon-containing gas stream.
  • Cold hydrocarbon-containing gas is supplied into a regulation zone of the reactor to reduce the temperature of the hydrocarbon-containing gas thereby to provide a redistribution of the ratio of products to produce corresponding quantities of methanol and formaldehyde.
  • Methanol produced can then be injected into a natural gas stream to reduce the formation of hydrates within the pipeline.
  • Figures 1A and 1 B are views schematically showing a system of an apparatus for producing methanol in accordance with the present teachings;
  • Figures 2 and 3 are views illustrating concentrations of oxygen, formaldehyde and methanol during reactions in accordance with the prior art and in accordance with the present invention correspondingly;
  • Figure 4 represents a graph depicting the yield oxygenates of the system as a function of recycle ratio
  • Figure 5 represents an alternate methane to methanol plant according to the teachings of the present invention.
  • Figure 6 represents an optional oxygen producing plant shown in Figure 5;
  • Figure 7 depicts a gas processing portion of the plant shown in
  • Figure 8 represents the liquid processing portion of the plant shown in Figure 5.
  • An apparatus for producing methanol in accordance with the present invention has a reactor 100 which facilitates a gas phase oxidation of a hydrocarbon-containing gas is shown in Figures 1A and 1B.
  • Figure 1 B details the inputs and outputs of the reactor.
  • the reactor 100 has a reaction zone 102 which is provided with a device 104 for introducing a heated hydrocarbon-containing gas stream and a device 105 for introducing an oxygen-containing gas.
  • the oxygen-containing gas preferably has greater than 80% oxygen content to reduce the accumulation of inert gases by the recycling process.
  • the reactor 100 further has a regulation zone 108 provided with an optional device 110 for introducing a cold hydrocarbon-containing gas stream for reducing the temperature of reaction during operation of the apparatus.
  • the reactor 100 is provided with thermal pockets 112 for control and regulation of temperatures in corresponding zones, provided for example with thermocouples.
  • the apparatus has a device 114 for cooling the reaction mixture before separation. Additionally, the partial condenser 122 incorporates a gas- liquid heat exchanger to further reduce the temperature of the products.
  • the condenser 122 separates H 2 O and alcohols from a hydrocarbon-CO2 mixture.
  • the partial condenser 122 is preferably isobaric, as opposed to isothermal, to avoid pressure losses.
  • the product stream enters, and liquid stream and gaseous stream exit the condenser 122.
  • Block 139 represents equipment which is configured to separate contaminants and products from a hydrocarbon-containing recycle gas component.
  • the equipment 139 is configured to remove CO 2 from the reduced product stream.
  • the equipment 139 can take the form of a purge valve, absorber, membrane separator, or an adsorber. It is envisioned the equipment 139 can be used to regulate the percentage of other non-reactive components such as N 2 with, for example, a purge valve.
  • the gaseous reduced product stream leaves the isobaric condenser 122 and is passed to the scrubber 134.
  • Other potential methods which can be utilized use materials such as various amines known to remove CO 2 and formaldehyde.
  • modification of the flow rate of methanol or operating temperature of the scrubber column can be used. If it is desirable to operate at extremely low absorbent flow rates, then a lower temperature can be utilized, for example O 0 C. If it is desirable to operate at ambient temperatures or temperatures achievable via cooling water, then a high flow rate can be utilized, for example, ten times that of the flow rate for 0 0 C. In either scenario, the pregnant methanol absorbent stream 14 is completely regenerated by the formaldehyde distillation column 138.
  • the stream 14 from the scrubber 134 can be passed through the condenser 122 to provide cooling of the product stream and preheating of the methanol recycle to improve the energy efficiency of the formaldehyde distillation column 138.
  • the reactor 100 is connected with a compressor 124 and heater 126 for supply of compressed and heated oxygen-containing gas.
  • the raw hydrocarbon-containing gas is mixed with cleaned hydrocarbon gas from the scrubber 134 and is heated using a heater 136.
  • the raw hydrocarbons can be mixed with the reduced product hydrocarbon stream from the condenser 122 prior to the entry of the scrubber 134 for removal of contaminant gases prior to entering the reactor.
  • the apparatus further has a unit for rectification of methanol which includes a flash drum 132, rectification column 128, and a vessel 130 from which methanol is supplied to storage or further processing.
  • This rectification column 128 is used to separate methanol (light-key component) from ethanol (heavy-key component) and water (non-key component).
  • methanol light-key component
  • ethanol heavy-key component
  • water non-key component
  • Stream 8 has some amount of ethanol (and perhaps methanol, if ultra pure methanol was produced) and will be used as the basis of the aqueous makeup of the commercial formalin stream (stream 11). In this manner, some of the ethanol is recovered before the remainder is discarded in the liquid waste stream.
  • a flash drum 132 Disposed between the column 128 and the condenser 122 is a flash drum 132 for removal of CO 2 and formaldehyde from the liquid product stream.
  • the purpose of the flash drum 132 is to drop the pressure to an appropriate level before entry into the methanol rectification column 128 and to substantially remove any dissolved gases, typically CO 2 and formaldehyde, from the liquid product stream.
  • the raw hydrocarbon-containing gas stream with a methane content for example up to 98% and the reduced hydrocarbon product stream are supplied from an installation for preparation of gas or any other source to the heater 136, in which it is heated to temperature 430-470 0 C.
  • the heated hydrocarbon-containing gas is then supplied into the reaction zone 102 of the reactor 100.
  • Compressed air with pressure, for example, of 7-8 MPa and with a ratio 80% to 100% and, preferably, 90% to 95% oxygen is supplied by the compressor 124 also into the reaction zone 102 of the reactor 100. Oxidation reaction takes place in the reaction zone 102 of the reactor 100.
  • the O 2 stream is preferably substantially pure, thus limiting the amount of N 2 entering the system.
  • An optional second stream of cold or in other words a lower temperature coolant than the gases in the reactor is supplied through the introducing device 108 into the regulation zone of the reactor 100.
  • This stream is regulated by the regulating device 120, which can be formed as a known gas supply regulating device, regulating valve or the like.
  • This cold stream can be, for example, composed of a raw hydrocarbon stream, a recycled stream, or a portion or combination of the two.
  • the regulator is configured to adjust the volume or pressure of cold hydrocarbon-containing gas based on system parameters such as, but not limited to, pressure, temperature or reaction product percentages down stream in the system.
  • the coolant which is supplied from a coolant source, functions to reduce the temperature of the partially oxidized methane to reduce the continued oxidation or decomposition of formaldehyde.
  • This coolant can be any material which can easily be separated from the reaction product stream.
  • the coolant can be an unheated hydrocarbon or methane containing gas stream.
  • the coolant can be any non-oxidizing material which can be easily separated from the reaction products.
  • the coolant can be gaseous or an aerosoled or misted liquid of, for example, CO 2 , formaldehyde, methanol, water or steam. It is additionally envisioned that the coolant can further be a mixture of recycled reaction products, water, steam, and/or raw hydrocarbon gases.
  • the reaction mixture is subjected to the reaction in the reactor without the introduction of the cold hydrocarbon-containing gas if it is desired to produce exclusively methanol.
  • the introduction of the cold hydrocarbon-containing gas is used when it is desired to produce methanol and formaldehyde.
  • the temperature of the reaction is reduced for example by 30-90° so as to preserve the content of formaldehyde into the separated mixture by reducing the decomposition of the formaldehyde to CO 2 .
  • the reaction mixture is supplied into the heat exchanger 114 for transfer of heat to the reactor input stream from the reaction mixture exiting the reactor, and after further cooling is supplied within partial condenser 122. Separation of the mixture into high and low volatility components, (dry gas and raw liquid, respectively) is performed in the partial condenser 122 which may absorb at least some of the formaldehyde into the raw liquid stream as desired. The dry gas is forwarded to a scrubber 134, while the raw liquids from the condenser 122 are supplied to the flash drum 132.
  • the scrubber 134 functions to remove the CO 2 and formaldehyde from the dry gas stream.
  • the scrubber 134 uses both H 2 O and methanol at between 7-8 MPa pressure and between about 0°C and about 50°C to absorb CO 2 and formaldehyde.
  • the reduced stream of hydrocarbon gas is recycled by mixing the reduced stream with the raw hydrocarbon-containing gas stream either before or within the reactor, as desired.
  • the raw hydrocarbon and reduced streams, individually or in combination, are then inputted into the reaction chamber 100 at input 104 or input 110 after being heated by heat exchanger 116 and heater 136 as previously described.
  • the rectification column is used to separate carbon dioxide (non-key component) and formaldehyde (light-key component) from methanol (heavy-key component) and water (non-key component).
  • the pregnant methanol steam, stream 14 enters the rectification column and is separated into a formaldehyde distillate, stream 16, and a bottoms stream, stream 15.
  • Some amount of methanol in the distillate stream is desirable since methanol is used as a stabilizer for the production of commercial grade formalin (6-15% alcohol stabilizer, 37% formaldehyde, and the balance being water).
  • the formaldehyde, water, methanol and CO 2 removed by scrubber 134 are passed to formaldehyde rectification column 138.
  • Column 138 removes formaldehyde and CO 2 from the methanol-water stream. Small amounts of methanol are combined with produced methanol and are inputted into the scrubber 134 to remove additional amounts of CO 2 and formaldehyde from the reduced hydrocarbon stream.
  • Free or non-aqueous formaldehyde is allowed to remain in the gas phase by operation of the isobaric condenser 122.
  • the liquid methanol product stream, or raw liquids, would then comprise methanol, ethanol, and water by allowing formaldehyde to remain in the gaseous stream.
  • the liquid stream exiting the isobaric condenser 122 can bypass the formaldehyde rectification portion of the process and enter the methanol rectification column after having optionally passed through the flash drum 132.
  • Figures 2 and 3 show diagrams of the concentration of oxygen, formaldehyde and methanol in reactions without cooling and with cooling, respectively.
  • Figure 2 approximately after 2 sec, oxygen is burnt completely. At this moment the reaction temperature reaches its maximum and methanol and formaldehyde are produced in their respective proportions within the reaction mixture. Methanol is a more stable product at the end of the reaction and its concentration remains substantially stable after reaching its maximum concentration. Formaldehyde is less stable, and therefore with a temperature increase (the temperature increases until oxygen is burnt completely) its concentration somewhat reduces.
  • Figure 4 represents a graph depicting the yield of oxygenates for the system as a function of the recycle ratio of the recycling hydrocarbon gasses. Shown is a graph depicting the use of Michigan Antrim gas having 97% CH 4 and 1 % N 2 . In this regard, the graph shows a significant increase in product yield using the same input stream and with little increase in capital costs. As the system efficiently manages pressure and integrates process energy usage, energy requirements are minimized, thus increasing the overall system economics.
  • Figure 5 represents an alternate methane to methanol plant 150.
  • the plant 150 is positioned to process methane from gas being discharged from either a combined oil and gas field 152 or the gas field 154.
  • the plant 150 which is preferably located in close proximity to the well bore, is generally formed of a gas processing plant 156, a liquid processing plant 158, and an oxygen producing plant 160. Additionally associated with the plant 150 are waste water treatment and utility plants 162 and 164.
  • an optional oxygen producing plant 160 can be used to assist in the regulation of the partial oxidation of the hydrocarbon stream in the reactor 100.
  • the oxygen producing plant 160 has a compressor 161 coupled to a heat exchanger 163 which functions to prepare the compressed oxygen for injection into a plurality of absorbers 165. After passing through the absorbers, the produced oxygen stream is compressed and forwarded directly to the reactor 100.
  • the gas processing portion of the plant 156 generally functions as described above (see Figures 1A and 1 B).
  • the gas processing plant 156 has compressors 170 and 172 for raising the pressure of a cleaned incoming hydrocarbon stream 174.
  • This stream 174 is then divided and reacted with oxygen in the reactor 100 to partially oxidize methane as described above.
  • the parameters such as time of reaction and temperature and pressure within the reactor can be adjusted to selectively control the amount of CO 2 , H 2 O, formaldehyde and methanol which is produced in the reactor 100.
  • the reaction products 176 from the reactor are then transferred to the liquid processing plant 158.
  • the liquid processing plant 158 generally functions as described above to separate the methanol and formaldehyde from the reaction product stream 176. Shown are associated distillers, blenders and flash drums which are used to separate the constituent materials of the reaction product stream as described in detail above. Specifically, CO 2 is removed from the reaction product stream as are methanol and, if desired, formaldehyde.
  • the scrubber 134 (see Figure 5) prevents the accumulation of CO 2 and allows the physical capture of formaldehyde.
  • the scrubber 134 can utilize a mixture of methanol and water to physically absorb formaldehyde and CO 2 from the hydrocarbon gas recycle loop 135.
  • the efficiency of the scrubber 134 which can operate adequately without refrigeration, is made possible due to the high operating pressure of the recycle loop 135. This is opposed to cryogenically low temperatures utilized by traditional absorption processes.
  • the gases enter the scrubber 134 as a "dirty" gas with some amount of formaldehyde and CO 2 present. These components will only be present in relatively dilute amounts, so the duty of the methanol absorbent is also relatively small.
  • the output of the reactor can be selectively adjusted so as to minimize the amount of formaldehyde being produced by the gas process portion of the plant 156.
  • the CO 2 can be vented, it is specifically envisioned that the CO 2 from the reaction products can be injected, at a predetermined distance from the well, into the ground to increase the output of the well.
  • the CO 2 can be injected at any appropriate distance from the well so as to allow for the increase of subterranean pressures to increase the gas or oil output of the well.
  • the CO 2 can be injected into the casement of the wellbore or in the near-wellbore zone, to increase the output of the gas or oil and gas producing well.
  • the plant 100 can be associated with an off-shore oil rig.
  • the plant 100 would either be on the off-shore rig or would be a predetermined short distance from the rig, such as immediately adjacent to the off-shore rig on a floatable platform.
  • the methanol converted from the methane containing hydrocarbon stream would be injected into a second portion of the methane containing hydrocarbon stream to improve the flow of the hydrocarbon stream from the off-shore oil well to land. This methanol is injected to reduce the formation of hydrates within the piping. The methanol associated with the natural gas would then be removed from the hydrocarbon containing stream after the stream reaches the shore.
  • any of the other reaction products namely, CO 2 , water or methanol can be injected directly into the hydrocarbon containing subterranean formations surrounding the platform or a land-based well.
  • methanol can be injected into hydrate structures surrounding the well so as to increase the output of natural gas from a natural gas producing well.
  • the CO 2 can be injected into one portion of the well while methanol or other reaction products can be injected into other portions of the well.
  • facilities may be provided to manage nitrogen build-up in the recycle loop.
  • outputs of any particular well 152, 154 are low, it is envisioned that a single plant 100 having a truncated process can be used. In these situations, only portions of the facility related to the partial oxidation of the hydrocarbon stream and associated facilities to remove CO 2 will be used near the well.
  • Removed CO 2 can be collected, vented or reinjected into the ground. Immediately after removal of the natural gas and associated CO 2 by the scrubber, the remaining liquid products can be transported in liquid form from the well site to another location for separation of formaldehyde, methanol and water from the waste stream.
  • a centralized liquid processing plant to finalize the processing of the liquid processes (158) can be located at a significant distance from the stranded natural gas locations. This allows for the use of a centralized liquid process facility 158. It is also envisioned that the conditions of the reactor can be adjusted to produce a liquid phase which contains a commercial grade of formalin.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Dispersion Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

L'invention concerne un dispositif et un procédé de production de méthanol, qui comporte les étapes consistant à: mettre à réagir un gaz chauffé contenant un hydrocarbure et un gaz contenant de l'oxygène dans un réacteur; prévoir un flux de produit contenant du méthanol; et transférer la chaleur provenant du flux de produit vers le gaz contenant un hydrocarbure afin de chauffer ce gaz; après extraction du méthanol et du CO2 du flux de produit, mélanger les hydrocarbures non traités avec le gaz contenant un hydrocarbure en vue d'un retraitement dans le réacteur. Les sous-produits du réacteur sont injectés dans le sol afin d'accroître la production d'un puits de production d'hydrocarbures.
PCT/US2006/037448 2005-12-27 2006-09-26 Procede et systeme de production de methanol WO2007075204A2 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
BRPI0621143-7A BRPI0621143A2 (pt) 2005-12-27 2006-09-26 método de produção de metanol, método de transferência de uma corrente que contém hidrocarboneto gasoso de uma plataforma costa-afora e método de transporte de uma corrente de hidrocarboneto contendo metano de um poço de produção de hidrocarboneto costa-afora
JP2008548504A JP5281897B2 (ja) 2005-12-27 2006-09-26 メタノール生産のための方法およびシステム
CN2006800493197A CN101346331B (zh) 2005-12-27 2006-09-26 用于生产甲醇的方法和系统
EP06815449A EP2054362A4 (fr) 2005-12-27 2006-09-26 Procede et systeme de production de methanol

Applications Claiming Priority (10)

Application Number Priority Date Filing Date Title
US11/319,093 2005-12-27
US11/319,093 US8202916B2 (en) 2004-07-29 2005-12-27 Method of and apparatus for producing methanol
US11/351,532 US7642293B2 (en) 2004-07-29 2006-02-10 Method and apparatus for producing methanol with hydrocarbon recycling
US11/351,532 2006-02-10
US11/432,692 2006-05-11
US11/432,692 US8293186B2 (en) 2004-07-29 2006-05-11 Method and apparatus for producing methanol
US11/446,371 2006-06-02
US11/446,371 US9180426B2 (en) 2004-07-29 2006-06-02 Scrubber for methanol production system
US11/526,824 US7910787B2 (en) 2004-07-29 2006-09-25 Method and system for methanol production
US11/526,824 2006-09-25

Publications (2)

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WO2007075204A2 true WO2007075204A2 (fr) 2007-07-05
WO2007075204A3 WO2007075204A3 (fr) 2007-11-22

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US2004714A (en) * 1931-07-23 1935-06-11 Hanlon Buchanan Inc Treatment of hydrocarbons
US2722553A (en) * 1952-08-30 1955-11-01 Chemical Construction Corp Partial oxidation of hydrocarbons
DE2743113C3 (de) * 1977-09-24 1980-09-04 Chemische Werke Huels Ag, 4370 Marl Verfahren zur Herstellung von Gemischen aus Formaldehyd und Methanol durch partielle Oxidation von Methan
US4383842A (en) * 1981-10-01 1983-05-17 Koch Process Systems, Inc. Distillative separation of methane and carbon dioxide
NO982491L (no) * 1998-05-29 1999-11-30 Naturkraft As Fremgangsmåte for å fremstille en gassblanding og anvendelse av den fremstilte gassblandingen
DE19849337A1 (de) * 1998-10-26 2000-01-27 Linde Ag Verfahren und Vorrichtung zum Fördern von Erdgas aus Gashydratlagerstätten
JP3690514B2 (ja) * 2001-06-22 2005-08-31 川崎重工業株式会社 地下の石炭層を用いて燃料と燃焼ガスのクローズドシステムを構築したガスタービン設備
WO2003018958A1 (fr) * 2001-08-31 2003-03-06 Statoil Asa Procede et installation permettant une recuperation de petrole amelioree et une synthese simultanee d'hydrocarbures a partir de gaz naturel
NO20026021D0 (no) * 2002-12-13 2002-12-13 Statoil Asa I & K Ir Pat Fremgangsmåte for ökt oljeutvinning
JP2005330170A (ja) * 2004-05-21 2005-12-02 Toshiba Corp 水素製造システムおよび水素製造方法

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JP2009521530A (ja) 2009-06-04
JP5281897B2 (ja) 2013-09-04
EP2054362A4 (fr) 2010-05-26
EP2054362A2 (fr) 2009-05-06
WO2007075204A3 (fr) 2007-11-22
BRPI0621143A2 (pt) 2011-11-29

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