Abstract:
A process for the treatment of biomass to render structural carbohydrates more accessible and/or digestible using concentrated ammonium hydroxide with or without anhydrous ammonia addition, is described. The process preferably uses steam to strip ammonia from the biomass for recycling. The process yields of monosaccharides from the structural carbohydrates are good, particularly as measured by the enzymatic hydrolysis of the structural carbohydrates. The monosaccharides are used as animal feeds and energy sources for ethanol production.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    This application is a continuation of U.S. patent application Ser. No. 12/226,763 filed on Oct. 27, 2008, which application is a U.S. National Stage Application of International Application No. PCT/US2007/010454 filed on Apr. 30, 2007, which application claims benefit to U.S. Provisional Application Ser. No. 60/796,375, filed May 1, 2006, each of which is incorporated herein by reference in its entirety. 
     
    
     FIELD 
       [0002]    The present invention relates to a process for the treatment of a lignocellulosic biomass with concentrated ammonium hydroxide and preferably with ammonia gas to increase the availability of structural carbohydrates (polysaccharides). Preferably, steam under pressure is used to strip ammonia from the biomass for recycling. In particular, the present invention relates to a process which enables the efficient conversion of the polysaccharides to monosaccharides preferably by enzymatic hydrolysis. 
       BACKGROUND 
       [0003]    A wide variety of methods (e.g. concentrated or dilute acids or bases, high temperatures, radiation of various forms) have been used to pretreat lignocellulosic biomass to extract structural carbohydrates to be used to obtain monosaccharides for many different uses. The goal of these pretreatments is to increase the rate and/or yield at which the monosaccharides are subsequently obtained from the structural carbohydrates by chemical or biochemical means such as acid catalysis, enzymatic catalysis, fermentation or animal digestion. In general, these pretreatments have fallen short of desired economic and technical performance for several reasons: 1) many pretreatments degrade some of the sugars, e.g. to acids or aldehydes, thus reducing yields and inhibiting subsequent biological conversion of the remaining sugars; 2) when chemicals are used Ln the pretreatment, it is frequently difficult to recover these chemicals at reasonable cost; 3) residual chemicals can negatively affect downstream conversion operations; and 4) the effectiveness of many pretreatments is limited so that the ultimate conversions of structural carbohydrates obtained, independent of lost yield by sugar degradation reactions, is inadequate for competitive process economics. Thus there are many prior art methods, and they have numerous drawbacks including those outlined above. 
         [0004]    Sufficiently inexpensive monosaccharides from renewable plant biomass can become the basis of chemical and fuels industries, replacing or substituting for petroleum and other fossil feedstocks. Effective, economical pretreatments are required to make these monosaccharides available at high yield and acceptable cost. 
         [0005]    The prior art in the pretreatment of plant biomass with anhydrous liquid ammonia or ammonium hydroxide solutions is extensive. Illustrative are the following patents and literature references: 
         [0000]    U.S. Pat. No. 4,600,590 to Dale
 
U.S. Pat. No. 4,644,060 to Chou
 
U.S. Pat. No. 5,037,663 to Dale
 
U.S. Pat. No. 5,171,592 to Holtzapple et al.
 
U.S. Pat. No. 5,865,898 to Holtzapple et al.
 
U.S. Pat. No. 5,939,544 to Karsents et al.
 
U.S. Pat. No. 5,473,061 to Bredereck et al.
 
U.S. Pat. No. 6,416,621 to Karstens
 
U.S. Pat. No. 6,106,888 to Dale et al.
 
U.S. Pat. No. 6,176,176 to Dale et al.
 
Felix, A., et al., Anim. Prod, 51 47-61 (1990)
 
Waiss, A. C., Jr., et al., Journal of Animal Science 35 No. 1, 1.09-112 (1972). All of these patents and publications are incorporated herein in their entireties.
 
         [0006]    In particular, ammonia fiber explosion (AFEX) represents a unique and effective pretreatment for biologically converting lignocellulosic biomass to ethanol (Dale, B. E., 1986. U.S. Pat. 5,037,663; Dale, B. E., 1991, U.S. Pat. 4,600,590; Alizadeh, H., F. Teymouri, T. I. Gilbert, B. E. Dale, 2005. Pretreatment of Switchgrass by Ammonia Fiber Explosion. Applied Biochemistry and Biotechnology, 121-124:1133-1141; Dale, B. E., 1991. U.S. Pat. No. 4,600,590; Dale, B. E., 1986, U.S. Pat. No. 5,037,663). In AFEX pretreatment, lignocellulosic biomass is exposed to concentrated ammonia at elevated pressures sufficient to maintain ammonia in liquid phase and moderate temperatures (e.g. around 100° C.). Residence times in the AFEX reactor are generally less than 30 minutes. To terminate the AFEX reaction, the pretreated biomass is depressurized (flashed). The AFEX process is not limited to anhydrous ammonia with AFEX. Some water is added to the biomass, so that any anhydrous ammonia is immediately converted into a concentrated ammonia water mixture on beginning the AFEX treatment. 
         [0007]    Recovery of ammonia used in AFEX pretreatment is a key objective when integrating AFEX into a broader biomass conversion process design. The existing ammonia recovery design (Eggeman, T. 2001). Ammonia Fiber Explosion Pretreatment for Bioethanol Production, National Renewable Energy Laboratory (NREL) Subcontract No. LCO-1-31055-01), which is depicted in  FIG. 1 , calls for compressing ammonia, which is vaporized as a result of the flash operation, and separating liquid ammonia that remains in contact with the pretreated solids via evaporation in a dryer. The resulting vapor, which also contains water, is then delivered to a distillation column to purify the ammonia. The ammonia from the column is pumped up to pressure and, together with the compressed flash ammonia, is recycled to the AFEX reactor.  FIG. 1  shows the existing ammonia recovery approach. 
         [0008]      FIG. 1  shows the prior art system  10  including a closed AFEX reactor vessel  12  into which biomass, water and ammonia are introduced under pressure. Valve V 1  is used to release pressure from the vessel  12 . The treated biomass is transferred to a heated dryer  14 . The dried biomass is transferred out of the dryer  14  for subsequent treatment. Ammonia from the dryer  14  is condensed by condenser  22  and sent to slurry column  16 . Water is removed and condensed by condenser  18 . Ammonia is condensed in condenser  20  and recycled to the vessel  12 . Ammonia gas is pressurized in a compressor  24 , condensed and recycled into vessel  12 . 
         [0009]    The problem is that the processes either produce low yields of the monosaccharides and/or require large amounts of liquid ammonia or ammonium hydroxide solutions. 
       OBJECTS 
       [0010]    It is therefore an object of the present invention to provide a process which effectively combines the use of concentrated ammonium hydroxide to extract the structural carbohydrates with an effective recycling of the ammonia. Further, it is an object of the present invention to provide an economical process which enables the production of monosaccharides in high yield from the structural carbohydrates. These and other objects will become increasingly apparent by reference to the following description and the drawings. 
       SUMMARY 
       [0011]    The present invention relate to a process for the treatment of structural carbohydrates in lignocellulosic biomass which comprises: (a) reacting the biomass with a heated aqueous ammonium hydroxide solution having a concentration greater than about 30% by weight ammonia in a closed vessel at 50° C. or above at an elevated pressure from atmospheric pressure while simultaneously manipulating the temperature, a mass ratio of ammonia to a dry biomass and a mass ratio of water to the dry biomass to increase the digestibility and/or accessibility of the structural carbohydrates; (b) rapidly releasing the pressure in the vessel; (c) recovering at least some of the ammonia and ammonium hydroxide from the biomass and the solution; and (d) optionally further processing the treated biomass via enzymes, microbial conversion or animal digestive processes. Preferably the structural carbohydrates are recovered as a mixture of glucose, xylose, arabinose and other sugars in step (d). Preferably the structural carbohydrates made available by the further treatment which is the microbial conversion which produces organic acids, alcohols, and other byproducts. Preferably the carbohydrates made available by the process are utilized by the animal digestive processes in either ruminant or non-ruminant animal diets. Preferably the temperature of the mixture of ammonia, biomass and water in the closed vessel is at a temperature between about 50° C. and 120° C. Preferably the pressure in the closed vessel is between about 4 and 50 atm. Preferably ammonia gas is added to the vessel to fill any void space in the vessel. The ammonia treatment does not directly solubilize very much of the biomass. About 20% or so of the hemicellulose (xylan polymer primarily) can be solubilized, but essentially none of the glucan structural polysaccharides (cellulose) are solubilized. What happens is that they are “activated” or rendered much more susceptible to hydrolysis. The term “structural carbohydrates” means cellulose and hemicellulose. 
         [0012]    The present invention also relates to a process for the treatment of a 
         [0013]    lignocellulosic containing plant biomass comprising structural carbohydrates with water naturally present in the biomass to produce more digestible or accessible structural carbohydrates which comprises: (a) reacting the biomass with a heated aqueous ammonium hydroxide solution in an amount greater than about 30% by weight ammonia in the aqueous ammonium hydroxide solution in a closed vessel at an elevated pressure and at an elevated temperature without degrading the lignocellulose to remove the structural carbohydrates from the biomass into the solution, wherein an amount of water provided with the biomass is greater than 1% by weight and less than 50% by weight of the biomass; (b) releasing the pressure in the biomass in the vessel; (c) removing a slurry of the biomass with the structural carbohydrates from the vessel; and (d) stripping the ammonium hydroxide solution and ammonia from the slurry to provide the structural carbohydrates in the slurry, wherein greater than 85% of the available glucose in the structural carbohydrates can be recovered as a result of enzymatic hydrolysis of the structural carbohydrates. Preferably the ammonia is recycled. Preferably the sugars comprise a mixture of xylose and glucose. Preferably a temperature of the mixture of ammonia, biomass and water in the closed vessel is between about 50 and 120° C. Preferably ammonia gas is added to fill any void space in the vessel. Preferably the pressure is released rapidly. Preferably the pressure is between about 6.9 and 20.7 atm. 
         [0014]    The present invention further relates to a process for recovery of ammonia from an ammonia fiber explosion (AFEX) treatment of a lignocellulosic biomass which comprises: (a) treating the biomass with an aqueous solution of ammonium hydroxide in a closed reaction vessel under pressure to form a slurry; (b) releasing the pressure in the vessel of the reaction vessel and pumping the slurry to a stripping column; (c) stripping ammonia from an upper portion of the stripping column, using steam under pressure with removal of a stripped slurry from a bottom portion of the column; (d) introducing the stripped ammonia from the upper portion of the column into a mixer and adding water under pressure to the mixer to form a diluted aqueous ammonia solution; (e) cooling the diluted aqueous ammonia solution from the mixer; and (f) introducing the cooled aqueous ammonia solution into the reaction vessel along with the additional biomass under pressure. Preferably, the reaction is continuous. The, present invention also relates to a system for performing the process as described herein. 
         [0015]    The substance and advantages of the present invention will become increasingly apparent by reference to the following drawings and the description. 
     
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         [0016]      FIG. 1  is a process flow diagram for a prior art AFEX pretreatment with ammonia recovery and recycling. 
           [0017]      FIG. 2  is a process flow diagram for the present invention for AFEX pretreatment with an efficient ammonia recovery. 
       
    
    
     DESCRIPTION OF THE PREFERRED EMBODIMENTS 
       [0018]    Cellulosic biomass contains large amounts of structural carbohydrates or polysaccharides (cellulose, hemicellulose, and the like) that can provide much less expensive single sugars for fermentation or non-biological transformation to a variety of products or as improved animal feeds. However, these polysaccharides are difficult to access. The present invention provides pretreatment process using concentrated ammonium hydroxide under pressure to improve the accessibility/digestibility of the polysaccharides from a cellulosic biomass. The present invention preferably uses combinations of anhydrous ammonia and concentrated ammonium hydroxide solutions to obtain results that are not obtained by either dilute ammonium hydroxide or anhydrous ammonia acting alone. 
         [0019]    In the present invention the lignocellulosic material is treated with concentrated ammonium hydroxide in an amount greater than 30% by weight in an ammonium hydroxide solution. The process can be performed in a continuous reactor or a batch reactor as in the Examples. 
         [0020]    The biomass contains water which is naturally present. Typically this natural water represents about 1% to 20% by weight of the biomass. In general this natural water tends to be bound in the biomass and thus the water which is primarily relied upon is that added with the ammonium hydroxide solution. Water can also be added to the biomass and, if so, then this mixes with the ammonium hydroxide to provide the ammonium hydroxide solution. Up to 50% of the biomass can be added water. 
         [0021]    The term “lignocellulosic biomass” means a naturally derived lignin and cellulose based material. Such materials are, for instance, alfalfa, wheat straw, corn stover, wood fibers, and the like. Preferably the materials are comminuted into particles in a longest dimension. 
         [0022]    The term “structural carbohydrates” means the polysaccharide materials containing monosaccharide moieties available by hydrolysis. 
         [0023]    The mass ratio of a lignocellulose biomass to ammonia is preferably 1 to 1. 
         [0024]    The reaction temperature is preferably 90° C.; however the temperature can be between 50° C. and 120° C. 
         [0025]    The pressure is preferably between 100 psia and 300 psi (6.9 to 20.7 atm); however, pressures between 4 and 50 atm can be used. 
         [0026]    Hot ammonium hydroxide/water solutions or hot ammonia/water vapors can be added to ground lignocellulosic biomass in a contained vessel to obtain final mixture temperatures of 50° C. or above, preferably 90° C. A preferred ammonia to dry biomass mass weight ratio was about 0.2 to 1.0. A preferred water to dry biomass mass ratio was about 0.4 to 1.0. 
         [0027]      FIG. 2  shows the improved system  100  with AFEX reactor vessel. The slurry is sent directly to the stripping column  104  and condenser in condenser  106  and is sent to mixer  108  for addition of water. High pressure steam is used in the stripping column  104  to remove the ammonia from the slurry. The hot aqueous shiny is removed from the bottom of the stripping column. Condensers  110  and  112  are used to cool the water and ammonia mixture which is recycled into the vessel  102 . By comparing  FIGS. 1 and 2 , it can be seen that the process is more efficient. 
       Examples 1 to 20 
       [0028]    A 300 ml pressure vessel  102  was first filled with a given mass of corn stover wetted to the desired moisture level as indicated in Table 1 and the vessel  102  was sealed. Then a concentrated ammonium hydroxide mixture was prepared by mixing the right proportions of anhydrous ammonia and water in another pressure vessel and this mixture was added to the corn stover in the 300 ml reactor vessel  102  to achieve the desired final level of ammonia and water. In this case the target was 1 kg of ammonia per kg of dry biomass and 0.6 kg of water per kg of dry biomass. The mixture of ammonia, water and biomass was then heated to 90° C., held at that temperature for 5 minutes and the pressure rapidly released. 
         [0029]    The resulting solid was hydrolyzed to mixtures of monosaccharides containing, for example, glucose, xylose and arabinose. 
         [0030]    The results of the present invention are shown in Table 1 in Examples 2 to 15. 
         [0000]    
       
         
               
             
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Glucose and Xylose yields of ammonia treated corn stover after 
               
               
                 168 hr (7 days) for hydrolysis with a cellulose enzyme. Different 
               
               
                 ammonia concentrations were used. All runs are at 1 kg NH3: 1 Kg 
               
               
                 dry stover (BM), 90° C. reactor temperature, 0.6 kg water/kg 
               
               
                 dry stover (except for the last 4 experiments 17 to 20) and 5 min 
               
               
                 residence time. 15 FPU cellulase enzyme/gram glucan in BM. 
               
             
          
           
               
                   
                 Kg NH 3 /kg 
                   
                   
                 % 
                   
                   
               
               
                   
                 water in 
                 Ammonia 
                 Water 
                 Glu- 
                 % 
               
               
                 Expt. 
                 ammonium 
                 distri- 
                 distri- 
                 cose 
                 Xylose 
                 Re- 
               
               
                 # 
                 hydroxide 
                 bution 
                 bution 
                 yield 
                 yield 
                 peats 
               
               
                   
               
             
          
           
               
                  1(a) 
                 1 kg NH 3   
                 All NH 3   
                 All in BM 
                 92.96 
                 74.25 
                 2 
               
               
                  2 
                 0.5 
                 ¾ NH 3   
                 ½ in 
                 92.20 
                 78.85 
                 2 
               
               
                   
                   
                 and ¼ 
                 NH 4 OH ½ 
               
               
                   
                   
                 NH 4 OH 
                 in BM 
               
               
                  3 
                 0.5 
                 3.4 NH 3   
                 All in 
                 79.88 
                 64.90 
                 2 
               
               
                   
                   
                 and ¼ 
                 NH 4 OH 
               
               
                   
                   
                 NH 4 OH 
               
               
                  4 
                 0.41 
                 ⅔ NH 3   
                 All in 
                 86.60 
                 70.54 
                 1 
               
               
                   
                   
                 and ⅓ 
                 NH 4 OH 
               
               
                   
                   
                 NH 4 OH 
               
               
                  5 
                 0.58 
                 ⅔ NH 3   
                 ½ in 
                 78.23 
                 65.83 
                 1 
               
               
                   
                   
                 and ⅓ 
                 NH 4 OH ½ 
               
               
                   
                   
                 NH 4 OH 
                 in BM 
               
               
                  6 
                 0.5 
                 ½ NH 3   
                 All in 
                 57.65 
                 47.85 
                 1 
               
               
                   
                   
                 and ½ 
                 NH 4 OH 
               
               
                   
                   
                 NH 4 OH 
               
               
                  7 
                 0.8 
                 ½ NH 3   
                 ¾ in 
                 85.50 
                 70.37 
                 1 
               
               
                   
                   
                 and ½ 
                 NH 4 OH ¼ 
               
               
                   
                   
                 NH 4 OH 
                 in BM 
               
               
                  8 
                 0.66 
                 ½ NH 3   
                 ½ in 
                 97.78 
                 81.98 
                 2 
               
               
                   
                   
                 and ½ 
                 NH 4 OH ½ 
               
               
                   
                   
                 NH 4 OH 
                 in BM 
               
               
                  9 
                 0.79 
                 ½ NH 3   
                 ¾ in 
                 98.54 
                 78.70 
                 2 
               
               
                   
                   
                 and ½ 
                 BM ¼ 
               
               
                   
                   
                 NH 4 OH 
                 in NH 4 OH 
               
               
                 10 
                 0.38 
                 ⅓ NH 3   
                 All in 
                 74.52 
                 56.47 
                 1 
               
               
                   
                   
                 and ⅔ 
                 NH 4 OH 
               
               
                   
                   
                 NH 4 OH 
               
               
                 11 
                 0.73 
                 ⅓ NH 3   
                 ½ in 
                 81.51 
                 69.66 
                 1 
               
               
                   
                   
                 and ⅔ 
                 NH 4 OH ½ 
               
               
                   
                   
                 NH 4 OH 
                 in BM 
               
               
                 12 
                 0.66 
                 All NH 4 OH 
                 All in 
                 71.00 
                 57.00 
                 2 
               
               
                   
                   
                   
                 NH 4 OH 
               
               
                 13 
                 0.75 
                 All NH 4 OH 
                 ½ in 
                 96.78 
                 79.00 
                 3 
               
               
                   
                   
                   
                 NH 4 OH ½ 
               
               
                   
                   
                   
                 in BM 
               
               
                 14 
                 0.88 
                 All NH 4 OH 
                 ¾ in 
                 97.11 
                 79.00 
                 2 
               
               
                   
                   
                   
                 NH 4 OH ¼ 
               
               
                   
                   
                   
                 in BM 
               
               
                 15 
                 0.72 
                 All NH 4 OH 
                 ¼ in 
                 88.31 
                 75.37 
                 2 
               
               
                   
                   
                   
                 NH 4 OH ¾ 
               
               
                   
                   
                   
                 in BM 
               
               
                 16(b) 
                 0.3 
                 All NH 4 OH 
                 2.3 g water 
                 83.58 
                 68.18 
                 1 
               
               
                   
                   
                   
                 per g BM 
               
               
                 17(b) 
                 0.15 
                 All NH 4 OH 
                 5.6 g water 
                 70.50 
                 42.46 
                 1 
               
               
                   
                   
                   
                 per g BM 
               
               
                 18(b) 
                 0.1 
                 All NH 4 OH 
                 9 g water 
                 64.85 
                 49.31 
                 1 
               
               
                   
                   
                   
                 per g BM 
               
               
                 19(b) 
                 0.05 
                 All NH 4 OH 
                 19 g water 
                 51.26 
                 39.32 
                 1 
               
               
                   
                   
                   
                 per g BM 
               
               
                 20(c) 
                 Control 
                 No 
                 Not 
                 29.5 
                 17.5 
                 2 
               
               
                   
                   
                 ammonia 
                 applicable 
               
               
                   
               
               
                 Note: 
               
               
                 Pressures range from about 100 psia to about 300 psia except for Expt. 16-19, which are at atmospheric pressure 
               
               
                 (a)Comparative Example 1 shows the AFEX process described in U.S. Pat. Nos. 4,600,590 and 5,037,663 to Date, exemplified by FIG. 1. Comparative Examples 16 to 19 
               
               
                 (b)show the results at atmospheric pressure with ammonium hydroxide Example 20 
               
               
                 (c)shows the process without ammonia. 
               
             
          
         
       
     
         [0031]    Table 1 shows the results for the conversion of corn stover to glucose and xylose following treatment with ammonia and water. The total amount of water, ammonia and biomass and the system temperature is the same in all cases. The biomass was treated with 1 kg of ammonia per 1 kg dry biomass (the untreated stover has a moisture content of about 15% dry basis). The experiments were run at 90° C. with a five minute holding time at that temperature and the treated material of Example 1 was hydrolyzed with 15 filter paper units of cellulose per gram of cellulose in the stover. From the point of view of the final conditions to which the stover was subjected, these conditions are identical. 
         [0032]    The first two (2) columns of the Table show how this was done. For example, the column titled “Ammonia Addition” shows whether the ammonia (as NH 3 ) was added as anhydrous ammonia or as ammonium hydroxide (ammonia in water). For example, “all NF 3 ” means that all of the ammonia was added to the biomass as anhydrous liquid ammonia as in Example 1 directly from the pressure tank. “ALL NH 4 OH” means all of the ammonia was added as aqueous ammonium hydroxide. 
         [0033]    The second column shows whether the water was added to the stover directly or added as part of the ammonium hydroxide. In the first row, “all NH 3 ” and “All of the water in EM” means that all the ammonia was added as anhydrous and all of the water was in the biomass as in Example 1. The last set of rows is for “All NH 4  OH” meaning that ail of the ammonia was added as ammonium hydroxide and the water was added either to the stover or with the ammonium hydroxide. 
         [0034]    Thus, depending on how the ammonia and water are added, very different results are obtained. Eighty-five percent (85%) conversion of cellulose to glucose is used as the minimum for a cost competitive process. Using that criterion, the final column shows the % yield after 168 hours of hydrolysis for both glucose (G) and xylose (X). In no case, when all of the water was added as ammonium hydroxide (comparatively more dilute ammonium hydroxide) is the 85% criterion achieved. 
         [0035]    It appears from Table 1 that the ammonium concentration is important. Water naturally associated with the biomass does not act as free water available to dilute the ammonia. 
         [0036]    The specific features of the process of the present invention that make it more advantageous than prior art methods are as follows: (1) it does not degrade any biomass carbohydrates so that yield is not compromised due to the pretreatment; (2) high overall yields of glucose (nearly 100% of theoretical) and 85% of theoretical yields of xylose, are obtained; (3) low application rates of otherwise expensive hydrolytic enzymes are needed to obtain these yields; (4) residual ammonia can serve as a nitrogen source for subsequent fermentations or animal feeding operations; (5) treated biomass and polysaccharides can be fed at very high solids levels to subsequent process operations, thereby increasing the concentration of all products and reducing the expense of producing other chemicals from the polysaccharides; and (6) using ammonia and ammonium hydroxide combinations fits well into recovery operations for the ammonia. 
         [0037]    Markets that can use this invention include: (1) the U.S. chemical industry which is beginning to move away from petroleum as a source of chemical feedstocks and is interested in inexpensive monosaccharides as platform chemicals for new, sustainable processes; (2) the fermentation industry, especially the fuel ethanol production industry which is also interested in inexpensive sugars from plant biomass; and (3) the animal feed industry which is strongly affected by the cost of available carbohydrates/calories for making animal feeds of various kinds, 
         [0038]    The following Example 16 describes two (2) design features that reduce process energy requirements relative to existing designs of ammonia recovery for AFEX pretreatment: (1) steam stripping of pretreated material; and (2) water quench condensation of ammonia vapor.  FIG. 2  presents a process flow sheet of these features in the context of the broader AFEX pretreatment design. 
       Steam Stripping of Pretreated Material 
       [0039]    After the AFEX pretreatment is complete, the pretreated material is flashed to a lower pressure, as in the existing design. Unlike the existing design; however, the present invention uses steam-stripping of the resulting pretreated solids to recover residual ammonia. This feature enables the elimination of energy intensive solids drying that is used in the design of  FIG. 1 . The processing equipment can be similar to that used for direct steam drying of solids for which there are an increasing number of commercial examples (Kudra, T., A. S. Mujumdar, 2002. Advanced Drying Technologies, New York, N.Y.: Marcel Dekker, Inc.; Pronyk, C., S. Cenkowski, 2003. “Superheating Steam Drying Technologies,” ASAE Meeting Presentation, Paper Number RRV03-0014.). 
       Water Quench Condensation of Ammonia Vapor 
       [0040]    Ammonia vapor coming from the ammonia recovery steam stripping column is combined with ammonia vapor arising from the post-AFEX flash operation and condensed by first adding water in the mixer and then indirectly cooling the aqueous solution in two steps, first with cooling water, and then with chilled water. The condensed aqueous mixture is then pressurized via liquid pumping and recycled to the AFEX reactor. These steps eliminate the need for ammonia vapor compression that is used in the design of  FIG. 1 . 
       Utility of Invention 
       [0041]    Based on Aspen Plus (a commercially available modeling software) process simulations of the process of  FIGS. 1 and 2 , the present invention requires significantly less process energy relative to the existing design, as indicated in Table 2. Furthermore, it is anticipated that the invention will result in lower processing costs as well. 
         [0000]    
       
         
               
             
               
               
               
             
               
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                 Comparison of process energy requirements: proposed versus 
               
               
                 existing design for AFEX pretreatment with ammonia recovery. 1,2   
               
             
          
           
               
                   
                 FIG. 1 Design 
                 FIG. 2 Design 
               
               
                   
                 Required Energy 
                 Required Energy 
               
               
                   
                   
               
             
          
           
               
                 Energy Flow 
                 % feedstock LHV) 
                 (% feedstock LHV) 
               
               
                 Steam to dryer 
                 7.73% 
                 — 
               
               
                 Steam to NH 3  column 
                 2.87% 
                 3.82% 
               
               
                 Power to compressor 
                 0.02% 
                 — 
               
               
                 Power to chilled water unit 
                 — 
                 0.14% 
               
               
                 Total 
                 10.62%  
                 3.96% 
               
               
                   
               
               
                   1 Energy necessary to achieve AFEX reaction temperature is met entirely by heat of mixing between ammonia and water in the reactor. 
               
               
                   2 Both designs use the same ammonia and water loadings: 0.3 g NH 3 /g biomass; 0.5 g H 2 0/g biomass. 
               
             
          
         
       
     
         [0042]    While the present invention is described herein with reference to illustrated embodiments, it should be understood that the invention is not limited hereto. Those having ordinary skill in-the art and access to the teachings herein will recognize additional modifications and embodiments within the scope thereof. Therefore, the present invention is limited only by the claims attached herein.