Abstract:
Systems and methods for processing a methane rich producer gas are provided in which the producer gas is preferably produced via steam-hydrogasification. The product stream from the steam-hydrogasification is then subjected to autothermal reforming, steam is removed after the reforming step via condensation, and sulfur impurities are subsequently eliminated. In most preferred aspects, the process pressure is substantially maintained throughout all steps, typically in a range of 150 psi to 500 psi.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is a Continuation in part of U.S. Ser. No. 12/286,165, filed Sep. 29, 2008 (now U.S. Pat. No. 8,118,894), which is a continuation-in-part of U.S. Ser. No. 12/218,653, filed Jul. 16, 2008 (now U.S. Pat. No. 8,143,319), which is a continuation-in-part of U.S. Ser. No. 11/879,267, filed Jul. 16, 2007 (now U.S. Pat. No. 7,619,012), which is a continuation-in-part of abandoned U.S. Ser. No. 11/879,456, filed Jul. 16, 2007, which is a continuation-in-part of U.S. Ser. No. 11/879,241, filed Jul. 16, 2007 (now U.S. Pat. No. 8,268,026), which is a continuation-in-part of U.S. Ser. No. 11/879,266, filed Jul. 16, 2007 (now U.S. Pat. No. 7,897,649), which is a continuation-in-part of co-pending U.S. Ser. No. 11/635,333, filed Dec. 6, 2006, which is a continuation-in-part of abandoned U.S. Ser. No. 11/489,353, filed Jul. 18, 2006, which is a continuation-in-part of abandoned U.S. Ser. No. 11/489,298, filed Jul. 18, 2006, which is a continuation-in-part of abandoned 11/489,299, filed Jul. 18, 2006, which is a continuation-in-part of abandoned 11/489,308, filed Jul. 18, 2006, which is a continuation-in-part of U.S. Ser. No. 10/911,348, filed Aug. 3, 2004 (now U.S. Pat. No. 7,500,997), which is a continuation-in-part of International application PCT/US03/03489, filed Feb. 4, 2003, which claims priority to U.S. provisional application US 60/355,405, filed Feb. 5, 2002. 
     All of the above cited applications are incorporated herein by reference in their entirety. 
    
    
     FIELD OF THE INVENTION 
     The field of the invention is the production of synthesis gas. 
     BACKGROUND OF THE INVENTION 
     There is a need to identify new sources of chemical energy and methods for its conversion into alternative transportation fuels, driven by many concerns including environmental, health, safety issues, and the inevitable future scarcity of petroleum-based fuel supplies. The number of internal combustion engine fueled vehicles worldwide continues to grow, particularly in the midrange of developing countries. The worldwide vehicle population outside the U.S., which mainly uses diesel fuel, is growing faster than inside the U.S. This situation may change as more fuel-efficient vehicles, using hybrid and/or diesel engine technologies, are introduced to reduce both fuel consumption and overall emissions. Since the resources for the production of petroleum-based fuels are being depleted, dependency on petroleum will become a major problem unless non-petroleum alternative fuels, in particular clean-burning synthetic diesel fuels, are developed. Moreover, normal combustion of petroleum-based fuels in conventional engines can cause serious environmental pollution unless strict methods of exhaust emission control are used. A clean burning synthetic diesel fuel can help reduce the emissions from diesel engines. 
     The production of clean-burning transportation fuels requires either the reformulation of existing petroleum-based fuels or the discovery of new methods for power production or fuel synthesis from unused materials. There are many sources available, derived from either renewable organic or waste carbonaceous materials. Utilizing carbonaceous waste to produce synthetic fuels is an economically viable method since the input feed stock is already considered of little value, discarded as waste, and disposal is often polluting. Alternatively, one can use coal as a feedstock to upgrade low grade dirty solid fuel to a value added convenient clean liquid fuel, such as high quality, environment friendly synthetic diesel or other hydrocarbon fuels. 
     Liquid transportation fuels have inherent advantages over gaseous fuels, having higher energy densities than gaseous fuels at the same pressure and temperature. Liquid fuels can be stored at atmospheric or low pressures whereas to achieve liquid fuel energy densities, a gaseous fuel would have to be stored in a tank on a vehicle at high pressures that can be a safety concern in the case of leaks or sudden rupture. The distribution of liquid fuels is much easier than gaseous fuels, using simple pumps and pipelines. The liquid fueling infrastructure of the existing transportation sector ensures easy integration into the existing market of any production of clean-burning synthetic liquid transportation fuels. 
     The availability of clean-burning liquid transportation fuels is a national priority. Producing synthesis gas (a mixture of hydrogen and carbon monoxide, also referred to as “syngas”) cleanly and efficiently from carbonaceous sources, that can be subjected to a Fischer-Tropsch type process to produce clean and valuable synthetic gasoline and diesel fuels, will benefit both the transportation sector and the health of society. A Fischer-Tropsch type process or reactor, which is defined herein to include respectively a Fischer-Tropsch process or reactor, is any process or reactor that uses synthesis gas to produce a liquid fuel. Similarly, a Fischer-Tropsch type liquid fuel is a fuel produced by such a process or reactor. A Fischer-Tropsch type process allows for the application of current state-of-art engine exhaust after-treatment methods for NO x  reduction, removal of toxic particulates present in diesel engine exhaust, and the reduction of normal combustion product pollutants, currently accomplished by catalysts that are poisoned quickly by any sulfur present, as is the case in ordinary stocks of petroleum derived diesel fuel, reducing the catalyst efficiency. Typically, Fischer-Tropsch type liquid fuels, produced from synthesis gas, are sulfur-free, aromatic free, and in the case of synthetic diesel fuel have an ultrahigh cetane value. 
     Biomass material is the most commonly processed carbonaceous waste feed stock used to produce renewable fuels. Waste plastic, rubber, manure, crop residues, forestry, tree and grass cuttings and biosolids from waste water (sewage) treatment are also candidate feed stocks for conversion processes. Biomass feed stocks can be converted to produce electricity, heat, valuable chemicals or fuels. California tops the nation in the use and development of several biomass utilization technologies. Each year in California, more than 45 million tons of municipal solid waste is discarded for treatment by waste management facilities. Approximately half this waste ends up in landfills. For example, in just the Riverside County, California area, it is estimated that about 4000 tons of waste wood are disposed of per day. According to other estimates, over 100,000 tons of biomass per day are dumped into landfills in the Riverside County collection area. This municipal waste comprises about 30% waste paper or cardboard, 40% organic (green and food) waste, and 30% combinations of wood, paper, plastic and metal waste. The carbonaceous components of this waste material have chemical energy that could be used to reduce the need for other energy sources if it can be converted into a clean-burning fuel. These waste sources of carbonaceous material are not the only sources available. While many existing carbonaceous waste materials, such as paper, can be sorted, reused and recycled, for other materials, the waste producer would not need to pay a tipping fee, if the waste were to be delivered directly to a conversion facility. A tipping fee, presently at $30-$35 per ton, is usually charged by the waste management agency to offset disposal costs. Consequently not only can disposal costs be reduced by transporting the waste to a waste-to-synthetic fuels processing plant, but additional waste would be made available because of the lowered cost of disposal. 
     The burning of wood in a wood stove is a simple example of using biomass to produce heat energy. Unfortunately, open burning of biomass waste to obtain energy and heat is not a clean and efficient method to utilize the calorific value. Today, many new ways of utilizing carbonaceous waste are being discovered. For example, one way is to produce synthetic liquid transportation fuels, and another way is to produce energetic gas for conversion into electricity. 
     Using fuels from renewable biomass sources can actually decrease the net accumulation of greenhouse gases, such as carbon dioxide, while providing clean, efficient energy for transportation. One of the principal benefits of co-production of synthetic liquid fuels from biomass sources is that it can provide a storable transportation fuel while reducing the effects of greenhouse gases contributing to global warming. In the future, these co-production processes could provide clean-burning fuels for a renewable fuel economy that could be sustained continuously. 
     A number of processes exist to convert biomass and other carbonaceous materials to clean-burning transportation fuels, but they tend to be too expensive to compete on the market with petroleum-based fuels, or they produce volatile fuels, such as methanol and ethanol that have vapor pressure values too high for use in high pollution areas, such as the Southern California air-basin, without legislative exemption from clean air regulations. An example of the latter process is the Hynol Methanol Process, which uses hydro-gasification and steam reformer reactors to synthesize methanol using a co-feed of solid carbonaceous materials and natural gas, and which has a demonstrated carbon conversion efficiency of &gt;85% in bench-scale demonstrations. 
     Synthesis gas can be produced through one of two major chemical processes, steam reforming and partial oxidation. Steam reforming is used when the feed consists of light hydrocarbons such as natural gas, and when hydrogen is the main product. Partial oxidation is used with heavier feeds, or when a relatively high yield of carbon monoxide is desired. Table 1 summarizes various commercial processes under operation for the production of synthesis gas [1]. 
     
       
         
               
               
               
               
             
               
               
               
               
             
           
               
                   
                 TABLE 1 
               
               
                   
                   
               
               
                   
                   
                   
                 Syngas Ratio 
               
               
                   
                 Chemical Process 
                 Feedstock 
                 (H 2 /Co, mole) 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                   
                 Steam Reforming 
                 Natural gas, steam 
                 4.76 
               
               
                   
                 Steam Reforming 
                 Methane, steam 
                 3 
               
               
                   
                 Steam Reforming 
                 Naptha, steam 
                 2 
               
               
                   
                 Steam Reforming 
                 Natural gas, CO 2 , steam 
                 2 
               
               
                   
                 Partial Oxidation 
                 Coal, steam, O 2   
                 0.68 
               
               
                   
                 Partial Oxidation 
                 Coal, steam, O 2   
                 0.46 
               
               
                   
                 Partial Oxidation 
                 Coal, steam, O 2   
                 2.07 
               
               
                   
                   
               
             
          
         
       
     
     The ratio of hydrogen to carbon monoxide in the synthesis gas is called the syngas ratio and is strongly dependent on the process used and the nature of the feedstock. 
     Syngas is used as a feedstock in the manufacture of various chemicals and also in the gas-to-liquid processes, which use the Fischer-Tropsch type synthesis (FTS) to produce liquid fuels. Alternatively, syngas can be used in the so called integrated gasification combined cycle, where it is directly burned with air to produce the heat necessary to operate steam turbines used in electricity generation. Depending on the desired usage, the H 2 /Co ratio of syngas needs to be adjusted. Table 2 summarizes the optimum syngas ratios required for different processes [2]. 
     
       
         
               
               
               
               
             
           
               
                   
                 TABLE 2 
               
               
                   
                   
               
               
                   
                   
                   
                 Syngas Ratio 
               
               
                   
                   
                   
                 Required 
               
               
                   
                 Desired Product 
                 Chemical Process 
                 (H 2 /Co, mole) 
               
               
                   
                   
               
             
             
               
                   
                 Synthetic fuels 
                 FTS - Co catalyst 
                 2.05-2.15 
               
               
                   
                 Synthetic fuels 
                 FTS - Fe catalyst 
                 1.65 
               
               
                   
                 Methanol 
                   
                 2 
               
               
                   
                 Ethylene glycol 
                   
                 1.5 
               
               
                   
                 Acetic acid 
                   
                 1 
               
               
                   
                 Benzene-toluene-xylene 
                   
                 1.5 
               
               
                   
                   
               
             
          
         
       
     
     In general, the syngas ratio can be lowered by using the pressure swing adsorption process or by using hydrogen membrane systems. Alternatively, adding a downstream water-gas shift reactor can increase the syngas ratio. 
     A process was developed in our laboratories to produce synthesis gas in which a slurry of particles of carbonaceous material in water, and hydrogen from an internal source, are fed into a hydro-gasification reactor under conditions to generate rich producer gas. This is fed along with steam into a steam pyrolytic reformer under conditions to generate synthesis gas. This process is described in detail in Norbeck et al. U.S. patent application Ser. No. 10/503,435 (published as US 2005/0256212), entitled: “Production Of Synthetic Transportation Fuels From Carbonaceous Material Using Self-Sustained Hydro-Gasification.” In a further version of the process, using a steam hydro-gasification reactor (SHR) the carbonaceous material is heated simultaneously in the presence of both hydrogen and steam to undergo steam pyrolysis and hydro-gasification in a single step. This process is described in detail in Norbeck et al. U.S. patent application Ser. No. 10/911,348 (published as US 2005/0032920), entitled: “Steam Pyrolysis As A Process to Enhance The Hydro-Gasification of Carbonaceous Material.” The disclosures of U.S. patent application Ser. Nos. 10/503,435 and 10/911,348 are incorporated herein by reference. 
     Producing synthesis gas via gasification and producing a liquid fuel from synthesis gas are totally different processes. Of particular interest to the present invention is the production of synthesis gas using a steam methane reformer (SMR), a reactor that is widely used to produce synthesis gas for the production of liquid fuels and other chemicals. The reactions taking place in the SMR can be written as follows.
 
CH 4 +H 2 ΠCO+3H 2   (1)
 
or
 
CH 4 +2H 2 OΠCO 2 +4H 2   (2)
 
     Carbon monoxide and hydrogen are produced in the SMR by using steam and methane as the feed. Heating process water in a steam generator produces the required steam. The methane is usually supplied in the form of compressed natural gas, or by means of a light molecular weight off-gas stream from a chemical or refinery process. 
     BRIEF SUMMARY OF THE INVENTION 
     This invention provides an improved, economical alternative method to supply steam and methane to an SMR, and to control the synthesis gas composition obtained from the SMR. This is accomplished by a combination of new procedures, wherein product gas from an SHR is used as the feedstock for the SMR by removing impurities from the product stream from the SHR with a gas cleanup unit that operates at process pressures and is located in between the SHR and SMR. 
     In one embodiment of the invention, product gas from an SHR is used as the feedstock for the SMR. As described above, this steam and methane rich product gas is generated by means of hydro-gasification of the slurry, which is a mixture of carbonaceous material and water. This product gas, a mixture of methane rich gas and steam, where the steam is present as a result of the superheating the water in the feedstock, serves as an ideal feed stream for the SMR. The SMR requires no other input of gases other than the mixture of methane rich gas and steam produced by hydrogasifier. 
     The other procedure requires removing impurities from the product stream from hydrogasifiers, such as fine particles of ash &amp; char, hydrogen sulfide (H 2 S) and other inorganic components. These impurities must be removed in order to prevent poisoning of the catalyst used in the SMR. Conventionally, a combination of particulate filters, a solvent wash (amines, SELEXOL™, RECTISOL™), and hydro-desulphurization by means of the Claus process are used for this purpose. In the Claus process, H 2 S is partially oxidized with air in a reaction furnace at high temperatures (1000-1400 deg C.). Sulfur is formed, but some H 2 S remains unreacted, and some SO 2  is made requiring that the remaining H 2 S be reacted with the SO.sub.2 at lower temperatures (about 200-350 deg C.) over a catalyst to make more sulfur. However, because the SMR feed stream needs to be maintained high temperatures, these conventional clean-up techniques are prohibitive from an energy viewpoint, since the re-heating of the gas stream consumes a significant amount of energy. Moreover, the benefits supplied by retaining the steam from the SHR product stream are lost. Accordingly, in another embodiment of the invention, a gas cleanup unit is provided that operates at process pressures and is located in between the SHR and SMR. 
     More particularly, a process is provided for converting carbonaceous material to synthesis gas, comprising simultaneously heating carbonaceous material in the presence of both hydrogen and steam, at a temperature and pressure sufficient to generate a stream of methane and carbon monoxide rich gas product, which can be called a producer gas. Impurities are removed from the producer gas stream substantially at the process pressure at a temperature above the boiling point of water at the process pressure, and the resultant producer gas is subjected to steam methane reforming under conditions whereby synthesis gas comprising hydrogen and carbon monoxide is generated. In a specific process, for converting municipal waste, biomass, biosolids, wood, coal, or a natural or synthetic polymer to synthesis gas, the carbonaceous material is simultaneously heated in the presence of both hydrogen and steam, at a temperature of about 700° C. to about 900° C. and pressure about 132 psi to 560 psi whereby to generate a stream of methane and carbon monoxide rich producer gas. Impurities are removed from the producer gas stream at the process pressure and at a temperature above the boiling point of water at the process pressure (which can be substantially at the process temperature), following which the resultant producer gas is subjected to steam methane reforming under conditions whereby to generate synthesis gas comprising hydrogen and carbon monoxide at a H 2 :CO mole ratio range of about 3 to 1. The required H 2 :CO mole ratio of a Fischer-Tropsch type reactor with a cobalt based catalyst is 2:1. Accordingly, there is an excess of hydrogen, which can be separated and fed into the SHR to make a self-sustainable process, i.e., without requiring an external hydrogen feed. The synthesis gas generated by the steam methane reforming can be fed into a Fischer-Tropsch type reactor under conditions whereby a liquid fuel is produced. Exothermic heat from the Fischer-Tropsch type reaction can be transferred to the hydro-gasification reaction and/or steam methane reforming reaction. 
     In a further embodiment, a method for enhancing the operability of hot gas cleanup of methane rich producer gas is provided. This is accomplished by changing the sequence of the process to a sequence comprising:
         steam-hydrogasification;   autothermal reforming of methane;   steam removal by condensation; then   hot gas cleanup.       

     More particularly, a process is provided for enhancing the operability of hot gas cleanup for the production of synthesis gas in which a stream of methane rich gas is autothermally reformed at a temperature and pressure sufficient to generate a stream of synthesis gas rich in hydrogen and carbon monoxide, about 550° C. to about 750° C. The synthesis gas is subjected to condensation and removing the resultant water, and sulfur impurities are removed from the resultant synthesis gas stream in the absence of moisture, which condition is favorable to sulfur capture by the sorbents. The synthesis gas stream resulting from condensation is heated to substantially the temperature at which the impurities are removed from the synthesis gas stream, about 250° C. to about 400° C. 
     The stream of methane rich producer gas can be produced from separate steam pyrolysis and hydro-gasification reactors, but preferably, the stream of methane rich producer gas is produced from steam-hydrogasification before being subjected to autothermal reforming. Again preferably, the pressure of the steam-hydrogasification, autothermal reforming, condensation, and sulfur impurity removal is substantially the same throughout, about 150 psi to 500 psi. 
     In another embodiment, an apparatus is provided for converting carbonaceous material to synthesis gas, comprising a steam-hydrogasification reactor for simultaneously heating carbonaceous material with liquid water in the presence of both hydrogen and steam, at a temperature and pressure sufficient to generate a stream of methane rich gas, and autothermal methane reforming means to generate a stream of synthesis gas rich in hydrogen and carbon monoxide, means for condensing subjecting said synthesis gas to condensation, whereby synthesis gas is substantially devoid of water, and means for removing sulfur impurities from the said synthesis gas stream devoid of water. 
     The apparatus can include a Fischer-Tropsch type reactor for receiving the purified generated synthesis gas to produce a liquid fuel. Means can be provided for transferring exothermic heat from the Fischer-Tropsch type reaction to the steam-hydrogasification reactor and/or autothermal methane reforming means. 
     In yet another embodiment, this invention provides an improved, economical method to control the synthesis gas composition obtained from a steam methane reformer that obtains its feedstock as product gas directly from a steam hydro-gasification reactor. The method allows control of the H 2 /CO ratio by predetermining/adjusting the hydrogen feed and the water content of feedstock into the SHR that supplies the SMR. In a particular embodiment, H 2 :CO mole ratio of about 0.5:1 to 16:1 and more particularly of about 1:1 to 6:1 can be produced as a result of adjusting/predetermining the hydrogen feed and the water content of feedstock into the SHR. 
     To control the sygnas ratio, one of two methods are used to adjust the hydrogen feed. In one embodiment, the hydrogen is obtained by diverting a portion of hydrogen separated from the synthesis gas to the slurry water. In another, preferred embodiment, the hydrogen is obtained by diverting a portion of the synthesis gas itself to the hydrogasification reactor, without separating hydrogen from the synthesis gas. By controlled recycling, using a portion of the synthesis gas, a steady state desired H 2 /H 2 O ratio is obtained, which occurs quite rapidly. 
     As described above, the steam and methane rich product gas of the SHR is generated by means of hydro-gasification of the slurry, which is a mixture of carbonaceous material and water. This product gas, a mixture of methane rich gas and steam, where the steam is present as a result of the superheating the water in the feedstock, serves as an ideal feed stream for the SMR. Impurities such as fine particles of ash &amp; char, hydrogen sulfide and other inorganic components are removed from the SHR product stream, for instance using some of the embodiments disclosed above. 
     The mass percentages of the product stream at each stage of the process are calculated using a modeling program, such as the ASPEN PLUS™ equilibrium process that can relate the synthesis gas ratio of hydrogen to carbon monoxide to conversion ratios of the carbon content of the carbonaceous material. In accordance with the invention, by varying the parameters of solid to water ratio and hydrogen to carbon ratio, a sensitivity analysis can be performed that enables one determine the optimum composition of the slurry feedstock to the SHR to obtain a desired syngas ratio output of the SMR. Thus, the ratio of hydrogen to slurry water is determined by analysis of the effect on the synthesis gas ratio of (a) the ratio of solid content of the carbonaceous material to the slurry water and (b) the ratio of the hydrogen to carbon content of the carbonaceous material. This enables one to adjust the hydrogen feed and the water content of feedstock into the SHR that supplies the SMR to provide the desired ratio of hydrogen to carbon monoxide in the synthesis gas output of the SMR. 
     More particularly, a process is provided for converting carbonaceous material to synthesis gas, comprising simultaneously heating carbonaceous material in an SHR in the presence of a predetermined ratio of hydrogen and water in the form of steam, at a temperature and pressure sufficient to generate a stream of methane and carbon monoxide rich gas product, which can be called a producer gas. Impurities are removed from the producer gas stream substantially at the process temperature and pressure (either by hot gas cleanup alone or in combination with autothermal reforming and condensation), and the resultant producer gas is subjected to steam methane reforming in an SMR under conditions whereby synthesis gas comprising hydrogen and carbon monoxide is generated having a hydrogen/carbon monoxide ratio determined by the ratio of hydrogen and water in the SHR. While the hydrogen can be obtained by diverting a portion of hydrogen separated from the synthesis gas to the slurry water, it is preferred to obtain the hydrogen by diverting a portion of the synthesis gas itself, without separation of hydrogen from the synthesis gas, to the slurry water. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
       For a more complete understanding of the present invention, reference is now made to the following descriptions taken in conjunction with the accompanying drawing, in which: 
         FIG. 1  is a flow diagram of the process of this invention in accordance with a first embodiment in which hydrogen is separated from a portion of the SMR output and recirculated; 
         FIG. 2  is a flow diagram of the mass balance of the process of the first embodiment; 
         FIG. 3  is flow diagram of the process of this invention in accordance with a second embodiment where a portion of the output of the SMR is itself recycled without separation of its hydrogen; 
         FIG. 4  is flow diagram of the mass balance of the process in accordance with the second embodiment before recycling of a portion of the SMR; 
         FIG. 5  is flow diagram of the mass balance of the process in accordance with the second embodiment after recycling a portion of the SMR; 
         FIG. 6  shows the H 2 /CO and steam/CH 2  molar ratios for each run in accordance with the second embodiment until after steady values are achieved; 
         FIG. 7  is a sensitivity analysis using the ASPEN PLUS™ modeling program showing various conversions and the syngas ratio when parameters of solid to water ratio and hydrogen to carbon ratio are varied. 
         FIG. 8  shows the H2/CO syngas ratios obtainable when wood is used as the feedstock. 
         FIG. 9  shows the H2/CO syngas ratios obtainable when coal is used as the feedstock. 
         FIG. 10  shows a flow diagram of the process of this invention in accordance with a specific embodiment. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     This invention provided several embodiments for improved cleanup and production of synthesis gas. Regardless of the embodiment, simultaneously heating of the carbonaceous material in the presence of both hydrogen and steam (at the steam hydrogasification stage) can occur in the absence of catalysts, injection of air, oxygen (i.e. partial oxidation conditions), or other initiating chemicals. 
     In one embodiment of the invention, the feedstock for an SMR is a mixture of steam and methane rich product gas generated by means of hydro-gasification of a mixture of carbonaceous material and water in an SHR. The steam is present as a result of superheating the water in the feedstock and serves as an ideal feed stream for the SMR. 
     In another embodiment, a hot gas cleanup method is provided for removing impurities from the product stream from the SHR, such as fine particles of ash &amp; char, hydrogen sulfide (H 2 S) and other inorganic components. These impurities must be removed in order to prevent poisoning of the catalyst used in the SMR while maintaining the SMR feed stream at its high process temperatures. Accordingly, in another embodiment of the invention, a gas cleanup unit is provided that operates at the process pressure and at a temperature above the boiling point of water at the process pressure, and is located between the SHR and SMR. 
     In a more particularized embodiment, this invention provides autothermal reforming of methane and steam removal by condensation prior to the above mentioned hot gas cleanup stage. This process can be used where there are separate steam pyrolysis and hydro-gasification reactors, or in a steam hydrogasification reactor, followed by an autothermal reforming reactor, in a process for producing a synthesis gas for use as fuel for process heat and/or in a fuel engine or gas turbine that can generate electricity; or as feed into a Fischer-Tropsch type reactor to produce a liquid paraffinic fuel, recycled water and sensible heat, in a substantially self-sustaining process. 
     In yet another embodiment, a method is provided that enables one to control of the H 2 /CO ratio output of an SMR by adjusting the hydrogen feed and the water content of feedstock into the SHR that supplies the SMR. The steam and methane rich product gas of the SHR is generated by means of hydro-gasification of the slurry, which is a mixture of carbonaceous material and water. This product gas, a mixture of methane rich gas and steam, where the steam is present as a result of the superheating the water in the feedstock, serves as an ideal feed stream for the SMR. 
     The mass percentages of the product stream at each stage of the process are calculated using a modeling program, such as the ASPEN PLUS™ equilibrium process. By varying the parameters of solid to water ratio and hydrogen to carbon ratio, a sensitivity analysis can be performed that enables one determine the optimum composition of the slurry feedstock to the SHR to obtain a desired syngas ratio output of the SMR. Thus one can adjust the hydrogen feed and the water content of feedstock into the SHR that supplies the SMR to determine the syngas ratio output of the SMR. 
     Impurities are removed from the SHR product stream, such as fine particles of ash &amp; char, hydrogen sulfide and other inorganic components. These impurities must be removed in order to prevent poisoning of the catalyst used in the SMR. Conventionally, a combination of particulate filters, a solvent wash (amines, SELEXOL™, RECTISOL™), and hydro-desulphurization by means of the Claus process are used for this purpose. In the Claus process, H 2 S is partially oxidized with air in a reaction furnace at high temperatures (1000-1400° C.). Sulfur is formed, but some H 2 S remains unreacted, and some SO 2  is made requiring that the remaining H 2 S be reacted with the SO 2  at lower temperatures (about 200-350° C.) over a catalyst to make more sulfur. However, because the SMR feed stream needs to be maintained at high temperatures, these conventional clean-up techniques are prohibitive from an energy viewpoint since the re-heating of the gas stream consumes a significant amount of energy. Moreover, the benefits supplied by retaining the steam from the SHR product stream are lost. Accordingly, to maintain the SMR feed stream at high temperatures, a gas cleanup unit is provided that operates at process pressures and at a temperature above the boiling point of water (or above the steam condensation point). The unit is located between the SHR and SMR. 
     More particularly, a process is provided for converting carbonaceous material to synthesis gas of a desired H 2 /CO ratio, comprising simultaneously heating carbonaceous material in an SHR in the presence of a predetermined ratio of hydrogen and water in the form of steam, at a temperature and pressure sufficient to generate a stream of methane and carbon monoxide rich gas product, which can be called a producer gas, the ratio of hydrogen and water being determined by a modeling program, such as the ASPEN PLUS™ equilibrium process. In accordance with the invention, by varying the parameters of solid to water ratio and hydrogen to carbon ratio, a sensitivity analysis is performed that enables one determine the optimum composition of the slurry feedstock to the SHR to obtain a desired syngas ratio output of the SMR. Impurities are removed from the producer gas stream substantially at the process temperature and pressure, and the resultant producer gas is subjected to steam methane reforming in an SMR under conditions whereby synthesis gas comprising hydrogen and carbon monoxide is generated having a hydrogen/carbon monoxide ratio determined by the ratio of hydrogen and water in the SHR. 
     In a specific process, for converting municipal waste, biomass, wood, coal, biosolids, or a natural or synthetic polymer to synthesis gas, the carbonaceous material is simultaneously heated in the presence of both hydrogen and steam, at a temperature of about 700° C. to about 900° C. and pressure about 132 psi to 560 psi whereby to generate a stream of methane and carbon monoxide rich producer gas. Steam can come from the feedstock or introduced separately. Impurities are removed from the producer gas stream substantially at the process temperature and pressure, following which the resultant producer gas is subjected to steam methane reforming under conditions whereby to generate the desired synthesis gas ratio of hydrogen and carbon monoxide. For example, the required H 2 :CO mole ratio of a Fischer-Tropsch type reactor with a cobalt based catalyst is 2.1:1. By appropriate adjustment, as described below, of the H 2 /H 2 O ratio, a H 2 /CO mole ratio range of about 3 to 1 can be achieved to provide an excess of hydrogen, which can be fed into the SHR to make a self-sustainable process, i.e., without requiring any external hydrogen feed. The synthesis gas generated by the steam methane reforming can be fed into a Fischer-Tropsch type reactor under conditions whereby a liquid fuel is produced. Exothermic heat from the Fischer-Tropsch type reaction can be transferred to the hydro-gasification reaction and/or steam methane reforming reaction. 
     In one embodiment, the hydrogen is obtained by diverting a portion of hydrogen separated from the synthesis gas to the slurry water. In another, preferred embodiment, the hydrogen is obtained by diverting a portion of the synthesis gas itself to the slurry water, without separation of hydrogen from the synthesis gas. By controlled recycling, using a portion of the synthesis gas, a steady state desired H 2 /H 2 O ratio is obtained, which occurs quite rapidly. 
     Example 1 
       FIG. 1  is a flow diagram a SHR to SMR process one embodiment of the invention in which a desired H 2 /CO ratio output of an SMR is obtained by separating hydrogen from the SMR output, diverting it to the HGR, and adjusting the hydrogen feed and the water content of feedstock into the SHR that supplies the SMR. An internally generated hydrogen feed  10  is fed into an SHR  12  along with a carbonaceous feedstock  14  and water  16 , which are heated to 750° C. at 400 psi in the SHR  12 . The resulting producer gas is directed to a gas clean up filter  18 , e.g. a candle filter assembly, at about 350° C. at about 400 psi. From there, after removal of sulfur and ash, the effluent is directed to an SMR  20  where synthesis gas is generated and fed to a Fischer-Tropsch type reactor  22 , from which pure water  24 , and diesel fuel and/or wax  26  is obtained. The SMR  20  output is passed through a hydrogen separator  27  where a portion of its hydrogen is separated and diverted from the SMR  20 , at  28  to be fed back to the HGR  12 . Heat  30  from the Fischer-Tropsch type reactor  22  is used to supplement the heat at the SMR. 
     Operating the unit above the bubbling temperature of the water allows the water to be present as steam in the gaseous product stream from the SHR, thereby enabling the process to retain most of the sensible heat in the effluent stream. The following example will illustrate the invention. 
     A mass balance process flow diagram is shown in  FIG. 2 . The mass percentages of the product stream at each stage of the process are provided in the figure. ASPEN PLUS™ equilibrium process modeling was used to calculate these values. ASPEN PLUS™ is a commercial computer modeling program that allows a process model to be created by specifying the chemical components and operating conditions. The program takes all of the specifications and simulates the model, executing all necessary calculations needed to solve the outcome of the system, hence predicting its behavior. When the calculations are complete, ASPEN PLUS™ lists the results, stream by stream and unit by unit, and can present the data in graphical form with determining ordinate and abscissa. 
     As shown in  FIG. 2 , an SHR feedstock of hydrogen and 41% coal slurry results in the production of synthesis gas with a 3.4:1 mole ratio of hydrogen to carbon monoxide in the SMR. The required feed hydrogen for the SHR can be supplied through external means or by internal feedback of a portion of the hydrogen produced in the SMR. In a particular example, a slurry of 41% coal, 52% water and 7% hydrogen is used, obtained following the procedures of Norbeck et al. U.S. Ser. No. 10/911,348. This results in an output from the SHR to the cleanup filter of a gaseous mixture containing 32 wt % CH 4 , 2 wt % H 2 , 2 wt % Co, 3 wt % CO 2 , 51 wt % H 2 O, 4 wt % ash, 5 wt % char, and 1 wt % other impurities. 
     The output of the SHR-cleanup unit is a methane rich, producer gas containing 36 wt % CH 4 , 2 wt % H 2 , 2 wt % CO, 3 wt % CO 21  and 57 wt % H 2 O, having a steam to methane mole ratio of 1:4. The output of the SHR is fed to the SMR, which is operating at 800° C. and 28 atmospheres to yield synthesis gas having a mole ratio of H 2  to CO of 3.4, and containing 4 wt % CH 4 , 14 wt % H 2 , 58 wt % CO, 3 Wt % CO 2 , and 21 wt % H 2 O. 
     Example 2 
     This Example, shown in  FIGS. 3-6 , illustrates a second, preferred embodiment in which a portion of the output of the SMR is itself recycled.  FIG. 3  is flow diagram of the SHR to SMR process in which a desired H 2 /CO ratio output of an SMR is obtained by without separating hydrogen from the SMR output, but diverting a portion of the SMR output itself to the HGR, and adjusting the hydrogen feed and the water content of feedstock into the SHR that supplies the SMR. The process is the same as described in Example 1 but for those changes reflecting the direct use of a portion of the SMR as feed to the SHR. Accordingly, while some hydrogen is used to start the process, as shown in  FIG. 4 , discussed below, internally generated hydrogen feed is that component of the SMR output, as shown at  10   a  in  FIG. 3 . As in Example 1, the SMR portion  10   a  is fed into an SHR  12  along with a carbonaceous feedstock  14  and water  16 , which are heated to 750° C. at 400 psi in the SHR  12 . The resulting producer gas is directed to the gas clean up filter  18 , and from there, after removal of sulfur and ash, the effluent is directed to the SMR  20  where synthesis gas is generated and fed to a Fischer-Tropsch type reactor  22 , from which pure water  24 , and diesel fuel and/or wax  26  is obtained. 
     In contrast to Example 1, the SMR  20  output is not passed through a hydrogen separator, but a portion, indicated at  28   a  is directly diverted from the SMR  20  to be fed back to the HGR  12 . As in Example 1, heat  30  from the Fischer-Tropsch type reactor  22  is used to supplement the heat at the SMR. 
     A mass balance process flow diagram for the initial run is shown in  FIG. 4 . As in Example 1, the mass percentages of the product stream at each stage of the process are provided in the figure, obtained using ASPEN PLUS™ equilibrium process modeling. 
     As shown in  FIG. 4 , an initial SHR slurry feedstock containing 4% hydrogen, 32% coal, and 64% water results in the production of synthesis gas with a 3.8:1 mole ratio of hydrogen to carbon monoxide in the SMR. This results in an output from the SHR to the cleanup filter of a gaseous mixture containing 16 wt % CH 4 , 3 wt % H 2 , 5 wt % CO, 23 wt % CO 2 , 48 wt % H 2 O, 2 wt % ash, 2 wt % char, and 0 wt % other impurities. 
     The output of the SHR-cleanup unit is a gas containing 17 wt % CH 4 , 3 wt % H 2 , 5 wt % CO, 24 wt % CO 2 , and 51 wt % H 2 O, having a steam to methane mole ratio of 2:7. The output of the SHR is fed to the SMR, which is operating at 850° C. and 27.2 atmospheres to yield synthesis gas having a mole ratio of H 2  to CO of 3.8, and containing 5 wt % CH 4 , 8 wt % H 2 , 28 wt % CO, 21 wt % CO 2 , and 39 wt % H 2 O. 
       FIG. 5  shows a mass balance flow diagram after 12 recycle runs where it reached a final steady H 2 /CO exit ratio. The steady state feedstock contained 3% hydrogen, 21% coal, 42% water, 19% CO, 13% CO 2 , and 2% CH 4 , resulting in the production of synthesis gas with a 1.9:1 mole ratio of hydrogen to carbon monoxide in the SMR. This results in an output from the SHR to the cleanup filter of a gaseous mixture containing 16 wt % CH 4 , 2 wt % H 2 , 8 wt % CO, 43 wt % CO 2 , 29 wt % H 2 O, 1 wt % ash, 2 wt % char, and 0 wt % other impurities. 
     The output of the SHR-cleanup unit is a gas containing 16 wt % CH 4 , 2 wt % H 2 , 9 wt % CO, 44 wt % CO 2 , and 30 wt % H 2 O, having a steam to methane mole ratio of 1.6. The output of the SHR is fed to the SMR to yield synthesis gas having a mole ratio of H 2  to CO of 1.9, and containing 5 wt % CH 4 , 5 wt % H 2 , 39 wt % CO, 26 wt % CO 2 , and 24 wt % H 2 O. 
       FIG. 6  shows the H 2 /CO and steam/CH 2  molar ratios for each run until after steady values are achieved. This diagram demonstrates the ability of the process of this preferred embodiment to produce synthesis gas at a desired H 2 /CO ratio through controlled recycling of a fraction of the SMR product stream. 
     In these examples, the filter is operating at 300° C. and 28 atmospheres of pressure. Any filter capable of operating at the process temperature can be used at the gas cleanup station. One such commercially available filter is a candle filter, which is well known to the art. See, for example U.S. Pat. No. 5,474,586, the disclosure of which is incorporated herein by reference. An available gas cleanup unit that can be used in this invention is what is known as a candle filter in which a series of candle-shaped filters are carried in a filter vessel. The candle filters are made of stainless steel metal frit to remove fine particulate matter (ash, inorganic salts and unreacted char) from the gas stream. The slurry is fed into the vessel at a bottom inlet and filtrate is taken out at a top outlet. Particulate matter is taken from another outlet as cake. Sulfur impurities existing in the SHR product gas, mostly in the form of hydrogen sulfide, are removed by passing the product gas through a packed bed of metal oxide sorbents in the gas cleanup unit, particulate matter being taken from a cake outlet. 
     Active sorbents include, but are not limited to, Zn based oxides such as zinc oxide, sold by Sod-Chemie, Louisville, Ky. Porous metal filter elements are available from Bekaert in Marietta, Ga. in the appropriate forms and sizes, such as BEKPOR® Porous Media—which is made from stainless steel sintered fiber matrix with a pore size of 1. These sorbents and filter elements allow the effects of pressure drop and gas-solid mass transfer limitations to be minimized. At a pressure of 28 atm., temperatures in the range of 300° C. to 500° C. and space velocities up to 2000/hr have been used in the desulphurization of SHR product gas. The hydrogen sulfide content of the gas is diminished by means of sulfidation of the sorbents to levels low enough to avoid the deactivation of the SMR catalyst. The used sorbents in the gas cleanup unit can either be replaced with fresh sorbents or regenerated in-situ with diluted air in parallel multiple sorbent beds. 
     As described, the syngas ratio obtained from the SMR can be adjusted by varying the solid to water ratio and hydrogen to carbon ratio in the SHR feedstock. Sensitivity analysis was performed using the ASPEN PLUS™ equilibrium modeling tool by varying these parameters. The results are in  FIG. 7 , showing various conversions and the syngas ratio when parameters of solid to water ratio and hydrogen to carbon ratio are varied. The solid lines             represent the percentage of carbon converted to CH 4  (mole CH 4 /mole C in ). The long dashed lines           represent the percentage of carbon converted to CO (mole CO/mole C in ). The dotted lines           represent the percentage of carbon converted to CO 2  (mole CO 2 /mole C in ). The dash-dot-dot-dash lines           represent sustainable H 2 , and the short dashed lines           represent the syngas ratio of H 2 /CO (mole H 2 /mole CO). The H2/C ratio of the feed is always on a molar basis and the H2O/Feed ratio is always on mass basis.
     The last parameter is of key interest in this invention.  FIG. 7  clearly demonstrates that the final syngas ratio can be adjusted by adjusting the water to solid ratio (represented as H 2 O/C mass ratio in  FIG. 7 ) and the hydrogen to carbon ratio of the feedstock. Thus, an optimum composition of the slurry to obtain a sustainable hydrogen feedback and the desired syngas ratio for the Fischer-Tropsch synthesis (2.1:1) was found to be 3.1 when the mole ratio of hydrogen to carbon in the feed was set to one. 
       FIG. 8  shows the H 2 :CO ratio of the SMR product stream being varied by changing the H 2 /C and H 2 O/wood ratios of the wood feed. For instance, to obtain a desired syngas ratio of about 6:1, a 2:1 ratio of H 2 /C and 2:1 ratio of H 2 O/wood of the feed can be used; alternatively, the same syngas ratio can be obtained using a 1:1 ratio of H 2 /C and 3:1 ratio of H 2 O/wood of the wood feed.  FIG. 9  shows the H 2 :CO ratio of the SMR product stream being varied by changing the H 2 /C and H 2 O/coal ratios of the coal feed. 
     For simulations performed, the results of which are shown in  FIGS. 8 and 9 , the temperature of the SHR and SMR was set to be 850° C. All the reactors were at a pressure of 400 psi. The H 2 /CO ratios shown in these figures are calculated before the separation of excess H 2  for recycle to the SHR. 
     Similar syngas ratio predeterminations can be made using other carbonaceous material feedstocks such as, but not limited to, municipal waste, biomass, biosludge, or a natural or synthetic polymer. Here, the H 2 /C ratio of the feed is always on a molar basis and the H 2 O/Feed ratio is always on mass basis. 
     More generally, the process of this invention can produce composition of synthesis gas having a H 2 :CO mole ratio range of about 0.5:1 to 16:1. The resulting effluent is a synthesis of gases rich in hydrogen, carbon monoxide, and steam. Hydrogen produced in the SMR is recycled back to the HGR. Consequently, no outside source of hydrogen is needed to maintain steady state operation. The HGR and SMR processes, therefore, may be considered to be chemically self-sustaining. The remaining synthesis gas is then available for the production of fuels and process heat. 
     In an embodiment of the invention, the synthesis gas is fed to a Fischer-Tropsch reactor in a process that can produce a zero-sulfur, ultrahigh cetane value diesel-like fuel and valuable paraffin wax products. The absence of sulfur enables low pollutant and particle emitting diesel fuels to be realized. Useful by-products can be produced, foe example, purified water, which can be re-cycled to create the slurry feed into the process. The Fischer-Tropsch reactions also produce tail gas that contains hydrogen, CO, CO 2 , and some light hydrocarbon gases. Hydrogen can be stripped out of the tail gas and recycled either to the HGR or the Fischer-Tropsch reactor. Any small amounts of other gases such as CO and CO may be flared off. 
     In yet another embodiment, this invention provides an improved process scheme that can enhance the operability of hot gas cleanup of steam-hydrogasification producer gas by insertion of an autothermal reforming of methane and steam removal by condensation step prior to the hot gas cleanup step. 
     The improved process scheme can be used where there are separate steam pyrolysis and hydro-gasification reactors, followed by an autothermal reforming reactor, in a process for producing a synthesis gas for use as fuel for process heat and/or in a fuel engine or gas turbine that can generate electricity; or as feed into a Fischer-Tropsch type reactor to produce a liquid paraffinic fuel, recycled water and sensible heat, in a substantially self-sustaining process. 
     Preferably, the improved process scheme is used with a steam hydro-gasification reactor (SHR) in which carbonaceous material is heated in the presence of both hydrogen and steam to undergo steam pyrolysis and hydro-gasification in a single step. 
     In other embodiments, this additional step can be used in any process where methane rich gas is produced. 
     In order to adopt this improved process that incorporates autothermal reforming of methane and steam removal by condensation, a number of requirements have to be met: (i) the catalyst used for autothermal reforming of methane should be able to maintain activity for methane reforming satisfactorily in high-sulfur environment, and (ii) the temperature for steam condensation prior to hot gas cleanup should not be significantly lower than that for hot gas cleanup at the operating pressure so as to enable modest amounts of heat to be added to bring the resultant gas stream up to substantially the temperature of the hot gas cleanup. 
     In the preferred embodiment, the first step in the improved process involves feeding hydrogen, internally generated, into a SHR along with a carbonaceous feedstock and liquid water. The resultant producer gas, which is rich in methane, enters the autothermal reforming reactor. Oxygen diluted with nitrogen is separately fed to the autothermal reforming reactor: oxygen content needs to be preferably about 15% volm to 25% volm. 
     Within the autothermal reforming reactor, noble metal catalysts are preferably used. Compared with the nickel-based catalysts used for steam reforming of methane, noble metal catalysts used for autothermal reforming of methane are known to have higher activity and superior sulfur-resistance as well as regenerability. Therefore, methane-rich gas produced from steam-hydrogasification can be reformed with the increased operability by means of autothermal reforming: the methane-rich gas containing high concentration of hydrogen sulfide can be reformed to synthesis gas for extended time on stream and the used catalyst can be regenerated in an inert gas atmosphere. Examples of noble metal catalysts which can be used are Engelhard&#39;s ATR-7B and Haldor Topsoe&#39;s RKS-2-7H or RKS-2P. 
     After the autothermal reforming of methane, steam can be removed from the process by condensation at a temperatures not substantially lower than that for hot gas cleanup. In the case of 28 bar operating pressure, steam condenses to water at 230° C., which can then be removed from the process stream before it is fed to the stage of hot gas cleanup. By removing the steam prior to hot gas cleanup, the sulfur capture capacity of the metal oxide sorbents used in the hot gas clean up stage can be fully utilized; and the energy load required to reheat the process stream for hot gas cleanup can be lowered to a great extent as the specific heat of the process stream decreases significantly due to steam removal. For example, optimum temperature for hot gas cleanup by ZnO sorbent is around 300° C., therefore, the process stream cooled down to 230° C. for steam condensation needs to be reheated only by 70° C. 
     After removal of the steam, the resulting synthesis gas is directed to a hot gas cleanup process, as described above. 
     Once nitrogen is separated by a gas-separation device for being recycled to the autothermal reforming reactor, the resulting synthesis gas is then available for the production of fuels and process heat, or the synthesis gas is fed to a Fischer-Tropsch type reactor in a process that can produce a zero-sulfur, ultrahigh cetane value diesel-like fuel and valuable paraffin wax products. The absence of sulfur enables low pollutant and particle emitting diesel fuels to be realized. Useful by-products can be produced, for example, purified water, which can be recycled to create the slurry feed into the process. The Fischer-Tropsch reaction also produces tail gas that contains hydrogen, CO, CO 2 , and some light hydrocarbon gases. Hydrogen can be stripped out of the tail gas and recycled either to the SHR or the Fischer-Tropsch reactor. Any small amounts of other gases such as CO 2  and CO may be flared off. 
     Referring to  FIG. 10 , a schematic flow diagram of the process involving the autothermal and condensation step is shown. A mixture  10  of about coal 41% wt, H 2 0 52% wt, and H 2  7% wt is introduced into a reactor of steam pyrolysis and hydro-gasification  12  at a temperature of about 750° C., and a starting pressure of about 28.0 bar. This reaction produces a mixture  14  of H 2  15.3% (volm), CO 1.1% (volm), CO 2  1.0% (volm), CH 4  34.3% (volm), H 2 O 48.3% (volm), and H 2 S 1000 ppm, whereupon ash, the un-reacted residue from the hydro-gasification reaction, is periodically removed from the bottom of the reactor vessel. 
     At the next stage autothermal reforming of methane  18  occurs with the mixture  14  and a mixture  16  (in % volm) of oxygen 17% and nitrogen 83% at a temperature of about 550° C., and a starting pressure of about 28.0 bar, resulting in a mixture  20  (in % volm) of H 2  41.9%, CO 12.8%, CO 2  2.5%, CH 4  1.8%, H 2 O 13.7%, N 2  27.3%, and H 2 S 550 ppm. The volume ratio of the mixture  16  to the mixture  14  is about 0.41. 
     Steam is then removed by condensation at stage  22  at a temperature of about 230° C., and a starting pressure of about 28.0 bar. The water resulting from the condensation of steam is then removed from the process stream before the hot gas clean up stage  26 , leaving a mixture  24  (in % volm) of H 2  48.6%, CO 14.8%, CO 2  2.9%, CH 4  2.1%, N 2  31.6%, and H 2 S 640 ppm. This mixture  24  enters the hot gas clean up stage  26  where a temperature of about 300° C., and a starting pressure of about 28.0 bar is applied to produce a desulfurized gas mixture  28  (in % volm) of H 2  48.6%, CO 14.8%, CO 2  2.9%, CH 4  2.1%, N 2  31.6%, and H 2 S less than 0.1 ppm. 
     Although the present invention and its advantages have been described in detail, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims. Moreover, the scope of the present application is not intended to be limited to the particular embodiments of the process and apparatus described in the specification. As one of ordinary skill in the art will readily appreciate from the disclosure of the present invention, processes and apparatuses, presently existing or later to be developed that perform substantially the same function or achieve substantially the same result as the corresponding embodiments described herein may be utilized according to the present invention. Accordingly, the appended claims are intended to include such processes and use of such apparatuses within their scope. 
     REFERENCES 
     
         
         1. Van der Laan, G. P., Thesis, University of Groningen, Netherlands, 1999. 
         2. Sheldon, R. A., Chemicals from Synthesis Gas, 1983 and FT Technology: Studies in surf Science and Catalysis, ed. Steynberg, A., Dry, M. E., Vol 152, 2004.