M.S.

no abstract provided by author / Ph. D.

This investigation was conducted to provide laboratory scale equipment that will facilitate an accurate study of the affect of ultrasonic energy on mass transfer in two-phase multiple-component liquid systems. A liquid-liquid extractor incorporating an ultrasonic generator and transducer was designed and constructed to the following specifications: (1) insonation frequency of 400 kilocycles per second, (2) insonation intensities equivalent to plate currents of 0 to 200 milliamperes, and (3) flow rate of solvent and feed through the reactor ranging approximately from one-half to 24 pounds per minute, in varying solvent-to-feed ratios. A special glass reactor, or contactor, was constructed from a standard, 60° pyrexx glass funnel and fitted with an acoustical window of 0.001-inch sheet nickel. Photographic studies were made of the two-phase mixing taking place inside the reactor in both the presence and absence of ultrasonic insonation. An all metal reactor, of the same general design as the glass reactor, was constructed for use with the extractor when investigations were to be made that would involve high pressures or sudden liquid surges through the reactor. An evaluation of the extractor was conducted employing the system moetons-water-1,1,2-trichloroethane. Stage efficiencies calculated for the individual tests, eleven in all, varied from 94.3 to 110.0 percent. An observed yellow color in the extract samples, probably due to dissolved impurities in the 1,1,2-trichloroethane, could have been responsible for the observation of refractive index readings that did not give true representation of the acetone concentration of the sample. Cavitation was observed in the reactor which the test system was undergoing ultrasonic insonation. The gross stirring effects resulting from cavitation in the liquids caused a mixing of the two phases that was more intense than that taking place in the reactor without insonation. / Master of Science

It was the purpose of this investigation, using the ternary system acetone-toluene-water in the extraction of acetone from toluene using distilled water, to determine the operating characteristics of a pulse extraction column, and to determine the effects of solvent-to-feed ratio, feed concentration, and pulse amplitude on the overall mass transfer coefficient. The equipment used was operated at a temperature of 25±1 ºC, and consisted of a two-inch diameter glass column with eight sieve plates having 1/16-inch diameter holes on triangular centers, and a plate-free area of twenty-three per cent. The plate spacing used was eight inches. Pulsation of the liquids in the column was accomplished by means of a brass bellows actuated by a push rod driven by a motor-driven cam. The determination of the column operating characteristics resulted in curves defining the operating flow rates at which the column could be operated without light- or heavy-phase flooding. The shape of the curves was a function of the feed and solvent flow rates, but was independent of the pulse amplitude. Using flow rates taken from the column operating characteristic curves, a total or forty-five tests were made to determine the effect or pulse amplitude, feed concentration, and the solvent-to-feed ratio on the overall mass transfer coefficient. It was found that the overall mass transfer coefficient was the highest at a volumetric solvent-to-feed ratio of 0.50 for conditions of blowing, reached a minimum at a volumetric solvent-to-reed ratio of 1.00 at which there was no blowing or dumping, and increased slightly at a volumetric solvent-to-feed ratio or 1.50 at which dumping occurred. The overall mass transfer coefficient increased with increased feed concentration in a straight-line relationship. The overall mass transfer coefficient was also increased by an increase in the pulse amplitude. / Master of Science

The purpose of this investigation was to determine the effect of a homologous series of solutes on the overall mass-transfer coefficients for liquid-liquid extraction. The solutes used were ethylene glycol dimethyl ether, diethylene glycol dimethyl ether, triethylene glycol dimethyl ether, and tetraethylene glycol dimethyl ether. The carrier solvent was water, and the extracting solvent was toluene. The phase diagrams for these systems were determined at 30 °C. The phase diagrams were found to be similar and to have maximum solubilities ranging from 69.9 to 76.7 weight per cent of solute.. Three of the systems exhibited solutropes, and the system containing tetraethylene glycol dimethyl ether approached a solutrope at a solute concentration of approximately 64 per cent. A countercurrent-flow, 1-1/2-inch diameter, horizontal, pyrex glass tube, eight feet long with an interfacial surface area of one square foot, was used for the extraction tests. The feed concentration ranged from 9.10 to 15.18 weight per cent of solute in water. The flow rates of the water phase varied from 15.20 to 34.72 pounds per hour, and the solvent phase flow rates varied from 18.86 to 33.83 pounds per hour. The overall mass-transfer coefficients based on the water phase were found to vary between 0.0098 and 0.0133, 0.0036 and 0.0051, 0.0035 and 0.0063, and 0.0023 and 0.0063, for the systems investigated. The solvent phase coefficients were found to vary between 0.0097 and 0.0149, 0.0057 and 0.0079, 0.0092 and 0.0172, and 0.0087 and 0.0237. The overall coefficients were not affected appreciably by changing the molecular weight of the solute. Also, experimentally determined values of the overall coefficients based on the solvent phase did not agree with those values of the coefficients calculated by previously determined equations. / Master of Science

In the preparation of tannin extract from chestnut wood chips there is present in the extract, along with the tannin, certain insoluble non-tannin constituents. If allowed to remain in the extract, these materials make the tanning solution unsuitable for use in the manufacture of leather. To accomplish the separation of the non-tannin constituents from the tannin, the Lead Corporation of Lynchburg, Virginia, now employs a process of concentration and mechanical settling. For the past twenty years the company has been engaged in research to develop a better process. The investigations have been concentrated mainly on the idea of varied forms of mechanical separation. So far no solution to the problem has been found, thereby giving rise to the opinion that perhaps mechanical separation is the wrong approach to the problem. In a preliminary study of this problem 6), research work has been done at V.P.I. using several new approaches, the most important of these being electrophoresis and adsorption. Of these two procedures, adsorption save indications of having the greater potentialities. The following thesis will deal with additional research work using coals of varying grades as an adsorbing medium. The American Viscose Company of Roanoke, Virginia has installed units for clarifying the spinning bath solutions. The units incorporate coal as an adsorbing medium. The process is extremely successful and therefore strengthens the belief that it may be applicable to the clarification of tannin extract solutions. Adsorption methods are often applied industrially to remove impurities, especially if they are present in low concentrations. Small amounts of impurities often interfere with processes such as crystallization, filtration, and distillation, but by the application of adsorption the impurities may be separated and the fault corrected. Often times adsorbents are used to recover valuable constituents, which otherwise would be lost completely or require for more costly processing. Separation by adsorption is made possible because of the fact that different materials differ in the degree to which they are adsorbed by a given adsorbent. The object of the research work is to investigate the possibility of developing an economically feasible process, based on adsorption, using coal as the adsorbent, for the separation of the insoluble non-tannin constituents present in a fresh tannin extract. / Master of Science

Solvent extraction, as a chemical engineering method, has been the subject of a great deal of research during the past quarter century. The analogy between this operation and the other diffusional processes, distillation and gas absorption has long been recognized; common theoretical foundations have been found for all three processes. In each case mass is transferred from one fluid phase to another across an interface. Recent progress in the field of extraction has been in the direction of determining the quantitative data for the design of equipment in expanding and improving such industrial applications as have already been made, and in developing new modifications of the basic process of simple liquid extractions. Among these developments is that of fractional liquid extraction. The process of fractional liquid extraction is analogous to that of fractional distillation in that the components to be separated are distributed unequally between two fluid phases. In the case of fractional extraction the two phases concerned are the two solvents, and the components to be separated are distributed between these two phases in a manner which is dependent on their relative solubility in the solvents chosen. Somewhat better separation than that attainable by distillation is theoretically possible by fractional extraction in that two solvents are chosen, each of which has a preferential effect on certain components of the mixture to be separated. Yet even in the case of fractional extraction, the possibilities of economy inherent in the thermodynamic advantages of extraction over distillation apparently are not completely attained. The difficulty seems to be one of obtaining better contact between the two phases involved in this and other methods of extraction. The problem of securing intimate and continuous contact between the solvents and feeds involved is one that has greatly vexed the designers of extraction equipment, as evidenced by the numerous patents that have been obtained on ingenious designs. Many different combinations of sprays and baffles, with and without packing, have been developed, the former to produce the necessary dispersion of one liquid within another, and the latter to maintain this dispersed phase in contact with the continuous phase that constitutes the main body of liquid within the equipment. The question of interfacial tension between the two phases is intimately related to the question of contact in that it vitally affects the production and maintenance of the dispersed phase. The effect is mentioned qualitatively in the literature, but little data on the relationship of surface tension to extraction efficiency are found. It was the purpose of this investigation to study the effect of a wetting agent, sodium lauryl sulfate, on the efficiency of the fractional liquid extraction of a mixture of ethanol and ethanol and isopropanol with benzene and water. / Master of Science

It was the purpose of this investigation to ascertain the qualitative nature of the interracial tension equilibrium characteristics of the systems hexane-acetone-water and toluene-acetone-water by studying the effect of drop velocity on drop weight through use of the modified drop weight procedure, and comparing these results with those obtained from systems known to have time dependent interfacial tension relationships; to then evaluate the effect of interfacial tension on the rate or mass transfer by obtaining extraction data for the above systems in a horizontal, countercurrent liquid-liquid extraction tube for a series of interfacial tension values achieved through variation of the total acetone concentration in the system; and finally, to attempt to obtain an equation correlating the overall mass transfer coefficient based on the solvent film with the physical and operational variables of the systems and extractor. The observation that some three component, ternary systems containing high molecular weight solutes required time to reach interfacial tension equilibrium, prompted a more careful consideration of the assumption that determinations or this property obtained under static conditions represented the values existing under extracting conditions. The drop weight method was selected for comparison studies. An equation relating drop weight to drop velocity was derived, and took the form: m = 2πrσØ/g - Aρv²/g where: m = drop weight, gm 2, π = constants r = tip radius, cm σ = interfacial tension, dynes/cm g = acceleration due to gravity, cm A = cross sectional area of capillary tube, sq cm ρ = density of fluid flowing in capillary, gm/cu cm v = drop velocity, drops/min Ø = correction factor for non-ideal drop detachment from tip. The equation predicted that if (σ') and (Ø) were constants, a plot or drop weight (m) versus the square or the drop velocity (v²) would result in a straight line. The systems used to test the validity of the above equation were arabic acid and acetone as solutes with each of the following liquid pairs: benzene-water, cyclohexane-water, and toluene-water. From this study, it was concluded that 1. Adjustment of interfacial tension for the systems acetone in toluene, benzene, or cyclohexane with water was so rapid that equilibrium was reached as quickly as the drops could be formed. 2. The interfacial tension values of systems containing solutes having a molecular weight of 50 to 60 measured by equilibrium methods will be representative of the interfacial tension values for the systems under extracting conditions. 3. Equilibrium methods are not suitable for evaluating interfacial tension under extracting conditions for solutes having a molecular weight on the same order of magnitude as that for arabic acid. 4. The experimental method used in this investigation failed to show any transient values of interfacial tension less than the equilibrium values as postulated by Christiansen and Hixon. Extraction tests were made on the systems toluene-acetone-water and hexane-acetone-water at 25 to 29 °C, in an effort to determine the effect of interfacial tension on the overall mass transfer coefficient. Phase flow rates covered a range of 1,000 to 10,000 pounds per hour per square foot for both phases. Concentration ranged from 35 to 5 weight per cent acetone in the inlet water stream, and 20 to zero weight per cent acetone in the inlet toluene stream. For the hexane system. the concentrations varied from 45 to 15 weight per cent in acetone in the inlet water phase, and 5 to zero per cent acetone in the inlet hexane phase. The results of this study led to the following conclusions: 1. The overall mass transfer coefficient for acetone from water to hexane based on the hexane film, increased from 0.012 to 0.060 with an increase in interfacial tension from 7.6 to 24.0 dynes per centimeter, as controlled by decreasing acetone concentration. 2. The overall mass transfer coefficient for acetone from water to toluene based on the toluene film, decreased from 0.145 to 0.048 with an increase in interfacial tension from 6.6 to 22.5 dynes per centimeter, as controlled by decreasing acetone concentration. 3. Because of the opposite effect of interfacial tension on transfer of acetone from water to hexane and to toluene, no generalization as to the effect of interfacial tension on the overall mass transfer coefficient could be made. 4. The mass transfer coefficient for acetone to toluene was 0.1 to 0.025 ot the transfer coefficient for acetone from water to toluene. 5. The overall mass transfer coefficient based on the solvent phase concentrations can be correlated with 67 percent accuracy with the physical properties of the system by the equation: K_sd/D_s = 2.708 x 10⁻²¹(dσ/μ_sD_s)^0.7227(μ_w/μ_s)^4.0592(μ_s/ρ_sD_s)^5.4361(dG_s/μ_s)^0.4701(dG_w/μ_w)^0.3027 where: K_s = overall mass transfer coefficient based on solvent phase, lb/hr- sq ft-ΔC d = diameter of horizontal extraction tube, ft D_s = diffusivity of solute in solvent, sq ft/hr σ = interfacial tension, lb/hr² ρ_s = density of solvent phase, lb/cu ft μ_w, μ_s = viscosity of water and solvent phases, respectively, lb/ft-hr G_w, G_s = mass velocity of water and solvent phases, respectively, lb/hr-sq ft. 6. Equations correlating the individual film coefficients with physical properties of the system derived from binary extraction studies could not be used to predict ternary overall mass transfer coefficients. / Ph. D.

The purpose of this investigation was to redesign, construct, and operate a two-inch experimental pulse liquid-liquid extractor, and to determine the effects of the pulse amplitude, the number of plates, and the plate-free-area on the stage efficiency of the column. The optimum liquid flow rates were also determined. An examination of the literature was conducted for a review of the available information on pulse extractors. Although a great deal of literature was available on the topic of liquid-liquid extraction, detailed information on only two pulse extractors could be found. The results obtained during this investigation compare favorably with those reported in the literature. A two-inch experimental pulse-type extractor was constructed. The liquids were pulsed by means of a sylphon-type bellows operated by a push rod which was driven by an eccentric cam. For the satisfactory operation of the extractor various auxiliary apparatus was required; important among these were the supporting framework, the push-rod bearing, the reduction train for the can, the storage tanks, and the tubing and fittings. Twenty-seven individual experimental tests were conducted, extracting acetone from carbon tetrachloride with water, to determine the effects of the various operating parameters on the stage efficiency of the pulse column. During the experimental tests the following variables were studied: pulse amplitude at one, two, and three inches of vertical liquid displacement; number of plates with four, eight, and twelve plates; and plate-free-area with eight, sixteen, and thirty-two per cent free area. It was found that the pulse amplitude, the number of plates, and the plate-free-area each have an independent significant effect on the stage efficiency of the pulse column; the plate-free-area has the largest relative effect, while the pulse amplitude has the smallest relative effect. It was further proven by this investigation that the interactions between the pulse amplitude and number of plates, the pulse amplitude and plate-free-area, and the number of plates and plate-free-area have no significant effect on the stage efficiency of the pulse column. The flow rates for satisfactory column operation are 1807, 2211, 1478, and 2299 pounds per hour-square foot of column cross-section for the feed, solvent, raffinate, and extract, respectively. / Master of Science

Dissertation (PhD(Eng))--University of Stellenbosch, 2001. / ENGLISH ABSTRACT: Coal pyrolysis liquors are a major source of phenolic compounds. The separation of the phenolic compounds from the neutral oils and nitrogen bases also present in the pyrolysis liquors is difficult due to low relative volatilities and the formation of azeotropes. The desired phenolic recovery and phenolic product purity of 99.5 % can therefore not be achieved by means of conventional separation processes. Alternative processes such as liquid-liquid extraction with various low-boiling solvents, mixtures of high-boiling solvents and extractive distillation have been investigated. Disadvantages of these processes include the high solvent ratios required, low recovery of the higher substituted phenolic compounds, inability to treat a wide-boiling feedstock in one process step and complex post-purification of the phenolic product. A solvent system consisting of a selective solvent, water as a co-solvent, and hexane as a countersolvent, is proposed. An industrial heavy naphtha stream was analysed and the most prevalent phenolic compounds, neutral oils and nitrogen bases identified. Three synthetic feed streams were compiled to represent the industrial stream, namely: 1. phenol + benzonitrile + aniline + mesitylene + 5-et-2-me-pyridine 2. m-cresol + o-tolunitrile + o-toluidine + pseudocumene + undecane + indene 3. 2,4-xylenol + 3,5-xylenol + 3,4-xylenol + indane + dodecane + naphthalene The stream containing phenol was used as a basis for solvent selection, with emphasis on the separation of phenol from benzonitrile. A variety of molecules containing hydroxyl and ether functional groups were identified as potential solvents by means of computer-aided molecular design using a genetic algorithm. Of the commercially available solvents tested on batch extraction scale, triethylene glycol achieved the highest phenol-benzonitrile, phenol-aniline and phenol-5-et-2-me-pyridine separation factors as well as the highest phenol recovery. It was concluded from the solvent selection process that effective solvents for the problem under investigation were those containing hydroxyl groups positioned on the molecule backbone in such a way as to facilitate hydrogen bonding with more than one phenolic molecule at a time. Two commercially unavailable solvents, 1,3-(ethoxy-2- hydroxy)-propane-2-01 and 1,3-(diethoxy-4-hydroxy)-propane-2-01 were therefore synthesised from ethylene glycol and diethylene glycol respectively. The molecular structures of these two solvents are analogous to that of triethylene glycol, and contain an additional hydroxyl group. The performance of the synthesised solvents was evaluated and compared to that of triethylene glycol on the basis of m-cresol-otolunitrile, 2,4-xylenol - o-tolunitrile, and 2,4-xylenol - o-toluidine separation factors and phenolic recoveries achieved by means of batch extraction tests. 1,3-(Diethoxy-4- hydroxy)-propane-2-01 yielded higher phenolic recoveries, but lower separation factors than did triethylene glycol. Triethylene glycol was therefore selected for further process development as it is commercially available. A series of batch extractions were carried out on each of the synthetic feed streams using the proposed solvent system. For phenol and m-cresol, recoveries in excess of 99% were obtained in a single stage. Recoveries in excess of 98% were obtained for the xylenol isomers. It was found that the recoveries of the xylenol isomers were more sensitive to changes in the solvent ratios. The separation of phenolic compounds from paraffins, naphthalene, indene, indane and the alkyl-substituted benzenes was trivial using the proposed solvent system. Highly satisfactory separation of the phenolic compounds from pyridines and aromatic nitriles was achieved. The separation of phenol from aniline, although satisfactory, was not as good. The optimum solvent to feed, water to solvent and hexane to feed ratios were identified as being 3.0, 5.0 and 0.25 respectively. Binary interaction parameters for the NRTL equation were obtained by regression of the equilibrium data from the batch extraction tests. The NRTL model fitted the equilibrium data satisfactorily. The proposed solvent system was tested on pilot plant scale. The performance of the extraction column was optimised using a synthetic feed stream consisting of m-cresol, p-cresol, aniline and o-tolunitrile. The optimum solvent ratios and operating parameters were then implemented in further tests on an industrial heavy naphtha stream. A phenolic product purity of 99.75% was achieved for this stream. The corresponding phenolic recovery was in excess of 91 %. The proposed separation process, including solvent recovery was simulated using the NRTL model with the experimentally determined interaction parameters. A single stream consisting of all the components used in the batch extraction tests was specified as the feed stream to the simulated process. A final simulated phenolic product purity of 99.5% and recovery in excess of 94% was obtained after solvent recovery. The optimum solvent to feed, hexane to feed and water to solvent ratios were determined as being 3.0, 5.0 and 0.25 in both the pilot plant tests and the simulated extraction process. It can be concluded that the proposed separation process is successful in recovering high purity phenolic compounds from tar liquors. Further development of the process has commenced in industry. / AFRIKAANSE OPSOMMING: Die pirolise van steenkool is 'n belangrike bron van fenoliese verbindings. Die skeiding van die fenoliese komponente vanuit die neutrale olies ook teenwoordig in die pirolise mengsel word bemoeilik deur lae relatiewe vlugtighede en die vorming van aseotrope. Dit is dus nie moontlik om die gewenste hoë fenoliese herwinning en fenoliese produk suiwerheid van 99.5% d.m.v. konvensionele distilleerprosesse te behaal nie. Alternatiewe prosesse soos ekstraktiewe distillasie en vloeistof-vloeistof ekstraksie met verskeie laagkokende oplosmiddels en mengsels van hoogkokende oplosmiddels is al ondersoek. Die hoë oplosmiddel verhoudings wat benodig word, lae herwinning van die hoërgesubstitueerde fenoliese verbindings, onvermoë om in een prosesstap 'n prosesstroom met In wye kookgebied te behandel en die ingewikkelde suiwering van die fenoliese produk tel onder die nadele van hierdie prosesse. 'n Oplosmiddelsisteem wat In selektiewe oplosmiddel, water as polêre oplosmiddel en heksaan as teenoplosmiddel bevat is as 'n alternatiewe proses voorgestel. 'n Industriële swaar nafta prosesstroom is ge-analiseer en die fenoliese verbindings, neutrale olies en stikstofbasisse met die hoogste konsentrasies daarin geïdentifiseer. Drie sintetiese strome is op grond van hierdie analise saamgestelom die industriële stroom te verteenwoordig: 1. fenol + benzonitriel + anilien + mesitileen + 5-et-2-me-piridien 2. m-kresol + o-tolunitriel +o-toluïdien + pseudokumeen + undekaan + indeen 3. 2,4-xilenol + 3,5-xilenol + 3,4-xilenol + indaan + dodekaan + naftaleen Die fenolbevattende stroom is as basis vir oplosmiddelkeuring gebruik, met die klem op die skeiding van fenol vanuit benzonitriel. Verskeie molekules wat hidroksie- en eter funksionele groepe bevat is as potensiële oplosmiddels uitgeken d.m.v. rekenaargesteunde molekulêre ontwerp met In genetiese algoritme. Hierdie oplosmiddels is d.m.v. enkellading ekstraksie toetse geëvalueer. Die kommersieel beskikbare oplosmiddel wat die hoogste fenol-benzonitriel, fenol-anilien en fenol-5-et-2-me-piridien skeidingsfaktore, sowel as die hoogste fenol herwinning op enkellading ekstraksie toetsvlak gelewer het, was triëtileenglikol. Vanuit die proses vir die keuse van 'n oplosmiddel was dit duidelik dat, vir hierdie skeidingsprobleem, die mees effektiewe oplosmiddels dié is met hidroksiel groepe wat so geposisioneer is in die oplosmiddel molekuul dat dit waterstofbindings kan vorm met meer as een fenoliese molekuul. Twee oplosmiddels wat nie kommersiëel beskikbaar is nie, 1,3-(etoksie-2-hidroksie)-propaan-2-01 en 1,3-(diëtoksie-4-hidroksie)-propaan-2- ol, is gesintetiseer vanuit etileenglikol en diëtileenglikol onderskeidelik. Die molekulêre strukture van hierdie twee oplosmiddels is analoog aan dié van triëtileenglikol en bevat 'n addisionele hidroksielgroep. Die effektiwiteit van die gesintetiseerde oplosmiddels is geëvalueer en met dié van triëtileenglikol vergelyk op grond van rn-kresol-o-tolunltriel, 2,4-xilenol - o-tolunitriel en 2,4-xilenol - o-toluïdien skeidingsfaktore en fenoliese herwinning behaal d.m.v. enkellading ekstraksie toetse. Hoër fenoliese herwinning en laer skeidingsfaktore is behaal met 1,3-(diëtoksie-4-hidroksie)-propaan-2-01as met triëtileenglikol. Triëtileenglikol is dus gekies vir verdere prosesontwikkeling aangesien dit kommersiëel beskikbaar is. Enkellading ekstraksie toetse is op elk van die sintetiese voerstrome uitgevoer met die voorgestelde oplosmiddelsisteem. Fenol- en m-kresol herwinning van meer as 99% en xilenol herwinning van meer as 98% is behaal. Die skeiding van fenoliese verbindings vanuit paraffiene, naftaleen, indeen, indaan en die alkielgesubstitueerde benseenverbindings is triviaal met die voorgestelde oplosmiddelsisteem. Hoogs aanvaarbare skeiding van fenoliese verbindings van die piridiene en aromatiese nitriele is vermag. Die skeiding van fenol en anilien is nie so goed nie, maar is nog steeds aanvaarbaar. Die optimum oplosmiddel tot voer, water tot oplosmiddel en heksaan tot voer is as 3.0, 5.0 en 0.25 vasgestel. Binêre interaksie parameters vir die NRTL vergelyking is verkry d.m.v. regressie van die ewewigsdata wat deur die enkelladingstoetse gegenereer is. Die NRTL model het die ewewigsdata goed gepas. Die voorgestelde oplosmiddelsisteem is op loodsaanlegvlak getoets. Die werking van die ekstraksie kolom is ge-optimeer met In sintetiese voerstroom wat uit m-kresol, pkresol, anilien en o-tolunitriel bestaan. Die optimum oplosmiddel verhoudings en bedryfstoestande is verder toegepas op 'n industriële swaar naftastroom. 'n Fenoliese suiwerheid van 99.75% is behaal met hierdie stroom. Die ooreenkomstige fenoliese herwinning was groter as 91%. Die voorgestelde skeidingsproses, insluitende oplosmiddelherwinning is gesimuleer met die NRTL model wat op die eksperimentele data gepas is. 'n Enkele stroom wat bestaan het uit al die komponente wat in die enkelladingstoetse gebruik is, is as die voerstroom tot die gesimuleerde proses gespesifiseer. 'n Finale gesimuleerde fenoliese produksuiwerheid van 99.5% en herwinning groter as 94% is na oplosmiddelherwinning behaal. Die optimum oplosmiddel tot voer, heksaan tot voer en water tot oplosmiddel verhoudings is vasgestel as 3.0, 5.0 en 0.25 onderskeidelik vir beide die gesimuleerde proses en die loodsaanleg toetse. Die voorgestelde skeidingsproses kan dus 'n hoogs suiwer fenoliese produk uit pirolisestrome herwin. Verdere ontwikkeling van die proses is in die industrie begin.