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WO1997016506A2 - Processus de raffinage de petrole en une etape - Google Patents

Processus de raffinage de petrole en une etape Download PDF

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Publication number
WO1997016506A2
WO1997016506A2 PCT/RU1996/000312 RU9600312W WO9716506A2 WO 1997016506 A2 WO1997016506 A2 WO 1997016506A2 RU 9600312 W RU9600312 W RU 9600312W WO 9716506 A2 WO9716506 A2 WO 9716506A2
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Prior art keywords
feedstock
gas
temperature
reaction zone
products
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PCT/RU1996/000312
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English (en)
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WO1997016506A3 (fr
Inventor
Vladimir Petrovich Agashkov
Viktor Alexeevich Krjuchkov
Valery Timofeevich Popov
Dmitry Ippolitovich Slovetsky
Vladimir Ippolitovich Slovetsky
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Priority to AU75106/96A priority Critical patent/AU7510696A/en
Publication of WO1997016506A2 publication Critical patent/WO1997016506A2/fr
Publication of WO1997016506A3 publication Critical patent/WO1997016506A3/fr
Anticipated expiration legal-status Critical
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/02—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in retorts

Definitions

  • This invention relates to the refining of liquid and solid hydrocarbon feedstocks, especially those containing components boiling at 360 °C or more, to produce higher value products such as hydrocarbon fuels and products for use in the chemical industry. More particularly, this invention relates to a single-stage process for refining heavy hydrocarbon feedstocks such as crude petroleum, residual oils, tar, bitumen, gas condensate, and the like, while enabling a high recovery of light hydrocarbon products.
  • vacuum distillation of the residual oil followed by recovery of vacuum distillate, e.g., gas oil boiling at from about 350 °C to about 500 °C; and yielding a heavy residual oil or tar boiling at higher than about 500 °C.
  • Methods of refining the gas oil include, e.g., catalytic cracking wherein a finely-devel- oped catalyst is introduced into a high-velocity stream of gas oil vapors at a temperature of 520-550 °C, and the oil-catalyst contact time ranges from 2-10 sec.
  • the products include light hydrocarbons boiling at under 350 °C, e.g., gasoline, kerosene, diesel fuel, C1-C4 gases; and coke which deposits onto the catalyst.
  • Regener- ation of the catalyst is provided via burning the coke from the catalyst.
  • the residual oil of atmosphere distillation is refined to produce boiler fuel via processes such as: - visbreaking (i.e., reducing the viscosity via partial pyrolysis of the residual oil); hydrocracking (i.e., catalytic hydrogenation employing hydrogen and partial cracking of heavy components at high pressure (above 150 atm) and a tempera- ture of about 400-425 °C); hydrorefining (i.e., subjecting the oil to hydrogenation of sulfurous, nitrogenous and oxygen- containing compounds and of nonsaturated hydrocarbons ) .
  • the process employs a pressure of about 5 atm and a tem- perature of about 380-420 ⁇ C.
  • Methods of refining the tar include: - thermocatalytic cracking at atmospheric pressure and a temperature of about 500-550 °C.
  • the tar is fed to a reactor as a vapor or liquid droplets.
  • the reactor is partially filled by catalyst.
  • Coke may be used as the catalyst.
  • the products are: C1-C4 hydrocarbon gases (9-14 %), gasoline (10-14 %), kerosene and diesel fuel (boiling at under 350 °C) (15-20 %), gas oil (boiling at 350-500 °C) (20-40 %), and coke (10-23 %).
  • the above products yields (shown in percent by weight) depend on the composition of the tar.
  • Produced coke is burned as a fuel, e.g., to provide the needed heating of the reactor or gasified into fuel gas containing carbon monoxide and hydrogen.
  • - delayed coking at a temperature of 370-480 °C and a pressure of 2-6 atm.
  • the coke yield is up to 70 %.
  • Ad ⁇ ditionally, some amounts of diesel or boiler fuel are also produced.
  • Duration of the process (which runs in a closed reactor) ranges from 2-12 hours; and - oxidation of tar at a temperature of 180-400 °C and a pressure of 4-4.5 atm via bubbling air or oxygen through the tar for 2-12 hours, and yielding up to 70 % bitumen.
  • Shortcomings of these known methods of refining include:
  • the gases are supplied via either injecting the gases into the still or through perforations in the still's wall, bubbling the gases through the bottom of a still or via feeding the gas upwardly through a jet nozzle placed in the bottom toward the liquid mixture fed from the top of the still, and wherein a special cylinder is inserted into the still to provide a narrow gap between the cylinder and the still's wall in order to provide good mixing and uniform tempera ⁇ ture distribution.
  • Freeman (US Patent 2,095,863) suggested to produce low-boiling-hydrocarbons from high-boiling ones or solid materials containing hydrocarbon components (e.g., coal, shales, etc. ) via passing such materials through a train of heated chambers.
  • Each chamber has its own temperature and the temperature increases from one chamber to another.
  • contact is arranged between the processed materials and hydrocarbon gases or vapors obtained either as a product in earlier chambers or from separate source. It was suggested to produce some preliminary activation of these gases by passing them through special vessels over heated alkaline materials before feeding them into the refining chambers. No quantitative characteristics of the processes are reported.
  • Naumann suggested a refining process for distilling high-boiling hydrocarbons having a boiling temperature greater than 200 °C to provide higher yields of distillates and production of new products: i.e., black wax.
  • the idea of the method is to heat the high-boiling hydrocarbons fed into a stationary reactor by continuously circulating a neutral gas, which does not contain an oxidant (nitrogen is preferred, but combustion products may be used) and which is heated up to 800-1400 °C. Heating of the high-boiling hydrocarbons in the reactor is provided wholly by heat exchange with the hot gas, and the temperature of the withdrawn product does not exceed 250-360 °C.
  • the main shortcomings of the foregoing process are: it is multistage; it is a cyclic process; the productivity is low; and it requires a high power consumption. Besides, heating the feed by hot gases results in local overheating of liquid hydrocarbons, inevitably causing an increased conversion of the hydrocarbons into coke or pyrocarbon which may constitute up to 30 % by weight of the feedstock.
  • the present invention provides an improved process for the refining of oil and other hydrocarbons containing heavy fractions, which employs either a batch or continuous type reactor, and differs from prior art processes by the following:
  • the average heating rate during the processing is much higher (i.e., more than 5 °C per minute); - it implements bubbling of a non-oxidizing gas, i.e., non-condensing hydrocarbon or other gases which do not oxidize the feedstock components, through the feedstock at temperatures including the temperature range within which the cracking of hydrocarbons and chemical interaction between hydrocarbons of the stock material and bubbling gases take place; and
  • a non-oxidizing gas i.e., non-condensing hydrocarbon or other gases which do not oxidize the feedstock components
  • the specific average flow rate of the bubbling gas during the processing is more than 0.3 % by weight of the feedstock in the reaction zone per minute. (Averaging is over the processing time).
  • Additional objects of the present invention are to provide a process which:
  • Still a further object of the present invention is an oil refining process which permits faster refining of heavy oil feedstocks, increased yields of light hydro ⁇ carbon products, and reduced yields of coke. Additional objects and advantages of the invention will appear in the following description, and other objects and advantages will be apparent from that description, or may be learned by practice of the inven ⁇ tion. The stated objects and advantages of the invention may be realized and attained by the process steps and their interaction, and operational features particularly pointed out in the appended claims.
  • a process for refining a liquid hydrocarbon feedstock which comprises introducing the feedstock into a reaction zone; heating the feedstock in the reaction zone from an initial tem ⁇ perature in the range of about 80-375 °C (depending on feedstock composition) to a final temperature in the range of from about 520 °C to about 580 °C at an average heating rate of about 5 °C/minute or greater, while maintaining the pressure in the reaction zone at atmospheric pressure; introducing a heated non-condensing and non-oxidizing gas into the reaction zone at an average flow rate of at least 0.3 % of feedstock weight in the reaction zone per minute; and recovering from the reaction zone refined liquid and gaseous hydrocarbon products and coke.
  • Feedstocks well suited for use in the invention are heavy oil feedstocks, such as crude oils, residual oils, gas condensates, tars, bitumens, shale oil and coal- derived liquids, or fractions of any of the above.
  • Such feedstocks typically contain substantial quantities of hydrocarbons boiling above about 360 °C.
  • non-condensing and non- oxidizing gas refers to hydrocarbon gases which are gaseous at standard conditions and contain no compounds which could oxidize the hydrocarbon feedstock, and preferred such gases are C1-C4 hydrocarbons, especially methane, ethane, propane and butane and their mixtures, gaseous products of oil refining and coal processing, and nitrogen, and hydrogen and rare gases etc.
  • the liquid and gaseous hydrocarbon products are withdrawn at a tempera- ture not higher than about 330 °C from a first portion of the reaction zone wherein the feedstock is heated to a temperature of about 360-430 °C, and the remaining portion of the feedstock is passed to a second portion of the reaction zone wherein it is heated to a higher tempera- ture, e.g., from about 520 °C to about 580 °C, while a heated non- condensing and non-oxidizing gas is bubbled through it, completing the process and forming dry coke, which is recovered from the second portion of the reaction zone.
  • a tempera- ture e.g., from about 520 °C to about 580 °C
  • Figure 1 illustrates laboratory scale apparatus for the batch-type operation of the process of the present in ⁇ vention
  • Figure 2 is a schematic flow diagram of the continuous-type operation of the process of the present invention.
  • Figure 3 is a plot of the total time required for refining a crude oil feedstock versus the average rate of heating the feedstock, employing the process of the present invention
  • Figure 4 is a plot of the amounts of gas, liquid and solid products obtained versus the average heating rate when processing a crude oil feedstock in accordance with the present invention
  • Figure 5 is a plot of the amounts of coke and pyrocarbon produced when refining a crude oil feedstock in accordance with the present invention at varying average gas flow rates and average feedstock heating rates
  • Figure 6 is a plot of the output of light hydro- carbons, coke plus pyrocarbon and energy consumption obtained when processing crude oil and residual oil feedstocks in accordance with the present invention. Description of Preferred Embodiments
  • An object of the present process of oil refining is to reduce the duration of thermal processing of liquid- phase raw material (also referred to herein as feedstock or stock) at atmospheric pressure by stimulation of both evaporation processes and chemical reactions due to bubbling the hydrocarbon gases (e.g., natural gas, petro- chemical gases, propane-butane mixture, etc. ) through the feedstock (raw material ) .
  • hydrocarbon gases e.g., natural gas, petro- chemical gases, propane-butane mixture, etc.
  • the gas flow removes the evaporating fractions faster, and permits a reduction in the working tempera ⁇ tures needed for extraction of that fractions. It also shortens the processing time and increases the degree of evaporation.
  • the gas bubbling stimulates the chemical reactions due to appropriate turbulent gas flow, which results in easier access of raw material to metals which are in admixture with the raw material and which posses catalytic properties, (i.e., homogeneous catalysis by natural ad ⁇ mixtures in the raw material is stimulated), in that the hydrocarbon gases start to enter into chemical reactions so as to increase the yield of light products.
  • the bubbling of the gas changes both the characteristics of the process of coking and the texture of the produced coke.
  • the produced coke is a highly porous powder which can be removed easily from the reactor where any type of liquid hydrocarbons may be refined ( starting from crude oil to tars and remains of deasphalting) .
  • the flow rate of bubbled gas may be adjusted for the desired intensity of gas evolution or rate of chemical reactions.
  • the type of bubbled gas is selected in dependence on the composition of products or coke texture desired and taking into account the economics of the processing.
  • the complete refining of raw material (up to 97- 99 %) is provided via a single stage operation at atmospheric pressure. The duration of such refining is more than 2-3 times faster than that of the standard practices.
  • the present process results in reducing the yields of coke and other heavy products, and it excludes the formation of heavy residues such as the oil residue formed during crude oil refining, tar formed during oil or oil residue refining, and the like. Instead of these heavy residues, light fractions, such as gases, light liquids and some amount of heavy liquids are formed.
  • the heavy oil produced by the present process is a mixture of low- volatility hydrocarbons with boiling temperatures of 500 °C and higher and which does not contain heavy products contributing to coke or soot formation during further processing or use.
  • gas oil produced by the present process may be used instead of residual oil as a fuel for boilers.
  • the coke produced by the present process is also a valuable product. For example, it may be used in metallurgy, since it concentrates 100 % of the iron, about 50 % of the nickel and about 50 % of the vanadium contained in the parent raw material. This coke can be easily removed from reactor. During refining by the present process more than
  • the liquid products were analyzed using atmospheric distillation wherein such products were heated to a tem ⁇ perature of 190 °C at atmospheric pressure, and after that, heated to a temperature of 240 °C at a pressure of 100 Torr, followed by heating to a temperature of 300 °C at a pressure of 5 Torr, and lastly, heating to 300 °C at a pressure of 1 Torr.
  • the fractional composition was obtained via weighing the liquid products and their fractions.
  • the elemental composition i.e., H, N, C, S, and metals
  • the elemental composition i.e., H, N, C, S, and metals
  • Other methods of analysis were also used: e.g., differential thermochemical analysis (DTA), mass-spectro- metry, gas-liquid chromatography, and determination of molecular weight distributions for both the raw material and liquid products, phase X- ray analysis of coke.
  • a cylindrical reactor (1) was used.
  • the reactor had an inner diameter of 45 mm, a length of 270 mm, and working space of 0.43 1 between its ends.
  • a pipe (2) through the cylinder head was used to feed the hot gas into a collector (3 ) .
  • the gas passed upwardly through holes in perforated diaphragm (4) into the working space of the reactor and was bubbled through the stock ( 5 ) being refined.
  • the holes were 0.5 mm in diameter and they numbered 256. Uniformity of the bubbling was provided by uniform distribution of the holes across the diaphragm and by having the total area of the holes be several times less than cross-section area of the collector.
  • the tem ⁇ perature of the bubbling gas was equal to the temperature of the feedstock in the area of the gas.
  • a sleeve (6) was placed for withdrawing the products of refining, which were carried away by the bubbling gas.
  • the sleeve was covered on its outside by heatinsulating material down to the branch pipe (7) provided for withdrawing low boiling components.
  • the branch pipe (7) provided for these outgoing gases led to a water cooled refrigerator (8 ) from which the condensed vapors and liquid products were drained into the receiving tank (19).
  • Products which were not condensed in this first refrigerator passed into a trap (9) cooled by liquid nitrogen or by a mixture of "dry ice” (frozen carbon dioxide) and acetone ( 10) .
  • the gas passed through a pipe (11) equipped with a gas sampler (12) (used for carrying out the gas chromatographic analyses of the outgas composition) and flow meter (13) and was combusted then in the burner ( 1 ) .
  • the reactor was made of high-temperature steel. Some of the branching sleeves and the trap were made of glass. Tight connections between the metal and glass parts were provided by oil and heat resistant rubber placed over the joints.
  • the bubbling gas was delivered to the reactor through flow meter (15), and then heated to a temperature approximately equal to the temperature of the feedstock in the reactor zone wherein said gas was introduced in a heat exchanger (17).
  • Gas feeding tube (2) was input into reactor (1) through tight asbestos isolation (16).
  • the temperature of the supplied gas near the inlet was measured by thermocouple (18), and the temperature of the stock by thermocouple (20).
  • the temperature of gases and vapors in the zone of products withdrawal was measured by thermocouple (21).
  • the process was conducted as follows: stock was loaded into the reactor at room temperature. For each run the weight of the stock varied from 50-100 gms. After loading, the reactor was placed vertically into the electric oven (22). Heating was controlled via the appropriate variation of the voltage supplied to the oven. The average heating rate was varied in different runs from 2-30 °C per minute.
  • the reactor was opened and the produced coke was allowed to pour out.
  • the coke was a fine powder.
  • Weighing of the reactor was carried out to estimate the amount of pyrocarbon deposited on the wall (the empty reactor was weighed also). No resin and pyrocarbon formation was observed on the reactor wall or pipes during any process conducted within the range of optimal regimes (and for any stock material ranging from crude oil to heavy asphaltenes ) .
  • Fractional composition of liquid products was determined via standard fractionation and weighing of every separated fraction with different boiling tempera ⁇ tures. The amount of produced coke also was determined by appropriate weighing.
  • the elemental composition of the parent stock material and liquid and solid products was determined via standard methods of elementary analysis (C, H, N, S and metals Fe, Ni, V).
  • the coke structure was identified via X-ray analysis.
  • the group composition of parent hydrocarbons and liquid products was investigated by mass- spectrometry, differential thermal analysis, highly efficient gasliquid chromatography and measuring the heat effects at condensation.
  • Outgas composition was controlled on a time to time basis by gas-chromatography via sampling the gas through the sleeve (12).
  • the amount of non- hydrocarbon gaseous products i.e., hydrogen sulfide, oxygen, and nitrogen
  • the amount of non- hydrocarbon gaseous products i.e., hydrogen sulfide, oxygen, and nitrogen
  • the output of products began at a temperature of 90-105 °C and terminated in 29 min. at a temperature of 470 °C.
  • the coking terminated after 34 min. at a temperature of 525 °C so the average heating rate was 12.5 °C per minute.
  • the temperature of the gaseous and vaporized products withdrawing was less than 330 °C.
  • the composition of the products is shown in Table 1. More than 89 % of the crude oil was refined into liquid products. This included 86 % light petroleum products and light gasoil which are useful either as fuel for car engines or boilers, or as raw material for further refining into more valuable petrochemicaL products.
  • Typical composition of produced coke is as follows
  • the produced coke is suitable for various applications, such as metallurgy - since the coke accumulates the heavy metals which are used as dopants. If the parent crude oil contains metals in large concentrations, then the produced coke may be used as a raw material for producing such metals. It has been observed that 100 % of the iron, 35- 40 % of the nickel and 38-45 % of the vanadium are accumulated in the produced coke.
  • the present method of oil refining has been found to have the following effects with respect to sulfur contained in the feedstock.
  • 1-1.5 % of the sulfur transfers into gas (i.e., hydrogen sulfide), some small amount is accumulated in the coke and the rest of the sulfur remained in liquid products (mainly as mercaptans).
  • concentration of other polar compounds is reduced by about 80 %.
  • the total consumption of methane during the present process was found to be about 10 % of weight of the feedstock.
  • nitrogen i.e., an inert or non-reacting gas
  • methane causes lower yields of liquid products (at the same conditions) and higher yields of gases (C1-C4) and coke.
  • the temperature range used in the present process (200-530 °C) coincides with the temperature range which is used in standard four-staged refining; however, the duration of the present process is more than 2 times shorter.
  • stage I+II Products Present Process Technology change of (single stage) (stage I+II) yield, % by weight
  • stage IV stage IV (stage I+II+ yield, %
  • Asphaltite produced by deasphalting i.e., one of the heaviest products was used as heavy residue feedstock for refining.
  • Characterization of feedstock used a) mean molecular weight: 1400 amu (atomic mass unit) ; b) melting temperature: 150 °C; c) composition (by groups), % by weight:
  • the chemical composition of the bubbling gas affects the composition of the products mixture noticeably.
  • bubbling is performed with a mixture of propane/butane, then the total yield of products exceeds the weight of the parent sample. This confirms the participation of the hydrocarbon gases in reactions converting the raw material.
  • the produced coke is a highly porous fine-grain freeflowing powder, which easily pours out the reactor.
  • composition (by groups), % by weight:
  • FIG. 2 A preferred embodiment of a reactor and related apparatus for use of the present process in a continuous operation is shown in Fig. 2.
  • the reactor consists of three sections 101, 102 and
  • the reactor is situated vertically.
  • Feedstock heated in heat exchanger 109 to a beginning temperature e.g., 80-375 ⁇ C (depending on its composition) is introduced continuously to reactor section 101, wherein the feedstock temperature is further Increased due to furnace heater 107 during the feedstocks flowing downwardly.
  • a portion of the bubbling gas (Ggl) is passed though flowmeter 113 ⁇ and heater 110 (heat exchanger) to collector 115 provided with multiple small holes into the lower portion of the section 101.
  • the gas temperature measured by thermocouple 118 should be approximately equal to the temperature of the feedstock in the bottom of section 101. It is not so low as to cool the feedstock below its temperature in zone, where gas is introduced and is not so high as to increase coke output due to local overheating of feedstock in input zone.
  • the feedstock temperature is measured by thermocouple 122 and is preferably equal to about 430 'C in the bottom of this section.
  • section 101 selection of volatile products intensified by the bubbling gas takes place, and vaporized products are withdrawn with the bubbling gas and pass upwardly through the section 102.
  • the temperature in the top portion of section 102 is maintained with heater or heat exchanger 106 at 330 °C or lower, which is the tem- perature of the products outlet.
  • Liquid fractions are withdrawn through line 129 and separated into liquid products, and a nonconditioned part (particularly the fraction Tboil> 500 °C) may be returned into section 101 through line 125 for reprocessing.
  • Liquid products are withdrawn by line 129, they may be cooled in heat exchangers 106, 109, 110 and/or 111.
  • Feedstock remaining after processing in section 101 flows down to the reactor section 103, where it is heated by furnace heater 108 up to the final temperature of processing, about 520-580 ⁇ C.
  • the feedstock is bubbled by gas Gg2 introduced through the holes in collector 116 arranged in the lower part of section 103.
  • the feedstock flow rate is measured with flowmeter regulator 112, and the flow rate is controlled so as to maintain an approximately constant level of liquid feedstock in the section 101.
  • the ratio of bubbling gas flow rates Ggl/Gg2 - is in accordance with the ratio of the feedstock treated in the section 101 to the feedstock remainder in section 103.
  • the total average bubbling gas flow rate Ggl+Gg2 is more than 0.3 wt. % per minute of the feedstock weight in the reactor.
  • thermocouples 120, 121, 122 and 123 each appropriately arranged in sections 101, 102 and 103, the temperature of which can be controlled by regulation of heaters 107, 108 and 109.
  • Solid product (coke) is accumulated at the bottom of the section 103 and after a certain level therein is reached, the coke is periodically passed to tank 105 through a controlled valve 104 by the action of weight or by any other suitable way (mechanically, pneumatically etc. ) .
  • the geometry of the reactor section 101 is such that an approximately constant velocity of the feedstock will be achieved in spite of changes in the feedstock mass due to the loss of gaseous and vapor products.
  • the geometry and temperature distribution in section 103 are arranged to provide coke formation in a zone higher than the maximum level of coke accumulation therein. These parameters will depend on the initial composition and flow rate of the feedstock in accordance with obtained experimental data (see examples) .
  • the average heating rate of the feedstock should be more than about 5 ⁇ C per minute and preferably should be in the range of 15 °C per minute to about 25 ⁇ C per minute.
  • Fig. 3 it may be seen that maintaining the average heating rate of the feedstock in the reactor at least about 5 "C/min while it is heated from the initial to the final temperature results in a significantly reduced processing time. It should also be noted that the use of a feedstock heating rate greater than about 15 °C/min does not- provide a significant further reduction in processing time, and so is generally not warranted because of associated increase in energy requirements.
  • Fig. 5 is a plot of the coke/pyrocarbon product output versus hydrocarbon average gas flow rate when refining a crude oil using average feedstock heating rates of 12 + 2 C/min, 3.8 C/min, and 2.4 /min.
  • the data plotted therein demonstrate the desirability of maintaining the average flow rate of the bubbling gas at a high value, while at the same time maintaining a high average high heating rate of the feedstock, in order to attain the objects of the present invention.
  • Fig. 6 is plot of the amounts of coke/pyrocarbon, gases and light liquid products produced and energy consumption for processing at different feedstock average heating rates for each of crude oil and mazute (residual oil) feedstocks.
  • the optimal feedstock average heating rate ranges from 5 "C/min up to about 15-20 "C/min.
  • the experimental data obtained related to the investigation of the present process shows that all increases of the average heating rate above the minimum value (5 °C/min) leads to further decreasing of the coke and pyrocarbon output and overall treatment time. But significant such decrease is observed only to the value 15-20 ⁇ C/min.
  • An increase of the heating rate to 30 ⁇ C/min does not lead to further a decrease of treatment time and coke output.
  • an increase of the heating rate to 30 ⁇ C/min leads to an increases of the maximum treatment temperature, which corresponds to the end of liquid and gaseous products output.
  • the light liquid hydrocarbons output is decreased by at least 5 % and the output of heavier products is increased correspondingly.
  • the bubbling gas be heated to a temperature approximately equal to the temperature of the feedstock at the location in the reactor when the gas is introduced; however, the temperature of the heated gas may be varied as long as it does not adversely affect the refining operation. It should be not so low as to cool the feedstock in zone where gas in introduced but it should be not so high to lead to local overheating of feedstock accompanied by increased coke formation.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Coke Industry (AREA)

Abstract

Cette invention concerne un processus en une étape permettant d'effectuer le raffinage complet de matières premières consistant en des hydrocarbures lourds. La matière première est chauffée de manière continue sous pression atmosphérique et à une vitesse minimale d'environ 5° C par minute, ceci jusqu'à ce qu'elle atteigne une température finale située entre 520 et 580° C. Un gaz non oxydant et ne générant pas de condensation est ensuite introduit par barbotage dans la matière première lors du processus de chauffage de cette dernière, ceci selon un débit d'au moins 0,3 % en poids par minute. On procède enfin à la récupération des produits hydrocarbures gazeux et liquides raffinés, ainsi qu'à la récupération du coke.
PCT/RU1996/000312 1995-11-01 1996-10-31 Processus de raffinage de petrole en une etape Ceased WO1997016506A2 (fr)

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Application Number Priority Date Filing Date Title
AU75106/96A AU7510696A (en) 1995-11-01 1996-10-31 Single stage oil refining process

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RU95117999/04A RU2112008C1 (ru) 1995-11-01 1995-11-01 Способ переработки углеводородсодержащего сырья
RU95117999 1995-11-01

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WO1997016506A2 true WO1997016506A2 (fr) 1997-05-09
WO1997016506A3 WO1997016506A3 (fr) 1997-06-05

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RU2180919C1 (ru) * 2000-12-08 2002-03-27 Курашов Виктор Михайлович Микробиологический способ получения углеводородов нефти и отдельных углеводородных фракций из твердых горючих ископаемых
CA2444620A1 (fr) * 2001-04-20 2002-10-31 Shell Internationale Research Maatschappij B.V. Separateur a cyclone
RU2217472C1 (ru) * 2002-09-17 2003-11-27 Деревякин Владимир Александрович Способ переработки тяжелого углеводородного сырья
RU2261263C2 (ru) * 2003-10-03 2005-09-27 Золотухин Владимир Андреевич Способ подготовки жидкого углеводородного сырья для дальнейшей переработки
RU2318859C1 (ru) * 2006-05-04 2008-03-10 Государственное унитарное предприятие "Институт нефтехимпереработки Респулики Башкортостан" (ГУП "ИНХП РБ") Установка для проведения термодеструкции нефтяных остатков (варианты)
RU2395560C2 (ru) * 2008-07-30 2010-07-27 Закрытое Акционерное Общество "Сибирская Технологическая Компания "Цеосит" Способ переработки нефти и газового конденсата
RU2495085C1 (ru) * 2012-05-31 2013-10-10 Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Московский государственный университет тонких химических технологий имени М.В. Ломоносова" (МИТХТ имени М.В. Ломоносова) Способ переработки углеводородсодержащего сырья и устройство для его реализации

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2095863A (en) * 1936-01-09 1937-10-12 Freeman Nat Harris Extraction of volatile hydrocarbons from solid or high boiling point liquid hydrocarbons
US2700016A (en) * 1950-11-27 1955-01-18 Naumann Carl Distillation of high boiling hydrocarbons and products therefrom
SU1673854A2 (ru) * 1989-08-25 1991-08-30 Предприятие П/Я А-1846 Пьезометрический уровнемер

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