JP5281897B2 - Method and system for methanol production - Google Patents

Description

The present invention relates to a method and system method for methanol production.

Methods and apparatus for converting methane to methanol are known. For example, Karavaev M.M. M.M. Leonov B. E. , Et al., “Technology of Synthetic Methanol”, Moscow, “Chemistry”, 1984, pages 72-125, followed by gas phase conversion of methane to synthesis gas (a mixture of CO and H ₂ ), followed by It is known to perform catalytic conversion to methanol. However, to realize this process, we provide complex equipment, satisfy high demands on gas purity, obtain synthesis gas and spend a lot of energy to purify it, It is necessary to have a significant number of intermittent steps.
Furthermore, it is not efficient for medium and small businesses with a capacity of less than 2000 t / day.

  A device close to the present invention is disclosed in Russian Patent 2,162,460. It includes a source of hydrocarbon-containing gas, a compressor and heater for compressing and heating the gas, and a source of oxygen-containing gas having a compressor. It further comprises a continuously arranged reactor having alternating mixing zones and reaction zones and means for supplying hydrocarbon-containing gas to the first mixing zone of the reactor, supplying oxygen-containing gas to each mixing zone Means for cooling, having a heat transfer heat exchanger for cooling the reaction mixture, cooled through the wall by a flow of cold hydrocarbon-containing gas of heated hydrocarbon-containing gas entering the heater, a cooling condenser; A partial condenser for the separation of liquid product and waste gas and subsequent methanol, and a pipeline for the supply of waste oxygen-containing product into the first mixing zone of the reactor.

In this device, however, due to the inherent limitations of heat exchangers, it is not possible to provide fast removal of heat from the highly exothermic reaction of hydrocarbon-containing gas oxidation. This leads to the need to reduce the amount of hydrocarbon-containing gas supplied. And it reduces the degree of conversion of the hydrocarbon-containing gas. Furthermore, even when oxygen is used as the oxidant, it is impossible to provide efficient recirculation of the hydrocarbon-containing gas due to the rapid increase in the concentration of carbon oxide inside. Significant portion of the supplied oxygen is consumed for oxidation of CO ₂ in the CO, which further reduces the degree of conversion of the first hydrocarbon-containing gas, to provide additional heating of the reaction mixture. The apparatus further requires an additional amount of combustion of the initial hydrocarbon-containing gas to provide a process for rectifying the liquid product with steam. As each gas reactor cools the gas-liquid mixture for separation of the liquid product and heats it before the next reactor, the apparatus is inherently complex, increasing the number of units and adding Energy is wasted.

  A further method and apparatus for producing methanol is disclosed in Russian Patent 2,200,731. Here, a compressed and heated hydrocarbon-containing gas and a compressed oxygen-containing gas are introduced into the mixing zone of a continuously arranged reactor and the heat pickup controlled by cooling the reaction mixture with water condensate The reaction is carried out with steam and steam is obtained, and the degree of cooling of the reaction mixture is regulated by the parameters of the lost steam. Lost steam is used in the liquid product rectification process.

For example, U.S. Pat. Nos. 2,196,188; 2,722,553; 4,152,407; 4,243,613; 4,530,826; 5,177,279; 5,959,168 and International Publication WO 96 /. Other documents such as 06901 show further solutions for the conversion of hydrocarbons.
It is believed that existing methanol production methods and equipment can be further improved.

  It is an object of the present invention to provide a method and apparatus for producing methanol that further improves existing methods and apparatuses.

  Another aspect of the present disclosure is a method and apparatus for producing methanol, which can be used with minimal processing of gas and condensate deposits, and for all gas customers such as powder plants, gas distributors, gas reducing. Provide equipment that can be used by stations, chemical production facilities, etc., or small methane producers (ie coal mines, oil production (flares), landfills, farms)

  To achieve these objectives and the objectives that will become apparent from the following description, one aspect of the present invention, in brief, is a process for producing methanol comprising supplying a hydrocarbon-containing gas stream to a reactor, Supplying oxygen-containing gas to the reactor; oxidizing the hydrocarbon-containing gas in the reactor with oxygen of the oxygen-containing gas; and after removing impurities and products from the reaction system, It relates to a process comprising the step of recycling the hydrocarbon gas of the reaction to a hydrocarbon-containing gas stream for further reaction.

Another aspect of the present invention is an apparatus for producing methanol, a reactor for receiving and reacting hydrocarbon-containing gas and oxygen-containing gas from a well or other source, oxygen in the oxygen-containing gas It is related with the apparatus containing the reactor which oxidizes the hydrocarbon containing gas heated by.
The apparatus of the present invention further supplies a non-oxidizing coolant to the reactor at a later stage of the reaction to inhibit oxidation and decomposition of formaldehyde so that the heated hydrocarbon-containing gas and the oxygen-containing gas. And a mechanism for direct mixing with the mixture. Unreacted hydrocarbon-containing gas is then recovered and recycled into the hydrocarbon-containing gas stream with product and impurities recovered. Reaction by-products such as CO ₂ can be injected into the ground at a predetermined distance from the well to increase the production of the well.

In accordance with the teachings of the present invention, a heated hydrocarbon-containing gas stream and an oxygen-containing gas are fed into a reaction zone or reactor, and gas phase oxidation of the hydrocarbon-containing gas takes place in the reaction zone at elevated temperature and pressure. It is. The reaction mixture is cooled and separated into waste gas and liquid product. The waste gas is scrubbed to remove formaldehyde and CO ₂ and returned to the heated hydrocarbon-containing gas stream. The cold hydrocarbon-containing gas is fed to the reactor's regulatory zone to reduce the temperature of the hydrocarbon-containing gas, thereby providing a product redistribution ratio and producing corresponding amounts of methanol and formaldehyde. The produced methanol can then be injected into a natural gas stream to reduce hydroxide formation in the pipeline.

In accordance with the teachings of the present invention, during the cooling of the reaction mixture in a partial condenser, heat is transferred to the feed stream supplied to the formaldehyde rectification column for rectification of formaldehyde and simultaneously regeneration of the main scrubber solvent, methanol. It is done. Within the partial condenser, the dry gas is separated from the crude liquid containing methanol, ethanol and water. The crude liquid is fed to the rectification column through a flash drum. The temperature at the top of the column is between about 70 and about 75 ° C. and the pressure in the column is for example up to 0.2 MPa. The final product is supplied for storage or further processing. The dry gas is scrubbed to remove CO ₂ and formaldehyde and then returned to the reactor in the hydrocarbon input stream. CO ₂ can be injected into the ground at a predetermined distance from the well to increase well production

  The novel aspects that are considered characteristic of the invention are set forth with particularity in the claims. The invention itself will be understood from the following specific examples and drawings for both its construction and method of operation, as well as additional objects and their effects.

BRIEF DESCRIPTION OF THE DRAWINGS FIGS. 1A and 1B show a system of an apparatus for producing methanol of the present invention;
Figures 2 and 3 show the oxygen, formaldehyde and methanol concentrations during the reaction of the prior art and the invention, respectively;
FIG. 4 is a graph showing the oxygenate yield of the system as a function of the recycle rate.
FIG. 5 represents a methane to methanol plant of different embodiments of the present invention;
FIG. 6 shows the optional oxygen production plant shown in FIG. 5;
FIG. 7 shows the gas processing part of the plant shown in FIG. 5;
FIG. 8 shows the liquid processing portion of the plant shown in FIG.

DESCRIPTION OF THE PREFERRED EMBODIMENTS The apparatus for producing methanol of the present invention has a reactor 100 that facilitates gas phase oxidation of hydrocarbon-containing gases, as shown in FIGS. 1A and 1B. FIG. 1B details the reactor inputs and outputs. The reactor 100 has a reaction zone 102 having a device 104 for introducing a heated hydrocarbon-containing gas stream and a device 105 for introducing an oxygen-containing gas. As described in detail below, the oxygen-containing gas preferably has an oxygen content greater than 80% to reduce the accumulation of inert gas due to the recycling process.

  The reactor 100 further has a regulation zone 108, which is optionally provided with a device 110 for introducing a cold hydrocarbon-containing gas stream to reduce the reaction temperature during operation of the apparatus. . In addition, the reactor 100 is provided with a thermal pocket 112 for temperature control and regulation in the corresponding zone, eg provided with a thermocouple.

The apparatus has a device 114 for cooling the reaction mixture prior to separation. In addition, the partial condenser 122 has a gas-liquid heat exchanger to further reduce the product temperature. The condenser 122 separates H ₂ O and alcohol from the hydrocarbon-CO ₂ mixture. The partial condenser 122 is preferably isobaric rather than isothermal and avoids pressure loss. As the product stream enters, the liquid and gas streams exit the condenser 122.

Block 139 represents the equipment formed to separate impurities and products from recycle gas components containing hydrocarbons. From this point, the device 139 is formed to remove CO ₂ from the product stream. The instrument 139 can be used with, for example, a purge valve to regulate the percentage of other non-reactive components such as N ₂ .

When the system is configured to recover formaldehyde, the gaseous product stream passes through the isobaric condenser 122 and through the scrubber 134. Another potential method that can be used is the use of various amine-like materials known to remove CO ₂ and formaldehyde.

  To meet the minimum requirements for absorption, the methanol flow rate can be changed or the scrubber column operating temperature can be changed. For example, if it is desired to operate at a very low absorbent flow rate, a low temperature, such as 0 ° C., can be utilized. If it is desired to operate at ambient temperature or a temperature achieved by cooling water, a high flow rate, for example 10 times the flow rate at 0 ° C., can be used. In one scenario, the full methanol absorbent stream 14 is completely regenerated by the formaldehyde distillation column 138. Optionally, stream 14 from scrubber 134 can pass through condenser 122 to cool the product stream and preheat recycled methanol, improving the energy efficiency of formaldehyde distillation column 138.

The reactor 100 is connected to a compressor 124 and a heater 126 to supply a compressed and heated oxygen-containing gas. The feed hydrocarbon containing gas is mixed with the cleaned hydrocarbon gas from the scrubber 134 and heated using a heater 136. If the feed hydrocarbon has a high CO ₂ content, the feed hydrocarbon enters the reactor after mixing it with the return product hydrocarbon stream after removal of impurity gases from the condenser 122 into the scrubber 134. I can enter.

  The apparatus further comprises a unit for methanol rectification, which includes a flash drum 132, a rectification column 128 and a vessel 130, from which methanol is supplied for 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). As before, it is desirable that some of the heavy key components enter the distillate stream (as directed by the commercial specifications for formalin). For methanol rectification, over 99% or typically 99.999% can be achieved with multiple columns. Stream 4 enters the column and distillate stream 5 and bottom stream 8 exit the column in the liquid phase. Stream 8 contains some amount of ethanol (and possibly methanol if ultrapure methanol is produced) and is used as the basis for the aqueous make-up of the commercial formalin stream (11). In this way, some of the ethanol is recovered before the remainder is discarded into the liquid waste stream.

A flash drum 132 for the recovery of CO ₂ and formaldehyde from the liquid product stream is disposed between the column 128 and the condenser 122. The purpose of the flash drum 132 is to drop the pressure to an appropriate level before entering the methanol rectification column 128 to remove substantially all dissolved gases, typically CO ₂ and formaldehyde, from the liquid product stream. It is to be.

For example, a feed hydrocarbon-containing gas stream with a methane content of up to 98% and a return hydrocarbon product stream are fed to a heater 136 from a gas production unit or other source and heated to 430-470 ° C. therein Is done. Thereafter, the heated hydrocarbon-containing gas is supplied to the reaction zone 102 of the reactor 100. For example, compressed air supplied by a compressor 124 pressurized to 7-8 MPa and having 80-100%, preferably 90-95% oxygen, is also supplied to the reaction zone 102 of the reactor 100. The oxidation reaction takes place in the reaction zone 102 of the reactor 100. 2-3% O ₂ of the total volume of the reactants are reacted with the heated hydrocarbon-containing gas stream as described above. In order to limit the amount of N ₂ in the system, for example to less than 30-40%, or to reduce the required size of the purge stream to achieve similar results, the O ₂ stream is preferably substantially It is pure and thus limits the amount of N ₂ entering the system.

  An optional second stream of cold hydrocarbon-containing gas or, in other words, hydrocarbon-containing gas that is cooler than the gas in the reactor, is fed through device 108 to the regulation zone of reactor 100. This flow is regulated by the adjusting device 120. It can be formed as a known gas supply regulator, regulator valve or the like. This cold stream can consist of a feed hydrocarbon stream, a recycled stream, or a part or combination of the two. The regulator is configured to adjust the volume or pressure of the cold hydrocarbon-containing gas based on system parameters such as pressure in the system, temperature, proportion of reaction products downstream in the system, and the like.

  The coolant supplied from the coolant source functions to reduce the temperature of the partially oxidized methane and reduce the continued oxidation or decomposition of formaldehyde. The coolant can be any material that can be easily separated from the reaction product stream. For example, as described in more detail below, the coolant can be an unheated hydrocarbon or methane-containing gas stream.

Preferably, the coolant can be any non-oxidizing material that can be easily separated from the reaction product. In this regard, the cooling agent can be, for example, CO _2, formaldehyde, methanol, or atomized liquid or vapor is an aerosol of water. The coolant can also be a mixture of recycled reaction products, water, steam and / or feed hydrocarbon gas.

If it is desired to produce methanol exclusively, depending on the intended operating mode of the device, and in particular on the intended methanol or methanol and formaldehyde production, the reaction mixture can be used for the introduction of cold hydrocarbon-containing gas. The reaction is not carried out in a reactor. If it is desired to produce methanol and formaldehyde, the introduction of a cold hydrocarbon-containing gas is used. With the introduction of the cold hydrocarbon-containing gas, the temperature of the reaction is reduced by 30-90 ° C., maintaining the formaldehyde content in the separated mixture by reducing the decomposition of formaldehyde to CO ₂ .

  The reaction mixture is fed to heat exchanger 114 for heat transfer from the reaction mixture exiting the reactor to the reactor input stream. Thereafter, it is further cooled in the partial condenser 122. Separation of the mixture into highly volatile and less volatile components (dry gas and unpurified liquid, respectively) takes place in partial condenser 122, optionally with at least some formaldehyde into the unpurified liquid stream. Absorb. The drying gas is transferred to the scrubber 134, and the unpurified liquid from the condenser 122 is supplied to the flash drum 132.

The scrubber 134 functions to remove CO ₂ and formaldehyde from the dry gas stream. In this regard, the scrubber 134 uses both H ₂ O and methanol and is at a pressure of 7-8 MPa and a temperature of about 0 ° C. to about 50 ° C. to absorb CO ₂ and formaldehyde. Once the CO ₂ and formaldehyde are recovered, the hydrocarbon gas stream is recycled by mixing the return stream and the feed hydrocarbon-containing gas stream, if desired, before or in the reactor. The feed hydrocarbon and return streams are introduced separately or in combination and then into the reaction chamber 100 from the inlet 104 or inlet 110 after being heated by the heat exchanger 116 and heater 136 as described above.

  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). A full methanol stream 14 enters the rectification column and is separated into a formaldehyde distillate stream 16 and a bottoms stream, stream 15. Because methanol is used as a stabilizer in the production of commercial grade formalin (6-15% alcohol stabilizer, 37% formaldehyde, and balance water), some amount of methanol in the distillate stream Is desirable. Separation is more easily achieved by flowing a portion of the heavy key component into the distillate stream; in addition, the process loss typically experienced during sorbent regeneration is the methanol in the distillate. Is used in formalin production and is consequently invalidated. Stream 15 is supplemented with stream 31 to replace any methanol transferred to distillate stream stream 16. Stream 31 and stream 15 are combined into stream 17 and then returned to scrubber 134 as regenerated methanol absorbent. Meanwhile, formaldehyde distillate stream 16 is combined with vapor stream 7 from flash drum 132 to form a mixture of formaldehyde, methanol and carbon dioxide.

Formaldehyde, water, methanol and CO ₂ recovered by the scrubber 134 are passed to the formaldehyde rectification column 138. Column 138 recovers formaldehyde and CO ₂ from the methanol-water stream. A small amount of methanol is combined with the methanol produced and enters the scrubber 134 to recover additional amounts of CO ₂ and formaldehyde from the 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 crude liquid contains methanol, ethanol and water by allowing formaldehyde to remain in the gas stream. In this case, the liquid stream exiting the isobaric condenser 122 avoids the formaldehyde rectification portion of the process and can optionally enter the methanol rectification column after passing through the flash drum 132.

  2 and 3 are diagrams showing the concentrations of oxygen, formaldehyde, and methanol in the reaction system when there is no cooling and when there is no cooling, respectively.

  As can be seen from FIG. 2, oxygen burns completely after approximately 2 seconds. At this moment, the reaction temperature reaches its maximum. At this moment, the reaction temperature reaches its maximum. In the reaction mixture, methanol and formaldehyde are produced in respective proportions. Methanol as a more stable product at the end of the reaction reaches its maximum concentration and in fact remains stable. Formaldehyde is not very stable. Therefore, as the temperature rises (the temperature increases until the oxygen is completely combusted), its concentration decreases somewhat.

  In the reaction with cooling shown in FIG. 3, cold gas is introduced when the formation of methanol and formaldehyde is completed, the temperature of the final period of the reaction is reduced, and as a result, decomposition of formaldehyde is prohibited.

FIG. 4 shows the oxygenate yield of the system as a function of the recycled hydrocarbon gas recycle rate. A graph using Michigan Antrim gas containing 97% CH ₄ and 1% N ₂ is shown. In this regard, the graph shows a significant increase in product yield using the same input stream, a small increase in capital costs. As the system efficiently manages pressure and integrates process energy usage, energy requirements are minimized, thereby improving overall process economics.

  FIG. 5 shows a plant 150 from different methane to methanol. Plant 150 is arranged to process methane from gas and gas released from either oil field 152 or gas field 154. The plant 150, preferably located in the immediate vicinity of the wellbore, is generally made from a gas processing plant 156, a liquid processing plant 158, and an oxygen generation plant 160. Further, a wastewater treatment plant 162 and a utility plant 164 are provided in the plant 150.

  As shown in FIG. 6, any oxygen production plant 160 can be used to help regulate the partial oxidation of the hydrocarbon stream in the reactor 100. The oxygen generation plant 160 has a compressor 161 combined with a heat exchanger 163 and functions to prepare compressed oxygen for injection into a plurality of absorbers 165. After passing through the absorber, the generated oxygen stream is compressed and directly advanced to the reactor 100.

Referring to FIG. 7, the gas processing portion of plant 156 generally functions as described above (see FIGS. 1A and 1B). In this regard, the gas processing plant 156 has compressors 170 and 172 to increase the pressure of the clean input hydrocarbon stream 174. This stream 174 is then split and reacts with oxygen in the reactor 100 to partially oxidize methane as described above. Parameters such as reaction time and temperature and pressure within the reactor can be adjusted to selectively control the amount of CO ₂ , H ₂ O, formaldehyde and methanol produced in the reactor 100. Thereafter, the reaction product 176 from the reactor is transferred to a liquid processing plant 158.

As shown in FIG. 8, the liquid processing plant 158 generally functions as described above to separate methanol and formaldehyde from the reaction product stream 176. A distiller, blender and flash drum are shown used to separate the components of the reaction product stream as described in detail above. In particular, CO ₂ is removed from the reaction product stream, which is methanol and, if desired, formaldehyde. A scrubber 134 (see FIG. 5) prevents the accumulation of CO ₂ and allows physical capture of formaldehyde. In order to physically absorb formaldehyde and CO ₂ from the hydrocarbon gas recycle loop 135, the scrubber 134 utilizes a mixture of methanol and water. The efficiency of the scrubber 134 that can operate sufficiently without refrigeration is made possible by the high operating pressure of the recycle loop 135. This is in contrast to the cryogenic temperature utilized by conventional absorption methods. The gas enters the scrubber 134 as a “dirty” gas with a certain amount of formaldehyde and CO ₂ . These components are simply present in relatively low concentrations and therefore the methanol absorbent loading is relatively small.

As noted above, it is contemplated that the reactor output is selectively adjusted to minimize the amount of formaldehyde produced by the gas process portion of the plant 156. Although CO ₂ can be exhausted, it is also contemplated that CO ₂ from the reaction product will be injected into the ground a predetermined distance away from the well to increase the yield of the well. In this regard, it is contemplated that the CO ₂ is injected at any suitable distance from the well in order to allow an increase in underground pressure and increase the production of well gas or oil. Furthermore, CO ₂ can be injected into the opening of the well hole or in a region close to the opening to increase the output of the gas or gas and oil output well.

  Although illustrated as an onshore plant, it is also contemplated that the plant 100 is provided for offshore oilfield drilling rigs. In this regard, the plant 100 may be on an offshore drilling rig, or may be adjacent to an offshore drilling rig, eg, on a buoyant platform, at a predetermined short distance from the drilling rig. In the case of an offshore drilling rig (which produces natural gas), the methanol converted from the methane-containing hydrocarbon stream is injected into the second part of the methane-containing hydrocarbon stream and from the offshore well to land Improve the flow of the hydrocarbon stream. This methanol is injected to reduce the formation of hydrates in the piping. Thereafter, the methanol associated with the natural gas is removed from the stream containing hydrocarbons after the stream arrives at the shore.

Any other reaction product, ie CO ₂ , water or methanol, can be injected directly into the hydrocarbon-containing underground formation surrounding the platform or land well. In particular, methanol can be injected into the hydrate structure surrounding the well to increase the production of natural gas from the natural gas production well.

Returning to FIG. CO ₂ can be injected into one part of the well, while methanol or other reaction products can be injected into the other part of the well. If natural gas is left on the beach, or if there is more than 4% nitrogen, facilities may be provided to manage nitrogen build-up in the recycle loop. If the output of any particular well 152, 154 is low, a single plant 100 with a shortened process can be used. In these situations, only a portion of the apparatus and ancillary equipment associated with partial oxidation of a hydrocarbon stream, is used near the well in order to recover the CO _2.

The recovered CO ₂ can be collected and discharged or reinjected into the ground. Immediately after the collection of natural gas and associated CO ₂ by scrubber, the remaining liquid product, formaldehyde from waste effluent to another location from the well site for methanol and water separation can be transported in liquid form. In this regard, it is contemplated that the centralized liquid processing plant for completing the liquid processing treatment process (158) will be located at a location that is far from the remaining natural gas arrangement. This allows the use of a centralized liquid process facility 158. In addition, reactor conditions can be adjusted to produce a liquid phase containing commercial grade formalin.

  It is understood that each of the elements described above may find useful applications for other types of applications and may be combined in different ways and structures than the types described above two or more. Will be done. While the present invention has been illustrated as an embodiment of a method and apparatus for producing methanol, it is not limited to that disclosed, and various modifications and structural changes depart from the scope of the present invention. Can be done without.

Without further analysis, the above description very completely clarifies the gist of the present invention. By applying current knowledge, a third party can easily apply to various applications from the viewpoint of the prior art without omitting the features that properly constitute the general aspect of the present invention or the essential characteristics of a specific aspect. Can be adapted to. Inventions that are novel and seek protection as patents are set forth in the following claims.
The present invention includes the following embodiments.
Embodiment 1: A process for producing methanol comprising:
Converting the first methane-containing gas into methanol, CO ₂ , H ₂ O, ethanol, and formaldehyde using a partial oxidation reaction;
Separating CO ₂ from the reaction product;
Inject CO ₂ into the ground at a predetermined distance from the well to increase the yield of the well.
Embodiment 2: By adjusting the composition of the feed to the reactor and the process parameters to influence the selectivity of the reaction and adjusting the amount of CO ₂ , H ₂ O and formaldehyde produced, the first The process according to embodiment 1, wherein conversion of the methane-containing gas of methane is carried out.
Embodiment 3: Converting methane gas to methanol provides an oxygen-containing gas;
Providing a first methane-containing gas; reacting an oxygen-containing gas with the methane-containing gas to form a reaction product stream; and mixing a coolant directly with the reaction product stream to reduce the degree of oxidation of formaldehyde. The method of embodiment 1, comprising adjusting and thereby increasing the ratio of CO ₂ and H ₂ O to formaldehyde.
Embodiment 4: The method of embodiment 4, wherein mixing the direct coolant comprises mixing the second methane-containing gas directly into the reaction product stream.
Embodiment 5: The method of embodiment 5, wherein at least some of the first and second methane-containing gas streams are obtained from a well.
Embodiment 6: The method of embodiment 5, wherein the first and second methane-containing gas streams are obtained from a well.
Embodiment 7: A process for producing methanol comprising:
Partially oxidizing the hydrocarbon gas-containing stream to form a reaction product stream comprising CO ₂ ;
Separating CO ₂ from the reaction product stream; and injecting CO ₂ into the ground within a predetermined distance from the well.
Embodiment 8: A method according to embodiment 7, wherein the hydrocarbon stream comprises methane.
Embodiment 9: The method of embodiment 7, wherein the partial oxidation of the hydrocarbon gas comprises reacting the methane containing stream with the oxygen containing stream to form a reaction product stream.
Embodiment 10: The method of embodiment 9, further comprising injecting a second hydrocarbon gas from the reaction product stream to regulate the reaction product.
Embodiment 11: A process according to embodiment 10, wherein the reaction product stream comprises methanol, formaldehyde, H ₂ O and CO ₂ .
Embodiment 12: The method of embodiment 11, further comprising reacting the reaction stream to convert formaldehyde to CO ₂ and H ₂ O.
Embodiment 13: A method of transporting hydrocarbon gas from an offshore platform, comprising:
Converting a portion of the methane-containing gas from the hydrocarbon gas-containing stream to methanol, CO ₂ , H ₂ O, ethanol and formaldehyde;
Separating methanol from the reaction product;
Injecting methanol into the methane-containing gas stream; and separating CO ₂ from the reaction product.
Embodiment 14: The method of embodiment 13, further comprising injecting CO ₂ into the ground at a predetermined distance from the well to increase the yield of the well.
Embodiment 15: A process according to embodiment 13, wherein in the conversion of the methane-containing gas, the amount of CO ₂ , H ₂ O and formaldehyde produced in the partial oxidation reactor is controlled.
Embodiment 16: Conversion of the methane-containing gas comprises partially oxidizing the methane stream using a plurality of reactors, increasing the conversion of methane to methanol per pass, and further adding CO ₂ and H to _{2 O} to oxidize the formaldehyde product, embodiment 13, the method described.
Embodiment 17: Converting methane gas to methanol comprises
Providing an oxygen-containing gas;
Providing a first methane-containing gas; reacting the oxygen-containing gas and the methane-containing gas to form a reaction product stream; and directly mixing the coolant and the reaction product stream to form CO ₂ and H for formaldehyde. further comprising, embodiment 13, the method according to adjust the ratio of _{2 O.}
Embodiment 18: The method of embodiment 17, wherein mixing the gas directly comprises mixing the second methane-containing gas directly into the reaction product stream.
Embodiment 19: The method of embodiment 5, wherein the first and second methane-containing gas streams are obtained from a well.
Embodiment 20: A process for producing methanol comprising:
Partially oxidizing the hydrocarbon gas-containing stream to form a reaction product stream comprising methanol and CO ₂ ;
Separating CO ₂ from the reaction product stream; and injecting CO ₂ into the ground within a predetermined distance from the well.
Embodiment 21: The method of embodiment 20, wherein the hydrocarbon stream comprises methane and greater than 4% nitrogen.
Embodiment 22: Partially oxidizing hydrocarbon gas reacts a methane-containing stream with an oxygen-containing stream to form a reaction product stream in a plurality of reactors and minimizes the formation of formaldehyde. Embodiment 22. The method of embodiment 21, wherein the method is 5% or less.
Embodiment 23: The method of embodiment 22, further comprising injecting a second gas from the reaction product stream to regulate the reaction product.
Embodiment 24: A method according to embodiment 23, wherein the reaction product stream comprises methanol, formaldehyde, H ₂ O, ethanol and CO ₂ .
Embodiment 25: The method of embodiment 24, further comprising reacting the reactant stream to convert formaldehyde to CO ₂ and H ₂ O.
Embodiment 26: A method of transporting a methane-containing hydrocarbon stream from an offshore hydrocarbon production well comprising:
Converting methane from a first portion of the methane-containing hydrocarbon stream to methanol and reaction products within a predetermined first distance from the well;
Separating methanol from the reaction product; and injecting methanol into the second portion of the methane-containing hydrocarbon stream.
Embodiment 27: further comprising, embodiments 26 The method according to separate the CO ₂ from the reaction product.
Embodiment 28: The method of embodiment 27, further comprising injecting CO ₂ at a predetermined second distance from the offshore hydrocarbon production well.
Embodiment 29: A method according to embodiment 26, wherein the reaction product comprises H ₂ O, ethanol and formaldehyde.
Embodiment 30: separating H ₂ O from the reaction stream and injecting at least one of CO ₂ and H ₂ O into the ground at a third predetermined distance from the offshore hydrocarbon production well. 30. The method of embodiment 29, further comprising:
Embodiment 31: The method of embodiment 27, further comprising injecting CO ₂ into a well casing of an offshore hydrocarbon production well.
Embodiment 32: Converting the methane-containing hydrocarbon stream to methanol provides an oxygen-containing gas;
Providing a first methane-containing gas, reacting the oxygen-containing gas and the methane-containing gas to form a reaction product stream, and mixing the coolant directly with the reaction product stream in the reactor to formaldehyde 27. The method of embodiment 26, wherein the degree of oxidation of is adjusted, thereby increasing the ratio of CO ₂ and H ₂ O to formaldehyde.
Embodiment 33: The method of embodiment 32, wherein the direct mixing of the coolant comprises mixing the second methane-containing gas stream directly into the reaction product stream.
Embodiment 34: The method of embodiment 33, wherein the first and second methane-containing gas streams are obtained from offshore hydrocarbon production wells.
Embodiment 35: A process for producing methanol comprising:
Partially oxidizing a first portion of a hydrocarbon gas-containing stream from an offshore hydrocarbon production well at a first offshore location to form a reaction product stream comprising CO ₂ and methanol;
Separating CO ₂ from the reaction product stream;
Injecting CO ₂ into the ground within a predetermined distance from the well; and injecting methanol into the second portion of the hydrocarbon gas stream at a second offshore location.
Embodiment 36: The embodiment 35, wherein the partial oxidation of the first portion of the hydrocarbon gas-containing stream comprises reacting the methane-containing gas stream with the oxygen-containing stream to form a reaction product stream. Method.
Embodiment 37: The method of embodiment 36, further comprising injecting coolant directly into the reaction product stream to regulate the reaction products in the reaction product stream.
Embodiment 38: The method of embodiment 35, further comprising regulating the amount of nitrogen in the first portion of the hydrocarbon gas-containing stream.
Embodiment 39: A method according to embodiment 35, further comprising injecting the reaction product in the vicinity of the well region.
Embodiment 40: A method according to embodiment 38, wherein the reaction product comprises methanol.
Embodiment 41: A process for producing methanol comprising:
Providing a hydrocarbon gas-containing stream;
Regulating the amount of nitrogen in the hydrocarbon-containing stream;
Partially oxidizing the first portion of the hydrocarbon-containing stream to form a reaction product comprising methanol and CO ₂ ;
Separating CO ₂ from the product stream; and injecting CO ₂ into the ground within a predetermined distance from the well.
Embodiment 42: The method of embodiment 41, further comprising removing from the hydrocarbon stream a hydrocarbon component having a molecular weight equal to or greater than propane prior to partial oxidation of the first portion.
Embodiment 43: A method according to embodiment 42, further comprising separating methanol from the reaction stream.
Embodiment 44: The method of embodiment 43, further comprising injecting methanol into at least one of the second portion of the well-containing or hydrocarbon-containing gas.
Embodiment 45: A method according to embodiment 42, wherein the regulation of the amount of nitrogen in the hydrocarbon-containing stream is to dilute the hydrocarbon-containing stream.

FIG. 1A shows a system of an apparatus for producing methanol of the present invention; FIG. 1B shows a system of an apparatus for producing methanol of the present invention; FIG. 2 shows the prior art oxygen, formaldehyde and methanol concentrations during the reaction; FIG. 3 shows the concentration of oxygen, formaldehyde and methanol during the reaction of the present invention; FIG. 4 is a graph showing the oxygenate yield of the system as a function of the recycle rate. FIG. 5 represents a methane to methanol plant of different embodiments of the present invention; FIG. 6 shows the optional oxygen production plant shown in FIG. 5; FIG. 7 shows the gas processing part of the plant shown in FIG. 5; FIG. 8 shows the liquid processing portion of the plant shown in FIG.

Claims (1)

Heating the hydrocarbon-containing gas and supplying the heated hydrocarbon-containing gas to the reactor;
Supplying oxygen-containing gas to the reactor;
Oxidizing the hydrocarbon-containing gas heated by oxygen of the oxygen-containing gas in the reactor; and
A cold hydrocarbon-containing gas is fed into the reactor when the formation of methanol and formaldehyde is complete, reducing the temperature of the gas in the reactor by at least 30 ° C., thereby producing methanol and formaldehyde A method for producing methanol comprising providing a material flow comprising:
  CO from the reaction product ₂ And CO obtained ₂ Injecting into the ground at a predetermined distance from the well to increase the gas output of the well.

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