WO2017149728A1 - Appareil de traitement de pétrole - Google Patents

Appareil de traitement de pétrole Download PDF

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Publication number
WO2017149728A1
WO2017149728A1 PCT/JP2016/056627 JP2016056627W WO2017149728A1 WO 2017149728 A1 WO2017149728 A1 WO 2017149728A1 JP 2016056627 W JP2016056627 W JP 2016056627W WO 2017149728 A1 WO2017149728 A1 WO 2017149728A1
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WO
WIPO (PCT)
Prior art keywords
oil
crude oil
cdu
kbd
dcfcc
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Application number
PCT/JP2016/056627
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English (en)
Japanese (ja)
Inventor
渡邉　哲哉
厚徳 佐藤
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日揮株式会社
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Publication date
Application filed by 日揮株式会社 filed Critical 日揮株式会社
Priority to JP2018502454A priority Critical patent/JPWO2017149728A1/ja
Priority to PCT/JP2016/056627 priority patent/WO2017149728A1/fr
Publication of WO2017149728A1 publication Critical patent/WO2017149728A1/fr

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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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique

Definitions

  • the present invention relates to a petroleum processing apparatus.
  • CDU atmospheric distillation unit
  • LPG light naphtha
  • heavy naphtha heavy naphtha
  • kerosene light oil
  • RFCC residual oil fluid catalytic cracking device
  • a crude oil heating furnace is provided upstream of the atmospheric distillation tower, fuel is poured in the heating furnace, and the crude oil is heated to about 350 ° C.
  • the white oil fraction is evaporated and then introduced into the atmospheric distillation column.
  • equipment provided with CDU and RFCC is generally used (see Patent Document 1).
  • An object of the present invention is to provide a petroleum processing apparatus capable of greatly reducing energy consumption.
  • a first aspect of the present invention is an oil comprising a crude oil fluidized catalytic cracking reaction apparatus through which crude oil or a mixed oil of crude oil and atmospheric residue is passed, and a reaction product distillation facility. It is a processing device. According to a second aspect of the present invention, there is provided a petroleum processing apparatus comprising a prefractionator, a crude oil fluid catalytic cracking reaction apparatus, and a reaction product distillation facility.
  • the first embodiment which is a petroleum processing apparatus comprising a crude oil fluidized catalytic cracking reactor for passing crude oil and a reaction product distillation facility,
  • the oil is cracked by passing it through a crude fluid fluid catalytic cracking device (Direct Crude Fluid Catalytic Cracking, hereinafter sometimes referred to as “DCFCC”) and then distilled in the reaction product distillation facility after the cracking.
  • DCFCC is composed of a crude oil fluid catalytic cracking reactor for fluid catalytic cracking of crude oil and a reaction product distillation facility for fractionating and purifying the reaction product therefrom.
  • the crude oil is directly passed through the DCFCC without passing through the CDU.
  • the first embodiment includes a crude oil fluid catalytic cracking reaction device for passing crude oil, and a reaction product distillation facility.
  • crude oil is directly passed through DCFCC, and the crude oil is subjected to fluid catalytic cracking.
  • Fluid catalytic cracking means that crude oil is brought into contact with a catalyst held in a fluid state and decomposed into light hydrocarbons mainly composed of gasoline and light olefins.
  • all the decomposition products produced in the reactor are gaseous hydrocarbons.
  • the catalyst that has come into contact with crude oil adheres to the coke produced by the reaction and decreases the reaction activity. It is regenerated by burning.
  • the crude oil passed through the reactor is evaporated and decomposed using the heat generated in the regeneration tower during catalyst regeneration as described above, so that the crude oil heating furnace required by the CDU to process the crude oil is used. The corresponding heating furnace becomes unnecessary.
  • crude oil preheated to about 250 ° C. is passed through a crude oil fluid catalytic cracker (DCFCC) via a line 11.
  • DCFCC crude oil fluid catalytic cracker
  • examples of the catalyst used for fluid catalytic cracking include a silica / alumina catalyst and a zeolite catalyst.
  • a commercial item may be used for these catalysts.
  • crude oil is decomposed at a reaction temperature of 560 to 570 ° C. by contacting with a catalyst having a high temperature of about 700 ° C.
  • the heat required for the evaporation and reaction of crude oil is covered by the heat during catalyst regeneration generated in the DCFCC regeneration tower.
  • the outlet temperature of the reaction zone for fluid catalytic cracking in DCFCC is preferably 500 ° C. or higher and 600 ° C. or lower, and more preferably 520 ° C. or higher and 570 ° C. or lower.
  • the contact time between the crude oil and the catalyst in fluid catalytic cracking is preferably from 1.5 seconds to 10 seconds, and more preferably from 2 to 8 seconds.
  • the components decomposed by DCFCC are introduced into the reaction product fractionation equipment through the line 12 and distilled. In the same fractionation equipment, it is separated into each fraction such as light gas, LPG, propylene, naphtha, middle distillate, and residual oil according to the boiling point. Each separated fraction is subjected to a treatment such as reforming as necessary, and can be appropriately used as a petroleum product base material.
  • olefins such as propylene can be obtained with high yield.
  • propylene is further decomposed by further decomposition of a naphtha fraction generated by decomposition of a heavy oil fraction in addition to olefins derived from a naphtha fraction in a raw material oil. This is because olefins such as can be obtained.
  • a refinery equipped with a conventional CDU and heavy oil desulfurization equipment it is possible to increase the production of about 340,000 tons of propylene per year.
  • the second embodiment is an embodiment in which the first embodiment and the conventional CDU facility are used in combination. That is, the second embodiment includes a CDU and a DCFCC.
  • the atmospheric distillation residue oil obtained by CDU and crude oil are mixed and passed through DCFCC for decomposition, and after the decomposition, the product is purified by a reaction product distillation facility.
  • a second embodiment will be described with reference to FIG.
  • Light oil (carbon number: 3) and LPG are mixed with LPG refined by CDU via line 22 and sent to a propylene recovery unit (PRU).
  • PRU propylene recovery unit
  • Naphtha performs hydrodesulfurization treatment by a hydrodesulfurization apparatus (CCG-HDS in FIG. 2) having a catalyst layer filled with a hydrodesulfurization purification catalyst.
  • CCG-HDS hydrodesulfurization apparatus
  • a mixed LPG of 30.1 kBD propylene and 27.9 kBD can be obtained.
  • the second embodiment is an embodiment in which conventional CDU equipment is used in combination.
  • the hydrodesulfurization apparatus (NH-HDS and KR-HDS in FIG. 2) provided with a catalyst layer filled with CDU and hydrodesulfurization purification catalyst used in the second embodiment can use facilities that have been used conventionally. *
  • propylene as much as 30.1 kBD can be purified from 200,000 BPSD crude oil.
  • a DCFCC having a crude oil processing capacity of 50,000 BPSD is introduced into an existing refinery having a crude oil processing capacity of 150,000 BPSD to increase the crude oil processing capacity to 200,000 BPSD.
  • DCFCC the amount of crude oil processed can be increased without modifying existing CDUs.
  • the third embodiment is an embodiment using an oil processing apparatus equipped with a CDU and a DCFCC. In processing 200,000 BPSD crude oil, 150.0 kBD crude oil is converted into CDU. The remaining 50.0 kBD crude oil is passed through DCFCC.
  • 59.3 kBD atmospheric distillation residue oil obtained by CDU is mixed with 50 kBD crude oil through line 21, and 109.3 kBD crude oil and atmospheric distillation residue oil is mixed with DCFCC.
  • Light oil (carbon number: 3) and LPG are mixed with LPG refined by CDU via line 22 and sent to a propylene recovery unit (PRU).
  • PRU propylene recovery unit
  • Naphtha performs hydrodesulfurization treatment by a hydrodesulfurization apparatus (CCG-HDS in FIG. 3) having a catalyst layer filled with a hydrodesulfurization purification catalyst.
  • CCG-HDS hydrodesulfurization apparatus
  • 24.4 kBD light oil carbon number: 3
  • 22.4 kBD LPG and 3.0 kBD LPG refined by CDU.
  • 24.4 kBD of propylene and 22.2 kBD of mixed LPG can be obtained.
  • as much as 24.4 kBD of propylene can be purified from 200,000 BPSD of crude oil.
  • the fourth embodiment is a petroleum processing apparatus including a prefractionator, a crude oil fluid catalytic cracking reaction apparatus, and a reaction product distillation facility.
  • the prefractionator is a distillation column that operates to remove a substance having a low boiling point to some extent. Using a prefractionator, the heavy oil is divided into two fractions, a light fraction from LPG to naphtha and a heavy oil, and the heavy oil is passed through DCFCC.
  • the crude oil is passed through the line 11 to the prefractionator.
  • the prefractionator it is fractionated into a lighter fraction lighter than naphtha having about 5 to 7 carbon atoms and a heavier heavy oil.
  • the light fraction fractionated by the prefractionator enters the reaction product distillation facility via line 15 and is fractionated together with the reaction product by fluid catalytic cracking.
  • the heavy oil obtained after passing through the pre-fractionator is passed through the line 13 to the crude oil fluid catalytic cracking reactor to undergo fluid catalytic cracking.
  • the components decomposed by the crude oil fluid catalytic cracking reactor are introduced into the reaction product fractionation equipment through the line 14 and distilled. In the same fractionation equipment, it is separated into each fraction such as light gas, LPG, propylene, naphtha, middle distillate, and residual oil according to the boiling point.
  • Each separated fraction is subjected to a treatment such as reforming as necessary, and can be appropriately used as a petroleum product base material.
  • FIG. 4 shows a comparative example in which the total amount of crude oil of 200,000 BPSD is fractionated by CDU, and the atmospheric residue is decomposed by hydrodesulfurizer and RFCC.
  • the amount of propylene refined from the crude oil of 200,000 BPSD was 18.5 kBD, which was a low yield compared to the second to third embodiments.

Abstract

Cet appareil de traitement de pétrole est caractérisé en ce qu'il comprend un dispositif de réaction de craquage direct catalytique de fluide brut, au travers duquel on fait passer du pétrole brut ou un mélange de pétrole brut et de pétrole résiduel atmosphérique, et un équipement de distillation du produit de réaction.
PCT/JP2016/056627 2016-03-03 2016-03-03 Appareil de traitement de pétrole WO2017149728A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2018502454A JPWO2017149728A1 (ja) 2016-03-03 2016-03-03 石油の処理装置
PCT/JP2016/056627 WO2017149728A1 (fr) 2016-03-03 2016-03-03 Appareil de traitement de pétrole

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/JP2016/056627 WO2017149728A1 (fr) 2016-03-03 2016-03-03 Appareil de traitement de pétrole

Publications (1)

Publication Number Publication Date
WO2017149728A1 true WO2017149728A1 (fr) 2017-09-08

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JP (1) JPWO2017149728A1 (fr)
WO (1) WO2017149728A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH01304183A (ja) * 1988-03-25 1989-12-07 Amoco Corp 未精製原油の接触分解方法
JP2000336375A (ja) * 1999-05-05 2000-12-05 Bar Co Processes Joint Venture 改良された高転化率の残油流動接触分解方法
JP2007501311A (ja) * 2003-08-04 2007-01-25 ストーン アンド ウェブスター プロセス テクノロジー インコーポレーテッド 触媒ストリッパー中の触媒温度の制御

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH01304183A (ja) * 1988-03-25 1989-12-07 Amoco Corp 未精製原油の接触分解方法
JP2000336375A (ja) * 1999-05-05 2000-12-05 Bar Co Processes Joint Venture 改良された高転化率の残油流動接触分解方法
JP2007501311A (ja) * 2003-08-04 2007-01-25 ストーン アンド ウェブスター プロセス テクノロジー インコーポレーテッド 触媒ストリッパー中の触媒温度の制御

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