Neopentyyliglykolin ja propionihapon välisen esteröintireaktion kinetiikka

Glykolien esterit ovat haluttuja pintareaktiivisia aineita. Niitä voidaan valmistaa esteröintireaktiolla karboksyylihappojen kanssa katalyytin läsnä ollessa, jolloin toivottu reaktiotuote on yleensä muodostuva monoesteri. Monoesterin saannon lisäämiseksi reaktiossa muodostuvaa vettä voidaan poistaa jatkuvasti reaktiosta. Reaktion tasapainotilan tutkiminen on kuitenkin tärkeää, jotta reaktion kinetiikka tunnettaisiin mahdollisimman hyvin. Tällöin reaktiotuotteita ei poisteta reaktioseoksesta reaktion aikana. Glykolit esteröityvät happojen kanssa kahdessa vaiheessa. Ensimmäisessä vaiheessa muodostuu monoesteriä ja vettä ja toisessa vaiheessa diesteriä ja vettä. Kokeiden perusteella ensimmäinen vaihe on selvästi toista vaihetta nopeampi reaktio. Kirjallisuudessa on esitetty myös kaksi sivureaktiota, transesteröityminen ja disproportionaatio. Reaktion kinetiikka voidaan kuvata ilman näitä pieniä sivureaktiota, mutta täydellisen kuvaamisen vuoksi on ne myös otettava huomioon. Reaktion kinetiikan tutkimiseksi suoritettiin viisi laboratoriokoetta eri lämpötiloissa neopentyyliglykolilla ja propionihapolla homogeenisen para-tolueenisulfonihapon toimiessa katalyyttina. Lähtöaineiden ja tuotteiden konsentraatioita seurattiin ajan funktiona ja saatujen tulosten perusteella sovitettiin reaktiomekanismin differentiaaliyhtälöiden reaktionopeusvakiot. Nopeusvakioiden lämpötilariippuvuutta tutkittiin Arrheniuksen yhtälön avulla. Lisäksi määritettiin tasapainovakiot kullekin osareaktiolle.

A reaction engineering approach to homogeneously catalyzed glycerol hydrochlorination

The production of biodiesel through transesterification has created a surplus of glycerol on the international market. In few years, glycerol has become an inexpensive and abundant raw material, subject to numerous plausible valorisation strategies. Glycerol hydrochlorination stands out as an economically attractive alternative to the production of biobased epichlorohydrin, an important raw material for the manufacturing of epoxy resins and plasticizers. Glycerol hydrochlorination using gaseous hydrogen chloride (HCl) was studied from a reaction engineering viewpoint. Firstly, a more general and rigorous kinetic model was derived based on a consistent reaction mechanism proposed in the literature. The model was validated with experimental data reported in the literature as well as with new data of our own. Semi-batch experiments were conducted in which the influence of the stirring speed, HCl partial pressure, catalyst concentration and temperature were thoroughly analysed and discussed. Acetic acid was used as a homogeneous catalyst for the experiments. For the first time, it was demonstrated that the liquid-phase volume undergoes a significant increase due to the accumulation of HCl in the liquid phase. Novel and relevant features concerning hydrochlorination kinetics, HCl solubility and mass transfer were investigated. An extended reaction mechanism was proposed and a new kinetic model was derived. The model was tested with the experimental data by means of regression analysis, in which kinetic and mass transfer parameters were successfully estimated. A dimensionless number, called Catalyst Modulus, was proposed as a tool for corroborating the kinetic model. Reactive flash distillation experiments were conducted to check the commonly accepted hypothesis that removal of water should enhance the glycerol hydrochlorination kinetics. The performance of the reactive flash distillation experiments were compared to the semi-batch data previously obtained. An unforeseen effect was observed once the water was let to be stripped out from the liquid phase, exposing a strong correlation between the HCl liquid uptake and the presence of water in the system. Water has revealed to play an important role also in the HCl dissociation: as water was removed, the dissociation of HCl was diminished, which had a retarding effect on the reaction kinetics. In order to obtain a further insight on the influence of water on the hydrochlorination reaction, extra semi-batch experiments were conducted in which initial amounts of water and the desired product were added. This study revealed the possibility to use the desired product as an ideal “solvent” for the glycerol hydrochlorination process. A co-current bubble column was used to investigate the glycerol hydrochlorination process under continuous operation. The influence of liquid flow rate, gas flow rate, temperature and catalyst concentration on the glycerol conversion and product distribution was studied. The fluid dynamics of the system showed a remarkable behaviour, which was carefully investigated and described. Highspeed camera images and residence time distribution experiments were conducted to collect relevant information about the flow conditions inside the tube. A model based on the axial dispersion concept was proposed and confronted with the experimental data. The kinetic and solubility parameters estimated from the semi-batch experiments were successfully used in the description of mass transfer and fluid dynamics of the bubble column reactor. In light of the results brought by the present work, the glycerol hydrochlorination reaction mechanism has been finally clarified. It has been demonstrated that the reactive distillation technology may cause drawbacks to the glycerol hydrochlorination reaction rate under certain conditions. Furthermore, continuous reactor technology showed a high selectivity towards monochlorohydrins, whilst semibatch technology was demonstrated to be more efficient towards the production of dichlorohydrins. Based on the novel and revealing discoveries brought by the present work, many insightful suggestions are made towards the improvement of the production of αγ-dichlorohydrin on an industrial scale.

Green diesel synthesis by hydrodeoxygenation of lipids extracted from Chlorella algae in supercritical hexane

Lipids were extracted from Chlorella algae with supercritical hexane. The high lipids yield of approximately 10% was obtained at optimum conditions of 300 rpm stirring speed and 2 h duration compared to the total contents of lipids being 12%. Furthermore, an easiness of hexane recovery may be considered as economically and ecologically attractive. For the first time, in the current work catalytic hydrodeoxygenation (HDO) of Chlorella algal lipids was studied over 5 wt% Ni/H-Y-80 and 5 wt% Ni/SiO2 at 300 C and under 30 bar total pressure in H2. A comparative HDO of stearic acid was carried out under similar conditions. The conversion of lipids was about 35% over 5 wt% Ni/H-Y-80 after 6h, whereas, 5 wt% Ni/SiO2 was totally deactivated after 60 min. The selectivity to hydrocarbons (C15-C18) is 6%. As a comparison, complete conversion of stearic acid over 5 wt% Ni/H-Y-80 was achieved in 6 h. The transformation of lipids proceeded mostly via hydrogenation and hydrolysis with formation of free fatty acid (FFA). The lower activity might be attributed to deactivation of catalysts caused by chlorophylls and carotenoids. Even though the conversion is low, future studies in HDO of lipids extracted from other algae species having higher lipid content could be proposed. Coke resistant catalyst might be considered to improve catalytic activity.