RU69064U1 - OIL REFINING SCHEME WITH SEPARATION UNIT (OPTIONS) - Google Patents

Abstract

The utility model relates to the oil refining industry, and specifically to the field of oil preparation and refining, including heavy oil, residues of oil refining and petrochemical industries, oil sludge, waste oils and other liquid organic media for their further advanced processing and can be used in the production of hydrocarbon fuel. The technical result, which is aimed at solving a utility model, consists in the implementation of a substantially comprehensive purification of the feedstock from many impurities at once, which allows further independent (without dilution with light oil) deep and cost-effective processing of heavy highly viscous oil and other hydrocarbon feedstocks with possible increased productivity and service life of standard equipment of the oil refinery. This goal is achieved by the fact that in the oil refining production scheme, before feeding the raw materials to the fractionation unit (AT or ABT), or immediately after it, a separation unit is included to produce high molecular weight high boiling fractions and the light separation part enriched in fuel compositions and depleted in harmful impurities. High boiling fractions contain tarry and asphaltene substances and most of sulfur, sulfur compounds, metals and other harmful substances that adversely affect oil refining. In the separation unit, in addition, in order to increase the depth of processing of raw materials and the yield of the target fuel compositions, a cracking process, for example, thermal or thermomechanical, is carried out simultaneously with its separation into two parts. 4 s.p. crystals, 2 ill., 1 tab.

Description

The utility model relates to the oil refining industry, and specifically to the field of oil preparation and refining, including heavy oil, residues of oil refining and petrochemical industries, oil sludge, used oils and other liquid organic media for their further in-depth processing to produce guest products and can be used in the production of hydrocarbon fuels.

The decrease in oil reserves of traditional fields increases interest in the production and, consequently, in the processing of heavy oil (Ratov AN, Nemirovskaya GB and others. Problems of oil development in the Ulyanovsk region. "Chemistry and technology of fuels and oils", No. 4, 1995). Heavy oil is understood to mean oil with a density of more than 900 kg / m ³ , as a rule, with a low content of light fractions and a high content of resinous - asphaltene substances and other harmful impurities. These features of the composition of heavy oil cause serious difficulties both in production and transportation - high viscosity and pour points, and during its processing - a significant content of various impurities, resins, asphaltenes, paraffins, etc., and low (mainly up to 30 % mass.) the content of fuel compositions - gasoline, kerosene and diesel fractions. Transportation of heavy oil is also significantly complicated due to the high content of tar-asphaltene substances and paraffins. Deposits on the working surfaces of equipment are the cause of its failure. And sulfur and metal compounds, especially vanadium, as well as chloride salts, usually found in such oil, have an increased corrosive effect on oil refining equipment.

Currently, heavy oils are processed in a mixture with conventional light oil. Nevertheless, even in this case, the processing process causes great damage to equipment and the environment. It can be expected that over time the problem of refining heavy oil will become more acute: on the one hand, the demand for refining of such oil increases, as the reserves of light oil are depleted, and the reserves of heavy oil are quite large all over the world, on the other hand, the composition of oil products on the content of sulfur and metals.

Thus, the preparation of heavy oil for refining is a process that determines the profitability of the entire refinery

production. The facilities for the preparation and primary processing of oil are the leading ones at oil refineries and the efficiency of their work largely determines the technical and economic indicators of the plant as a whole.

Known and widely used in industry are such methods of preparing the feedstock as dehydration and desalting of oil, as well as degassing. After the above oil treatment, it is heated and fed to the rectification unit, atmospheric or vacuum (depending on the set goal) processing. Next, light fractions are sent to commercial product units: a hydrotreating unit, a gasoline fraction is sent to an octane increasing unit (reforming, zeoforming, compounding, etc.). Heavy fractions (bottoms after an atmospheric tube) can be used as boiler fuel, for the production of oil products after a vacuum column, for the production of bitumen in a bitumen reactor and for the production of other heavy commercial products. The above methods (degassing, dehydration, desalting) of oil preparation in the oil refining scheme solve a certain narrow problem, but they do not allow to significantly purify the source oil from other harmful compounds, such as sulfur compounds, organochlorine, tar-asphaltene substances, paraffins that interfere further oil refining. Practically no methods are used in industry for the purification of initial oil (raw materials), especially heavy and sour, from sulfur compounds.

The technical result, which the proposed utility model is aimed at, consists in the implementation of a substantially comprehensive purification of the feedstock from many impurities at once, which allows further independent (without dilution with light oil) deep and cost-effective processing of heavy, highly viscous oil, bottoms and other hydrocarbon media with increasing productivity and service life of standard equipment of the oil refinery, as well as with increasing depth operations, i.e. an increase in the yield of light products (gasoline, kerosene and diesel fractions).

This object is achieved by the fact that in the technological scheme of processing liquid hydrocarbon raw materials, including the desalination and dehydration unit, fractionation units and production of commercial products, before the fractionation unit (before feeding to atmospheric AT or atmospheric vacuum AVT tubing), or after it, include separation unit, in which the feedstock is divided into two parts: the heavy part - high molecular weight high boiling fractions mainly with a boiling point of 340-380 ° C and above and containing ovnuyu part of sulfur compounds, resinous - asphaltene substances, metals and other

harmful impurities and components, the so-called separation residue (OR), and the light part of the separation of raw materials, which contains lower boiling fractions and is an "improved" oil containing significantly less harmful impurities, the so-called wide fraction of distillates (HFD), which contains mainly (about 90%) gasoline, kerosene and diesel fractions.

If the raw material is heavy oil, bottoms of oil refining and petrochemical industries, the organic part of oil sludge, waste oil and other residues, the oil refining operation scheme with a separation unit is shown in Fig. 1. Figures 1 and 2 indicate: 1 - separation unit, 2 - fractionation unit, atmospheric or atmospheric vacuum tube (AT or AVT), 3 - production products unit (hydrotreating, RF, reforming, platforming, zeoforming or at the first stage compounding block, etc., 4 - a bitumen block for the production of oxidized bitumen or a bitumen block combined with a vacuum block for the production of non-oxidized bitumen, as well as equipment for the production of bitumen coatings, emulsions, boiler fuel and other commercial products.

Dehydrated and desalted (at least partially) raw materials are fed to the separation unit (Fig. 1, position 1), in which the raw materials are divided into two parts: the light part is the wide fraction of distillates (HFD) and the heavy part is the remainder of the separation (OR), when in order to increase the depth of processing and yield of the target fuel fractions (gasoline, kerosene and diesel) in the separation unit, raw materials are cracked, for example thermomechanical, using hydrodynamic devices for sound, ultrasonic and cavitation processing of raw materials. A wide fraction of distillates, like high-potential oil, whose composition is close to gas condensate (the content of gasoline, kerosene and diesel fractions in the HFD is approximately 90%) after the separation unit (Fig. 1, position 1) is fed to the AT or ABT fractionation units (Fig. 1 , position 2). The gasoline and diesel fractions separated in the AT and ABT blocks are fed to the commercial products production block (Fig. 1, position 3). The bottom residue (fuel oil) after AT or ABT (FIG. 1, position 2) is returned to the separation unit (FIG. 1, position 1) for reprocessing and cracking. The remainder of the separation (OR) after the separation unit (Fig. 1, position 1) is fed to the production unit for commercial bitumen or other heavy commodity products (Fig. 1, position 4). The distillation after the bitumen block is returned to the separation block (Fig. 1, position 1) for reprocessing and cracking.

If the raw material for processing is medium or light oil, then the best option from the point of view of reducing energy costs, capital costs for equipment is the option of supplying raw materials first to the fractionation unit AT or ABT (figure 2, position 2), so that

do not crack light fractions of the source oil in the separation unit and reduce the performance of the separation unit. After AT or ABT (figure 2, position 2), gasoline and diesel fractions are fed to the unit for obtaining marketable products (figure 2, position 3), and bottoms (fuel oil) are fed for processing to the separation unit (figure 2, position one). From the separation unit (FIG. 2, position 1), the HFD is fed to the input of the AT or ABT units (FIG. 2, position 2) in addition to the feedstock together with it or separately, which leads to an increase in the processing depth, and OR is fed to the production unit bitumen (figure 2, position 4). The distillation after the bitumen block is returned to the separation block (figure 2, position 1) for reprocessing and cracking.

The option of constructing a separate block for the separation of heavy, sour, but cheap oil (or the remnants of oil refining and petrochemical industries) with obtaining the remainder of the separation and enriched in fuel fractions and depleted in harmful impurities SHF, is economically viable and quickly paid back. light and significantly more expensive oil. Even more profitable is the option of processing the proposed technology of used machine oils, old fuel oils and oil sludges. The yield of fuel fractions is up to about 60-80%, depending on the type of raw material. The remainder of the separation (it will be approximately 20-40%) is a waste-free raw material for bitumen production. ShFD is sold as a high-potential (fuel fraction content of approximately 90%) oil with a low content of harmful impurities. In this embodiment, the process of obtaining marketable products (gasoline, kerosene, diesel fuel, bitumen, etc.) from intermediates (HFD and OR) obtained after the separation unit is remote from the enterprise and the site on which the separation unit is located, and may organizationally belong to others enterprises, regions, countries. For this, one or both parts of the separation (SHF, OR) are sent to cooling units to obtain intermediate products with the aim of transporting them to the place of further processing and obtaining marketable products. Effectively, both parts of the separation (SHF and OR) after the separation unit are sent to a mixing device for producing synthetic oil with an increased potential content of light fuel products and a significantly lower density and viscosity in comparison with the feedstock.

OR contains the main amount of harmful impurities that are not involved in the further processing of “improved” oil. For example, for oil produced in the Ulyanovsk region, the mass fraction of sulfur and sulfur compounds in the “improved” oil after the release of OR decreases from 4-5% of the mass. up to 0.5-0.7% of the mass. Accordingly, the mass fraction of chlorides is from 500-5000 mg / l to 20 mg / l. In addition, the majority of metals, such as vanadium, also go into OR. At the stage of allocation of PR, in addition, at the same time can be carried out

cracking process, for example, thermal or thermomechanical. This increases the amount of light fractions in the feedstock for further processing at standard refinery equipment. At the stage of hydrotreating from sulfur, gasoline fractions after AT or ABT come with a content of 0.1-0.2%. Such a content of sulfur and sulfur compounds corresponds to their level during the processing of low-sulfur oil, for example, West Siberian. The remainder of the OP separation in an amount dependent on the composition of the oil is then sent directly to obtain marketable products: bitumen or other heavy products (bitumen emulsions and coatings, boiler fuel, pitch, coke, etc.). For Ulyanovsk oil, this amount is 25-30% of the mass of the original oil. Sulfur compounds do not interfere with the production of quality bitumen. It is believed that the sulfur compounds of the processed raw materials do not play a direct role in the conversion reactions, but are oxidation accelerators in the process of bitumen production, as well as plasticizers. This reduces the time of the oxidation process and the products of such accelerated methods have a smaller change in consistency with a change in temperature (Gruze V.A., Steven D.R. Oil refining technology. L., Chemistry, 1964, p. 550, 551).

As a result of using the separation unit in the oil refining scheme, fractions with a boiling point of 340-380 ° C are obtained not at the end of the sequence of stages AT or ABT, but at the beginning of the refining process. After the isolation of OP, the further sequence of stages of oil refining does not differ from the sequence of stages of refining light oil. In this case, the refinery equipment operates in a sparing mode, since it does not process heavy initial high-viscosity oil containing undesirable impurities from the point of view of preserving the resource of the equipment and the quality of the products obtained, but “improved” oil enriched with light in relation to the initial oil, fractions with a boiling point up to 360 ° C, and depleted in harmful impurities. The resource of equipment during the processing of heavy oil in this case (subject to preliminary allocation of PR) is not less than the resource of the corresponding equipment for processing light oil. Isolation of its heavy part (OR) from raw materials in an amount of about 20-40% (depending on the composition of the raw materials) reduces the subsequent material flow of raw materials for processing, but with an increase in light fractions due to cracking of the raw materials in the separation unit. Technological devices may be of less capacity, but at the same time the quantity of light petroleum products obtained is maintained or increased, or productivity can be increased on the same equipment. This is due to the fact that OP does not go through the entire technological chain of AT, ABT, etc. devices, but is removed at the beginning of the technological process and is sent further as raw materials for the production of bitumen and other heavy products.

The separation process can be implemented using an evaporator, the design of which is similar to the well-known and widely used evaporator-heat exchanger with a steam (vapor-gas form - HFD) space (A. Dekhterman. Oil refining according to the fuel version. M., Chemistry, 1988, p. 23). Unlike simple heat exchangers, this apparatus has enough volume to evaporate the heated product. The evaporator is a cylindrical tank. At the bottom of its housing is an integrated tubular heat exchanger. Inside the tubes of the heat exchanger serves a coolant for heating the product (oil). Typically, water vapor is used as a heat transfer medium. A light portion of the oil (feedstock) evaporates and is discharged through the top fitting. The remaining oil is poured through the drain plate and is discharged through the corresponding fitting. The amount of evaporated part of the oil depends on the temperature in the apparatus, that is, on the surface of the heat exchanger and the temperature of the coolant. Water vapor also satisfies other requirements for heat carriers: availability, fire safety, etc. The main disadvantage of water vapor is a significant increase in pressure with increasing temperature, therefore, to obtain a temperature in the apparatus in the range of 350-450 ° C, it is better to use high-temperature heat carriers. It is advisable to use as high-temperature coolants: high-boiling organic liquids, molten salts or liquid metals, high-temperature gaseous coolants (Kasatkin AG, Main processes and apparatuses of chemical technology. M., “Chemistry”, 1971, p.334-338).

The proposed scheme was implemented in a pilot unit for the separation of oil with a capacity of up to 0.2 t / h.

As the source of raw materials used oil field Vishenskoye Ulyanovsk region. (Ratov AN, Nemirovskaya GB and other problems of oil development in the Ulyanovsk region. "Chemistry and technology of fuels and oils", No. 4, 1995). Oil contains a significant amount of resinous compounds and impurities. To study the applicability of this refining scheme, oil and other fields were used, respectively, with a different composition. At this installation, the technological process of separation of raw materials is worked out. Comprehensive analyzes of the composition of the obtained fractions were made: high-boiling fractions with a boiling point of 340-380 ° C (OR) and “improved” oil (HFD). Their properties were studied for the purpose of further processing according to the classical scheme. Further processing of the “improved” oil was carried out, reproducing most of the operations according to the classical scheme in order to obtain fuel components and study their properties.

The table shows a typical fractional composition of the source oil (Vishenskoye field, Filippovskaya group. Ulyanovsk region) and products of the separation process according to the proposed scheme

refining said oil into light (SHF) and heavy (OR) parts. The content of selicagel resins in the light part of the separation decreased compared to the original oil from 18.4 to 1.1% by weight, asphaltenes from 3.0 to 0.06% by weight, coking ability decreased from 8.6 to 0.2 %, and ash content from 0.069 to 0.002%. For comparison, the same table shows the fractional composition of light West Siberian oil, Samotlor field. As can be seen from the data presented, when the OR fraction is extracted from the original oil in an amount of about 25-30% (mass.), The viscosity of the HFD is significantly reduced and it is enriched by cracking with light hydrocarbons. In this case, the bulk of the impurities goes into the OP. Recalculation of the amount of products obtained for the initial heavy oil shows that the yield of light fractions with a boiling point up to 350 ° C is 55-59%, i.e. twice as much as the original heavy oil (Vishenskoye field, Filippovskaya group. Ulyanovsk region). This amount is comparable to the potential yield of similar products from light Samotlor oil.

Properties of oil of the Ulyanovsk region, West Siberian oil and oil products obtained in a pilot installation with a separation unit.

Table Product Density,
g / cm ³ Viscosity,
cSt Sulfur,
% Chlorides
mg / l The yield of fractions,% before
200 ° C up to 350 ° C Cherry Oil 0.9482 72.9 (50 ° C) 3.91 500-5000 8.3 30,0 Samotlor Oil 0.8426 6.1 (20 ° C) 0.96 500-1500 30.6 58.2 ShFD ("improved" oil) 0.79-0.81 1.8 (20 ° C) 0.5-0.7 20-30 23-28 * 55-59 * OR 0.99-1.1 260 (50 ° C) 5.0-6.0 1000-3000 0 5-6 * * In terms of the original oil before separation.

Thus, the proposed utility model — a scheme of oil refining production with a separation unit — allows for complex preparation and purification of feedstock from many impurities at once, which makes it possible in the future to carry out independent (without dilution with light oil) in-depth and highly profitable processing of heavy high-viscosity oil, oil refining residues and petrochemical industries with a possible increase in productivity and service life of standard equipment for oil refining Avoda. This goal is achieved by introducing into the refinery scheme a separation unit for separating high-boiling oil fractions (OR) in the initial stage of oil refining, containing mainly products with a boiling point of 340-380 ° C and above, which contain the main amount of harmful impurities of the original oil, which are then used for the preparation of heavy commercial products such as bitumen, boiler fuel, pitch, coke, etc., and the second part of the separation is the light part of oil (HFD), enriched in target fractions and depleted in harmful and impurities — they are sent for further processing to obtain light oil products (gasoline, kerosene, diesel fuel) using standard equipment of oil refineries, and to increase the potential content of light fuel compositions in the light part of the separation in the separation apparatus, thermal or thermomechanical cracking of the raw materials is carried out by installing apparatus for separating cavitation, sound and ultrasonic devices for hydrocarbon liquids.

Claims (4)

1. Scheme of oil refining production with a separation unit for the preparation and processing of oil, including heavy oil, residues of oil refining and petrochemical industries and other liquid organic media, including desalination and dehydration processes, as well as fractionation and production of commercial products, characterized in that the production scheme before the fractionation unit (before feeding to atmospheric AT or atmospheric vacuum AVT tubing), or after it, include a separation unit, in which e raw materials are divided into two parts: the heavy part of the separation is high molecular weight high-boiling fractions containing mainly products with a boiling point of 340-380 ° C and above, in which the bulk of the harmful components and impurities of the feedstock are concentrated, which are then used to prepare heavy commercial products such as bitumen, pitch, coke, boiler fuel, etc., and the light part of the separation of raw materials, enriched in target fuel fractions and depleted in harmful impurities, which is sent to the next processing to obtain light petroleum products (gasoline, kerosene, diesel fuel), and to increase the depth of processing in the separation unit, the process of cracking the feedstock is carried out. 2. The scheme according to claim 1, characterized in that one or both parts of the separation are sent to cooling units to obtain intermediates for the purpose of their transportation to the place of further processing and obtaining marketable products. 3. The scheme of the plant according to claim 1, characterized in that both parts of the separation are sent to a mixing device for producing synthetic oil with an increased potential content of light fuel products and a significantly lower density and viscosity in comparison with the feedstock. 4. The circuit according to claim 1, characterized in that in the separation unit, thermal or thermomechanical cracking of the raw material is carried out by installing cavitation, sound and ultrasonic effects on hydrocarbon liquids in the separation unit.