CN111500317A - Production process of isomerized gasoline - Google Patents
Production process of isomerized gasoline Download PDFInfo
- Publication number
- CN111500317A CN111500317A CN202010329529.3A CN202010329529A CN111500317A CN 111500317 A CN111500317 A CN 111500317A CN 202010329529 A CN202010329529 A CN 202010329529A CN 111500317 A CN111500317 A CN 111500317A
- Authority
- CN
- China
- Prior art keywords
- tower
- isopentane
- heat exchange
- cooled
- stabilizing
- Prior art date
- Legal status (The legal status 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 status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
- C10G61/02—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses an isomerized gasoline production process, which can rapidly produce isomerized oil to meet increasing demands, and the isomerized gasoline is favorable for improving the antiknock index of blended gasoline, and simultaneously can adjust the octane number of the front end of the gasoline to ensure that the octane number of gasoline fractions is reasonably distributed, thereby improving the starting performance of an engine and being an ideal component of clean gasoline.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a process for producing isomerized gasoline.
Background
In recent years, with the increasing importance of the country on environmental protection, the quality specification of the motor gasoline product is higher and higher, and the limitation on the content of aromatic hydrocarbon and olefin in the gasoline is stricter and stricter. The isomerized gasoline is an environment-friendly product with low sulfur, no olefin, no benzene and no aromatic hydrocarbon, and is an excellent blending component of the motor gasoline. As the restriction of the motor gasoline on the content of aromatic hydrocarbons and olefins becomes more and more strict, the demand for the isomerized oil with a high octane number is greatly increased, and thus the production of the isomerization becomes more important. The invention provides a production process of gasoline isomerization, which can rapidly produce isomerized oil to meet increasing demands.
Disclosure of Invention
The invention aims to provide an isomerized gasoline production process, which can rapidly produce isomerized oil to meet increasing demands.
In order to solve the technical problems, the invention adopts the following technical scheme:
the invention relates to an isomerized gasoline production process, which comprises the following specific steps:
A. feeding light naphtha into a feeding buffer tank, and pressurizing the light naphtha by a feeding pump of a de-isopentane tower;
B. conveying the pressurized light naphtha into a raw material-product heat exchanger for heat exchange to 50-70 ℃, and then conveying the light naphtha into an isopentane removal tower;
C. the gas phase at the tower top is conveyed to a public rectifying tower for continuous separation;
D. cooling the gas phase at the top of the public rectifying tower by an air cooler of an isopentane removal tower, sending the cooled gas phase to a reflux tank of the isopentane removal tower, pressurizing the isopentane by a reflux pump of the isopentane removal tower, circulating the isopentane to the isopentane removal tower, and pressurizing the liquid phase at the bottom of the public rectifying tower by a circulating pump at the bottom of the public rectifying tower and returning the liquid phase to the isopentane removal tower;
E. the heavy component at the bottom of the tower is pressurized to 3.5MPa by a reaction feed pump, then mixed with circulating hydrogen, enters a reaction feed-discharge heat exchanger for heat exchange, enters a steam heater for vaporization after the heat exchange is carried out to 136 ℃, is heated to the reaction temperature of 140 ℃, and then is sent to an isomerization reactor for reaction to form a reaction product;
F. the reaction product is sent into a reaction feeding and discharging heat exchanger for heat exchange and cooling to 106 ℃, then sent into a raw material-product hot gas for heat exchange with the newly sent light naphtha, the heat is fully recovered until the temperature is cooled to 77 ℃, and the cooled reaction product is cooled to 40 ℃ by a water cooling agent and then sent to a reaction product buffer tank for gas-liquid separation;
G. crude hydrogen gas phase enters a recycle hydrogen compressor after being separated from the tank top of a reaction product buffer tank through a compressor inlet buffer tank, is mixed with fresh hydrogen after being pressurized to 3.35MPa, is sent to a compressor outlet buffer tank for liquid separation, is sent to a dryer, and is recycled to an isomerization reactor after moisture in the recycle hydrogen is removed;
H. the liquid phase at the bottom of the reaction product buffer tank enters a stabilizing tower feeding and discharging heat exchanger under self pressure, and enters the stabilizing tower after heat exchange and temperature rise to 120-125 ℃;
I. the gas phase at the top of the stabilization tower is cooled to 45-50 ℃ by a condenser at the top of the stabilization tower and then enters a reflux tank of the stabilization tower, the gas phase dry gas in the reflux tank of the stabilization tower is cooled to 40 ℃ by a cooler of the reflux tank of the stabilization tower and then discharged to a fuel gas pipe network, and the liquid is pressurized by a reflux pump of the stabilization tower and then flows back to the top of the stabilization tower;
J. the isomerized gasoline at the bottom of the stabilizing tower is subjected to heat exchange and temperature reduction to 75-80 ℃ by a stabilizing tower charging and discharging heat exchanger, then is conveyed to a product cooler to be water-cooled to 40 ℃, and then is conveyed to a tank field.
Further, the heat exchange temperature of the pressurized light naphtha is optimally 60 ℃ when the pressurized light naphtha is conveyed into a raw material-product heat exchanger.
Further, the light naphtha after heat exchange is sent to a de-isopentane tower, wherein the top of the operating pressure in the de-isopentane tower is 0.18MPa, the bottom of the operating pressure is 0.21MPa, the operating temperature is 60 ℃ at the top, and the temperature at the bottom is 85 ℃.
Further, the gas phase at the top of the tower is conveyed to a public rectifying tower for continuous separation, the operation pressure at the top of the tower is 0.17MPa, the operation temperature is 50 ℃, the pressure at the bottom of the tower is 0.18MPa, and the operation temperature is 60 ℃.
Further, the liquid phase at the bottom of the reaction product buffer tank enters a stabilizing tower feeding and discharging heat exchanger under self pressure, and enters the stabilizing tower after the heat exchange temperature is raised to 123 ℃.
Further, the gas phase at the top of the stabilizing tower is cooled to 47 ℃ by a condenser at the top of the stabilizing tower through water and then enters a reflux tank of the stabilizing tower.
Further, the isomerized gasoline at the bottom of the stabilizing tower exchanges heat and is cooled to 77 ℃ through a feed and discharge heat exchanger of the stabilizing tower.
Compared with the prior art, the invention has the beneficial technical effects that:
the invention provides a production process of isomerized gasoline, which can rapidly produce isomerized oil to meet increasing demands, and the isomerized gasoline is favorable for improving the antiknock index of blended gasoline, and simultaneously can adjust the octane number of the front end of the gasoline to ensure that the octane number of gasoline fraction is reasonably distributed, thereby improving the starting performance of an engine and being an ideal component of clean gasoline.
Detailed Description
A production process of isomerized gasoline comprises the following steps:
A. feeding light naphtha into a feeding buffer tank, and pressurizing the light naphtha by a feeding pump of a de-isopentane tower;
B. conveying the pressurized light naphtha into a raw material-product heat exchanger for heat exchange to 60 ℃, and then conveying the light naphtha into a de-isopentane tower (the top of the operating pressure is 0.18MPa, the bottom of the operating pressure is 0.21MPa, the operating temperature is 60 ℃ at the top, and the bottom of the operating temperature is 85 ℃);
C. the gas phase at the top of the tower is conveyed to a public rectifying tower for continuous separation (the operation pressure at the top in the tower is 0.17MPa, the operation temperature is 50 ℃, the pressure at the bottom of the tower is 0.18MPa, and the operation temperature is 60 ℃);
D. cooling the gas phase at the top of the public rectifying tower by an air cooler of an isopentane removal tower, sending the cooled gas phase to a reflux tank of the isopentane removal tower, pressurizing the isopentane by a reflux pump of the isopentane removal tower, circulating the isopentane to the isopentane removal tower, and pressurizing the liquid phase at the bottom of the public rectifying tower by a circulating pump at the bottom of the public rectifying tower and returning to the isopentane removal tower;
E. the heavy components at the bottom of the de-isopentane tower are pressurized to 3.5MPa by a reaction feed pump, mixed with circulating hydrogen, enter a reaction feed-discharge heat exchanger for heat exchange, enter a steam heater for vaporization after the heat exchange is carried out to 136 ℃, are heated to the reaction temperature of 140 ℃, and are sent to an isomerization reactor for reaction to form a reaction product;
F. the reaction product is sent into a reaction feeding and discharging heat exchanger for heat exchange and cooling to 106 ℃, then sent into a raw material-product hot gas for heat exchange with the newly sent light naphtha, the heat is fully recovered until the temperature is cooled to 77 ℃, and the cooled reaction product is cooled to 40 ℃ by a water cooling agent and then sent to a reaction product buffer tank for gas-liquid separation;
G. crude hydrogen gas phase enters a recycle hydrogen compressor after being separated from the tank top of a reaction product buffer tank through a compressor inlet buffer tank, is mixed with fresh hydrogen after being pressurized to 3.35MPa, is sent to a compressor outlet buffer tank for liquid separation, is sent to a dryer, and is recycled to an isomerization reactor after moisture in the recycle hydrogen is removed;
H. the liquid phase at the bottom of the reaction product buffer tank enters a stabilizing tower feeding and discharging heat exchanger under self-pressure, and enters the stabilizing tower after the heat exchange and temperature rise to 123 ℃;
I. the gas phase at the top of the stabilization tower is cooled to 47 ℃ by a condenser at the top of the stabilization tower and then enters a reflux tank of the stabilization tower, the gas phase dry gas in the reflux tank of the stabilization tower is cooled to 40 ℃ by a cooler of the reflux tank of the stabilization tower and then discharged to a fuel gas pipe network, and the liquid is pressurized by a reflux pump of the stabilization tower and then flows back to the top of the stabilization tower;
J. the isomerized gasoline at the bottom of the stabilizing tower is subjected to heat exchange and temperature reduction to 77 ℃ by a stabilizing tower charging and discharging heat exchanger, then is conveyed to a product cooler to be water-cooled to 40 ℃, and then is conveyed to a tank area.
The above-described embodiments are merely illustrative of the preferred embodiments of the present invention, and do not limit the scope of the present invention, and various modifications and improvements of the technical solutions of the present invention can be made by those skilled in the art without departing from the spirit of the present invention, and the technical solutions of the present invention are within the scope of the present invention defined by the claims.
Claims (7)
1. A process for producing isomerized gasoline is characterized in that: the method comprises the following specific steps:
A. feeding light naphtha into a feeding buffer tank, and pressurizing the light naphtha by a feeding pump of a de-isopentane tower;
B. conveying the pressurized light naphtha into a raw material-product heat exchanger for heat exchange to 50-70 ℃, and then conveying the light naphtha into an isopentane removal tower;
C. the gas phase at the tower top is conveyed to a public rectifying tower for continuous separation;
D. cooling the gas phase at the top of the public rectifying tower by an air cooler of an isopentane removal tower, sending the cooled gas phase to a reflux tank of the isopentane removal tower, pressurizing the isopentane by a reflux pump of the isopentane removal tower, circulating the isopentane to the isopentane removal tower, and pressurizing the liquid phase at the bottom of the public rectifying tower by a circulating pump at the bottom of the public rectifying tower and returning the liquid phase to the isopentane removal tower;
E. the heavy component at the bottom of the tower is pressurized to 3.5MPa by a reaction feed pump, then mixed with circulating hydrogen, enters a reaction feed-discharge heat exchanger for heat exchange, enters a steam heater for vaporization after the heat exchange is carried out to 136 ℃, is heated to the reaction temperature of 140 ℃, and then is sent to an isomerization reactor for reaction to form a reaction product;
F. the reaction product is sent into a reaction feeding and discharging heat exchanger for heat exchange and cooling to 106 ℃, then sent into a raw material-product hot gas for heat exchange with the newly sent light naphtha, the heat is fully recovered until the temperature is cooled to 77 ℃, and the cooled reaction product is cooled to 40 ℃ by a water cooling agent and then sent to a reaction product buffer tank for gas-liquid separation;
G. crude hydrogen gas phase enters a recycle hydrogen compressor after being separated from the tank top of a reaction product buffer tank through a compressor inlet buffer tank, is mixed with fresh hydrogen after being pressurized to 3.35MPa, is sent to a compressor outlet buffer tank for liquid separation, is sent to a dryer, and is recycled to an isomerization reactor after moisture in the recycle hydrogen is removed;
H. the liquid phase at the bottom of the reaction product buffer tank enters a stabilizing tower feeding and discharging heat exchanger under self pressure, and enters the stabilizing tower after heat exchange and temperature rise to 120-125 ℃;
I. the gas phase at the top of the stabilization tower is cooled to 45-50 ℃ by a condenser at the top of the stabilization tower and then enters a reflux tank of the stabilization tower, the gas phase dry gas in the reflux tank of the stabilization tower is cooled to 40 ℃ by a cooler of the reflux tank of the stabilization tower and then discharged to a fuel gas pipe network, and the liquid is pressurized by a reflux pump of the stabilization tower and then flows back to the top of the stabilization tower;
J. the isomerized gasoline at the bottom of the stabilizing tower is subjected to heat exchange and temperature reduction to 75-80 ℃ by a stabilizing tower charging and discharging heat exchanger, then is conveyed to a product cooler to be water-cooled to 40 ℃, and then is conveyed to a tank field.
2. The isomerized gasoline production process of claim 1, wherein: the heat exchange temperature of the pressurized light naphtha is optimally 60 ℃ when the pressurized light naphtha is conveyed into a raw material-product heat exchanger.
3. The isomerized gasoline production process of claim 1, wherein: and (3) feeding the light naphtha subjected to heat exchange into a de-isopentane tower, wherein the top of the operation pressure in the de-isopentane tower is 0.18MPa, the bottom of the operation pressure is 0.21MPa, the operation temperature is 60 ℃ at the top, and the temperature at the bottom of the operation temperature is 85 ℃.
4. The isomerized gasoline production process of claim 1, wherein: the gas phase at the top of the tower is conveyed to a public rectifying tower for continuous separation, the operation pressure at the top in the tower is 0.17MPa, the operation temperature is 50 ℃, the pressure at the bottom of the tower is 0.18MPa, and the operation temperature is 60 ℃.
5. The isomerized gasoline production process of claim 1, wherein: the liquid phase at the bottom of the reaction product buffer tank enters a stabilizing tower feeding and discharging heat exchanger under self pressure, and enters the stabilizing tower after the heat exchange temperature is raised to 123 ℃.
6. The isomerized gasoline production process of claim 5, wherein: and the gas phase at the top of the stabilizing tower is cooled to 47 ℃ by a condenser at the top of the stabilizing tower through water and then enters a reflux tank of the stabilizing tower.
7. The isomerized gasoline production process of claim 1, wherein: the isomerized gasoline at the bottom of the stabilizing tower is cooled to 77 ℃ through heat exchange of a feed and discharge heat exchanger of the stabilizing tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010329529.3A CN111500317A (en) | 2020-04-24 | 2020-04-24 | Production process of isomerized gasoline |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010329529.3A CN111500317A (en) | 2020-04-24 | 2020-04-24 | Production process of isomerized gasoline |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111500317A true CN111500317A (en) | 2020-08-07 |
Family
ID=71866646
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010329529.3A Pending CN111500317A (en) | 2020-04-24 | 2020-04-24 | Production process of isomerized gasoline |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111500317A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101544905B (en) * | 2008-03-27 | 2012-09-12 | 中国石油化工股份有限公司 | Light hydrocarbon isomerization method |
| CN104945212A (en) * | 2015-06-03 | 2015-09-30 | 上海河图工程股份有限公司 | C5/C6 alkane low-temperature isomerization method |
| US20170044447A1 (en) * | 2014-04-29 | 2017-02-16 | Axens | Gasoline production process comprising an isomerization step followed by at least two separation steps |
| CN209113783U (en) * | 2018-11-26 | 2019-07-16 | 山东海成石化工程设计有限公司 | A kind of separation system using divided wall column separating high-purity isopentane and pentane |
-
2020
- 2020-04-24 CN CN202010329529.3A patent/CN111500317A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101544905B (en) * | 2008-03-27 | 2012-09-12 | 中国石油化工股份有限公司 | Light hydrocarbon isomerization method |
| US20170044447A1 (en) * | 2014-04-29 | 2017-02-16 | Axens | Gasoline production process comprising an isomerization step followed by at least two separation steps |
| CN104945212A (en) * | 2015-06-03 | 2015-09-30 | 上海河图工程股份有限公司 | C5/C6 alkane low-temperature isomerization method |
| CN209113783U (en) * | 2018-11-26 | 2019-07-16 | 山东海成石化工程设计有限公司 | A kind of separation system using divided wall column separating high-purity isopentane and pentane |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN216536963U (en) | Separation system of sulfuric acid alkylation reaction product | |
| CN115317945B (en) | Two-tower thermal coupling and heat pump combined separation process and separation device for alkylation reaction product | |
| CN105647581B (en) | Gasoline hydrogenation method | |
| CN101092570B (en) | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon | |
| CN104784953A (en) | Reaction product separation system for preparing propylene with methanol and quenching system of reaction product separation system | |
| CN108587684A (en) | A kind of joint aromatics production line CONTINUOUS REFORMER unit | |
| CN105670689A (en) | Kerosene-hydrogenation production process and system | |
| CN111500317A (en) | Production process of isomerized gasoline | |
| CN105331389B (en) | One kind reforms heat recovery and utilization technique and device | |
| CN216536970U (en) | Deisobutanizer energy-saving separation system | |
| CN113150825B (en) | Gasoline light fraction deep processing technology | |
| RU128612U1 (en) | ENGINE FOR FUEL FUELS | |
| CN205188215U (en) | Reformation heat recovery utilizes device | |
| CN111534327B (en) | Reforming pretreatment system, reforming pretreatment method and application | |
| CN115716771A (en) | Quenching oil system and quenching method of ethylene cracking device | |
| CN212025224U (en) | Fine separation device for olefin catalytic cracking products | |
| WO2016000456A1 (en) | Method for preparing light oil | |
| CN115948180B (en) | Energy-saving and environment-friendly process for producing mixed aromatic hydrocarbon by cracking carbon nine and hydrogenation | |
| CN114085682B (en) | Sulfuric acid alkylation reaction method and device and heat extraction method for sulfuric acid alkylation reaction | |
| CN114958418B (en) | Method for producing residual oil by heating furnace | |
| CN111217665B (en) | Fine separation device and separation method for olefin catalytic cracking product | |
| CN111362773A (en) | Equipment and process for preparing pentane foaming agent by reforming topped naphtha | |
| CN210065671U (en) | Device for producing white oil by direct coal liquefaction | |
| CN104449827B (en) | A kind of system and method reducing ethylene unit quench oil viscosity | |
| CN210825992U (en) | Device for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200807 |
|
| RJ01 | Rejection of invention patent application after publication |