Patent Application: US-536501-A

Abstract:
a process for producing plastic / wood fiber composite foamed structures includes the steps of pre - drying wood fiber filler ; mixing it with plastic to form a mixture ; feeding the mixture into an extruder ; introducing and mixing a blowing agent ; subject the mixture to high shear forces and extruding the mixture to produce a plastic / wood fiber composite foamed structure . the filler has a degradation temperature and an active volatization temperature . during the pre - drying step the temperature is maintained below the degradation temperature . during the mixing step the mixing temperature is maintained below the active volatilizing temperature . during the introducing and mixing step a blowing agent is introduced into the plastic / wood fiber mixture and is mixed therewith to produce a plastic / wood fiber / gas mixture . during the subjecting step the plastic / wood fiber / gas mixture is subjected to high shear forces in the presence of high pressures and the temperature is maintained below an active volatilizing temperature .

Description:
the objective of the invention is to produce fine - celled plastic / wood - fiber composite foams . a fine - celled structure is characterized by uniform distribution of a very large number of cells or voids . in order to ensure fine - celled morphology , the contents of moisture and other volatiles such as extractives of wood - fibers need to be reduced as much as practicable , using any of the standard drying techniques , such as , online devolatilization , oven drying , hot air convective drying , drying in k - mixer and the like . generally the wood - fibres are dried as much as possible and heated to a temperature below the degradation temperature . that is the wood fiber should not be heated so high that the structural integrity of the wood is degraded . in the moisture or volatile - free mixture , a chemical blowing agent ( cba ) or a physical blowing agent ( pba ) is introduced with other additives , and the processing parameters are optimized so that the blowing gases are finely dispersed or dissolved into the polymer matrix under high temperature and pressure . the molten composite mixture or solution is subjected to a rapid pressure drop under predetermined processing conditions to produce fine - celled plastic / wood - fiber foams . moreover , optionally adopting techniques for reducing the processing temperature can assist the shaping of extrudate and the control of foam density . the above - described method can be embodied in at least the following six processes : process a : drying or devolatilizing the moisture and other volatiles such as extractives , using any conventional technique , at a temperature lower than the degradation temperature and generally lower than 170 ° c . or slightly higher and using the pba foaming process , in which the maximum processing temperature is maintained lower than the active volatilization temperature , generally 170 ° c ., to generate a fine - celled structure in the plastic / wood - fiber composites . process b : devolatilizing the moisture and other volatiles , through a vent at the intersection of two cascading extruders , at a temperature lower than the degradation temperature and generally lower than 170 ° c . and using the pba foaming process , in which the maximum processing temperature is maintained lower than active volatilization temperature , generally 170 ° c ., to generate a fine - celled structure in the plastic / wood - fiber composites . process c : drying or devolatilizing the moisture and other volatiles , using any conventional technique , at a temperature lower than the degradation temperature and generally lower than 170 ° c . or slightly higher and using the cba foaming process , in which the maximum processing temperature is restricted to the minimum level required to decompose the blowing agent and preferably is less than the active volatilization temperature , to generate a fine - celled structure in the plastic / wood - fiber composites . process d : devolatilizing the moisture and other volatiles , through a vent at the intersection of two cascading extruders , at a temperature lower than the decomposition temperature of the cba and preferably lower than the degradation temperature , and using the cba foaming process , in which the maximum processing temperature is restricted to the minimum level required to decompose the blowing agent and preferably is lower than the active volatilization temperature , to generate a fine - celled structure in the plastic / wood - fiber composites . process e : utilizing the volatile emissions given out by the wood - fiber to generate a fine - celled structure in the plastic / wood - fiber composites without using any blowing agent , and using a single extrusion system with pre - dried wood - fibers , in which substantial volatile material has been removed during the drying process . process f . utilizing the volatile emissions given out by the wood - fiber to generate a fine - celled structure in the plastic / wood - fiber composites without using any blowing agent , and using a tandem extrusion system with a devolatilizing vent using un - dried wood - fibers . for process a , the present invention focuses on removal of moisture and / or other volatiles such as extractives of wood - fiber and utilization of a gaseous pba for fine - celled foaming of plastic / wood - fiber composite foams with a significantly improved cell structure . the main advantages of using an inert pba , are that it is non - hazardous and more economical than other blowing agents . the pba used can be any of the non - reactive gases such as co 2 , n 2 , he , ar , air , etc ., or a mixture of these gases in any combination and proportion . when the pba is injected in the extruder barrel , it usually acquires a supercrtical state . the processing temperatures and pressures in the barrel are usually sufficiently high for this to happen , even though the injected pba may be in a liquid , gas or super critical state . the supercritical point , i . e . the critical temperature and the critical pressure , of most of the non - reactive gases is lower than the conditions prevailing in the extruder barrel , so that the above statements apply to nearly all of them . the processing conditions in the barrel are maintained so as to dissolve , or well disperse , all the gas in the supercritical state into the polymer matrix . the dissolution of the gas into the polymer will depend upon the solubility of the gas in the polymer at the barrel temperature and pressure . we can choose to inject , either a soluble amount of gas or , if needed , an amount greater than the solubility limit and cause it to be finely dispersed by adjusting the conditions in the barrel . since the solubility of gas in the polymer is almost proportional to the pressure , the injected gas will not be completely dissolved in the polymer if the pressure is lower than the solubility pressure . although the cell structure is observed to be better , in general , by completely dissolving the gas , according to our experimental results , very fine cell structures have also been achieved by finely dispersing the gas bubbles using an effective mixing device . whether the injected gas completely dissolves in the polymer or not , a fine cell foam can be made from the plastic / wood - fiber composites using the developed systems as long as the volatiles are not generated from the wood - fibers during processing . extensive experimental results show that the volatiles , including moisture , coming out of the wood - fiber during extrusion processing in general deteriorate the cellular structure of plastic / wood - fiber composite foams . in order to produce a fine - celled structure , the role of the blowing agent should be dominant and the role of the volatiles should be minimized . in order to minimize the amount of volatiles coming out of wood - fibers during processing , the wood - fiber should be dried or devolatilized enough and the processing temperature should be maintained low enough so that additional evaporation of volatiles is reduced . in brief , the strategy adopted is that , the wood - fibers are pre - dried or pre - devolatilized by using any one of the commonly used industrial methods , such as , oven drying , hot air convective drying , drying in k - mixer and the like , while maintaining the drying temperature below the degradation temperature and generally lower or slightly higher than 170 ° c . then the dried wood - fiber is mixed with the polymer powder / pellets , a coupling agent , and a cell - nucleating agent , such as talc , in a dry blending tumbler to generally achieve homogeneity . the blended mixture is then fed into an extruder through a feeder . a special feeder may be required because the natural adhesiveness of the wood fiber may prevent the mixture from being gravity - fed into the extruder from the hopper . the pre - dried wood - fibers and additives are plasticized and uniformly dispersed in the plastic matrix , in the initial section of an extruder . the pba is injected and dispersed or dissolved in mid and final zone of the extruder . the temperature of the melt can be reduced optionally and finally it is extruded through a die with a rapid pressure drop ( more than 1000 psi across the die ) to induce large nucleation . the temperature of the melt may not have to be decreased for high - density applications . controlling the die and melt temperatures controls the expansion ratio . in order to maximize the removal of the volatiles , including moisture , while preventing degradation , the wood - fibers are dried at a temperature below the degradation temperature and generally lower or slightly higher than 170 ° c . in extrusion processing , care should be taken that the processing temperature does not exceed the drying temperature . it was found that at higher temperatures , the moisture is continually released at a gradual rate , even if it has been completely dried at that temperature . in other words , additional moisture is released even though the wood - fiber has been pre - dried at the processing temperature , and the amount of this moisture will depend upon the extrudates &# 39 ; residence time and processing temperature in the equipment . thus , an additional important processing parameter is to minimize the residence time so that the moisture content can be minimized while maintaining or preferably decreasing the processing temperature below the active volatilization temperature generally below 170 ° c . the use of pba is particularly suited for this process , as the higher temperature required to decompose a cba is not needed . another beneficial effect of using the inert gas co 2 or n 2 ( pba ) is that it has a plasticizing effect on the polymer / wood - fiber mixtures , therefore , not only would it aide in the dispersion of wood - fiber in the plastic , but would also enable higher content of wood - fiber to be used . the plasticizing effect may also enable materials , such as polypropylene ( pp ) and polystyrene ( ps ) for which a higher processing temperature is needed , to be processed at temperatures lower than 170 ° c ., so that the detrimental effect of moisture or other volatiles may be reduced . process description : fig1 ( a - d ) show the different configurations possible for this process . in the preparatory stage , the wood - fibers are pre - dried or devolatilized by using any one of the commonly used industrial methods , such as , oven drying , hot air convective drying , drying in k - mixer and the like , while keeping the drying temperature below or slightly above 170 ° c . this is necessary to ensure that the volatiles do not evolve and deteriorate the cell morphology of the final extrudate in extrusion processing . then the dried wood - fibers are mixed with the polymer powder / pellets , a coupling agent , and a nucleating agent , such as talc , in a dry blending tumbler . the blended mixture is then fed into an extruder 20 through a feeder 22 . in this example the extruder 20 is a twin screw extruder but it could also be a single screw extruder . a special feeder may be used because the natural adhesiveness of the wood fiber may inhibit the mixture from being gravity - fed into the extruder 20 from the hopper . this mixture is plasticated and further mixed in the initial sections of the screw . in the mid zone of the extruder , a metered amount of physical blowing agent ( pba ) is injected into the polymer / wood fiber matrix at 24 . for example as shown in fig1 a , the pba is co 2 which is stored in a pba tank 26 . a positive - displacement pump 28 may be used to inject the pba into the mixture . a numeric controller or valve 30 is used to meter the flow of the pba into the mixture . a second valve 31 is used for filling the pump with pba from the pba tank . during this filling process , the numeric controller or valve 30 between the pump 28 and the extruder 26 is closed . during extrusion foaming operation , the second valve 31 is closed and numeric controller is opened . this mixture is then subjected to high shear forces by the screw and / or by any type of mixers , in the presence of high pressure ( typically the pressure is higher than 2000 psi ). this ensures the complete dissolution or thoroughly uniform dispersion of the pba gases into the polymer matrix . during this process some additional moisture or volatiles may be released from the wood - fiber , but this is difficult to avoid . to reduce these emissions , the residence time in extruder 20 should be minimized . optimally , the melt temperature of the polymer / gas mixture can be homogeneously reduced in a heat exchanger 32 . a commonly well - known static mixer in a cooling heat exchanger wherein the mixer has vanes positioned such that the core fluid is transported away from the center and the peripheral material is moved to the core . the mixer housing is enclosed in a jacket through which the cooling fluid flows . such a mixer is shown in fig1 a may be used . the mixture passes from the heat exchanger 32 to a die 36 . for high wood - fiber content a cooling extruder 34 , shown in fig1 b , may be used as a cooling device instead of a heat exchanger with a static mixer . added cost of an extruder can be justified by achieving higher pressure at the die if cooling is required . the extrudate finally passes through the die where its pressure is rapidly dropped , which produces a large number of nucleation sites due to the spinodal decomposition of polymer and gas . the gas from the adjacent polymer matrix diffuses into these sites and causes expansion . the temperature of the die can be controlled so as to freeze the surface layer of the polymer , which prevents the diffusion of gases into the atmosphere . this in turn helps in achieving expansion . the die temperature can also be lowered to control the unfoamed skin thickness of the extrudate for the profile dies . the profile dies can be based on the celuka die [ 23 , 24 ], where a dividing mandrel is inserted and foaming is induced to occur inward . the art of celuka die is well known as described in references 23 and 24 . the profile die can also be of other non - celuka designs . fig1 c and 1 d illustrate the use of a single screw extruder 38 instead of a twin screw extruder shown in fig1 a and 1 b . otherwise the configurations shown in fig1 c and 1 d correspond with fig1 a and 1 b , respectively . high - density polyethylene ( hdpe 2710 ) supplied by nova chemicals was utilized in the experiments . the 05 wt % wood - fibers used were standard softwood ( pine ) grade 12020 , supplied by american wood fibers . the physical blowing agent ( pba ) was commercial co 2 from matheson gas products . 3 wt % coupling agent was used for improving the adhesion between the hydrophobic pe and the hydrophyllic wood - fiber . the coupling agent was fusabond adhesive resin e - mb - 100d from dupont , canada . wood - fibers were dried in vacuum oven at 105 ° c . for 12 hours to remove the moisture and volatiles . all the materials were used as received a schematic of the equipment for process a is shown in fig1 a . in the preparatory stage , wood - fiber oven - dried at 105 ° c . for 12 hours is mixed with the polymer powder / pellets , a coupling agent , and a nucleating agent such as talc in a dry blending tumbler , and fed into the extruder 20 , using a feeder 22 . a metered amount of co 2 ( 4 wt %) was injected into the molten polymer / wood - fiber mixture at 24 in the barrel , using a positive displacement pump . in experimental setup herein the injection site was about ⅔ rd away from inlet . however , it will be appreciated by those skilled in the art that the actual location is not important as long as the polymer has been already melted completely by the time the melt gets to the location of the gas - injection port and as long as the pressure at this port is high enough to be able to dissolve all the injected gas . the pressure in the extruder and downstream was maintained high enough to expedite dissolution of co 2 into the plastic matrix . however , the processing temperature was not increased over 155 ° c . to minimize the release of further moisture or volatiles and to prevent the thermal degradation of wood - fiber . the temperature of the melt was then homogeneously lowered in a heat exchanger 32 . finally , it was extruded out through a die 36 where the surface temperature was further reduced to stabilize the foam . samples were taken at various nozzle temperatures for density measurement and cell morphology characterization the removal of moisture and other volatiles , injection of co 2 , dissolution of co 2 , cooling , and the rapid pressure drop ( more than 1000 psi across the die ) resulted in a significant improvement of the cell structure of foams . the scanning electron micrographs ( sems ) of the foams produced on the system described herein clearly reveal that the cell structure was much more regular and smaller in size when compared to the foam structure obtained using un - dried wood - fibers . the largest cells were smaller than 200 microns and the distribution of cell size was very uniform . the density of hdpe / wood - fiber composite foams was successfully controlled to be in the desired range of 0 . 5 g / cm 3 to 0 . 8 gl 3 by controlling the amount of pba and the die temperature . the surface quality was dramatically improved with the dried wood - fibers . foams obtained from un - dried wood - fibers from single extruder system exhibited a very non - uniform cell structure and a rough surface . the cross - sectional dimensions were very irregular and blister like bubbles were present on the surface . for the foams produced by the process described herein , the surface finish was smooth and regular . most of the prior art drying methods for drying the wood fibers suffer from two disadvantages . firstly , they involve costly batch processing which is not desirable for continuous processes . secondly , the wood - fiber cannot be heated to a temperature higher than 100 ° c . for a longer period without causing its degradation with the presence of oxygen . to overcome some of these disadvantages cascade extruders may be used for devolatilization and removal of moisture and other volatiles while the molten plastic is transferred from one extruder ( or compounder ) to the second extruder in a tandem or cascade arrangement . controlling the material feed rate from the first extruder into the second extruder controls the material loss at the vent . if there is any flow out of the vent , it can be suppressed by reducing the rotational speed of the first extruder and / or by reducing the feed rate into the hopper . process description : process b is a subset of process a in which online devolatilization , instead of separate batch process drying , is used for purging out the moisture and other volatiles from the plastic / wood - fiber / additives mixture . the strategy adopted is that , the un - dried wood - fibers , plastic and additives are dry blended and the blended mixture is then fed into an extruder through a feeder 22 . the first extruder 40 can be a single or twin - screw mixing extruder or compounder , where plastication and mixing takes place . during this process most of the moisture and other volatiles are evaporated due to the elevated temperature ( typically between 145 ° c . to 170 ° c .). the molten mixture is then devolatilized at a vent 41 in a cascade extrusion system and conveyed into the second extruder . on - line devolatilization can be accomplished within the first extruder if a twin screw extruder is used as the first extruder , and devolatilizing ports 51 can be opened along the screws as shown in fig8 and 9 . in the second extruder 42 , a metered amount of physical blowing agent ( pba ) is injected into the polymer / wood fiber matrix at 44 . this mixture is then subjected to high shear forces by the screw and / or by any type of mixers , in the presence of high pressures ( typically the pressure is above 2000 psi ). this ensures the complete dissolution or thoroughly uniform dispersion of the pba gases into the polymer matrix . during this process some additional moisture or volatiles may be released from the wood - fiber , but this is difficult to avoid . to reduce these emissions , the residence time should be minimized . optionally , the melt temperature of the polymer / gas mixture can be homogeneously reduced in a heat exchanger 32 . a commonly well - known static mixer in a cooling heat exchanger shown in fig2 a can be used . as above , for high wood - fiber content a cooling extruder 34 , shown in fig2 b , can be used as a cooling device instead of a heat exchanger 32 with a static mixer . the extrudate finally passes through the die 36 where its pressure is rapidly dropped , which produces a large number of nucleation sites due to the spinodal decomposition of polymer and gas . the gas from the adjacent polymer matrix diffuses into these sites and causes expansion . the temperature of the die can be controlled by a cooling jacket and a band beater so as to freeze the surface layer of the polymer , which prevents the diffusion of gases into the atmosphere . this in turn helps in achieving expansion . the die temperature can also be lowered ( from around 150 ° c . down to melting temperature of pe , which is typically around 130 ° c .) to control the unfoamed skin thickness of the extrudate for the profile dies . the profile dies can be based on the celuka die [ 23 , 24 ], where a dividing mandrel is inserted and foaming is induced to occur inward . the profile die can also be of other non - celuka designs . in regard to processes a and b , the results were observed to be best when the highest processing temperature was maintained lower than 170 ° c . it seems that processing the composites under 170 ° c . substantially prevented the generation of moisture and other volatiles . the tga analysis also confirmed this observation , as it was observed that the weight loss rate of wood - fibers increased at temperatures higher than 170 ° c . it seemed that a severe degradation of wood - fiber occurs and thereby severe deterioration of mechanical properties of plastic / wood - fiber composites occurs above 205 ° c . however , even before the degradation of the mechanical properties of wood - fiber , there seems to be an excessive amount of weight loss above 170 ° c ., according to the tga results . this is probably due to the evaporation of some of the extractives / volatiles , when heated above 170 ° c . although the mechanical properties may not be appreciably affected due to loss of some of these extractives / volatiles , the evaporation of these materials significantly contributes to the deterioration of foam structure . therefore , it is preferably to reduce these emissions by minimizing the processing temperatures and residence time , even if the wood - fibers were well devolatilized before processing . hdpe grade 2710 from nova was used as the base polymer for the composites . 50 wt % standard wood - fibers softwood grade 12020 , supplied by american wood fibers , were used . 3 wt % coupling agent ( fusabond adhesive resin e - mb - 100d from dupont , canada ) was used for improving the adhesion between the pe and the wood - fiber . commercial co 2 , upto 4 wt %, from matheson gas was used as the pba . all the materials were used as received . a schematic of the equipment for process b is shown in fig2 a . in the preparatory stage , un - dried wood - fiber is mixed with the polymer powder / pellets , a coupling agent , and a nucleating agent such as talc in a dry blending tumbler , and fed into the first twin - screw extruder 40 , using a feeder 22 . the temperature at the exit of this extruder was maintained at the highest processing temperature , which in this case was 180 ° c ., for completely vaporizing the moisture and other volatiles from the wood - fiber . the output of this extruder was fed into the second extruder . at the interconnection , which was open to atmosphere , generally all the vaporized volatiles were devolatilized and the moisture and generally volatile - free mixture was conveyed into the second extruder by the motion of the screw . a metered amount of co 2 was injected into the molten polymer / wood - fiber mixture at 44 in the middle of the barrel of the second extruder 42 , using a positive displacement pump 28 . the pressure in the second tandem extruder 42 and downstream was maintained high enough ( typically the pressure is above 2000 psi ) to expedite dissolution of co 2 into the plastic matrix . the temperature of the melt was then homogeneously lowered in a heat exchanger 32 . finally , it was extruded out through a die 36 where the surface temperature was further reduced to stabilize the foam . samples were taken at various nozzle temperatures for density measurement and cell morphology characterization . the foam density of hdpe / wood - fiber composites produced , using the tandem extrusion system with a devolatilizing vent at the interconnection was successfully controlled in the range of 0 . 5 to 0 . 8 g / cm 3 . the cell morphology of the foams produced was very uniform with the largest cell size being under 150 microns . the surface quality of the foams was very good too . for process c , the present invention focuses on moisture removal and utilization of a cba for fine - celled foaming of plastic / wood - fiber composite foams with a significantly improved cell structures . the basic strategy adopted is same as described for process a , with the difference that the cba is dry blended along with plastic and wood - fiber before being fed into an extruder in which the resin is plasticated and the mixture is conveyed further into the extruder where it is heated so that the cba is decomposed and releases all its gaseous contents . further processing is again similar to that described for process a . process description : in the preparatory stage , the wood - fibers are predried by using any one of the commonly used industrial methods , such as , oven drying , hot air convective drying , drying in k - mixer and the like , while maintaining the drying temperature below or slightly higher than 170 ° c . the drying temperature can be even very high up to the decomposition temperature of the cba to be used , which may cause slight degradation of the wood - fiber . however , drying over 205 ° c . should be avoided because of the severe degradation of the wood - fiber , this reduces the moisture and other volatiles , and thereby reduces the deterioration of the cell morphology of the final extrudate . then the dried wood - fiber is mixed with the polymer powder / pellets , a cba , a coupling agent , and a nucleating agent , such as talc , in a dry blending tumbler . the blended mixture is then fed into an extruder 20 through a feeder 22 . this arrangement is shown in fig3 a and is similar to those discussed above in regard to fig1 a and 2 a but there is no injection of a pba . this mixture is plasticated and further mixed in the initial sections of the screw . in the last zone 23 of the extruder the temperature is increased so as to decompose the cba . during this process some additional moisture or volatiles may be released from the wood - fiber , but this is difficult to avoid for cba processing unless the drying temperature was as high as the decomposition temperature of cba . to reduce these emissions , the residence time should be minimized . this mixture is then subjected to high shear forces by the screw and / or by any type of mixers , in the presence of high pressures ( typically the pressure is above 2000 psi ). this facilitates the dissolution or dispersion of the decomposed gases into the polymer matrix . the melt temperature of the polymer / gas solution is reduced to about 150 ° c . lower limit is determined by material and its mfi . in some cases it can go even below 140 ° c . in a heat exchanger 22 . a commonly well - known static mixer in a cooling heat exchanger shown in fig3 a can be used . for a high wood - fiber content , a cooling extruder 34 , as shown in fig3 b , can be used as a cooling device instead of a heat exchanger with static mixer . the extrudate finally passes through the die where its pressure is rapidly dropped , which produces a large number of nucleation sites due to the spinodal decomposition of polymer and gas . the gas from the adjacent polymer matrix diffuses into these sites and causes expansion . the temperature of the die can be controlled so as to freeze the surface layer of the polymer , which prevents the diffusion of gases into the atmosphere . this in turn helps in achieving expansion . [ 0093 ] fig3 c and 3 d show the other configurations possible for this process . specifically fig3 c is similar to fig3 a but shows a single screw extruder 38 rather than a twin screw extruder 20 . similarly fig3 d is similar to fig3 b and it shows a single screw extruder 38 rather than a twin screw extruder 20 . as discussed above , an efficient method , which offers many advantages , is to use cascade devolatilization and to remove moisture while the molten plastic is transferred from one extruder ( or compounder ) to the second extruder in a tandem arrangement . this may also be used in association with the cba process . process description : process d is a subset of process c in which online devolatilization is used for substantially purging out the moisture and other volatiles from the plastic / wood - fiber / additives mixture . in the preparatory stage , the un - dried wood - fiber is mixed with the polymer powder / pellets , a cba , a coupling agent , and a nucleating agent , such as talc , in a dry blending tumbler . the blended mixture is then fed into the first extruder 20 through a feeder 22 . this arrangement is similar to that shown in fig2 a but it does not include the injection of a pba . the first extruder 40 can be a single or twin - screw mixing extruder or compounder , where plastication and mixing takes place . during this process most of the moisture and other volatiles are evaporated through the hopper due to the elevated temperature . the molten mixture is then devolatilized at a vent in a cascade extrusion system and conveyed into the second extruder 42 . care should be taken that the temperature at the vent should not be high enough to decompose the cba . as noted previously , on - line devolatilization can be accomplished within the first extruder if a twin screw extruder is used as the first extruder , and devolatilizing ports can be opened along the screws . in the second extruder 42 , the temperature of the molten mixture is elevated so as to decompose the cba . during this process some additional moisture or volatiles will be released from the wood - fiber , but this is difficult to avoid . to reduce these emissions , the residence time should be minimized . this mixture is then subjected to high shear forces by the screw and / or by any type of mixers , in the presence of high pressures and temperatures . this facilitates the dissolution or dispersion of the gases evolved from the cba , into the polymer matrix . the melt temperature of the polymer / gas mixture is reduced in a heat exchanger . a commonly well - known static mixer in a cooling heat exchanger shown in fig4 a can be used . for high wood - fiber content a cooling extruder 34 , as shown in fig4 b , can be used as a cooling device instead of a heat exchanger with static mixer . the extrudate finally passes through the die where its pressure is rapidly dropped , which produces a large number of nucleation sites due to the spinodal decomposition of polymer and gas . the gas from the adjacent polymer matrix diffuses into these sites and causes expansion . the temperature of the die can be controlled so as to freeze the surface layer of the polymer , which prevents the diffusion of gases into the atmosphere . hdpe grade 58g from novacor was used as the base polymers for the composites . the wood - fibers were standard softwood ( pine ) grade 12020 , supplied by american wood fibers . the cba , hydrocerol compound ( hc ), was supplied by boehrnger ingelheim . the coupling agent used for improving the adhesion between the pe and the wood - fiber was fusabond adhesive resin e - mb - 100d from dupont , canada . all the materials were used as received . the cascade or tandem extrusion system shown in fig4 a was used in the experiments . the mixtures were dry blended and fed into the first twin - screw extruder 40 , using a feeder 22 . the temperature in this extruder was maintained at a level sufficient for vaporizing the moisture ( 145 ° c . to 170 ° c .) give a range , but not so high as to cause the decomposition of cba and the degradation of wood - fiber . the output of this extruder was fed into the second extruder 42 . at the interconnection , which was open to atmosphere , substantially all the vaporized water and other volatiles were devolatilized and the moisture and volatile - free mixture was conveyed into the second extruder 42 by the motion of the screw . the temperatures in the second tandem extruder 42 were maintained at 155 ° c . and 165 ° c . in zones 1 ( 43 ) and 2 ( 45 ), respectively . the cba was decomposed in zone 3 ( 47 ) and the released gases were dissolved in the polymer matrix under the action of high shear at elevated temperature and pressure . the temperature of the melt was then lowered ( typically to 150 ° c .) in a heat exchanger 22 . finally , it was extruded out through the die 36 where the surface temperature was further reduced ( to about 150 ° c . lower limit is determined by material and its mfi . in some cases it can go even below 140 ° c .) to increase the stabilization of the foaming process . samples were taken at various die temperatures for density measurement and cell morphology characterization . using this system , composite foams could be produced with controllable foam density varying from 0 . 5 g / cm 3 to 0 . 8 g / cm 3 . these composites also exhibited uniform cell distribution and superior surface quality as compared to those produced on a non - devolatilized system . the generation of large sized cells was successfully suppressed , and the cell population density was increased by one order of magnitude . therefore , the uniformity of cell structure was significantly improved by adopting the process described herein . the use of cba requires some special material and processing considerations . the processing temperature in the first extruder and the vent should be lower than the decomposition temperature of the blowing agent . the onset of decomposition for hc , the blowing agent used , is 160 ° c ., so the previously mentioned temperatures should not exceed this limit . this would suggest that the polyethylene materials could be effectively foamed with a hc on this system . for process e , the present invention uses the volatile emissions from the wood - fibers for generating a fine - celled foamed structure without utilizing any other blowing agent . the wood - fiber will release moisture or volatiles at high temperatures as mentioned earlier . these volatiles , in general , will affect foaming negatively , especially at a larger content . but with certain materials and under certain processing conditions , as long as the amount of volatiles is not high , these volatiles can be utilized to generate an acceptable cell structure in plastic / wood - fiber composite foams having good surface properties as well . usually , the higher the temperature , the greater the amount of moisture / volatiles released . in order to suppress the adverse effects of the excessive moisture / volatiles on the cell structure , we can lower the processing temperature is lowered to a reasonable degree and the foaming process is controlled while utilizing these emissions . process description : process e utilizes same equipment as process c in which no other blowing agent is used . the material is pre - dried by any of the conventional methods , such as oven drying , k - mixer blending or hot air - drying so that most of the moisture and other volatiles are removed either from the wood - fibers or from the plastic / wood - fiber / additives mixture . if dried wood - fibers are used , they are mixed with plastic and coupling agent and dry blended . if a k - mixer is used , the mixture is granulated in a granulator . the blended mixture is then fed into the extruder 20 through a feeder 22 if dried wood - fibers are used or directly into the hopper if k - mixer was used . the equipment used is same as in fig3 a and the processing steps are also same as in process c , except the heating temperature is not determined by the decomposition temperature of chemical blowing agent . care should be taken that the barrel temperature should not be too high to generate excessive volatiles ( below 170 ° c .). the temperature of the molten mixture is controlled so that a limited amount of moisture or volatiles can be released from the wood - fiber , which is used for foaming . consider a specific case of cascade extrusion processing at 170 ° c ., in which the residence time in the first extruder is 3 minutes and the processing time in the second extruder is 2 minutes . in addition to loosing all the moisture , the wood fibers will loose an additional 0 . 65 % weight in the first extruder . these wood fibers will loose a further 0 . 2 % weight while being processed in the second extruder , part of which will be entrapped and contribute to foaming . the amount of volatile emissions which contribute to foaming can be controlled by varying the processing temperature and the residence time in the extruder . this mixture is then subjected to high shear forces by the screw and / or by any type of mixers , in the presence of high pressures and temperatures . temperatures and pressures are measured and the temp . can be controlled by band heaters and the pressure by controlling the flow rate . this facilitates the dissolution or dispersion of the gases emitted by the wood - fiber , into the polymer matrix . the melt temperature of the polymer / gas mixture is reduced ( typically to 150 ° c .) in a heat exchanger . a commonly well - known static mixer in a cooling heat exchanger shown in fig3 a can be used . for high wood - fiber content a cooling extruder 34 , as shown in fig3 b , can be used as a cooling device instead of a heat exchanger with static mixer . the extrudate finally passes through the die where its pressure is rapidly dropped , ( more than 1000 psi across the die ) which produces a large number of nucleation sites due to the spinodal decomposition of polymer and volatiles . the volatiles from the adjacent polymer matrix diffuses into these sites and causes expansion . the temperature of the die can be controlled so as to freeze the surface layer of the polymer and / or to decrease the diffusivity of volatiles , which prevents the diffusion of gases into the atmosphere . for process f , the present invention envisages the use of the volatile emissions from the wood - fibers for generating a fine - celled foamed structure without utilizing any other blowing agent . the concept of using these emissions from the wood - fiber is same as described for process e , the only difference being that the excessive moisture and volatiles are removed through a vent in a tandem system . process description : process f utilizes same equipment as of process d while no other blowing agent is used . online devolatilization is used for purging out most of the moisture and other volatiles from the plastic / wood - fiber / additives mixture . in the preparatory stage , the un - dried wood - fiber is mixed with the polymer powder / pellets and a coupling agent , in a dry blending tumbler . the blended mixture is then fed into the first extruder 20 through a feeder 22 . the equipment used is same as in fig4 a and the processing steps are also same as in process d . the first extruder 40 can be a single or twin - screw mixing extruder or compounder , where plastication and mixing takes place . during this process , most of the moisture and other volatiles are evaporated through the hopper due to the elevated temperature . the molten mixture is then devolatilized at a vent in a cascade extrusion system and conveyed into the second extruder 42 . care should be taken that the temperature at the vent should not be high enough to degrade the wood - fibers . on - line devolatilization can be accomplished within the first extruder if a twin screw extruder is used as the first extruder , and devolatilizing ports can be opened alone the screws . in the second extruder 42 , the temperature of the molten mixture is controlled so that a limited amount of moisture or volatiles can be released from the wood - fiber , which is used for foaming . this mixture is then subjected to high shear forces by the screw and / or by any type of mixers , in the presence of high pressures and temperatures . this facilitates the dissolution or dispersion of the gases emitted by the wood - fiber , into the polymer matrix . the melt temperature of the polymer / gas mixture is reduced in a heat exchanger . a commonly well - known static mixer in a cooling heat exchanger shown in fig4 a can be used . for high wood - fiber content , a cooling extruder 34 , as shown in fig4 b , can be used as a cooling device instead of a heat exchanger with static mixer . the extrudate finally passes through the die where its pressure is rapidly dropped , which produces a large number of nucleation sites due to the spinodal decomposition of polymer and volatiles . the volatiles from the adjacent polymer matrix diffuse into these sites and causes expansion . the temperature of the die can be controlled so as to freeze the surface layer of the polymer and / or to decrease the diffusivity of volatiles , which prevents the diffusion qf gases into the atmosphere . hdpe grade 2710 from novacor was used as the base polymers for the composites . the wood - fibers were standard softwood ( pine ) grade 12020 , supplied by american wood fibers . the coupling agent used for improving the adhesion between the pe and the wood - fiber was fusabond adhesive resin e - mb - 100d from dupont , canada . all the materials were used as received . the tandem extrusion system shown in fig4 a was used in the experiments . the mixtures were dry blended and fed into the first twin - screw extruder 40 , using a feeder 22 . the temperature in this extruder was maintained at a level sufficient for adequate processing of material , but not so high as to cause the degradation of wood - fiber ( from 145 ° c . to 170 ° c .). the output of this extruder was fed into the second extruder , at the interconnection , which was open to atmosphere , all the vaporized water and other volatiles were devolatilized and the moisture and volatile free mixture was conveyed into the second extruder by the motion of the screw . the temperatures ( from 145 ° c . to 160 ° c .) in the second tandem extruder were maintained at low levels in zones 1 and 2 . additional gases were evolved from wood - fiber by elevating the mixture temperature in zone 3 and the released gases were dissolved in the polymer matrix under the action of high shear at elevated temperature and pressure . typically the pressure was between 2000 - 3000 psi . a range of temperatures were tested and it was determined that temperatures between 150 ° c . and 185 ° c . worked . however , the barrel temperature should be typically below 170 ° c . the temperature of the melt was then lowered in a heat exchanger 22 ( to about 150 ° c .). finally , it was extruded out through the die 36 where the surface temperature was further reduced to increase the stabilization of the foaming process . two sets of procedures were adopted to produce hdpe / wood - fiber composite foams . in the first set of experiments , the devolatilizing vent temperature was set at three different values , and the highest barrel temperature was varied at 5 ° c . intervals for each vent temperature . in the second set of experiments , the devolatilizing vent temperature was kept constant , but the highest barrel temperature was set at three different values , and the die temperature was varied at 5 ° c . intervals for each barrel temperature . a set of experiments of hdpe mixed with undried wood - fiber and 3 % coupling agent , without a blowing agent were carried out to identify the relationship between processing temperatures and the cell structure , while fixing the drying ( i . e ., devolatilizing ) conditions . this was done to find the lowest processing temperature at which the moisture / volatiles generation from wood - fiber is minimized and the small amount generated could be utilized for foaming . in this set of experiments , three different devolatilizing temperatures at the vent were used and for each of these , the barrel temperature in the second extruder was varied to identify its effect on the cell structure . the die temperature was maintained to be 140 ° c . [ 0129 ] fig5 shows that the foam density of wood - fiber composites was decreased as the barrel temperature in the second extruder increased . at a higher barrel temperature , the wood - fiber released more moisture / volatiles out , and therefore , the foaming effects of these volatiles were increased and the foam density was reduced . for the barrel temperature range of 145 ° c .- 170 ° c ., the foam density was around 1 . 1 g / cm 3 . above 170 ° c ., the foam density decreases quickly to 0 . 85 g / cm 3 . this implies that a lot of moisture / volatiles were released from wood - fiber above 170 ° c . and resulted in significant foaming . fig6 shows some typical cell morphologies of the wood - fiber / hdpe composite foam samples blown without any blowing agents . at the same devolatilizing temperature of 160 ° c ., when the barrel temperature increased from 145 ° c ., 165 ° c ., to 175 ° c ., it is observed that foaming occurred due to the volatiles / moisture generated from the wood - fiber , and the corresponding foam density was 1 . 1 g / cm 3 , 1 . 0 g / cm 3 , and 0 . 87 g / cm 3 , respectively . at the barrel temperature 145 ° c ., there was almost no foaming in the composite . as the barrel temperature was increased to 165 ° c ., some small sized bubbles and voids appeared . when the barrel temperature was further increased to 175 ° c ., it is obvious that more volatiles were released from wood - fiber resulting in significant foaming with an irregular cellular structure . this implies that when the amount of generated moisture and volatiles is significant , due to the high processing temperature , the formation of big voids is difficult to avoid . therefore , to minimize the effects of moisture / volatiles on foaming , the maximum processing temperature in the second extruder should be low , preferably below 170 ° c . [ 0130 ] fig5 also shows that the foam density of composites generally increased as the devolatilizing temperature t v was increased . this implies the devolatilizing vent is effective in removing moisture / volatiles from wood - fiber . another interesting observation from this figure is that the foam density decreased slightly as the second barrel temperature t b increased while t b & lt ; t v . when t b & gt ; t v , the foam density decreased sharply when the barrel temperature was increased . this shows wood - fiber will further release moisture / volatiles even after the devolatilization at the vent , because of the higher processing temperature than the drying ( i . e ., devolatilization ) temperature . therefore , it is essential to set the barrel temperature lower than the devolatilizing temperature , to minimize the gaseous emissions additionally generated during processing , and thereby , to produce a fine celled structure . this inference is also equally applicable to the pre - drying case of process a and process c . another set of experiments of hdpe mixed with un - dried wood - fiber and 3 % coupling agent , without a blowing agent were carried out to identify the relationship between die temperatures and the foam density at three different barrel temperature , while fixing the drying ( i . e ., devolatilizing ) condition at 170 ° c . this was done to find the lowest density achievable when the moisture / volatiles generation from wood - fiber is utilized for foaming , while the amount of moisture and volatile is minimal to produce a fine - celled structure , by maintaining the second extruder barrel temperature below 170 ° c . experiment was also conducted at high second extruder barrel temperature above 170 ° c . for comparison puspose . [ 0133 ] fig7 shows that the foam density of wood - fiber composites was decreased significantly as the die temperature decreased , when the barrel temperature was 175 ° c . however , because of too high a barrel temperature , the wood - fiber released too much moisture / volatiles , and as a result , irregular - shaped , big - sized cells were observed and the foam structure was very non - uniform . for the barrel temperature of 160 ° c ., the foam density could be lowered below 0 . 75 g / cm 3 , by decreasing the die temperature below 140 ° c . the foam structure was very fine because of the small amount of volatiles generated at this low barrel temperature . for a barrel temperature of 145 ° c ., no foaming could be obtained . in fact the final density was always more than the density of the individual components indicating that the high extrusion pressures compacted the composite . this also indicates that lower processing temperature suppresses the volatile emission from the wood - fiber which has been dried ( ie ., devolatilized ) at a higher temperature . 1 . balatinecz , j . j ., and woodhams , r . t ., “ wood - plastic composites : doing more with less ,” j . forestry . 91 , 22 ( 1993 ). 2 . chtourou , h ., riedl , b ., and ait - kadi , a ., “ reinforcement of recycled polyolefins with wood - fibers ,” j . of reinforced plastics and composites . 11 , 372 ( 1992 ). 3 . raj , r . g ., kokta , b . v ., groleau , g . & amp ; daneault , c ., “ use of wood fiber as a filler in polyethylene : studies on mechanical properties ”, plastics and rubber processing and applications , 11 , 215 ( 1989 ). 4 . youngquist , j . a ., and rowell , r . m ., in proceedings , 23rd international particleboard / composite materials symposium . t . m . maloney , ed ., was . state univ ., pullman , p . 141 ( 1990 ). 5 . matuana , l . m ., balatinecz , j . j ., and park , c . b ., polym . eng . sc ., 38 , 765 ( 1998 ). 6 . rauwendaal , c ., polymer extrusion , 3rd ed ., hanser publishers ( 1994 ). 7 . brooke , j . g ., goforth , b . d ., goforth , c . l ., u . s . pat . no . 5 , 082 , 605 , 1992 . 8 . goforth , b . d ., goforth , c . l ., brooke , j . g ., u . s . pat . no . 5 , 096 , 046 , 1992 . 10 . turk , d . l ., grill , o ., u . s . pat . no . 5 , 858 , 522 , 1999 . 11 . deaner , m . j ., puppin , g ., heikkila ., u . s . pat . no . 5 , 827 , 607 , 1998 . 12 . deaner , m . j ., puppin , g ., heikkila ., u . s . pat . no . 5 , 539 , 027 , 1996 . 13 . deaner , m . j ., puppin , g ., heikkila ., u . s . pat . no . 5 , 486 , 553 , 1996 . 14 . deaner , m . j ., puppin , g ., heikkila ., u . s . pat . no . 5 , 932 , 334 , 1999 . 15 . pelikan , h . d ., titz , s ., u . s . pat . no . 4 , 104 , 207 , 1978 . 19 . bejan , a ., “ advanced engineering thermodynamics ”, john wiley & amp ; sons , n . y . 1997 . 20 . m . lee , c . tzoganakis , and c . b . park , “ extrusion of polymer blend with supercritical co 2 ”, advances in polymer technology , august 1999 . 21 . a . a . marra , technology of wood bonding : principles in practice , van nostrand reihold , n . y . 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