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DOI: http://dx.doi.org/10.20534/AJT-17-1.2-102-104
Khudoyberganov Abrorjon Akbarovich, Bukhara refinery Deputy Chief Engineer for the implementation of innovative projects and technologies in production Bukhara refinery E-mail: abrorjon_@mail.ru
Studying of process steaming of kerosene fraction by hydrocarbonic steams
Abstract: In article resulted results of studying process of steaming kerosene fraction are by hydro-carbonic steams.
Keywords: hydrocarbonic, distillation, rectification, water steam, stripping — column, oil, gascondensate.
Introduction
As is known, by distillation of oil and a gas condensate receive hydrocarbonic fractions which are intermediate products for motor TonAHB. Process is carried out in installation of the primary distillation consisting in basic from rectification and the stripping-columns [1; 2; 3].
Under the existing «know-how» at steaming distillate fractions it is used heating water steam. As the steaming agent it is possible to carry to the basic lacks of application of water steam: increase in expenses of thermal energy at process; increase of loading of a column on steam, leading to increase in its diameter; condensate formation, its branch from fuel fractions and clearing of impurity demands additional expenses; strengthening of corrosion of working surfaces of the equipment under the influence of a water condensate, watery mineral oil and their necessity of the subsequent drying, etc. [2; 4].
For these reasons in the technological plan sharp reduction of the expense of water steam on process of distillation of oil is expedient, in particular, at steaming distillates, or carrying out of the given process without its participation. Thus one of technological decisions of a problem, use of steams of the oil fractions leaving from rectification ofa column, as the alternative heat-carrier instead of water steam is [4]. Such technological decision promotes elimination of the above-stated negative phenomena which are taking place at distillation oilgascond-ensate of raw materials with participation of water steam.
The analysis of a condition of process of primary distillation of hydrocarbonic raw materials in oil refining factories shows, that because of not enough effective organisation ofprocesses in rectification to a column the expense of thermal energy for process realisation raises, that is reflected in growth of the cost price of let out production. Therefore perfection of processes of distillation of hydrocarbonic raw materials, working out of
highefficiencies, energo — and resource saver up technological processes and rectification devices corresponds to the basic directions of dynamic development of oil refining branch.
Experiment
Proceeding from the above-stated, we collect the experimental stand for process studying steaming (decontaminations) of the kerosene fraction leaving from difficult rectification of a column of installation of primary distillation Bukhara oil treatment factory (fig. 1). The main objective of experimental researches was definition of quality indicators — fractional structure, density and temperature of flash of the kerosene fraction leaving installation of primary distillation and from the subsequent processing by its hydrocarbonic heat-carrier (the steaming agent).
Object of research is the kerosene fraction received from local oilgascondensate of raw materials (at a parity of 70 % of a gas condensate and 30 % of oil) on Bukhara OTF.
Experimental decontamination device consists of capacity 1 for easy fraction, thermometers 2, 7 and 9, electrotiles 3 and 10, a manometre 4, a sand bath 5, a gas torch 6, flask Angler 8, a refrigerator 11 and flasks for gathering of light fractions 12.
During experiments the capacity 1 is filled with easy fraction and it heats up by means of an electrotile 3. The capacity is supplied by the thermometers established in pockets 2 and manometres 4 for constant control of working temperature and pressure of investigated fraction. The working temperature of the hydrocarbonic heat-carrier in the given capacity is supported in limits from 350 T° to 400 T° by means of the sand bath 5 which are warmed up by a gas torch 6. The temperature of a sand bath is supervised under indications of the thermometer 7. During experiment in a flask 8 with volume three
Studying of process steaming of kerosene fraction by hydrocarbonic steams
litres fill in the kerosene selected from a sampler industrial rectification of installation, not subjected to steam processing — steaming. The investigated liquid in a flask 8 heats up by means of an electrotile 10 to temperature of 110 T° and the ferry easy fraction from capacity 1 is processed. Thus the liquid temperature in a flask 8 is supervised by the thermometer 9. Leaving steams of easy fraction from a flask 8 are condensed in water refrigerator
Libikha 11. The received condensate, i. e. the decontaminated easy fraction of kerosene, gathers in a flask 12.
At carrying out of experiences every 15 minutes defined temperatures and pressure of investigated fraction, according to regime parametres of the plant (Tw = 30-85 °C and Pw = 40-150 kPa). Results of experiences on decontamination of kerosene fraction of local hydrocarbonic raw materials are resulted in the table 1.
Table 1. - Results of experiences on decontamination of kerosene fraction of local hydrocarbonic raw materials
Kerosene fraction Allocated easy fraction in the course of decontami-
nation easy fraction
№ Indicators Unit of measure To strip-pmg — columns Decontaminated by water steam in a stripping-column After decontamination easy fraction on 52-280 T0 on 280-281 T0 Easy fraction
1 Density at 20 T0 kg/m 3 776.8 790.9 795.5 718.8 734 636
Fractional structure:
b. b. To 102 146 188 34 40 25
10 % To 131 167 193 55 64 30
20 % To 143 175 196 68 79 33
30 % To 156 182 198 81 97 36
2 40 % To 168 188 200 96 118 39
50 % To 177 194 202 111 156 42
60 % To 184 200 204 125 170 45
70 % To 191 205 207 138 177 49
80 % To 198 210 211 154 184 55
90 % To 205 217 216 175 197 62
e. b. To 216 228 225 198 211 67
3 Exit % 98.0 98.0 98.0 97 98 95
4 The rest % 1.0 1.0 1.0 1.2 0.8 0.5
5 Losses % 1.0 1.0 1.0 1.8 1.2 4.5
6 Flash temperature To - 38 46 - - -
From table data it is visible, that temperature of the beginning of boiling (b. b.) kerosene fraction to a stripping-column its temperature of the end of boiling (e. b. begins from 102 T and.) comes at 216 °C. Under production conditions, after decontamination of kerosene with water steam in a striping-column, it b. b. Makes 146 °C, and e. b. — 228 T °. After decontamination by the hydrocarbonic heat-carrier b. b. Kerosene fraction has made 188 °C, and e. b. — 225 T °. The allocated easy fractions in the course of decontamination of kerosene easy oil fraction at temperature of 52-280 T° had b. b. 34 °C and k. k. 198 T ° accordingly. At realization of the given process at temperatures 280-281 T ° easy fractions
of kerosene have h. k. 40 T ° and e. b. 211 T Thus, the made experiments show, that after kerosene decontamination easy hydrocarbonic fractions from structure of kerosene fraction pass in structure easy oil fraction.
The basic results of experimental data by definition of fractional structure of kerosene and its easy fractions before decontamination process are represented on fig. 2. The analysis of curves shows, that with increase in temperature the exit of easy fractions from structure of steamed kerosene increases. At a temperature mode within 197-225 T° in all variants of experiences achievement of necessary clearness of division of kerosene fraction from the accompanying components,
corresponding to requirements of the standard of quality of production is observed.
As we see, process of decontamination of kerosene by steams easy fraction occurs at rather high temperature modes (a curve 1), than it steaming water steam in a stripping-column (a curve 2). Thus rate of allocation easilyflying components from structure of kerosene fraction more intensively (a curve 4), than at decontamination of kerosene with water steam (a curve 5).
On a course of experiments also are defined temperature of flash of kerosene fraction [2; 3] in accordance with GOST 6356 (the tab. see). The temperature of flash of kerosene fraction (at the expense 24 m 3/h), decontaminated by water steam (at the expense 1.5 m 3/h) in a stripping-column Bukhara OTF makes 38 T and the kerosene fraction decontaminated by hydrocarbonic steams in the conditions of experiment, had temperature of flash equal 46 T °. The difference in values of temperature of flash speaks distinction of the mechanism of intermolecular interactions of the steaming agent and the kerosene expressed in various degree flying of easy fractions at decontamination.
During experiences the density of kerosene fraction was defined areomentric by a method [2; 3; 5],
according to GOST 1756. Apparently from the table, the density of kerosene fraction to a stripping-column makes 776.8 kg/m 3, and after its decontamination with easy oil fractions values ofthis indicator 795.5 kg/m 3 are equaled.
Conclusions
Generalising results of the spent experiments by definition of fractional structure of kerosene and its easy fractions in process steaming it is possible to draw a conclusion on possibility of an effective utilization of steams of hydrocarbonic fractions (for example, easy fraction, leaving of rectification columns) as the alternative steaming agent in exchange heated water steam. Application of the hydrocarbonic steaming agent promotes improvement of quality indicators of kerosene fraction, elimination of its possibility обводнения (especially aviakerosene and diesel fuel) and to clearness increase fraction distillates in rectification to a column. Because of distinction in physical and chemical and heatphysical properties of hydrocarbonic and water steams, efficiency spent warmly — and massexchange processes at steaming kerosene fraction in a stripping-column raises; speed of corrosion of working surfaces of the equipment thus decreases and the expense ingi-bitors corrosion is reduced.
References:
1. Skoblo A. I., Molokanov J. K., Vladimirov A. I., etc. Processes and devices oilgastreatment and petrochemistry: the Textbook for high schools. 3 publ., the reslave. - M.: Bowels, 2000. - P. 103-104.
2. Technology of oil refining. In 2 parts. A part the first. Primary oil refining/Under the editorship of O. F. Glagolevoj and V. M. Kapustin. - M.: Chemistry, the Colossus, 2006. - P. 99-105, 143-146, 331-345, 390-392.
3. Manovyan A. K. Technolog of primary oil refining and natural gas. The manual for high schools. 2 publ. - M., 2001 - P. 104-107, 138-140, 357-389.
4. Salimov Z. S., Hudajberdiev A. A., Sharipov K. K., Hurmamatov A. M. The Effective utilization of hydrocarbonic steams in primary distillation oilgascondensate raw materials//the Uzbek magazine of oil and gas. -2011. - № 2. - P. 34-35.
5. Tumanyan B. P. Practical of work on technology of oil. A small laboratory practical work. - M.: Technics, RSU oil and gas of I. M. Gubkin. Tuma groups, 2006. - P. 11-12.
Studying of process of decontamination of gasoil by hydrocarbonic couples
D OI: http://dx.doi.org/10.20534/AJT-17-1.2-105-107
Khudoyberganov Abrorjon Akbarovich, Bukhara refinery Deputy Chief Engineer for the implementation of innovative projects and technologies in production E-mail: abrorjon_@mail.ru
Saydakhmedov Shamshiddin Mukhtarovich,
Fergana oil refinery, Chief of Fergana oil refinery
Studying of process of decontamination of gasoil by hydrocarbonic couples
Abstract: In article results of pilot studies on use of kerosene fractions are given as the unpicking agent for decontamination of oil-gas condensate raw materials, change of density and kinematic viscosity, and also influence of the unpicking agent on quality ready production.
Keywords: pressure, temperature, kerosene, gasoil, water vapor, hydrocarbonic, gas condensate, distillation, water steam, light naphtha.
Development of the oil and gas processing and petrochemical industry at the present stage is characterized by considerable expansion of the range and products improvement of quality, increase in depth of oil refining, construction along with installations of big single power of modular low-tonnage installations of complex oil refining, gas and the gas condensate, allowing to receive wide scale of oil products taking into account needs for them oil and gas extraction areas [1; 2].
As a rule, oil and oil products divide by distillation into separate parts, each ofwhich is less difficult mix. Hydrocarbonic fractions in difference from individual connections have no constant temperature of boiling. They boil away in certain intervals of temperatures. Temperatures I began and the end of boiling depend on a chemical composition of fraction. Thus, the fractional composition of oil and oil products shows the contents in them the various fractions which are boiling away in certain temperature limits. This indicator has great practical value. On fractional composition of oil judge what oil products and in what quantities can be emitted from it, and the fractional composition of gasolines and other motor fuels characterizes their evaporability, completeness of evaporation, etc. For the purpose of creation of a demanded steam irrigation in distant-pasture section of columns, and also evaporations of low-boiling fractions of oil in practice widely apply distillation with supply of water vapor [1]. At input of water vapor in distant-pasture section the partsionalny pressure of vapors decreases and conditions under which liquid is as
though superheated that causes its evaporation (that is effect of water vapor similarly to vacuum) are created. The general consumption of water vapor entered into atmospheric columns of installations of distillation of oil makes 1.2-3.5, and in vacuum columns for fuel oil distillation — 5.8 % of masses. on overtaken raw materials. When using water vapor for distillation of oil there are following shortcomings: increase in expense of energy, increase of loading of columns on couples, deterioration of conditions of regeneration of heat in heat exchangers, increase in resistance and pressure increase in a column and other devices, flood of oil products and strengthening of corrosion of devices.
In this regard in recent years in world oil processing the tendency to existing restriction of application of water vapor and to transfer of installations on technology of dry distillation i. e. application of the hydrocarbonic steaming agent is shown.
Proceeding from the above, we collected model laboratory installation for carrying out experiments on decontamination of kerosene and gasoil fractions. Experiments are made in vitro Bukhara oil refinery to whom aviation fuel analyses Jet A-1 to an decontamination water vapor of stripping-columns and with an decontamination water vapor after stripping-columns are carried out. At creation of conditions of a temperature mode of stripping-columns experiments with application of light naphtha for an decontamination of kerosene fraction to stripping-columns [4] are in vitro made. The obtained experimental data are given in tab.1.
