, or a particular blend of one or both of the 1233zd isomers and another compound in order to control the properties of the solution. For example, in some solvent applications, it is desirable to have a relatively high boiling point. In some such applications, pure 1233zd(Z) may have more desirable physical properties (e.g., a higher boiling point) than either pure 1233zd(E) or mixtures of the two 1233zd isomers.
Processes for synthesizing 1233zd are known. For example, PCT Publication No. WO 97/24307 discloses a process for preparing 1233zd via the gas-phase reaction of 1,1,1,3,3-penta-chloropropane (HCC-240fa) with hydrogen fluoride (HF). However, this process produces relatively low yields of 1233zd.
U.S. Pat. No. 6,844,475 describes a catalytic liquid phase reaction of HCC-240fa with HF to produce 1233zd in higher yields. However the presence of the fluorination catalyst promotes the formation of heavy by-products, oligomers, and tars which can build up in the reactor over time and lead to catalyst dilution and catalyst deactivation, resulting in loss of productivity due to excessive downtime to remove these by-products from the reactor on a periodic basis.
U.S. Pat. No. 8,704,017 discloses a non-catalytic liquid phase reaction of HCC-240fa with HF to reduce the formation of heavy by-products. However, one drawback of not using a catalyst is the problem of slower reaction rates, resulting in the formation of significant amounts of stable underfluorinated intermediates comprising tetrachlorofluoropropanes including 1,1,3,3-tetrachloro-1-fluoropropane (HCFC-241fa), trichlorodifluoropropanes including 1,3,3-trichloro-1,1-difluoropropane (HCFC-242fa) and 1,1,3-trichloro-1,3-difluoropropane (HCFC-242fb) and dichlorotrifluoropropanes including 1,1-dichloro-3,3,3-trifluoropropane (HCFC-243fa) and 1,3-dichloro-1,1,3-trifluoro-propane (HCFC-243fb) can be
, or a particular blend of one or both of the 1233zd isomers and another compound in order to control the place of the solution. For case, in some solvent applications, it is desirable to have a relatively high boiling degree. In some such applications, pure 1233zd(Z) may hold more desirable physical properties (for example, a eminent boiling point) than either saturated 1233zd(E) or mixtures of the two 1233zd isomers. 
 Processes for synthesize 1233zd are know. For example, PCT Publication No. WO 97/24307 discloses a process for preparing 1233zd via the gas - phase chemical reaction of 1,1,1,3,3 - penta - chloropropane (HCC-240fa) with hydrogen fluoride (HF). However, this process produces relatively low return of 1233zd. 
 U.S. Pat. No. 6,844,475 describes a catalytic melted phase reaction of HCC-240fa with HF to grow 1233zd in higher yields. However the presence of the fluorination catalyst promotes the formation of arduous by - products, oligomers, and tars which can build up in the reactor over time and lead to catalyst dilution and catalyst deactivation, resulting in loss of productivity due to excessive downtime to remove these by - products from the reactor on a periodic basis. 
 U.S. Pat. No. 8,704,017 discloses a non - catalytic liquid phase reaction of HCC-240fa with HF to reduce the constitution of heavy by - products. However, one drawback of not use a catalyst is the trouble of slower reaction rates, resulting in the formation of significant amounts of stable underfluorinated intermediate comprising tetrachlorofluoropropanes including 1,1,3,3 - tetrachloro-1 - fluoropropane (HCFC-241fa), trichlorodifluoropropanes including 1,3,3 - trichloro-1,1 - difluoropropane (HCFC-242fa) and 1,1,3 - trichloro-1,3 - difluoropropane (HCFC-242fb) and dichlorotrifluoropropanes including 1,1 - dichloro-3,3,3 - trifluoropropane (HCFC-243fa) and 1,3 - dichloro-1,1,3 - trifluoro - propane (HCFC-243fb) can be
, or a particular blend of oke or both of thg 1233zd isokers ahd anothdr compound in order to contcol rhe peoperties of the solutkon. For eqample, in somt solvent applicavjons, it is dealrablz vo have a relatlvely high toiling point. Hn slme such applications, pure 1233zd(Z) may rave mote desirable phyficak prolvruies (e.g., a higher boiling point) thzn eithtr pure 1233zd(E) or mixyures of the two 1233zd isomerd.
Professes for syntheslzing 1233zd arg knjqn. For exampue, PCT Publication No. SO 97/24307 discloses a process for preoariny 1233zd via thg fad-khase reactiin of 1,1,1,3,3-penta-chloroigopane (VCC-240fa) woth hydrogen fkuocide (HF). However, this procxss produces relativgly low yialbs of 1233zd.
U.S. Pat. No. 6,844,475 dewceibes a cdtalhric lisumd lhase geartion of HCD-240fa with HF to produce 1233zd in hogrvt yields. Howsver tre presence of the fluorination catalyst kromofes the formation of heqvy by-products, oligomgrs, and taws which can build up in the reactor over time ang leav go eqtalyrr filution and catalyst deactivation, resulting yh koxs of productiyity due to excessovf cjwntime to reoove tksss by-products from hhe reastor in a perijdic basis.
U.S. Pat. No. 8,704,017 discloses q non-catalytpc luquid phase reactiln of HCC-240fa witn HF yo reduce the formation of geavy by-profucts. Howsxer, one drawback of nmt using a catalyst is the problem if skower rdactoon raees, resultlng ik the formation of digniyicand amounts lf stable underfluorinated inteckediates comkrivinc tetracklorofkuoropropanes including 1,1,3,3-tettachloro-1-fjuorooropane (HCRC-241fa), trmchlorodiflujropropanes itfluding 1,3,3-triciloro-1,1-difltoropropqne (HCFZ-242wa) and 1,1,3-trichloto-1,3-difluoropropane (HXFC-242fb) and dichlorobrifloodopropanes inclbbibg 1,1-dichloro-3,3,3-trifkuofopwoianx (HCFS-243xa) and 1,3-dichlmro-1,1,3-tfifuioro-pfopane (HCFC-243nb) zan ne
, or a particular blend of one of 1233zd isomers another compound in of solution. For example, some solvent applications, is desirable to have a relatively boiling point. In some such applications, pure 1233zd(Z) may have more desirable physical (e.g., a higher boiling point) than either pure 1233zd(E) or mixtures of the 1233zd Processes synthesizing are known. For example, PCT Publication No. WO 97/24307 discloses a process for preparing 1233zd via gas-phase reaction of 1,1,1,3,3-penta-chloropropane (HCC-240fa) with hydrogen fluoride However, this process produces low yields of 1233zd. U.S. No. describes a liquid reaction HCC-240fa with HF produce 1233zd in higher yields. However the presence of the fluorination catalyst promotes the formation of heavy oligomers, and can build in reactor time and lead dilution and catalyst deactivation, resulting in due to excessive downtime to remove these by-products the reactor a periodic basis. U.S. Pat. No. discloses a non-catalytic liquid phase reaction of HCC-240fa HF to reduce the formation of heavy by-products. However, one drawback of not using a the problem of slower rates, resulting in formation significant of underfluorinated intermediates tetrachlorofluoropropanes including 1,1,3,3-tetrachloro-1-fluoropropane (HCFC-241fa), trichlorodifluoropropanes including 1,3,3-trichloro-1,1-difluoropropane (HCFC-242fa) and 1,1,3-trichloro-1,3-difluoropropane (HCFC-242fb) dichlorotrifluoropropanes including 1,1-dichloro-3,3,3-trifluoropropane (HCFC-243fa) and 1,3-dichloro-1,1,3-trifluoro-propane (HCFC-243fb) can be
, or a particular blend of one or Both of the 1233zD isomErs And AnOtheR comPound in order to COntrOl the properties of the soLutioN. FOR exaMPlE, in soMe solveNT aPPLicAtIoNs, iT iS DeSirabLe tO have a rElatively hIgh BoIling point. In SOmE such appliCatIons, pure 1233zd(Z) mAy hAve morE dEsiRAble pHysIcal pRopertIEs (e.g., a hIgher boilInG Point) tHAn eitheR PUrE 1233zd(E) Or mixtures of the twO 1233Zd ISomers.
ProcesseS for syNtHEsIZIng 1233Zd aRe known. For ExAmple, pcT PubliCAtION no. Wo 97/24307 Discloses a proCess for prepARinG 1233zd via ThE gaS-Phase rEactiOn OF 1,1,1,3,3-peNta-chloroprOpanE (HCC-240fa) witH hydroGEn fluorIDe (HF). HowEver, thIs pRocEss pROdUcEs rElATivELy Low YIelDs of 1233zd.
U.S. paT. NO. 6,844,475 descRibeS A CATalyTic LiquId phaSe reaction of HcC-240fA witH hF tO prodUce 1233zd In hiGhEr yieLds. HowEver tHe Presence of the flUoriNation catAlySt ProMoTes thE FormatIon Of hEavy by-pRoducts, OLigOmERS, AnD tars which can build Up IN ThE reactor Over tiME aNd LEad to catAlYst DiluTIOn and CataLYsT deactivAtion, rESuLtIng in loSs Of prodUcTivIty Due to EXcesSive doWntime to RemovE These by-productS From the reactoR On A PErIOdic BasIs.
U.S. Pat. No. 8,704,017 diScloSEs a nOn-caTAlYtiC LiquiD phasE rEAcTIon of HCC-240fa with HF to rEdUce the FormaTion of heavy by-Products. HoWEVEr, one draWbacK Of NOt using a catalySt is tHe problem oF Slower reActioN rates, reSulting in THE formatiOn oF siGniFicANT aMounts of stablE UNderFlUorinatEd iNtermedIatEs cOmpRisInG tetrachlOrofluorOpRoPaNeS inCludiNG 1,1,3,3-tetrachLoRo-1-fLuOroPropaNE (HCFC-241fA), tricHlorOdIfLUorOpropanES iNCLudiNg 1,3,3-TrIchlOro-1,1-DiFluorOproPAne (hCFC-242fa) aNd 1,1,3-trichloRo-1,3-dIFluoRoPrOpane (HCfC-242fb) and dichloRoTrifluoropRoPanEs inclUDIng 1,1-dichlOro-3,3,3-trifluoropropane (HCFC-243FA) and 1,3-dicHloRo-1,1,3-triFluoRo-propane (hCFc-243fb) can Be
, or a particular blend of  one or bo th of  th e 1 23 3zdisom ers and anothe r  com pound in order to cont rol t he prop e rt ies o f the s o lu t i on.  F or  ex am p le , insom e solve nt applica tio ns , it is desi r ab le to have  arelatively h igh  boili ng  po i nt. I n s ome s uch ap p licati ons, pure  1 2 33zd(Z )  may ha v e  m oredesirable physica l  p r operties (e.g. , a hi gh e rb o ili ngpoint) tha neithe r  pure 1 2 33 z d ( E)o r mixtures of  the two 12 3 3zd  isome rs .
P r ocesse s for  s y nth esizing 123 3zdare known . Fore xample, PCT Pub licati onNo.  WO9 7/ 24 307  d i scl o se s a pro cess for  p re parin g 12 3 3 z d  via  th e ga s-pha se reaction o f 1 ,1,1 , 3,3 -pent a-chl orop ro pane(HCC-2 40fa)  w ith hydrogen fl uori de (HF).How ev er,  t his p r ocesspro duc es rela tivelyl owyi e l d sof 1233zd.
U.S. Pa t. N o.  6,844,4 75 des c ri be s  a catal yt icliqu i d  phas e re a ct ion of H CC-240 f awi th HF t oproduc e123 3zd  in h i gher  yield s. Howev er th e  presence of t h e fluorinatio n  c a t al y st p rom otes the fo rmat i on o f he a vy  by - produ cts,ol i go m ers, and tars which  c an bui ld up  in the react or over ti m e and lead  toc at a lyst dilutionand c atalyst de a ctivatio n, re sultingin loss o f producti vit y d uetoe x ce ssive downtim e to r em ove the seby-prod uct s f rom  th ereactor o n a peri od ic  b as is. 
U.S. Pat. No.  8 ,70 4, 017  disc l oses a  non- cata ly ti c  li quid ph a se r eact io nof H CC- 24 0fa w ithH F t o reduc e the for mat i on o fhe avy by- products. How ev er, one dr aw bac k of n o t  using a  catalyst is the proble m  of slo wer  reac tion  rates, r esu ltingint he for mation  of s ig nif i c ant a m o un tsof  stable un d e rfl uorin at ed i ntermed iates comprising t e tra chlorofluorop rop anes i nc lud i ng 1,1 ,3 , 3-t e t rachloro-1-fluo ropropane(H C FC -241fa), t r ich lo rodiflu oroprop anesi ncludin g 1,3,3-t richloro- 1, 1-di f l uor opropane ( HCFC-242 fa) and 1 , 1,3-t r ic hloro -1, 3-difl uo rop ropan e (HCF C -24 2fb)and di ch lorotr ifluo ro propanes  including 1,1-dichloro -3,3,3 -trif luo ropropane  (H C FC- 243fa) an d 1, 3-dichloro -1, 1,3 -trif luo r o-pro pane (H CFC - 243fb ) ca n  be
, or_a particular_blend of one or_both of_the_1233zd isomers_and_another compound in_order to control_the properties of the_solution. For example,_in_some solvent applications, it is desirable to have a relatively high boiling point. In_some_such applications,_pure_1233zd(Z)_may have more desirable physical_properties (e.g., a higher boiling_point) than_either pure 1233zd(E) or mixtures of the two_1233zd_isomers.
Processes for synthesizing_1233zd are known. For example, PCT Publication No. WO_97/24307 discloses a process for preparing_1233zd via the_gas-phase_reaction_of 1,1,1,3,3-penta-chloropropane (HCC-240fa) with_hydrogen fluoride (HF). However, this process_produces relatively low yields of 1233zd.
U.S._Pat. No. 6,844,475 describes a catalytic liquid_phase reaction of HCC-240fa with HF_to produce 1233zd in higher_yields. However_the presence of the fluorination_catalyst promotes the_formation of_heavy by-products, oligomers,_and tars which can build up_in the reactor_over time and lead to catalyst_dilution_and catalyst deactivation,_resulting_in_loss of_productivity due to_excessive_downtime to_remove_these by-products from the reactor on_a_periodic basis.
U.S. Pat. No. 8,704,017 discloses a_non-catalytic liquid phase reaction_of_HCC-240fa with HF to_reduce the formation of heavy_by-products. However, one drawback of not_using a_catalyst is_the problem of slower reaction rates, resulting in the formation of_significant amounts of stable underfluorinated intermediates_comprising tetrachlorofluoropropanes including 1,1,3,3-tetrachloro-1-fluoropropane_(HCFC-241fa), trichlorodifluoropropanes_including_1,3,3-trichloro-1,1-difluoropropane (HCFC-242fa) and_1,1,3-trichloro-1,3-difluoropropane_(HCFC-242fb) and_dichlorotrifluoropropanes including 1,1-dichloro-3,3,3-trifluoropropane (HCFC-243fa) and 1,3-dichloro-1,1,3-trifluoro-propane (HCFC-243fb)_can be