Abstract:
A process for the production of methanol comprises feeding an amount of a hydrocarbon feedstock and an amount of an oxygen feedstock and an optional carbon dioxide feedstock to a partial oxidation reactor and an optional reformer to produce a partial oxidation reactor effluent comprising hydrogen, carbon monoxide and carbon dioxide; electrolyzing water to produce hydrogen and oxygen and recovering at least a portion of the hydrogen to produce a hydrogen stream; adding an amount of a hydrogen feedstock, at least a portion of which is obtained from the hydrogen stream, to the partial oxidation reactor effluent to produce a synthesis gas stream having a predetermined ratio of hydrogen to carbon monoxide and optionally to carbon dioxide; subjecting the synthesis gas to methanol synthesis to produce a methanol product stream and a tail gas stream; separating the tail gas stream into at least two streams comprising a purge stream and a recycle stream, the recycle stream comprising a substantial portion of the tail gas stream; and, recycling the recycle stream to the partial oxidation reactor.

Description:
FIELD OF THE INVENTION  
         [0001]    This invention relates to a method of methanol production having reduced emission of carbon dioxide.  
         BACKGROUND OF THE INVENTION  
         [0002]    Methanol is a synthetic fuel which is produced from reactants which provide carbon, hydrogen and oxygen. There are various sources of each of these molecules. For example, the requisite carbon may be obtained from coal (see for example U.S. Pat. No. 4,476,249 Avery), natural gas (see for example U.S. Pat. No. 5,496,589 Fong et al.) and heavy hydrocarbons such as pitch and atmospheric and vacuum residues (see for example Canadian Patent Application No. 2,060,108 Naber). Similarly, the oxygen and hydrogen which are combined with the carbon during the synthesis step to form methanol may be obtained from various sources. These include electrolysis, as well as the water gas shift reaction. For example, Avery and U.S. Pat. No. 5,416,245 (McGregor et al.) disclosed the use of electrolysis to provide hydrogen and oxygen. In the case of Avery, the oxygen is added together with steam to a gasifier to produce carbon monoxide and hydrogen for synthesis (column 4, lines 46-50).  
           [0003]    Methanol is advantageous as a substitute fuel for gasoline as well as diesel fuel since it is a cleaner burning fuel (i.e. the fuel is converted to carbon dioxide and water with fewer by-products being produced). The reduced emissions associated with methanol will not favor its production unless methanol can be produced in a cost effective manner. In the retail marketplace, methanol must be priced competitively with gasoline and diesel fuel to be a commercial alternative fuel.  
           [0004]    The advantage of methanol being a low polluting fuel will be reduced, or potentially lost, if the process for producing methanol has substantial emissions of greenhouse gases. Typical commercial processes which are in operation to date produce about 600 to 1200 pounds of carbon dioxide per ton of methanol produced. Therefore, while the methanol produced by these processes may be relatively non-polluting compared to gasoline and diesel fuel when it is combusted, when considered with the manufacturing process, the production and use of methanol may in fact be a substantial source of greenhouse gases.  
         SUMMARY OF THE INVENTION  
         [0005]    In accordance with the instant invention, a process for the production of methanol is provided which has a reduced emission of carbon dioxide as a by-product of the manufacturing process. In particular, in accordance with the instant invention, a process for the production of methanol may result in the emission of only 240 pounds of carbon dioxide per ton of methanol produced and, preferably, 120 pounds or less of carbon dioxide per ton of methanol produced. In one embodiment of the present invention, the process has a net consumption of CO 2 . For example, the process may consume up to about 650 pounds of CO 2  per ton of methanol produced.  
           [0006]    In accordance with one aspect of this invention, a partial oxidation reactor is utilized to produce the synthesis gas which is then subjected to methanol synthesis to produce methanol and a tail gas stream. The tail gas stream has unreacted synthesis gases (including carbon dioxide) therein. A purge stream is removed to prevent the build up of inert gases therein. The remainder of the stream, or essentially all of the remainder of the stream, is recycled to the partial oxidation reactor. In this way, carbon dioxide, as well as carbon monoxide and methane, may be recycled through the system essentially to extinction except for the purge stream. The amount of greenhouse gases emitted by the process effectively depends upon the relative size of the purge gas stream to the recycle stream. The larger of the recycle stream, the smaller the greenhouse gases that are emitted. The recycle stream may comprise up to 95 weight percent, and preferably from 50 to 95 weight percent of the tail gas stream, based on the weight of the tail gas stream.  
           [0007]    In order to reduce the size of the purge stream, the introduction of inert gases into the system is reduced. To this end, the oxygen which is used in the partial oxidation reactor preferably comprises essentially pure oxygen. In prior art processes, air or oxygen enriched air is utilized. This results in the introduction of substantial quantities of nitrogen. Not only does this result in the need to increase the size of the process equipment to have the same through put of methanol, but it also requires a larger purge stream and the consequential emission of additional greenhouse gases.  
           [0008]    Typically, methanol production processes utilize reformers to provide additional hydrogen to the synthesis gas to obtain the desired stoichiometric of hydrogen to Co and CO 2 . Reformers, such as steam reformers, require the introduction of substantial quantities of water into the process and may result in the production of additional carbon dioxide at the expense of carbon monoxide formation. However, in one embodiment of the instant invention, a reformer is used to consume hydrogen in the conversion of CO 2  to CO. This is the reverse of the current practice of operating a reformer. In accordance with another aspect of the instant invention, a hydrogen source other than reformers is utilized to adjust the hydrogen balance of the synthesis gas just ahead of the methanol reactor. Preferably, at least some of the hydrogen is obtained by electrolysis and more preferably essentially all of the hydrogen is obtained by electrolysis.  
           [0009]    In a further preferred aspect of the instant invention, at least some of the electricity which is utilized in operating the electrolysis step is obtained as off-peak or valley power from a power grid. Typically, the power demand of a power grid varies throughout the day with the power demand from the grid being reduced at night when commercial and residential requirements are reduced. Not only may off-peak or valley power be obtainable at a reduced rate compared to peak demand time, but, in addition, the use of valley power may result in more efficient operation of power generating plants. For example, if it is necessary to reduce the electrical output of a power generation plant, then the efficiency of the plant may be reduced. Alternately, it may not be possible to reduce the power output of a generating plant thus resulting in the emission of greenhouse gases to produce power which is not required. Therefore, the use of valley power to run at least a portion of the electrolysis step may be highly beneficial. In fact, the oxygen and hydrogen produced by electrolysis such as at night may be stored in storage tanks so as to ensure a continuous supply of hydrogen and oxygen. Thus, if there is a power shortage during a peak demand period (e.g. during the day) then a continuous supply of hydrogen and oxygen may be provided. In this way, the feed of raw materials to produce a synthesis gas may be leveled to ensure a uniform continuous supply. In a further alternate embodiment, the electricity may be generated by running a fuel cell in reverse (i.e. a fuel cell may be operated to utilize an energy source such as electricity to produce hydrogen and oxygen).  
           [0010]    Another advantage of the instant invention is that the amount of hydrogen which is produced may in fact exceed the amount of hydrogen required to produce the desired stoichiometric balance of the synthesis gas which is fed to the methanol synthesizer. Accordingly, the process may in fact also produce hydrogen as a valuable commercial product.  
           [0011]    Accordingly, in accordance with this invention there is provided a process for the production of methanol comprising:  
           [0012]    (a) feeding an amount of a hydrocarbon feedstock and an amount of an oxygen feedstock to a partial oxidation reactor to produce a partial oxidation reactor effluent comprising hydrogen, carbon monoxide and carbon dioxide;  
           [0013]    (b) electrolyzing water to produce hydrogen and oxygen and recovering at least a portion of the hydrogen to produce a hydrogen stream;  
           [0014]    (c) adding an amount of a hydrogen feedstock, at least a portion of which is obtained from the hydrogen stream, to the partial oxidation reactor effluent to produce a synthesis gas stream having a predetermined ratio of hydrogen to carbon monoxide;  
           [0015]    (d) subjecting the synthesis gas to methanol synthesis to produce a methanol product stream and a tail gas stream;  
           [0016]    (e) separating the tail gas stream into at least two streams comprising a purge stream and a recycle stream, the recycle stream comprising a substantial portion of the tail gas stream; and,  
           [0017]    (f) recycling the recycle stream to the partial oxidation reactor.  
           [0018]    In one embodiment, the process further comprises reforming the partial oxidation reactor effluent prior to the hydrogen addition step to convert at least some of the carbon dioxide to carbon monoxide. Optionally, a carbon dioxide feed stream may be provided.  
           [0019]    In another embodiment, the process further comprises the step of recovering at least a portion of the oxygen produced by electrolyzing water to produce at least a portion of the oxygen feedstock.  
           [0020]    In another embodiment, the process further comprises the step of adjusting the amount of the oxygen feedstock to the amount of the hydrocarbon feedstock fed to the partial oxidation reactor such that the partial oxidation reactor effluent contains some unoxidized hydrocarbon feedstock. The partial oxidation reactor effluent may contain up to about 10 wt % of the unoxidized hydrocarbon feedstock based on the weight of the partial oxidation reactor effluent and, preferably, the partial oxidation reactor effluent contains less than about 4 wt % of the unoxidized hydrocarbon feedstock based on the weight of the partial oxidation reactor effluent.  
           [0021]    In another embodiment, the process further comprises the step of adjusting the amount of the oxygen feedstock to the amount of the hydrocarbon feedstock fed to the partial oxidation reactor such that the synthesis gas which is subjected to methanol synthesis is essentially free of oxygen.  
           [0022]    In another embodiment, the synthesis gas which is subjected to methanol synthesis has a ratio of hydrogen minus carbon dioxide mole fraction to carbon dioxide plus carbon monoxide mole fraction of from about 1:1 to about 3:1.  
           [0023]    In another embodiment, the synthesis gas, which is subjected to methanol synthesis has a ratio of hydrogen minus carbon dioxide mole fraction to carbon dioxide plus carbon monoxide mole fraction is about 2:1.  
           [0024]    In another embodiment, the tail gas stream contains nitrogen and the method further comprises separating at least a portion of the nitrogen from the waste gas stream such that the purge stream is nitrogen rich and the recycle stream is a nitrogen reduced waste gas stream.  
           [0025]    In another embodiment, a membrane separator is used to separate the tail gas into the nitrogen reduced waste gas stream and the nitrogen rich purge stream.  
           [0026]    In another embodiment, the process further comprises combusting the nitrogen rich purge stream to produce energy.  
           [0027]    In another embodiment, the combustion of the purge stream produces heat that is used to preheat at least one of the feedstocks of the partial oxidation reactor.  
           [0028]    In another embodiment, the combustion of the purge stream produces electricity that is preferably used to electrolyze water.  
           [0029]    In another embodiment, the partial oxidation reactor produces waste heat and the waste heat is used to generate electricity.  
           [0030]    In another embodiment, the electrolysis is conducted by running a fuel cell in reverse.  
           [0031]    In another embodiment, essentially all of the hydrogen and the oxygen is obtained by electrolysis.  
           [0032]    In another embodiment, at least a portion of electricity used to electrolyze the water is valley power.  
           [0033]    In accordance with another aspect of the instant invention, there is provided a process for the production of methanol comprising:  
           [0034]    (a) feeding an amount of a hydrocarbon feedstock and an amount of an oxygen feedstock to a partial oxidation reactor to produce a partial oxidation reactor effluent comprising hydrogen, carbon monoxide and carbon dioxide;  
           [0035]    (b) adding an amount of a hydrogen feedstock to the partial oxidation reactor effluent to produce a synthesis gas stream having a predetermined ratio of hydrogen to carbon monoxide; and,  
           [0036]    (c) subjecting the synthesis gas to methanol synthesis to produce a methanol product stream and a tail gas stream wherein reformation is not used to provide hydrogen as a product.  
           [0037]    In one embodiment, the process further comprises the step of recycling a portion of the tail gas stream to the partial oxidation reactor.  
           [0038]    In another embodiment, the process further comprising the step of withdrawing a purge stream from the tail gas stream and recycling essentially the remainder of the tail gas stream to the partial oxidation reactor.  
           [0039]    In accordance with another aspect of the instant invention, there is provided a process for the production of methanol comprising:  
           [0040]    (a) feeding a hydrocarbon feedstock to a partial oxidation reactor to produce a synthesis gas comprising hydrogen, carbon monoxide and carbon dioxide;  
           [0041]    (b) subjecting the synthesis gas to methanol synthesis to produce a methanol product stream and a tail gas stream;  
           [0042]    (c) separating the tail gas stream into at least two streams comprising a purge stream and a recycle stream, the recycle stream comprising a substantial portion of the tail gas stream; and,  
           [0043]    (d) recycling the recycle stream to the partial oxidation reactor.  
           [0044]    In another embodiment, the tail gas stream contains nitrogen and step (c) comprises subjecting the tail gas stream to a separation process such that the recycle stream is nitrogen reduced and the purge stream is nitrogen rich.  
           [0045]    In accordance with another aspect of the instant invention, a process for the production of methanol comprising:  
           [0046]    (a) electrolyzing water to produce hydrogen and oxygen and recovering at least some of the hydrogen to produce a hydrogen stream and recovering at least some of the oxygen to produce an oxygen stream;  
           [0047]    (b) feeding an amount of a hydrocarbon feedstock and an amount of an oxygen feedstock, at least a portion of which is obtained from the oxygen stream, to a partial oxidation reactor to produce an effluent gas stream comprising hydrogen, carbon monoxide and carbon dioxide;  
           [0048]    (c) adding an amount of a hydrogen feedstock, at least a portion of which is obtained from the hydrogen stream, to the partial oxidation reactor effluent to produce a synthesis gas having a predetermined ratio of hydrogen to carbon monoxide;  
           [0049]    (d) subjecting the synthesis gas to methanol synthesis to produce a methanol product stream and a tail gas stream:  
           [0050]    (e) recycling a portion of the tail gas stream to the partial oxidation reactor; and,  
           [0051]    (f) combusting the purge stream to obtain energy wherein reformation is not used to provide hydrogen as a product.  
           [0052]    In one embodiment, the process further comprises combusting the nitrogen rich purge stream to produce energy.  
           [0053]    In another embodiment, the combustion of the purge stream produces heat that is used to preheat at least one of the feedstocks of the partial oxidation reactor.  
           [0054]    In another embodiment, the combustion of the purge stream produces electricity that is preferably used to electrolyze water.  
           [0055]    In another embodiment, the partial oxidation reactor produces waste heat and the waste heat is used to generate electricity.  
           [0056]    In another embodiment, the electrolysis is conducted by running a fuel cell in reverse.  
           [0057]    In accordance with another embodiment of the instant invention, a process for the production of methanol comprises:  
           [0058]    (a) feeding an amount of a hydrocarbon feedstock and an amount of an oxygen feedstock to a partial oxidation reactor to produce a partial oxidation reactor effluent comprising hydrogen, carbon monoxide and carbon dioxide;  
           [0059]    (b) electrolyzing water to produce hydrogen and oxygen and recovering at least a portion of the hydrogen to produce a hydrogen stream;  
           [0060]    (c) reacting carbon dioxide with hydrogen to produce carbon monoxide; and,  
           [0061]    (d) subjecting a methanol synthesis gas obtained from the partial oxidation reactor effluent, at least a portion of the hydrogen stream and carbon monoxide produced by step (c) to methanol synthesis to produce a methanol product stream and a tail gas stream.  
           [0062]    In one embodiment, the process as further comprises separating the tail gas stream into at least two streams comprising a purge stream and a recycle stream, the recycle stream comprising a substantial portion of the tail gas stream; and recycling the recycle stream to the partial oxidation reactor.  
           [0063]    In another embodiment, the partial oxidation reactor effluent is fed to a reformer to produce a reformed synthesis gas and at least a portion of the hydrogen stream is combined with the reformed synthesis gas to produce the methanol synthesis gas.  
           [0064]    In another embodiment, the process further comprises combining a carbon dioxide feedstock with the partial oxidation reactor effluent to produce a carbon dioxide rich synthesis gas stream and feeding the carbon dioxide rich synthesis gas stream to the reformer to produce a reformed synthesis gas.  
           [0065]    In another embodiment, at least a portion of the hydrogen stream is combined with the reformed synthesis gas to produce the methanol synthesis gas.  
           [0066]    In another embodiment, wherein at least a portion of the hydrogen stream is introduced to the reformer or a feedstream to the reformer. 
       
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS  
       [0067]    These and other advantages of the instant invention may be more completely fully understood by means of the following description of the accompanying drawings of the preferred embodiments of the instant invention in which:  
         [0068]    [0068]FIG. 1 is a schematic drawing of a preferred embodiment of the instant invention;  
         [0069]    [0069]FIG. 2 is a schematic drawing of an alternate preferred embodiment in accordance with the instant invention;  
         [0070]    [0070]FIG. 3 is a schematic drawing of a further alternate preferred embodiment in accordance with the instant invention; and,  
         [0071]    [0071]FIG. 4 is a schematic drawing of a further alternate preferred embodiment in accordance with the instant invention. 
     
    
     DETAILED DESCRIPTION OF THE INVENTION  
       [0072]    As shown in FIG. 1, according to a preferred embodiment of the instant invention, the process comprises partial oxidation reactor  10  and methanol synthesis reactor  12 . Hydrocarbon feedstock  14  and oxygen feedstock  16  are fed to partial oxidation reactor  10  to produce synthesis gas  18 . Hydrogen feedstock  20  is combined with synthesis gas  18  to produce synthesis gas  22  wherein the stoichiometric balance has been adjusted. The adjusted synthesis gas  22  is fed to methanol synthesis reactor  12  to produce tail gas  24  and methanol  26 .  
         [0073]    In steam reformation processes, steam is added to a reformer. Further, the hydrocarbon feedstock fed to the stream reformer may be humidified (which provides a further source of water). Overall, the process gas streams contain substantial quantities of water and the methanol produced typically is treated such as by distillation to reduce the water content of the methanol. In accordance with one embodiment of the instant process a hydrogen gas stream which is relatively pure (e.g. more than about 97 weight percent hydrogen and more preferably more than about 99 weight percent hydrogen) is preferably utilized to adjust the chemical balance of the synthesis gas. In accordance with this embodiment, water need not be added to the process and is preferably not added to the process (except in so far as some quantities may be contained with the hydrocarbon feedstock such as may be contained for example in natural gas). Accordingly, the amount of water traveling through the process and accordingly exiting methanol synthesis reactor  12  is substantially reduced compared to steam reformation processes. Accordingly, methanol  26  may have a relatively low level of water.  
         [0074]    Methanol which contains as much as 10 weight percent water may be burned in convention combustion devices such as an internal combustion engine. In accordance with this embodiment of the instant invention, by avoiding the use of reformation in the process, methanol  26  (which is the product produced directly from methanol synthesis reactor  12  without distillation) may contain less than this amount of water and accordingly, may be a commercial product without further processing. More preferably, methanol stream  26  contains less than 6 weight percent water and, more preferably, less than about 2 weight percent water.  
         [0075]    Hydrocarbon feedstock  14  may be any gaseous or liquid hydrocarbon, is preferably a gaseous hydrocarbon and, more preferably comprises a substantial quantity of methane (e.g. more than 90 weight percent). In one particular embodiment, hydrocarbon feedstock  14  preferably comprises and, more preferably, consists essentially of natural gas or methane.  
         [0076]    As shown in FIG. 2, oxygen feedstock  16  may be obtained by electrolysis. In particular, water  32  is feed to electrolysis unit  28  to produce oxygen stream  32  and hydrogen stream  34 . Some or all of oxygen stream  32  may be fed directly to partial oxidation reactor  10  as oxygen stream  16  (as shown by the broken feed line shown in FIG. 2). Similarly, some or all of hydrogen stream  34  may be fed directly to synthesis gas  18  as hydrogen stream  20  (as shown by the broken feed line shown in FIG. 2). Preferably, storage tanks are utilized to produce a generally continuous flow of hydrogen and oxygen to streams  16  and  20 . To this end, one or more oxygen storage tanks  36  and one or more hydrogen storage tanks  38  may be provided.  
         [0077]    In operation, electricity for electrolysis unit  28  may be obtained from a power grid. During peak periods, when the cost of electricity is greater or, in some cases, when the requisite amount of electricity may not be available, the production of hydrogen and oxygen by electrolysis unit  28  may be reduced. In such cases, the amount of hydrogen and oxygen delivered to storage tanks  36  and  38  is reduced. However, depending upon the capacity of storage tanks  36  and  38 , the process may be supplied with hydrogen and oxygen via streams  42  and  40  at about the same rate regardless of the flow rate of hydrogen and oxygen into tanks  36  and  38  via streams  32  and  34 . In this way, tanks  36  and  38  may be utilized to produce a continuous flow of hydrogen and oxygen to the process.  
         [0078]    In another embodiment of the instant invention, electrolysis unit  28  may produce excess hydrogen and oxygen then are required for the operation of partial oxidation and methanol synthesis reactors  10  and  12 . In such cases, the excess amounts may be withdrawn as product oxygen stream  44  and/or product hydrogen stream  46 .  
         [0079]    In one embodiment, synthesis gas  22  has a ratio of hydrogen minus carbon dioxide mole fraction to carbon dioxide plus carbon monoxide mole fraction of from about 1.1 to about 3.1 and, preferably, the ratio is about 2.1. To achieve these ratios, particularly if hydrocarbon feedstock  14  substantially comprises or consists essentially of methane, a greater proportion of the oxygen produced by electrolysis unit  28  will be required then the hydrogen produced by electrolysis unit  28 . Accordingly, then in one embodiment of operation, electrolysis unit  28  may be operated to produce essentially the requisite amount of oxygen to produce this ratio resulting in essentially no product oxygen stream  44 . However, as less hydrogen will be required to produce the desired ratio, only a portion of the hydrogen produced by electrolysis unit  28  need be combined with synthesis gas  18  via stream  20 . Accordingly, the overall process will be a net producer of not only methanol but hydrogen as well via stream  46 .  
         [0080]    In accordance with another aspect of the instant invention, the process is preferably operated such that synthesis gas  22  essentially contains no oxygen (e.g. less than about 0.5 weight percent). If the oxygen content of the synthesis gas is too high, then oxygen will react with methanol in methanol synthesis reactor  12  to form carbon dioxide and water. To reduce the amount of oxygen in the synthesis gas, the amount of hydrocarbon feedstock  14  fed to partial oxidation reactor  10  is preferably adjusted, based upon the flow rate of oxygen stream  16  to partial oxidation reactor  10  such that the effluent from partial oxidation reactor  10  contains at least some unoxidized hydrocarbon feedstock. Preferably, the effluent contains from less than about 10 weight percent of the unoxidized hydrocarbon feedstock and, more preferably, less than about 4 weight percent of the unoxidized hydrocarbon feedstock, based on the weight of the effluent stream. At these levels, essentially all of the oxygen will be utilized in partial oxidation reactor  10 . It will be appreciated by those skilled in the art that the actual amount of unoxidized hydrocarbon which is required will vary in part depending upon the efficiency of partial oxidation reactor  10 .  
         [0081]    Referring to FIG. 3, in a further embodiment of the instant invention, tail gas stream  24  is subjected to gas separation unit  48  to produce tail gas recycle stream  50  and purge stream  52 . Preferably, gas separation unit  48  utilizes cryogenic separation or a membrane separator and, more preferably, a membrane separator. Purge stream  52  is utilized to remove inert material such as nitrogen, argon and the like. The inert material that is to be removed will vary depending upon the contaminants in the feedstocks. For example, if hydrocarbon feedstock stream  14  is natural gas, purge stream  52  is utilized to remove, for example, nitrogen that is present with the natural gas. The substantial portion of the tail gas is recycled as recycle stream  50 . In particular, recycle stream  50  may comprise up to about 95 weight percent and, more preferably from about 50 to about 95 weight percent of tail gas stream  24 . Accordingly, a substantial portion of a unreacted synthesis gas is recycled into the system. As shown in FIG. 3, recycle stream  50  is preferably combined with hydrocarbon feedstock stream  14  to produce blended hydrocarbon stream  54  which is then fed to partial oxidation reactor  10 . Alternately, recycle stream  50  may be fed directly to partial oxidation reactor  10 . In either case, the unreacted synthesis gases, which include carbon dioxide, is recycled through the partial oxidation reactor wherein some of the carbon dioxide may be converted to carbon monoxide which is then combined with hydrogen in the methanol synthesis reactor  12  to produce methanol.  
         [0082]    Purge stream  52  may be fed to a combustion unit  56 , such as a gas turbine, to produce power  58  and stack gases  60 . Power  58  may be in the form of mechanical power or electricity if combustion unit  56  is drivingly connected to a generator.  
         [0083]    Stack gases will be at an elevated temperature. Accordingly, excess heat from stack gases  60  may be recovered by means of heat exchanger  62 . For example, water  64  may be fed to heat exchanger  62  to indirectly heat the water to produce steam  66  and cooled stack gases  68 . In an alternate embodiment, shown in FIG. 1, purge gas  52  may be utilized to preheat a feedstock, e.g. hydrocarbon feedstock  14 . In such a case, purge stream  52  may be fed directly to indirect exchanger  62  or it may first be fed to combustion unit  56  to further increase the temperature of the purge stream prior to the heat exchange step.  
         [0084]    In a further alternate embodiment shown in FIG. 2, the excess heat generated by partial oxidation reactor  10  may be recovered to produce steam and, more preferably electricity. For example, referring to FIG. 2, partial oxidation reactor  10  may be provided with a jacket (e.g. a cooling jacket fed with water  72 ). The water is heated and thus moderates the temperature of partial oxidation reactor  10 . The water may be heated by its passage through jacket  70  to such an extent that it produces stream  74  which may be steam. Alternately, stream  74  may be superheated water which, upon passage though turbine  76  produces electricity  78  and water or wet steam  80 .  
         [0085]    In accordance with another embodiment of the instant invention, carbon dioxide in synthesis gas  18  and/or carbon dioxide from a feedstock  82  is converted to carbon monoxide to provide additional feed gas for conversion to methanol (see FIG. 4). Pursuant to this embodiment, reformer  86  is provided downstream from partial oxidation reactor  10 . Synthesis gas  18  is fed to reformer  86 . Conventionally, a reformer is operated to provide hydrogen as a product. In accordance with this embodiment, reformer  86  is operated to convert carbon dioxide to carbon monoxide by the overall reaction: 
         CO 2 +H 2 →CO+H 2 O 
         [0086]    Accordingly, hydrogen from one of the feedstocks is consumed by the process. As discussed previously, the instant process may be conducted to produce product hydrogen stream  46 . According to this embodiment, at least a portion of the product hydrogen stream could effectively be used by reformer  86 . In this way, the amount of product hydrogen stream  46  may be reduced or eliminated depending on the amount of hydrogen required for reformer  86 . By operating a reformer effectively in reverse, the product of the reformer (reformed synthesis gas stream  84 ) will contain water. Typically, reformer  86  will be operated at a pressure less than methanol synthesis reactor  12  and at a higher temperature. As the temperature of reformed synthesis gas stream  84  is reduced and the pressure is increased so that reformed synthesis gas stream  84  is suitable for feeding to methanol synthesis reactor  12 , water may be removed from reformed synthesis gas stream  84 .  
         [0087]    The carbon dioxide for reformer  86  may be supplied from synthesis stream  18 . Alternately, or in addition, a carbon dioxide feedstock stream  82  may be provided. Carbon dioxide feedstock stream  82  may be obtained from various sources and is preferably relatively pure since any contaminants will have to be purged from the system or will contaminate the methanol produced by the process. Carbon dioxide feedstock stream  82  may be obtained as excess carbon dioxide from a bottling plant or as exhaust gas produced by combustion. In the later case, the exhaust gas is preferably subjected to cleaning steps to remove undesirable contaminants. The carbon dioxide is preferably obtained as a by product of another process so that the instant process becomes effectively a temporary carbon sink to convert carbon dioxide, which would otherwise be released to the atmosphere, to a stored carbon source.  
         [0088]    Reformed synthesis gas stream  84  may be treated as discussed previously. Alternately, hydrogen may be added to the process upstream of reformer  86  (as shown by the dashed line in FIG. 4) or directly to reformer  84  (as shown by the dashed line in FIG. 4).  
         [0089]    It will be appreciated by those skilled in the art that each of the embodiments of the instant invention may be utilized individually or combined to produce an improved process for the production of methanol.