Patent Publication Number: US-8524175-B2

Title: Tandem reactor system having an injectively-mixed backmixing reaction chamber, tubular-reactor, and axially movable interface

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is a divisional of U.S. Pat. No. 7,879,296 issued Feb. 1, 2011 which is a continuation-in-part application of U.S. patent application Ser No. 11/526,824, filed Sep. 25, 2006, U.S. patent application Ser. No. 11/446,371, filed on Jun. 2, 2006, U.S. patent application Ser. No. 11/432,692, filed on May 11, 2006, and U.S. Pat. No. 7,642,293 B2, issued Jan. 5, 2010. U.S. patent application Ser. Nos. 11/526,824, 11/446,371, 11/432,692, and U.S. Pat. No. 7,642,293 B2 are continuation-in-part applications of U.S. patent application Ser. No. 11/319,093, filed on Dec. 27, 2005. The disclosures of the above applications are incorporated by reference in their entirety. 
    
    
     BACKGROUND OF THE INVENTION 
     The present invention relates to an apparatus for reacting two gaseous fluid streams (for example, without limitation, natural gas and oxidant under conditions to optimize the formation of desired alkyl oxygenates such as methanol). More specifically, the embodiments relate to a reactor system enabling individuated control of a primary free-radical induction sub-reaction separately from subsequent sub-reactions that respond to the induced free radicals. A focal area of application for such a reactor system relates to direct oxidation (under partial oxidation conditions) conversion of a C 1 -C 4  alkane and oxygen into an alkyl oxygenate, and, more particularly, of methane into methanol where an initial set of methyl free radicals are first generated that subsequently promote a substantial series of derived kinetic step sub-reactions. 
     The current industrial practice for methanol production is a two-step, Fischer-Tropsch type chemical process. The first step is the endothermic reforming of methane from natural gas to carbon monoxide and hydrogen, followed by a second step consisting of a solid-catalyzed reaction between carbon monoxide and hydrogen to form methanol. This technology is energy intensive and the process economics are unfavorable for all but very large scale methanol plants. 
     Various methods and apparatuses for the conversion of methane into methanol are known. It is known to carry out a vapor-phase conversion of methane into a synthesis gas (mixture of CO and H 2 ) with its subsequent catalytic conversion into methanol as disclosed, for example, in Karavaev M. M., Leonov B. E., et al “Technology of Synthetic Methanol”, Moscow, “Chemistry” 1984, pages 72-125. However, in order to realize this process it is necessary to provide complicated equipment, to satisfy high requirements for the purity of the gas, to spend high quantities of energy for obtaining the synthesis gas and for its purification, and to have a significant number of intermittent stages from the process. Also, for medium and small enterprises with the capacity of less than 2,000 tons/day it is not economically feasible. 
     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 gases 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. 
     In this apparatus, however, fast withdrawal of heat from the highly exothermic oxidation reaction of the hydrocarbon-containing gas in not achievable because of the inherent limitations of the heat exchanger. This leads to the need for reduction in the quantity of supplied hydrocarbon-containing gas and, further, it reduces the degree of conversion of the hydrocarbon-containing gas. Moreover, even with the use of oxygen as an oxidizer, it is not possible to provide an efficient recirculation of the hydrocarbon-containing gas due to the rapid increase of the concentration of carbon oxides. A significant part of the supplied oxygen is wasted for oxidation of CO into CO 2 , and thereby additionally reduces the degree of conversion of the initial hydrocarbon-containing gas to useful products and provides a further overheating of the reaction mixture. 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. 
     Other patent documents such as 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 96/06901 disclose further solutions for transformation of hydrocarbons. 
     There is also a need for a one step process that is also suitable for small-scale processing, overcoming process scale limitations of the Fischer Tropsch method, and also making “stranded gas” a valuable commodity. This approach makes use of a homogeneous, gas phase partial oxidation reaction, carried out by contacting natural gas and an oxidant, with the oxidant as the limiting reagent. The most abundant products are methanol and formaldehyde, coming from methane, the principal component of natural gas. Smaller amounts of ethanol and other oxygenated organic compounds are formed by oxidation of ethane, propane, and higher hydrocarbons that are all minor constituents of natural gas. These reaction products are all liquids, and are transportable to a central location for separation and/or subsequent use as fuels or as chemical intermediates. A central feature of such processes is that the process chemistry can be executed in the field at remote locations. 
     U.S. Pat. No. 4,618,732 (“Direct conversion of natural gas to methanol by controlled oxidation” to Gesser, et al.) describes a process for converting natural gas to methanol. The selectivity for methanol is indicated as resulting from careful premixing of methane and oxygen along with the use of glass-lined reactors to minimize interactions with the processing equipment during the reaction. The need for mixing prior to entering a reactor for reaction initiation is indicated in the following extract: 
     “The mixing of gases preferably takes place in a pre-mixing chamber or “cross” of relatively small volume and then pass through a short pre-reactor section before entering the heated reaction zone. However, when mixing gases at high pressure in a relatively small volume, laminar flow often takes place with the oxygen or air forming a narrow homogeneous stream within the general flow of natural gas. The oxygen or air has little chance of becoming dispersed throughout the reaction stream prior to reaching the reaction zone. Without wishing to be bound by theory, when this takes place it is postulated that the natural gas is oxidized initially to methanol which is further oxidized, at the periphery of the oxygen stream, i.e. in an oxygen-rich environment, to higher oxidation products.” 
     U.S. Pat. No. 4,618,732 to Gesser also emphasizes the need to keep the reaction from initiation until mixing is completed (—“mixing oxygen and natural gas prior to their introduction into a reactor”). 
     U.S. Pat. No. 4,982,023 (“Oxidation of methane to methanol” to Han, et al.) brings forth that a plurality of reactions is occurring in the direct oxygenation of methane to methanol. In this regard, U.S. Pat. No. 4,982,023 indicates some consideration of reaction-kinetics issues in the discussion of that patent&#39;s subject matter: 
     “The mechanism of methanol formation is believed to involve the methylperoxy radical (CH 3 OO) which abstracts hydrogen from methane. Unfortunately, up until now, the per pass yields have been limited. This limited yield has been rationalized as resulting from the low reactivity of the C—H bonds in methane vis-a-vis the higher reactivity of the primary oxygenated product, methanol, which results in selective formation of the deep oxidation products CO and CO 2  when attempts are made to increase conversion.” 
     U.S. Pat. No. 4,982,023 also makes it clear that methane and oxygen are to be premixed prior to reaction as noted in the following extract: “ . . . natural gas and the oxygen or air are kept separate until mixed just prior to being introduced into the reactor. However, if desired, the oxygen and natural gas may be premixed and stored together prior to the reaction”. 
     Unfortunately, laboratory results regarding methanol selectivity and single pass yield for non-catalyzed direct oxygenation of methane to methanol have not been reliably duplicated in scaling the reaction technology to manufacturing-sized systems. The need for an efficient and low cost reactor system for reacting two gaseous fluid streams where control of a plurality of free-radical sub-reactions is needed continues to prompt development. 
     SUMMARY 
     It is accordingly an object of the present invention to provide a reactor system for gas phase reacting of at least two fluid feed streams into a product stream, where the reactor system comprises an injectively-mixed backmixing reaction chamber in fluid communication with a tubular-flow reactor. The injectively-mixed backmixing reaction chamber has a backmixing reaction chamber housing, a bulkhead in slideably-sealed interface to the backmixing reaction chamber housing, an injectively-mixed backmixing reaction chamber internal volume defined by the backmixing reaction chamber housing and by the bulkhead, and a housing portion in opposite disposition to the bulkhead. The bulkhead is slideably movable during real-time operation of the reactor system to progress within the injectively-mixed backmixing reaction chamber housing toward the housing portion to either commensurately diminish the injectively-mixed backmixing reaction chamber internal volume, or, alternatively, to retract away from the housing portion to thereby commensurately expand the injectively-mixed backmixing reaction chamber internal volume. 
     In one embodiment, the bulkhead has at least one passageway for fluid communication of product stream from the injectively-mixed backmixing reaction chamber into the tubular-flow reactor. In one aspect of this, the bulkhead provides the passageway with at least one aperture having a cross-sectional area, and the reactor system has a blocking component for variably obstructing a portion of the cross-sectional area from passageway use during real-time operation of the reactor system. In another aspect, the bulkhead has at least one aperture as a first aperture, the blocking component has at least one second aperture, the first aperture and the second aperture have essentially identical dimensions, and the first aperture and the second aperture are mutually disposed to positionally align, in one relative positioning of the bulkhead and the blocking component, to define the passageway to have a cross-sectional area essentially equivalent to the cross-sectional area of the first aperture. 
     In another embodiment, the tubular-flow reactor has a tubular-flow reactor internal volume defined by a tubular-flow reactor housing and by the bulkhead. In one aspect of this, slideable movement of the bulkhead toward the housing portion commensurately diminishes the injectively-mixed backmixing reaction chamber internal volume while expanding the tubular-flow reactor internal volume, and alternative slideable movement of the bulkhead away from the housing portion commensurately expands the injectively-mixed backmixing reaction chamber internal volume while diminishing the tubular-flow reactor internal volume. 
     In yet another embodiment, the injectively-mixed backmixing reaction chamber has a first fluid input and a second fluid input for the reactor system; the injectively-mixed backmixing reaction chamber has a backmixing reaction chamber output; the tubular-flow reactor has a tubular-flow reactor input in fluid communication with the backmixing reaction chamber output; the first fluid input receives a first fluid feed stream into the injectively-mixed backmixing reaction chamber; the second fluid input receives a second fluid feed stream into the injectively-mixed backmixing reaction chamber; and the injectively-mixed backmixing reaction chamber has a space-time, respective to a combined feed rate of the first fluid feed stream and the second fluid feed stream, of from about 0.05 seconds to about 1.5 seconds. 
     In yet another embodiment, a first fluid stream in the fluid feed streams comprises methane and a second fluid stream in the fluid feed streams comprises oxygen. In one aspect of this, at least one alkyl oxygenate (e.g., without limitation, methanol, formaldehyde, and/or ethanol) is manufactured through partial oxidation reacting of a first fluid stream (in the fluid feed streams) comprising an alkane-containing gas feed stream (containing methane, ethane, propane, and/or butane) and a second fluid stream in the fluid feed streams comprising oxygen from an oxygen-containing gas feed stream; the injectively-mixed backmixing reaction chamber has an alkane gas input, an oxygen gas input, and a backmixing reaction chamber output; the tubular-flow reactor has an tubular-flow reactor input in fluid communication with the backmixing reaction chamber output; the alkane gas input receives the alkane-containing gas feed stream into the injectively-mixed backmixing reaction chamber; the oxygen gas input receives the oxygen-containing gas feed stream into the injectively-mixed backmixing reaction chamber; and the injectively-mixed backmixing reaction chamber has a space-time, respective to a combined feed rate of the alkane-containing gas feed stream and the oxygen-containing gas feed stream, sufficient for induction of alkyl free radicals from the alkane within the injectively-mixed backmixing reaction chamber and for providing at least a portion of the alkyl free radicals to the tubular-flow reactor input. In one aspect of this, the alkane gas input and the oxygen gas input are configured to turbulently agitate the injectively-mixed backmixing reaction chamber by injective intermixing of the alkane-containing gas feed stream and the oxygen-containing gas feed stream. 
     In yet another embodiment, the tubular-flow reactor has a tubular-flow reactor output, and the tubular-flow reactor has at least one cooling gas input disposed between the tubular-flow reactor input and the tubular-flow reactor output for receiving a cooling gas stream and thereby quenchably cooling the tubular-flow reactor. In one aspect, the tubular-flow reactor has an axis, and the cooling gas input is moveable along the axis during operation of the tubular-flow reactor. 
     In yet other embodiments, the injectively-mixed backmixing reaction chamber has an internal volume defined in part by a cylindrical surface having an injectively-mixed backmixing reaction chamber axis, and one feed stream of the feed streams is input into the internal volume from a plurality of apertures disposed along the axis and in non-parallel orientation to the axis. 
     In yet another embodiment, the injectively-mixed backmixing reaction chamber has an internal flow diverter defined by a conical surface having an axis, the diverter defines a conical base at one end of the axis, the conical surface defines an apexial end at the other end of the axis, the axis of the diverter is aligned with the axis of the injectively-mixed backmixing reaction chamber, the diverter is disposed within the housing such that the backmixing reaction chamber output is more proximate to the apexial end than to the conical base, and one feed stream of the feed streams is input into the internal flow space from a plurality of apertures disposed along the injectively-mixed backmixing reaction chamber axis and in non-parallel orientation to the injectively-mixed backmixing reaction chamber axis. 
     In yet another embodiment, the bulkhead has at least one passageway for fluid communication of an injectively-mixed backmixing reaction chamber product stream from the injectively-mixed backmixing reaction chamber into the tubular-flow reactor, the tubular-flow reactor has a tubular-flow reactor input in fluid communication with the backmixing reaction chamber output, the bulkhead provides the passageway with at least one aperture having a cross-sectional area, the tubular-flow reactor housing has an axis and a first portion and a second portion in threaded attachment to the backmixing reaction chamber housing, and the reactor system further comprises: a blocking component for variably obstructing a portion of the cross-sectional area from passageway use during real-time operation of the reactor system; and a variable-position cooling gas input disposed in the second portion in spiral orientation along the axis for quenchably cooling the tubular-flow reactor with a cooling gas stream; where the tubular-flow reactor housing second portion is in threaded attachment to the backmixing reaction chamber housing with threads that move the second portion along the axis when the second portion is rotated, and rotation of the second portion simultaneously repositions the bulkhead along the axis, the cooling gas input along the axis, and the blocking component to modify the cross-sectional area. 
     The novel features that are considered as characteristic for the present invention are set forth in particular in the appended claims. The invention itself, both as to its construction and its method of operation together with additional objects and advantages thereof, will be best understood from the following description of specific embodiments when read in connection with the accompanying drawings. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  schematically shows a system of an apparatus for producing alkyl oxygenate (e.g., without limitation, methanol) in accordance with the present teachings; 
         FIGS. 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; 
         FIG. 4  represents a graph depicting the yield oxygenates of the system as a function of recycle ratio; 
         FIG. 5  represents an alternate C 1 -C 4  alkane to alkyl oxygenate plant according to the teachings of the present invention; 
         FIG. 6  represents an optional oxygen producing plant shown in  FIG. 5 ; 
         FIG. 7  depicts a gas processing portion of the plant shown in  FIG. 5 ; 
         FIG. 8  represents the liquid processing portion of the plant shown in  FIG. 5 ; 
         FIG. 9  represents another alternate C 1 -C 4  alkane (e.g., without limitation, methane) to alkyl oxygenate (e.g., without limitation, methanol) plant according to the teachings of the present invention; 
         FIG. 10  represents yet another alternate C 1 -C 4  alkane (e.g., without limitation, methane) to alkyl oxygenate (e.g., without limitation, methanol) plant according to the teachings of the present invention; 
         FIG. 11  represents yet another alternate C 1 -C 4  alkane (e.g., without limitation, methane) to alkyl oxygenate (e.g., without limitation, methanol) plant according to the teachings of the present invention; 
         FIG. 12  presents a cross section simplified view of one embodiment of a reactor system having an injectively-mixed backmixing reaction chamber in close coupling to a tubular-flow reactor; 
         FIGS. 13A and 13B  present cross section simplified views of details in modifying the internal volume of the injectively-mixed backmixing reaction chamber of  FIG. 12 ; 
         FIG. 14A  presents a cross section simplified view of an alternative design for the injectively-mixed backmixing reaction chamber of  FIG. 12 ; 
         FIG. 14B  shows a view of the injectively-mixed backmixing reaction chamber of  FIG. 12  with a modified internal volume from that shown in  FIG. 12 ; 
         FIGS. 15A and 15B  present a cross section simplified view of a “hairbrush” fluid delivery insert for the injectively-mixed backmixing reaction chamber of the reactor system embodiments of  FIGS. 12 and 20 ; 
         FIG. 16  presents a cross section simplified view of internal fluid passageways for the conical fluid delivery insert for the injectively-mixed backmixing reaction chamber of the reactor system embodiments of  FIGS. 12 and 20 ; 
         FIGS. 17A and 17B  present a cross section simplified view of baffle details and positioning at the interface between the injectively-mixed backmixing reaction chamber and the tubular-flow reactor of the reactor system embodiments of  FIGS. 12 and 20 ; 
         FIGS. 18A and 18B  present a cross section simplified view of details and positioning for one variable position quenching inlet of the reactor system embodiments of  FIGS. 12 and 20 ; 
         FIGS. 19A and 19B  present a series of temperature profiles for the tubular-flow reactor of the reactor system embodiments of  FIGS. 12 and 20 ; 
         FIG. 20  presents a cross section simplified view of an alternative embodiment of a reactor system having an injectively-mixed backmixing reaction chamber in close coupling to a tubular-flow reactor; 
         FIG. 21  presents bulkhead/baffle details for an embodiment of the interface between the injectively-mixed backmixing reaction chamber and the tubular-flow reactor of the reactor system embodiments of  FIGS. 12 and 20 ; 
         FIGS. 22A-22C  show axial positioning detail for the interface between the injectively-mixed backmixing reaction chamber and the tubular-flow reactor of the  FIG. 20  reactor system embodiment; 
         FIG. 23  show further detail in the quenching inlet for the  FIG. 20  reactor system embodiment; 
         FIGS. 24A and 24B  show axial view detail for the  FIG. 20  reactor system embodiment; and 
         FIGS. 25A and 25B  show views of tubular-flow reactor systems having injectively-mixed entry zones, multi-position quenching, and multi-position temperature sensing. 
     
    
    
     DESCRIPTION OF THE PREFERRED EMBODIMENTS 
     The following definitions and non-limiting guidelines must be considered in reviewing the description of this invention set forth herein. 
     The headings (such as “Introduction” and “Summary”) and sub-headings (such as “Amplification”) used herein are intended only for general organization of topics within the disclosure of the invention, and are not intended to limit the disclosure of the invention or any aspect thereof. In particular, subject matter disclosed in the “Introduction” may include aspects of technology within the scope of the invention, and may not constitute a recitation of prior art. Subject matter disclosed in the “Summary” is not an exhaustive or complete disclosure of the entire scope of the invention or any embodiments thereof. 
     The citation of references herein does not constitute an admission that those references are prior art or have any relevance to the patentability of the invention disclosed herein. All references cited in the Description section of this specification are hereby incorporated by reference in their entirety. 
     The description and specific examples, while indicating embodiments of the invention, are intended for purposes of illustration only and are not intended to limit the scope of the invention. Moreover, recitation of multiple embodiments having stated features is not intended to exclude other embodiments having additional features, or other embodiments incorporating different combinations the stated of features. 
     As used herein, the words “preferred” and “preferably” refer to embodiments of the invention that afford certain benefits, under certain circumstances. However, other embodiments may also be preferred, under the same or other circumstances. Furthermore, the recitation of one or more preferred embodiments does not imply that other embodiments are not useful, and is not intended to exclude other embodiments from the scope of the invention. 
     As used herein, the word ‘include,” and its variants, is intended to be non-limiting, such that recitation of items in a list is not to the exclusion of other like items that may also be useful in compositions, materials, devices, and methods of this invention. 
     The examples and other embodiments described herein are exemplary and not intended to be limiting in describing the full scope of compositions and methods of this invention. Equivalent changes, modifications and variations of specific embodiments, materials, compositions and methods may be made within the scope of the present invention, with substantially similar results. 
     The embodiments relate to direct oxygenation conversion of at least one C 1 -C 4  alkane into as least one alkyl oxygenate. The direct oxygenation conversion of methane into methanol is a focal conversion goal of the technology. 
     One apparatus for producing methanol in accordance with the present invention has a reactor  100  facilitating a gas phase oxidation of a hydrocarbon-containing gas as shown in  FIG. 1 . In overview of reactor  100 , a heated hydrocarbon-containing gas stream (from valve  120  and heater  136 ) and an oxygen-containing gas from line  29  are introduced into reactor  100 . As explained in detail below, 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 optionally receives a quenching cold hydrocarbon-containing gas stream from valve  120  and heat exchanger  121  for reducing the temperature of reaction during operation of the apparatus. 
     The apparatus has a device  114  for cooling the reaction product stream mixture before separation. Additionally, 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-CO 2  mixture. The partial condenser  122  is preferably isobaric, as opposed to isothermal, to avoid pressure losses. The reaction product stream enters, and a liquid stream and gaseous stream exit condenser  122 . 
     Block  139  represents equipment that is configured to separate contaminants and products from a hydrocarbon-containing recycle gas component. In this regard, 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. 
     In the event the system is configured to recover formaldehyde, the gaseous reduced product stream leaves the isobaric condenser  122  and is passed to the scrubber  134 . Other potential methods that can be utilized use materials such as various amines known to remove CO 2  and formaldehyde. 
     To fulfill the minimum absorption requirements, 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 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° C. In either scenario, the pregnant methanol absorbent stream  14  is completely regenerated by the formaldehyde distillation column  138 . Optionally, 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 . In the event the raw hydrocarbons have a high CO 2  content, 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 that 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). As before, it is desirable for a portion of the heavy key component to enter the distillate stream (as dictated by commercial specification for formalin). For methanol rectification, 99% or higher purity is typical, and 99.999% is achievable with multiple columns. Stream  4  enters the column and the distillate, stream  5 , and bottoms, stream  8 , exit the column in liquid phase. 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  and formalin storage  191 ). In this manner, some of the ethanol is recovered before the remainder is discarded in the liquid waste stream. 
     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. 
     In operation, 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° C. The heated hydrocarbon-containing gas is then supplied into 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 reactor  100 . Oxidation reaction of methane to methanol and/or formaldehyde takes place in reactor  100 . Between 2% and 3% O 2  of the total volume of the reactants are reacted with the heated hydrocarbon-containing gas stream as previously described. To limit the amount of N 2  within the system, for example to less than 30%-40%, or reduce the requisite size of the purge stream to achieve the same, 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) coolant in the reactor is supplied into reactor  100  as previously outlined. This stream is regulated by the regulating device (valve)  120 , that 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 at a location further 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 that can easily be separated from the reaction product stream. For example, as better described below, the coolant can be an unheated hydrocarbon or methane containing gas stream. 
     Preferably, the coolant can be any non-oxidizing material easily separated from the reaction products. In this regard, the coolant can be gaseous, an aerosol, or misted liquid of, for example, CO 2 , formaldehyde, methanol, water, and/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. 
     Depending on the intended mode of operation of the apparatus, in particular the intended production of methanol or methanol and formaldehyde, 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 essentially/exclusively produce methanol. The introduction of the cold hydrocarbon-containing gas is used when methanol and formaldehyde are both desired as products. By introduction of the cold hydrocarbon-containing gas, the temperature of the reaction is reduced, for example by 30-90° Celsius, so as to preserve the content of formaldehyde in the separated mixture by reducing the decomposition of the formaldehyde into 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 to 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  that 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 . 
     Scrubber  134  functions to remove the CO 2  and formaldehyde from the dry gas stream. In this regard, 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. Once the CO 2  and formaldehyde are removed, 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 reaction chamber  100  at after being heated by heat exchanger  116  and heater  136  as previously described. 
     Rectification column  138  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 rectification column  138  and is separated into formaldehyde distillate stream  16  and bottoms 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). By allowing a portion of the heavy key component into the distillate stream the separation is more easily achieved; furthermore, process losses typically experienced during absorbent regeneration are subsequently nullified as methanol within the distillate is used for formalin production. Stream  15  is supplemented by stream  31  so as to replace any methanol that was transferred to the distillate stream, stream  16 . Combining stream  31  and stream  15  results in stream  17 , which then returns to the scrubber  134  as regenerated methanol absorbent. Meanwhile, the formaldehyde distillate, stream  16 , combines with the vapors from flash drum  132 , stream  7 , to form a mixture of formaldehyde, methanol, and carbon dioxide. 
     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, therefore comprise methanol, ethanol, and water insofar as formaldehyde remains in the gaseous stream. In this case, 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 . 
       FIGS. 2 and 3  show diagrams of the concentration of oxygen, formaldehyde and methanol in reactions without cooling and with cooling, respectively. 
     As can be seen from  FIG. 2 , approximately after 2 sec of reaction time, the oxygen is essentially completely reacted. 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 essentially completely consumed) its concentration somewhat reduces. 
     In the reaction with the cooling shown in  FIG. 3 , via the introduction of cold gas when the formation of methanol and formaldehyde is completed, the temperature of a final period of the reaction is reduced so as to inhibit the decomposition of formaldehyde. 
       FIG. 4  represents a graph depicting the yield of oxygenates for the system as a function of the fraction of hydrocarbon gas recycled. 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 overall 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. 
       FIG. 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 . 
     As shown in  FIG. 6 , 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 . 
     With general reference to  FIG. 7 , the gas processing portion of the plant  156  generally functions as described above (see  FIG. 1 ). In this regard, 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. It is envisioned that 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 that are produced in the reactor  100 . The reaction products  176  from the reactor are then transferred to the liquid processing plant  158 . 
     As shown in  FIG. 8 , 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 that 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  FIG. 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. 
     As previously mentioned, it is envisioned that 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 . While 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. In this regard, it is envisioned that 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. Additionally, it is envisioned that 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. 
     While shown as a land based plant, it is specifically envisioned that the plant  150  can be associated with an off-shore oil rig. In this regard, the plant  150  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. In the case of an off-shore rig, which is producing natural gas, it is envisioned that 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. 
     It is further envisioned that 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. Specifically, it is envisioned that 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. 
     Returning briefly to  FIG. 5 , it is envisioned that 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. In situations where the natural gas may be stranded or may have nitrogen contents of greater than 4%, facilities may be provided to manage nitrogen build-up in the recycle loop. When 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. In this regard, it is envisioned that 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 that contains a commercial grade of formalin. 
     Another process embodiment  900  is presented in  FIG. 9 . Air  902  is input to compressor  934  and then cooled in heat exchanger  904  for delivery to one of nitrogen separator  906  or nitrogen separator  962 . Oxygen feed is stored in tank  908  and compressed with compressor  910  for introduction as an oxygen-containing feed stream into reactor system  914  after heating in heater  912 . Alkane-containing raw feed  926  (at least one C 1 -C 4  alkane, primarily methane or natural gas) is compressed in compressor  928  and blended with scrubber  920  alkane recycle for further pressurization in compressor  922  and thermal cross exchange with reactor product stream reactor  936  in heat exchanger  930 . The recycle stream preferably provides a weight percentage proportion of from about 4:5 to about 20:21 of alkane in the alkane-containing feed stream to reactor  914 . In one embodiment, where scrubber  920  is pressurized to a pressure on the order of reactor system  914  (see  FIGS. 12 to 24B  and the accompanying text for further detail in reactor designs for reactor system  914 ), compressor  922  can be a centrifugal blower (non-positive displacement compressor). After thermal cross exchange with reactor product stream reactor  936  in heat exchanger  930 , the combined raw alkane and recycle stream is heated in heat exchanger  932  to provide an alkane-containing feed stream to reactor system  914 . Embodiments of reactor system  914  are further described in  FIGS. 12-24B . Scrubber  920  operates to absorb carbon dioxide and alkyl oxygenates (for example, without limitation, methanol, ethanol, and formaldehyde) while providing a recycle stream for combination with fresh alkane to provide a feed stream to compressor  922 . A purge at valve  924  removes non-reactive inerts (e.g., without limitation, nitrogen) from the reactor-scrubber process loop to augment efficient use of reactor system  914 . A cooling quench to reactor system  914  is also optionally enabled from valve  938 . Liquid bottoms from scrubber  920  are forwarded to flash drum  918  where overhead steam  942  separates from product stream  940  (comprising for example and without limitation, methanol, ethanol, and formaldehyde). Furnace or thermal oxidizer  916  oxidizes waste gases for discharge to the atmosphere. Process  900  is useful for providing a liquid material for further processing at another location into purified alkane oxygenates or for providing an alkane oxygenate blend useful for a fuel or other similar use where exact purity is not critical. 
       FIG. 10  shows another process embodiment  1000  with a front end process loop essentially similar to process  900  presented in  FIG. 9 , but incorporating an in-situ distillation system  1002  for separating methanol in steam  1004  (for absorbent in the scrubber), purified water in stream  1006  for use in knockdown drum  1012 , and generation of purified methanol  1008  and waste stream  1010 . Knockdown drum  1012  provides initial separation of liquid from the reactor product stream prior to the introduction of the remainder of the reactor product stream into the scrubber. 
       FIG. 11  presents process embodiment  1100  for generating a methanol product stream and formaldehyde with a front end process loop essentially similar to process  900  presented in  FIG. 9 , but incorporating an in-situ formaldehyde distillation system  1110  and methanol distillation system  1108  to generate methanol product stream  1102 . The stream from methanol distillation system  1108  cools formaldehyde distillation system  1110  overheads to separate carbon dioxide (product stream  1106 ) and formaldehyde (product stream  1104 ) in absorber-blender  1116 . A recycle stream of methanol to the scrubber is drawn from methanol distillation system  1108  and chilled in chiller  1112  to provide a high-efficiency scrubber for condensing the reactor product stream. Furnace or thermal oxidizer  1114  oxidizes a purge to remove non-reactive inerts (e.g., without limitation, nitrogen) with some alkane (methane) from the reactor-scrubber process loop and thereby augment efficient use of the reactor. 
     While a traditional tubular-flow reactor can be used with any of the above-described processes as either reactor  100  and/or reactor  914 , preferred reactor embodiments are described in the discussion of  FIGS. 12 to 24B . 
     Turning now to a deeper consideration of kinetics in the reaction and further embodiments for providing an improved reactor system for executing the overall reaction for the partial oxidation of natural gas to methanol, formaldehyde, and other oxygenates, several compact production facilities have been described in  FIGS. 1-11  that are suitable for small, isolated natural gas sources (stranded gas). Novel reactor systems for these processes are also further described beginning with  FIG. 12  and, more specifically, as overviewed in  FIGS. 12 and 20 . Beginning considerations in these reactor designs derive from the nature of the overall direct oxygenation reaction itself. 
     In overview, the method for reaction comprises passing a mixture of natural gas and oxidant through a heated, continuous flow reactor system under conditions to optimize the formation of methanol, and to manipulate the reactor temperature, total pressure, and fuel (e.g., without limitation, natural gas) to oxidant ratio to control the relative amounts of reaction products. The reaction is a partial oxidation of a C 1 -C 4  fuel, such as natural gas, by an oxidant, oxygen, air, or other suitable oxygen-containing compound (preferably oxygen in air or, most preferably, oxygen). The mixture contains a substantial excess of fuel (e.g., without limitation, natural gas) to prevent complete combustion to undesired products such as carbon dioxide and water. 
     The reaction is an exothermic, branched chain reaction. Chain branching causes an acceleration of the reaction rate via quadratic growth of chain carriers. Reactions of this type are characterized by an induction period during which chain carrier concentrations build up to the point where a very rapid rise in reaction rate and temperature occurs. The very rapid rise in reaction rate is because of the quadratic growth rate of chain carriers, and the very rapid rise in temperature is because of the increase of the rate of heat generation that accompanies the reaction rate. Complete consumption of oxidant, the limiting reagent, occurs before the fuel (e.g., without limitation, natural gas) is entirely consumed, which limits the temperature rise. The ratio of oxidant to fuel (e.g., without limitation, natural gas) is arranged so that the selectivity for formation of methanol is optimized. 
     Reaction conditions favoring the best selectivity for methanol and other oxygenates are as follows. The composition of the reaction mixture, after combining the alkane-containing feed stream and the oxygen-containing feed stream, should be from about 1 mol % to about 10 mol % oxidant, preferably from about 2 mol % to about 5 mol % oxidant, and most preferably at about 2.5 mol % oxidant. The total pressure of the gases in the reactor system should be in the range of from about 6 MPa to about 10 MPa, preferably from about 7.5 MPa to about 9 MPa, and most preferably at about 8 Mpa. The reactor system wall temperature should be in the range of from about 600 K to about 900 K, and more preferably from about 723 K to about 823 K. The overall reactor residence time should be in the range of from about 1 second to about 40 seconds, more preferably from about 1 second to about 10 seconds, and most preferably from about 1 second to about 2.5 seconds. 
     At these conditions, methanol selectivity is in the range of from about 0.35 to at least 0.60 with lower selectivities for the other oxygenates of the alkane-containing feed stream. The conversion of methane is approximately 5 to 10%, and conversion of the other hydrocarbon components of the natural gas is comparable. After the reaction, separation and recycle of the unreacted hydrocarbons is performed. 
     For continuous operation, the fuel (e.g., a C 1 -C 4  alkane or C 1 -C 4  alkanes such as provided in natural gas) and oxidant must be well-mixed. For this purpose a mixing chamber/reactor is supplied for both thoroughly mixing the reaction components and for also inducing the generation of alkyl (e.g., without limitation, methyl) free radicals that are then contained in the output stream from the mixing chamber. In this regard, the mixing chamber therefore effectively provides an injectively-mixed backmixing reaction chamber (“backmix reaction chamber”) in a reactor system having an injectively-mixed backmixing reaction chamber in fluid communication with a tubular-flow reactor for carrying out the overall reaction. While not falling ideally into either a classical continuously-stirred-tank reactor model or into a classical tubular flow reactor model, the injectively-mixed backmixing reaction chamber of the embodiments has a number of aspects that indicate an operational character having more of a continuously stirred tank reactor or CSTR model affinity (further denoted as a continuous feed stirred tank reactor or CFSTR; and yet further denoted as a steady-state backmix flow reactor) than of a tubular or plug-flow reactor model affinity. The injectively-mixed backmixing reaction chamber has a space-time, respective to a combined feed rate of the alkane-containing feed stream and the oxygen-containing feed stream, of from about 0.05 seconds to about 1.5 seconds (a preferably contemplated space-time is about 0.1 seconds) so that the feeds can be effectively mixed and so that an initial induction period for generating alkyl free radicals (e.g., without limitation, methyl free radicals) can be accommodated before the injectively-mixed backmixing reaction chamber product stream (methane, oxygen, and methyl free radicals) is fed to the tubular-flow reactor for further reaction into methanol. In a preferred embodiment, the design of the injectively-mixed backmixing reaction chamber enables injective intermixing of the C 1 -C 4  alkane and oxygen-containing feed streams to turbulently agitate streams together and to effectively turbulently agitate the injectively-mixed backmixing reaction chamber. In this regard, the generating of methyl free radicals is perceived to be the first kinetic step reaction in the set of kinetic step reactions that achieve direct oxygenation of methane to methanol (one respective alkyl oxygenate), and the use of an injectively-mixed backmixing reaction chamber prior to the tubular-flow reactor enables a degree of freedom for independent optimization of this methyl free radical induction step. Other free radicals derived from C 2 -C 4  alkanes should usually have a shorter induction period than the methyl free radical under comparable conditions. The subsequent chain branching kinetic sub-reactions (kinetic sub-reaction steps) then covert the methyl free radicals and other components of the injectively-mixed backmixing reaction chamber product stream to methanol and other products; these later sub-reactions are best controlled in the tubular-flow reactor environment that has traditionally received the admixed (but unreacted) methane (alkane) and oxygen of prior systems. 
     The reactor system accordingly provides several degrees of freedom (e.g., without limitation, reactor space-time, temperature, and injective mixing as further subsequently discussed herein) for augmenting the initial kinetic series sub-reaction(s) and also for augmenting, with some independency from conditions augmenting the initial kinetic series sub-reaction(s), the subsequent kinetic series sub-reactions in the overall set of sub-reactions that combine to achieve the overall direct oxidation reaction of at least one C 1 -C 4  alkane into at least one respective alkyl oxygenate. 
     With respect to methane in the alkane-containing feed stream, the induction of methyl free radicals in the mixing chamber/reactor (the injectively-mixed backmixing reaction chamber) is a clear departure from the prior teachings of documents such as U.S. Pat. Nos. 4,982,023 and 4,618,732, both of which, as noted in the Background, indicate that the feed streams are to be only mixed prior to their introduction into a reactor. 
     The reactants are fed to the mixing chamber/reactor (the injectively-mixed backmixing reaction chamber) in separate streams. Upon emergence from the injectively-mixed backmixing reaction chamber, the reactants are then fed to the tubular-flow reactor. The mixing must be done thoroughly, with the goal of attaining a uniform or essentially uniform distribution of reactant concentration in the injectively-mixed backmixing reaction chamber product stream. This is necessary to avoid oxidation of the desired products-methanol and other oxygenates. Such oxidation otherwise occurs in incompletely mixed regions where relatively high oxidant concentrations exist, with commensurate reduction of product yield. In this regard, the mixing time in the injectively-mixed backmixing reaction chamber must be relatively brief compared to the residence time in the tubular-flow reactor. In view of the overall preferred residence times for the reactor system as whole, from about 1 second to about 2.5 seconds, the residence time in the injectively-mixed backmixing reaction chamber must be at least 0.1 second. In this regard, actual turbulent intermixing of gases can be achieved in as little as 1 ms. While there are several embodiments for achieving satisfactory mixing, as will be hereinafter described, a preferred embodiment for use with the shortest residence times uses essentially opposed turbulent jets with a diverter diffuser cone having its apex-tending side (apexial end) closest to the tubular-flow reactor. The purpose of the cone is to minimize long residence times for sub-portions of the contents of the injectively-mixed backmixing reaction chamber in view of the high reactivity of the alkyl (e.g., methyl) free radicals. 
     The reactor walls must be inert in the chemical environment of the reaction. The reactor construction material must be steel, preferably stainless steel, to contain the necessary total pressure. Insofar as a steel surface diminishes methanol selectivity, the steel is preferably coated with an inert coating, such as Teflon™, or an organic wax. Insertion of a Pyrex™ or quartz sleeve into the reactor also provides a relatively inert surface. 
     A flow restriction baffle is positioned in the injectively-mixed backmixing reaction chamber output to augment pressure drop between the injectively-mixed backmixing reaction chamber and the tubular-flow reactor and thereby achieve a desired residence time fine turning feature (degree of freedom of control) in the injectively-mixed backmixing reaction chamber. In a preferred embodiment, the flow restriction baffle (bulkhead with apertures for enabling a fluid passageway) is conveniently axially movable so that alternative baffle positions can be deployed in custom-configuring the effective space-time in the injectively-mixed backmixing reaction chamber prior to a process run instance or during a process run. In a preferred embodiment, the flow restriction baffle is further in close proximity to a blocking component that is conveniently axially movable so that variable baffle (bulkhead) passageways can be defined by partially blocking the apertures in the baffle (bulkhead) in custom-configuring the effective space-time in the injectively-mixed backmixing reaction chamber prior to a process run instance or during a process run; this feature provides another degree of freedom for operational control. 
     Turning now to an overview of the tubular-flow reactor, the axial position of the temperature maximum is quite sensitive to the reactor inlet temperature, total flow rate, and reactant composition. Fluctuations in any of these quantities can cause the position of the reactor “hot spot” to move. In an extreme case, the “hot spot” can move out of the reaction vessel and thereby adversely affect performance. The tubular-flow reactor is therefore preferably equipped in one embodiment with a thermocouple that can be translated axially (along the axis of general flow in the reactor) via a sliding seal. In another embodiment, a plurality of thermocouples disposed to measure the tubular-flow reactor temperature profile along the axis of flow enable temperature monitoring. The thermocouple set monitors the axial gas phase temperature distribution in the reactor, and the thermocouple measurements are also used for control of the reactor. 
     The methanol, formaldehyde and other oxygenates can undergo thermal decomposition in the high temperatures of the tubular-flow reactor, resulting in product loss. Such decomposition is minimized by cooling of the reactor contents at a location immediately downstream from the “hot spot”. Because wall cooling is not sufficiently responsive, a preferred embodiment employs injection of a cold gas by means of a tube whose axial position can also be changed by means of a sliding seal. The cold gas is preferably natural gas, but carbon dioxide, nitrogen, or another inert substance may also be used. 
       FIG. 12  presents a cross section simplified view  1200  of a reactor system having an injectively-mixed backmixing reaction chamber  1202  in close coupling to a tubular-flow reactor  1204  so that a reactor system having an injectively-mixed backmixing reaction chamber in fluid communication with a tubular-flow reactor is provided for one of the processes described in conjunction with  FIGS. 1-11 . The main chamber and reactor sections of the reactor system are aligned along axis  1220  with the injectively-mixed backmixing reaction chamber having housing  1206  (defining internal volume  1234  with a cylindrical surface in co-operation with bulkhead  1232 ). Tubular-flow reactor  1204  has housing  1210  defining internal volume  1248  in co-operation with slideable tubular-flow reactor  1204  section having housing  1208  and with bulkhead  1232 . An alkane-containing gas feed stream (a first fluid stream) enters through alkane gas input  1222  and similar alkane gas inputs as depicted. An oxygen-containing gas feed stream (a second fluid stream) enters through oxygen gas input  1224  and conical diverter/distributor  1226 . Conical diverter/distributor  1226  has a conical base (base  1614  of  FIG. 16 ) connected to a portion of housing  1206  in opposite disposition to bulkhead  1232 . A backmixing reaction chamber output is established by bulkhead (baffle)  1232  and passageway  1270  (with its associated fluid passageways shown in more detail in  FIGS. 17A and 17B ) and optional blocking component  1230 . Bulkhead (baffle)  1232  and optional (for variable passageway definition in real-time operation of the reactor system) blocking component  1230  provide passageways such as passageway  1270  for feeding the injectively-mixed backmixing reaction chamber  1202  product stream to tubular-flow reactor  1204 . Tubular-flow reactor  1204  therefore has a tubular-flow reactor input in fluid communication through passageway  1270  with the backmixing reaction chamber  1202  output at bulkhead (baffle)  1232  and blocking component  1230 . Alkane gas input  1222  (along with similar alkane gas inputs as depicted) and oxygen gas input  1224  with conical diverter/distributor  1226  and oxygen input aperture  1228  (along with similar alkane gas inputs as depicted) are configured (positioned and sized with respect to the flows of the alkane-containing and the oxygen-containing feed streams) to turbulently agitate reaction components within internal volume  1234  of injectively-mixed backmixing reaction chamber  1202  by injective intermixing of the alkane-containing gas feed stream and the oxygen-containing gas feed stream. 
     Tubular-flow reactor  1204  has a tubular-flow reactor output  1260 , and tubular-flow reactor  1204  has cooling gas input  1274  disposed between the tubular-flow reactor input from passageways (passageway  1270 ) at bulkhead  1232  and tubular-flow reactor output  1260  for receiving a cooling gas stream (that enters at cooling input port  1236  and then into cooling gas internal input port  1250  before proceeding to cooling gas input  1274 ) and thereby quenchably cooling tubular-flow reactor  1204 . In this regard, cooling gas input  1274  in one embodiment is in an elongated tube (tube  1262 ) with at least one aperture  1274  (see  FIGS. 18A and 18B  for cross-sectional detail respective to axis  1220 ) for conveying the cooling quench flow into reactor space  1248 . Tube  1262  co-operates with guide tube  1264 . In one embodiment, tube  1262  rotates within guide tube  1264  to regulate the amount of quench delivered to a location. In an alternative embodiment, tube  1262  is axially slideable (with reference to axis  1220 ) to position within tubular-flow reactor  1204  and provide local quenching. In yet another embodiment, tube  1262  rotates within guide tube  1264  to regulate the amount of quench delivered to a location and also is axially slideable (with reference to axis  1220 ) to position within tubular-flow reactor  1204  and provide local quenching. The quenching components (including drawing references  1262 ,  1250 ,  1236 ,  1264 , and  1274 ) therefore provide a degree of freedom for managing the temperature profile along axis  1220  within tubular-flow reactor  1204 . Thermocouples such as thermocouple  1216  and similar thermocouples as depicted provide measurements for the temperature profile in one embodiment. A sliding thermocouple  1214  (with thermocouple sensor  1272  and sealed with sliding seal  1212  to housing  1210 ) provides measurements for the temperature profile in another embodiment.  FIG. 12  shows an embodiment having stationary thermocouples such as thermocouple  1216  was well as a sliding thermocouple  1214  (with thermocouple head  1272 ). 
     Tubular-flow reactor  1204  has housing  1210  defining internal volume  1248  in co-operation with the slideable tubular-flow reactor  1204  section having housing  1208  and also having bulkhead  1232  (with optional blocking component  1230  for providing passageway  1270  as a cross-sectionally-variable passageway). Bulkhead  1232  and blocking component  1230  are in slideably-sealed interface to backmixing reaction chamber housing  1206  and are therefore both effectively attached to the slideable tubular-flow reactor  1204  section having housing  1208 . Housing section  1208  is therefore in slideably-sealed interface to housing  1210  and also to housing  1206  with seals  1244 ,  1246 , and  1238  providing isolation from the external environment. Injectively-mixed backmixing reaction chamber  1202  has an injectively-mixed backmixing reaction chamber internal volume  1234  defined by backmixing reaction chamber housing  1206  and by bulkhead  1232  (with optional blocking component  1230 ). Bulkhead  1232  (and blocking component  1230 ) is therefore slideably movable during real-time operation of the reactor system of view  1200  to progress within backmixing reaction chamber housing  1206  toward input  1224  to thereby commensurately diminish internal volume  1234 , and bulkhead  1232  (and blocking component  1230 ) is alternatively slideably movable during real-time operation to retract away from input  1224  to thereby commensurately expand internal volume  1234 . In the embodiment of  FIG. 12 , tubular-flow reactor  1204  has a tubular-flow reactor internal volume  1248  defined by tubular-flow reactor housings  1208  and  1210  and by bulkhead  1232  (with blocking component  1230 ). Bulkhead  1232  (and blocking component  1230 ) is therefore slideably movable during real-time operation of the reactor system of view  1200  to thereby commensurately diminish internal volume  1248  when moving away from toward input  1224 , and bulkhead  1232  (with optional blocking component  1230 ) is alternatively slideably movable during real-time operation to move toward input  1224  to thereby commensurately expand internal volume  1248 . This moveable interface enables a degree of freedom for managing relative space-time (essentially equivalent, for gaseous flow, to internal reaction volume divided by volumetric flow rate moving through that internal reaction volume) within the reactor system of view  1200  between both tubular-flow reactor  1204  and injectively-mixed backmixing reaction chamber  1202 . 
     Essentially, the functionality enabled by the features of bulkhead  1232  (and blocking component  1230 ) is for a backmixing reaction chamber where the internal volume (defined by an internal surface of a housing and also by the surface of any component in moveably sealed interface to that internal surface) can be readily modified so that the space-time, provided by the backmixing reaction chamber to chemically reacting compositional components in gaseous fluids flowing within the internal volume, can be modified without necessarily modifying flow rate(s), turbulency, and/or pressure drop of those fluids. In this regard, any approach for modifying the internal volume from a first internal volume to a second internal volume is potentially useful. In one conceptualized embodiment, for instance, bulkhead  1232  is axially fixed, conical diverter/distributor  1226  has a base wide enough to slideably seal against backmixing reaction chamber housing  1206 , conical diverter/distributor  1226  has a slideable tube (not shown) interconnecting to input  1224 , and conical diverter/distributor  1226  thereby commensurately diminishes internal volume  1234  when moving away from input  1224  and commensurately expandes internal volume  1234  when moving toward input  1224 . In another conceptualized embodiment, housing  1206  has a movable portion that invades into the chamber to diminish internal volume  1234  and alternatively withdraws from the chamber to increase internal volume  1234 . In yet another conceptualized embodiment, an internal diaphramed component modifies its characteristics to commensurately modify internal volume  1234 . 
     Seal  1246 , seal  1212 , seal  1244 , seal  1238 , seal  1242 , and seal  1240  all enable slideable movement of the movable components of the reactor system of view  1200 . Rotation component  1218  enables rotation of blocking component  1230  during operation. As should be apparent, movement of components (especially during operation of the reactor system of view  1200 ) is preferably achieved with assistance from variable speed motors, levers, levers with associated gearing, and/or step-motors and with associated gearing (not shown but that should be apparent to those of skill). 
     In operation, an alkane-containing feed stream and an oxygen-containing feed stream are input to injectively-mixed backmixing reaction chamber  1202  through input ports such as input  1222  (alkane-containing feed stream) and input  1224  (oxygen-containing feed stream). Injectively-mixed backmixing reaction chamber  1202  internal conditions are managed to induce alkyl free radical formation in injectively-mixed backmixing reaction chamber  1202  to yield an injectively-mixed backmixing reaction chamber product stream for output and fluid communication into tubular-flow reactor  1204  through passageways such as passageway  1270  in bulkhead  1232  and blocking component  1230 . The components are sized and arranged to provide significant molecular momentum in the entering fluids so that injective mixing and a turbulent reaction fluid in injectively-mixed backmixing reaction chamber  1202  are established. The injectively-mixed backmixing reaction chamber product stream fed to tubular-flow reactor  1204  via passageway  1270  therefore comprises oxygen, unreacted alkane, and at least a portion of the alkyl free radicals that were induced in injectively-mixed backmixing reaction chamber  1202 . In this regard, the “reaction” of alkane to alkyl oxygenate (focally, the “reaction” of methane to methanol) involves a large plurality of reactions (termed herein also as kinetic series sub-reactions or kinetic sub-reactions); indeed, there may be at least 60 kinetic series sub-reactions in the overall “reaction” of methane to methanol and other alkyl oxygenates occurring in the system. The initial kinetic series sub-reaction occurs to induce an alkyl radical from an alkane when an alkane molecule is exposed to molecular oxygen. There is therefore efficacy in handling this reaction in a separated injectively-mixed backmixing reaction chamber that is in fluid communication with a tubular-flow reactor where a consistent (with time and at steady state operation) portion of the alkyl radicals will be essentially conveyed (fed into the tubular-flow reactor) to provide the basis for enabling the many subsequent parallel and sequential kinetic series sub-reactions that require a heat management approach more amenable to tubular-flow reactors than to injectively-mixed backmixing reaction chambers. Although close-coupled to a tubular-flow reactor in the embodiments, the injectively-mixed backmixing reaction chamber provides the reaction components with an essentially universal compositional and physical (temperature, pressure, and molecular momentum) operational state within its space-time compared to a tubular-flow system; this enables management of the critical alkyl radical induction step independently from the tubular-flow reactor where, along the axis of the tubular-flow reactor, the reaction components have an axially (and probably radially) differentiated composition and physical state. 
     As should be apparent to those of skill, the management of scale-up in such a system as the reactor system of view  1200  needs to manage the challenge of providing acceptable molecular momentum in increasing space-time situations; if the molecular momentum diminishes, the reaction fluid in the injectively-mixed backmixing reaction chamber will migrate toward the laminar flow range and the overall necessary consistency of the injectively-mixed backmixing reaction chamber reaction fluid may thereby become potentially compromised; therefore, a reactor according to view  1200  appears efficacious in small-scale processing for making “stranded gas” a valuable commodity. 
     The overall reactor system space-time, respective to a combined feed rate of the alkane-containing feed stream and the oxygen-containing feed stream, is not greater than 40 seconds, and is preferably not greater than 2.5 seconds. Reaction space-time for the injectively-mixed backmixing reaction chamber is managed to be not greater than 1.5 seconds. 
       FIGS. 13A and 13B  presents cross section simplified views  1300  and  1350  of details in modifying the internal volume of the injectively-mixed backmixing reaction chamber  1202  of  FIG. 12 . In this regard, an alternative view  1300  is presented for injectively-mixed backmixing reaction chamber  1202  in  FIG. 13A  where a “hairbrush” distributor  1308  (further detailed in  FIGS. 15A and 15B ) for the oxygen-containing feed stream is depicted. View  1300  of  FIG. 13A  generally shows a bulkhead  1304  and optional blocking component  1302  in fully expanded or extended orientation to housing  1306 . 
     Reactor view  1350  of  FIG. 13B  generally shows bulkhead  1304  and optional blocking component  1302  in inserted orientation to housing  1306  to diminish the volume (and, in steady state operation, the space time) of the injectively-mixed backmixing reaction chamber respective to the volume (space-time) of view  1300 . 
       FIG. 14A  presents a cross section simplified view  1400  of another alternative design for injectively-mixed backmixing reaction chamber  1202  of  FIG. 12 . In this regard, a hemispherical head portion  1402  is profiled for the housing, with a comparably hemispherical profile in the inserted bulkhead. 
       FIG. 14B  shows a view  1450  depicting the injectively-mixed backmixing reaction chamber  1202  of  FIG. 12  with a modified internal volume from that shown in  FIG. 12 . Bulkhead  1232  and (optional) blocking component  1230  are depicted in inserted orientation to housing  1206  to diminish the volume (and, in steady state operation, the space time) of the injectively-mixed backmixing reaction chamber  1202  respective to the volume (space-time) of view  1200 . 
       FIGS. 15A and 15B  present aligned cross-sectional views  1500  and  1550  of the “hairbrush” fluid delivery insert  1308  for an alternative design for injectively-mixed backmixing reaction chamber  1202  of  FIG. 12 . Axis  1504  is aligned with axis  1220  in the preferred embodiment, with view  1500  showing “hairbrush” distributor  1308  detail respective to a plane perpendicular to axis  1504 , and view  1550  showing “hairbrush” distributor  1308  detail respective to a plane parallel to axis  1504 . The oxygen-containing feed stream is input into internal flow space  1234  from a plurality of apertures (such as aperture  1502 ) disposed along the injectively-mixed backmixing reaction chamber axis in the essential centerline of the cylindrical surface of housing  1206  and in non-parallel orientation to the injectively-mixed backmixing reaction chamber axis  1220  when axis  1504  is essentially aligned with axis  1220 . 
       FIG. 16  presents a cross section simplified view  1600  of internals for conical fluid delivery insert  1226  for delivering the oxygen-containing feed stream into the injectively-mixed backmixing reaction chamber  1202  of  FIG. 12 . The internal flow diverter is defined by a conical surface  1604  having an axis  1602 . A conical base  1614  is at one end of axis  1602 , and apexial end  1612  (an end that, if the cone were extended, would ultimately converge to provide the apex of the cone) is at the other end of axis  1602 . As shown in view  1200  of  FIG. 12 , axis  1602  is aligned with axis  1220  of injectively-mixed backmixing reaction chamber  1202  when conical diverter  1226  is disposed within cylindrical housing  1206  such that the backmixing reaction chamber output (passageway  1270 ) is more proximate to apexial end  1612  than to conical base  1614 . The oxygen-containing feed stream is input into inlet  1610  (from inlet  1224  of  FIG. 12 ) and then into internal flow space  1234  from a plurality of apertures  1608  disposed along injectively-mixed backmixing reaction chamber axis  1220  (axis  1602 ) and in non-parallel orientation to axis  1220 . Internal passageway  1606  fluidly conveys the oxygen-containing feed stream to the plurality of apertures  1608 . 
       FIGS. 17A and 17B  present cross section simplified views of the interface baffle ( 1232 / 1230 ) details and positioning at the interface between injectively-mixed backmixing reaction chamber  1202  and tubular-flow reactor  1204  of the  FIG. 12  reactor system. In view  1700  of  FIG. 17A , bulkhead  1702  has at least one aperture  1704  defining a passageway (see passageway  1270  in  FIG. 12 ) for fluid communication of an injectively-mixed backmixing reaction chamber product stream from injectively-mixed backmixing reaction chamber  1202  into tubular-flow reactor  1204 . Bulkhead  1702  (bulkhead  1232  in  FIG. 12 ) provides the passageway with at least one aperture  1704  having a cross-sectional area. In a flowing fluid, bulkhead  1702  with apertures  1704  defines a baffle for creating a pressure drop between injectively-mixed backmixing reaction chamber  1202  and tubular-flow reactor  1204  as the flowing fluid passes from injectively-mixed backmixing reaction chamber  1202  into tubular-flow reactor  1204 . In a “tuned” reactor system, apertures  1704  can be precisely sized in one embodiment so that no blocking component is needed; such an arrangement has fewer degrees of freedom for operation, but also is less complex from a sealing and construction standpoint. For real-time operational varying of the effective passageway created by aperture  1704 , a blocking component  1230  is deployed in an alternative embodiment where, as shown in view  1750  of  FIG. 17B , blocking component  1230  can be rotated to “block” a portion of the cross-sectional area of aperture  1704  where a portion of blocking component  1706  (blocking component  1230  of  FIG. 12 ) is shown constricting the passageway of aperture  1704  (note that view  1750  can be conceptualized as a view parallel to axis  1220  and toward injectively-mixed backmixing reaction chamber  1202  from tubular-flow reactor  1204 ) and thereby restricting the passageway. 
     In a preferred embodiment, bulkhead ( 1232 / 1702 ) has at least one aperture  1704  as a first aperture, and blocking component ( 1230 / 1706 ) has at least one second aperture ( 1708 ). These first and second apertures preferably have essentially identical dimensions, and first aperture  1704  and second aperture  1708  are mutually disposed to positionally align, in one relative positioning of bulkhead ( 1232 / 1702 ) and blocking component ( 1230 / 1706 ), to define the passageway ( 1270 ) to have a cross-sectional area essentially equivalent to the cross-sectional area of the first aperture. In view  1750 , this can be appreciated by considering that the portion of aperture  1704  that is not blocked from passageway use by blocking component  1706  is also the portion of aperture  1708  that is not blocked from passageway use by bulkhead  1702 . 
     An alternative embodiment of the combination of bulkhead ( 1232 / 1702 ) and blocking component ( 1230 / 1706 ) that does not include use of rotation component  1218  is further discussed with respect to  FIG. 21 . In this alternative embodiment, bulkhead ( 1232 / 1702 ) is movable respective to stationary blocking component ( 1230 / 1706 ) where key slot  1710  provides an axially (with respect to axis  1220 ) slideable restraint against key  2110  ( FIG. 21 ) for prohibiting rotation of blocking component ( 1230 / 1706 ). In this embodiment, bulkhead ( 1232 / 1702 ) is firmly attached to housing  1208 , but housing  1208  further rotates about axis  1220  to achieve a variable passageway  1270  defined by aperture  1704  and aperture  1708 . Key  2110  is affixed to housing  1206  (details not shown), and aperture  1714  ( FIG. 17A ) provides a non-resistive opening for key  2110  to pass into internal volume  1248  so that bulkhead ( 1232 / 1702 ) and blocking component ( 1230 / 1706 ) move axially (axis  1220 ) respective to inlet  1224  with blocking component  1230 / 1706  always restrained and bulkhead  1232 / 1702  always capable of rotation about axis  1220 . 
     Ball bearings  1712  are used in preferred embodiments to augment smooth rotation of the movable component (either of bulkhead  1232 / 1702  or blocking component  1230 / 1706  depending upon their particular embodiment) against the non-movable component in the baffle system. 
       FIGS. 18A and 18B  present cross sectional simplified views  1800 ,  1850 , and  1860  of details and positioning for the variable position quenching inlet  1274  for the  FIG. 12  reactor system. Guide tube  1264  is shown in perpendicular cross-sectional in view  1800  respective to axis  1220  as tube cross-section  1802  having an elongated slot  1808  running along axis  1220 . The elongated slot is difficult to show in  FIG. 12 , but it is depicted in  FIGS. 18A and 18B  as fully open passageway  1808  to convey the axial slot; quench tube  1804 / 1262  is shown with aperture  1806 / 1274 —see inlet passageway  1274  in FIG.  12 —to show that it is an opening having substantially less axial dimension than the axial dimension of slot  1808  of guide tube  1802 / 1264 . Tube  1804 / 1262  co-operates with guide tube  1802 / 1264  as shown in view  1850  to not convey quench into internal volume  1248  when aperture  1806  is rotated to block the passageway ( 1274 ) with the internal surface of guide tube  1802 / 1264 . In one embodiment, tube  1804 / 1262  is axially slideable within guide tube  1802 / 1264  to reposition aperture  1806 / 1274  axially along axis  1220 . View  1860  then shows rotation of radial alignment between tube  1804 / 1262  and guide tube  1802 / 1264  so that passageway/inlet  1274  is enabled. Note that several alternative sets (not shown) of apertures  1806  can be readily provided at different radial positions of tube  1804  to provide alternative quench patterns as a function of the radial orientation of tube  1804 / 1262  along axis  1220  in tubular-flow reactor  1204 . 
       FIGS. 19A and 19B  present a series of temperature profiles for the tubular-flow reactor of the  FIG. 12  reactor system in operation. In this regard, axis of abscissas  1904  and axis of ordinates  1906  are identical throughout  FIGS. 19A and 19B , with axis of abscissas  1904  showing distance along axis  1220  of tubular-flow reactor  1204  and axis of ordinates  1906  depicting temperature within the reaction fluid of tubular-flow reactor  1204 . Locus  1902  ( FIG. 19A ) is a conceptualized depiction of a temperature profile for tubular-flow reactor  1204  without benefit of quenching. Locus  1922  ( FIG. 19B ) is a conceptualized depiction of a temperature profile for tubular-flow reactor  1204  with benefit of quenching at location  1938 . The afore-discussed kinetic series sub-reactions will vary in their activity depending upon the temperature profile along axis  1220  within tubular-flow reactor  1204 . So, for instance, the product mix from tubular-flow reactor  1204  will be different for each of Loci  1902 ,  1922 , and  1932  per their differentiated thermal profiles, commensurately differentiated energies, and commensurately differentiated kinetic activity for individual sub-reactions in the kinetic series sub-reaction set. The quenching tube design therefore affords yet another degree of freedom for optimizing the composition of an alkyl oxygenate reactor system product stream generated from a C 1 -C 4  alkane-containing feed stream and an oxygen-containing feed stream. 
       FIG. 20  presents a cross section simplified view  2000  of an alternative embodiment of a reactor system having an injectively-mixed backmixing reaction chamber in close coupling to a tubular-flow reactor. The interface baffle assembly (bulkhead  1232  and blocking component  1230  assembly embodiments as described with respect to  FIG. 12  and the alternative key-restrained deployment embodiments of  FIGS. 17A ,  17 B, and  21 ) is slideably movable and rotated during real-time operation of the reactor system of view  2000  to progress and/or retract away from input  2062  by use of a threaded seal and connection facilitated by male threading  2012  (male threading  2212  in FIGS.  21  and  22 A- 22 C). The majority of the injectively-mixed backmixing reaction chamber and the tubular-flow reactor share housing  2070 , that is further threaded to provide female threading for co-operating with threading  2012 / 2212 .  FIGS. 22A-22C  show further detail in this regard where  FIG. 22A  shows tubular-flow reactor sleeve  2016  in fully progressed position,  FIG. 22B  shows tubular-flow reactor sleeve  2016  in mid-point progression/retraction position, and  FIG. 22C  shows tubular-flow reactor sleeve  2016  in fully retracted position. 
     The backmixing reaction chamber and tubular-flow reactor of the reactor system of view  2000  are aligned along axis  2014 . An alkane-containing gas feed stream (a first fluid stream) enters through alkane gas input  2060  and the plurality of alkane gas input apertures as depicted. An oxygen-containing gas feed stream (a second fluid stream) enters through oxygen gas input  2062  and the hairbrush distributor as previously discussed with respect to  FIGS. 15A and 15B . In an alternative embodiment, a conical diverter/distributor ( FIG. 16 ) is used for the oxygen-containing feed stream. 
     The tubular-flow reactor has tubular-flow reactor sleeve  2016  in slideably sealed interface at seal  2008  to housing  2004  and provides a fluid output into a relatively small space defined by housing  2004 . Housing  2004  has an axial depth sufficient to accommodate the full axial traverse enabled by threading  2012 / 2212  (see also  FIGS. 22A-22C ). Housing  2004  has an output for the reactor product stream at output  2020 . Cooling gas input  2002  receives the previously-described cooling gas stream into cooling gas space  2072  (defined between the internal surface of housing  2070  and the external surfaces of sleeve  2016  and blocking tube  2006 ). The cooling gas stream then proceeds into the internal space of sleeve  2016  via spiral slot  2018 , at a point where an axial slot (axial slot  2032  of perpendicular cross section view  2028  across axis  2014  in right-facing orientation at  2042  and of  FIG. 23 ) of blocking tube  2006  and spiral slot  2018  align to define a passageway ( 2302  of  FIG. 23 ) and also to thereby quenchably cool the internal space of tubular-flow reactor sleeve  2016 . Sleeve  2016  therefore co-operates closely with blocking tube  2006 . 
     Sleeve  2016  is sealed to housing  2070  with slideable seal  2074  and thereby rotates to simultaneously process/regress respective to the injectively-mixed backmixing reaction chamber per threads  2012 / 2212  ( FIGS. 22A-22C ), regulate the amount of quench delivered to a location within tubular-flow reactor sleeve  2016  (described with  FIG. 20  and further described with  FIG. 23 ), and modify the passageway cross-sectional area (fixed-key baffle assembly as previously discussed and further discussed in  FIG. 21 ). While these three degrees of control freedom (baffle positional procession/regression, quench delivery, and baffle passageway cross-sectional area) are therefore not managed with full independence, differences in the rate of change of each with one rotation of sleeve  2016  enables a controllable system having fewer seals than the embodiment described with respect to  FIG. 12  and with only very limited convolution between these three degrees of freedom for normal operation. In this regard, one full rotation of sleeve  2016  achieves a full transfer of spiral slot  2018  position (its full axial analog range), perhaps about 2% of the full axial analog range for baffle positional procession/regression, and 600% of the passageway cross-sectional area full axial analog range for a baffle having 6 apertures ( FIGS. 17A and 17B ). Therefore, sleeve  2016  is first rotated to position within the axial analog range for baffle positional procession/regression, then to position within the axial analog range for quenching, and finally to position within the axial analog range for the passageway cross-sectional area. Insofar as baffle positioning is anticipated to be a relatively strategic operational setting for a particular alkane-gas feed stream composition, real-time operational adjustments should relate more to the single-rotation quench and (⅙ rotation) baffle passageway positioning. 
     Perpendicular cross section view  2030  across axis  2014  in left-facing orientation at  2040  shows further detail in aperture positioning for inputting feeds from input  2060  and  2062  into the backmixing reaction chamber. 
       FIG. 21  presents bulkhead/baffle details  2100  for the  FIG. 20  reactor system embodiment and also for the alternative embodiment of the interface between the injectively-mixed backmixing reaction chamber and the tubular-flow reactor of the  FIG. 12  reactor system embodiment as previously referenced with respect to  FIGS. 17A and 17B . Sleeve  2016  is reprised from  FIG. 20  with male threading  2012 / 2212 . As described for the alternative embodiment respective to  FIGS. 17A and 17B , blocking component  2108  is restrained from rotation by key  2110  (as inserted into slot  1710  ( FIG. 17B ) and bulkhead  2104  is in non-slideable attachment to sleeve  2016 . Ball bearings  2106  interface bulkhead  2104  (end of sleeve  2016 ) to blocking component  2108 . Bulkhead  2104  (sleeve  2016 ) rotates freely around key  2110  by virtue of non-restraining circular aperture  1714  ( FIG. 17A ). 
     As previously discussed,  FIGS. 22A-22C  show axial positioning details  2200 ,  2230 , and  2260  for the interface between the injectively-mixed backmixing reaction chamber and the tubular-flow reactor of the  FIG. 20  reactor system embodiment. Sleeve  2016  is reprised from  FIG. 20  with male threading  2012 / 2212 . 
       FIG. 23  shows further detail  2300  in the quenching inlet for the  FIG. 20  reactor system embodiment. In this regard, a vertical view of sleeve  2016  and blocking tube  2006  in alignment with the axis of entry for input  2002  ( FIG. 20 ) is shown. Sleeve  2016 , blocking tube  2006 , spiral slot  2018 , and axial slot  2032  (view  2028  of  FIG. 20 ) are all reprised from  FIG. 20 . Location  2302  shows the alignment point of blocking tube  2006  and spiral slot  2018  for delivery of the quenching gas into sleeve  2016  to thereby quenchably cool the internal space of the tubular-flow reactor. 
       FIGS. 24A and 24B  show axial view detail for the  FIG. 20  reactor system embodiment.  FIG. 24A  shows a right-facing view along axis  2014  ( FIG. 20 ) from the outside of the reactor system; inputs  2060  and  2062  are reprised from  FIG. 20 .  FIG. 24B  shows perpendicular cross section view  2450  across axis  2014  in left-facing orientation at  2022  ( FIG. 20 ); input  2002  is reprised from  FIG. 20  and apertures  1704 / 1706  are reprised from  FIGS. 17A and 17B . 
       FIGS. 25A and 25B  show views  2500  and  2550  of two tubular-flow reactor system embodiments having injectively-mixed entry zones (zone  2520  in both of  FIGS. 25A  &amp; B), multi-position quenching, and multi-position temperature sensing. Mixing zone  2520  in both  FIG. 25A  and  FIG. 25B  shows a symbolic conical distributor diverter  2502  with a full cone, highly similar to the conical diverter of  FIG. 16  and also of  FIG. 12 . System view  2500  of  FIG. 25A  shows multiple thermocouples (such as thermocouple  2510 ) and multiple quench inlet ports (such as quench inlet port  2508 ) in housing  2512 . System view  2550  of  FIG. 25B  shows variable position thermocouple  2504  and a variable position thermocouple quench inlet port  2506  sealing disposed within the internal space defined by housing  2514 . Quenching and temperature measurement are therefore highly similar in  FIG. 12  and  FIG. 25B  for the tubular-flow reactors of both of these embodiments. The systems of both  FIG. 25A  and  FIG. 25B  are useful in providing reactor systems that are highly similar to the embodiments of  FIGS. 12 and 20  except for the absence in  FIGS. 25A and 25B  of a separating baffle assembly defining a clear interface between an injectively-mixed backmix reaction chamber and the tubular-reactor. In this regard, data from operation of a system of either of  FIG. 25A  or  FIG. 25B , when compared to data from operation of a system of either of  FIG. 12  or  FIG. 20 , has value in indicating efficacy for settings respective to the baffled interface (bulkhead  1232 /component  1230  in  FIG. 12  or the threaded baffling assembly of  FIG. 20 ). 
     It will be understood that each of the elements described above, or two or more together, may also find a useful application in other types of methods and constructions differing from the types described above. While the invention has been illustrated and described as embodied in the method of and apparatus for producing methanol, it is not intended to be limited to the details shown, since various modifications and structural changes may be made without departing in any way from the spirit of the present invention. 
     Without further analysis, the foregoing will so fully reveal the gist of the present invention that others can, by applying current knowledge, readily adapt it for various applications without omitting features that, from the standpoint of prior art, fairly constitute essential characteristics of the generic or specific aspects of this invention.