RU2191800C2 - Method of primary distillation of hydrocarbon raw material (gas condensate and oil) - Google Patents

Abstract

FIELD: technological systems of module-type low-tonnage plants for development of small gas condensate and oil fields for local service pertaining to motor, boiler and furnace fuels. SUBSTANCE: preheated raw material is fed to separator-flash box at simultaneous delivery of non- condensed hydrocarbons ejected by flow of raw material fed to separator- flash box. Liquid separated in separator and additionally preheated vapor phase are directed in counter flow to absorption evaporation phase separator whose vapor phase is condensed and discharged to gasoline fraction product reservoir. One part of non-condensed hydrocarbons is discharged in form of fuel gas and remaining part is ejected by raw material flow into first-stage separator. Liquid phase (residue) thus obtained is directed from first evaporation stage to second evaporation stage. Mazut is introduced as liquid phase in form of residue. EFFECT: enhanced efficiency of procedure; facilitated procedure of distillation at minimum amount of equipment; enhanced operational safety; enhanced accuracy of separation; increased yield of white distillates. 1 dwg

Description

 The invention relates to the field of oil refining industry and can be used to produce motor and boiler fuel from hydrocarbon feedstocks.

 Known methods for the distillation of hydrocarbons in atmospheric tubular installations. In addition to pumps and heat exchange equipment, the installation includes tube furnaces and distillation columns. Small-tonnage distillation plants for primary distillation repeat the fundamental technological solutions of similar plants in oil refineries ([1]. G.A. Lastovkin et al. “Oil Refinery Handbook”. 1986, [2] V.N. Erlikh et al. “Chemistry and Technology oil and gas ". 1985, [3] SP Pavlova et al." Field processing of gas condensates and production of motor fuels. A review series. Preparation and processing of gas condensate ". Issue 3 VNIIEGAZprom. 1982 (L. 1), (A.2), (A.3)).

 Given the high cost and complexity of operation of small-tonnage installations for the production of motor fuel, performed according to the technological scheme of large-capacity refineries using distillation columns and tube fired furnaces, non-traditional technological solutions for the primary distillation of hydrocarbon raw materials are developed.

 So, for example, in the USA, such plants are used for the production of diesel and gas turbine fuels from pumped oil to cover the fuel demand for the drive of main oil pipeline pumps.

 “Typically, low-capacity refineries have a high capital cost, and their operation is expensive. Such refineries are used to produce diesel and gas turbine fuels from oil pumped through a pipeline. Typically, such refineries use the same oil distillation scheme as large-capacity and already The use of a distillation column alone makes such a plant uneconomical.

 Two units in Louisiana successfully tested multi-stage oil evaporators with heat supply from a circulating liquid coolant; a third such facility will be built in Texas. The capacity of each unit is 100,000 tons per year, but can be brought up to 500,000 tons per year "([4] Express information" Oil refining and petrochemicals "VNIIENEFTECHIM. 1980. 14 (L.4)).

 Closest to the technical nature of the claimed method (prototype) is the technological scheme of small-tonnage installations for producing motor fuels from hydrocarbon raw materials in the places of its production (L.3).

 The disadvantage of this technology is the large range of equipment, similar to large-scale oil refineries (refineries); equipping the installation with distillation columns and fire furnaces greatly complicates operation and safety, which is exacerbated by the low technological equipment of small-tonnage installations compared to refineries.

The aim of the invention is the creation of technology for small-tonnage production of light petroleum products and boiler and furnace fuel - simple and reliable in operation, with a minimum range of equipment and low investment; ensuring stable operation in conditions of significant fluctuations in the load of raw materials and changes in the composition of raw materials due to the use of non-condensed hydrocarbons as stripping gas, more complete extraction of light fuel fractions with a boiling point NK 35 ^o С - КК 130-180 ^o ; HK 130-180 ^o KK 360 ^o C and the remainder is fuel oil (SU 1074891).

 A schematic flow chart of the proposed method is presented in the drawing and includes the following devices: raw material heater (1), ejector (2), separator-separator (3), vapor phase heater (4), absorption-stripping phase separator filled with nozzle (5), condenser-cooler (6), separator (7), fraction collectors (8).

 The second stage of evaporation consists of similar equipment.

Hydrocarbon raw materials are heated in a heat exchanger (1) to a temperature of 180-220 ^o C depending on the potential content of gasoline and hydrocarbon components that determine the octane number of gasoline, fed through an ejector (2) to a separator expander (3). The boiling of heated raw materials and their separation into vapor and liquid phases in the separator expander (3) occurs in the presence of non-condensing hydrocarbons ejected by the raw materials, which are an active stream in the ejector (2). After mixing with hot raw materials, the ejected non-condensing hydrocarbons overheat to a temperature of 180-220 ^o C and, after throttling in the ejector, serve as exhaust gases, significantly increasing the yield of light fractions (SU 1074891).

 The right phase, the gasoline fraction overheats in the heat exchanger (4) and, as a blowing agent, is sent to the lower part of the adsorption-stripping phase separator, the liquid phase is supplied countercurrently.

 During the interaction of flows in the lower part of the adsorption-stripping separator, the light fractions are blown off with the superheated vapor phase and enriched with low-boiling components, in the upper part, the high-boiling components are absorbed by the liquid phase, the vapor phase (gasoline fraction) is depleted with heavy hydrocarbons: the liquid phase is from the phase separator of the first stage is the raw material for the subsequent stage of evaporation. The vapor phase of the second stage is the diesel fraction, and the liquid phase is the residue, fuel oil.

 Excess non-condensed hydrocarbons are removed from the system and used as fuel gas.

 To obtain fuel fractions, a unified evaporation module is used. The nominal capacity of the module for raw materials is 100,000 tons per year, the minimum and maximum productivity, respectively - 70,000 and 120,000 tons per year.

Claims (1)

 The method of primary distillation of hydrocarbon feedstocks (gas condensate and oil), including its heating and double evaporation using separators and ejectors and producing liquid and vaporous hydrocarbon fractions, characterized in that the heated feed is fed to a separator expander simultaneously with the supply of non-condensing hydrocarbons ejected the flow of raw materials supplied to the separator expander, after which the separated liquid and the additionally heated vapor phase are directed countercurrently into absorption-stripping phase separator, the vapor phase from which is condensed and taken into the gasoline fraction product tank, one part of non-condensing hydrocarbons is discharged in the form of fuel gas, and the remaining part is ejected by the feed stream into the separator of the first stage, the obtained liquid phase (residue) from the first stage is sent to the second stage stage of evaporation, and as a liquid phase, fuel oil is removed as a residue.