CN111019686A - A fractionation system for gasoline project - Google Patents
A fractionation system for gasoline project Download PDFInfo
- Publication number
- CN111019686A CN111019686A CN201911268786.4A CN201911268786A CN111019686A CN 111019686 A CN111019686 A CN 111019686A CN 201911268786 A CN201911268786 A CN 201911268786A CN 111019686 A CN111019686 A CN 111019686A
- Authority
- CN
- China
- Prior art keywords
- gasoline
- oil
- tank
- pipeline
- heat
- 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
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a fractionation system for a gasoline project, which relates to the field of petroleum processing and comprises the following components: a raw material tank: for storing the petroleum raw material produced by the production, the petroleum raw material generally comprises: petroleum gas, gasoline, kerosene, diesel oil, heavy oil, and the like; a heat exchanger: the system is used for preheating crude oil, gasoline and the like, heating the crude oil, the gasoline and the like to a certain temperature, and reducing the fuel consumption in the subsequent fractionation process; a gasoline prefractionator: the method is used for carrying out rough fractionation on gasoline, and heating the gasoline to evaporate substances with low boiling points in the raw materials and enter the top end of a prefractionator. By the aid of the gas buffer tank and the heat-conducting oil furnace, noncondensable gas generated during gasoline production and recovered hydrogen can be combusted through the incinerator in the heat-conducting oil furnace to heat exchange oil in the oil furnace, byproducts of raw materials can be fully utilized, the use efficiency of crude oil is improved, fuel consumption is reduced, and economic benefits are improved.
Description
Technical Field
The invention relates to the field of petroleum processing, in particular to a fractionation system for a gasoline project.
Background
In industry, petroleum is first heated to 400-500 deg.c to become vapor and then fed into fractionating tower. The higher the position in the fractionation column, the lower the temperature. The petroleum vapors are gradually liquefied, cooled and condensed into liquid fractions on the way up. The gaseous fraction having a small molecular weight and a low boiling point gradually rises along the column and condenses in the upper layer of the column, for example, Fuel Gas (Fuel Gas), Liquefied Petroleum Gas (LPG), light oil (Naphtha), Kerosene (Kerosene), and the like. The liquid fraction with larger molecules and higher boiling point is condensed at the bottom of the tower, such as Diesel oil (Diesel), lubricating oil and wax. The viscous residue left at the bottom of the column is bitumen and Heavy Oil (Heavy Oil), which can be used as feedstock for coking and bitumen production or as boiler fuel. The various fractions are collected at each level and transported via conduits away from the fractionation column. These fractionated products are petrochemical feedstocks and can be further processed into a variety of chemicals. It is a physical change.
At present when gasoline fractionates, can adopt multiunit heater and condenser to heat cooling treatment to crude oil, make the different material separation in the crude oil, but when heating cooling treatment, can not abundant utilization heat, need repeatedly heat up the cooling to crude oil, cause thermal loss, reduce economic benefits, and the waste gas that produces after the crude oil schizolysis separation is usually through burning furnace direct emission, does not retrieve it, causes the waste.
Disclosure of Invention
The invention aims to: in order to solve the problems that when heating and cooling treatment are carried out, heat cannot be fully utilized, crude oil needs to be heated and cooled repeatedly, heat loss is caused, economic benefit is reduced, waste gas generated after crude oil cracking and separation is generally directly discharged through an incinerator, and is not recycled, so that waste is caused, and a fractionation system for a gasoline project is provided.
In order to achieve the purpose, the invention provides the following technical scheme: a fractionation system for a gasoline project, comprising:
a raw material tank: for storing the petroleum raw material produced by the production, the petroleum raw material generally comprises: petroleum gas, gasoline, kerosene, diesel oil, heavy oil, and the like;
a heat exchanger: the system is used for preheating crude oil, gasoline and the like, heating the crude oil, the gasoline and the like to a certain temperature, and reducing the fuel consumption in the subsequent fractionation process;
a gasoline prefractionator: the method is used for carrying out rough fractionation on gasoline, heating the gasoline to evaporate substances with low boiling points in raw materials and feeding the evaporated substances into the top end of a prefractionator;
a cooler: the cooling device is used for cooling and radiating the high-temperature cooling liquid to restore the cooling liquid to normal temperature;
a reflux tank: the naphtha and the non-condensable gas are temporarily stored, and part of the naphtha is pumped back to the fractionating tower to provide a liquid phase;
naphtha oil tank: for storing naphtha;
a gas buffer tank: the device is used for storing non-condensable gas and inflammable gas such as hydrogen sulfide in the subsequent process;
a gasoline fractionating tower: the system is used for fractionating gasoline, and the gasoline is fractionated into different kinds of gasoline according to different alkane values;
a storage oil tank: the gasoline storage tank is used for storing the qualified gasoline after rectification, mixing the qualified gasoline with external additives such as MTBE (methyl tert-butyl ether), xylene (mixed benzene) and the like, and converting the gasoline into finished oil;
a hydrogenation buffer tank: the cracking device is used for carrying out hydrotreating on unqualified gasoline for cracking, so that the unqualified gasoline is cracked into gasoline meeting the standard;
a hydrogenation device: for supplying a sufficient amount of pure hydrogen to the hydrogenation buffer tank;
a heat-conducting oil furnace: the system is used for heating the heat exchange oil inside by burning fuel and supplying heat to equipment needing to be heated in the system by the heat exchange oil;
and (3) tail gas treatment device: the method is used for recycling the waste gas generated in the gasoline production.
Preferably, the top of the gasoline prefractionator is provided with an air-cooled heat exchanger, the air-cooled heat exchanger is connected with a cooler through a pipeline, the bottom of the air pressure prefractionator is provided with a reboiler, the reboiler is connected with the heat-conducting oil furnace through a pipeline, and the bottom of the gasoline prefractionator is connected with a gasoline fractionating tower through a pipeline.
Preferably, the top of gasoline prefractionator, gasoline fractionating tower all are provided with the backward flow jar, the inside of backward flow jar is provided with the backwash pump, the backward flow jar is connected with gasoline prefractionator, gasoline fractionating tower through the pipeline, the top of backward flow jar is provided with the atmospheric pressure valve, the backward flow jar is connected with the gas buffer tank through atmospheric pressure valve and pipeline.
Preferably, the outside of gas buffer tank is provided with pressure sensor, the passing through pipeline of gas buffer tank is connected with the feed inlet of heat conduction oil stove.
Preferably, the top of gasoline fractionating tower is provided with the air cooling heat exchanger, and the air cooling heat exchanger passes through the pipeline and is connected with the cooler, the bottom of gasoline fractionating tower is provided with the reboiler, the reboiler passes through the pipeline and is connected with the heat conduction oil stove, the heat exchanger sets up the one side at the gasoline fractionating tower.
Preferably, the oil storage tank comprises an oil storage tank, a blending tank and a finished product tank, the oil storage tank, the blending tank and the finished product tank are sequentially connected through a pipeline, a plurality of groups of additive tanks are arranged on the outer side of the blending tank, and the plurality of groups of additive tanks are connected with the blending tank through pipelines.
Preferably, the hydrogenation buffer tank is connected with the gasoline fractionating tower through a pipeline, the hydrogenation buffer tank is connected with the hydrogenation device through a pipeline, a plurality of groups of catalyst plates are arranged inside the hydrogenation buffer tank, and a reboiler is arranged at the bottom end inside the hydrogenation buffer tank.
Preferably, the hydrogenation device comprises a mixing tower, a catalytic tower, a washing tower and a plurality of groups of pressure equalizing towers, and the raw materials for hydrogen production are methanol and desalted water.
Preferably, the tail gas treatment device is provided with a plurality of groups of collecting tanks, each group of collecting tanks is filled with different types of adsorbents, the collecting tanks are connected in series through pipelines, and the collecting tanks are connected with a discharge port of the heat-conducting oil furnace through pipelines.
Compared with the prior art, the invention has the beneficial effects that:
1. according to the invention, by arranging the heat-conducting oil furnace, the oil return tank and the heat exchanger, after high-temperature crude oil steam and the air-cooled heat exchanger exchange heat during production, cooling water in the air-cooled heat exchanger absorbs a large amount of heat and then enters the heat exchanger through a pipeline, a high-temperature cooling water pipe is close to a crude oil pipe which is about to enter a fractionating tower in the heat exchanger, so that the high-temperature cooling water pipe heats the crude oil, the initial temperature of the crude oil when entering the fractionating tower is improved, the heating time of a reboiler is reduced, and the utilization efficiency of the heat is improved;
2. through the gas buffer tank and the heat conduction oil furnace that set up, can burn the noncondensable gas that produces when producing petrol and the hydrogen of retrieving through the burning furnace that burns in the heat conduction oil furnace, heat the heat transfer oil in the oil furnace, the by-product of raw materials can make full use of, has improved the availability factor of crude oil, has reduced the consumption of fuel, has improved economic benefits.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1, a fractionation system for a gasoline project includes:
a raw material tank: for storing the petroleum raw material produced by the production, the petroleum raw material generally comprises: petroleum gas, gasoline, kerosene, diesel oil, heavy oil, and the like;
a heat exchanger: the system is used for preheating crude oil, gasoline and the like, heating the crude oil, the gasoline and the like to a certain temperature, and reducing the fuel consumption in the subsequent fractionation process;
a gasoline prefractionator: the method is used for carrying out rough fractionation on gasoline, heating the gasoline to evaporate substances with low boiling points in raw materials and feeding the evaporated substances into the top end of a prefractionator;
a cooler: the cooling device is used for cooling and radiating the high-temperature cooling liquid to restore the cooling liquid to normal temperature;
a reflux tank: the naphtha and the non-condensable gas are temporarily stored, and part of the naphtha is pumped back to the fractionating tower to provide a liquid phase;
naphtha oil tank: for storing naphtha;
a gas buffer tank: the device is used for storing non-condensable gas and inflammable gas such as hydrogen sulfide in the subsequent process;
a gasoline fractionating tower: the system is used for fractionating gasoline, and the gasoline is fractionated into different kinds of gasoline according to different alkane values;
a storage oil tank: the gasoline storage tank is used for storing the qualified gasoline after rectification, mixing the qualified gasoline with external additives such as MTBE (methyl tert-butyl ether), xylene (mixed benzene) and the like, and converting the gasoline into finished oil;
a hydrogenation buffer tank: the cracking device is used for carrying out hydrotreating on unqualified gasoline for cracking, so that the unqualified gasoline is cracked into gasoline meeting the standard;
a hydrogenation device: for supplying a sufficient amount of pure hydrogen to the hydrogenation buffer tank;
a heat-conducting oil furnace: the system is used for heating the heat exchange oil inside by burning fuel and supplying heat to equipment needing to be heated in the system by the heat exchange oil;
and (3) tail gas treatment device: the method is used for recycling the waste gas generated in the gasoline production.
Example 1
As a preferred embodiment of the present invention: the top end of the gasoline prefractionator is provided with an air-cooled heat exchanger, the air-cooled heat exchanger is connected with a cooler through a pipeline, the bottom end of the air pressure prefractionator is provided with a reboiler, the reboiler is connected with the heat-conducting oil furnace through a pipeline, and the bottom end of the gasoline prefractionator is connected with a gasoline fractionating tower through a pipeline;
crude oil is introduced into a gasoline prefractionator through a raw material tank, the crude oil is heated through a reboiler until the temperature of the bottom end of the gasoline prefractionator is kept at about one hundred twenty degrees, the temperature of the top of the tower is kept at about one hundred degrees, the crude oil is heated, most of substances with lower boiling points inside are evaporated to form a gas phase to rise, the gas phase passes through an air cooling heat exchanger after reaching the top end of the gasoline prefractionator and exchanges heat with cooling water in the air cooling heat exchanger, part of substances in the gas phase are cooled and liquefied into naphtha, and the naphtha enters a reflux tank along with the gas phase through a pipeline.
Example 2
As a preferred embodiment of the present invention: reflux tanks are arranged at the top ends of the gasoline prefractionator and the gasoline fractionating tower, reflux pumps are arranged in the reflux tanks, the reflux tanks are connected with the gasoline prefractionator and the gasoline fractionating tower through pipelines, the top ends of the reflux tanks are provided with air pressure valves, and the reflux tanks are connected with a gas buffer tank through the air pressure valves and the pipelines;
naphtha is continuous storage in the backward flow jar, noncondensable gas in the gaseous phase is also not many storage in the backward flow jar, noncondensable gas when in the backward flow jar is collected too big, the inside atmospheric pressure of backward flow jar increases to certain extent, push up the atmospheric pressure valve, make noncondensable gas enter into in the gas buffer tank through atmospheric pressure valve and pipeline, the convenience is collected noncondensable gas, the backwash pump that the bottom of backward flow jar set up, can return part naphtha to in the gasoline prefractionator through the backwash pump, provide the liquid phase for the fractionation process, increase the fractional distillation efficiency of crude oil.
Example 3
As a preferred embodiment of the present invention: a pressure sensor is arranged on the outer side of the gas buffer tank, and the gas buffer tank is connected with a feed inlet of the heat-conducting oil furnace through a pipeline;
can know the gas content in the gas buffer tank through pressure sensor, avoid the too big accident that causes of pressure, after pressure reached certain numerical value, let in the gas buffer tank to the fuel of heat conduction oil stove through the pipeline and add the mouth, act as the heat transfer oil of fuel in to the heat conduction oil stove temporarily and heat, abundant utilization the crude oil accessory substance, also reduced the consumption of fuel, improved economic benefits.
Example 4
As a preferred embodiment of the present invention: the top end of the gasoline fractionating tower is provided with an air-cooled heat exchanger, the air-cooled heat exchanger is connected with a cooler through a pipeline, the bottom end of the gasoline fractionating tower is provided with a reboiler, the reboiler is connected with the heat-conducting oil furnace through a pipeline, and the heat exchanger is arranged on one side of the gasoline fractionating tower;
the gasoline fractionating tower can rectify the bottom oil in the gasoline prefractionator to separate most impurities in the bottom oil from gasoline, the overall structure of the gasoline fractionating tower is similar to that of the gasoline prefractionator, but the outer side of the gasoline fractionating tower is provided with a heat exchanger which can regulate the temperature of the gasoline.
Example 5
As a preferred embodiment of the present invention: the oil storage tank consists of an oil storage tank, a blending tank and a finished product tank, the oil storage tank, the blending tank and the finished product tank are sequentially connected through a pipeline, a plurality of groups of additive tanks are arranged on the outer side of the blending tank, and the plurality of groups of additive tanks are connected with the blending tank through pipelines;
after the gasoline fractionation is finished, the gasoline is introduced into an oil storage tank, the gasoline is conveyed into a blending tank through a pipeline, an additive tank arranged on the outer side of the blending tank sequentially adds internal additives into the blending tank through a pipeline, and the gasoline and the additives are fully mixed in the blending tank to form finished product oil which is conveyed into a finished product tank.
Example 6
As a preferred embodiment of the present invention: the hydrogenation buffer tank is connected with the gasoline fractionating tower through a pipeline, the hydrogenation buffer tank is connected with the hydrogenation device through a pipeline, a plurality of groups of catalyst plates are arranged inside the hydrogenation buffer tank, and a heater is arranged at the bottom end inside the hydrogenation buffer tank;
unqualified gasoline fractionated in a gasoline fractionating tower is cracked with hydrogen and a catalyst under a high-temperature and high-pressure environment, so that high-molecular alkane is cracked into multiple groups of small-molecular alkane, and qualified gasoline is formed.
Example 7
As a preferred embodiment of the present invention: the hydrogenation device comprises a mixing tower, a catalytic tower, a washing tower and a plurality of groups of pressure equalizing towers, wherein the raw materials for hydrogen production are methanol and desalted water;
hydrogenation equipment provides sufficient pure hydrogen for the system, through vaporizing methanol and desalinized water after intensive mixing, under certain temperature through the catalyst, makes methanol and desalinized water take place chemical reaction, and the reaction formula is: CH3OH + H2O → CO2+3H2-49.5KJ/mol, then unreacted methanol in the methanol is absorbed by a washing tower, impurities in hydrogen are absorbed by a plurality of groups of pressure equalizing towers, and then the hydrogen is sent into a heating oil furnace to be combusted to heat the heat exchange oil.
Example 8
As a preferred embodiment of the present invention: the tail gas treatment device is provided with a plurality of groups of collecting tanks, different types of adsorbents are filled in each group of collecting tanks, the collecting tanks are connected in series through pipelines, and the collecting tanks are connected with a discharge port of the heat-conducting oil furnace through pipelines;
the waste gas that produces when making production petrol can absorb wherein harmful gas through aiming at the collecting vessel, reduces atmospheric pollution, and can be collected the gas that can retrieve in the waste gas through collecting vessel group, is convenient for retrieve.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Claims (9)
1. A fractionation system for a gasoline project, characterized by: the method comprises the following steps:
a raw material tank: for storing the petroleum raw material produced by the production, the petroleum raw material generally comprises: petroleum gas, gasoline, kerosene, diesel oil, heavy oil, and the like;
a heat exchanger: the system is used for preheating crude oil, gasoline and the like, heating the crude oil, the gasoline and the like to a certain temperature, and reducing the fuel consumption in the subsequent fractionation process;
a gasoline prefractionator: the method is used for carrying out rough fractionation on gasoline, heating the gasoline to evaporate substances with low boiling points in raw materials and feeding the evaporated substances into the top end of a prefractionator;
a cooler: the cooling device is used for cooling and radiating the high-temperature cooling liquid to restore the cooling liquid to normal temperature;
a reflux tank: the naphtha and the non-condensable gas are temporarily stored, and part of the naphtha is pumped back to the fractionating tower to provide a liquid phase;
naphtha oil tank: for storing naphtha;
a gas buffer tank: the device is used for storing non-condensable gas and inflammable gas such as hydrogen sulfide in the subsequent process;
a gasoline fractionating tower: the system is used for fractionating gasoline, and the gasoline is fractionated into different kinds of gasoline according to different alkane values;
a storage oil tank: the gasoline storage tank is used for storing the qualified gasoline after rectification, mixing the qualified gasoline with external additives such as MTBE (methyl tert-butyl ether), xylene (mixed benzene) and the like, and converting the gasoline into finished oil;
a hydrogenation buffer tank: the cracking device is used for carrying out hydrotreating on unqualified gasoline for cracking, so that the unqualified gasoline is cracked into gasoline meeting the standard;
a hydrogenation device: for supplying a sufficient amount of pure hydrogen to the hydrogenation buffer tank;
a heat-conducting oil furnace: the system is used for heating the heat exchange oil inside by burning fuel and supplying heat to equipment needing to be heated in the system by the heat exchange oil;
and (3) tail gas treatment device: the method is used for recycling the waste gas generated in the gasoline production.
2. A fractionation system for a gasoline project according to claim 1, wherein: the top of the gasoline prefractionator is provided with an air cooling heat exchanger, the air cooling heat exchanger is connected with a cooler through a pipeline, the bottom of the air pressure prefractionator is provided with a reboiler, the reboiler is connected with a heat-conducting oil furnace through a pipeline, and the bottom of the gasoline prefractionator is connected with a gasoline fractionating tower through a pipeline.
3. A fractionation system for a gasoline project according to claim 1, wherein: the top of petrol prefractionator, gasoline fractionating tower all is provided with the backward flow jar, the inside of backward flow jar is provided with the backwash pump, the backward flow jar is connected with petrol prefractionator, gasoline fractionating tower through the pipeline, the top of backward flow jar is provided with the atmospheric pressure valve, the backward flow jar passes through the atmospheric pressure valve and the pipeline is connected with the gas buffer tank.
4. A fractionation system for a gasoline project according to claim 1, wherein: a pressure sensor is arranged on the outer side of the gas buffer tank, and the gas buffer tank is connected with a feed inlet of the heat-conducting oil furnace through a pipeline;
5. a fractionation system for a gasoline project according to claim 1, wherein: the top of gasoline fractionating tower is provided with the air cooling heat exchanger, and the air cooling heat exchanger passes through the pipeline and is connected with the cooler, the bottom of gasoline fractionating tower is provided with the reboiler, the reboiler passes through the pipeline and is connected with the heat conduction oil furnace, the heat exchanger sets up the one side at the gasoline fractionating tower.
6. A fractionation system for a gasoline project according to claim 1, wherein: the oil storage tank comprises oil storage tank, blending tank and finished product jar, and oil storage tank, blending tank and finished product jar connect gradually through the pipeline, the outside of blending tank is provided with multiunit additive jar, multiunit the additive jar passes through the pipeline and is connected with the blending tank.
7. A fractionation system for a gasoline project according to claim 1, wherein: the hydrogenation buffer tank is connected with the gasoline fractionating tower through a pipeline, the hydrogenation buffer tank is connected with the hydrogenation device through a pipeline, a plurality of groups of catalyst plates are arranged inside the hydrogenation buffer tank, and a reboiler is arranged at the bottom end inside the hydrogenation buffer tank.
8. A fractionation system for a gasoline project according to claim 1, wherein: the hydrogenation device is internally composed of a mixing tower, a catalytic tower, a washing tower and a plurality of groups of pressure equalizing towers, and the raw materials for hydrogen production are methanol and desalted water.
9. A fractionation system for a gasoline project according to claim 1, wherein: the tail gas treatment device is provided with a plurality of groups of collecting tanks, each group of collecting tanks are filled with different types of adsorbents, the collecting tanks are connected in series through pipelines, and the collecting tanks are connected with a discharge port of the heat-conducting oil furnace through pipelines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911268786.4A CN111019686A (en) | 2019-12-11 | 2019-12-11 | A fractionation system for gasoline project |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911268786.4A CN111019686A (en) | 2019-12-11 | 2019-12-11 | A fractionation system for gasoline project |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111019686A true CN111019686A (en) | 2020-04-17 |
Family
ID=70206007
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911268786.4A Pending CN111019686A (en) | 2019-12-11 | 2019-12-11 | A fractionation system for gasoline project |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111019686A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112899014A (en) * | 2021-01-28 | 2021-06-04 | 洛阳瑞华新能源技术发展有限公司 | Method for indirectly heating hydrocarbon reaction material by using hot high-molecular gas of hydrogenation reaction product of expanded bed |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4436902A (en) * | 1982-02-12 | 1984-03-13 | Phillips Petroleum Company | Removal of contaminants in liquid purification |
| CN101265417A (en) * | 2008-04-30 | 2008-09-17 | 山东金诚重油化工有限公司 | Method for providing heat for petroleum fractioning hydrogenation |
| CN105062559A (en) * | 2015-08-10 | 2015-11-18 | 华南理工大学 | Novel process for reducing energy consumption of catalytic gasoline hydrogenation refining process |
-
2019
- 2019-12-11 CN CN201911268786.4A patent/CN111019686A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4436902A (en) * | 1982-02-12 | 1984-03-13 | Phillips Petroleum Company | Removal of contaminants in liquid purification |
| CN101265417A (en) * | 2008-04-30 | 2008-09-17 | 山东金诚重油化工有限公司 | Method for providing heat for petroleum fractioning hydrogenation |
| CN105062559A (en) * | 2015-08-10 | 2015-11-18 | 华南理工大学 | Novel process for reducing energy consumption of catalytic gasoline hydrogenation refining process |
Non-Patent Citations (3)
| Title |
|---|
| 朱赤仁: "《环境污染治理技术（第三版）》", 31 August 2008, 中国环境科学出版社 * |
| 沈建跃: "《大变革 甲醇能源时代》", 28 February 2018, 新华出版社 * |
| 王妍等: "兰州石化汽油在线管道调合的应用", 《甘肃科技》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112899014A (en) * | 2021-01-28 | 2021-06-04 | 洛阳瑞华新能源技术发展有限公司 | Method for indirectly heating hydrocarbon reaction material by using hot high-molecular gas of hydrogenation reaction product of expanded bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101218324B (en) | Method for processing hydrocarbon pyrolysis effluent | |
| CN106811234B (en) | A kind of delayed coking system and method | |
| CN101218320B (en) | Method for processing hydrocarbon pyrolysis effluent | |
| CN101381617B (en) | Fractionation method of hydrocarbon mixtures | |
| CN112266799A (en) | Delayed coking method for realizing energy consumption reduction of absorption stabilization system | |
| CN205740904U (en) | Petroleum naphtha hydrogenation refines low pressure deoxidation and the system of charging heat exchange optimization | |
| CN216536963U (en) | Separation system of sulfuric acid alkylation reaction product | |
| CN1861759A (en) | Catalyzing cracking slurry oil topping tech. and industry apparatus thereof | |
| CN111019686A (en) | A fractionation system for gasoline project | |
| US20100155296A1 (en) | Systems and methods of generating renewable diesel | |
| CN106062139B (en) | Method for heating in crude oil | |
| US9751072B2 (en) | Treatment of heavy crude oil and diluent | |
| RU2567534C1 (en) | Method and device for obtaining of high-octane gasoline by combined processing of hydrocarbon fractions and oxygen-containing organic raw material | |
| EP1577366A2 (en) | Process for conversion of waste material to liquid fuel | |
| CN216439988U (en) | Novel grading flash evaporation equipment | |
| CN103265973B (en) | Method and equipment for producing automotive diesel fuel from medium temperature coal tar light oil as raw material | |
| CN107267202B (en) | Method and device for stripping fractionation and negative pressure desorption of hydrogenated diesel refinery gas | |
| RU2546677C1 (en) | Method and installation of hydrocracking with obtaining motor fuels | |
| CN106520190A (en) | Light aromatic production method | |
| CN109181766A (en) | A kind of modified light aromatic hydrocarbons hydrogenation plant and its operating method | |
| CN113975839B (en) | Grading flash evaporation equipment and process | |
| CN206279156U (en) | A kind of biological heavy oil atmospheric cracking device | |
| CN111019687A (en) | Finished oil fractionation system | |
| CN114958419B (en) | Method for processing catalytic diesel oil | |
| CN214612311U (en) | Heavy oil combined fractionating device |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200417 |