RU34530U1 - Installation for hydrocarbon processing - Google Patents

Installation for hydrocarbon processing Download PDF

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Publication number
RU34530U1
RU34530U1 RU2003122471/20U RU2003122471U RU34530U1 RU 34530 U1 RU34530 U1 RU 34530U1 RU 2003122471/20 U RU2003122471/20 U RU 2003122471/20U RU 2003122471 U RU2003122471 U RU 2003122471U RU 34530 U1 RU34530 U1 RU 34530U1
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RU
Russia
Prior art keywords
column
heat exchanger
output
air
cooling
Prior art date
Application number
RU2003122471/20U
Other languages
Russian (ru)
Inventor
Б.Е. Сельский
А.А. Смотрич
Е.А. Лихтер
Original Assignee
Сельский Борис Евсеевич
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Application filed by Сельский Борис Евсеевич filed Critical Сельский Борис Евсеевич
Priority to RU2003122471/20U priority Critical patent/RU34530U1/en
Application granted granted Critical
Publication of RU34530U1 publication Critical patent/RU34530U1/en

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Abstract

A hydrocarbon processing plant, comprising a series-connected furnace, first and second distillation columns, first, second and third heat exchangers, first, second, third and fourth air-cooling units, an evaporator and a separator, the inlet of which is connected to the output of the second heat exchanger, and the output is light fractions of which are connected to the output of the gasoline fraction of the second distillation column, and the condensate outlet is fed into the furnace through the pipe space of the third heat exchanger, the output of the heavy residue from the bottom of the first column is fed through the evaporator to recover heat and heat the bottom of the second column to the third air-cooling apparatus for condensing boiler fuel, the output of the lower product of the second column is sent through the evaporator and second heat exchanger to the second air-cooling apparatus for condensing boiler fuel, and the fourth air cooling is connected to the output of the intermediate kerosene fraction of the second column, characterized in that the distillation columns are installed in this way ohm, that their bottom is raised to a height from a zero mark of at least four diameters of the column body, the second heat exchanger along the middle generatrix of its diameter is installed at a height of at least four diameters of the shell of the heat exchanger from the zero mark, and the third heat exchanger is located not lower than the raw material inlet into the second column moreover, the first heat exchanger at the outlet pipe from the pipe space is located 0.3 m above the inlet fittings in the first air cooling apparatus.

Description

Installation for hydrocarbon processing
The utility model relates to the oil and gas refining industry, in particular, to primary methods for processing hydrocarbon raw materials by dividing it into fractions, i.e. distillation.
Known installations for the distillation of hydrocarbons using distillation columns (I.L. Gurevich, "Oil and gas processing technology, part 1, Publishing house" Chemistry, Moscow, 1972, p. 202-203).
These installations are complex and expensive, require special equipment operating in the factory. Known distillation of oil with a single evaporation (I. L. Gurevich, "Technology of oil and gas processing, part 1, Publishing house" Chemistry, Moscow, 1972, S. 199-202). Installation for its implementation is simpler, requires less heat.
Its disadvantage is the poor clarity of the separation of oil into fractions, the low efficiency of the process.
The objective of the utility model is to increase the efficiency of the installation due to a clearer separation of hydrocarbon feedstock into fractions, as well as reducing energy consumption and lowering the cost of the installation.
The problem is solved by the installation for processing hydrocarbon raw materials containing a series-connected furnace, first and second distillation columns, first, second and third heat exchangers, first, second, third and fourth air cooling units, an evaporator, a separator, the input of which is connected to the output of the second heat exchanger , and the output of light fractions of which is connected with the output of the gasoline fraction of the second column, and the condensate outlet is fed into the furnace through the pipe space of the third heat exchanger, the output is th residue from the bottom of the first column is fed through an evaporator for heat recovery and heating of the bottom of the second column to the third air cooling apparatus for condensing boiler fuel, and
2003122471
: MPKS10O7 / 00
boiler condensation condensation, and the fourth air-cooling apparatus is connected to the output of the intermediate kerosene fraction of the second column, in which, unlike the prototype, distillation columns are installed in such a way that their bottom is raised to a height of at least four diameters of the column body, the second heat exchanger in the middle its forming diameter is installed at a height from a zero mark of at least four diameters of the heat exchanger body, and the third heat exchanger is located not lower than the raw material inlet in the second column, and the first heat exchanger at the outlet of the pipe space is located above the inlet fittings in the first air cooling apparatus no more than the size of the diameter of the heat exchanger body.
The process of separation of hydrocarbon feedstocks at the proposed plant is based on the scheme of a single distillation of hydrocarbons with the simultaneous evaporation of the entire “light part of the feedstock in one distillation column, followed by their separation into fractions in another column. At the same time, the introduction of an evaporator as an intermediate heat exchanger into the installation allows condensing the diesel fraction before entering the “light fractions” into the second distillation column, thereby the second column is unloaded through hydrocarbon vapors, which significantly affects the quality of the rectification and the plant’s performance.
The output of the intermediate kerosene fraction can improve the quality of the gasoline fraction (reduce the content of heavy fractions) and the diesel fraction (reduce the content of light fractions, i.e., increase the flash point, viscosity).
The arrangement of plant elements, proposed in accordance with the essence of the utility model, relative to the zero mark allows its operation without pumps due to the natural overflow of components of the processing process. This leads to a significant reduction in energy consumption, an increase in reliability due to the simplification of the installation.
The essence of the utility model is illustrated by the drawing, which presents
schematic diagram of a plant for processing hydrocarbon feedstocks.
The installation comprises a furnace 1, first 2 and second 3 distillation columns, first, second and third heat exchangers, respectively 4, 5, 6, an evaporator 7, first, second, third, fourth air-cooling units, respectively 8, 9, 10, 11, separator 12 technological capacities 13,14,15,16.
Distillation columns 2 and 3 are installed at a height of at least 2 from the zero mark of at least four diameters of the column body. The first heat exchanger 4 along the outlet pipe from the pipe space is located 0.3 m above the inlet fittings in the first air cooling apparatus 8 no more than the size of the diameter of the heat exchanger body. The second heat exchanger 5 is installed at a height from a zero mark of at least four diameters of the heat exchanger body. The third heat exchanger 6 is located not lower than the inlet fitting of raw materials into the second column.
Installation works as follows.
Hydrocarbon feed from the commodity stock is pumped into the annulus of the first heat exchanger 4, where it is heated by the flow of the gasoline fraction from the top of the second column, then into the tube space of the second heat exchanger 5, in which it is heated by the flow of diesel fraction. After this, the feed stream is directed by gravity to the separator 12 for preliminary removal of light gasoline fractions from it, which are fed into the gasoline fraction stream from the second column 3 in front of the first air-cooling apparatus 8. The condensate from the separator 12 is gravity-fed is sent to the pipe space of the third recuperative heat exchanger 6, where is heated by a stream of a wide fraction coming from the top of the first column 2, and enters the furnace 1. Heated in the furnace to a temperature of 283 - 295 ° C, the raw material enters the bottom of the first distillation to columns 2: A broad fraction (a mixture of gasoline, kerosene and diesel fractions) is discharged on top of the first column 2, a heavy residue of over 340 s OZ / -) /
3 360 ° C. cap irrigation on the plates is created by feeding
parts of the diesel fraction to the top of the column.
The heavy residue from the bottom of the nerve column 2 is sent to the evaporator 7 to recover heat and heat the bottom of the second column 3, after which it is cooled in the third air-cooling apparatus 10 and enters the tank 16 (boiler fuel) with a temperature not exceeding 70 ° С. The upper product of the first column 2 is cooled, passing through the annulus of the third heat exchanger 6, and flows by gravity to the lower part of the second column 3, and the diesel fraction is mainly already in the liquid phase.
A gasoline fraction is taken from the top of the second column 3, which is first sent to the first heat exchanger 4 (tube space), where it gives its heat to the feed stream, then mixes with the light gasoline fraction from the separator 12. The total stream is cooled down in the first air-cooling apparatus 8 and enters in tank 13 (gasoline fraction).
A kerosene fraction is taken from the second column 3 by lateral distillation, which is sent through the fourth air-cooling apparatus 11 to the technological vessel 4. The lower product of the second column — the diesel fraction — is sent to recover heat to the second heat exchanger 5 (through the evaporator 7), then it is supplied to the after-cooling unit the second air-cooling apparatus 9 and from there to the tank 15 (diesel fraction).
Thus, the claimed utility model allows you to create a small tonnage fractionating unit that provides efficient and clear separation of hydrocarbon feeds into fractions, while the proposed arrangement of the unit's units relative to the zero mark provides a reduction in energy consumption and its cost reduction, as well as an increase in reliability.
4

Claims (1)

  1. A hydrocarbon processing plant comprising a series-connected furnace, first and second distillation columns, first, second and third heat exchangers, first, second, third and fourth air-cooling units, an evaporator and a separator, the inlet of which is connected to the output of the second heat exchanger, and the output is light fractions of which are connected to the output of the gasoline fraction of the second distillation column, and the condensate outlet is fed into the furnace through the pipe space of the third heat exchanger, the output of the heavy residue from the bottom of the first column is fed through the evaporator to recover heat and heat the bottom of the second column to the third air-cooling apparatus for condensing boiler fuel, the output of the lower product of the second column is sent through the evaporator and second heat exchanger to the second air-cooling apparatus for condensing boiler fuel, and the fourth air cooling is connected to the output of the intermediate kerosene fraction of the second column, characterized in that the distillation columns are installed in this way ohm, that their bottom is raised to a height from a zero mark of at least four diameters of the column body, the second heat exchanger along the middle generatrix of its diameter is installed at a height of at least four diameters of the shell of the heat exchanger from the zero mark, and the third heat exchanger is located not lower than the raw material inlet to the second column moreover, the first heat exchanger at the outlet of the pipe space is located 0.3 m above the inlet fittings in the first air-cooling apparatus.
    Figure 00000001
RU2003122471/20U 2003-07-21 2003-07-21 Installation for hydrocarbon processing RU34530U1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
RU2003122471/20U RU34530U1 (en) 2003-07-21 2003-07-21 Installation for hydrocarbon processing

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
RU2003122471/20U RU34530U1 (en) 2003-07-21 2003-07-21 Installation for hydrocarbon processing

Publications (1)

Publication Number Publication Date
RU34530U1 true RU34530U1 (en) 2003-12-10

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Family Applications (1)

Application Number Title Priority Date Filing Date
RU2003122471/20U RU34530U1 (en) 2003-07-21 2003-07-21 Installation for hydrocarbon processing

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RU (1) RU34530U1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2683267C1 (en) * 2018-10-01 2019-03-27 Александр Владимирович Данилов Installation for processing liquid hydrocarbons

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2683267C1 (en) * 2018-10-01 2019-03-27 Александр Владимирович Данилов Installation for processing liquid hydrocarbons

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Legal Events

Date Code Title Description
MM1K Utility model has become invalid (non-payment of fees)

Effective date: 20070722