WO1997043355A1 - Procede et installations de fractionnement du petrole brut - Google Patents

Procede et installations de fractionnement du petrole brut Download PDF

Info

Publication number
WO1997043355A1
WO1997043355A1 PCT/RU1997/000124 RU9700124W WO9743355A1 WO 1997043355 A1 WO1997043355 A1 WO 1997043355A1 RU 9700124 W RU9700124 W RU 9700124W WO 9743355 A1 WO9743355 A1 WO 9743355A1
Authority
WO
WIPO (PCT)
Prior art keywords
πaροv
gasoline
vapours
gas
πρeimuschesτvennο
Prior art date
Application number
PCT/RU1997/000124
Other languages
English (en)
Russian (ru)
Inventor
Valery Georgievich Leontievsky
Anatoly Georgievich Korolkov
Original Assignee
Valery Georgievich Leontievsky
Anatoly Georgievich Korolkov
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.)
Filing date
Publication date
Application filed by Valery Georgievich Leontievsky, Anatoly Georgievich Korolkov filed Critical Valery Georgievich Leontievsky
Priority to AU30505/97A priority Critical patent/AU3050597A/en
Publication of WO1997043355A1 publication Critical patent/WO1997043355A1/fr

Links

Classifications

    • 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
    • C10G7/00—Distillation of hydrocarbon oils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination

Definitions

  • the invention is subject to the processing of oil and gas condensates.
  • the gasoline burns 5 and is packaged in a furnace, and the resulting liquid is inactive during the process, Benzin ⁇ vye ⁇ a ⁇ tsii ⁇ dyaschie ve ⁇ m ⁇ l ⁇ nny, and ⁇ lazhdayu ⁇ ⁇ ndensi ⁇ uyu ⁇ , ⁇ v ⁇ dya ⁇ e ⁇ l ⁇ in ⁇ uzhayuschuyu s ⁇ edu, ⁇ v ⁇ dya ⁇ iz0 se ⁇ a ⁇ a ⁇ a su ⁇ y gas Part ⁇ ndensa ⁇ a v ⁇ zv ⁇ aschayu ⁇ on ⁇ shenie ⁇ l ⁇ nny, balans ⁇ v ⁇ e ⁇ liches ⁇ v ⁇ ⁇ ndensa ⁇ a na ⁇ avlyayu ⁇ to further ⁇ e ⁇ e ⁇ ab ⁇ u.
  • the side dishes are cooled first in the heat exchangers, by eating the cooler, then they are cooled in the end coolers, and 5 are removed from the system. From the atmos- phere, the fans dispose of fuel oil and direct them to further processing.
  • the drawbacks of the described analogue are increased energy consumption due to the loss of energy, due to the low degree of heat recovery, and increased
  • ⁇ therein is ⁇ dnuyu ne ⁇ nag ⁇ evayu ⁇ ⁇ e ⁇ l ⁇ m ⁇ ndensatsii benzin ⁇ vy ⁇ ⁇ a ⁇ v, d ⁇ g ⁇ evayu ⁇ za ⁇ em d ⁇ 120 ° C ⁇ e ⁇ u ⁇ e ⁇ a ⁇ ivny ⁇ ⁇ e ⁇ l ⁇ bmenni ⁇ a ⁇ , and ⁇ bess ⁇ livayu ⁇ ⁇ bezv ⁇ zhivayu ⁇ in ele ⁇ degid ⁇ a ⁇ a ⁇ , nag ⁇ evayu ⁇ hereinafter ⁇ e ⁇ u ⁇ e ⁇ a ⁇ ivny ⁇ ⁇ e ⁇ l ⁇ bmenni ⁇ a ⁇ d ⁇ 260 ° C and se ⁇ a ⁇ i ⁇ uyu ⁇ .
  • Vapors and gases in the unit are protected by water, after which they are transferred to the atmosphere and liquid phase is sent to the furnace.
  • the liquid effluent from the furnace having a temperature of 340-350 ° C, is discharged to the atmospheric chamber.
  • the possibility of compensation for lateral losses is caused by a circulatory system, giving rise to a malfunction.
  • the vapors of the tower are condensing, giving way to the warm source.
  • the gas phase from the gasoline fraction is sucked out by the compressor, the liquid phase is partially returned to the environment, the balance of the liquid is inactive to the Otherwise, there is a stable stabilization of fatty gas, which, together with a cooled gas, is used to dispense deethanization.
  • the main product of the deethanization is dry gas, which is directed to the furnace and then to the blower to the atmospheric and industrial gases, the lower product is the product (lower product).
  • thermal oil derived from an atomic ring. Petroleum products are dry and liquefied gases, light and heavy gasolines, kerosin, diesel oil, atmospheric gas oil and heavy fuel oil.
  • the benefits of the selected products are increased energy costs and increased cost-effectiveness of the economy. The cost is due to the low degree of heat recovery and, therefore, the use of single gasoline and the use of gasoline fractions are used.
  • the invention solves the problem of reducing energy consumption on the extraction and reduction of material consumption of basic equipment.
  • Task ⁇ eshae ⁇ sya ⁇ em, ch ⁇ in s ⁇ s ⁇ be, v ⁇ lyuchayuschem s ⁇ u ⁇ encha ⁇ y ⁇ e ⁇ u ⁇ e ⁇ a ⁇ ivny nag ⁇ ev ne ⁇ i ⁇ dyaschimi and tsi ⁇ uli ⁇ uyuschimi ⁇ ami, mezhs ⁇ u ⁇ encha ⁇ e ele ⁇ bess ⁇ - Riverside ⁇ delenie and ⁇ myv ⁇ u ⁇ a ⁇ v, ⁇ sleduyuschy nag ⁇ ev and u ⁇ a ⁇ ivanie ne ⁇ yan ⁇ g ⁇ ⁇ s ⁇ a ⁇ a, ⁇ a ⁇ tsi ⁇ ni ⁇ vanie ⁇ a ⁇ v and zhid ⁇ y ⁇ azy in ⁇ l ⁇ nne with is ⁇ lz ⁇ vaniem ⁇ s ⁇ g ⁇ and tsi ⁇ uly
  • the non-volatile residual heat up the transient with interstitial separation of the steam i.e. with activity in the distillation process.
  • the indicated steam and liquid supply are introduced separately and into various zones, i.e. It distributes at a high level, and, therefore, the critical cross-section is at the place of the input of liquid quick-charge due to the large volume of gas due to the large volume of gas.
  • the consequent section of the column will be substantially smaller.
  • the well-known large-scale enterprises organize sluggish cleaning processes with large quantities of large, high light-weighted quantities and small, small ones. At this height, the crones reach 36–40 meters.
  • the server works as a diesel engine and has one side.
  • the easy digestion numbers of the disappearing and enlarging section are small, the number of cars is reduced, the height is more than 10-12 meters. As a result, the cross-section and height are reduced, the material consumption is reduced, and energy costs are reduced.
  • the invention solves the problem of reducing energy consumption for the reduction and reduction of material used in basic equipment.
  • source 1 affecting coefficient 2; end-rooms 3, 4, 5; Party 6; pump 7; electrical dehydration 8; Evaporators 9, 10, 11; parties 12, 13, 14; stove 15; interstitial unit 16; Column 17; hydrocarbon feed gas heater 18; carbon dioxide of the gas 19; stabilization block 20; the final refrigerator 21; battery 22; condensation section 23; the end ⁇ warehouse 24; Saturday 25, 26, 27, 28, 29; collector fuel gas 30; pump 31; compression pump 32; pumps 33, 34; gasoline average 35; lightweight kerosene 36; heavy rubber heavy 37; dry gas 38; gas liquefied gas 39; 40% stabilized gasoline; fuel oil 41; diesel engine 42.
  • model carbohydrates are delivered to the processing plant (composition of fractions in% of the mass):
  • the original source of 1 in the amount of 14.75 kg / sec at a pressure of 0.75 PS, at a temperature of 20 ° C is divided into four flows at a ratio of 7: 0.5: 1: 1.5.
  • the first basic outlet will open up the operating condenser 2, the others in the final refrigerators 3, 4, 5 are respectively. They cool down to 40 ° C and are available with the installation of kerosene and petrol fractions. I hope that in the end-use refrigerators, it is possible to introduce an operable condenser. Leaving from a condensing condensate and heated to 139 ° ⁇ , a quick liquid separates the pressure at a pressure of 6 p.p.
  • ⁇ y ⁇ i ⁇ ayuschie in is ⁇ a ⁇ i ⁇ elya ⁇ ⁇ i s ⁇ u ⁇ encha ⁇ m ⁇ e ⁇ u ⁇ e ⁇ a ⁇ ivn ⁇ m ⁇ d ⁇ g ⁇ eve ne ⁇ i ⁇ a ⁇ y ⁇ a ⁇ tsy 67-92 ° C, 92-133 ° C, 133-206 ° C (n ⁇ m. Pressure.)
  • ⁇ benzinennuyu and chas ⁇ ichn ⁇ ⁇ e ⁇ sinennuyu ne ⁇ is ⁇ a ⁇ i ⁇ elya from 11 to 10.07 ⁇ liches ⁇ ve ⁇ g / se ⁇ na ⁇ avlyayu ⁇ in ⁇ ech 15. ⁇ ⁇ e ⁇ v ⁇ y s ⁇ u ⁇ eni ⁇ echi ne ⁇ nag ⁇ evayu ⁇ d ⁇ 318 ° C Pressure 0.32 ⁇ d ⁇ Pa, ⁇ i e ⁇ m ⁇ eimusches ⁇ venn ⁇ ⁇ e ⁇ sin ⁇ vye and Part dizelny ⁇ ⁇ a ⁇ tsy Convert to a vapor phase with a boiling point of 260 ° C at normal pressure.
  • Cross-seperate 16 and industrial steams are available in quantities of 1,473 kg / sec. In total 17 on-line.
  • the remaining liquid phase in the amount of 8.624 kg / sec at a pressure of 0.3 ⁇ is heated up to 410 ° ⁇ .
  • diesel fractions are transferred to the vapor phase.
  • the resulting two-phase flow consisting of diesel fumes (2,472 kg / sec) and fuel oil (6,152 kg / sec), is introduced into the upper outdoor section of the truck.
  • the existing light hydrocarbon gas in the amount of 0.1 kg / sec is heated in the heater 18 of the furnace before the temperature
  • Gas for combustion in the furnace is extracted from a collection of fuel gas 30.
  • the written-down equipment and installation for its use in the process of the use of technology and the convenience of the consumers are free of gas and gas
  • the raw materials are divided into the following fractions: fuel oil; diesel; blue and light; gasoline light and medium; liquefied and dry gas. Dry gas is used at the factory mainly in the form of a primary energy source. By reconditioning, it is possible to use solid fuel oil and diesel fuel.
  • the raw materials for the processes of the primary processing are fuel oil, gasoline and gasoline fractions, from bitumen, diesel, automobile tires are produced from gasoline, diesel, and automobiles. In cases of processing of the raw material and high-quality raw materials of the process of the primary processing, the processes of the processing and processing of the sys- tem are fed.

Landscapes

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

Abstract

Cette invention concerne un procédé et des installations permettant de séparer le pétrole brut ou des condensés gazeux, et d'obtenir les fractions suivantes: mazout, diesel, kérosènes lourd et léger, essences lourde et moyenne et, enfin, gaz liquéfié et sec. Ce procédé comprend les étapes suivantes: (a) séparation des vapeurs, de préférence après chaque étage supérieur de chauffage de récupération; (b) envoi par des voies distinctes des vapeurs séparées vers l'étape de condensation; (c) condensation des vapeurs et fractionnement; (d) chauffage par étages et vaporisation des résidus pétroliers avec séparation des vapeurs entre les étages et envoi de ces dernières dans la colonne. Les installations permettant de mettre en oeuvre ce procédé comprennent les éléments suivants: (e) un ou plusieurs condensateurs de fractionnement ainsi que des évaporateurs; et (f) un dispositif à étages multiples permettant de séparer les vapeurs, chaque étage comprenant un séparateur de vapeur; (g) ces séparateurs de vapeurs ainsi que le sommet de colonnes sont connectés au condensateur de fractionnement; (h) le chauffage et la vaporisation des résidus pétroliers s'effectuent par étages dans un four, les vapeurs étant séparées entre les étages et envoyées dans la colonne.
PCT/RU1997/000124 1996-05-12 1997-04-29 Procede et installations de fractionnement du petrole brut WO1997043355A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU30505/97A AU3050597A (en) 1996-05-12 1997-04-29 Method and equipment for fractioning crude oil

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU96109533/04A RU2100403C1 (ru) 1996-05-12 1996-05-12 Способ фракционирования нефти и установка для его осуществления
RU96109533 1996-05-12

Publications (1)

Publication Number Publication Date
WO1997043355A1 true WO1997043355A1 (fr) 1997-11-20

Family

ID=20180491

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/RU1997/000124 WO1997043355A1 (fr) 1996-05-12 1997-04-29 Procede et installations de fractionnement du petrole brut

Country Status (3)

Country Link
AU (1) AU3050597A (fr)
RU (1) RU2100403C1 (fr)
WO (1) WO1997043355A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1452576A2 (fr) * 2001-12-07 2004-09-01 Gamlet Alievich Mirzoev Procede de transformation de dechets de petrole mixtes et installation pour sa mise en oeuvre
SG125089A1 (en) * 2002-08-23 2006-09-29 Boc Group Inc Method and apparatus for producing a purified liquid

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2184136C1 (ru) * 2001-01-17 2002-06-27 Открытое акционерное общество "Эттис" Способ получения светлых нефтепродуктов и установка для его осуществления
RU2547479C2 (ru) * 2013-08-26 2015-04-10 Андрей Владиславович Курочкин Способ рекуперации тепла на установке первичной перегонки нефти
RU2581360C2 (ru) * 2014-06-02 2016-04-20 Акционерное общество "Инженерно-промышленная нефтехимическая компания" Установка первичной перегонки нефти
RU2759496C1 (ru) * 2021-04-27 2021-11-15 Александр Владимирович Данилов Установка для стабилизации, отбензинивания и обезвоживания нефти

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4292140A (en) * 1979-02-13 1981-09-29 Ishikawajima-Harima Jukogyo Kabushiki Kaisha Process for recovering heat in distillation process
FR2560204A1 (fr) * 1984-02-24 1985-08-30 Elf Aquitaine Procede et installation de distillation de petrole par separations progressives
SU1574625A1 (ru) * 1988-05-10 1990-06-30 Уфимский Нефтяной Институт Способ перегонки нефти
RU2058368C1 (ru) * 1993-08-02 1996-04-20 Талгат Галеевич Умергалин Способ фракционирования нефти

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4292140A (en) * 1979-02-13 1981-09-29 Ishikawajima-Harima Jukogyo Kabushiki Kaisha Process for recovering heat in distillation process
FR2560204A1 (fr) * 1984-02-24 1985-08-30 Elf Aquitaine Procede et installation de distillation de petrole par separations progressives
SU1574625A1 (ru) * 1988-05-10 1990-06-30 Уфимский Нефтяной Институт Способ перегонки нефти
RU2058368C1 (ru) * 1993-08-02 1996-04-20 Талгат Галеевич Умергалин Способ фракционирования нефти

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1452576A2 (fr) * 2001-12-07 2004-09-01 Gamlet Alievich Mirzoev Procede de transformation de dechets de petrole mixtes et installation pour sa mise en oeuvre
EP1452576A4 (fr) * 2001-12-07 2007-03-07 Gamlet Alievich Mirzoev Procede de transformation de dechets de petrole mixtes et installation pour sa mise en oeuvre
SG125089A1 (en) * 2002-08-23 2006-09-29 Boc Group Inc Method and apparatus for producing a purified liquid

Also Published As

Publication number Publication date
RU2100403C1 (ru) 1997-12-27
AU3050597A (en) 1997-12-05

Similar Documents

Publication Publication Date Title
JP2918695B2 (ja) 高真空精油装置及び方法
US10961460B2 (en) Delayed coking plant combined heating and power generation
JP4773563B2 (ja) 飲料用アルコール、特にウイスキーの蒸留のためのプラント
US4336046A (en) C4 Separation process
NO169903B (no) Fremgangsmaate for separering av komponenter i raa-olje
US4292140A (en) Process for recovering heat in distillation process
US4236974A (en) Process and apparatus for purifying waste waters
KR20110086591A (ko) 통합된 보일러용 공기 분리 및 물 가열 장치
WO1997043355A1 (fr) Procede et installations de fractionnement du petrole brut
RU2491321C2 (ru) Способ и устройство для предварительного нагрева сырья с помощью охладителя отходящих газов
JPS6325801B2 (fr)
WO1996016711A1 (fr) Installation de distillation sous vide d'un produit liquide
US4131538A (en) Method of separating a predetermined fraction from petroleum oil using multistage evaporators
RU2392028C1 (ru) Способ создания вакуума в вакуумной колонне перегонки нефтяного сырья и установка для осуществления способа
RU2124682C1 (ru) Способ подготовки нестабильного углеводородного конденсата к транспортированию по трубопроводу в однофазном состоянии
US2078407A (en) Method of treating hydrocarbons
RU2401296C1 (ru) Установка первичной перегонки нефти и способ первичной перегонки нефти
CA2565477A1 (fr) Appareil et methode de production de vapeur
RU2254897C1 (ru) Установка атмосферной перегонки нефти
WO2008049201A1 (fr) Dispositif et procédé de génération de vapeur
US2047779A (en) Conversion of hydrocarbon oils
US1619896A (en) Process for converting or cracking hydrocarbon oils
RU2108364C1 (ru) Способ получения низших олефинов из нефти
US68426A (en) Improvement in apparatus for distilling petroleum
SU1273378A1 (ru) Способ разделени продуктов каталитического крекинга

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU CA CN JP KR MX US AM AZ BY KG KZ MD RU TJ TM

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LU MC NL PT SE

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
121 Ep: the epo has been informed by wipo that ep was designated in this application
NENP Non-entry into the national phase

Ref country code: JP

Ref document number: 97540773

Format of ref document f/p: F

122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: CA