referring now to fig1 a suitable method to produce a lyocell dissolving pulp from low specific gravity wood is illustrated . the method may be considered to include two broad processing areas , pulping depicted as block 126 and bleaching depicted as block 128 . in block 100 , low specific gravity wood chips are loaded or fed into a digester . specific gravity , according to the handbook of pulping and papermaking , 2 d ed ., by christopher j . biermann , is the ( unit less ) ratio of the solid wood density to the density of water at the same temperature . as used herein , specific gravity is the average specific gravity of any population of wood feedstock material . the solid wood density may be determined using the green volume , the oven - dry volume , or intermediate volumes . the wood chips used in practicing the invention can be made from any cellulose source . contrary to conventional thinking , low specific gravity wood has been found to be suitable for use as a source of cellulose for making lyocell - molded bodies . a suitable range of low specific gravity wood used for the present invention is any wood material having a specific gravity about equal or less than 0 . 41 . low specific gravity wood results in a lower brownstock pulp viscosity , which is believed to reduce the use of bleaching chemicals in the bleach plant . representative sources of low specific gravity wood may be derived from “ thinnings ” and “ juvenile ” wood . juvenile wood is defined as the first 10 growth rings surrounding the pith , according to biermann . however , others define it as wood formed near the pith of the tree , often characterized by wide growth rings , lower density , and shorter fibers . however , in some instances the juvenile wood may extend to the 15 - ring or more . specific gravity increases with the increasing height of the tree , so specific gravity at 16 feet , 32 feet , or 48 feet is incrementally greater than at the butt of the tree . in some embodiments , the specific gravity will be less than 0 . 41 , and could be less than 0 . 38 , 0 . 36 , 0 . 34 , 0 . 32 , or 0 . 30 , or less . digesters for use in the present invention can include any digester suitable to pulp low specific gravity wood . one example of a suitable digester is a continuous digester that is often referred to as a “ kamyr ” digester . ( it should be noted that kamyr is the name of a company that designed and built such digesters and as such , the term kamyr is loosely associated with a continuous digester . kamyr no longer exists as a company . such continuous digesters are supplied by kvaerner .) these digesters have been used in the pulp and paper industry for several years with the first one being installed in sweden in 1950 . over the years , the modifications have been made to these digesters to improve their operation . the digester system may be either a single vessel or a two - vessel system . “ kamyr ” digesters are typically used in kraft or alkaline wood pulping , but may also be used in semi - chemical pulping methods . other continuous digesters , such as the m & amp ; d digester and the pandia digester , are also suitable to use in the present invention . however , the present invention can also be practiced using any batch or other continuous digester . referring to fig1 within the pulping process , block 126 , there are several operations , depicted as blocks 100 - 116 . loading , or feeding chips as discussed above , occurs in block 100 . the wood chips may be presteamed prior to cooking , block 102 . steam at atmospheric pressure preheats the chips and drives off air so that liquor penetration will be enhanced . after the pre - steaming operation is completed , cooking liquor , referred to as white liquor , containing the pulping chemicals may be added to the chips , block 104 . the white liquor and chips are then fed into the digester . in kraft pulping , the active chemical compounds are naoh and na 2 s . other chemicals may be added to influence or impart desirable effects on the pulping process . these additional chemicals are well known to those of skill in the art . the present invention provides a lower brownstock pulp viscosity from relatively lower specific gravity wood as composed with wood having a higher specific gravity , i . e ., specific gravity is related to kappa number . impregnation , block 106 , is the period during which the chemicals are allowed to impregnate the low specific gravity wood material . good liquor penetration helps assure a uniform cooking of the chips . “ cooking ” occurs in blocks 108 and 110 . the co - current liquid contact operation , block 108 , is followed by the counter - current liquid contact operation , block 110 . cooking of the low specific gravity wood occurs during these two operations . in either block 108 or 110 , the cooking liquor and chips can be brought to temperature . digester washing , block 112 , is accomplished by introducing wash liquor into the bottom of the digester and having it flow counter - current to the cooked pulp . cooking for the most part ends when the pulp encounters the cooler wash liquor . upon completion of the cook operation , and digester washing , the digester contents are blown , block 112 . digester blowing involves releasing the wood chips and liquor at atmospheric pressure . the release occurs with a sufficient amount of force to cause fiber separation . if desired , the blow tank may be equipped with heat recovery equipment to reduce operating expenses . in block 114 , the pulp is sent from the blow tank to external brownstock pulp washers . the separation of black liquor from the pulp occurs at the brownstock washers . in one embodiment of a method of making a pulp from low specific gravity wood to be used in the manufacture of lyocell - molded bodies , the time allowed for impregnation in block 106 is about 35 minutes . the initial percent effective alkali is about 8 . 5 . the percent effective alkali at 5 minutes is about 1 . 6 . the percent sulfidity is about 29 . the liquor ratio is about 4 . the initial temperature is about 110 ° c . the residual grams per liter of effective alkali is about 9 . 63 . the residual percent effective alkali is about 3 . 85 . the ph is about 12 . 77 , and the h factor is about 2 . in one embodiment of the co - current operation , block 108 , the percent effective alkali is about 4 . 2 . according to biermann , the effective alkali is the ingredients that will actually produce alkali under pulping conditions . the percent sulfidity is about 29 . according to biermann , the sulfidity is the ratio of sodium sulfide to the active alkali , expressed as a percent . the liquor addition time is about 1 minute . the temperatures may be ramped to the final cooking temperature with a hold at one or more temperatures . the first temperature platform is about 154 ° c . the time to reach the temperature is about 9 minutes and the time at the temperature is about 5 minutes . a second and higher cooking temperature at the co - current operation is provided at 170 ° c . the time to reach the second temperature is about 51 minutes and the time at temperature is about 3 minutes . the effective alkali remaining after a cook operation is called the residual alkali . the residual grams per liter of effective alkali is about 9 . 42 , following the co - current operation . the residual percent effective alkali is about 3 . 77 . the ph is about 12 . 92 , and the h factor is about 649 . in one embodiment of the counter - current operation , block 110 , the percent effective alkali is about 8 . the percent sulfidity is about 29 . 2 . capability also exists for ramping to two different temperatures in the counter - current step . however , in one embodiment , the first and second cooking temperatures are both about 171 ° c . the time to reach temperature is about 54 minutes and the time at the temperature is about 162 minutes . the effective alkali grams per liter is about 16 . 0 . the displacement rate is about 93 ml per minute . the displacement volume is about 20 liters . the volumes given here are relatively small , since the method was tested on a lab - scale bench reactor . however , with the parameters provided herein , and with no undue experimentation , the process can be scaled to any rate . the residual grams per liter of effective alkali is about 9 . 95 . the residual percent effective alkali is about 3 . 98 . the ph is about 12 . 74 and the h factor is about 3877 . in one embodiment , the total time is about 319 minutes and the percent effective alkali for the total cook is about 22 . 3 . in one embodiment , after washing , the viscosity of the brownstock pulp is about 153 cp . the total yield on oven dried wood is about 41 . 04 . following the pulping process , generally depicted as reference numeral 126 in fig1 the brownstock pulp made from low specific gravity wood is bleached to reduce its viscosity . the bleaching process does not lead to a substantial reduction of the hemicellulose content of the pulp . the method according to the invention produces a bleached dissolving pulp that is suitable for lyocell - molded body production . bleaching of chemical pulps involves the removal of lignin with an attendant decrease in the pulp fiber length and viscosity . however , the bleaching process does not cause a substantial reduction to the hemicellulose content of the pulp . bleaching brownstock pulp made from low specific gravity wood may require fewer chemicals than the conventional highly refined , high - alpha pulps presently being used for lyocell . in one embodiment , the low specific gravity brownstock pulp made according to the invention can be treated with various chemicals at different stages in the bleach plant . the stages are carried out in vessels or towers of conventional design . one representative bleaching sequence is ode p d . the operations occurring in the bleaching plant are represented collectively by reference numeral 128 in fig1 . other embodiments of post bleaching the pulp after pulping are described in u . s . pat . no . 6 , 331 , 354 , and u . s . application ser . no . 09 / 842 , 274 , incorporated herein by reference in their entirety . the first stage of bleaching is an o stage , block 116 . the o stage comprises bleaching with oxygen . however , according to biermann , some consider oxygen bleaching to be an extension of the pulping process . oxygen bleaching is the delignification of pulps using oxygen under pressure . the oxygen is considered to be less specific for the removal of lignin than the chlorine compounds . oxygen bleaching takes place in an oxygen reactor . suitable oxygen reactors capable of carrying out the method of the present invention are described in u . s . pat . nos . 4 , 295 , 925 ; 4 , 295 , 926 ; 4 , 298 , 426 ; and 4 , 295 , 927 , fully incorporated herein by reference in their entirety . the reactor can operate at a high consistency , wherein the consistency of the feedstream to the reactor is greater than 20 % or it can operate at medium consistency , where the medium consistency ranges between 8 % up to 20 %. preferably , if a high consistency oxygen reactor is used , the oxygen pressure can reach the maximum pressure rating for the reactor , but more preferably is greater than 0 to about 85 psig . in medium consistency reactors , the oxygen can be present in an amount ranging from greater than 0 to about 100 pounds per ton of the pulp , but is more preferably about 50 to about 80 pounds per ton of pulp . the temperature of the o stage ranges from about 100 ° c . to about 140 ° c . in one embodiment of the method to make a pulp suitable to be used in making lyocell - molded bodies , a d stage , block 118 follows the o stage , block 116 . the d stage comprises bleaching the pulp coming from the oxygen reactor with chlorine dioxide . chlorine dioxide is more selective than oxygen for removing lignin . the amount of chlorine dioxide used in this stage ranges from about 20 to about 30 lb / ton , which may be lower than a conventional bleach plant that processes pulp from wood chips with a specific gravity not within the low specific gravity range of this invention . the temperature of the d stage ranges from about 50 ° c . to about 85 ° c . in one embodiment of the method to make a pulp suitable to be used in making lyocell - molded bodies , an e p stage , block 120 , follows the d stage , block 118 . the e p stage is the hydrogen peroxide reinforced extraction stage where lignin is removed from the pulp using caustic in an amount ranging from about 20 to about 50 lb / ton . the amount of hydrogen peroxide ranges from about 20 to about 60 lb / ton , which may be lower than a conventional bleach plant that processes pulp from wood chips having a specific gravity not considered within the low specific gravity range of this invention . the temperature of the ep stage ranges from about 75 to about 95 ° c . in one embodiment , a second d stage , block 122 , follows the e p stage , block 120 . the amount of chlorine dioxide used in this stage ranges from 10 to about 30 lb / ton , which may be lower than a conventional bleach plant that processes pulp from wood chips having a conventional specific gravity not considered to be within the low specific gravity range of this invention . the temperature of the d stage ranges from about 60 ° c . to about 90 ° c . one embodiment of a pulp made from low specific gravity wood has a hemicellulose content of at least 7 % hemicellulose , a pulp viscosity less than 32 cp , a copper number less than 2 . 0 , and in some instances less than 1 . 3 ( tappi t430 ), a weighted average fiber length less than 2 . 7 mm , and a coarseness less than 23 mg / 100 m . other embodiments of pulps made according to the present invention have a combined copper , manganese , and iron content less than 2 ppm , a total metal load less than 300 ppm , and a silicon content less than 50 ppm . lyocell molded bodies made from the pulps of the invention will have a correspondingly high hemicellulose content of at least 7 % by weight , and cellulose . hemicellulose is measured by a sugar content assay based on tappi standard t249 hm - 85 . methods for measuring pulp viscosity are well known in the art , such as tappi t230 . copper number is a measure of the carboxyl content of pulp . the copper number is an empirical test used to measure the reducing value of cellulose . the copper number is expressed in terms of the number of milligrams of metallic copper , which is reduced from cupric hydroxide to cuprous oxide in an alkaline medium by a specified weight of cellulosic material . the degree to which the copper number changes during the bleaching operation is determined by comparing the copper number of the brownstock pulp entering the bleaching plant and the copper number of the bleached pulp after the bleaching plant . a low copper number is desirable because it is generally believed that a high copper number causes cellulose and solvent degradation during and after dissolution of the bleached pulp to form a dope . the weighted average fiber length ( wafl ) is suitably measured by a fqa machine , model no . lda93 - r9704 , with software version 2 . 0 , made by the optest company of hawkesbury , ontario , canada . transition metals are undesirable in pulp because they accelerate the degradation of cellulose and nmmo in the lyocell process . examples of transition metals commonly found in bleached pulps include iron , copper , and manganese . preferably , the combined metal content of these three metals in the pulps of the invention is less than about 20 ppm by weyerhaeuser test no . am5 - pulp - 1 / 6010 . additionally , pulps of the invention have a total metal load of less than 300 ppm by weyerhaeuser test no . am5 - pulp - 1 / 6010 . the total metal load refers to the combined amount , expressed in units of parts per million ( ppm ), of nickel , chromium , manganese , iron and copper . once the pulp has been bleached to reduce its viscosity without substantially increasing its copper number or decreasing the hemicellulose content , the pulp can either be washed in water and transferred to a bath of organic solvent , such as n - methyl - morpholine - n - oxide ( nmmo ), for dissolution prior to lyocell - molded body formation . alternatively , the bleached washed pulp can be dried and broken into fragments for storage and / or shipping in a roll , sheet or bale , for example . in order to make lyocell products from the low specific gravity wood pulps , the pulp is first dissolved in an amine oxide , preferably a tertiary amine oxide . representative examples of amine oxide solvents useful in the practice of the present invention are set forth in u . s . pat . no . 5 , 409 , 532 , incorporated herein by reference in its entirety . the preferred amine oxide solvent is nmmo . other representative examples of solvents useful in the practice of the present invention include dimethylsulfoxide ( d . m . s . o . ), dimethylacetamide ( d . m . a . c . ), dimethylformamide ( d . m . f .) and caprolactan derivatives . the bleached pulp is dissolved in amine oxide solvent by any known means such as ones set forth in u . s . pat . nos . 5 , 534 , 113 ; 5 , 330 , 567 ; and 4 , 246 , 221 , incorporated herein by reference in their entirety . the pulp solution is called dope . the dope is used to manufacture lyocell fibers , films , and nonwovens or other products , by a variety of techniques , including melt blowing , spun - bonding , centrifugal spinning , dry - jet wet , or any other suitable method . examples of some of these techniques are described in u . s . pat . nos . 6 , 235 , 392 ; 6 , 306 , 334 ; 6 , 210 , 802 ; and 6 , 331 , 354 , incorporated herein by reference in their entirety . examples of techniques for making films are set forth in u . s . pat . nos . 5 , 401 , 447 ; and 5 , 277 , 857 , incorporated herein by reference in their entirety . meltblowing , centrifugal spinning and spunbonding used to make lyocell fibers and nonwoven webs are described in u . s . pat . nos . 6 , 235 , 392 and 6 , 306 , 334 , incorporated herein by reference in their entirety . dry - jet wet techniques are more fully described in u . s . pat . nos . 6 , 235 , 392 ; 6 , 306 , 334 ; 6 , 210 , 802 ; 6 , 331 , 354 ; and 4 , 142 , 913 ; 4 , 144 , 080 ; 4 , 211 , 574 ; 4 , 246 , 221 ; incorporated herein by reference in their entirety . one embodiment of a method for making lyocell products , including fibers , films , and nonwoven webs from dope derived from pulp is provided , wherein the pulp is made from low specific gravity wood , the pulp having at least 7 % hemicellulose , a viscosity less than or about 32 cp , a copper number less than or about 2 , a weighted average fiber length less than or about 2 . 7 mm , and a coarseness less than or about 23 mg / 100 m . the method involves extruding the dope through a die to form a plurality of filaments , washing the filaments to remove the solvent , regenerating the filaments with a nonsolvent , including water or alcohol , and drying the filaments . fig2 shows a block diagram of one embodiment of a method for forming lyocell fibers from the pulps made from low specific gravity wood according to the present invention . starting with low specific gravity wood pulp in block 200 , the pulp is physically broken down , for example by a shredder in block 202 . the pulp is dissolved with an amine oxide - water mixture to form a dope , block 204 . the pulp can be wetted with a nonsolvent mixture of about 40 % nmmo and 60 % water . the mixture can be mixed in a double arm sigma blade mixer and sufficient water distilled off to leave about 12 - 14 % based on nmmo so that a cellulose solution is formed , block 208 . alternatively , nmmo of appropriate water content may be used initially to eliminate the need for the vacuum distillation block 208 . this is a convenient way to prepare spinning dopes in the laboratory where commercially available nmmo of about 40 - 60 % concentration can be mixed with laboratory reagent nmmo having only about 3 % water to produce a cellulose solvent having 7 - 15 % water . moisture normally present in the pulp should be accounted for in adjusting the water present in the solvent . reference is made to articles by chanzy , h ., and a . peguy , journal of polymer science , polymer physics ed . 18 : 1137 - 1144 ( 1980 ), and navard , p ., and j . m . haudin , british polymer journal , p . 174 ( december 1980 ) for laboratory preparation of cellulose dopes in nmmo and water solvents . the dissolved , bleached pulp ( now called the dope ) is forced through extrusion orifices in a process called spinning , block 210 , to produce cellulose filaments that are then regenerated with a non - solvent , block 202 . spinning to form lyocell - molded bodies , including fibers , films , and nonwovens , may involve meltblowing , centrifugal spinning , spun bonding , and dry - jet wet techniques . finally , the lyocell filaments or fibers are washed , block 214 . the solvent can either be disposed of or reused . due to its high costs , it is generally undesirable to dispose of the solvent . regeneration of the solvent suffers from the drawback that the regeneration process involves dangerous , potentially explosive conditions . the following examples merely illustrate the best mode now contemplated for practicing the invention , but should not be construed to limit the invention . a commercial continuous extended delignification process was simulated in the laboratory utilizing a specially built reactor vessel with associated auxiliary equipment , including circulating pumps , accumulators , and direct heat exchangers , etc . reactor temperatures were controlled by indirect heating and continuous circulation of cooking liquor . the reactor vessel was charged with a standard quantity of equivalent moisture free wood . an optional atmospheric pre - steaming step may be carried out prior to cooking . a quantity of cooking liquor , ranging from about 50 % to 80 % of the total , was then charged to the digester along with dilution water to achieve the target liquor to wood ratio . the reactor was then brought to impregnation temperature and pressure and allowed to remain for the target time . following the impregnation period , an additional portion of the total cooking liquor was added to the reactor vessel , ranging from about 5 % to 15 % of the total . the reactor was then brought to cooking temperature and allowed to remain there for the target time period to simulate the co - current portion of the cook . following the co - current portion of the cook , the remainder of the cooking liquor was added to the reactor vessel at a fixed rate . the rate is dependent on the target time period and proportion of cooking liquor used for this step of the cook . the reactor was controlled at a target cooking temperature and allowed to remain there during the simulation of the counter - current portion of the cook . spent cooking liquor was withdrawn from the reactor into an external collection container at the same fixed rate . at the end of the cook , the reactor vessel was slowly depressurized and allowed to cool below the flash point . the reactor vessel was opened and the cooked wood chips were collected , drained of liquor , washed , screened and made ready for testing . three cooks of low specific gravity wood chips were prepared , along with three cooks of non - low specific gravity wood . one cook for low specific gravity wood chips had the following parameters . inwoods low specific gravity wood chips were pulped into an alkaline kraft pulp with a kappa number of 16 . 8 ( tappi standard t236 cm - 85 and a viscosity of 239 cp ( tappi t230 ). the brownstock pulp was treated with oxygen in a pressure vessel with high consistency mixing capabilities . the vessel was preheated to about 120 ° c . an amount of sodium hydroxide ( naoh ) equivalent to 100 pounds per ton of pulp was added to the alkaline pulp . the reaction vessel was then closed and the pressure was increased to 60 psig by introducing oxygen into the pressure vessel . water was present in the vessel in an amount sufficient to provide a 10 % consistency . after 45 minutes , the stirring was stopped and the pulp was removed from the pressure vessel and washed . the resulting washed pulp viscosity was 35 . 3 cp , and had a kappa number of 3 . 8 . the d stage treated the pulp processed in the o stage by washing it three times with distilled water , pin fluffing the pulp , and then transferring the pulp to a polypropylene bag . the consistency of the pulp in the polypropylene bag was adjusted to 10 % with the addition of water . chlorine dioxide corresponding to an amount equivalent to 28 . 4 pounds per ton of pulp was introduced to the diluted pulp by dissolving the chlorine dioxide in the water used to adjust the consistency of the pulp in the bag . the bag was sealed and mixed and then held at 75 ° c . for 30 minutes in a water bath . the pulp was removed and washed with deionized water . the washed pulp from the d stage was then placed in a fresh polypropylene bag and caustic was introduced with one - half of the amount of water necessary to provide a consistency of 10 %. hydrogen peroxide was mixed with the other one - half of the dilution water and added to the bag . the hydrogen peroxide charge was equivalent to 40 pounds per ton of pulp . the bag was sealed and mixed and held for 55 minutes at 88 ° c . in a water bath . after removing the pulp from the bag and washing it with water , the mat was filtered and then placed back into the polypropylene bag and broken up by hand . chlorine dioxide was introduced a second time to the pulp in an amount equivalent to 19 pounds per ton of pulp with the dilution water necessary to provide a consistency of 10 %. the bag was sealed and mixed , and then held for 3 hours at 88 ° c . in a water bath . the treated pulp had a copper number of about 0 . 9 measured by tappi standard t430 and had a hemicellulose ( xylan and mannan ) content of 12 . 7 %. low specific gravity wood having a specific gravity of 0 . 410 was pulped using the kraft process , and subsequently , bleached and treated with varying amounts of oxygen to reduce its viscosity . components in the pulps made using inwoods low specific gravity wood chips are 7 . 2 % xylans and 5 . 5 % mannans . table 2 shows the results for three different cooking conditions . while brownstock pulp wafl is provided , it is apparent that bleaching the brownstock pulp to reduce its viscosity without substantially reducing the hemicellulose content , in accordance with the conditions of the present invention , will not result in any appreciable increase in the bleached pulp wafl and may in fact be lower than the brownstock pulp wafl . a conventional tolleson wood chip made from wood having specific gravity of 0 . 495 was pulped using a kraft process and subsequently treated with varying amounts of oxygen to reduce its viscosity . table 3 shows the pulping conditions for one cook of tolleson wood chips . table 4 shows the results of three different cooks using a conventional tolleson wood chip made from a non - low specific gravity wood . components in the pulps made using tolleson non - low specific gravity wood chips are 6 . 5 % xylose ; 6 . 6 % mannose ; 5 . 7 % xylans ; and 5 . 9 % mannans . it can be seen that the viscosity of the pulps made from the inwoods low specific gravity wood chips is lower than the viscosity of the pulps made from the tolleson non - low specific gravity wood chips . it can be seen that the viscosity of the pulps made from the inwoods low specific gravity wood chips is lower than the viscosity of the pulps made from the tolleson non - low specific gravity wood chips . while the preferred embodiment of the invention has been illustrated and described , it will be appreciated that various changes can be made therein without departing from the spirit and scope of the invention .