the present invention relates to an improvement in a process for expanding a cellulosic material by contacting the cellulosic material with a swelling agent which impregnates the cellulosic material and then rapidly reducing the pressure to thereby expand the cellulosic material by gaseous expansion of the swelling agent , which comprises : ( a ) injecting the swelling agent and the cellulosic material into a screw in a barrel having a feed throat leading to the screw in rotating contact with the barrel along part of a length of the screw so that the screw is sealed in operation , with an inlet for feeding the swelling agent into the feed throat under pressure to the screw and with an outlet from the barrel adjacent to the screw ; ( b ) compacting the swelling agent and cellulosic material by rotation of the screw in the barrel ; ( c ) removing the swelling agent and the cellulosic material from the barrel through the outlet from the extruder so that the swelling agent expands the cellulosic material ; and ( d ) optionally recovering the swelling agent from the cellulosic material . further the present invention relates to an improved apparatus with at least one rotatable screw mounted in a barrel with opposed ends , a feed inlet to the screw through the barrel , and a feed outlet from the screw and removal through the barrel , and optional heating and cooling means between the ends of the barrel , which comprises : a liquid inlet to the screw through the barrel intermediate the ends , whereby the liquid is fed to the screw under pressure so that a cellulosic material is expanded or by change of the liquid to a gas upon removal of the cellulosic material from the barrel by the rotation of the screw . the present invention also relates to a system for expanding a cellulosic material which comprises : ( a ) an apparatus with at least one rotatable screw mounted in a barrel with opposed ends , a feed inlet to the screw through the barrel , and a feed outlet from the screw and removal through the barrel , and optional heating and cooling means between the ends of the barrel , which comprises a liquid inlet to the screw through the barrel intermediate the ends , whereby the liquid is fed to the screw under pressure so that a cellulosic material is expanded upon removal of the cellulosic material from the barrel by the liquid becoming a gas by the rotation of the screw ; ( b ) a liquid supply under pressure to the inlet of the liquid inlet ; ( c ) a confined space in which the system is placed ; and ( d ) gas removal means adjacent the ends of the barrel for removing gas which is released upon expansion of the material . the primary goal of this invention is in the use of a screw and barrel apparatus 10 ( shown in fig1 ) to improve the ammonia fiber explosion ( afex ) process , which had previously performed only in a batch reactor . effectiveness of the treatment using the extruder apparatus 10 was defined as an increase in enzymatic or rumen in situ digestibility . the first step was to develop a safe environment in which to work with ammonia . to do this , the office of radiation , chemical , and biological safety ( orcbs ) at michigan state university ( msu ), east lansing , michigan was contacted . following their advice , the area around the extruder apparatus 10 , which enclosed the supplemental ventilation units in the room , was completely surrounded with vinyl stripping to contain any ammonia leaks . testing of this enclosure was done with a smoke bomb that emitted 10 , 000 ft 3 of smoke in 1 minute , none of which was observed to escape . additionally , a horizontal fume hood 11 was attached to one of the ventilation ducts to concentrate ventilation immediately around the extruder feed 12 and outlet 13 , as well as the ammonia injection port 14 . finally , two full - face respirators with removable ammonia cartridges were purchased for use during all experimentation . a safety protocol was developed and reviewed with each person assisting in any experimentation . the extruder apparatus 10 was a baker - perkins mpc / v - 30 ( saginaw , mich .) with parallel twin screws 17 side by side , each made up of screw elements 100 , 101 and 102 and kneading blocks 200 and 201 ( fig2 to 10 ). the motor 15 supplied 3 hp at 500 rpm . the barrel 16 configuration diameter was 30 mm with a length to diameter ratio ( l / d ) of 10 : 1 . the two ( 2 ) screws 17 were co - rotating and self wiping with a variable profile . fig1 shows the position of the segments 100 , 101 , and 103 and kneading blocks 200 and 201 . table 1 shows the positions of the elements . table 1______________________________________zone element length______________________________________1 forward transport screw 3 13 / 16 &# 34 ; 2 1 kneading block 1 / 4 &# 34 ; 3 forward transport screws 1 3 / 4 &# 34 ; 4 mixing zone 5 kneading blocks , 1 / 4 &# 34 ;, 1 1 / 4 &# 34 ; each , 5 total , 45 ° alignment5 forward transport screw 6 1 / 2 &# 34 ; 6 kneading block 1 / 8 &# 34 ; 7 modified camel back discharge screw 3 1 / 2 &# 34 ; ______________________________________ the extruder apparatus 10 was supplied with controls ( not shown ) for both heating and cooling . heating was supplied by electric cartridge heaters (+ in fig1 ) in three zones along the barrel 16 and the die block 18 . cooling was supplied along the barrel 16 length by chilled water fed through cored barrel sections ( x and o in fig1 ). the dimensions are shown in table 2 . the barrel 16 and die block 18 are heated between about 30 ° c . to 100 ° c . along its length . preferably the die block 18 is heated in this range . table 2______________________________________water inlet water outlet heater locationslocations 1 1 / 8 &# 34 ; locations 1 1 / 8 &# 34 ; 1 1 / 2 &# 34 ; above andabove and below above and below below centerlinecenterline at : center line at : at : ______________________________________2 3 / 4 &# 34 ; 1 / 2 &# 34 ; 3 5 / 16 &# 34 ; 5 3 / 8 &# 34 ; 3 3 / 4 &# 34 ; 4 11 / 16 &# 34 ; 10 7 / 8 &# 34 ; 8 13 / 16 &# 34 ; 6 7 / 16 &# 34 ; 12 15 / 16 &# 34 ; 11 3 / 4 &# 34 ; 8 5 / 16 &# 34 ; 9 5 / 16 &# 34 ; 11 5 / 16 &# 34 ; 13 15 / 16 &# 34 ; 14 5 / 8 &# 34 ; ______________________________________ the die 18a through which the treated fodder was released , was air cooled . the die block 18 was provided with heaters (+ in fig1 ). all interior surfaces of the extruder apparatus 10 were nitrided with a 63 μ - inch finish which provided excellent corrosion resistance . screw elements 100 , 101 and 102 and kneading block 200 and 201 ( fig2 , 4 , 5 and 6a to 6i ) were made of heat treated alloy steel . the corrosion resistance of a single screw element 100 , 101 was determined prior to any experimentation and no corrosion was observed throughout the experimentation . a reciprocating diaphragm metering pump 50 used to deliver ammonia was an american lewa ( holliston , mass .). the pump 50 head was made of 316 stainless steel with teflon seals . the pump 50 was capable of metering 0 . 23 to 23 . 0 gph . the drive supplied 3 hp . the pump 50 was calibrated with water and the necessary conversions were done to determine the amount of liquid ammonia fed using a specified stroke length and speed setting . all tubing , fittings , and valves used were of 316 ss . the tubing used was 3 / 8 &# 34 ; od with 0 . 065 &# 34 ; walls , rated to 6500 psig . all fittings were rated to the burst pressure of the tubing . the pressure ratings of the materials used are well in the safe range . this was done to insure safety while working with ammonia . most of the connections were swagelok fittings , but a few were npt . a check valve 51 and by - pass valves 52 and 53 were provided . an ammonia tank 54 with a shut - off valve 55 was the ammonia supply . a purge valve 56 was used to clear the system of ammonia . a needle valve 57 was used to meter ammonia into the extruder apparatus 10 . biomass was fed into the extruder apparatus 10 via the feed tube 20 . a feeder 19 to the feed tube 20 was calibrated by feeding material for a known period of time and determining the mass . samples that contained different amounts of moisture were calibrated individually . the primary material investigated in this project was corn fodder or stover . the sample material is also referred to herein as biomass . this includes all above ground portions of a corn plant except the grain and cob . corn fodder was obtained in a large square bale . this material was coarsely chopped using a tractor mounted grinder . the material was then dried ( less than 5 % moisture ) and further milled to pass a 2 mm screen in a rotary knife mill . the size is between about 0 . 01 inch to 1 inch . the material was stored in plastic bags inside cardboard drums . water was added in an amount by weight 10 % to 80 %. fresh material can be used ( usually at about 80 % moisture , based upon dry matter weight ). the unmodified extruder apparatus 10 had been primarily used for processing of polymers and thus required significant modification . thus , it was necessary to make several modifications . first , a port 14 was machined to allow the injection of ammonia . the port 14 was approximately half way down the length of the barrel 16 . the port 14 was chosen to maximize the equilibration time of the biomass and ammonia . the equilibration time was approximately one ( 1 ) minute , but depended on feed rate , ammonia load , die temperature and the like . the injection port 14 was installed with a teflon seal to minimize ammonia loss through the port 14 . second , the screw 17 configuration was modified significantly in an effort to minimize ammonia loss through the feed tube 20 . additionally , two ( 2 ) camel screw elements 102 ( one shown in fig9 and 10 ) were provided at the discharge end of the screw 17 . originally these screws were flat on the end . the original design plugged the die block 18 . by building the end of each of the screw 103 into a more conical shape , the biomass was directed into the die block 18 and out through the die 18a , rather than plugging . the ammonia used was supplied in a 50 lb . cylinder 54 equipped with a dip tube to insure liquid delivery . the pump 50 allowed for control and accuracy in the delivery of ammonia . a check valve 51 was installed just prior to the injection port 14 to maintain the pressure on the ammonia in the tubing after the pump to help insure liquid delivery . once the pressure generated by the pump 50 reached the cracking pressure of the check valve 51 , the ammonia would flow directly into the extruder apparatus 10 . the reseal pressure was set above the vapor pressure of ammonia to prevent any leakage through the check valve 51 . several bypass valves 52 and 53 were provided to allow the tubing to be purged by purge valve 56 after use of the extruder apparatus 10 to clean the apparatus . once it was verified that ammonia and biomass would flow together through the extruder apparatus 10 , increasingly restrictive dies 18 were used . at first , the die block 18 was not used . however , as more confidence was gained , the block 18 was added , as well as die 18a . several explosions were obtained with only the block 18 in use , but the enzymatic digestibility of the samples was only moderately higher than the untreated samples . additionally , the increased pressure generated from a smaller orifice of the die 18a provided a more effective treatment . much work has been done on the design of extrusion dies 18a . however , the biomass mixture is unlike any polymer or food which can be extruded throughout a standard die . several preliminary dies 18a were tried with minimal success . these were machined by hand and the rough edges and interior surfaces created problems with biomass flow through the restriction . the die 18a that proved most useful was machined with a 5 ° end mill to give a smooth , gradual contraction of 40 % of the inlet area ( i . e ., out let was 60 % of the area of the inlet ). with this die block 18 , explosions could be consistently obtained . this die 18a is shown in fig1 , 14 and 15 . the dimensions are shown as follows : larger orifice is the inlet and faces the extruder . ## equ1 ## area of smaller orifice = 0 . 268 in 2 the explosions typically came at regular intervals . some trials showed reproducibility of ± 15 seconds . depending on the ammonia load and temperature , the steady state operation was either continuous or periodic . higher loads of ammonia (& gt ; 1 . 5 mass ammonia / mass biomass ) prompted the material to slowly discharge from the extruder apparatus 10 for several minutes and then violently discharge from the die 18a . ammonia loads are given in a mass ratio . for example , an ammonia load of 3 signifies 3 pounds ( or kilograms , or grams , etc .) of ammonia to 1 pound ( or kilograms , or grams , etc .) of dry biomass . hereafter , ammonia loads are given m / m units , connoting mass to mass ratio . pressure was observed to build to 300 psig , and torque would approach 50 %, until the explosion where pressure would drop to 0 psig and - 11 % torque ( typical no load value ). alternatively , lower amounts of ammonia (& lt ; 1 . 5 m / m ) demonstrated continuous minor explosions which was the preferred mode of operation . other modifications were made as well . for example , teflon sheeting was used to minimize extruder pressure loss . it was observed several times that two metal - metal interfaces ( the interface of the extruder apparatus 10 and die block 18 , as well as between the die block 18 and the die isa ) were allowing a portion of the high pressure to escape as evidenced by slight foaming at the interface . the teflon sheeting ( not shown ) was cut to fit around the orifice that it sealed and was then installed between the two surfaces . after the installation of these seals , no further foaming was observed . the main parameters varied were temperature and ammonia loading . water content of the biomass was also varied , but with little success . moisture content higher than 60 % led to the water being squeezed out of the biomass and flowing back to the biomass feed port . biomass moisture levels are given as the percent of total mass ( 60 % moisture is 60 grams of water in 100 grams of a biomass and water mixture ). this created problems with feeding the biomass into the extruder apparatus 10 due to foaming in the feed tube 20 caused by the ammonia . alternatively , moisture levels lower than 60 % did not allow for effective equilibration with the ammonia , and hence , no explosions were obtained . thus , all trials referred to in the results section were obtained at 60 % moisture . temperature was varied in several ways at zones 1 to 3 of fig1 . typically , first zone 1 , centered on the biomass feed port , was unheated and cooling was shut off . in this case , heating refers to heating above room temperature . the cooling ability of the first zone was removed because it created condensation around the feed port that led to clogging of the feed . the second zone 2 , at the ammonia injection point 14 was heated slightly , depending on the set point temperature of the die block 18 . too much heating would vaporize the ammonia and result in a less effective treatment . the third zone 3 was usually heated to a temperature near the average of the set points of the second zone and the die block 18 ( fig1 ). the die block 18 temperature was considered the reaction temperature . it appeared that there was an upper bound to the die block 18 temperature , as no explosions were obtained above a set point of 70 ° c . this is probably due in part to partial vaporization of the ammonia in the third heating zone 3 . the die temperature necessarily caused a temperature rise in the third zone 3 by conductive heat transfer . this leads to an increased amount of ammonia vaporization and a less effective treatment . additionally , the ammonia can be forced out through the biomass feed tube 20 because of a higher die block 18 temperature . because the ammonia was not trapped as effectively as desired , the vapor was free to leave the extrusion apparatus 10 . lower temperature treatments would not generate as high a pressure towards the feed tube 20 and are not as subject to this effect . ammonia load was the other main parameter varied . the ammonia load was varied from 0 . 5 to 2 . 0 m / m . the calculated ammonia load is only an estimation of the actual treatment amount . the extruder apparatus 10 used had a relatively small l / d ( 10 : 1 , d = 30 mm ), with a measured barrel 16 length of about 15 . 25 &# 34 ; and the only practically allowable port 14 for ammonia injection was approximately half way down the barrel 16 . this created some problems with ammonia flowing back through the biomass feed tube 20 . several efforts were made , by altering the screw 17 configuration , to create a zone of high mixing prior to the ammonia injection port 14 that would effectively provide a plug that would restrict ammonia flow back to the feed tube 20 . the screw elements 100 , 101 and 102 and kneading blocks 200 and 201 are set forth in table 2 . the first three screw elements 100 , 101 and 102 were permanently attached to the screw shaft due to the stresses of heating and cooling . these first sections were predominately forward transport screws which typically run at 50 % capacity and did not provide an effective restriction . thus , with a limited amount of the screw shaft available to implement the mixing zone , only five ( 5 ) mixing paddles could be used . there were other limitations with regard to the mixing zone . kneading blocks 200 and 201 are aligned on an individual rod 105 at various angles . when kneading blocks 200 and 201 are aligned at angles from 0 to 90 ° as shown in fig6 a , 6b , 6c , 6d , 6e , 6f , 6g , 6h and 6i , the forward transport of the mixing zone increases as the angle approaches 45 ° from either direction , and decreases as the angle diverges away from 45 °. angles are determined by looking down the rod 105 from the discharge end 15 , i . e ., towards the feed tube 20 . the angle given is the angle of the outermost kneading block 201 to the next one 200 down the shaft 21 . for example , kneading blocks 200 and 201 aligned at 30 ° have one paddle on the shaft , and the next one rotated 30 ° clockwise with respect to the previous . at 0 ° there is no mixing , and at 90 ° there is maximum mixing . kneading blocks 200 and 201 aligned at negative angles are reversing and force the flow in the opposite direction . the following table shows the conveyability of the kneading blocks 200 and 201 where f is forward and r is reverse . ## equ2 ## several mixing zone alignments were tried , but most of them were torque limited . in other words , only a small amount of biomass could be fed through the machine before the torque would approach its maximum value . torque limits are dependent on rotation speed of the dual shafts 21 ( supported by rods 105 ). thus , a 45 ° mixing zone was implemented . this allowed for a good plug to be formed and also permitted a large flow of biomass . inspection of the screw elements 100 and 101 after filling showed that the mixing zone prior to port 14 was ˜ 90 % full , while other sections beyond the port 14 were ˜ 50 % filled . unfortunately , the length of the mixing zone was not long enough to provide a significant restriction for the ammonia vapors . so , some of the injected ammonia was lost through the feed tube 20 due to vaporization . thus , the actual amount of ammonia used in a treatment is somewhat uncertain , but all runs were categorized by the amount of ammonia injected . initially , the primary means of quantifying the effectiveness of the process was enzymatic hydrolysis . since the main goal was to prove the screw in barrel technology for delivering afex worked , maximum sugar concentrations were not the focus , but rather relative digestibility . thus , all samples were hydrolyzed in a ph = 4 . 8 citrate buffer with a cellulase loading of 15 iu / g and a β - glucosidase loading of 1 ml / ml of cellulase . the cellulase used was celluclast and the β - glucosidase used was novo 188 , both by novo nordisk ( franklinton , n . c .). all samples were hydrolyzed at 50 ° c . in an agitated water bath in a 5 % ( weight ) solution for up to 48 hours . the primary analysis took place on a lead hplc column for glucose , xylose , galactose , arabinose and mannose . other analyses were done on an acid column which gave glucose and composite sugar peak which consisted of xylose , mannose and galactose concentrations . finally , a ysi ( yellow springs , ohio ) instrument was also used and gave glucose concentrations . use of the die block 18 alone gave an explosion that resulted in total sugar ( the sum of the concentrations of glucose , xylose , galactose , arabinose and mannose ) concentration after enzymatic hydrolysis for 24 hours of 2 . 4 times that of completely untreated sample . the glucose concentration of this material was 2 . 1 times that of the completely untreated material after the same amount of time . the same material gave a total sugar concentration 2 . 0 times greater than the biomass treated in a screw in barrel apparatus without ammonia and the corresponding glucose concentration was 2 . 5 times that of the biomass treated in a screw in barrel apparatus without ammonia . further trials with the die block 18 alone ( without die 18a ) gave total sugar concentrations as much as 3 . 5 times greater than the unprocessed material and 3 . 4 times greater than untreated material after 24 hours of hydrolysis . the best results obtained with the die 18a showed a total sugar concentration 2 . 4 times greater than the completely untreated material after 6 hours of enzymatic hydrolysis . the glucose concentration at this point was 2 . 3 times greater than that obtained from completely untreated material . in general , the most effective treatments for enzymatic hydrolysis were lower temperature runs . the higher the die block 18 temperature used ( greater than 70 ° c . ), the less effective the treatment . this may be due in part to more of the ammonia escaping the apparatus 10 at a higher temperature . however , with a lower temperature , the ammonia will remain in contact with the biomass longer and a more effective treatment is the result . the results of these tests are shown in fig1 to 22 and table 3 . table 3______________________________________treatment matrix for in situ trialsample temperature ° c . ammonia moisture______________________________________a - untreated 50 n / a 60 % b no heat 1 . 0 60 % c 55 1 . 5 60 % d 65 0 . 8 60 % e 65 1 . 0 60 % f 65 1 . 5 60 % g 65 1 . 6 60 % h 65 2 . 0 60 % i 55 1 . 5 60 % ______________________________________ after enzymatic digestibility tests , the ruminant digestibility of the material in an in - situ trial was desired . to accomplish this , several samples were generated with different temperature treatments and ammonia loads . these were taken to the texas a & amp ; m university animal science department ( college station , tex .) and analyzed by in - situ digestibility . samples were analyzed on a dry basis for weight loss over a known period of time . the material was placed in a small permeable bag of known weight and dried to determine the mass of dry matter . the bags were then placed in the rumen of a fistulated steer . this is a steer that has had a tube surgically inserted that allows access to the animal &# 39 ; s rumen . by removing the bags at specific intervals ( 0 , 3 , 6 , 12 , 24 , 48 and 96 hours ), thoroughly rinsing and drying , the digestibility of the materials was determined as percent of material weight lost . the weight loss of the material in a specific bag is called the dry matter digestibility , or dmd . an in - situ trial was run . the trial focused on screw in barrel treated materials , with the control being a sample treated at 50 ° c . with no ammonia . results of the trial are shown in fig2 to 29 . the 48 hour digestibility of the trial is tabulated in table 4 . the trial showed that the digestibility of the extrusion treated material at 48 hours was up to 77 . 4 % digestible as compared to the digestibility of 63 . 0 % of the screw in barrel treated but untreated ( by ammonia ) control . typical rumen passage time is 48 hours or less . table 4______________________________________48 hours dry matter digestibility for trialid dmd nh . sub . 3 load t (° c .) ______________________________________f 77 . 4 1 . 5 65h 76 . 1 2 . 0 65c 73 . 5 1 . 5 55i 73 . 4 1 . 5 55e 71 . 6 1 . 0 65g 70 . 5 1 . 6 65b 70 . 4 1 . 0 0d 68 . 0 0 . 8 65a 63 . 0 0 . 0 50______________________________________ notes : dmd is the dry matter digestibility , reported as a percent . nh . sub . 3 load is the mass of ammonia injected per mass of biomass treated . t (° c .) is the die setpoint . at 48 hours , the effects of temperature and ammonia loading are not extremely clear . the two most effective treatments obtained are at 65 ° c . with an ammonia load of 1 . 5 and 2 . 0 ( samples f & amp ; h respectively ). the digestibility of f ( 77 . 4 %) was only slightly greater than h ( 76 . 1 %). however , sample g , with an ammonia load of 1 . 6 m / m and temperature 65 ° c . was only the 6th most digestible material , at 70 . 5 %. the third and fourth most effective treatments ( samples c and i respectively ) are duplicate samples and show excellent agreement in that they are separated by only 0 . 05 % points and have an average digestibility of 73 . 5 %. samples i and c were generated at an ammonia load of 1 . 5 m / m with a temperature of 55 ° c . throughout the trial , samples h and f were consistently the most digestible , with sample h being the most digestible at all time points except 48 and 96 hours . the composition of each material at each time point was determined as well . assays were used to determine the amount of neutral detergent fibers ( ndf ), acid detergent fibers ( adf ), lignin and insoluble ash . the ndf assay gave the amount of cellulose , hemicellulose , lignin and ash in a sample . the adf procedure removed the hemicellulose , the lignin procedure removed the cellulose , and the ash procedure removed the lignin . cellulose and hemicellulose are both considered somewhat digestible while lignin is considered indigestible . thus , a reduction in apparent lignin content is desired , and this has been achieved . results show that the lignin content of the samples treated in the apparatus at 65 ° c . were reduced up to 20 . 9 % as compared to the control which was treated in the apparatus without ammonia , with an average of 11 . 9 % reduction . the rate at which digestion occurs is important as well . in all cases , the initial rate of digestion for all ammonia treated samples was higher than the material treated in the apparatus but without ammonia . in this case , the initial rate of digestion was determined as the rate of digestion between hours 3 and 6 . in many cases , the samples gained weight from the 0 to 3 hour samples which does not provide acceptable data . this may be explained by insufficient washing of the 3 hour samples which would leave dust , soluble fractions and microbes trapped in the bag . another explanation is that the material used to fill the 0 hour bags contained more dust than the 3 hour sample , and would thus allow for more material to be rinsed out . the maximum rate of digestion was 2 . 25 times that of the control in the trial ( untreated control ). the maximum observed rate was shown by sample h at 6 . 16 %/ hr . the data also show that both hemicellulose and cellulose fractions decrease over time implying the digestion of these components is occurring . the hemicellulose content of the first trial decreased until 12 hours , rose at 24 hours , then decreased again until test completion . the cellulose fraction rose until 12 hours and then dropped off . this suggests that the hemicellulose is being digested first , until the cellulose is effectively broken down , then the hemicellulose is digested again . as expected , the indigestible lignin concentration steadily increased as the trial progressed . in examples 1 and 2 , the screw in barrel apparatus 10 was used to facilitate the afex process . the total sugar yield from enzymatic digestibility of the corn fodder has been increased up to 250 %, and the in - situ ruminate digestibility has increased 32 % ( from 53 . 8 % to 71 . 2 %) over the completely untreated sample . additionally , the total sugar yield from enzymatic digestibility of the corn fodder has been increased up to 240 %, and the in - situ ruminate digestibility has increased 19 % ( from 63 . 0 % digestible to 77 . 4 %) over the material that was treated in the screw in barrel apparatus with no ammonia . the screw in barrel process also gave results that compare well with the batch process , leading to the conclusion that such a process can be made as effective as the batch process has proven to be . other results of the trials are encouraging as well . a reduction in apparent lignin is desired and have been achieved with an average decrease of 11 . 9 % ( maximum reduction of 20 . 9 % from 8 . 42 % to 6 . 66 %). a high rate of digestion has also been observed . the highest rates of digestion were 2 . 3 times the rate of digestion experienced by the control used in the respective trials . finally , the higher level of reduction of cellulose and hemicellulose observed during the trials implies utilization of these constituents . the system of the present invention can be used to recover the gas removed by the hood 11 . conventional gas ( ammonia ) receiving is used . this aspect of the present invention is well known to those skilled in the art . various types of equipment can be used to practice the present invention . plastics extruders can be modified to practice the invention . also , pulping defibrillators can be modified to perform the process of the present invention where the screw is in closely spaced contacting relation with a barrel . all of these variations will be obvious to those skilled in the art . it is intended that the foregoing description be only illustrative of the present invention and that the present invention be limited only by the hereinafter appended claims .
a process and screw in barrel apparatus for expanding cellulosic materials is described . the expanded cellulosic material is useful as an animal feed and a nutrient source for fermentation processes .