while this invention is susceptible of embodiment in many different forms , this specification and accompanying drawings disclose only some specific forms as an example of the use of the invention . the invention is not intended to be limited to the embodiments so described , and the scope of the invention will be pointed out in the appended claims . the apparatus of this invention is used with certain conventional components the details of which , although not fully illustrated or described , will be apparent to those having skill in the art and an understanding of the necessary functions of such components . more specifically with reference to fig1 the integrated system comprises one or more oxidizing vessel , such as oxidizing vessel 11 shown with means for agitating the liquid in the oxidation zone such as stirrer 17 if desired or needed by the particular design of oxidizing vessel 11 and the manner in which gas containing free oxygen such as air is introduced into the oxidation zone . to oxidize the three methyl groups to cooh groups the theoretical oxygen is 4 . 5 moles per mole of pseudocumene . the operation of the system is started by charging to oxidizing vessel 11 , the c 9 aromatic hydrocarbon through feed stock conduit 10 , solvent and catalyst through conduit 15 generally as a solution of a source of bromine such as an organic or inorganic bromide and a source of heavy metal oxidation catalyst such as a solution of a salt of the heavy metal in a small amount of water or acetic acid solvent or dissolved in the c 9 aromatic feed stock . acetic acid solvent recycle is withdrawn from vessel 168 through transfer line 170 by pump 171 discharging through conduit 172 into heater 173 and transfer line 174 . the acid may also be heated by coil 169 in vessel 168 . as shown in fig1 the ingredients that go to make up the liquid phase reaction mixture in the oxidation zone all flow into acetic acid recyle conduit 12 and thence into oxidizing vessel 11 . the liquid mixture can be passed through a preheater ( not shown ) before entering oxidizing vessel 11 and be heated to a temperature at which oxidation will at least be initiated or the liquid mixture can be heated to reaction temperature in oxidizing vessel by the means provided for adding external heat during the latter portion of the oxidation reaction . pressurized air is charged through conduit 16 into the liquid phase reaction mixture through the bottom of oxidizing vessel 11 . oxidation reaction effluent is withdrawn through valved conduit 28 , is discharged into reactor surge 31 through pressure reducer 29 and conduit 30 below the liquid level in reactor surge 31 . heat is given off during the oxidation causing boil - up of solvent and / or hydrocarbon . their vapors together with by - product water vapor leave the oxidation zone in admixture with nitrogen , unreacted oxygen and oxides of carbon . this gasiform mixture leaves oxidizing vessel 11 through conduct 18 , passes through cooler 19 and conduit 20 to liquid - gas separator 21 . condensate in separator 21 is returned to oxidizing vessel 11 through conduit 22 . the uncondensed gases and vapors are scrubbed in high pressure ( h . p .) absorber 24 with acetic acid to remove hydrocarbons , such as pseudocumene , which are recycled to feed mix preparation through transfer line 27 where it is combined with recycle acetic acid in vessel 168 . the uncondensed gases and vapors are then scrubbed with water in high pressure absorber 24 to remove acetic acid vapors and the scrubbed gases are vented by conduit 26 through a pressure control valve ( not shown ) to the atmosphere . the aqueous acetic acid from h . p . absorber 24 is sent to acetic acid concentration by conduits 29 and 50 . upon completion of the oxidation reaction , liquid effluent from the oxidation zone is discharged through valved conduit 28 , pressure reducer 29 and conduit 30 . reactor surge 31 can handle oxidation reaction effluent from one or more oxidizing vessels . advantage can be taken of the pressure of and the temperature of the liquid effluent to cool the oxidation reaction effluent by removal of sensible heat as before mentioned . this can be advantageously done by flashing solvent and water in reactor surge tank 31 . the resulting vapors exit through conduit 35 and are condensed by cooler 36 . the condensate flows through line 37 to liquid - vapor separator 38 and the liquid is withdrawn by valved conduit 45 - 46 and sent via conduit 50 to acetic acid concentration . any uncondensed gases and vapors are vented as is required through conduit 39 , pressure reducing valve 40 and line 39 into atmospheric absorber 41 . the aqueous acetic acid from the atmospheric absorber 41 is sent to acetic acid concentration by conduits 43 and 50 . scrubbed vapors are vented through line 44 . the amount of solvent , wet acetic acid , flashed off in surge tank 31 will depend on the temperature and pressure of the liquid effluent removed from oxidizing vessel 11 . the cooled and depressurized mixture in reactor surge 31 flows therefrom through valved conduit 60 to batch crystallizer 61 operated at reduced pressure , as before disclosed , imposed therein by any means ; e . g ., vacuum jet 72 through conduit 71 connected to the vapor space in liquid - gas separator 67 which receives condensate and vapors from crystallizer 61 through conduit 64 , cooler 65 and conduit 66 . condensate from separator 67 can be withdrawn by pump 76 , conduit 68 and valved conduit 70 for solvent concentration . crystallizer 61 has a stirrer or agitator 62 to keep in suspension the crystallized trimellitic acid . separation of the solid phase ( crystallized trimellitic acid ) from the liquid phase ( acetic acid mother liquor ) can be accomplished by the use of any device for accomplishing such a phase separation . for example , the phase separation can be carried out by decantation , filtration or centrifugation . centrifugal filters , filter presses or vacuum rotary filters can be employed for recovering the crystallized trimellitic acid from the mother liquor . the slurry of trimellitic acid crystals is withdrawn from crystallizer 61 through conduit 78 discharging into solid - liquid separator 80 to obtain a trimellitic acid crystal cake . mother liquor is collected through conduit 81 in mother liquor surge 82 shown on fig2 . wet cake is discharged through transfer line 100 to acid product dehydrator 200 shown in fig3 . transfer line 100 is preferably a screw conveyor although belt or scoop conveyors can also be used in this service . fig2 illustrates the portion of the integrated system for processing acetic acid . here the mother liquor from recovery of solid trimellitic acid collected in mother liquor surge 82 is charged through conduit 84 by pump 85 and conduit 86 into mother liquor stripper 90 . the stripper feed contains trimellitic acid and aromatic co - products and by - products as before described . a mixture of water and acetic acid vapors is removed from the top of mother liquor stripper 90 by vapor transfer conduit 93 and charged directly into acetic acid dehydration tower 140 . water vapor with a small amount of acetic acid vapor and any pseudocumene present comes off as overhead through vapor line 145 through cooler 146 and condensate line 147 to separator 148 where hydrocarbon is drawn off via line 149 when need be . a part of the water condensate is returned as reflux as shown . acetic acid of 93 to 98 % by weight is withdrawn from the bottom of acetic acid dehydrating tower 140 through conduit 141 , cooled by heat exchanger 160 and collected in acetic acid storage tank 162 . makeup acetic acid is charged to tank 162 through line 163 . acetic acid for charging oxidizing vessel 11 is withdrawn by pump 164 discharging into conduit 165 . recycle acetic acid is used as reflux for the mother liquor stripper . liquid from the bottom of stripper 90 flows through transfer lines 94 and 95 to boiler 96 . liquid - gas effluent from boiler 96 is charged to the bottom of stripper 90 . the stripper bottoms liquid is withdrawn through transfer line 104 by pump 105 discharging though line 106 into stripper stillpot vessel 107 heated , for example by coil 108 . vapor from the stripper stillpot 107 flows into stripper 90 through vapor transfer line 98 . a bottom fraction from distillation of crude trimellitic anhydride product , shown on fig3 flows into the stripper stillpot 107 through conduit 227 and the bottom fraction is admixed with the liquid in the stripper stillpot 107 forming a residue having high melting solids and catalyst metals . the residue is withdrawn from the stripper stillpot 107 through transfer line 109 ( heat traced ) by pump 110 discharging through heat traced line 111 . a fraction of the residue flows to waste disposal through conduit 112 and a fraction of the residue flows to the first acid product dehydrator 200 , shown on fig3 through conduit 114 , flow controller 115 and transfer line 116 . now turning to fig3 the wet cake from solid - liquid separator 80 is fed through transfer line 100 to hopper 202 and thence by screw feed 203 into first acid product dehydrator 200 that contains a molten crude anhydride . the wet cake charged to the molten liquid in acid product dehydrator 200 heated as by means of internal coil 204 or other heat exchanger in which , for a source of heat , can be any fluid remaining liquid , the temperature employed to dehydrate trimellitic acid to its anhydride . advantageously , liquids are fed to internal coil 204 at about 600 ° to 700 ° f . such materials as diphenyl oxide , chlorinated biphenyls , and chlorinated terphenyls which are fluids at 400 ° to 700 ° f . can be employed as heat transfer media . as the wet cake is introduced into dehydrator 200 , the adhering acetic acid and water of dehydration flash off and are withdrawn as vapors through conduit 205 to mother liquor surge vessel 82 . residue from the stripper stillpot is added to the first dehydrator 200 through line 116 . the thermal dehydration of trimellitic acid to its anhydride in the first acid product dehydrator 200 is conducted at about atmospheric pressure . effluent from the first acid product dehydration 200 flows into the second acid product dehydration 210 through valved transfer line 206 . the second dehydrator 210 operates at a pressure below atmospheric , preferably at a pressure less than about 550 mm . hg absolute , which pressure is maintained by vacuum jet 215 . the pool of liquid is heated by coil 211 or an external heat exchanger , similar to the first dehydrator 200 . after dehydration , the crude trimellitic anhydride product is processed to obtain a product having a high anhydride content , 97 % or above by withdrawing a portion of the liquid from acid product dehydrator 210 through valved conduit 217 to anhydride distillation 220 supplied by heat for example by vaporizer 218 . trimellitic acid anhydride is distilled using as reflux liquid trimellitic anhydride product through conduit 237 . the anhydride vapors are transferred by conduit 221 through vapor cooler 228 and conduit 229 that discharges into liquid anhydride product receiver 230 . light ends are removed from liquid anhydride product receiver 230 through conduit 231 by steam jet 234 . liquid anhydride product is withdrawn from liquid anhydride product receiver 230 through transfer line 235 by pump 236 and discharged through transfer line 238 into flaker 239 where the liquid anhydride product is finally cooled and flaked . the flaked product is discharged down chute 240 to storage or packaging . the bottoms from the anhydride distillation tower flow through conduit 222 to evaporator 223 , for example a kontro thin film evaporator , trimellitic anhydride vapors return to tower 220 through conduit 224 . concentrated bottoms containing catalyst metals and high boiling compounds are transferred to the stripper stillpot 107 through conduits 225 and 227 by pump 226 .