Abstract:
A hydrogen production method that integrates a catalytic steam reformer and a gasifier. Hydrogen is generated in a catalytic steam reformer at a high production rate or design capacity. The catalytic steam reformer is then turned down to a fraction of design capacity while a gasifier produces the needed hydrogen. During the turned down state of the catalytic steam reformer, more of a hydrogen-containing stream formed from gasifier effluent is fed to the catalytic steam reformer as a feed thereby reducing the flow rate of feedstock required for the catalytic steam reformer in the turned down state. Optionally, hydrogen mixtures from the catalytic steam reformer and gasifier are fed to one or more adsorbers for hydrogen purification and adsorber effluent is fired as fuel in the steam reformer furnace to provide a majority of the heat needed for the reforming reaction.

Description:
BACKGROUND 
     The present invention relates generally to hydrogen production and more specifically to a method for producing hydrogen from catalytic steam reformers and gasifiers. 
     Upgrading of heavy oil into more valuable products usually requires large quantities of hydrogen. Traditionally, this hydrogen is generated by catalytically reacting natural gas and steam in a so-called steam-methane reformer (SMR). More recently, refiners engaged in upgrading projects are considering gasification of petroleum coke or heavy oil as a more cost effective means for generating the large quantities of hydrogen required. This is being driven by the increased cost of natural gas compared to the low cost of a gasifier feedstock. 
     In steam-methane reforming, natural gas or other suitable feedstock is mixed with an appropriate amount of process steam and heated as it flows through catalyst filled tubes contained within the steam-methane reformer furnace. In the reformer tubes, a portion of the process steam and most of the natural gas feed is converted to synthesis gas (syngas), which contains primarily hydrogen, carbon monoxide and unreacted steam along with lesser amounts of carbon dioxide and unreacted methane. 
     The hot synthesis gas stream from the reformer tubes is cooled to recover valuable waste heat, which is used to preheat the feed and to generate steam needed for the steam reforming process. In the cooling operation, the reformer effluent is generally passed over one or more beds of water-gas shift catalyst to convert most of the carbon monoxide contained in the synthesis gas to additional hydrogen and carbon dioxide. The synthesis gas is cooled to near ambient temperatures to condense unreacted excess steam so that it can be separated from the raw hydrogen stream prior to sending the stream to a pressure swing adsorption unit (PSA) for product purification. 
     The PSA produces a purified hydrogen product stream and a PSA desorption effluent or tail gas stream. The tail gas contains unrecovered hydrogen along with other impurities contained in the PSA feed, including carbon monoxide, carbon dioxide, methane and nitrogen. This tail gas stream is typically fired as fuel in the steam reformer furnace to provide the majority of the heat needed to drive the endothermic reforming reaction. Additional heat is provided by also firing a supplemental fuel such as natural gas or refinery fuel gas. The hot flue gas generated in the steam reforming furnace is also cooled to recover waste heat used for preheating steam reformer feed, generating steam and preheating combustion air. 
     In gasification processes, a suitable hydrocarbon feedstock such as coal, petroleum coke or heavy oil is prepared and fed to one or more gasifiers. In the gasifier vessel, the feedstock is heated and reacted with oxygen to generate a syngas containing predominantly carbon monoxide and hydrogen with lesser amounts of methane, carbon dioxide, nitrogen, argon, steam and sulfur compounds. The gasifier effluent can be quenched via direct injection of water or can be cooled by generating steam in heat recovery equipment. 
     Since the gasifier effluent contains a significant amount of carbon monoxide, the synthesis gas stream is passed over multiple beds of sulfur-tolerant shift catalyst to convert a portion of the carbon monoxide to hydrogen via the water-gas shift reaction. 
     Additional waste heat generated by the exothermic shift reaction is recovered in the shift section. The shifted synthesis gas is then routed to an acid gas removal unit (AGR) for removal of sulfur and carbon dioxide contained in the synthesis gas. The raw hydrogen stream from the acid gas removal unit is fed to a PSA for purification of the hydrogen product. 
     Alternatively, the acid gas removal unit may remove the sulfur compounds, followed by a water-gas shift, followed by either a CO 2  removal AGR and a PSA. 
     There has been much activity recently related to expansion of the Canadian oil sands operations, primarily to upgrade the bitumen or heavy oil contained in the oil sands to a more valuable synthetic crude oil. Since the upgrading process usually consumes large quantities of hydrogen, refiners must choose between the steam reforming process or the gasification process as the means to produce the hydrogen. 
     In the Fort Hill Sturgeon Upgrader project by Petro-Canada Oil Sands Inc., the refiner is planning on installing steam reformers fed with natural gas to provide a reliable supply of hydrogen for the initial phase(s) of the expansion as discussed in the Application for Approval of Fort Hills Sturgeon Upgrader, Vol. 1, Project Description, Section 2 Processing Facilities, subsection 2.5.2.7 Gasification Unit, Dec. 2006. As the expansion progresses to subsequent phases and heavy oil, asphaltene or petroleum coke becomes available, the refiner plans to install gasifiers to supply essentially all of the hydrogen required for the full expansion. The steam reformer hydrogen plant constructed in Phase 1 will be operated at minimum throughput to reduce the import of natural gas. The Gasification unit will provide the remainder of the total 410,000 Nm 3 /h hydrogen during Phases 2 and 3. During periods of gasification unit maintenance outages and other operation interruptions, the steam reformer hydrogen plant will be ramped up to meet the hydrogen demand, which will eliminate the need for a spare gasification unit train. The gasification unit allows for potential future CO 2  recovery and sequestration. 
     The problem of operating the catalytic steam reformer even at deep turndown is that it will continue to consume costly feedstock such as natural gas. 
     It would be desirable to reduce the consumption of catalytic steam reformer feedstock and/or feedstock used as fuel during turndown and/or deep turndown of the catalytic steam reformer. 
     BRIEF SUMMARY 
     The present invention relates to a hydrogen production method which integrates a catalytic steam reformer and a gasifier. 
     The hydrogen production method comprises generating hydrogen in a gasifier thereby forming a gasifier effluent, and forming a hydrogen-containing mixture and a first adsorber feed from at least a portion of the gasifier effluent. The method further comprises introducing the hydrogen-containing mixture into a catalytic steam reformer at a first hydrogen-containing mixture volumetric flow rate and generating hydrogen in the catalytic steam reformer at a first hydrogen production rate thereby forming a catalytic steam reformer effluent. The method further comprises introducing the hydrogen-containing mixture into the catalytic steam reformer at a second hydrogen-containing mixture flow rate and generating hydrogen in the catalytic steam reformer at a second hydrogen production rate. The second hydrogen production rate is less than the first hydrogen production rate and the second hydrogen-containing mixture volumetric flow rate is greater than the first hydrogen-containing mixture volumetric flow rate. The first hydrogen-containing mixture volumetric flow rate may be zero. 
     The second hydrogen production rate may be 5% to 50%, or 5% to 40%, or 5% to 25%, or 5% to 15% of the first hydrogen production rate. 
     The second hydrogen-containing mixture volumetric flow rate may be 25% to 150% of the second hydrogen production rate. 
     The second hydrogen-containing mixture volumetric flow rate may be at least 1×10 6  normal cubic feet per day greater than the first hydrogen-containing mixture volumetric flow rate. 
     The step of forming the hydrogen-containing mixture and the first adsorber feed may comprise introducing the gasifier effluent into a first shift converter to form a first shift converter effluent from the gasifier effluent, taking a first portion of the first shift converter effluent for forming the hydrogen-containing mixture, and taking a second portion of the first shift converter effluent for forming the first adsorber feed. 
     The step of forming the hydrogen-containing mixture and the first adsorber feed may comprise introducing the gasifier effluent into a first shift converter to form a first shift converter effluent from the gasifier effluent, introducing the first shift converter effluent into an acid gas removal unit to form an acid gas removal unit effluent from the first shift converter effluent, taking a first portion of the acid gas removal unit effluent for forming the hydrogen-containing mixture, and taking a second portion of the acid gas removal unit effluent for forming the first adsorber feed. 
     The step of forming the hydrogen-containing mixture and the first adsorber feed may comprise introducing the gasifier effluent into an acid gas removal unit to form an acid gas removal unit effluent from the gasifier effluent, introducing the acid gas removal unit effluent into a first shift converter to form a first shift converter effluent from the acid gas removal unit effluent, taking a first portion of the first shift converter effluent for forming the hydrogen-containing mixture, and taking a second portion of the first shift converter effluent for forming the first adsorber feed. 
     The method may further comprise introducing the first adsorber feed into a first adsorber to form a first hydrogen product and a first desorption effluent, and introducing at least a portion of the first desorption effluent into the catalytic steam reformer as at least a portion of a catalytic steam reformer fuel. 
     The catalytic steam reformer fuel may consist essentially of the first desorption effluent. 
     The method may further comprise forming a second adsorber feed from at least a portion of the catalytic steam reformer effluent, introducing the second adsorber feed into a second adsorber thereby forming a second hydrogen product and a second desorption effluent, and introducing at least a portion of the second desorption effluent into the catalytic steam reformer as a second portion of the catalytic steam reformer fuel. 
     The method may further comprise forming a second adsorber feed from at least a portion of the catalytic steam reformer effluent, introducing the first adsorber feed and the second adsorber feed into a common adsorber to form a hydrogen product and a desorption effluent, and introducing at least a portion of the desorption effluent into the catalytic steam reformer as a portion of a catalytic steam reformer fuel. 
     The step of forming the second adsorber feed may comprise introducing the catalytic steam reformer effluent into a second shift converter to form a second shift converter effluent from the catalytic steam reformer effluent, and taking at least a portion of the second shift converter effluent for forming the second adsorber feed. 
    
    
     
       BRIEF DESCRIPTION OF SEVERAL VIEWS OF THE DRAWINGS 
         FIG. 1  is a schematic of a facility suitable for carrying out the method. 
     
    
    
     DETAILED DESCRIPTION 
     The indefinite articles “a” and “an” as used herein mean one or more when applied to any feature in embodiments of the present invention described in the specification and claims. The use of “a” and “an” does not limit the meaning to a single feature unless such a limit is specifically stated. The definite article “the” preceding singular or plural nouns or noun phrases denotes a particular specified feature or particular specified features and may have a singular or plural connotation depending upon the context in which it is used. The adjective “any” means one, some, or all indiscriminately of whatever quantity. 
     For the purposes of simplicity and clarity, detailed descriptions of well-known devices, circuits, and methods are omitted so as not to obscure the description of the present invention with unnecessary detail. 
     The present invention relates to a hydrogen production method which integrates a catalytic steam reformer and a gasifier. 
     Catalytic steam reforming, also called steam methane reforming (SMR) or steam reforming, is defined as any process used to convert reformer feedstock to synthesis gas by reaction with steam over a catalyst. Synthesis gas, commonly called syngas, is a mixture comprising hydrogen and carbon monoxide. 
     A catalytic steam reformer, also called a steam methane reformer, is defined herein as any fired furnace used to convert feedstock containing elemental hydrogen and carbon to synthesis gas by a reaction with steam over a catalyst with heat provided by combustion of a fuel. Feedstock may be natural gas, methane, naphtha, propane, refinery offgas, or other suitable reformer feedstock. A catalytic steam reformer may have a plurality of catalyst-containing reformer tubes through which the reformer feed gas mixture is passed to form a reformed gas mixture comprising hydrogen. As used herein, plurality means at least two. Catalyst-containing reformer tubes have been loaded with suitable catalyst known in the art. Suitable catalysts for reforming reformer feedstock are known in the art. Suitable materials for making reformer tubes are known in the art. Suitable operating temperatures and pressures for a catalytic steam reformer are known in the art. 
     A gasifier, also called a partial oxidation reactor, is defined herein as any reactor in which the partial oxidation of a feedstock takes place, converting the feedstock into synthesis gas. Partial oxidation reactors are well known in the art, as are the partial oxidation reaction conditions. See, for example, U.S. Pat. Nos. 4,328,006, 4,959,080 and 5,281,243, all incorporated herein by reference. The feedstock of a gasifier is reacted with an oxygen-containing gas, such as air, enriched air, or nearly pure oxygen, and a temperature modifier, such as water or steam, in a gasifier to produce the synthesis gas. The oxygen is used to partially oxidize the carbon in the feedstock into primarily carbon monoxide and hydrogen gas. The temperature modifier is used to control the temperature inside the gasifier. Together, the oxygen and the temperature modifier can impact the composition of the synthesis gas. The feedstock for the gasifier may be petroleum coke, bitumen or heavy oil from tar sands, coal or other suitable feedstock known in the art. 
     The method will be described with reference to  FIG. 1 . 
     The method comprises generating hydrogen in a gasifier  10  thereby forming a gasifier effluent  12 . The method further comprises forming a hydrogen-containing mixture  32  and an adsorber feed  36  from at least a portion of the gasifier effluent  12 . The hydrogen-containing mixture  32  may be taken from any location downstream of the gasifier  10 . Feed stream  8  comprises gasifier feedstock, oxidant, and water or steam. 
     Forming may include a combination of various steps, for example, mixing, reacting, heating, cooling, compressing, expanding, throttling, separating, etc. A mixture is formed from a first gas and a second gas if the mixture comprises one or more elemental constituents from the first gas and one or more elemental constituents from the second gas. For example, a mixture comprising elemental carbon and/or elemental hydrogen from a methane-containing first gas and elemental hydrogen and/or elemental oxygen from a water-containing second gas is formed from the methane-containing first gas and the water-containing second gas. The mixture may comprise the element carbon and element hydrogen as methane from the methane-containing first gas and the element hydrogen and the element oxygen as water from the water-containing second gas. Or the methane-containing first gas and the water-containing second gas may be reacted so that the mixture comprises the element carbon from the methane-containing first gas and element oxygen from the water-containing second gas as carbon dioxide. 
     A first mixture is formed from a second mixture if the first mixture comprises one or more elemental constituents from the second mixture. For example, a first mixture comprising elemental carbon, elemental hydrogen, and elemental oxygen as carbon dioxide and hydrogen may be formed from via a shift reaction of a second mixture comprising elemental carbon, elemental hydrogen and elemental oxygen as carbon monoxide and water. 
     The step of forming hydrogen-containing mixture  32  and adsorber feed  36  may comprise introducing gasifier effluent  12  into shift converter  20  to form shift converter effluent  22  from gasifier effluent  12 , introducing shift converter effluent  22  into acid gas removal unit  30  to form acid gas removal unit effluent  34  from shift converter effluent  22 , taking a first portion of acid gas removal unit effluent  34  for forming the hydrogen-containing mixture  32 , and taking a second portion of acid gas removal unit effluent  34  for forming adsorber feed  36 . 
     A shift converter may comprise one or more shift reactors in parallel or in series each containing various shift catalysts, each active in different temperature ranges. Suitable arrangements of high temperature shift, medium temperature shift, and low temperature shift may be used and may be determined without undue experimentation. 
     Alternatively, the step of forming the hydrogen-containing mixture  32  and adsorber feed  36  may comprise introducing gasifier effluent  12  into shift converter  20  to form shift converter effluent  22  from the gasifier effluent  12 , taking a first portion of shift converter effluent  22  for forming the hydrogen-containing mixture, and taking a second portion of shift converter effluent  22  for forming adsorber feed  36 . The first portion of the shift converter effluent may be passed to acid gas removal unit  30 . The second portion of the shift converter effluent may be passed to another acid gas removal unit (not shown). 
     A shift reactor is defined as any device where carbon monoxide reacts with water to form hydrogen and carbon dioxide in the presence of a catalyst. Any suitable shift reactor may be used and may be selected without undue experimentation. Shift reactors are well known in the art. 
     An acid gas removal unit is any device or system for removing at least a portion of the carbon dioxide and hydrogen sulfide, if present. Acid gas removal units are well known in the art, for example, amine gas treating, the Selexol process (licensed by UOP LLC), and the Rectisol process (licensed by Lurgi AG). 
     Amine gas treating refers to a group of processes that use aqueous solutions of various amines to remove hydrogen sulfide and carbon dioxide from gases. It is a common unit process used in refineries, petrochemical plants, natural gas processing plants and other industries. Various amines may be used, for example, monoethanolamine (MEA), diethanolamine (DEA), methyl diethanolamine (MDEA), diisopropylamine (DIPA), and diglycolamine (DGA). 
     Selexol, and Rectisol are physical solvents that dissolves (absorbs) the acid gases from the gas. The Selexol solvent is a mixture of the dimethyl ethers of polyethylene glycol. Rectisol uses methanol as the solvent. 
     One skilled in the art may readily select a suitable acid gas removal unit. 
     Shift converter  20  may precede acid gas removal unit  30 , as shown, or acid gas removal unit  30  may precede the shift converter  20 . 
     The method further comprises introducing hydrogen-containing mixture  32  into catalytic steam reformer  50  at a first hydrogen-containing mixture volumetric flow rate and generating hydrogen in catalytic steam reformer  50  at a first hydrogen production rate thereby forming catalytic steam reformer effluent  52 . The first hydrogen production rate may correspond to about the full production rate or design production rate. Full production may be required prior to commissioning a gasifier or during repair or routine maintenance of a gasifier. For the purposes of this disclosure, the hydrogen production rate is the volumetric flow rate of hydrogen leaving the catalytic steam reformer. The volumetric flow rate of hydrogen may be determined based on a measurement of the hydrogen mole fraction and the total volumetric flow rate. 
     The first hydrogen-containing mixture volumetric flow rate may be zero. There may be no flow of the hydrogen-containing mixture as a feed into the catalytic steam reformer at the first hydrogen production rate. The first hydrogen production rate may correspond to a condition where the gasifier is not yet on-stream and therefore no hydrogen-containing mixture is available. 
     Feed  6  comprising steam and catalytic steam reformer feedstock, separately or as a mixed feed, are introduced into catalytic steam reformer  50 . All or part of catalytic steam reformer fuel  54  may be provided by fuel stream  4 . Catalytic steam reformer fuel  54  is introduced into the catalytic steam reformer to provide heat by combustion of the fuel. Fuel  4  may be the same as the feedstock for feed  6 , e.g. natural gas. Various other combustible streams may be used to form catalytic steam reformer fuel  54  to provide heat by combustion. The various streams may be added together or separately. 
     The method further comprises introducing hydrogen-containing mixture  32  into catalytic steam reformer  50  at a second hydrogen-containing mixture flow rate and generating hydrogen in catalytic steam reformer  50  at a second hydrogen production rate. The second hydrogen production rate is less than the first hydrogen production rate and may correspond to turndown or deep turndown conditions. The second hydrogen production rate may be 5% to 50% or 5% to 40%, or 5% to 25%, or 5% to 15% of the first hydrogen production rate. 
     The method is characterized by a greater volumetric flow rate of the hydrogen-containing mixture  32  into catalytic steam reformer  50  when generating hydrogen in catalytic steam reformer  50  at the lesser second hydrogen production rate than when generating hydrogen in catalytic steam reformer  50  at the greater first hydrogen production rate. The second hydrogen production rate is less than the first hydrogen production rate and the second hydrogen-containing mixture volumetric flow rate is greater than the first hydrogen-containing mixture volumetric flow rate. 
     Hydrogen-containing mixture  32  may be introduced into catalytic steam reformer  50  along with the feedstock and steam to generate hydrogen by the reforming reaction over a reformer catalyst. 
     The second hydrogen-containing mixture volumetric flow rate may be 25% to 150% of the second hydrogen production rate. The greater volumetric flow rate may be at least 1×10 6  normal cubic feet per day greater than the first hydrogen-containing mixture volumetric flow rate. Normal conditions are 1 atmosphere pressure and 32° F. 
     The method may comprise one or more of the following characteristics, taken alone or in any possible technical combinations. 
     The method may further comprise introducing adsorber feed  36  into adsorber  40  to form hydrogen product  45  and desorption effluent  42  and introducing at least a portion of desorption effluent  42  into the catalytic steam reformer  50  as at least a portion of catalytic steam reformer fuel  54 . Desorption effluent  42  may provide some or all of the catalytic steam reformer fuel. Adsorber  40  may be any suitable adsorption type system, for example, a pressure swing adsorption system (PSA) or a vacuum swing adsorption system (VSA). Adsorbers are known in the art. The adsorber may comprise multiple vessels containing one or more adsorbent materials suitable for hydrogen separation. 
     Desorption effluent is commonly called tail gas. Desorption effluent is any gas withdrawn from the adsorber system during desorption of an adsorber bed, for example during purge and/or blowdown. 
     The catalytic steam reformer fuel may consist essentially of desorption effluent downstream of a gasifier, meaning that at least 95 volume % of the catalytic steam reformer fuel is desorption effluent from an adsorber that processes effluent from a gasifier. 
     The method may further comprise forming adsorber feed  68  from at least a portion of catalytic steam reformer effluent  52 , introducing adsorber feed  68  into adsorber  70  thereby forming hydrogen product  75  and desorption effluent  72 , and introducing at least a portion of desorption effluent  72  into catalytic steam reformer  50  as another portion of catalytic steam reformer fuel  54 . 
     The step of forming adsorber feed  68  may comprise introducing catalytic steam reformer effluent  52  into shift converter  60  to form shift converter effluent  62  from the catalytic steam reformer effluent  52 , and taking at least a portion of shift converter effluent  62  for forming adsorber feed  68 . 
     The catalytic steam reformer fuel may consist essentially of desorption effluent  42  and desorption effluent  72  meaning that at least 95 volume % of the catalytic steam reformer fuel is desorption effluent from an adsorber that processes effluent from a gasifier and desorption effluent from an adsorber that processes effluent from a catalytic steam reformer. 
     Shift converter  60  may comprise one or more vessels containing various shift catalysts, each active in different temperature ranges. 
     The method may further comprise introducing catalytic steam reformer effluent  52  into shift converter  60  to form shift converter effluent  62  from catalytic steam reformer effluent  52 , introducing shift converter effluent  62  into adsorber  70  thereby forming hydrogen product  75  and desorption effluent  72 , and introducing at least a portion of desorption effluent  72  into catalytic steam reformer  50  as a portion of a catalytic steam reformer fuel  54 . 
     The gasifier and the reformer may use a common adsorber. The method may further comprise forming adsorber feed  68  from at least a portion of catalytic steam reformer effluent  52 , introducing the adsorber feed  36  and adsorber  68  into a common adsorber to form hydrogen product and desorption effluent, and introducing at least a portion of the desorption effluent into the catalytic steam reformer as a portion of catalytic steam reformer fuel. 
     The step of forming adsorber feed  68  may comprise introducing catalytic steam reformer effluent  52  into shift converter  60  to form shift converter effluent  62  from the catalytic steam reformer effluent  52 , taking at least a portion of shift converter effluent  62  to form adsorber feed  68 . 
     The method may employ various heat recovery schemes. Heat recovery from catalytic steam reformers and shift reactors are well-known in the art. 
     EXAMPLE 
     Several simulations were carried out to show the benefit of the present method. 
     Table 1 provides an estimate of how much natural gas can be saved by using the present method. The values shown in the column for the design case presents the estimate of how much natural gas feed and fuel are consumed to operate the catalytic steam reformer (SMR) producing 165×10 6  standard cubic feet per day of hydrogen. The values shown in the column for turndown—100% nat. gas feed shows an estimate of how much natural gas feed and fuel are consumed to operate the catalytic steam reformer to produce only 33×10 6  standard cubic feet per day of hydrogen, representing a turndown to 20% of the design production rate. 
     The values in the column for turndown—gasifier hydrogen-containing mixture import with no PSA tail gas import show the estimated natural gas feed and fuel consumption associated with the use of 25×10 6  standard cubic feet per day of hydrogen-containing gas mixture from the gasifier as a portion of the catalytic steam reformer feed. Although the gross hydrogen production rate is reduced slightly in this case from 33 to 30.5×10 6  standard cubic feet per day, the natural gas feedstock is reduced by 67%. The natural gas fuel stream is also reduced by almost 10%. 
     Hydrogen-containing mixture import values are higher heating values (HHV). Natural gas consumption values are higher heating values (HHV). Reformer firing values are lower heating values (LHV). 
     The assumed concentration for the hydrogen-containing mixture from the gasifier was 93.0% H 2 , 2.0% CO 2 , 4.2% CO, 0.1% CH 4 , 0.2% Ar, 0.3% N 2 , and 0.2% H 2 O. This flow and composition results in a blended feed (including nat. gas feed) H 2  concentration of 80%. Percentages are on a volume basis. 
     While using some of the hydrogen-containing mixture produced by the gasifier as feed to the turned down catalytic steam reformer will result in a higher gasifier feed rate, the significant natural gas saving in the catalytic steam reformer will more than offset the cost of the increased gasifier feedstock since the gasifier uses a low value feedstock. 
     Another benefit of this method is that the carbon dioxide emitted in the catalytic steam reformer stack gas is reduced. 
     The values in the column for turndown-gasifier hydrogen-containing mixture import with PSA tail gas import show the estimated natural gas feed and fuel consumption associated with the use of 25×10 6  standard cubic feet per day of hydrogen-containing gas mixture from the gasifier as a portion of the catalytic steam reformer feed. In addition, 47.5 MMBtu/h (based on lower heating value, LHV) of gasifier PSA tail gas is fired in the catalytic steam reformer. This has the benefit of reducing the catalytic steam reformer natural gas trim fuel by 43%. This method will also further reduce carbon dioxide emissions from the catalytic steam reformer. 
     Another potential benefit of this method is that an acceptable PSA tail gas firing duty turndown ratio can be maintained in the catalytic steam reformer burners. In the example presented, without tail gas import from the gasifier PSA, an SMR tail gas burner turndown ratio of at least 8:1 would be required. This can be reduced to a ratio of 6:1 with tail gas import, simplifying the burner design. 
     The amount of export steam available using the method is reduced. 
     
       
         
               
               
             
               
               
               
               
               
             
               
               
               
               
               
               
             
           
               
                   
                 TABLE 1 
               
             
             
               
                   
                   
               
               
                   
                 Turndown - 
               
               
                   
                 Gasifier hydrogen- 
               
               
                   
                 containing mixture 
               
               
                   
                 import 
               
             
          
           
               
                   
                   
                 Turndown 
                 No 
                   
               
               
                   
                   
                 100% 
                 PSA 
                 PSA tail 
               
               
                   
                 Design 
                 Nat. gas 
                 tail gas 
                 gas 
               
               
                   
                 Case 
                 feed 
                 import 
                 import 
               
               
                   
                   
               
             
          
           
               
                 H2 Production 
                   
                   
                   
                   
                   
               
               
                 Gross Generation 
                 MMSCFD 
                 165 
                 33 
                 30.5 
                 30.5 
               
               
                 H2-containing 
                 MMSCFD 
                 0 
                 0 
                 25 
                 25 
               
               
                 mixture import 
                 MMBtu/h 
                 0 
                 0 
                 329 
                 329 
               
               
                 from gasifier 
               
               
                 Natural gas 
               
               
                 consumption 
               
               
                 Feed 
                 lb · mols/h 
                 6979 
                 1406 
                 454 
                 454 
               
               
                   
                 MMBtu/h 
                 2653 
                 535 
                 173 
                 173 
               
               
                 Fuel 
                 lb · mols/h 
                 1082 
                 390 
                 353 
                 201 
               
               
                   
                 MMBtu/h 
                 411 
                 148 
                 134 
                 76 
               
               
                 Total 
                 lb · mols/h 
                 8061 
                 1797 
                 807 
                 655 
               
               
                   
                 MMBtu/h 
                 3065 
                 683 
                 307 
                 249 
               
               
                 Export Steam 
               
               
                 Pressure 
                 psig 
                 610 
                 610 
                 610 
                 610 
               
               
                 Temperature 
                 ° F. 
                 775 
                 804 
                 783 
                 776 
               
               
                 Flow rate 
                 lb/h 
                 315670 
                 36850 
                 28684 
                 24748 
               
               
                 Reformer firing 
               
               
                 Trim fuel 
                 MMBtu/h 
                 371 
                 134 
                 121 
                 69 
               
               
                 Total PSA tail gas 
                 MMBtu/h 
                 902 
                 187 
                 112 
                 160 
               
               
                 (incl. imported 
               
               
                 Imported PSA tail 
                 MMBtu/h 
                 0 
                 0 
                 0 
                 48 
               
               
                 gas 
                   
                   
                   
                   
               
               
                 Total 
                 MMBtu/h 
                 1273 
                 321 
                 233 
                 229 
               
               
                   
               
             
          
         
       
     
     Although the present invention has been described as to specific embodiments or examples, it is not limited thereto, but may be changed or modified into any of various other forms without departing from the scope of the invention as defined in the accompanying claims.