Burumbaeva, G. R.

Nazarov, G. Y.

Seytenova, G. J.

Electronic archive of Tomsk Polytechnic University

 Секция 7.  Химия и химическая технология на иностранном языке513base. Gadolinium (Gd) was chosen as a main con-trast agent due to its excellent magnetic properties [3] and ability to form chelates. It was agreed to use diethylenetriaminepentaacetic acid (DTPA) an-hydride to form a strong chelate with Gd because it is fairly easy attached to a free amine group of the ADS. The scheme of a process is shown in Scheme 2.Such substance could become a base for devel-oping new theranostic agent and further research in utilization of ZVI NPs in medical and pharmaceu-tical fields.references1. O.A. Guselnikova, A.I, Galanov, A.K. Gutakovs-ki, P.S. Postnikov // Beilstein J. Nanotechnol, 2015.– 6.– 1192–1198.2. Guselnikova O.A., Gromov M.V., Galanov A.I. // Advanced Materials Research.– Trans Tech Publications, 2014.– Т.1040.– С.309–313.3. Ya.N. Ertas, N.N. Jarenwattananon, and L.-S. Bouchard // Chem.Mater., 2015.– 27.– 5371−5376.the testinG of a kinetiC model of CatalytiC CraCkinG in the “C-200” seCtion of the kt-1/1 installation of oil refininG Plants in kaZakhstanG.Y. Nazarov1, G.R. Burumbaeva1, G.J. Seytenova2Scientific Supervisors – PhD, Professor, E.D. Ivanchina1; PhD, Professor, E.N. Ivashkina1 Linguistic Advisor – Senior Lecturer, O.V. Mikhailova11National Research Tomsk Polytechnic University Russia, 634050, Tomsk, 30 Lenina ave. 2Pavlodar State University after S. Toraigyrov Kazakhstan,  burumbaeva.galiya@gmail.comThe Strategy of the development of the Repub-lic of Kazakhstan until 2030 emphasizes the oil and gas industry, making energy resources a number one priority. This program is the basis for improv-ing the competitiveness of the oil and gas industry of Kazakhstan [1]. Nowadays the Republic of Kazakhstan has three oil refineries – the Atyrau Refinery, the Shy-mkent Refinery and the Pavlodar refinery, for which the increase in the depth of crude oil refining is an urgent task.The aim of this work is to test the kinetic model of the process of catalytic cracking in the Section “C-200” of the installation KT-1/1 of the Pavlodar scheme 1.  Synthesis of ZVI NPs using p-aminobenzenediazonium tosylatescheme 2.  Synthesis of Gd-based MRI contrast compoundXVII Международная научно-практическая конференция имени профессора Л.П. Кулёва514oil refining plant in Kazakhstan.The testing of the kinetic model of the catalytic cracking process requires some information about the group composition of the raw materials and the catalytic cracking products. The laboratory studies were carried out to determine the group composi-tion of the catalytic cracking products.The kinetic parameters of the catalytic cracking reactions are presented in table 2.The adequacy of the model calculations is pre-sented in table 3. The adequacy of the model cal-culations was verified by comparing the calculated and experimental data on the concentration of the streams of hydrocarbon groups after the reactor and the gasoline fractioning.The table shows that the reactions of par-affins cracking (0.10–1), hydrogen redistribution (56.05 l • s–1 • mol–1), the dealkylation of aromatic hydrocarbons (0.44–1) and naphthenes (0.22–1), as well as the condensation of aromatic compounds (2.15 l • s–1 • mol–1) and the coke formation (0.62 l • s–1 • mol–1) occur at the greatest speed.table 1. Group composition of vacuum distillateThe group of hy-drocarbonsThe vacuum distillate, the content of wt %Paraffins + naphthenes 73.13Aromatic hydrocarbons 23.31Alcohol-benzene resin 3.56table 2. Kinetic parameters for catalytic cracking reactions at T °C = 522.52, P = 0.09 MPaReactionsThe rate constantkпрkобThe cracking of paraffins С13-С40 0.10 – sec–1The cracking of isoparaffins С13-С40 0.67 – sec–1The cracking of n-paraffins С5-С11+ 0.17 – sec–1The isomerization of paraffins С5-С11+ 5 • 10–4 3 • 10–4 sec–1The cracking of isoparaffins С5-С11+ 0.16 – sec–1The cracking of olefins С5-С11+ 0.67 9.3 • 102 sec–1The redistribution of hydrogen 56.05 – l • sec–1 • mol–1The dealkylation of naphthenes 0.22 0 sec–1The dealkylation of aromatic hydrocarbons 0.44 3.7 • 10–5 sec–1The cracking of naphthenes 0.44 – sec–1The condensation of aromatic compounds 2.15 – l • sec–1 • mol–1The formation of coke (polycondensation) 0.62 – l • sec–1 • mol–1The cyclization of olefins 0.05 0.016 sec–1The dealkylation of aromatic hy-drocarbons of gasoline0.15 1.3 • 10–5 sec–1table 3. The adequacy of model calculationsComponent The calcul. wt  % Experiment, % wt. Accuracy (relative), %High molecular weight paraffins 3.16 3.17 0.35Medium molecular paraffins 1.58 1.52 4.01Isoparaffins 11.73 11.91 1.55Olefins 7.13 7.07 0.82Gas 33.44 33.50 0.18Naphthenes 4.16 4.09 1.72Monoaromatic hydrocarbons 18.66 18.68 0.13High molecular weight naphthenes 2.36 2.33 1.40Aromatic hydrocarbons 12.26 12.24 0.16Gums 0.43 0.41 4.11Coke 5.08 5.07 0.20 Секция 7.  Химия и химическая технология на иностранном языке515references1. Address of the President of the Republic of Ka-zakhstan, Nursultan Nazarbayev, to the People of Kazakhstan, January 29, 2010.– (in Russian) http://www.akorda.kz/ru.the imPaCt of Catalyst temPerature from reGenerator on the CatalytiC CraCkinG ProCess PerformanCeG.Y. Nazarova, V.I. Stebeneva, A.A. KhanScientific Supervisor – Professor, E.N. Ivashkina Linguistic Advisor – N.S. BelinskayaNational Research Tomsk Polytechnic University Russia, Tomsk, 634050, st.Lenina,30, silko@tpu.ru The yield and composition of the catalytic cracking products are determined by a whole set of records of operation for non-stationary adjoint sys-tem "riser-regenerator".The most important parameters of a techno-logical mode determined by the temperature of the catalytic cracking process are the catalyst tempera-ture after regeneration, feedstock temperature, the ratio of catalyst: feedstock and steam flow into the reaction zone of the riser reactor [1]. Catalyst circu-lation ratio is determined depending on the tempera-ture of the catalyst after regeneration, which in turn depends on the coke content on the catalyst after the riser reactor. Coke content depends from the com-position of the feedstock and temperature mode of the riser reactor.The purpose of this research is to evaluate the effect of catalyst temperature on the vacuum distil-fig. 1.  The impact of catalyst temperature after regeneration on the process temperature and on the conversion of feedstockfig. 2.  The impact of catalyst temperature after regeneration on the gasoline yield and on the coke content on the catalyst

The testing of a kinetic model of catalytic cracking in the “C-200” Section of the KT -1/1 Installation of oil refining plants in Kazakhstan

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