WO2009094934A1 - A system and a process for producing high quality gasoline - Google Patents

A system and a process for producing high quality gasoline

Info

Publication number
WO2009094934A1
WO2009094934A1 PCT/CN2009/070239 CN2009070239W WO2009094934A1 WO 2009094934 A1 WO2009094934 A1 WO 2009094934A1 CN 2009070239 W CN2009070239 W CN 2009070239W WO 2009094934 A1 WO2009094934 A1 WO 2009094934A1
Authority
WO
Grant status
Application
Patent type
Prior art keywords
gasoline
oil
light
heavy
distillation
Prior art date
Application number
PCT/CN2009/070239
Other languages
French (fr)
Chinese (zh)
Inventor
Ranfeng Ding
Original Assignee
Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd
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

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G53/00Treatment of hydrocarbon oils in the absence of hydrogen, by two or more refining processes
    • C10G53/16Treatment of hydrocarbon oils in the absence of hydrogen, by two or more refining processes plural parallel stages only
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10GCRACKING 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
    • C10G2400/00Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02Gasoline

Abstract

A system for producing high quality gasoline comprises a distilling apparatus (1), extraction systems (2-1, 2-2), and a hydrogenation apparatus (3). The upper portion of the distilling apparatus (1) is connected with the light gasoline extraction system (2-1) through a pipeline for light gasoline, a product is collected from the upper portion of the light gasoline extraction system (2-1) through a pipeline, and the lower portion of the light gasoline extraction system (2-1) is connected with the hydrogenation apparatus(3) through a pipeline; the lower portion of the distilling apparatus (1) is connected with the heavy gasoline extraction system (2-2)through a pipeline for heavy gasoline; a product is collected from the upper portion of the heavy gasoline extraction system (2-2) through a pipeline, and the lower portion of the heavy gasoline extraction system (2-2) is connected with the hydrogenation apparatus (3) through a pipeline. The process for producing high quality gasoline comprises fractionating the raw oil primarily, then separating the fractions by extraction, and thereafter subjecting the extracts to hydrogenation according to the requirements for sulfur content, alkene content, and Octane Number.

Description

Technical Field A system and method for the preparation of high quality gasoline

The present invention relates to a system and a method of preparing high quality gasoline.

Background technique

Catalytic cracking, catalytic cracking and heavy oil catalytic cracking technology is a core technology of the oil refining, catalytic cracking into gas oil catalytic cracking, heavy oil cracking; production from these processes are collectively referred to as catalyzed hydrocarbon product oil obtained through the catalytic hydrocarbon processing, typically fractionation fractionator, fractionation may dry gas, liquefied petroleum gas, gasoline, diesel, heavy oil products, gasoline, diesel fuel occupies more than 70%, the total amount of the diesel supply market.

With increasingly stringent environmental requirements, standard petrol, diesel continues to increase, the existing catalytic hydrocarbon processing methods through the fractionation column fractionation show the following disadvantages: one is the quality of the treatment produced gasoline and diesel to be improve: high olefin content of gasoline, the octane number (RON) is low, the cetane number of diesel fuel is low, the stability does not meet the requirements; the second is the above-described processing method can not produce more gasoline at the same reference numerals, and product variety single; third is the production of diesel, gasoline ratio does not match the needs of the market, can not meet the demand for diesel, gasoline and oversupply.

To solve the above problems, Patent No. "catalytic hydrocarbon recombination treatment method" of the Chinese Patent 03148181.7 provides a catalytic hydrocarbon recombination treatment method, and patents, respectively Chinese invention patent 200310103541.9 and 200310103540.4 discloses the improvement patent, directed to washing with water and solvent recovery systems, but none of these patents disclosed relates to how the sulfur reduction and olefin reduction.

The current GB17930 gasoline standard requires a sulfur content of not greater than 0. 05% (wt), the olefin content of not greater than 35% (v), benzene content of not more than 2. 5% (v), most of the refineries can assure the quality of gasoline. However, upcoming national standards for gasoline III implemented in 2010 requires: sulfur content of not greater than 0. 015% (wt), the olefin content of not greater than 30% (v), benzene content not greater than 1% (v). For most refiners, we must face higher gasoline national standards IV: the sulfur content of not greater than 0. 005% (wt), the olefin is not greater than 25% (V) or less. Solutions must take into account the quality of petrol from the national standards for gasoline ΠΙ transition to the national IV standard gasoline, better planning should be in accordance with national IV standards for gasoline-time plan.

Since a large proportion of gasoline blending components of each product differences with developed countries, a high percentage of FCC gasoline, reformulated gasoline, alkylate petrol smaller proportion, and that this situation will persist. Therefore, to upgrade the quality of gasoline sulfur reduction to be solved and olefin reduction issues mainly related issues catalytic gasoline.

Is generally believed, 5-10% total sulfur FCC feedstock will enter the gasoline fraction according to the refinery catalytic feed hydrotreating of small capacity, larger capacity secondary processing catalytic cracking and coking of resid characteristic, low processing sulfur (0.3% sulfur) crude oil refinery FCC gasoline sulfur content of about 200 ppm, 0.8% sulfur and processing oil, the sulfur content of FCC gasoline about 900ppm, therefore, difficult to upgrade the quality of gasoline from olefin reduction into reduction of sulfur problem. Improved catalytic cracking process or a catalyst not solve the problem of sulfur fundamentally due to the catalytic cracking feedstock hydrodesulfurization investment, high operating costs, limited refinery existing conditions can not be large-scale applications, but also for working with low sulfur crude oil refinery does not apply, at the same time, an excessive decrease in the olefin cracking unit will aggravate the loss of light products and gasoline octane number (RON) of.

Caustic washing desulfurization with olefins can not be separated, but also cause environmental pollution; through the hydrotreating of light gasoline, not only high energy consumption, costs are also high.

Accordingly, a low-cost, low-power, low sulfur content, low olefin content and octane prepared pollution (RON) of the processing system and method for higher gasoline pool has become an urgent need in the art to solve the technical problems.

SUMMARY

One object of the present invention is to provide a low cost, low power, low sulfur content, low olefin content and improved pollution prepared octane number (RON) of the system.

To achieve the above object, the present invention adopts the following technical scheme:

One of the program:

Preparing a high-quality fuel system, comprising a distillation means; characterized in that: said upper portion of distillation apparatus are connected via a line to a light gasoline extraction system; upper part of the light gasoline product extraction system through line direct recovery, the a lower light gasoline extraction system connected by line to the hydrogenation unit; a lower portion of the distillation apparatus via line connected to the extraction system of the heavy gasoline; upper portion of the heavy gasoline extraction system taken through line product directly, the heavy gasoline a lower extraction system is connected via a line to the hydrogenation unit.

A preferred technical scheme, characterized in that: said central cutting gasoline distillation apparatus and outputs connected by a line to the hydrogenation unit.

Program II:

Preparing a high-quality fuel system, comprising a distillation means; characterized in that: said upper portion of distillation apparatus are connected via a line to a light gasoline extraction system; upper part of the light gasoline product extraction system through line direct recovery, the a lower light gasoline extraction system connected by line to the hydrogenation unit; a lower portion of said distillation means coupled through line to the hydrogenation unit; the line connected by hydrogenating the heavy petrol extraction system means; said weight an upper gas extraction system through line directly collected product, the lower part of the heavy gasoline extraction system connected by line to the upper portion of the light petrol pipeline extraction system.

Program three:

Preparing a high-quality fuel system, comprising a distillation means; characterized in that: said upper portion of distillation apparatus are connected via a line to a light gasoline extraction system; upper part of the light gasoline product extraction system through line direct recovery, the a lower light gasoline extraction system connected by line to the hydrogenation unit; a lower portion of the distillation apparatus via line connected to the extraction system of the heavy gasoline; upper portion of the heavy gasoline extraction system connected via another line to the hydrogenation unit or the product was taken directly; a lower portion of said heavy gasoline extraction system connected by line to the hydrogenation unit; said distillation means coupled through line central to the gasoline extraction system; upper part of the extraction system through line gasoline and other a hydrogenation unit is connected to a lower portion of the gasoline extraction system connected by line to the hydrogenation unit.

Four programs:

- preparation of high quality gasoline such systems, characterized by: a distillation system and the extraction system hydrogenation apparatus, an upper portion of the distillation system is connected via a line to a light petrol hydrogenation unit; the lower portion of the distillation system through line and said extraction system is connected; upper portion of the extraction system through line and raffinate hydrotreating unit is connected to the lower part of the extraction system is connected via a line to extract oil hydrogenation unit; extracting oil hydrogenation unit through the line with the light gasoline hydrogenation unit is connected to the end of the tubing.

Another object of the present invention is to provide such a method to produce high quality gasoline.

One of the program:

A method for preparation of high quality gasoline, comprises the following steps: addition of the stabilizer or stabilizing a gasoline fractionating distillation apparatus with gasoline and naphtha, and hydrotreated coker gasoline, light gasoline cut is fractionated and the heavy gasoline; the light gasoline by distillation light gasoline upper device enters the extraction system for extraction separation, and the separated oil extracted raffinate; oil after the extraction to the hydrogenation unit through line blending process with the use of light gasoline, raffinate oil as the gasoline pool directly Produced; the heavy gasoline separated and extracted heavy gasoline extraction system, separated and extracted raffinate oil; oil after the extraction to the hydrogenation unit through line extraction process to obtain hydrogenated oil, and then with the light gasoline reconcile the use of the raffinate as chemical light oil.

In a preferred embodiment, wherein: said middle cut distillation apparatus is fractionated into the gasoline hydrogenation unit and hydrotreating.

In a preferred embodiment, wherein: said distillation apparatus an overhead temperature of 77~86 ° C, the bottom temperature is 190~192 ° C; overhead pressure of the distillation apparatus is 0. 11~0 28MPa. (absolute), the column bottom pressure of 0. 12~ 0. 30MPa (absolute); the control light gasoline distillation range at 30 ° C~90 ° C; the distillation range of the heavy gasoline is controlled to 90 V~205.

In a preferred embodiment, wherein: said control light gasoline distillation range at 30 ° C~65 ° C; gasoline distillation range of the controlled 65 ° C~90 ° C; distillation range of the heavy gasoline control 90 ° C~205 ° C.

In a preferred embodiment, wherein: said hydrogenation unit is full hydrogenation catalyst catalyst GHT-22; volume airspeed ratio of the hydrogenation apparatus 2 or 3; hydrogen / oil ratio of 200-300 ; operating temperature of 285~325 ° C, the operating pressure of 1. 5~2 5MPa (absolute).

Program II:

A method for preparation of high quality gasoline, comprises the following steps: addition of stabilized gasoline fractionation distillation apparatus, and the light gasoline cut is fractionated heavy gasoline; the light gasoline separated and extracted by the extraction system into the upper portion of the light gasoline distillation apparatus, separating the raffinate and extract oil; oil after the extraction to the hydrogenation unit through line blending process with the use of light gasoline, the raffinate is taken directly as a gasoline blending; said heavy naphtha and gasoline plus heavy coker gasoline together into hydrogen gas extraction system for extraction separation, the separated and extracted raffinate oil; hydrogenated extracting the oil obtained after extracting oil hydrogenation unit through line into the process, and then be reconciled with the use of light gasoline, the raffinate oil as the high vinyl material.

Program three:

- The method of preparation of high quality gasoline kind, comprises the following steps: addition of the stabilizer or stabilizing a gasoline fractionating distillation apparatus with gasoline and naphtha, and hydrotreated coker gasoline, light gasoline cut is fractionated and the heavy gasoline; the light gasoline by distillation light gasoline upper device enters the extraction system for extraction separation, and the separated oil extracted raffinate; raffinate oil as the gasoline pool directly taken out, the extract oil hydrogenation unit through line process before entering into the heavy gasoline pump provide separate extraction system; the heavy petrol hydrogenation unit through the post-treatment also enters the extraction system of the heavy gasoline is separated and extracted; the extract oil was separated and extracted raffinate separated through extraction system of the heavy gasoline; after extracting the oil recovery through line I oil blending gasoline with the pumping light, the raffinate taken out as a high-quality vinyl material.

In a preferred embodiment, wherein: said distillation apparatus an overhead temperature of 77~86 ° C, the bottom temperature is 189~192 ° C; overhead pressure of the distillation apparatus is 0. 11~0 28MPa. (absolute), the column bottom pressure of 0. 12~ 0. 30MPa (absolute); the control light gasoline distillation range at 30 ° C~100 ° C; the distillation range of the heavy gasoline is controlled to 100 ° C ~ 205 ° C.

Four programs:

A method for preparation of high quality gasoline, comprises the following steps: addition of the stabilizer or stabilizing a gasoline fractionating distillation apparatus with gasoline and naphtha, and hydrotreated coker gasoline, light gasoline cut fractionation, gasoline and heavy gasoline; the light gasoline was extracted by separation into the upper portion of the distillation apparatus light gasoline extraction system, separated light gasoline and light gas oil extraction raffinate; a light raffinate oil as gasoline blending gasoline direct recovery, the extraction of oil through line light gasoline after the processing means to the hydrogenation light gasoline raffinate oil blend used; in the extraction of gasoline in the gasoline extraction system, separated from the gasoline and gasoline oil extraction raffinate; the gasoline extract oil after obtaining the hydrogenation unit through line into the withdrawn oil hydrogenation process, then reconciled with the use of light gasoline, the gasoline raffinate oil hydrogenation unit through line into the process as a high-recovery ethylene feed; in the heavy gasoline heavy gasoline extraction system for extraction separation, the separated heavy gas oil and heavy gasoline extraction raffinate; the heavy gasoline withdrawn through line oil After processing the obtained hydrogenated extract oil hydrogenation unit, then after mixing the light gasoline as a gasoline blending recovery, the heavy gasoline raffinate directly or as a low pour diesel oil recovery, or as a treatment after the hydrogenation unit high vinyl material taken out.

In a preferred embodiment, wherein: said distillation apparatus an overhead temperature of 77~86 ° C, the bottom temperature is 190~192 ° C; overhead pressure of the distillation apparatus is 0. 11~0 28MPa. (absolute), the column bottom pressure of 0. 12~ 0. 30MPa (absolute); the control light gasoline distillation range at 30 ° C~80 ° C; gasoline distillation range of the controlled 80 ° C ~ 160 ° C; the distillation range of the heavy gasoline is controlled to 160 ° C~205 ° C.

In a preferred embodiment, wherein: said hydrogenation unit is full hydrogenation catalyst catalyst GHT-22; volume airspeed ratio of the hydrogenation apparatus 2 or 3; hydrogen / oil ratio of 200-300 ; operating temperature of 285~325 ° C, the operating pressure of 1. 5~2 5MPa (absolute).

Program five:

A method for preparation of high quality gasoline, the following steps: a raw material in the distillation system cutting fractionation, respectively light gasoline and heavy gasoline, light gasoline through the upper part of the distillation system was distilled off, and then enters the light petrol hydrogenation apparatus for hydrotreating, hydrotreated light gasoline as a gasoline blending recovery; extraction of the heavy gasoline enters the extraction system to separate the heavy gasoline and heavy gasoline raffinate oil extraction; the heavy oil into gasoline raffinate hydrogenation apparatus raffinate hydrotreating the hydrotreated feed out a high-quality ethylene material or reforming mining; after extracting the heavy oil into gasoline hydrogenation apparatus for extracting oil hydrotreating process and the hydrotreated light gasoline mixed as gasoline pool recovery.

In a preferred embodiment, wherein: said distillation system is a distillation column overhead temperature of 78~97 ° C, bottom temperature 167 ~ 187 ° C; column top pressure 0.15~0.25MPa (absolute), the column bottom pressure 0.20~0.30MPa (absolute); the control light gasoline distillation range at 30 ° C~110 ° C; the distillation range of the heavy gasoline is controlled to 110 ° C ~ 185 ° C.

In a preferred embodiment, wherein: said light petrol hydrogenation unit is selective hydrogenation catalyst is a catalyst GHT-20; volume airspeed ratio of the light gasoline hydrogenation unit is 1.0~4.0h- hydrogen / oil a volume ratio of 100 to 300; operating temperature of 150 ~ 220 ° C, operating pressure 1.0 ~ 4.0MPa (absolute).

In a preferred embodiment, wherein: said raffinate oil hydrogenation unit is full hydrogenation catalyst catalyst GHT-22; the raffinate hydrotreating apparatus 1.0~4.0h- hourly space velocity ratio hydrogen / oil volume ratio is 250-500; operating temperature of 250 ~ 320 ° C, operating pressure 1.0 ~ 4.0MPa (absolute).

The solvent may be any other conventional mixing ratio of these solvents at least two or solvents used in the invention, or.

In the present invention, light gasoline, heavy gasoline and gasoline stripping system can share a solvent recovery system may be used in different solvent recovery system, respectively.

The present invention naphtha, gasoline, and stabilized gasoline may be hydrotreated coker any ratio.

Light gasoline of the invention, gasoline and heavy gasoline cut points (boiling range) can be adjusted.

The present invention is used in the distillation system (or distillation column, distillation apparatus) of Patent Number "catalytic hydrocarbon recombination treatment method" Chinese Patent No. 03148181.7 of the invention disclosed in the distillation system. The extraction system used (extraction column) for the Chinese patent No. 200310103541.9 and 200310103540.4 of the invention disclosed in the extraction system, comprising water and a solvent recovery system.

The hydrotreating apparatus of the present invention is a conventional hydrotreating unit, including heating furnace, heat exchanger, high-pressure separator, air condenser and water condenser.

Below the invention is further illustrated by the drawings and detailed description are not meant to limit the scope of the present invention. BRIEF DESCRIPTION

1 a schematic flowchart of FIG. 1 and Example 2 of the present invention.

FIG 2 is a schematic flowchart of the embodiment 3 of the present invention.

FIG 3 is a schematic flowchart of the embodiment 4 of the present invention.

4 is a schematic flowchart of FIG. 5 and 6 embodiment of the invention.

FIG 5 is a schematic flowchart of the embodiment 7 of the present invention.

FIG 6 is a schematic flowchart of the embodiment 8 of the present invention.

FIG 79, 10 and 11 is a schematic flowchart of the embodiment of the present invention.

detailed description

Example 1

As shown in FIG. 1, a schematic flow chart of Example 1 of the present invention. The distillation range of 30-205 ° C, sulfur content is 2000ppm, mercaptan content is 50ppm, olefin content is 40% (v), diolefin content of 1. 0% (v), aromatic hydrocarbon content of 19% (v ), octane number (RON) of 91, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) at 10 tons / year traffic cut fractionated in a distillation column overhead temperature of the distillation column 1 is 86 V, the bottom temperature was 192 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (distillation range of 30 -9CTC) distilled off through the upper portion of the distillation tower 1, the total amount of distilled 43,000 tons / year, and then into light gasoline 2-1 extraction of the extraction system, and the separated oil extracted raffinate; the said extraction system used in the solvent is 2-1 N- formyl morpholine, the extraction temperature is 80 ° C, solvent ratio (solvent / feed) is 2.5 (mass), ratio of water raffinate 0.2 (mass), the solvent recovery temperature is 149 ° C, the solvent recovery pressure of 0. 112MPa (absolute); extracting said oil is 10,800 tons / year pumping flow rate to the hydrogenation apparatus 3 as the hydrogenation after hydrotreating Blending with gasoline blending oil recovery, the catalyst in the hydrotreating unit 3 is full hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 3 2h- ratio hydrogen / oil volume ratio of 250; the operation temperature of 295 ° C, the operating pressure of 2. 5MPa (absolute); the raffinate oil is 32,300 tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (distillation range of 90-205) to 57,000 tons / year into the flow of heavy gasoline extraction system 2-2 was separated and the separated extract oil and raffinate; the extraction system 2 -2 solvent used is N- formyl morpholine, the extraction temperature is 115 ° C, solvent ratio (solvent / feed) is 3.5 (mass), ratio of water raffinate 0.2 (mass), the solvent recovery temperature of 151 ° C, the solvent recovery pressure of 0. 112MPa (absolute); after the extraction oil is 20,100 tons / year into the flow hydrogenation apparatus 3 as the hydrogenation hydrotreated oil extraction and blending the produced gasoline blending; the raffinate oil is 36,000 tons / year as the flow of chemical light oil recovery.

The resulting distillation range of the gasoline blending 30-205 ° C, a sulfur content of 28. 4ppm, mercaptan content is 1. 0ppm, olefin content of 21. 3% (v), diolefin content is less than 0. 01% (v ) (trace, not detected); aromatic content of 32. 15% (v), octane number (RON) is 93.1, the density is 721.4 kg / m 3, the amount of recoverable 64000 tons / year. The resulting distillation range of chemical light oil is 90-205 ° C, a sulfur content of 10. 0ppm, mercaptan content is 1. 0ppm, olefin content of 52. 0% (v), diolefin content is less than 0.01% ( v) (trace, can not be measured), an aromatic hydrocarbon content of 3. 0% (v), octane number (RON) is 82.0, the density is 740.0 kg / m 3, taken out in an amount of 3.6 tons / year.

Physicochemical properties of all the hydroprocessing hydrogenation catalyst GHT-22 apparatus as shown in the following table.

Method of the present invention is used (the same below):

1. Distillation range: GB / T6536-1997 petroleum products - Determination of distillation;

2, sulfur content: SH / T0689-2000 light hydrocarbon and the total sulfur content of fuel oils and other assay (ultraviolet fluorescence method);

3, mercaptan sulfur: GB / T1792-1988 mercaptan sulfur distillate fuel oil in the assay (potentiometric titration);

4, the olefin: GB / T11132-2002 hydrocarbon liquid petroleum products assay (fluorescent indicator adsorption method);

5, an aromatic hydrocarbon: GB / T11132-2002 hydrocarbon liquid petroleum products assay (fluorescent indicator adsorption method);

6, the octane number: GB / T5487 assay gasoline octane number (research);

7. Density: GB / T1884-2000 Crude Petroleum and Liquid product density laboratory assay (densitometer method);

8, the measurement diene (diolefin): The titration.

9, the hydrogenation catalyst analysis method: CoO Colorimetric SH / T0345-1992

W0 3 colorimetry

Physical properties of the instrument used in the analysis method

A low temperature nitrogen adsorption surface area of ​​2400 Sorption

A pore volume of mercury intrusion method Auto Pore II 9200

Crush strength of the strength measuring method DL II type intelligent particle strength tester

Bulk density weighing method

Example 2

Process Example 1 and the embodiment of the present invention is the same as FIG. The distillation range of 30-205 ° C, sulfur content is 100ppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0. 1% (v), aromatic hydrocarbon content of 15% (v ), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1; the same time, the distillation range of 30- 205 ° C, 200 ppm sulfur content, mercaptan content is lppm, olefin content is less than 0. 1% (v) (trace, can not be detected); diene content of less than 0. 01% (V) (traces, can not be detected), an aromatic hydrocarbon content of 8% (v), octane number (RON) of 82, a density of 732 kg of naphtha / m 3 to 20,000 tons / year traffic cut fractionated in the distillation column 1; At the same time, the distillation range of 30-205 ° C, sulfur content is 150ppm, mercaptan content is lppm, olefin content is 6% (v), diolefin content is less than 0. 01% (V) (traces, can not be detected), an aromatic hydrocarbon content of 10% (v), octane number (RON) of 79, a density of 721 kg / m 3 hydrotreated coker gasoline to 20,000 tons / year traffic cut fractionated in the distillation column 1 ; overhead temperature of the distillation column 1 A degree of 82 ° C, bottom temperature 190 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (evaporated Cheng is 30-9CTC) through the upper part of the distillation column 1 was distilled off, the total amount of distilled 40,000 tons / year, and then enters the light gasoline extraction system extraction 2-1, separated and extracted raffinate oil oil; 2-1 in the extraction system used in the solvent is N- formyl morpholine, the extraction temperature is 80 ° C, solvent ratio (solvent / feed) is 2.5 (mass), ratio of water raffinate 0.2 (mass), the solvent recovery temperature is 149 ° C, the solvent recovery pressure of 0. 112MPa (absolute); extracting said oil is 08,000 tons / year into the flow of the hydrotreating unit 3 as hydrotreating hydrogenated extract oil recovery and blending gasoline blending, the catalyst in the hydrogenation of 3 means the entire hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 3 is hydrogen ratio of 2. 5h- / oil volume ratio 200; operating temperature of 285 ° C, the operating pressure of 1. 5MPa (absolute); the raffinate oil is 32,000 tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (distillation range 90-205 ° C) to 60,000 tons / year into the flow of heavy gasoline extraction system 2-2 was separated and the separated extract oil and raffinate; the extract 2-2 of the solvent system is N- formyl morpholine, the extraction temperature is 115 ° C, solvent ratio (solvent / feed) is 3.5 (mass), ratio of water raffinate 0.2 (mass) after extracting the extracted oil as hydrogenated oil is 12,000 tons / year into the flow hydrogenation apparatus 3 hydrotreated; solvent recovery temperature is 151 ° C, the solvent recovery pressure of 0. 112MPa (absolute) Produced blending with gasoline pool; the raffinate oil is 48,000 tons / year as the flow of chemical light oil recovery.

The resulting distillation range of the gasoline blending 30-205 ° C, a sulfur content of 7. 9ppm, mercaptan content <lppm (trace, not detected), an olefin content of 11. 8% (v), diolefin content is less than 0. 01% (V) (traces, not detected); aromatic content of 22. 1% (v), octane number (RON) is 92.12, the density is 717.76 kg / m 3, recovery in an amount of 52,000 tons / year.

The resulting distillation range of chemical light oil is 90-205 ° C, a sulfur content of 31. 0ppm, mercaptan content is 1. 0ppm, olefin content of 18. 9% (v), diolefin content is less than 0.01% ( v) (trace, not detected), an aromatic hydrocarbon content of 2. 0% (v), octane number (RON) is 76.5, the density is 738.1 kg / m 3, taken out in an amount of 4.8 tons / year.

All assay methods and physicochemical properties of the hydrogenation catalyst GHT-22 3 the same as in Example 1 Hydrogenation apparatus.

Example 3

2, a schematic flow chart of Example 3 of the present embodiment of the invention. The distillation range of 30-205 ° C, a sulfur content of lOOppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0. 1% (v), aromatic hydrocarbon content of 15% (v ), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1; the same time, the distillation range of 30- 205 ° C, 200 ppm sulfur content, mercaptan content is lppm, the olefin content is less than 0. 1% (ν) (trace, can not be detected), diolefin content is less than 0. 01% (V) (traces, not detection), an aromatic hydrocarbon content of 8% (v), octane number (RON) of 82, a density of 732 kg / m 3 of naphtha at 2 tons / year traffic cut fractionated in the distillation column 1; and Meanwhile, the distillation range of 30-205 ° C, sulfur content is 150ppm, mercaptan content is lppm, olefin content is 6% (v), diolefin content is less than 0. 01% (V) (traces, not detection), an aromatic hydrocarbon content of 10% (v), octane number (RON) of 79, a density of 721 kg hydrotreated coker gasoline / m 3 to 20,000 tons / year traffic cut fractionated in the distillation column 1; overhead temperature of the distillation column 1 77 ° C, bottom temperature 192 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline, gasoline and heavy gasoline; the light gasoline ( distillation range 30-65 ° C) through the upper portion of distillation column 1 was distilled off, the total amount of distilled 30,000 tons / year, then extracted into the extraction system separator 2-1 light gasoline, oil separated out and raffinate; 2-1 in the extraction system used in the solvent is N- formyl morpholine, the extraction temperature is 80 ° C, solvent ratio (solvent / feed) is 2.5 (mass), the raffinate water ratio is 0.2 (mass), the solvent recovery temperature is 149 ° C, the solvent recovery pressure of 0. 112MPa (absolute); extracting said oil is 04,000 tons / year hydrogenation flow rate to the hydrogenation apparatus 3 after the extraction process as the hydrogenation of oil recovery and blending gasoline blending, hydrogenation apparatus 3 in the entire catalyst is a hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 3 ratio Sh- 1; hydrogen / oil volume ratio is 300; operating temperature of 325 ° C, the operating pressure of 2. 5MPa (absolute); the raffinate oil is 26,000 tons / year as the flow rate of the produced gasoline blending; the gasoline (Distillation range 65-90 ° C) to 10,000 tons / year flow into the hydrogenation unit through line 3 as the hydrotreating and hydrogenation of the gasoline blending the produced gasoline blending; the heavy gasoline (boiling range extraction is 90-205) to 60,000 tons / year into the flow of heavy gasoline extraction system 2-2 is separated, and the separated oil extracted raffinate; 2-2 of the extraction system used in the solvent N - formyl morpholine, the extraction temperature is 115 ° C, solvent ratio (solvent / feed) is 3.5 (mass), ratio of water raffinate 0.2 (mass), the solvent recovery temperature is 151 ° C, after extraction the extracted oil is 12,000 tons / year into the flow hydrogenation apparatus 3 hydrotreated oil and a hydrogenated gasoline pool blending recovery;; solvent recovery pressure of 0. 112MPa (absolute) of the raffinate to 48,000 tons / year of recovery as a chemical feedstock flow.

The resulting distillation range of the gasoline blending 30-205 ° C, a sulfur content of 6 ppm, mercaptan content <lppm (trace, not detected), the olefin content of 11. 3% (v), diolefin content is less than 0. 01% (V) (traces, not detected); aromatic content of 22. 1% (v), octane number (RON) is 92.1, the density is 717.8 kg / m 3, the amount of recovery 52,000 tons / year.

The resulting distillation range of chemical light oil is 90-205 ° C, a sulfur content of 31. 0ppm, mercaptan content is 1. 0ppm, olefin content of 19. 5% (v), diolefin content is less than 0.01% ( v) (trace, not detected), an aromatic hydrocarbon content of 2. 0% (v), octane number (RON) is 76.5, the density is 738.1 kg / m 3, taken out in an amount of 4.8 tons / year.

Determination of physicochemical properties and full hydrogenation catalyst GHT-22 in the hydrotreating unit 3 in Example lo

Example 4

As shown in FIG. 3, a schematic flow chart of Example 4 of the present invention. The distillation range of 30-205 ° C, a sulfur content of lOOppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0. 1% (v), aromatic hydrocarbon content of 15% (v ), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1; column top temperature of the distillation column 1 is 82 ° C, bottom temperature 190 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (distillation range 30-9CTC) distilled off through the upper portion of the distillation tower 1, the total amount of distilled 24,000 tons / year, and then enters the light gasoline extraction system extraction 2-1, separated and extracted raffinate oil; the extraction system used in the solvent is 2-1 sulfolane, the extraction temperature is 70 ° C, solvent ratio (solvent / feed) is 2.0 (mass), ratio of water raffinate 0.2 (mass), solvent recovery temperature is 153 ° C, the solvent recovery pressure of 0. 112MPa (absolute); after the extraction oil is 04,800 tons / year flow rate to the hydrogenation apparatus 3 as hydrotreating the hydrogenated extract oil and the modulation After recovery and gasoline blending the catalyst in the hydrotreating unit 3 is full hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 2. 5h- 3 ratio of hydrogen / oil volume ratio is 200; the operation temperature of 285 ° C, the operating pressure of 1. 5MPa (absolute); the raffinate oil is 19,200 tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (distillation range of 90-205) to 36,000 tons / year into the flow of heavy gasoline extraction system Extraction of 2-2, while the distillation range of 90-205 ° C, sulfur content is 326ppm, mercaptan content is lppm, olefin content is less than 0. 1% (ν) (trace, can not be detected); diene content of less than 0. 01% (v) (trace, can not be detected), aromatics content 12% (v), octane number (RON) of 81, a density of 739 kg / m 3 of naphtha to 20,000 tons / year into the flow rate of the heavy gasoline extraction separation extraction system 2-2; at the same time the distillation range of 90-205 ° C, a sulfur content of 283 ppm, a thiol lppm content, olefin content of 5% (v), diolefin content is less than 0. 1% (v) (trace, can not be detected) aromatic hydrocarbon content of 14% (v), octane number (RON) of 80, a density of 741 kg / m 3 hydrotreated coker gasoline to 20,000 tons / year of heavy gasoline flow rate was extracted into the extraction system 2-2 separated; and the separated oil extracted raffinate; 2-2 in the extraction system used in the solvent is sulfolane, the extraction temperature is 110 ° C, solvent ratio (solvent / feed) is 3.5 (mass), the raffinate oil water ratio of 0.2 ( By mass), the solvent recovery temperature is 157 ° C, the solvent recovery pressure of 0. 112MPa (absolute); after the extraction oil is 16,000 tons / year into the flow hydrogenation apparatus 3 as the hydrogenation hydrotreated extracting oil recovery blending gasoline pool; the raffinate oil is 60,000 tons / year of ethylene feed flow rate as high recovery.

The resulting distillation range of the gasoline blending 30-205 ° C, a sulfur content of 17. 0ppm, mercaptan content <lppm (trace, not detected), the olefin content of 17. 3% (v), diolefin content is less than 0. 01% (V) (traces, can not be measured); aromatic content of 32. 6% (v), octane number (RON) is 92.8, the density is 733.9 kg / m 3, recovery an amount of 40,000 tons / year.

The resulting material quality ethylene distillation range of 90-205 ° C, a sulfur content of 33. 0ppm, mercaptan content is 1. 0ppm, olefin content of 12. 9% (v), diolefin content is less than 0.01% ( V) (traces, not detected), an aromatic hydrocarbon content of 2. 0% (v), octane number (RON) is 79.0, the density is 732.0 kg / m 3, the amount of recovery is 6.0 tons / year.

All assay methods and physicochemical properties of the hydrogenation catalyst GHT-22 3 of the hydrogenation apparatus according to the same embodiment Example 5

4, a schematic flow chart of the present invention of Example 5. The distillation range of 30-205 ° C, sulfur content is 100ppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0. 1% (v), aromatic hydrocarbon content of 15% (v ), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in a distillation column overhead temperature of the distillation column 1 is 82 ° C, bottom temperature 190 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (distillation range 30-10CTC) distilled off through the upper portion of the distillation tower 1, the total distilled off was 2.4 million tons / year, and then into light gasoline extraction system 2-1 was separated and the separated extract oil and raffinate; the 2-1 said extraction system used in the solvent is sulfolane, the extraction temperature is 70 ° C, solvent ratio (solvent / feed) is 2.0 (mass), ratio of water raffinate 0.2 (mass), the solvent recovery temperature of 153 ° C, the solvent recovery pressure of 0. 112MPa (absolute); the oil was extracted light gasoline 04,800 tons / year flow rate to the hydrogenation apparatus 3 after hydrotreating heavy gasoline pumping into the Extraction of the stripping system 2-2, the catalyst is a hydrotreating unit 3 all the hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 2. 5h- 3 ratio of hydrogen / oil volume ratio of 200 ; operating temperature of 285 ° C, the operating pressure of 1. 5MPa (absolute); the light gasoline raffinate to 19,200 tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (distillation range 100-205 ° C) to 36,000 tons / year flow into the extraction system for extracting heavy gasoline 2-2 separated, isolated heavy gasoline and heavy gasoline oil extraction raffinate; 2-2 the extraction system used in the solvent is sulfolane, the extraction temperature is 98 ° C, solvent ratio (solvent / feed) is 3.5 (mass), ratio of water raffinate 0.2 (mass), solvent recovery temperature is 157 ° C, the solvent recovery pressure of 0. 112MPa (absolute); the heavy gasoline raffinate to 27,800 t / year of quality ethylene feed flow rate as taken out; the heavy gas oil is withdrawn flow 13,000 tons / year of the rear light petrol raffinate oil recovery mixture as gasoline pool.

The resulting distillation range of the gasoline blending 30-205, sulfur content 14. 5ppm, mercaptan content is less than 1. Oppm (trace, not detected), the olefin content of 21. 7% (v), diolefin content is low in 0. 01% (V) (traces, not detected); aromatic content of 26. 5% (v), octane number (RON) is 95.7, the density is 735.0 kg / m 3, Cai an amount of 32,200 tons / year.

The resulting material quality ethylene distillation range 100-205 ° C, a sulfur content of 5. 0ppm, mercaptan content is less than 1. Oppm (trace, not detected), the olefin content of 1. 2% (v), two olefin content of less than 0. 01% (v) (trace, not detected), an aromatic hydrocarbon content of 2. 0% (v), octane number (RON) is 73.8, the density is 720.0 kg / m 3 , recovery capacity of 27,800 tons / year.

All physical and chemical properties and the method of measuring apparatus hydrogenation catalyst GHT-22 the same as in Example 1 Hydrogenation. Example 6

4, a schematic flow chart of Example 6 of the present embodiment of the invention. The distillation range of 30-205 ° C, sulfur content is 800ppm, mercaptan content was 9ppm, olefin content of 36% (v), diolefin content of 0. 9% (v), aromatic hydrocarbon content of 17% (v ), octane number (RON) of 91, a density of 731 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1; the same time, the distillation range of 30- 205 ° C, 200 ppm sulfur content, mercaptan content is lppm, the olefin content is less than 0. 1% (v) (trace, not detected), diolefin content is less than 0. 01% (V) (traces, not detected), an aromatic hydrocarbon content of 8% (v), octane number (RON) of 82, a density of 732 kg / m 3 of naphtha at 2 tons / year traffic cut fractionated in the distillation column 1 ; At the same time, the distillation range of 30-205 ° C, sulfur content is 150ppm, mercaptan content is lppm, olefin content is 6% (v), diolefin content is less than 0. 01% (V) (traces , not detected), an aromatic hydrocarbon content of 10% (v), octane number (RON) of 79, a density of 721 kg hydrotreated coker gasoline / m 3 to 20,000 tons / year of traffic in the distillation column 1 cutting fractionation; overhead temperature of the distillation column 1 To 82 ° C, bottom temperature 190 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline and heavy gasoline, the light gasoline (boiling range is 30-10CTC) distilled off through the upper portion of the distillation tower 1, the total amount of distilled 45,000 tons / year, and then enters the light gasoline extraction system extraction 2-1, separated and extracted raffinate oil ; 2-1 the extraction system used in the solvent is sulfolane, the extraction temperature is 70 ° C, solvent ratio (solvent / feed) is 2.0 (mass), ratio of water raffinate 0.2 (mass) , the solvent recovery temperature is 153 ° C, the solvent recovery pressure of 0. 112MPa (absolute); the oil was extracted light gasoline 12,600 tons / year flow rate to the hydrogenation apparatus 3 after entering the hydrotreating heavy gasoline extraction extraction system 2-2, the catalyst is a hydrotreating unit 3 all the hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 3 ratio of 2. 5h-; hydrogen / oil volume ratio of 200 ; operating temperature of 285 ° C, the operating pressure of 1. 5MPa (absolute); the light gasoline raffinate to 32,400 tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (distillation range 100-205 ° C) to 55,000 tons / year flow into the extraction system for extracting heavy gasoline 2-2 separated, isolated heavy gasoline and heavy gasoline oil extraction raffinate; 2-2 the extraction system used in the solvent is sulfolane, the extraction temperature is 98 ° C, solvent ratio (solvent / feed) is 3.5 (mass), ratio of water raffinate oil is 0.2 (mass), the solvent recovery temperature is 157 ° C, the solvent recovery pressure was 0.112MPa (absolute); the heavy gasoline raffinate to 48,700 t / year of quality ethylene feed flow rate as taken out; the heavy gas oil is withdrawn 18,900 tons / year traffic recovery of the light gasoline as a gasoline blending the raffinate after mixing.

The resulting distillation range of the gasoline blending 30-205 ° C, sulfur content is 36.5ppm, 1.26 ppm mercaptan content, olefin content is 13.4% (v), diolefin content is less than 0.01% (V) (trace detection out); aromatic content of 23.2% (v), octane number (RON) is 95.8, the density is 701.4 kg / m 3, taken out in an amount of 51,300 tons / year.

The resulting material quality ethylene distillation range 100-205 ° C, sulfur content is 6.0ppm, the thiol content of less than

1. Oppm (trace, not detected), the olefin content of 1.2% (v), diolefin content is less than 0.01% (v) (trace, not detected), an aromatic hydrocarbon content of 3.0% (v), octane value (RON) is 70.5, the density is 761.0 kg / m 3, the amount of recovery of 48,700 tons / year.

All assay methods and physicochemical properties of the hydrogenation catalyst GHT-22 3 the same as in Example 1 Hydrogenation apparatus.

Example 7

5, a schematic flowchart of the embodiment 7 of the present invention. The distillation range of 30-205 ° C, a sulfur content of lOOppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0.1% (v), aromatic hydrocarbon content of 15% (v), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) at 10 tons / year traffic cut fractionated in the distillation column 1, a distillation column overhead temperature was 82 V the bottom temperature was 190 ° C, column top pressure is 0.2MPa (absolute), the column bottom pressure was 0.25MPa (absolute), respectively light gasoline, gasoline and heavy gasoline; the light gasoline (distillation range of 30- 8CTC) distilled off through the upper portion of the distillation tower 1, the total distilled amount of 3.8 million tons / year, and then enters the light gasoline extraction system extraction 2-1, separated light gasoline and light gas oil extraction raffinate; the extraction system used in the solvent is 2-1 sulfolane, the extraction temperature is 70 ° C, solvent ratio (solvent / feed) is 2.0 (mass), ratio of water raffinate oil is 0.2 (mass), the solvent recovery temperature is after the extraction oil is 15,000 tons / year flow rate to the hydrogenation apparatus 3-1 hydrotreating; 153 ° C, the solvent recovery pressure was 0.112MPa (absolute) As the hydrogenated oil extraction and recovery blending gasoline blending, the catalyst in the hydrogenation apparatus 3-1 is full hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation apparatus 3-1 ratio 2.5h- ; hydrogen / oil volume ratio of 200; operating temperature of 285 ° C, the operating pressure is 1.5MPa (absolute); the light gasoline raffinate of 2.3 million tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (distillation range 160-205 ° C) to 20,000 tons / year into the flow of heavy gasoline extraction system 2-2 was separated and the separated heavy gasoline and heavy gasoline oil extraction raffinate; the extraction system 2-2 in the solvent is sulfolane, the extraction temperature is 115 ° C, solvent ratio (solvent / feed) is 3.5 (mass), the raffinate water wash is 0.2 (mass), the solvent recovery temperature is 157 ° C, the solvent recovery pressure of 0.112MPa (absolute); the heavy oil fuel out of 0.8 million tons / year, as traffic enters the hydrogenated oil extraction and blending gasoline blending postharvest hydrotreating hydrogenation unit 3-1 out; after the raffinate heavy gasoline to 12,000 tons / year flow into the hydrogenation unit 3-2 hydrotreated feedstock as high ethylene recovery. The Gasoline (distillation range 80-16CTC) to 42,000 tons / year into the gasoline flow extraction system 2-3 was separated and the separated extract oil and gasoline gasoline raffinate; the 2-3 extraction system used in the solvent is sulfolane, the extraction temperature is 95 ° C, solvent ratio (solvent / feed) is 2.5 (mass), ratio of water raffinate 0.2 (mass), the solvent recovery temperature of 155 ° C, the solvent recovery pressure of 0. 13MPa (absolute); the oil is withdrawn in gasoline 13,000 tons / year as the hydrogenation drawn into the flow after hydrotreating hydrogenation unit 3-1 mixing the oil and the produced gasoline blending; gasoline in the raffinate to 29,000 tons / year into the flow after hydrotreating hydrogenation unit 3-2 as a high vinyl material taken out.

The resulting distillation range of the gasoline blending 30-205 ° C, a sulfur content of 23. 14ppm, mercaptan content is 0. 8ppm, olefin content of 18. 8% (v), diolefin <0. 01% (V) (trace, not detected), an aromatic hydrocarbon content of 22. 9% (v), octane number (RON) is 94.6, the density is 724.3 kg / m 3, taken out in an amount of 59,000 tons /year.

The resulting material quality ethylene distillation range 160-205 ° C, a sulfur content of 2. 0ppm, mercaptan content <lppm (trace, not detected), an olefin content of 1. 0% (v), diolefin < 0. 01% (V) (traces, not detected), an aromatic hydrocarbon content of 3. 6% (v), octane number (RON) is 70.2, the density is 733.4 kg / m 3, recovery in an amount of 41,000 tons / year.

3-1 apparatus and method for measuring physicochemical properties GHT-22, and all the hydrogenation catalyst in the hydrogenation of 3-2 in Example 1.

Example 8

6, a schematic flow chart of Example 8 of the present invention. The distillation range of 30-205, lOOppm sulfur content, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0. 1% (v), aromatic hydrocarbon content of 15% (v), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1, while the distillation range of 30-205 ° C, 200 ppm sulfur content, mercaptan content is lppm, the olefin content of <0. 1% (v) (trace, not detected), diene content <0. 01% (V) (traces, not detected a), an aromatic hydrocarbon content of 8% (v), octane number (RON) of 82, a density of 732 kg / m 3 of naphtha at 2 tons / year traffic cut fractionated in the distillation column 1; and Meanwhile, the distillation range of 30-205 ° C, sulfur content is 150ppm, mercaptan content is lppm, olefin content is 6% (v), diolefin content of <0. 01% (V) (trace detection not), an aromatic hydrocarbon content of 10% (v), octane number (RON) of 79, a density of 721 kg / m 3 hydrotreated coker gasoline to 20,000 tons / year traffic cut fractionated in the distillation column 1 ; overhead temperature of the distillation column 1 was 82 ° C, The bottom temperature was 190 ° C, the column top pressure was 0. 2MPa (absolute), the column bottom pressure of 0. 25MPa (absolute), respectively light gasoline, gasoline and heavy gasoline, light gasoline the (distillation range of 30 -8CTC) distilled off through the upper portion of the distillation tower 1, the total distilled amount of 37,000 tons / year, and then enters the light gasoline extraction system extraction 2-1, separated light gasoline and light gasoline pumping out oil raffinate oil; 2-1 of the extraction system used in the solvent is sulfolane, the extraction temperature is 70 ° C, solvent ratio (solvent / feed) is 2.0 (mass), ratio of water raffinate 0.2 ( by mass), the solvent recovery temperature is 153 ° C, the solvent recovery pressure of 0. 112MPa (absolute); gasoline after the light oil is extracted 14,000 tons / year flow rate to the hydrogenation apparatus 3-1 as hydrotreating extracting the hydrogenated gasoline blending oil recovery mixture, the catalyst in the hydrogenation apparatus 3-1 is full hydrogenation catalyst GHT-22; the space velocity of the hydrogenation unit 3-1 volume ratio of 2. 5h- ; hydrogen / oil volume ratio of 200; operating temperature of 285 ° C, the operating pressure of 1. 5MPa (absolute); the light gasoline raffinate to 23,000 tons / year as the flow rate Gasoline pool recovery. The heavy gasoline (distillation range 160-205 ° C) to 21,000 tons / year flow into the extraction system for extracting heavy gasoline 2-2 separated, isolated heavy gasoline and heavy gasoline oil extraction raffinate; 2-2 the extraction system used in the solvent is sulfolane, the extraction temperature is 115 ° C, solvent ratio (solvent / feed) is 3.5 (mass), ratio of water raffinate 0.2 (mass), solvent recovery temperature is 157 ° C, the solvent recovery pressure of 0. 112MPa (absolute); the heavy gasoline withdrawn oil is 08,000 tons / year into the flow after hydrotreating added as a hydrogenation unit 3-1 after the hydrogen extracting oil mixed with the produced gasoline blending; gasoline after the heavy raffinate to 13,000 tons / year flow into the hydrogenation unit 3-2 is performed as a low pour diesel hydrotreating recovery. The Gasoline (distillation range 80-16CTC) to 42,000 tons / year into the gasoline flow extraction system 2-3 was separated and the separated extract oil and gasoline gasoline raffinate; the 2-3 extraction system used in the solvent is sulfolane, the extraction temperature is 95 ° C, solvent ratio (solvent / feed) is 2.5 (mass), gasoline raffinate water ratio of 0.2 (mass), solvent recovery temperature is 155 ° C, the solvent recovery pressure of 0. 13MPa (absolute); the oil is withdrawn in gasoline 09,500 tons / year into the flow after hydrotreating added as a hydrogenation unit 3-1 after the hydrogen extracting oil mixed with the produced gasoline blending; gasoline in the raffinate to 32,500 tons / year into the flow after hydrotreating hydrogenation unit 3-2 as a high vinyl material or as a raw material reforming recovery.

The resulting distillation range of the gasoline blending 30-205 ° C, a sulfur content of 23. 7ppm, mercaptan content is 0. 4ppm, olefin content of 15. 0% (v), diolefin content of <0. 01% (V ) (trace, not detected); aromatic content of 20. 3% (v), octane number (RON) is 92.8, the density is 720.5 kg / m 3, the amount of recoverable 54500 tons / year.

The resulting reforming feedstock (or quality ethylene material) distillation range of 160-205 ° C, a sulfur content of 0. 50ppm, mercaptan content <lppm (trace, not detected), the olefin <0. 1% (v ) (trace, not detected), diene <0. 01% (V) (traces, not detected), an aromatic hydrocarbon content of 3. 0% (v), octane number (RON) is 74.1 and a density of 727.0 kg / m 3, taken out in an amount of 32,500 tons / year.

The resulting low pour diesel fuel distillation range 160-205 ° C, sulfur content 32. Oppm, mercaptan content is 1. 0ppm, olefin content of 28. 2% (v), diolefin <0. 01% (V ) (trace, not detected), an aromatic hydrocarbon content of 3. 5% (v), a density of 759.0 kg / m 3, the amount of recovery of 13,000 tons / year.

3-1 apparatus and method for measuring physicochemical properties GHT-22, and all the hydrogenation catalyst in the hydrogenation of 3-2 in Example 1.

Example 9

As shown in FIG. 7, a schematic flow chart of Example 9 of the present invention. The distillation range of 30-185 ° C, sulfur content is 100ppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0.1% (v), aromatic hydrocarbon content of 15% (v), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1, a distillation column overhead temperature of 78 ° C, bottom temperature 167 ° C, column top pressure of 0.15 MPa (absolute), the column bottom pressure of 0.20 MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (distillation range of 30-110 ° C) distilled off through the upper portion of distillation column 1, a total of 2.95 was distilled tons / year, and then enters the light petrol hydrogenation unit 3-1 hydrotreating catalyst in the hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20; volume space velocity of the hydrogenation unit 3-1 ratio ^ Oh- 1; hydrogen / oil volume ratio of 300; operating temperature of 150 ° C, the operating pressure is l.OMPa ( absolute); light petrol after the hydrogenated to 29,500 tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (; distillation range 110-185 ° C) to 30,500 tons / year into the flow of heavy gasoline extraction and separation in an extractor 2, an oil separated heavy gasoline and heavy gasoline extraction raffinate; the pumping column 2, the solvent is sulfolane, the extraction temperature is 120 ° C, solvent ratio (solvent / feed) is 3.5 (mass), the raffinate water wash is 0.2 (mass), the solvent recovery temperature is 165 ° C, the solvent a pressure recovery O. lMPa (absolute); the heavy gasoline raffinate to 19,500 tons / year into the flow hydrogenation apparatus 3-2 hydrotreating catalyst in the hydrogenation apparatus 3-2 is full hydrogenation catalyst GHT-22; a space velocity of the hydrogenation apparatus 3-2 volume ratio ^ Oh; hydrogen / oil volume ratio of 500; operating temperature of 320 ° C, the operating pressure is 4.0MPa (absolute); the heavy oil fuel out of 1.1 million tons / year flow into the hydrogenation unit 3-3 hydrotreating catalyst in the hydrogenation apparatus 3-3 is full hydrogenation catalyst GHT-22; the hydrogenation apparatus 3 LHSV -3 Oh ratio; hydrogen / oil volume ratio of 500; operating temperature of 290 ° C, the operating pressure is 4.0MPa (absolute); after the raffinate heavy gasoline hydrogenation to Flow rate of 19500 tons / year as the high ethylene feed or reforming material taken out; the heavy gasoline after extracting oil hydrogenated to the light gasoline mixed flow 11000 tons / year as the hydrogenated gasoline pool Mining out.

The resulting distillation range of the gasoline blending 30-185 ° C, a sulfur content of 11.5 ppm, mercaptan content is less than l.Oppm (; trace, not detected), the olefin content is 22.5% (v), diolefin content is 0.01 % (v); aromatic content of 20.8% (v), octane number (RON) is 94.9, the density is 716.6 kg / m 3, taken out in an amount of 40,500 tons / year.

The resulting material quality ethylene material or the reforming distillation range 110-185 ° C, a trace amount of sulfur, not detected, mercaptan content is less than l.Oppm (; trace, not detected;), olefin content trace, not detected, the bromine index (bromine number) 39 (0.039), an aromatic hydrocarbon content of 2.0% (v), octane number (RON) is 72.8, the density is 753.0 kg / m 3, the amount of recoverable 19500 tons / year.

Selective hydrogenation catalyst 3-1 in the physicochemical properties of the light gasoline hydrogenation unit GHT-20 are as follows in Table 1, the hydrogenation catalyst in all hydrogenation unit 3-2 and the 3- 3 GHT-22 the physical and chemical properties and the same as in Example 1.

Table 1

Indicators Unit GHT-20

Appearance Gray trefoil

Size mm Φ1.5-2.0 strength N / cm 170

Bulk density g / ml 0.70

Surface area m 2 / g 180

Pore ​​volume ml / g 0.5-0.6

wo 3 m% 6.6

NiO m% 2.1

CoO m% 0.16

Method of the present invention is used (the same below):

1. Distillation range: GB / T6536-1997 petroleum products - Determination of distillation;

2, sulfur content: SH / T0689-2000 light hydrocarbon and total sulfur fuel and other oil-containing titration winding (Ultraviolet Fluorescence);

3, mercaptan sulfur: GB / T1792-1988 mercaptan sulfur distillate fuel oil in the assay (potentiometric titration);

4, the olefin: GB / T11132-2002 hydrocarbon liquid petroleum products assay (fluorescent indicator adsorption method);

5, an aromatic hydrocarbon: GB / T11132-2002 hydrocarbon liquid petroleum products assay (fluorescent indicator adsorption method);

6, the octane number: GB / T5487 assay gasoline octane number (research);

7. Density: GB / T1884-2000 Crude Petroleum and Liquid product density laboratory assay (densitometer method);

8, diene; assay (diolefin): The titration.

9, the hydrogenation catalyst analysis method:

10, the bromine index (bromine number) subject ¾ GB / T- 11136- 1989

Example 10

The same procedure as in Example 9 a schematic. The distillation range of 30-185 ° C, sulfur content is 100ppm, mercaptan content is 5ppm, olefin content of 30% (v), diolefin content is 0.1% (v), aromatic hydrocarbon content of 15% (v), octane number (RON) of 89, a density of 728 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1; the same time, the distillation range of 30-185 ° C, 200 ppm sulfur content, mercaptan content is lppm, the olefin content is less than 0.1% (v) (trace, not detected), diolefin content is less than 0.01% (v) (trace, not detected), an aromatic hydrocarbon content of 8% (v), octane number (RON) of 82, a density of 732 kg of naphtha / m 3 to 20,000 tons / year traffic cut fractionated in the distillation column 1; meanwhile, the a distillation range of 30-185 ° C, sulfur content is 150ppm, mercaptan content is lppm, olefin content is 6% (v), diolefin content is less than 0.01% (V) (; trace, not detected), an aromatic hydrocarbon content of 10% (v), octane number (RON) of 79, a density of 721 kg hydrotreated coker gasoline / m 3 to 20,000 tons / year traffic cut fractionated in the distillation column 1; distillation column 1 overhead temperature is 88 ° C, bottom temperature 178 ° C, column top pressure of 0.20 MPa (absolute), the column bottom pressure was 0.25MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (distillation range of 30-110 ° C) distilled off through the upper portion of the distillation tower 1, the total distilled is 4.5 million tons / year, and then enters the light petrol hydrogenation unit 3-1 hydrotreating catalyst in the hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20; volume space velocity of the hydrogenation unit 3-1 ratio l.Oh; hydrogen / oil volume ratio of 100; the operating temperature is 220V, the operation pressure is 4.0MPa (absolute); the said light gasoline raffinate of 4.5 million tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (; distillation range 110-185 ° C) to 55,000 tons / year into the flow of heavy gasoline extraction and separation in an extractor 2, an oil separated heavy gasoline and heavy gasoline extraction raffinate; the pumping in column 2 is N- methylpyrrolidone solvent used, the extraction temperature is 130 ° C, solvent ratio (solvent / feed) is 2.5 (mass), ratio of water raffinate was 0.25 (mass), the solvent recovery temperature is 177 ° C, the solvent recovery pressure of 0.15 MPa (absolute); the heavy gasoline raffinate to 40,000 tons / year flow into the hydrogenation unit 3-2 hydrotreating the hydrogenation apparatus 3-2 all catalyst is a hydrogenation catalyst GHT-22; volume space velocity of the hydrogenation unit 3-2 ratio l.Oh "1; hydrogen / oil volume ratio of 250; operating temperature of 250 ° C, the operating pressure of l. OMPa (absolute); the heavy oil fuel out of 1.5 million tons / year into the flow hydrogenation apparatus 3-3 hydrotreating catalyst in the hydrogenation apparatus 3-3 is full hydrogenation catalyst GHT-22 ; volume space velocity of the hydrogenation apparatus 3-3 l.Oh- ratio of hydrogen / oil volume ratio of 250; operating temperature of 250 ° C, the operating pressure is l.OMPa (absolute); the heavy truck Raffinate oil hydrogenation of 4.0 million tons / year as the high ethylene feed flow rate of reforming or mined materials; said heavy gasoline hydrogenation extract oil at a rate of 15,000 tons / year of the light gasoline hydrogenation (45,000 traffic tons / year) as a mixed recovery reconcile gasoline.

The resulting distillation range of the gasoline blending 30-185 ° C, a sulfur content of 23.5 ppm, mercaptan content is less than l.Oppm (; trace, not detected), the olefin content is 15.6% (v), diolefin content is trace, not detected; aromatics content of 19.5% (v), octane number (RON) is 94.1, the density is 716.4 kg / m 3, the amount of recovery is 6.0 million tons / year.

The resulting material quality ethylene material or the reforming distillation range 110-185 ° C, a trace amount of sulfur, not detected, mercaptan content is less than l.Oppm (; trace, not detected;), olefin content trace, not detected, the bromine index (bromine number) 32 (0.032), an aromatic hydrocarbon content of 2.1% (v), octane number (RON) is 71.4, the density is 744.5 kg / m 3, the amount of recoverable 40000 tons / year. GHT-20, as well as physical and chemical properties, and method for measuring the selective hydrogenation catalyst in all hydrogenation apparatus 3-1 other hydrogenation catalyst GHT-22 means the same as in Example 9 Hydrogenation embodiment.

Example 11

The same procedure as in Example 9 a schematic. The distillation range of 30-185 ° C, sulfur content is 800ppm, mercaptan content was 9ppm, olefin content of 36% (v), diolefin content is 0.9% (v), aromatic hydrocarbon content of 17% (v), octane number (RON) of 91, a density of 731 kg / m 3 stabilized gasoline (catalytic gasoline) to 60,000 tons / year traffic cut fractionated in the distillation column 1; the same time, the distillation range of 30-185 ° C, 200 ppm sulfur content, mercaptan content is lppm, the olefin content is less than 0.1% (v) (trace, not detected), diolefin content is less than 0.01% (v) (trace, not detected), an aromatic hydrocarbon content of 8% (v), octane number (RON) of 82, a density of 732 kg of naphtha / m 3 to 20,000 tons / year traffic cut fractionated in the distillation column 1; meanwhile, the a distillation range of 30-185 ° C, sulfur content is 150ppm, mercaptan content is lppm, olefin content is 6% (v), diolefin content is less than 0.01% (V) (; trace, not detected), an aromatic hydrocarbon content of 10% (v), octane number (RON) of 79, a density of 721 kg hydrotreated coker gasoline / m 3 to 20,000 tons / year traffic cut fractionated in the distillation column 1; distillation column 1 top temperature of 97 ° C The bottom temperature was 187 ° C, column top pressure is 0.25MPa (absolute), the column bottom pressure was 0.30MPa (absolute), respectively light gasoline and heavy gasoline, light gasoline the (distillation range 30-110 ° C) an upper portion of the distillation column 1 through evaporated, the total distilled is 4.5 million tons / year, and then enters the light petrol hydrogenation system 3-1 hydrotreating catalyst in the hydrogenation apparatus 3-1 is selective hydrogenation catalyst GHT-20; volume airspeed ratio of the hydrogenation apparatus 3-1 is 2.511- 1; hydrogen / oil volume ratio of 150; operating temperature of 180 ° C, the operating pressure is 2.0MPa (absolute); the said light gasoline raffinate of 4.5 million tons / year as the flow rate of the produced gasoline blending. The heavy gasoline (; distillation range 110-185 ° C) to 55,000 tons / year into the flow of heavy gasoline extraction and separation in an extractor 2, an oil separated heavy gasoline and heavy gasoline extraction raffinate; the pumping in column 2 the solvent used is N- formyl morpholine, the extraction temperature is 150 ° C, solvent ratio (solvent / feed) is 6.0 (mass), ratio of water raffinate oil is 0.3 (mass), the solvent recovery temperature is 185 ° C, the solvent recovery pressure is 0. 2MPa (absolute); the heavy gasoline raffinate to 39,000 tons / year flow into the hydrogenation unit 3-2 hydrotreating the hydrogenation unit 3-2 all of the catalyst is a hydrogenation catalyst GHT-22; the hydrogenation ratio of 3-2 LHSV means of 2.511- 1; hydrogen / oil volume ratio of 300; operating temperature of 285 ° C, an operating pressure of 2.5MPa (absolute); the heavy oil fuel out of 1.6 million tons / year flow into the hydrogenation unit 3-3 hydrotreating catalyst in the hydrogenation apparatus 3-3 is full hydrogenation catalyst GHT-22; the space velocity hydrogenation apparatus 3-3 2.5h- ratio of hydrogen / oil volume ratio of 300; operating temperature of 270 ° C, the operating pressure is 2.5MPa (absolute); the heavy gasoline Raffinate oil hydrogenation of 3.9 million tons / year as the high ethylene feed flow rate of reforming or mined materials; said heavy gasoline hydrogenation the hydrogenated oil is extracted light gasoline mixed with the flow of 16000 tons / year as gasoline pool recovery.

The resulting distillation range of the gasoline blending 30-185 ° C, sulfur content is 25.2ppm, mercaptan content is less than l.Oppm (; trace, not detected;), the olefin content is 19.4% (v), diolefin marks amount, not detected; aromatics content of 20.9% (v), octane number (RON) is 94.3, the density is 718.1 kg / m 3, the amount of recovery of 6.1 million tons / year. The resulting material quality ethylene material or the reforming distillation range 110-185 ° C, a sulfur content trace, not detected, mercaptan content is less than l.Oppm (; trace, not detected;), olefin content trace, not detected, the bromine index (bromine number) 25 (0.025), an aromatic hydrocarbon content of 2.4% (v), octane number (RON) is 74.1, the density is 749.3 kg / m 3, the amount of recoverable 39000 tons / year.

GHT-20, as well as physical and chemical properties, and method for measuring the selective hydrogenation catalyst in all hydrogenation apparatus 3-1 other hydrogenation catalyst GHT-22 means the same as in Example 9 Hydrogenation embodiment.

Industrial Applicability

Advantage of the system and method of the present invention for preparing low sulfur content and low olefin content of the gasoline is: compared with the caustic, the system and method of the present invention first distillation cut, separated and then extracted, and then added depending on the circumstances hydrogen treatment. Not only de-olefins, but also mercaptans, diene (diolefin); secondly, the hydrogenation apparatus according to the present invention, a small, low cost; Finally, the present invention addresses the diverse material, not only processing stabilization of gasoline, can also handle stable and the mixture was hydrogenated naphtha and coker gasoline gasoline. Hydrotreated coker naphtha and gasoline also contains aromatics, optimized chemical light oil, to increase the oil extracted from the gasoline pool, octane enhancers.

Claims

Claims
1, a high-quality gasoline preparation system comprising a distillation means; characterized in that: said upper portion of distillation apparatus are connected via a line light gasoline and light gasoline extraction system; upper part of the extraction system the produced light gasoline directly through line product, the lower part of the light gasoline extraction system connected by line to the hydrogenation unit; a lower portion of the distillation apparatus are connected via a line heavy gasoline and heavy gasoline extraction system; upper portion of the heavy gasoline directly to the extraction system through line recovery product, the lower part of the heavy gasoline extraction system connected by line to the hydrogenation unit.
2. The preparation of high quality gasoline system according to claim 1, wherein: said middle cutting gasoline distillation apparatus and outputs connected by a line to the hydrogenation unit.
3, a method of preparing high quality gasoline, comprises the following steps: stabilizing gasoline or gasoline and naphtha stabilizer added after the distillation apparatus and mixed hydrotreated coker gasoline fractionation, fractionation cut light gasoline and heavy gasoline; the light gasoline was extracted by separation into the upper portion of the distillation apparatus light gasoline extraction system, separated and extracted raffinate oil; oil after the extraction to the hydrogenation unit through line blending process with the use of light gasoline, raffinate oil as the gasoline pool directly taken out; the heavy gasoline separated and extracted heavy gasoline extraction system, separated and extracted raffinate oil; hydrogenated said extracted oil obtained after extracting oil hydrogenation unit through line into the process, and then the gasoline blending using said light, said raffinate as chemical light oil.
The method according to claim 3 of the preparation of high quality gasoline, characterized in that: said cutting means fractionated distillation in the middle and into the gasoline hydrogenation unit hydrotreating.
5. The method according to claim 3 in the preparation of high quality gasoline, characterized in that: said apparatus is a distillation column top temperature of 77~86 ° C, the bottom temperature is 190~192 ° C; the distillation apparatus overhead pressure
. 0. 11~0 28MPa (absolute), the column bottom pressure of 0. 12~0 30MPa (absolute); The control light gasoline distillation range at 30 ° C~90 ° C; distillation range of the heavy gasoline control 90 ° C~205 ° C.
6, according to the method of preparation of high quality gasoline according to claim 4 or claim 5, wherein: said control light gasoline distillation range at 30 ° C~65 ° C; the control in the gasoline distillation range at 65 ° C~90 ° C; the distillation range of the heavy gasoline is controlled to 90 ° C ~ 205. C.
7. A method of preparing high quality gasoline as claimed in claim 6, characterized in that: said hydrogenation unit is full hydrogenation catalyst catalyst GHT-22; volume airspeed ratio of the hydrogenation unit is 2 3; hydrogen / oil volume ratio is 200-300; operating temperature of 285~325 ° C, operating pressure 1.5~2.5MPa (absolute); all the physical and chemical properties of the hydrogenation catalyst in a hydrogenation unit GHT-22 are as follows table. Indicators Unit GHT-22
Appearance - Gray trefoil
Specifications mm Φ 1. 5-2. 0
Strength N / cm 180 Bulk density g / ml 0. 73
The specific surface area m / g 180
Pore ​​volume ml / g 0. 5-0. 6
wo 3 m% 15
NiO m% 1. 7
CoO m% 0. 15
Ν¾0 m% <0. 09
Fe 2 0 3 m% <0 . 06
Si0 2 m% <0. 60
Vector m% 82. 4
8. A method of preparing high quality gasoline, comprises the following steps: addition of stabilized gasoline fractionation distillation apparatus, and the light gasoline cut is fractionated heavy gasoline; light gasoline enters the light gasoline extraction system by separating the upper portion of distillation extraction apparatus separating the raffinate and extract oil; oil after the extraction to the hydrogenation unit through line processing using said light gasoline blending, the raffinate is taken directly as a gasoline blending; the heavy gasoline and naphtha hydrogenated coker gasoline and heavy gasoline together into separate extraction system was extracted, separated and extracted raffinate oil; hydrogenated extract oil obtained after extraction of the oil into the hydrogenation unit through line processing, then the light gasoline blending using, as the raffinate feed quality ethylene.
9, a high quality gasoline preparation system comprising a distillation means; characterized in that: said upper portion of distillation apparatus are connected via a line to a light gasoline extraction system; upper part of the light gasoline product extraction system through line direct recovery, a lower portion of the light gasoline extraction system connected by line to the hydrogenation unit; a lower portion of the distillation apparatus are connected via a line to the hydrogenation unit; means connected to said hydrotreating the heavy gasoline via line extraction system; the an upper portion of said heavy gasoline extraction system through line directly collected product, the lower part of the heavy gasoline extraction system connected by line to the upper portion of the light petrol pipeline extraction system.
10. A method of preparing high quality gasoline, comprises the following steps: addition of the stabilizer or stabilizing a gasoline fractionating distillation apparatus with gasoline and naphtha, and hydrotreated coker gasoline, light gasoline cut is fractionated and the heavy gasoline; the light gasoline was extracted by separation into the upper portion of the distillation apparatus light gasoline extraction system, separated and extracted raffinate oil; raffinate oil as the gasoline pool is taken directly out of the oil extraction process through line before entering into the hydrogenation unit weight gas extraction system for extraction separation; the heavy petrol hydrogenation unit through the post-treatment also enters the extraction system of the heavy petrol separated and extracted; isolated after separation extracted through an extraction system of the heavy fuel oil, and heavy gasoline withdrawn heavy gasoline raffinate; the heavy gas oil through a line drawn with the light petrol raffinate oil drainage after mixing as a gasoline blending, the heavy gasoline raffinate taken out as a high-quality vinyl material.
11. The method of claim preparation of high quality gasoline according to claim 10, wherein: the distillation apparatus is a distillation column overhead temperature of 77~86 ° C, the bottom temperature is 189~192 ° C; overhead pressure to 0. 11~
0. 28MPa (absolute), the column bottom pressure of 0. 12~0 30MPa (absolute); The control light gasoline distillation range at 30 ° C -100 ° C; the distillation range of the heavy gasoline is controlled to 100 ° C~205 ° C.
12. The method according to claim 11 to produce high quality gasoline, characterized in that: the catalyst in the hydrogenation apparatus is a full hydrogenation catalyst GHT-22; space velocity of the hydrogenation unit was 2.5; hydrogen / oil volume ratio of 200; operating temperature of 285 ° C, the operating pressure of 1. 5MPa (absolute).
13, a high-quality gasoline preparation system comprising a distillation means; characterized in that: said upper portion of distillation apparatus are connected via a line to a light gasoline extraction system; upper part of the light gasoline product extraction system through line direct recovery, a lower portion of the light gasoline extraction system connected by line to the hydrogenation unit; a lower portion of the distillation apparatus via line connected to the extraction system of the heavy gasoline; upper portion of the heavy gasoline extraction system through line to another phase hydrogenation unit the product was taken directly connected or; a lower portion of said heavy gasoline extraction system connected by line to the hydrogenation unit; said distillation means coupled through line central to the gasoline extraction system; upper part of the extraction system through line gasoline hydrogenation unit is connected to a further, lower part of the extraction system through line gasoline hydrogenation unit is connected with.
14. A method of preparing high quality gasoline, comprises the following steps: stabilizing gasoline or naphtha and gasoline stabilization hydrotreated coker gasoline fractionation distillation apparatus is added together, fractionation light gasoline cut, gasoline and heavy gasoline; the separating said extracted light gasoline distillation apparatus enters through the upper light gasoline extraction system, separated light gasoline and light gas oil extraction raffinate; a light raffinate oil as gasoline blending gasoline direct recovery, the light gasoline extract oil use the remaining oil mixed with the light gasoline pumped to the hydrogenation unit through line after treatment as gasoline pool; gasoline in the gasoline in the separatory extraction extraction system, separated from the gasoline and gasoline oil extraction raffinate; after obtaining the extraction of the oil in the gasoline to the hydrogenation unit through line extract oil hydrogenation treatment, then after mixing the light gasoline used as gasoline blending, the gasoline raffinate oil hydrogenation unit through line into the process as a high vinyl material taken out; the heavy gasoline separated and extracted heavy gasoline extraction system, separated from the extracted oil and heavy gasoline heavy truck Raffinate; after oil extraction the heavy gasoline hydrogenation unit through line enters the extraction process to obtain hydrogenated oil, and then after mixing the light gasoline used as gasoline blending, the weight low pour diesel oil or petrol raffinate oil as a direct Produced as a Postharvest quality ethylene material or to the hydrogenation unit through line process.
15. The method of preparing high quality gasoline claimed in claim 14, wherein: the distillation apparatus is a distillation column overhead temperature of 77~86 ° C, the bottom temperature is 190~192 ° C; overhead pressure of 0. 11~ 0. 28MPa (absolute), the column bottom pressure of 0. 12~0 30MPa (absolute); the control light gasoline distillation range at 30 ° C ~ 80 ° C; in the gasoline control the distillation range at 80 ° C~160 ° C; the distillation range of the heavy gasoline is controlled to 160 ° C~205 ° C.
16. The method according to claim 15 to produce high quality gasoline, characterized in that: said hydrogenation unit is full hydrogenation catalyst catalyst GHT-22; volume airspeed ratio of the hydrogenation unit is 2 3; hydrogen / oil volume ratio is 200-300; operating temperature of 285~325 ° C, the operating pressure of 1. 5~2 5MPa (absolute).
17. A system for producing high quality gasoline, characterized by: a distillation system and the extraction system hydrogenation apparatus, an upper portion of the distillation system is connected via a line to a light petrol hydrogenation unit; a lower portion of the distillation system through line connected to the extraction system; the extraction system through line with the upper raffinate phase hydrogenation unit is connected to the lower part of the extraction system is connected via a line to the oil hydrogenation extracting means; hydrogenating said extract oil means connected by a line to the end line light petrol hydrogenation unit.
18, a method of preparing high quality gasoline, the following steps: a raw material in the distillation system cutting fractionation, respectively light gasoline and heavy gasoline, light gasoline through the upper part of the distillation system was distilled off, and then enters the light petrol hydrogenation unit in hydrotreating, hydrotreated light gasoline as a gasoline blending recovery; extraction of the heavy gasoline enters the extraction system, the extract oil was separated heavy gasoline and heavy gasoline raffinate; the heavy gasoline raffinate after extracting the heavy oil into gasoline hydrogenation apparatus for extracting oil hydrotreating processing; raffinate oil hydrogenation unit into the hydrotreating the hydrotreated feed out a high-quality ethylene material or reforming mining Produced as a gasoline pool after the hydrogenation treatment after mixing light gasoline.
19. A method for preparing high quality gasoline according to claim 18, wherein: said distillation system is a distillation column overhead temperature of 78~97 ° C, the bottom temperature is 167~187 ° C; overhead pressure 0.15~ 0.25MPa (absolute), the column bottom pressure 0.20~0.30MPa (absolute); the control light gasoline distillation range at 30 ° C ~ 110 ° C; the distillation range of the heavy gasoline is controlled to 110 ° C~185 ° C.
20. The method according to claim 19 to produce high quality of the gasoline, which is characterized in that: said light petrol hydrogenation unit is selective hydrogenation catalyst is a catalyst GHT-20; empty volume of the light petrol hydrogenation unit ratio of lO Oh- 1; hydrogen / oil volume ratio of 100~300; operating temperature of 150~220 ° C, operating pressure 1.0~4.0MPa (absolute); raffinate oil hydrogenation catalyst in the pumping apparatus is full hydrogenation catalyst GHT-22; the raffinate hydrotreating apparatus 1.0~4.0h- hourly space velocity ratio hydrogen / oil volume ratio of 250~500; operating temperature of 250~320 ° C, the operating pressure of 1.0 ~4.0MPa (absolute); extracting the oil hydrogenation unit is full hydrogenation catalyst catalyst GHT-22; volume airspeed ratio of the extracted oil hydrogenation apparatus for lO ^ .Oh; hydrogen / oil volume ratio 250 to 500; the operating temperature is 250 290 ° C, operating pressure 1.0 ~ 4.0MPa (absolute).
21. The method as claimed in claim 20, the preparation of high quality gasoline, characterized in that: the extraction system used in the solvent is sulfolane, the extraction temperature is 120 ° C, solvent ratio (solvent / feed) is 3.5 (mass ), washed with water raffinate oil is 0.2 (mass), the solvent recovery temperature is 165 ° C, the solvent recovery pressure is 0.1MPa (absolute).
22. The method of claim preparation of high quality gasoline according to claim 20, wherein: the extraction system used in the solvent is N- methylpyrrolidone, extraction temperature of 130 ° C, solvent ratio (solvent / feed) 2.5 (mass), ratio of water raffinate was 0.25 (mass), the solvent recovery temperature is 177 ° C, the solvent recovery pressure of 0.15 MPa (absolute).
23. The method of claim preparation of high quality gasoline according to claim 20, wherein: the extraction system used in the solvent is N- formyl morpholine, the extraction temperature is 150 ° C, solvent ratio (solvent / feed ) is 6.0 (mass), ratio of water raffinate oil is 0.3 (mass), the solvent recovery temperature is 185 ° C, the solvent recovery pressure is 0.2MPa
(Absolutely).
24. A method according to claim 23 to produce high quality gasoline according to any one of claim 21, wherein: Properties selective hydrogenation catalyst GHT-20 of the light gasoline hydrogenation unit in the following table 1 shown, the raffinate oil hydrogenation apparatus and physicochemical properties of the extracted oil hydrogenation full hydrogenation catalyst GHT-22 apparatus in the table 2 below.
Table 1
PCT/CN2009/070239 2008-01-29 2009-01-21 A system and a process for producing high quality gasoline WO2009094934A1 (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
CN200810005207.2 2008-01-29
CN 200810005206 CN101497807B (en) 2008-01-29 2008-01-29 System and method for preparing high quality petrol
CN 200810005208 CN101497808B (en) 2008-01-29 2008-01-29 System and method for preparing high quality petrol
CN200810005205.3 2008-01-29
CN 200810005205 CN101497806B (en) 2008-01-29 2008-01-29 System and method for preparing high quality petrol
CN 200810005207 CN101497809B (en) 2008-01-29 2008-01-29 Method for preparing high quality petrol
CN200810005206.8 2008-01-29
CN200810005208.7 2008-01-29

Publications (1)

Publication Number Publication Date
WO2009094934A1 true true WO2009094934A1 (en) 2009-08-06

Family

ID=40912282

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2009/070239 WO2009094934A1 (en) 2008-01-29 2009-01-21 A system and a process for producing high quality gasoline

Country Status (1)

Country Link
WO (1) WO2009094934A1 (en)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1994022980A1 (en) * 1993-04-02 1994-10-13 Mobil Oil Corporation Gasoline upgrading process
US6007704A (en) * 1996-09-24 1999-12-28 Institut Francais Du Petrole Process for the production of catalytic cracking gasoline with a low sulphur content
CN1400282A (en) * 2001-07-31 2003-03-05 中国石油化工股份有限公司 Catalytic conversion method for reducing olefine, sulfur and nitrogen contents in gasoline
WO2003080769A1 (en) * 2002-03-21 2003-10-02 Chevron U.S.A. Inc. New hydrocracking process for the production of high quality distillates from heavy gas oils
CN1470607A (en) * 2003-07-04 2004-01-28 北京金伟晖工程技术有限公司 Catalytic hydrocarbon reforming treatment method
CN201154953Y (en) * 2007-11-09 2008-11-26 丁冉峰 System for preparing high quality gasoline by catalytic hydrocarbon recombination
CN201186917Y (en) * 2008-01-29 2009-01-28 丁冉峰 System for preparing high-quality petrol

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1994022980A1 (en) * 1993-04-02 1994-10-13 Mobil Oil Corporation Gasoline upgrading process
US6007704A (en) * 1996-09-24 1999-12-28 Institut Francais Du Petrole Process for the production of catalytic cracking gasoline with a low sulphur content
CN1400282A (en) * 2001-07-31 2003-03-05 中国石油化工股份有限公司 Catalytic conversion method for reducing olefine, sulfur and nitrogen contents in gasoline
WO2003080769A1 (en) * 2002-03-21 2003-10-02 Chevron U.S.A. Inc. New hydrocracking process for the production of high quality distillates from heavy gas oils
CN1470607A (en) * 2003-07-04 2004-01-28 北京金伟晖工程技术有限公司 Catalytic hydrocarbon reforming treatment method
CN201154953Y (en) * 2007-11-09 2008-11-26 丁冉峰 System for preparing high quality gasoline by catalytic hydrocarbon recombination
CN201186917Y (en) * 2008-01-29 2009-01-28 丁冉峰 System for preparing high-quality petrol

Similar Documents

Publication Publication Date Title
US5059303A (en) Oil stabilization
US5021143A (en) Process of fractionation and extraction of hydrocarbons allowing obtaining a cut of increased octane index and a kerosene of improved smoke point
CN101787307A (en) Gasoline hydrodesulfurization method
CN1465668A (en) Method for producing low sulfur gasoline
CN101469274A (en) Method for producing high-octane petrol
CN1903994A (en) Method of producing fuel oil by coal tar hydrogenation modifying
CN201241102Y (en) Naphtha fecundation aromatic hydrocarbons reforming system
CN1746265A (en) Catalyzing and cracking process of inferior oil
CN102757818A (en) Sulfur-free gasoline production method
CN101024780A (en) Method for hydrogenation cracking anthracent
CN101028985A (en) Method for producing benzene arenes from coarse benzene
CN103013559A (en) Hydrocracking method for selective increasing of aviation kerosene yield
CN103205272A (en) Method for production of purified coal tar pitch from high temperature coal tar
CN101575533A (en) Improved method for preparing fuel oil by coal tar hydrogenation
CN1144259A (en) Method for producing extraction solvent naphtha by catalytic reforming device
US7122114B2 (en) Desulfurization of a naphtha gasoline stream derived from a fluid catalytic cracking unit
CN102041029A (en) Comprehensive utilization method of hydrocracking tail oil
CN1470607A (en) Catalytic hydrocarbon reforming treatment method
US20040094455A1 (en) Process for desulfurization comprising a stage for selective hydrogenation of diolefins and a stage for extraction of sulfur-containing compounds
CN1900032A (en) Method for producing benzene aromatic hydrocarbon from crude benzole
CN103305258A (en) Method for reducing viscosity of quenching oil of ethylene unit
CN1590510A (en) Highly desulfur and decolour method of diesel oil distillation fraction
CN101899326A (en) Shale oil catalytic upgrading method
CN1613976A (en) Catalytic hydrocarbon recombinant treating method
CN101089144A (en) Heavy oil and residual oil combined treating process

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09707043

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase in:

Ref country code: DE

122 Ep: pct app. not ent. europ. phase

Ref document number: 09707043

Country of ref document: EP

Kind code of ref document: A1