REFERENCE TO GOVER MEN RIGHTS jlHMli J Ilk liveMsofi was trade with gpvettrTO sup r tinder SAO960I 60 awarded by the . partmeixt of irietgy, The-gowmment has cer n. ri ts k the iaveati

f§TO2| Biomass. is a source for rene able li id fuel prodrscrioiL lmdet§a ^: mg a series of theoMochemical eaction, called last pyrolysis, bferrass can be decomposed. iote» a vapor- phase ^■ mi ture df. small r«oieetsk§ of comr^ynds and a catfKMMricli mM im

(teowa as o~eIiar) en it is heated in. m oxygtfi-S'e envimnkent Se^tmdally, the mpet mixture & be ^pa i fromth© hk-ehar using cyejg&as td½f Ulim _* After separation;, the vapor or ure ca« be eoedeased itm a liquid-phase roduct {called btooit mm% condensers at tettt emwms bete 0 *€ _> lea in »0» o«.4e«sa 1 gaseows fraction (also called sysips) separated from bio-os! aadfek-char.

fKMIIJ Bioniass fast pyro!ysis is a very praaisiRg technology for prod¾te½.g renewable liquid t ek because bio-βϋ ears, be easily trarssperael: aaJ stored, burned diectl k ther l power station for steam, prodaedon driv gas t ^y rtkiesy m*& -u gra ed <¾?· injected iato a eon etjtfeiml pe«-ole«ra refinery to htak ti¾»spota _. to liquid fuels ipsoltee, d se mtVm jet ik;!) or Yalae-added ehemicaJs, Moreo e, the byproducts, syngas ao bio-chat; c n be ed as hloiueis or to produce value-added ctatels,

f W \ Tie pwpetlfe an yield p orti of fmt pr y products (hio~olL bio-char, and synjps) de end the feedstock species used _* reactor type, and operating c-onditiom Reacio» tetwpeaare tad pessure, mtm$ .rate, tmlfece time, ami the efficieaefes oirriass and energy transfer are critical o erati g parameters for a b raass last pyrolysis process, and ^" are a iec ted by t e struckra! desiga an pp ratbss. of a pyrolysis reactfjr, A oomher of

-ml k reactor desi js are available. However:, devetepkg-.ati efficient reactor with low m for prodydag high quality hi®-©!, h chalferigkg.. for exam le, both ktb kg arid circrilatiug fhd taf-hed reactors can handle high htoraass tbroiighptsts and trio-oil yields, however, the quality ©fhle-oil produced, s low and the eac r operation is complicated doe o the need ipr a large volum tric flow f high pepae carder gas, suc as kttogsra, that mmt e ated a«d compressed. Asatlw type of pyrolysis reactor, aa Aoger reactor, eaa eiirsikiate t e seed tot a canier as, ;bm the yield of bk si! tow a« the teactor scale ^ MiBtad by low heat transfer eiBe!encks.:

SUMMARY fittiSJ Reactors for the pyrolysis of pyro1y¾ih¼ matter, pyrolysis systems ^' hscorporatmg the reactors md methods -Of using fee reactors are provided. Also provided re s sems and metho s far IrrtsgrM g the pyrotysis and h ikotleoxygciMi!osi of pyroiy¾bie watter,

| §tM*€f One em odiment of a reactor for the pyrolysis. of pyroIy:a te matter comprises: a hodiiatai rotat b!e reactor drum ^' comprising a imtar wall disposed around a

axis, herein die «mh wail. Is permeable pamcidate material; ^■ .rotation drive e rieeed to the rotttahle t crnt drum and eoai¾pred to rotate the tptatahfc reaetor drum abott the ho«¾o»tai axis; a feed conduit eoailgusred to transport pyr«!y¾a ie totter from a source of pyroly^abk matter Into oMta k reactor dram and a .re ction elMurhet m which: the rotatahk reactor dwm a»d at least a portion of the feed e nddt are housed,

f ^§ # ^§ 7J fee emhodimsat of a system tor the pyrolysis- of pyroly¾abk matter comprises: the reactor described above; so ree of py:roiy¾a ie matter, whereat the soaree comprises particulate pytolyxabk tastier aod is eonigatecl to deliver d¾ particulate pymly¾able totter to the feed e©n **¾ and bea t transfer particles disposed, within ths.i»¾mbie reactor drarrt

Ou.e etuhodituets t of a method for pwoly og p m!ys$ !e m$t comprises; (a|

tra sfe particles disposed therein, herek the rotating reactor dram comprises an amudar wall that is siifesia tially irtipoo¾eabk: lo the particulate p mly¾aMe totter being delivered and to the beat transfer particles; aad (b) h n^ot ily rotating the rotatabk tractor drum c ntainng the respiting mixture of particulate pyrolysthk matter and beat transfer particles far a time, and at a e emmre, sufficient to result in the pyroiysis of t paniculate pyraiyzabk matter to fbrai a mixture of pyrolysis products eoasprisinu solid char particles a»d a vap r- a e eomp_¼fog eoikietisabie organic m lecules arid aoft-c ndeftsabe molecules; w ereitu the saaula wall of the rotating: reactor irara is sttbstaritiaily permeable to the solid char particles, such .the solid char particles exit the rotating reactor drum through the anayiar wait f#IM f Om embodi nt of a asethoil t% di : iegtat d yrolysis of yre^ahle at ter

matter b a pyraiysis reacor m. the reserve of hydrogeo md p folysb a«d bydrogetiatiott catalysts, such, that, oxygenized orgaak pyro!ysis product moecules undergo hydregmatiofi reactions Is t e yrotysis reactor; separarbg solid pyroly&k oducts ^' item va oi-phase products, the vapor-phase products ^■ com ising pyroly&ts an hydropmstfers. od ct^ ami hydrodeoxygenat g separated vap©r-j*hase products in the presence of hydrogen d & Iwdxodeosy Ciiati n catalyst- is a Isydrxleoxy wioB re¾0t r, fWltf In one as ect, a drop-in feio-fiiei is disclosed, where the drop~b b.io-feel has a water -content of less tlMnabam C,2¾ WL md m yg i ontent of between Aom 1.4 to a ou 1, 72% wt la a .related aspect, the oxygea content ½ less tfeai* a out 2%: wt, l Ml} Ober p ip features and advanta es of ihe niOT will become ap arent tft those skilled m the art upe>« review of -the Allo in drawings, the deiiiied deserf †jorj _s a«d the a pended daiias,

B KF PES !Ei ri !S OF THE i¾AWl S f 801 j lttstirative emboibnents of ifee inverairjn will hereater be described with *et¾rwe to the acoompaiyjjg dfflwiigs, wherein b¾e mu»emfs demote like elements.

0i3J FIG, 1. is a schematic diagram how g a eross-^etkmal view of om embodiment of a rotating :fltadked»W fast pyroiysis react r, fWl: | FIG.. % m a schematc gr m showbg a cross-seetlonai view of the react r dt¾i¾ akea aloog line ii-ii of Fill 1 s the direcion of the aro s _*

[001 Sf F!Cf 3 is a schematic diagram howing a- eross-seetkmal side vie of the reactor drum ofRG.2.

[10MJ FIG.4 h l!o% ^? chart, illustrating a system for the ii»egmr « of the pyrolysls of pyroly¾abk matter idt the Irydrodeoxygenatbo of pyrolysis roducts,

{W t7\ FICl 5 shows a GC/MS analysis of the upgraded ks-otl produced ftom mm stover. DETAILED DISCillFTIOM jMt.Sj Reactors fdt the pytolysis of pyroi aihte matter,, pytolysis systems teeerjKmithsg rhe reactors an met ods of usiitg the tractors are -provided. Also provided are systems and etho s for integratin the pyrotysis aad feydrode xyg««»io¾ of pyrolyzahJe matter,

\m)i §\ 7 & pytolysis c rmm a hotiMiitidl ates* _; fldcii¾^-bed ½ which pyolystable maied stall as homss, can he ecstvefted ^' via pyrofpss iato ii<pid Ib k mdiw value-added chemicas. Duri g the conversion process, the pyrohzahle matter ke attimottsb/ led nto a rotating reactor drur& that is hoosed: tton a :f¾i¾ iso:o ehaiB.her where It eornes iitto dirct m mt with a partieatete teat nwsfer :raedl«m. Pior fe lite .»«¾iitcik« of yrol ^hle ^■ matter MIS the rotating reactor mm, the particulate- feeat m¥ w &&m is- .placed In the i m a.od protested IBejj ro!y tbie i&atter is then eo ^j ttkaalty pyroly ed: iatoa afo&m of ola le rganc eorapoands aed soids-p ase c ar particles. The rodu t stream of volatile va rs a«d chat particles $m then ext the rotating reactor drum rid enter a o&i

separating usjt, where the char particles are separated lka¾ the strata a pottim of te vapor is «o¾n$e into m. oil, and another porti n, comprising the syngas,, is separated from the oil. The ^■■ •syng s eats then be withdrawn. m the p$mtysi* reactor fo use m dow irmm application,

f ^§ i*2l.t| The m ting re-aefor 4twn oods he yoi ^hle ntatter gaterkg t e drum with the partienkte heat traasfe m erial to ibrm a moving and rotating llaidk^d^d for i¾st pyrolysis reactions. This desi n elteiaates the need for a ressured inert carre gas, such as those used to f dize ^' the bed & e-keiilaimg- i dt¾ i hod pynrfysis i:eactor¾. Com^uemly* the pyrolysls ^' re ct r si¾« tm snhstantialy redtice the pressure dro m&td of the reaction chamber cm he decreased, the processing system can be simplified, and -the roce ssin cost can he redaoei i l fi to other pyrolvsis reactos,

f §02 ϊ I Allow lag the pyrolyzah!e feedstock to contact directl the particulate teat mm material mih the rotating iMdi.¾e bed enables the pyrol stable matter to nMlntairi IS I eoosaet ifh the large sortaoe area provided hy the patdcoate heat trartster material and with any eataiysfe; such as catalyst pellets, resen ia the rotating reactor dram. This, cat*

sp.tf¾atily ioctease the ^' heating rate and the mass aad energy fransfeel eiencks between the pyrofysis .reaetaats arid the heat, transer oiaierial, and em also increase catalysis reacti n rales and ¾ecf¾aw he rtnmtef of hed m d«¼s necessary fe large systm capacity, thereb improviag die ovefall processing efficiency a d ptodrtet yield. ^' oeover, the re-saliiag re action in the reaetant resideaee thnes d $ to mmkm . abtmi e -wear on catalyst particles awl. therefore, sue r aves the .lifetime of the catalys

|fii>22| A. ba t milmlmeni o f the pyrafyds reactor com o e a. reaction chamber lit which pyi ^' lysis is earned ¾ fedi g unit, eontljptred to tmroduee- pyrolysis maefants into the reaetloii chamber and a product se arating unit adapted to separate solid-phase pyrolysis prodncts front va o- hase pyralysis ro ucts, A reaeior drato configured o rotate about a ho««oatai $ Cle, _s . a rotataMc realto dain) is housed wit a the reacti n t¾mber. The reactor d m k connected, to a rotation drive that is confptred to rotate the reactor drum about the horizontal axis. The feeding -unit includes a feci conduit configured to transport woi able jmatf fr m a source ofpyeolyaafote rnaiier htto he reactor dum.

|ift23| Tie rotataMc reactor drwm eontpthsas an annular wail having m sutler surface and art outer srsdhce, wter fe the «r wall efines m interior space. The aminlar wall is positioned annalarly w» d the mtational axis afep t which the dram is configured to rotate when the reactor s ½ operation.. Ait intake apettoe, deined la a all of the totatable reactor d m, s provided to slow pyroiy^ab!e matter to be iotro oeed into the in terior of the dram.. The reac tor dram can take on a variety of f rms, both symmetric and «on*symt¾etric, In sotac et¾ih&dis¾tc«s, th reactor d m has a cylindrical shape hi which the annidar wall is the cylinder wall and the i ake, a eture is defin d In, or defined by, the end of the cylinder ftO J WitMn the reaction chamber, the totatable reactor drum s disposed horizontally a out a. horizontal, axis of rotation...As used herei , the tnm "horizoruar and "h rizontally" are used to Indicate thai the axis abont which tie reactor dram is configured to rotate mm, perpendicular to, or f bsiassially perpeudic tslar to, the direction of eart 's gmvtatlanal force. The term horizontal does not exchtdc configurations in which the reactor dram and the « of rotation deviate s mewhat om a perfect hoizontal position, pr vided that tn cotatfonal axis Is more closely aligned with the direction per eodica Ia.r to the direction of earth's

gr vitatioiiai forc than with the diree» of t hat force.

fiOilSJ Tie annular wail of the roiatahle reactor drenn i s d si ned sweh that ft Is penneabie to the solid char particles ferried ^■ within the reactor dmnt dumig pyrolysls, kit impernieahfe to the pittieriiate pyroteable matter that is fetto nced ¾o the reactor dttun through the feed conduit, impertaeahle to heat transfer particles tha are housed within the reactor drm and im meaWe to |>artfc« te catal sts and/ r paniculate eo^reaetants hoosed within the reactor drasn. As sueh, the annular wall Is able to eoittintsonsly expe-i solid, particulate pyro!ysis produets _: ithout expellirsg heat transfe particfes, _; pyrolysis catal st particles, o eo-^aeaat particles , hi som υΙ κϋΐϊΐ& Ε, the per eabr!ity of the mnm^r &lhc&itbo provided by a luralit ef holes that extend though it¾e wail, The diameters of t e tels will -de wl of the sfees. of the t ctant particles, hmi transfer pariicks and my catalyst anices used By way of .illas&miott ο»Ι¾ la so ^' ms emtx>dimefifs the oles have diameters of m greater than .about 30 mm, T¾is meiides em dnwais in which the holes have diameters in to rait&e fr m 0.5 to

20 mm, further l?¾e1odes m diments in ich the holes have diameters in the range i¼m I® 10 mm and still turl er indodfes ath d Be:rts in which the oles ha dt p¾¾ites¾ in th mage from .1 to 5 m .<

|W | Tbe hea ttaof fe particles cart be rsade of a riety ^' of materials provided they am ahle t» absorb heat .from a ea srr rce and toRsfer the heat to the particles &f pytolyxahle matter whet* they are placed it* eonta&t that matter; The heat transfer particles ar desirably made of an roett: material such that the d© s t participate m, or interfere with, the pyro!ys!s r aeiotis. Ex mple of saable tpaierlals lor die fsMitetts!cr particles arc satKi al meiat , jW27| As me«io«ed boe, olber particles that .may he held tf t* the tsaetor di¾t» include catab/sf paricles, siieb. as pyroiysls catalyst pellets atni/or hy ro-eiisr a catalyst peliets, aod particles of c Hr acams (Le,, reacMtts thai eac wit the pyroiyzable matter dtiring jiyrolysis).

ftOISj The feed eottdmt of the pyroiysls reactor is iu fluid c&mmw catida with the s t t 4mm &ηύ is e it ur to transp particulate pyroly¾a e matter ttovn a sottree o said matter into the .inferior of the reactor- .drui¾. As used herein, the phrase ^u fluid

C Bim& c&ti - witlr s tssed to uidieaie thit the designated coffi ottesits ae emffieeied through a path long which a -material cm travel from one location to- another. The particular path C take o» a wide variety of forms,- The teed co.rtdt.it deftees m input a rtare through which part icles of a pyroly^able matte ae introduced- itm die .conduit and an ottipat aperture through which particles oT pymlyzabfe matter exit the conduit The input and output aperture are eopoeetetl hy a ehatttsei The feed cortdutt tnay further co is a conveyo oieehanism e s!i tSfed. to eoiidaa usly trans ort parpctslate tratier al ng the charmel from the mpai aperture to the output aperture, Exam les oCcots eyor rnec baui tns inclu e augers an conveyor belts >

102 I The reactor 4mm. and, desirably, -at least a portion, of the feed condui t are b used lfhia a reaction c ambe. The reaction chamber Is designed to help contain vapor-phase pyto!ysis products exittag the ractor iktaa and to allow for thermal isolation of the pymlysrs maetioo e:Ewko«»l in s me en od¾ oeots ti resei a .chamber, deli tes m a&nul&r space arop d the rosatiihle reactor 3rmi md the portkra of the ieed conveyor. This annular s ac , hkh ma take a variety of sha es. Is hi f M m mmk&iion with tiM iOiarabie reactor mm such that vapor-phase pyml sis pr dt¾js formed in the ro tahle reactor drum are able to flow into die annular space aroimd tie Iced coadriii Usi« this design, the wpor-phase product ssre&m can he to heat the feed con ye s»eh thai the parieulaie pyroiy¾able

carried within s peheated w eit it is s w!aecd km the reader drntit

fWMf The interior of Ihe reaehor chamber mi mor speeifieady, he interior of the reactor drum, ear* fee heated by one or m re hear so ees disposed exterior to the teaetkm chamber, disposed interior to the reaction chamber, .but exterior the eader 4mm, and/or disposed withlo the reaeor $mm< Suitable heat souces iectede radiation (eg. _s UV radiation) sources, contact heaters and fuel banters, ta soai embodttBessts of the reactors, a beat source is provided at the center of the reaetor drum. By roviding a heat utee at the center of the reactor drum for large sea ie reactors, the tftaxinftmi aaiOuai of available heat can be utilized, the seed, for expensive qwartfc windows aged some current reactos cm be elimijmted arid, particles cast he kept away from the radiation source.

|Ki3l| The product separating ««it is i fluid DanMrobeatien with the .reaction cheiber and positioned to accept both solid- and vapor-phase pyro!ysis prodocrs i g the reaction chamber.. arious ff du separadtrg writs ear.* be employed, ioctodteg cyelo»e ype- filters, l¾e product separating waii generally camp-rises a product collection, cham er; Imvlng an mptii port in fluid cornotuihestsots with the reaction chamber atxt an ontpat port which rosy be m fluid eomistsnicatioa with a o nstmn roc ssng device, mch a condenser, la soots erstb diotcats, the product separating unit fuslher comprises a product conducting ebanrtel that extends from the reaction ch&uite h¾o th roduct collection ehanrber artd further com ises a lite oused tMn. the prodoei colleetiori. chamber and disposed around the roduct conduction channel, saeh !bat vapor-phase pyrolysis products entering de product collection ehm»h t throagfe said, chauue ^' i will pass through the ilier before they cap exit through the product collection chamber " output pott- in soroe etufeodntestts, the product collection chamber is positioned directly below the reactor 4mm soel thai solid char particles drop f the dram mm. the product coileetion chamber.

8i32| Methods for mm$ the pesent pyrolysss reactors com rise the steps of delivering parieiiiate pyro!yxable roatter into- a hori:«ontaliy rotating reactor drrait into which beat tmosfo partices anil, pti#a ¾ catalyst particles and/or c0'O¾ ct nt particles- have been pre- InserteC and ki«Ma«al! rot ti g ^' - the reaaor dam for time and ;.u a erapstature sufficient, to s t to pyro!ys!s of the particulate pytdyzable matter. Bxa.«ip!es of pyrotyMb!e mate inchsde btomass, which is a com osite of cellulose, heraieelluloses aad lignta, Soar es of bk¾»ass include, ^' bat. are am. limited to, wood, plants, mrueaes, algae and bacteria.

I §033 As the reacor drum rotates, the sold particle ed contained therein ^' undegoes a tum ling moto that estates a f¾idi*.ed particle bed- without the we d for pressarracd carrier g ses. Irs fact, he present jjyroiysi methods east be carried ut at am ien sir and at atmospheric pressure Alternatively, in $ rne embodbueots m elevated ^' ressure,, such as a presswe u to about 1 aroi, is employed.. Typical p¾lysk ^' te ctfoitt«e» «!r§i¾tes in the reacor drum arc m me ange of about 200: to about SOD * Typical reactor drura rotation rates are in th ma e from a ^' b n lO to 800 RFM. 90 J Because the annular all of tie reactor drum is substantially impermeable t¾> dte solid char particles r duced via p%aotysis, those char particles co tinuously p ss «H of the reactor drum, iato gft the atte!at wal. As tuted hemt the phrase "stibstan!ial!

iu^emteabkr is sed to- indicate that a majority of he char particles are able to pass, through the aoooai wall The expelled char particles and the ap r-phase pyroiysis products cm then be collected is the product eel!eebou ham er, wherein the vapor-phase products - re.

separated from i¾« char and other solids. Finally, be n enMb!e organc molecules can be co de se fmoi tbe vapor-phase to ovide a l.i<§uM product* such as a fuel oil Coodensabl orga.uk molecules ^' that may be f rmed fey pyroiysis include saccharides, aah d«?. ts, aldehydes, tat¾ ketones, alcohols, and carboxylie acids.

|003$J FIG.: I is a schematic diagram .shewing eross-seetiooa! view of ne specific em diment of a rotating tiuiifed-bed fast pyroiysis reactor, In the embedment depicted this igwre, the feed unit comprises a sere ^ype conveyor feeder. This feeder comprises of a bi mass hopper 102, a feed comltwt 104 _: , and as auger .106 homed within th feed conduit and comprising an auger blade 108 that efi es a .helical coil about a coil asis tat coincides with the ecMrai longitudinal xis 1.10 of feed conduit il! . I oroass hopper 102 contains a plp iiy of biofoass particles .1.0-3, feed conduit 1®4 defines an input aperture 1 5 through which bio oss particles 1#3 from, biomass hopper 1 2 are introduced into the conduit. A valve (not s o rf), such as an air-lock valve, east be ^' mstaited to eontol (start ami stops the few of biomass particles from b rnass hopper 102 into feed conduit 194. Feed conduit 10 further defines an output apertur 10?, positioned downstream from: inut aperture 105, through

S which hlorttass particles 103 exit the eondoii A«ger 106 is eoaoected. to m4 misled by a first as in icate fey arr ^s Af The tnoroa.ss feeding rare etO: be controlled by the f»f¾t « s e d of anger 1 6, desirably with a mtttiimttii r¼dl«g rate of zero, f &0 J The pyrolysis reactor comprises m interior reaction c anc 112 in which a tekotttally ro able reactor drum 114 p ion of feed c adtdt 10 are h used, ths enrbodisBeot, reaction cham er 112 om ises two serially joined pipes 116 _? U $ having different diameters, to h¾€0n¾ui tiosy an arsn a space 11 f is formed between feed coudnh Ml and pipes Hi, 1.18, The pymlysls reactor forth er com ises an exterior housing 11 .dis osed un reaction .ehatnher 1.1.2 and 'conigue to provide thermal isolation for d:rat chamber. The k*iem¾r spac 121 povided by xterio ho«siag 120 cm he filled with thermal isolatkm materials, s«eh as silica, ceramic foam or glass fiber. Pi es 116 aad Hi ears be heated separa jly ami dierefore, are able T provide two reactioo S fc-cbarabers

ehameteri¾ed by h aliag 20n.es a ng ifferen tenaperatares, f¾r ex m le, each of pipes 116 d 118 CM h t Ά sepaate electrica! heater t»o««d on its outer surface, However; otter ty es of heating soarees, such as hot air, ei©cin¾«iagsgik radiation or tiifared radiation cast also be used. 1037| Rotatahle reactor drum 114 defines aft intake aperture I IS into which feed e«Mt 10$ extends and through which blomass particles 103 can be introduced into the drum. IGS.

2 id 3 provide enlarged, eross-sectional views of rotatable tmctor d sm U4< FIG, 2 provides a view of reactor drum 11.4 takers aiortg line ii-ii of F G _* 1 in the direc tion of the arr ws, .i¾G„

3 provides a si e view of reactor 4mm 114 _* I¾ifirig operation of the reactor roMab!e reactor drum 114 will eootain a flitidiasd bed com rising a rnixttjie of solid panicles 122 tira e op of sonie combination of hiomass particles W$ _> beat .tra se particles 123, bio-char particles 135 a«d, typically, catalyst particles (not shown), la a related aspect, catalysts m includ , hut are not: iroked to, those fomatkted from noble metals wit supports of ¾ ik» (o,g,, ZS!vLS, available: from ACS Material, LLC, edfbrd, MA), al«n¾kta¾ oxide, or carbon, based catalysts suc as those sold, wader hie mm® A iE LYST (Rnom & Haas)...

[Q038J In d¾e:embodiffiein of FIG, 1 , TOta te reactor drum 11.4 eoffiprises an annular wall having in inner surface and a» oppositely disposed outer sarisce. The annula wall is positioned aon kr!y around the rotational axis 110 of the 4mm, The atmtdar wall defines a plurality of holes 117 that extend .from Its loner surface to its outer surface od thai are ^iz d to retain !ieat tratisiet particles 123 and any catalyst particles within the reactor rum, while allowin bio-char particles 2S to ass ooi of the reactor d am ! arid, sohserfoeotly, out: of reacton cisatsiber l ih vugh a ©at i* a rture 128 · disposed bel w o^tatable reactor dmrt 1:1.4,. ota!ahie reactor drum 114 Is c rrected to tod rotated by a second driving motor (not bowBi ck as a variable speed motor, as indicated by arrow ¾ ^: \ A shown in the figue, the connection m be made by a driving- rod 124 (e _t g., a bar) ^' connected to reactor 4mm H4 md positioned opposite intake aperture 115,. In the embodiment shown here, a eoo! g chamber 126 is disposed aroami :red 124. Cooling chambe 126 cm be. filled th a coolan material, snob as an oil.

|ift3 I Tie ose of a variable sped meter to drive the react ram allows die rotatiog dram to operate in. a range of low to intermediate speeds, providing legibility for eeding homass reaetants ittriag a variety of pmkk sue dfetriteiiom md biorross types. Tim fle ibilit cm provide t e reactors with a d ced .aeed for bioraass feedstock ereatrooot, tower overall r ssi COSOL better temperature control _* reduced reacatit ret nion time, and improved reactor performance re lative to other k«ow« pyrolysis reactors. Moreover, the se of a variable speed motor allows the void fraction in ti iMdlrf e die bod de ay .a»d _:t e mequ «fl> the bimdiiig of biornass and paticulate. he tm«st¾r raateriai t be

flhMtif Optionally, a heat ots∞ ma bo disposed width* m a le reactor 4mm 11 d eonftgnred. to boar the roaerautsi ^' n he il«idi¾ed bed, Examples of suitable beat sosrces kdade :t¾diaiioo. sources, ch as tfV te :> la mm embodments the radiation souce is a cylindrical lamp di sp sed witb.ro dre reactor draro and positioned a iular!y about the mtadoMl axis of the- drum,

fl) I j The r wf separating unit is ooofl red to accept a mixture of pyrolysis ptodoets, ioc!ediog bio-chax, bio-oil and bio-syngas, from the re¾etto.ti vessel, it* the eaibodlioerst shown I» FIG. I, these pyroiysts pr ducts pass Into the separation went -through a prodact. conducting ebaooel 13δ that exends between the reaction chamber .112 and die product separating mk aad opetis iuto the iaiedor of a pyroiysis prodet collection ehai ber 1.32, A filter 134 housed within product collection ehauthar 132 is configured such that vapor- phase pyrolysrs r du ex¾«tg product cond ciin m 136 will pass through the fitter to remove my ash. or rec nvered bo÷ s a i hto*ehar particle before it exits product collection chamber 132 through, exit pott I3& Exit pert I5§ is la fluid mtumuu.ic i .it with a emideoser 138 via a cooooctiog conduit 140, Asuciion draft lo e 142 coMjeeted m ^' m outlet of condenser 138 ^' is configured to: maintain a negative ressure in ioteriof reaction chamber 112 and to draw off non-condens ble gases 144 front, condenser .138. As u ed berein. the term. m^m rnh refers lo-ehemieat eoi^owads hayings* low slew point (below

ade»sahk ses hiehtde CO, C0 _¾ , lh sad€¾. A c∞d aser product chamber Ί.4&. m coni ued, to collect -eo&densed oduc 148, ncludin bio~oil, exiting the cond nser,

|i§42| A rocess for the pyro!ysis of hiom ss u t fhe retetof of WIG, Ϊ n comprise the iowiog steps. Whets the reactor k in operation, .motor dri ves driving rod: J 14 a d rotat s teas-tor dram 114 whie b i heat tl two s ^ha bers of Interior reaction chamber 111, As the te erate- ss 6f %vfadham e& rise, ifce eat t ie particles and catalyst particles, which are present in reactor dra 114 from the atsei of the process, are evenly he ted because the are r telpg eom tMt ¾¾¾d m drect contact with the amiularwafl of the reacor drum

(003 j Once interior T CPOT chamber 112 reaches a ps-selected ebvited temperature (typically a tent satw m the raage f m about 200 · to a o t 800 ^s C),y omass panicles ICO ae conveyd, through feed cot5du.it 1§4 by aug&c W& _> w ich Is driven by moto A, uatti they are deposited iimo ^' feact f dum 114,· where they .mix with ^' beat transfer particles- 123 attd catalyst paritcles, When the biorMss particles 183 travel thrmtgh feed eoaduit IM, they ma be war ed ap by the hot vapor-phase pyrolysls roduct, strea exiting reactor dmm 114 mm nrm space 119 , while said vapor-phase product stream is corres ndingly cooled down,

[W44\ The preheated bioraass particles W$ are desirably fed m reactor dmm 114 at a lew ratio of blomass to hear transfer partiefes. The solid particles of the resrdhrrg particle mi ture 122, which are ^' initially held asairtst the lower portion of the annular wall of reactor drum I 14, move In the direction οί ^' dram roMkm under the combined et!eets of eeai rilligaj. forces a¾d the otion between the particles d the annular wall of the mm. The lid particle nkmre 122 rotates p rd as the -dmm rotates until particle ntls/rore 12 MM bach to die particle bed held m die lower portion, of reactor dram.114 under the f rce of gravity. This c ¼^i.ot»i¾gfalil8f mote of the rtkte creates a mo ing I¾ldl¾ed ^» bed. jltMSJ Once bio iass particles 1 §3 have bm pyroly¾ed in. reactor dmtn 11.4 i«io solid hfo- ^« eh&r ard a vapor-pha.se eomprlsirig, or consisting esserrdally of organic co portttds d water vapor, the pyrolyais proa¼er stream ¾ a « away from iiterior ;reaetiors ehaniber 1.1.2 through conducting channel I md into pyrolysis product coMeetion ehamher !.J2 _;t where it is separated into- thre products: foio-chif, blo-oi:! _¾ nd hl -syasa¾ (the ors-eaad aMbie gases). Solids, siseh as ash. _? or^cotrverted hioi«ass artd bio-cha pardclcs are separated freat i the product vapor str am by -filter 134 a d stay inside prodi t e½r»her 13-S, The rem&uwng vap t-pferse product am Is drawn oat. of product collection chamber 1.32 and travels through eoMteetkg con ui 14i to condenser 138 _¥ where the eotsdeasabk€< ¾ «e«t$- in the vapor are condensed mo !kpid bio-oi! 148, which is collected in condense -product, c amber 1 & The ^' -««¾¾ifi.a% »o»C0U imbte gases 144 & drawn oif-fra** condenser 138 by Mower 1 2 for further cess g: or bum to provide bear for the pyro!ysis process.

[8 6.1 Anothe aspect of the ¾«tt€>a provides systems «I mtk U for integrating the pyrolysis of pyraiy abie matter with the hydrodeos: g r^:a:0 ^' srs (ROO) of vapor-phase, organic pvrolysis products to provide lor t&e eontimions conversion of the pyyo!y¾ahle matter into liquid bydtoearbon ue i s and other v&fue-added Uqmd Odnets, FIG, 4 provides a flowchart it!ast dng such a ystem.. In ths stem the pyr IyMble matter cars he, for example, solid btontass 02, Solid hkmtass 402 can ^' be prepared for pyrolysis h chopping irhto m inali pieces (e.$. ₅ into particles aving a roean siz (diameter) < SO swo), then placed Into a dryer 414 io reduce its r«st«re . (MCI lo s -value of, for exam le, lt$$ thm about! fi wt, % (wet basis} by espel ag: water 405, The dried hiomass may then be ground into a powder ng ¾ grinder 40 By way of iikstrapQi¾ onl , typical «a» particle w for the powder is Jess i n about 3 rarrr This biot»» powder is then fed via a feeding unit 40B into a pyrolysis reaction chamber 41 § where i t is py¾iy¾erl late a vapor- hase οο«ψΰ§η¾ί organic corapottods arid water vapor. Pyrotysis reaction chamber 11) can he heated with an external hea t source 40$, such as a. gas burner. Within the reaction; chamber boat carring particles aid and ^' s e up the pyrolysis process; Irs s m emb diment , the biomass feeding unit mi the eaction chamber of the ahr -descnbed rotating lloifeed-hed fast pyrolysis reactor are used as feedkg iwk 40g and reaction charnber 1 respectively.. Hydrogen gas: 411 is iatrod»c«4 into react ft chamber 40 aad _> - tit the resence of pyreiysk catalysts and/or hydrogeo&tior catalysis presetti i the reactor, .resnhy i the hydrogenatipa of oxygenated Mo-oil eotnponods produce via pyrolyss. The hydfogetsation reactions saturate the product hydrocarbons, which results iu m e slabte bydrocarb os having -a higher Bit ratio mi tea heavy tar. his is advantageous because i reduces catalyst touting problem an improves catalyst activit during the c nversi n process that takes place is the downstrem HDO reactor. Hydrogen 411 ma be prohased hydmgen 441 or u-ay be h d n ohtaked troro a water- s-shift iW S) reaction 442 using WGS reactor 444 that :recycles oon-condensab!e syu :s 446 edlccted. fmu the rlownsiream EDO .reactor. Optionally, hot 413 fr m the pyroiysis/hydregetratiou reactions cau be recycled to pro ide boa t dryer 404. fSMM? I Tie vapor- sail solid-phase pyrolysis md bydrogettattoa ptxxltiets thers pass out of reaeiori chamber 4I# a»d ism a filtration device 4.1.2, such as a eyetae-rype filter, where the soils! prcsditei particles 414 com rising blo-chaf md ash residues are sepaated f tie vapor-phase product steant 414 Trie se arated bk-dx&r caw he activated and used as a e&ialyst support n erial or a« activated arta, or as a, process Fu l or a soil additive,. The vapor-phase roducts 4I# are combine with hydrogen s ^: 41$ m additional time and c m essed by a eomp«s$ ^« _* ar 42# Wore they eater- a« HOO reactor 22, -suc as a tubular !ked }ed teaetw, where d^Jwygemts&E catal sis ttitege. the ox gen content

hydTOca,rb∞ts> that, when condened i« condenser 424, are of the qwlitf z w y to allow i sertion in a petroleom re:B«ry ^! s hydre racker md isomenxatiou units. The compfessor 2$ k vapor compressor i« which the vapor streatns are compressed to an elevated pressure typically in range irons about 1

reactor. Optionally, * 425 {mm condenser 4:24 cars e d back as a heat source for dryer 414.. The n n-eond t* ie gases 446 ma be seat to WG reactor 444, as discussed above, or tnay be butaed as a i¾el 448 in ktrner 4SCI to mp≠y h t air 52 as a e r ource lo dryer with .cond nsation and re-evaporatioa

}iKM$\ Tie cnaden ad.i grade bio-oil. hydocarb ns 4ίί -fmm eoaderrser 434 have a lower density than, and are substantially tasoiobie water.. Thus, these liquid hydro arbors bio&els 4 . am be separat d irotn the fee- hase system by separator 28, ^' The remaining acpeoas ducts 42 oas be either recycled back into ^" the bio-oil upgrading streara 431 for increasing bio-oi! yield or collected m qmd collector 43d for ta&er con esi n into ethanol by Ie mof5¾i a, or mto other vahte-added :chei»k¾ls.

$M$ Se ern! fatures ^' will be apparent to QM of skill m the art, cied g- 1 ). m mm gas is needed within tie .reactor chamber, 2) catalytic py.ro lysis can occur within the CFP reactor, ) i¾dstoek pa.rt.kle m cm be more variable and larger than current pyro!ysis technologies, 4) catalytic md sarsd or other heat ca yin devices remain ts tie reactor, no separation or recycling is required, 5) temperature is easily controlled, 6 high heat transfer rates are aehkved, T ^' s the ^:' eactor scalable, md 8 i tie reacto cart convert multiple feedstocks including waste wood, cro esidues and grasses,

[6058} As used herein, ^' 'llhstrative" means servtrsg as an example, instance, o

illustration. Any aspect m desiga described herein as 'ilksRMive" is eot Recessarily to e construe*, as. referred or ad asiagews over other aspects or signs. Farther, for the ur oses o this . isc sure mi otherwise specifi d, V or T m m ¾¾ or «*oe Stilt f & , the ose of "srf ^* or f ^* intended m lickde ^i: ¾.ijd/# ^v unless spedileally kdkaied ot erwise

|iiSI| As used, herei , *4rop-ut bk f«ei" m iO&eis thai are completely

.ktercfe&itgea ie with conveni nal fuels. For exampe, die m -m f«el rmy. he "FT-SPK ^* * which mea»s pr eessirig sold biom ss asag pyroysis to produce aralysis oil ©r gasification roduce a syngas which s then processed into F ^' F SPE (Fbcte--¾ psch Syntbede Paraffink Kerosene},

EXAMPLES

Feeds lock Preparation m& Feeding,

|§0S2| In ibis Example, to collect observed, bio-oil sample, 5f}0 grams of com stover was used 10 feed li the react r, Si raass (ie,, corn stover) was chopped Int small pieces less than about 29 mm in , dried to MC of less than about %% _f and it«¾« gt nd mm powder with, a parftele st¾o ofless t . nbi 3 aim. The dred biortmss w s then fed into the CFF reactor f wly . The yield rate of raw hio-oti is. about β$%<

jNJSSf The coon Mover po dbr in the CFP was deeotnposed into a mkture of son- corideusahk sysgas _* sw hlo~oil (orspaie eom ow stds a« ater vapor) md s l id M -char at a temperaipre w ch ranged fern about 400 to about at n t I ATM ..pressur ., inside t he reactor, while the con s stover powder i decomposi.«g, oxygenated com ounds of raw o~od vapor were hydrogenated ^' into .m te staid© Iwdrcscadson va ors to the resence of hydrogen, hear earryr«g parileies and solid. eat ys! particles. The hydrogen sed was g n rated the c«-ptod«cts (f e., raon-coodensable syngas) produced by the corn stover po wder decomposiiioo. Use of this source of Irydrogen for hydrogenaiios is applicable where outside hydrogen Is injected to increase hydrogen concentration ruside de reaction chamber. Catalysts like∞!ite based Mi, Cy Co, have been tested and used I» these reactions with soeeess. The ratio of Mcnnass w catalyst ranged fr m about 0,5 to These Itydr genatioi} reactions saturate the hydroc rbons,, producing a higher ί€ ratio of op to about 1 ,2 - 2,2 fibm core stover, aterst 0.2 ^■ -· ^■ CXt), diereby prodrrersrg a nrore stable hydoe rf:H>sr vapor.. Qualify hydmoaroors va ors, containing less heavy tas, significantly improve catalyst activity and life eyeie length in the sub$eqit i!Jt FIDO reactor, The hydrogen gas needed may he purchased or o tai ed fr m a water-gas-sbdt (WGS) reaction by recycling the »on- syngas prorkcei..

Bii -C ar Seimratlosi:.

|10S4| lie pyt !ysk arid hydragenstion. pKkinets streanm e it from t¾e C P reactor md mm a cyclone filtering se arator to remo e solid p»d«cts (e,g,,. to rterted bio-ebar sad ash -esdues. Om nwm additional fi m tmy b rssed. Activated carbon -mt be nsetl as a snpport material for the catalysts -used i« the HDO reactor, as wm bio-char may be used to serve the .same purpose.

Bio-Oii HEX) Upgrading,.

055) I%dtoear ^' b©»s and water va s wee combined w h a second addition of hydrogen, which, ©od atio was slightly compressed ri r to entering the HDO reactor. Within the MDO reactor, hydrocarbon vapoe wee de xygenated and ydroeraoked to .re» »w ox gen mi e i rise heav , long chain hydrocarbons to lighter, short: -chain hydroeartsoos ihat« y be Inserted i to f¾em>lett»s

units

Upgraded Bw M Cm mmkm.

Upon xi n th HDO reactor, the vapor of u g ded hydrocarbons and aqueous c m unds were transferred to a condenser, wiser® the roxture w¾ eo.Rdfe.med into a. two phase liquid ^■ .m tnre, sermon d (mm th&^y m stestrs, The JTOs-eoodemab!e gases sireaw were either seat to a water- gas-sh (WGS) reactor o produce hydrogen lor the process (see above) o r burned as ibel t p ly energy % ^' the process.

Sep ration of liquid Hydrocarbon Drop-In Fuels,

[$0§7f The enndensed npgraded b dl hydr ahdm ha - Sower dmsky and ate mostly imo!wble ra water. Thus* i ey were easily separ ted front h two-phase liquid mixtue and ^• collected for storage, Remamnig aqaeons products were either recycled back to the bio-oil pgrading stream fiat incre sing b nc . yield, or coUecied in a liquid tank tor further conversion into ethano.1 by fermentation, or valwe added chemicals by other processes.

Bio-CHI Analysis !#0§8f Ba sel e feto-m feedstock was fmkfoced fcoro co i stover m ¾ wdmt as bg the ternm m 4e«ii>ed, wills a yi ld of up to 65% raw bio~oil Diileie!t catalyse fotMuJatioa (as described above) were developed md tested with success, Seqaerstiali ttpgradbg raw p-oif m a separate ydr de xy Mto« (HDO) reactor produced a hig uality upgraded bio-oi, m. a yield of sppmskj i l 10%, A typical GCt/MS a»a lysis of the tugra ed fc¼-oil so produced is s ow** i« FKS, S, The OO S an lysis was eoriducied wills m Agdem GC/MS

C?S90A/$#7$e> _s f tiowed w e pr sent w¾h the iSTOS

ss Speetral librar . Over 85 ofmst tm y$mmb®m (m the rasge ©fC Cia) wereldespikd in the opgraded bWI. In accordance with AST standard (025 1, D- 2 8, 1-385, 04057, D4 5.05762, Dl 29S ₅ etc.), .he domination rf hysical aad ctemeafe properties of sampfcs of ra w bio-oil s upgraded oil as completed, The C, il _¾ 0 couteMs of die bio-oil samples were detsnmned using an eteraemary analyser (Perkin 2400 CMN Aoaly^et},. The water etmteM s m asur d liskg a Viscoaaaly¾8r (ATS K eosysiems,, The energy eetPeats: were m asta^d usi«g a hoo¾b calorimeter (Pai 1341), The pB mfees were measured using a pll met r (Fsher Sdentife AACCUMET ΛΒ 111

fiftSf J A side~b -skle corspadsors of the mm stover based raw bio-od, upgraded bio~oil tad ePol waj based gasoliae, diesel atidjei iiei s showr* i« Table L

Table 1 C omparison of ra w bio-oil aad upgrade bio-oii roduced from com st erm ^' d fofcum based gasoUae, dies t. aid jet. iwe!.

|§§S0| ^' The daia ladfeares the u grded fekMsi! piodaced s very similar to eP !etMa i» tems of physical md etettteal prop rties, efodmg h dfoca:f¼» eo«te»L Those

c amomiles llo the o~oil of the pee discos to be $li>sireaomt into a P ditiorial pePoIeum refeery f dmemcke aodior i iffiei at ft imts for cOiSi rsi o io "greeo fp renewifcle" gasoline md diesef !#061f Tie t¾e§&as $esetiptk»j of tlhisteaiive -emWmeitis of ike im tion km beer* fiseiitei! for ur oses of ilIosdM« ami of descri d n . taeri&d m e xh vt or to limit the ioveotioa. fo lie m font* disclosed, sad modifications md wriatiom are possible m !i hi of the above teachings or maybe ac u ed from praeteof th isveuioa. The .smfeodime s; were dmse« s«d described hi order to explarn he principfcs of thenventi and as practical a plications of the feveiitiofi to m≠> om skilled in the art t x iim i $ mvmmm m various ^ b dim^te and with. v rious cwi&atkw as ite4 to the paitictte «¾¾· w»t« plat$4 It is nternled t&at the se© © of sire in eattaft b© de&ed y the claims shaded ereto and t r o aieRts.,

i?