Synthesis gas manufacture
FIR xefi&#39;f all:  
  J United States Patent 1191 1111 3,874,116  
 White *Apr. 1, 1975 SYNTHESIS GAS MANUFACTURE 3,383,228 5/1968 Rekate et a1 48/209 x 3,471,275 /1969 Borggreen 48/209 [75] lnvemor- Rbert whlte Pmole, Cahf- 3,556,751- 1/1971 Slater et al.... 48/209 ux 73 Assignee; Chevron Research Company, San 3,759,677 9/1973 White 48/209 Francisco Ca 1115,320 3/1922 McDonald 48/209 Notice: The portion of the term of this OTHER PUBLICATIONS 1 subsequenf t0 P 18, l-laslam and Russell, Fuels and Their Combustion, p. i 1990, has been dlsclalmed- 68-70, (1st. Ed., 1926), TP318H3 AU171.  
 [22] Filed: Apr. 27, 1973 Primary E.taminerJoseph Scovronek [21] Appl&#39; 355353 Attorney, Agent, or Firm-G. F. Magdeburger; R. H.  
  Related US. Application Data Davies; De YOlmg [63] Continuation-in-part of Ser. No. 39.116, May 20,&#39;  
 1970, abandoned. [57] ABSTRACT [52] U 8 Cl 48/209 48 H 48/202 A process for producing synthesis gas under substan- 28/206 252/373 423/648 tially endothermic gasification conditions, which com- 51 1m. 01. (3101 3/00 c10j 3/16 prises: (a) feeding ganic feed material [58] Field of Search 48/209, 111, 197 A, 197 R, mg g f and least Q percent Xygen 18/202, 206 210; 423/648, 252/373; and contalnlng less than 5 welght percent sulfur, to a 210/2 5 23 25 reaction zone; (b) feeding steam to the reaction zone;  
 &#39; and (c) contacting the steam with the organic feed material in the reaction zone at a temperature be- [56] References Clted tween about 500 and 1,600F. Preferably the feed UNITED STATES PATENTS material is solid waste material, most preferably solid TCStl&#39;Up et ai municipal waste 2,126,150 8/1938 Stryker 48/209 UX 2,776,879 1/1957 Gumz 48/202 16 Claims, 1 Drawing Figure ORGANIC MATERIAL OR SOLID WASTE //3 70 I7 2 5 l k i I] I5 HEAT GAS RECOVERY PURIFICATION 26 30 at &#34;a w za Z7 14 2 25 co 7 9 H20 r SHIFT GAS 4{ k} CONVERSION PURIFICATION a2 2o SANITARY H2 RES IDUE (ASH) COMBUSTION CHAMBER &amp; 02 l SYNTHESIS GAS MANUFACTURE RELATED APPLICATION This application is a continuation-in-part of application Ser. No. 39,116, filed May 20, 1970 now aban- 5 doned.  
 BACKGROUND OF THE INVENTION The present invention relates to the production of synthesis gas. More particularly, the present invention relates to the production of synthesis gas by the endothermic reaction of carbonaceous material with steam. The term synthesis gas is used herein to mean a gas comprising hydrogen and carbon oxides and some methane.  
  Synthesis gas can be used for a number of purposes for example, the carbon oxides can be removed from the synthesis gas, usually after converting essentially all of the carbon monoxide to hydrogen and carbon dioxide, and the resulting purified hydrogen gas used in hydroconversion processes such as hydrocracking, to produce jet fuel or gasoline. The synthesis gas can also be used to synthesize methanol from the hydrogen and carbon oxides or to synthesize other chemicals such as ammonia when nitrogen is added to the synthesis gas, either after production of the synthesis gas or, preferably, during the reaction used to produce the synthesis gas. The synthesis gas can be used in a Fischer-Tropsch synthesis to form liquid hydrocarbons. Also, the synthesis gas can be used to form methane or it can be burned directly as a fuel gas.  
  Various methods have been suggested for the production of synthesis gas or hydrogen-rich gas mixtures. Among these methods are steam-hydrocarbon reforming, partial oxidation of hydrocarbons, Lurgi coal gasification, the traditional steam, redhot coke reaction, and modified methods of reacting carbonaceous matter with steam and oxygen, such as described in U.S. Pat. No. 1,505,065.  
  The processes most frequently used to generate hydrogen are steam-hydrocarbon reforming and partial oxidation of hydrocarbons.  
  In typical steam-reforming processes, a hydrocarbon feed is pretreated to remove sulfur compounds, which are poisons to the reforming catalyst. The desulfurized feed is mixed with steam and then is passed through tubes containing a nickel catalyst. While passing through the catalyst-filled tubes, most of the hydrocarbons react with steam to form hydrogen and carbon oxides. The tubes containing the catalyst are located in a reforming furnace, which furnace heats the reactants in the tubes to temperatures of l,200-l,700F. Pressures maintained in the reforming furnace tubes range from atmospheric to 450 psig. If a secondary reforming furnace or reactor is employed, pressures used for reforming may be as high as 450 psig to 700 psig. In secondary reformer reactors, part of the hydrocarbons in the effluent from the primary reformer is burned with oxygen. Because of the added expense, secondary reformers are generally not used in pure hydrogen manufacture, but are used where it is desirable to obtain a mixture of H and N as in ammonia manufacture. The basic reactions in the steam reforming process are:  
 e.g., methane-steam:  
  In typical partial oxidation processes, a hydrocarbon is reacted with oxygen to yield hydrogen and carbon monoxide. Insufficient oxygen for complete combustion is used. The reaction may be carried outwith gaseous&#39;hydrocarbons or liquid or solid hydrocarbons. For example, with methane the reaction is:  
 With heavier hydrocarbons, the reaction may be represented as follows:  
 C I-I 2.8 0 -1- 2.1 H 0 I, 6.3 CO +0.7 CO 8.1 &#34;2  
  Both catalytic and noncatalytic partial oxidation processes are in use. Suitable operating conditions include temperatures from 2,000F. up to about 3,200F. and pressures up to about 1,200 psig, but generally pressures between and 600 psig are used. Various specific partial oxidation processes are commercially available, such as the Shell Gasification Process, Fauser-Montecatini Process, and the Texaco Partial Oxidation Process.  
  There. is substantial carbon monoxide in the hydrogenrich gas generated by either reforming or partial oxidation. To convert the carbon monoxide to hydrogen and carbon dioxide, one or more CO shift conversion states are typically employed. The CO shift conversion reaction is:  
  This reaction is typically effected by passing the carbon monoxide and H 0 over a catalyst such as iron oxide activated with chromium.  
  Production of hydrogen and other gases from waste substances produced in the manufacture of paper from wood chips and the like has been discussed in the literature as, for example, in U.S. Pat. No. 3,317,292. In the manufacture of paper, wood chips are digested, for example, with an aqueous calcium sulfide liquid, thereby forming calcium lignin sulfonate waste product in solution, leaving wood pulp behind. As disclosed in U.S. Pat. No. 3,317,292, the waste substances containing lignin-derived organic components can be converted to a gas mixture comprising hydrogen by contacting the waste material with steam in a reaction zone at an elevated temperature. The sulfite waste liquor produced in the manufacture of paper from wood chips and the like is a relatively well-defined waste material, consisting mostly of lignin-type organic compounds and certain inorganic components, including at least 5 weight percent sulfur, calculated as the element sulfur, but present usually in the form of sulfur compounds.  
  U.S. Pat. No. 3,471,275 discloses a method for converting refuse or garbage-type material to gases, such as gases rich in hydrogen. According to the process disclosed in U.S. Pat. No. 3,471,275, the refuse is fed to a retort and heated therein to a temperature between about 1,650F. and 2,200F. The retort is externally heated. According to the U.S. Pat. No. 3,471,275 process, steam is not generally added to the retort. Any steam which is added to the retort is added to the bottom of the retort so that steam would flow countercurrent to the waste material which is introduced to the retort at the top of the retort.  
 SUMMARY OF THE INVENTION According to the present invention, a process is provided for producing synthesis gas under substantially endothermic reaction conditions, which process comprises reacting the feed with steam by: (a) feeding an organic feed material, containing hydrogen and at least 10 weight percent oxygen and containing less than 5 weight percent sulfur, to a reaction zone; (b) feeding steam to the reaction zone in an amount sufficient to maintain a gas mol fraction of steam in the range 0.1 to 0.9 and at a temperature sufficient to effect a contacting of the steam with the organic feed material in the reaction zone at a temperature between about 500 and l,600F.  
  It has been found that the defined organic feed material is conveniently converted at an unexpectedly high rate to synthesis gas when the conversion is carried out under substantially endothermic conditions in accordance with the present invention. Preferably little (less than 25 percent) or none of the endothermic heat required for gasification is furnished by in situ oxidation by molecular oxygen in the gasification zone, i.e., under essentially endothermic reaction conditions. The present process is especially advantageous in that the (CO H )/CO mol ratio of the product gas is in general at least 1.5.  
  The reason for the fast reaction rate in the process of the present invention is not completely understood, but it is believed that an important factor is the oxygen content of the organic feed material in the process of the present invention. The organic feed material, which in this specification is to be understood to contain hydrogen as well as carbon, must contain at least weight percent oxygen, which can be contrasted to the essentially nil amount of oxygen present in hydrogen feedstocks to synthesis gas-producing processes such as steam-light hydrocarbon reforming or hydrocarbon partial oxidation. The presence of chemically bound oxygen in the organic feed material in the process of the present invention may contribute to the relatively fast reaction rate by making the feed material more susceptible to reaction with steam to produce hydrogen than in the case of hydrocarbon material containing little or no oxygen. It has been found that it is particularly preferable in the process of the present invention to produce synthesis gas from organic feed material containing at least 25 weight percent oxygen, and still more preferably between about 35 and 70 weight percent oxygen. Broadly, oxygen contents of satisfactory feeds are in the range 10 to 70 weight percent.  
  It has also been found that organic feed material containing the oxygen substantially in the form of polyhydroxylated compounds is particularly advantageous from the standpoint of high reaction rates with steam to form synthesis gas. Feeds containing oxygen in the form of polyhydroxylated compounds are meant to include carbohydrates such as cellulose and sugars.  
  The oxygen and the hydrogen content in the organic feed material are to be understood as chemically combined carbon, oxygen and hydrogen, i.e., oxygen and hydrogen which are connected through one or more chemical bonds to the carbon present in the organic feed material.  
  It is important in the process of the present invention that the feed material contain less than 5 weight percent sulfur. The sulfur is calculated as the element, al-  
 though for those undesired and excluded feedstocks the sulfur is usually present as a compound as, for example, an organic sulfur compound or an inorganic sulfur compound present in the feed material. Thus, it is to be understood that the organic feed material reacted with steam according to the process of the present invention is free from a high percentage of inorganic or organic sulfur compounds, i.e., that the feed contains less than 5 weight percent sulfur either as sulfur chemically combined with the organic feed material or as inorganic sulfur compounds physically mixed with the organic feed material. Feeds such as Kraft black liquor produced as a waste material in the manufacture of paper pulp are not suitable in the process of the present invention because of the relatively high content of sulfur compounds in such feeds. It is undesirable to have substantial amounts of sulfur in the feed to the reaction zone in the process of the present invention because of the increased reactor cost and, more particularly, because of the increased problems in removing sulfur compounds from the synthesis gas produced in the reactor. It is preferred that the sulfur content of the organic feed material be below about 3 weight percent sulfur.  
  It is important that the gas mol fraction of the steam in the reaction zone be maintained at a value of at least 0.1. Steam is a reactant in the present process, and as such must be present in a substantial amount. Preferably the steam mol fraction should be in the range from about 0.2 to 0.6. Larger relative amounts, up to about 0.9 mol of steam per mol of gas may be employed. However, no particular advantage and some disadvantage is experienced where the steam mol fraction is large, i.e., the extra process burden, and the like.  
 It has been found that particularly suitable organic feed material for the process of the present invention includes solid waste material, including material commonly referred to as garbage. It has been found that high reaction rates are obtained in the process of the present invention for the conversion of solid waste ma terial to synthesis gas. The term solid waste material or solid waste is used herein to include solid municipal waste or common garbage, sewage, industrial waste such as sawdust, and agricultural waste such as corn husks and other discarded cellulosic material.  
  According to a particularly preferred embodiment of the present invention, the feed material is solid municipal waste, including what is commonly referred to as garbage, but excluding sewage. This solid municipal waste, consisting primarily of common garbage, is particularly preferred in that it has been found that, with simulated solid municipal waste, high conversion rates to synthesis gas can be obtained in the process of the present invention, and also sanitary, valuable products are produced, to alleviate an important disposal and pollution problem resulting from the increasing amounts of solid municipal waste which must be disposed of daily. In addition, it has been determined that the amount of solid municipal waste for a number of urban areas is roughly satisfactory from a feed requirement standpoint for the production of synthesis gas to be used in various processes mentioned previously.  
  Typically the solid municipal waste includes substantial amounts of at least proteins, fats, cellulose, sugars, starches, and hydrocarbons. In this connection, substantial amounts is used to mean at least about 1 weight percent of the total solid municipal waste feed.  
 Usually the solid municipal waste feed will contain at least 2 weight percent of each of the above-specified constituents. The feed, of course, must contain at least weight percent of combined oxygen, as discussed above.  
  The solid municipal waste feed which is used in the process of the present invention may contain a substantial amount of moisture. The term solid is used in distinction to free-running liquids, and does not mean that the solid municipal waste material is free of moisture.  
  It should be understood that the feed composition for such a diverse feedstock as solid municipal waste will be subject to variation from time to time. Therefore, the composition of the solid municipal waste feed should be determined as an averaged composition fed to the reactor. Unsatisfactory feed components, if present, exit the process via the ash discharge route.  
  As indicated above, although solid wastes other than municipal wastes can be processed to form synthesis gas in accordance with the process of the present invention, it is particularly preferred to convert solid municipal waste to synthesis gas, as it has been determined that the amount of municipal waste generated is particularly suited to the production of commercial amounts of hydrogen and that the municipal wastes are a surprisingly attractive feedstock in terms of synthesis gas yields.  
  One of the reactions occurring in the process of the present invention is the reaction of cellulosic material of sugar-type material with steam to produce hydrogen and carbon oxides. The cellulosic and sugar-type material can be considered on the basis of a simple sugar such as glucose, for which the following reaction applies:  
 Unlike a similar reaction where water is added to methane or carbon, the above reaction has a negative freeenergy change (AF) at 25C., so that, on the basis of thermodynamics, the reaction can occur at room temperatures. However, it has been found that the reaction rate is very slow at room temperatures. Therefore, elevated temperatures are preferred in the reaction zone according to the process of the present invention. However, it is particularly preferred to use temperatures below l,600F. Higher temperatures result in excessive heat requirements, increased reactor cost, lower yields of hydrogen, and ash fusion problems. Thus, preferably the contacting of the organic feed material with the steam is carried out in a reaction zone at a temperature between about 500 and l,600F., and more preferably between about 700F. and 1,600F. Temperatures between 1,000l ,400F. are particularly preferred. At these temperatures it has been found that the reaction of the organic feed material with steam is a surprisingly attractive route to produce hydrogen-rich gas, with relatively high H; yield, relatively low heat requirements, a desirable (CO H2)/CO mol ratio of at least 1.5, and results in a free-flowing, particulate ash residue.  
  The process of the present invention can be carried out over a wide range of pressures, from about 1 atmosphere to 200 atmospheres, preferably from about 4 to 150 atmospheres. According to a preferred embodiment of the present invention, the pressure in the reaction zone is maintained between about 4 and atmospheres. It has been found that these high pressures are particularly advantageous in the reaction of solid waste material with steam while the reaction zone is maintained at a temperature between about 500 and 1,600F. Because the reaction of solid waste material with steam has been found to be fairly rapid compared, for example, to the reaction of coke or carbon with steam, a substantial rate of production of hydrogen from solid waste material can be obtained at relatively high pressures, including pressures ranging from about 500 to 1,000 psig up to about 2,000 or 3,000 psig. The relatively low temperatures required in the process of the present invention, i.e., temperatures below 1,600F. and more preferably below l,400 F., are important in the preferred embodiment of the present invention, wherein high pressures are used in the reaction zone. The lower temperatures permit avoidance of the fusion of the ash, and consequently avoidance of clinker formation. They also result in considerable savings in the cost of the reactor, particularly at the preferred high reaction pressures. High reaction pressures afford the extremely important advantage of generating synthesis gas at a high pressure, so that the synthesis gas needs little or no compression before being used in a high-pressure hydroconversion process such as hydrocracking or hydrotreating. Also, CO is more economically removed from raw hydrogen generated at the preferred high pressures in accordance with the present invention, because the high-pressure CO can be removed from the hydrogen by absorbing the CO into a physical absorbent such as methanol or propylene carbonate, as opposed to the more expensive means of removing C0 at low pressure using a chemical absorbent such as an amine.  
  In the process of the present invention it is preferred that the temperatures required for the process be substantially maintained by control of the temperature of the reactive gases, steam or steam and combustion gases, which are introduced into the reaction zone. While heat can be supplied to this zone by in situ combustion of a minor portion of the organic material, at best only a minor fraction about 25 percent or less should be so supplied. In situ combustion usually is accompanied by local hot-spots, incandescent zones, and consequential fusion of the ash. For effective operation of the present process, a free-flowing, particulate ash is required. Indirect heat exchanger means such as coils, fire tubes, and the like, may also be used as heat sources. However, these means are in general satisfactory sources for but a fraction (less than 25 percent) of the heat requirement. The rate of heat supply to the reactants by indirect heat transfer is relatively slow, compared to direct heat supply via a gaseous react&#39;ant. Also, due to the very nature of the more ordinary organicfeed materials, waste materials, garbage, and the like,-  
 the presence of coils and other kinds of indirect heating elements tends to impede the desired steady flow of the feed through the gasification stage of the process.  
  In accordance with one embodiment of the present invention, the flow of organic feed material and steam feed to the reaction zone is concurrent within the reaction zone. Both the organic feed material and the steam are fed to the top or upper part of the reactor with basically a downward flow of the organic feed material and reactant steam in the reactor, and to withdraw produced hydrogen-rich gases from the lower part of the reactor. Operation in accordance with this embodiment results in less oily material and unconverted hydrocarbons being withdrawn from the reaction zone.  
 Also, the temperature in the reaction zone can be controlled at the preferred relatively low levels so as to further maximize the yield of synthesis gas in the reaction zone.  
  In accordance with another and a particularly preferred embodiment of my invention, the flows within the gasification zone of organic feed material and steam feed to the reaction zone are countercurrent.  
  The conversion of organic feed material, particularly solid wastes, to synthesis gas in accordance with the present invention operates as a heretofore-unharnessed use of the sun&#39;s energy. The sun puts a great deal of radiant (as opposed to thermal) energy into the constituents that make up organic feed materials such as solid wastes, but in the past the energy of solid waste has generally not been utilized in the United States. Instead, solid waste has mostly been a nuisance and sanitation problem. Living plants manufacture carbohydrates from carbon dioxide and water in the presence of sunlight and chlorophyll by means of a complex series of reactions (heat and nutrients in the soil are also needed). Radiant energy is an important factor in the transformation, commonly known as photosynthesis. The carbohydrates produced by the photosynthetic process in plants can be represented by the general formula C,.(HOI-I Using the general formula of a carbohydrate, an abbreviated chemical equation to represent photosynthesis can be written as follows:  
 The photosynthesis of a specific carbohydrate, glucose, may be represented by the equation:  
 + C H1205 &#34;l&#39; 602 kCal.  
 As is indicated by the -671 kilocalories after the above equation, radiant energy received from the sun is stored in carbohydrates such as the simple glucose carbohydrate in the above equation.  
  In the process of the present invention, clean hydrogen which has a high amount ofstored energy is produced from garbage-type feed material including carbohydrates. Thus, it may be noted that if the hydrogen produced in accordance with the present invention is burned with oxygen, there is a release of about 52,000 Btus per pound of hydrogen. The hydrogen is obtained from a carbohydrate (for example) by reaction of the carbohydrate with H O, requiring a heat input of about 6,600 Btus per pound of hydrogen produced. The other 45,600 Btu&#39;s per pound of hydrogen is put in by photosynthesis. Thus, about 87 percent of the stored energy in the hydrogen produced in the present invention comes from the sun the process of the present invention adds only another approximately 13 percent of the hydrogens stored heat energy.  
  A particularly preferred over-all process embodiment for producing high-pressure hydrogen for use, for example, in a hydroconversion process such as hydrocracking comprises the following steps:  
 a. reacting the organic feed material with steam in a reaction zone at a temperature between 500 and 1,600F. to generate a hydrogen-rich gas containing hydrogen, hydrogen sulfide, carbon monoxide, carbon dioxide and methane;  
 b. withdrawing the hydrogen-rich gas from the reaction zone at a temperature between 500 and 1,600F.; c. recovering heat from the hydrogen-rich gas by heat exchanging the hydrogen-rich gas with H O to obtain steam;  
 d. using at least a portion of the steam generated in step (c) as feed steam for reaction with the organic feed material according to step (a);  
 e. separating H S from hydrogen-rich gas withdrawn from heat recovery step (c);  
 f. shift-converting carbon monoxide present in the hydrogen-rich gas withdrawn from the H 8 separation step to obtain additional hydrogen gas;  
 g. centrifugally compressing I-h-CO gas withdrawn from step (f) to obtain a high pressure hydrogen gas; and  
 h. separating carbon dioxide from the high-pressure, hydrogen-rich gas by physical absorption of carbon dioxide present in the high-pressure hydrogen gas.  
 BRIEF DESCRIPTION OF THE DRAWING The drawing is a process flow diagram schematically indicating preferred embodiments of the present invention.  
 DETAILED DESCRIPTION OF THE DRAWING Referring now more particularly to the drawing, organic material is fed as indicated by arrow 1 to the process as is schematically indicated in the drawing. According to one preferred embodiment of the present invention, the organic feed material is ordinary municipal solid wastes or garbage. Preferably certain constituents such as metals in particular, iron-containing materials are removed from the solid wastes prior to reacting the solid wastes with steam. The constituents which make up the solid wastes generally include clothing, food particles and food peels, plastics, paper, cardboard, wood, etc. The process of the present invention is preferably applied to ordinary municipal or city garbage.  
  Referring again to the drawing, a conveyor belt, as indicated in the drawing by numeral 2, can be used to transport the organic feed material so that it falls as indicated by arrow 3 into hopper 4 for feeding to reactor 6 via line 5. In reactor 6, the organic feed material is contacted with steam introduced via line 7 or preferably line 7a. The steam and organic feed material react to form synthesis gas (hydrogen and carbon oxides) and usually minor amounts of various other gases such as hydrogen sulfide.  
  As indicated previously, the reaction of the organic feed material with steam to form hydrogen is basically an endothermic reaction. Therefore, heat must be supplied to the reaction zone. According to a particularly preferred embodiment of the process of the present invention, the temperature in the reactor, i.e., in reactor 6, is controlled by burning a portion of and recycling a relatively large amount of the synthesis gas effluent from heat recovery zone 12 back to the reactor via combustion chamber 28. For each part (weight) of oxygen introduced to chamber 28 via line 8, an amount of the effluent synthesis gas from zone 12 in the range 15 to 50- parts (weight) is also introduced to obtain a hot combustion gas product having a temperature of the order of about 1,500 to 1,900F. The hot effluent gas is then introduced to reactor 6 to obtain a temperature between about 700 and 1,600F., preferably about 1,200 to l,400F., in the reaction zone. If desired, and as a further control means for the process, the amount of oxygen introduced via line 8 may moderately exceed the stoichiometric requirement for the oxidation of the recycled synthesis gas. In this case, some combustion a minor amount, i.e., less than 25% of the heat required for the gasification of the organic feed will take place in reactor 6, and will furnish a portion of the required heat for the desired endothermic reaction.  
  This particularly preferred embodiment of the present invention can be briefly illustrated by an approximate quantitative example. About 3,700 tons per day of solid municipal waste is fed to one or more reactors maintained at a temperature of about 1,200F. and a pressure in the range from 4 to 20, preferably about 10, atmospheres. The 3,700 tons per day of solid municipal waste feed is reacted with steam by introducing steam at a temperature of about l,900F. and in an amount sufficient to maintain a mol fraction of steam in the reactor of about 0.6, into the reactor or reactors to produce a net product synthesis gas of about 100 million SCF per day of H plus CO. Both the solid municipal waste and the steam or water are fed to the upper part of each reactor, and the gross effluent gas is removed from the lower part of each reactor. After separating fly ash from the gross product gas in a cyclone separator, the gross effluent gas is cooled by giving up a large portion of its heat content to boiler feed water to generate steam in heat recovery zone 12. A major portion of the gross effluent gas from the reactor is passed via line 27 to combustion chamber 28 wherein it is burned with approximately 500 tons per day of oxygen. About 250 million Btus per hour are produced by the burning of the recycle gases introduced via line 27 to combustion chamber 28. The hot gases leave the combustion chamber at a temperature of about l,800F. via line 29. These hot gases are then introduced via lines 30, 31 and 32 to reactor 6 in order to supply the heat to achieve and maintain a reaction temperature of about 1,200F. in reactor 6. The ratio of recycle gas passed via line 27 to oxygen added via line 8 to the combustion chamber is between about and 50 on a weight basis. Preferably the weight ratio of recycle gas to oxygen is between about and 40 on a weight basis.  
  The net product of 100 million SCF per day of H plus CO is passed via line 15 to gas purification zone 16 for H 5 removal. In those instances where a synthesis gas comprising H and CO is desired, the synthesis gas may be withdrawn from the process after gas purification zone 16. In those instances where purified hydrogen is desired, the H and H CO is passed to shift conversion zone 20 and then to gas purification zone 22 so that a purified hydrogen stream can be withdrawn via line 24.  
  As indicated in the drawing, the sanitary residue remaining from the organic feed material can be removed from the lower part of the reaction zone after it has fallen through a grating, as indicated by numeral 9. Mechanical apparatus and means used for the reaction of carbonaceous material such as coal and similar material can be adapted to the process of the present invention wherein material such as solid wastes are reacted with steam and a sanitary residue or ash remains. Thus, it is apparent that various mechanical schemes can be used for the reactor in the process of the present invention.  
  Preferably the reaction is carried out at a temperature within the range of about 700 to 1,600F. Temperatures in the range of about 800 to 1,400F. have been found to be particularly attractive in terms of high synthesis gas yield. Usually there will be a temperature gradientin the reactor, with a somewhat higher temperature prevailing in the lower part of the reactor. The upper part of the reactor typically is cooled somewhat relative to the lower part of the reactor, because the solid waste material is being heated in this zone. In any event, the gases removed from the reactor via line 11, or preferably line 11a, are still at an elevated temperature, usually&#39;in the range of about l,O00F. These hydrogen-rich hot gases are passed via line 11 or 11a to heat recovery zone 12.  
  The reaction of solid waste material with steam to form synthesis gas is far more thermodynamically favorable than a similar reaction for either CH C, coke, coal or hydrocarbons. Therefore, it is possible to carry this reaction out at much greater pressures than are used with the other feedstocks. Thus, in the production of hydrogen, particularly preferred reaction pressures are between about 20 and atmospheres. These high pressures minimize or eliminate the need for subsequent compression of the hydrogen gas produced as, for example, when the hydrogen gas is to be used in a high-pressure hydroconversion process.  
  The steam for the process of the present invention can be generated in various manners, but it is preferred to recover heat present in the effluent gases from reactor 6 by heat exchange of the hot effluent gases from reactor 6 with water in heat recovery zone 12 to thereby generate steam removed via line 14 from heat recovery zone 12. If necessary, additional heat may be put into the steam in line 14 or line 7 before it is passed via line 7 to reactor 6.  
  In the process of the present invention, it is preferred to utilize a portion of the steam generated in heat recovery zone 12 in CO shift conversion zone 20, as is indicatedby the steam passed via line 19.  
  Inheat recovery zone 12, H 0 and oily material withdrawn in the gaseous or vapor stream via line 11 or 1 la from reactor 6 is condensed. The condensed H O will typically contain various gases produced in reactor 6 such as HCI, l-IBr, HI, NH I-IF, etc., as well as some CO CO and H5. The oily phase of the liquid condensed out of the hydrogen-rich gas withdrawn from reactor 6 will typically contain hydrocarbons and oxygenated hydrocarbon components such as methanol, acetic acid, formaldehyde, formic acid, acetone, etc.  
  The condensed aqueous phase and oily phase are shown schematically as withdrawn from the process via line 27. The materials withdrawn via line 27 can be passed to various further processing as, for example, processing for the recovery of oil and the separation of various chemicals.  
  In accordance with a particularly preferred embodiment of the process of the present invention, the flow of steam and solid waste material in reactor 6 is essentially concurrent, as opposed to countercurrent, flow. Thus, the solid waste material is introduced to reactor 6 via line 5 and, according to this preferred embodiment, steam is introduced to reactor 6 at the top of reactor 6 via line 7a. The upper part of the reactor will be cooler than the lower part of the reactor in most instances because of the relatively low temperature of the solid waste material introduced into the reactor. However, after a minor portion of the solid waste material has been reacted with oxygen to supply heat, the temperature will rise. Thus, the lower part of the reactor will be at a higher temperature than the upper part of the reactor. According to this preferred embodiment of the present invention, the raw hydrogen-rich gas is withdrawn from reactor 6 in the lower part of the reactor via line 11a. Operation in accordance with this preferred embodiment affords the advantage of reducing the amount of oily substances withdrawn from reactor 6 by converting these oily substances to synthesis gas or by burning the oily substances in combustion chamber 28. In countercurrent flow operation of reactor 6, steam introduced at the lower part of the reactor tends to strip or retort a certain amount of oil out of the solid waste feed to the upper part of reactor 6. 1n concurrent flow of the solid waste material and steam, this stripping or retorting is substantially reduced, and the raw hydrogen gas is withdrawn from a relatively hot zone of the reactor so that oily material obtained from the solid waste material will be substantially reduced by reaction with steam to form synthesis gas and/or by oxidation with oxygen to yield heat.  
  Valves 25 and 26 are closed when it is desired to operate reactor 6 with concurrent flow of solid waste ma terial and steam.  
  The gas withdrawn via line 11 or 1111 is the basic synthesis gas produced in accordance with the present invention. Zones l2, 16, 20 and 22 relate to further treatment of this synthesis gas, which is particularly preferred in the production of a relatively pure hydrogen stream. It is to be understood that these subsequent steps can be altered when other final products are desired, as, for example, in the case of methanol production.  
  According to the preferred over-all process embodiment shown in the drawing, the cooled gases from heat recovery zone 12 are passed via line 15 to gas purification zone 16. Usually, one or more additional cooling steps will be applied to the gases removed from zone 20 before they are purified in gas purification zone 16.  
  In gas purification zone 16, H s which may be present in the effluent from reactor 6 is removed, preferably by scrubbing the hydrogen-rich gas with an H absorbent. Various gas purification means may be employed in gas purification zone 16. The use of monoethanolamine (MEA) is a preferred absorbent for removing H 8 and other sulfur compounds. A portion of the CO present in the gases from reactor 6 is generally removed from the hydrogen-rich gas at the same time H 3 is removed from the hydrogen-rich gas, but H is preferred not to remove CO from the hydrogen-rich gas in gas purification zone 16. H 8 present in the hydrogen-rich gas produced in reactor 6 and removed from the hydrogen in gas purification zone 16 can be passed to other processing. For example, the H S can be passed via line 17 from gas purification zone 16 to a Claus process for the production of sulfur. Usually the H 8 will contain some CO but preferably only small amounts of CO.  
  After at least H 5 removal from the hydrogen-rich gas in gas purification zone 16, the hydrogen-rich gas is fed via line 18 to CO shift conversion zone 20. In the CO shift conversion zone, CO present in the hydrogenrich gas is reacted with steam added to the CO shift conversion zone to form CO and additional H Hydrogen-rich gas containing only small amounts of CO for example, between about 0.2 and 2.0 volume percent CO is withdrawn from C0 shift conversion zone 20 via line 21. The hydrogen-rich gas from C0 shift conversion can be directly passed to gas purification zone 22 for removal of CO using an absorbent which is selective for CO as opposed to H such as monoethanolamine.  
  However, it is preferred to centrifugally compress the H CO gas mixture from the CO shift conversion zone prior to removing the CO It is particularly preferred to centrifugally compress the H CO gas and then remove CO by physical absorption using a solvent such as propylene carbonate or methanol. The use of centrifugal compressors for H -CO compression is discussed in more detail in commonly assigned patent applications Serial Nos. 736,520 (now U.S. Pat. No. 3,618,331, issued Nov. 9, 1971), 788,299 (now U.S. Pat. No. 3,551,106, issued Dec. 29, 1970), and 788,262 (now U.S. Pat. No. 3,532,467, issued Oct. 6, 1970). The disclosures of these applications, particularly those portions relating to H CO centrifugal compression and also the disclosures relating to CO shift conversion and hydrogen gas purification are incorporated by reference into the present patent application.  
  In accordance with the preferred over-all process embodiment of the present invention wherein the 11,-- CO gas from shift conversion is centrifugally compressed and then treated for CO removal with a physical absorbent, the H withdrawn via line 24 from gas purification zone 22 usually will be at sufficiently high pressure for example, 1,000 to 2,500 psig for use of the H in a high-pressure hydroconversion process such as catalytic hydrocracking. In other instances, for example when the H produced in the process of the present invention is to be used as a fuel gas blending component, little or no compression of the hydrogen gas produced in reactor 6 is usually necessary, because reactor 6 is preferably operated at a pressure between about 4 and 20 atmospheres.  
 EXAMPLE 50 g of organic feed material was charged to a oneliter quartz reactor. The organic feed material used in this instance was simulated solid municipal waste composed of 50 weight percent paper, 10 weight percent sawdust, 3 weight percent wool, 2 weight percent plastic, 10 weight percent cotton, 10 weight percent iron, 2 weight percent aluminum, and 13 weight percent food peels such as orange peels, etc. The oxygen content of this particular organic feed material was approximately 50 percent by weight excluding the metallic materials, i.e., iron and aluminum, in the reactor charge.  
  53 ml. H O was added to the quartz reactor over a 4- hour period. The internal reaction zone in the reactor was maintained at a temperature of about l,200 to 1,400F. during most of the reaction time. No catalyst was used in this laboratory run.  
  Over the 4-hour period, the total gas production was approximately 22 liters under ambient conditions of temperature and pressure. The maximum gas production rate during the 4-hour run period was about 10 liters per hour. The gas produced contained about 60 volume percent H with the remainder being mostly CO and CO.  
  Recovered from the 50-g charge to the reactor was 11.8 g of residue. Of this residue, 6.3 g were iron and aluminum and their oxides. The carbon-hydrogenoxygen elemental analysis of the organic residue was about 85 weight percent C, about 1.4 weight percent H, and about 14 weight percent 0.  
  The above results illustrate that organic feed material, particularly solid municipal waste-type material, can be converted to substantial amounts of synthesis gas with the simultaneous production of a residue which is sanitary because of the high-temperature treatment of the solid municipal waste and the breaking down of the solid municipal waste into various constituents. The results also illustrate that the synthesis gas can be produced at a fairly high rate at relatively low temperatures; the rate of synthesis gas production from the solid municipal waste was surprisingly found to be considerably higher than the rate of hydrogen production by reacting carbon with H O under similar temperature conditions.  
  Although various embodiments of the invention have been described, it is to be understood that they are meant to be illustrative only and not limiting. Certain features may be changed without departing from the spirit or scope of the invention. The process of the present invention can be carried out in the absence of catalysts or in the presence of a catalyst. Particularly preferred catalysts are disclosed in application Ser. No. 34,834, filed May 5, 1970, now U.S. Pat. No. 3,759,677 issued Sept. 18, 1973. It is apparent that the present invention has broad application to the production of gases comprising hydrogen from certain organic feed materials by reaction of the organic feed materials with steam. Accordingly, the invention is not to be construed as limited to the specific embodiments&#39;or examples discussed, but only as defined in the appended claims.  
 What is claimed is:  
  l. A process for producing synthesis gas under substantially endothermic reaction conditions, which comprises reacting a solid organic feed material with steam in a reaction zone by:  
 a. passing said feed into the zone, said feed comprising carbon, hydrogen and oxygen in chemical combination wherein at least 25 weight percent of the feed is said oxygen and less than 5 weight percent of the feed, calculated as elemental sulfur, is sulfur;  
 b. feeding steam into the reaction zone and into contact with said feed, said steam being introduced in an amount sufficient to maintain a gas mol fraction of the steam in the reaction zone in the range from about 0.1 to 0.9 and said steam being at a temperature sufficient to substantially provide the heat required to effect said contacting at a temperature in the range from about 500F. to 1,600F.; and  
 c. recovering a synthesis gas having a (C H )/CO mol ratio of at least l.5.  
 2. A process as in claim 1, wherein a. said contact temperature is in the range from about 700 to 1,600F.;  
 b. said pressure is in the range from about 1 to 200 atmospheres;  
 c. said chemically bonded oxygen content of the organic feed is in the range from 25 to about weight percent; and  
 d. said gas mol fraction of steam in the reaction zone is in the range from 0.2 to 0.6.  
 3. A process as in claim 1 wherein said contact temperature is in the range 800 to l,400F.  
  4. A process as in claim I wherein said contact temperature is in the range from 1,000 to l,400F.  
  5. A process as in claim 1 wherein said oxygen content is in the range 35 to 70 weight percent.  
  6. A process as in claim 2 wherein said pressure is in the range from 4 to atmospheres.  
  7. A process as in claim 2 wherein said pressure is in the range from 4 to 20 atmospheres.  
  8. A process as in claim 2 wherein said reactants are introduced concurrently into said zone.  
  9. A process as in claim 2 wherein said reactants are introduced as countercurrent streams into said reaction zone,  
  10. A process as in claim 1 wherein said feed comprises solid waste material.  
  11. A process as in claim 10 wherein said feed comprises municipal waste.  
  12. A process as in claim 10 wherein said waste comprises agricultural waste.  
  13. A process as in claim 1 wherein a portion of said heat required to maintain said contact temperature is furnished by:  
 a. passing a portion of said recovered synthesis gas to a combustion zone;  
 b. combusting said portion with added molecular oxygen; and  
 c. passing the resulting combusted gas to said reaction zone.  
  14. A process as in claim 13 wherein sufficient molecular oxygen is added to said combustion zone to provide a moderate excess, said excess being in an amount wherein not more than 25% of the heat required to maintain said contact temperature is provided by the combustion of said feed in said reaction zone.  
  15. A process for producing synthesis gas having a (C0 H2)/CO mol ratio of at least 1.5, which comprises reacting steam with a solid organic feed material in a reaction zone, said reaction being carried out under substantially endothermic reaction conditions, by:  
 a. passing said feed into the zone, said feed comprising solid municipal waste and comprising carbon, hydrogen and oxygen in chemical combination, wherein at least 25 weight percent of the feed is said oxygen and less than 5 weight percent of the feed, calculated as elemental sulfur, is sulfur;  
 b. feeding steam into said reaction zone and into contact with said feed, said steam being introduced at a temperature in the range from l,500 to l,900F. and sufficient to effect said contacting at a temperature of about l,500F., and in an amount sufficient to maintain a mol fraction of steam in the reactor of about 0.6;  
 c. maintaining in said reaction zone a pressure in the range from about 4 to 20 atmospheres.  
 16. A process as in claim 5 wherein said contact temperature is in the range from 1,000F. to l,400F.