CN85108736A - Process for petroleum fractionating under the methane atmosphere - Google Patents
Process for petroleum fractionating under the methane atmosphere Download PDFInfo
- Publication number
- CN85108736A CN85108736A CN198585108736A CN85108736A CN85108736A CN 85108736 A CN85108736 A CN 85108736A CN 198585108736 A CN198585108736 A CN 198585108736A CN 85108736 A CN85108736 A CN 85108736A CN 85108736 A CN85108736 A CN 85108736A
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- China
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- oil
- gas
- methane
- distillation tower
- condenser
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- 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)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The fractionating method of methane atmosphere PetroChina Company Limited. is characterized in that in the fractionation of oil, contains gas and sends into condenser from the cat head of distillation tower being contained in methane in the oil, make it condensation, with after the high methane gas separation, this high methane gas is boosted send in the distillation tower in this condenser, recirculation is used.
Description
The present invention relates to the improvement of process for petroleum fractionating.In detail, relate to the olefiant fractionation of life of fractionation, coal tar oil content sulphur, hydroeracking unit and the hydrogenation a refining unit that can be used for crude oil, the fractionation of liquefied coal coil, contain the fractionation of the multicomponent system of rare gas element, and tar sand oils, the fractionating method of shale wet goods.
Fig. 3 illustrates former crude distillation flow process sketch chart.
Among Fig. 3, behind the crude oil 101 and water vapor 102 mixing from circuit 1, in process furnace 3, be warmed up to 350～400 ℃, enter distillation tower 4 from circuit 2.The working pressure of distillation tower 4 is near normal pressure.To feed at the bottom of the tower of distillation tower 4 from the stripping steam 103 of circuit 5, crude oil is fractionated into volatile oil 104, kerosene 105, solar oil 106, heavy gas oil 107 and Residual oil 108.Usually the cat head by distillation tower 4 takes out volatile oil, goes out kerosene, solar oil, heavy gas oil by the tower side-draw, takes out Residual oil at the bottom of the tower of distillation tower 4.
Come out to enter condenser 6, cooling and condensate trap 7, be condensed into water from cat head by the water vapor 103 that feeds at the bottom of the tower of distillation tower 4.The cut that comes out from distillation tower 4 cats head carries out heat exchange (not illustrating among the figure) with water the air-flow of condenser 6 fronts.
If before above-mentioned water vapor condensation, with regard to condensation, corrode by overhead material near water vapor in the cat head of water vapor dew point, distillation tower 4 for the heat exchange temperature of the overhead fraction of distillation tower 4, and therefore, the operation of distillation tower 4 should make above-mentioned heat exchange temperature be higher than dew point.
Usually contain gases (to call high methane gas in the following text) such as methane, ethane in the crude oil, in condensate trap 7, separate, they are used as fuel as tail gas 110.
As mentioned above, if according to original fractionating method, its shortcoming is: for fear of the water vapor condensation of distillation tower cat head and cause corrosion, control the heat exchange temperature of cat head with the temperature that is higher than dew point, thereby can not fully reclaim heat.Must outside system, introduce water vapor when also having stripping simultaneously, and this water of condensation needs problems such as draining processing.
The present invention is the water vapor that stripping uses in the original crude still of representative, in condensate trap, separate behind the methane-rich gas contained in the crude oil in distillation tower compression cycle and use methane-rich gas, perhaps by supplying with methane-containing gas outside the system, under methane atmosphere, carrying out fractionation, the more effectively method of fractionation crude oil.Feature just of the present invention is in the fractionation of so-called oil, the gas that contains that is contained in the methane in the oil is sent into condenser from the distillation tower cat head, make it condensation, after methane-rich gas separated, methane-rich gas boosted send into distillation tower recirculation and use as the process for petroleum fractionating under the methane atmosphere of feature.
In the method for the present invention, can be in above-mentioned circulation methane-rich gas the external gas that contains a small amount of methane of feeding system, also can not only infeed at distillation tower 4 but also in the air-flow of process furnace 3 fronts, its effect is identical.Distillation tower is that 0-100kg/cm G, temperature are to operate under the 100-500 ℃ of situation at pressure generally.
Following embodiment with reference to diagram illustrates in greater detail the present invention.
Fig. 1 is that schema, the Fig. 2 of the embodiment when the present invention is used for crude distillation is other embodiments of the invention schemas, and Fig. 3 is the crude distillation schema with original method, the ASTM curve of distilled oil that Fig. 4 is the embodiment of the invention.
Among Fig. 1, crude oil 101 and the gas that contains a small amount of methane that feeds by circuit 28 and in condensate trap 7, separate and the mixture of the methane-rich gas 113 that boosts in compressor 8 is sent in the process furnace together, in this stove, be warming up to 350～400 ℃, send in the distillation tower.The working pressure of distillation tower 4 is near normal pressure.
Feed from distillation tower 4 bottoms and to be used for steam stripped high methane gas 112, crude oil is fractionated into lightweight volatile oil 115, and heavy volatile oil 114, kerosene 105, light bavin is by 106, heavy gas oil 107 and Residual oil 108.
Distillate the overhead fraction 118 that contains methane and lightweight volatile oil from the cat head of distillation tower 4, (not illustrating among the figure) entered condenser 6 after this overhead fraction and water carried out heat exchange, was condensate in and was separated into methane-rich gas 111 and lightweight volatile oil 115 in the condensate trap 7.
Isolating high methane gas 111 boosts in compressor 8, and a part of high methane gas 112 is sent at the bottom of the tower of distillation tower 4, and a part of high methane gas 113 is sent into the air-flow of process furnace 3 fronts, makes it recirculation.Rest part is discharged outside the system as fuel as tail gas.Reclaim heavy volatile oil 114, kerosene 115, solar oil 106, heavy jackal oil 107 from the tower side of distillation tower 4, at the bottom of tower, take out Residual oil.
As mentioned above, because high methane gas is used for stripping, distillation tower moves under methane atmosphere, therefore, the dew point step-down of the cat head fraction of distillation tower, thereby do not have etching problem, and can reduce the heat exchange temperature in the distillation tower cat head and move.
Fig. 2 illustrates and uses the embodiment of Arabian crude as crude oil.
Crude oil is sent into distillation tower 4 by former oil-piping layout 11 through process furnace 3.On the other hand, by passing through high methane gas conduit 9,10, every 1m at the bottom of the tower of former oil-piping layout 11 and distillation tower 4
3Crude oil feeds 24Nm
3High methane gas (in the air-flow of process furnace front is 10%, is 90% in the distillation tower) is with the crude oil fractionation.The temperature out of process furnace 3 is that 346 ℃, the operating pressure of distillation tower 4 are 0.8kg/cm
2G.
It is 42 sections that table 1 illustrates this distillation tower 4(hop count) composition that comes out of fractionation.
Table 1
The temperature that the product product steams from distillation tower (℃) (yield volume %)
Volatile oil 60 21.7
Kerosene 187 19.3
Solar oil 259 15.7
Heavy gas oil 312 4.7
Residual oil 352 38.6
With the ASTM curve this separate stage is shown in Fig. 4.Find out by this embodiment result, the water vapor dew point of cat head fraction becomes 50 ℃ with respect to 95 ℃ of former method, if it is 100 that condenser duty is established former method, then present method is 56, can significantly reduce the load of condenser, that is to say, in crude distillation, do not inject water vapor and finish fractionation, the load of condenser is original 56%, and can suppress the corrosion of overhead material, thereby can adopt common carbon steel.
Then can obtain following effect according to the present invention:
(1) because fractionation in methane atmosphere then can prevent the destilling tower tower top corrosion, and the tower top temperature operation can be reduced, thereby recuperation of heat can be improved.
(2) water vapour that passes at the bottom of the distillation Tata in the former method is in the cat head condensation, and the load of condenser is big; And the present invention's method as long as the heat of removing the high methane gas cut just can, can significantly reduce condenser duty.
(3) do not need outside system, to feed the water vapor that stripping is used, and can also reduce the draining processing of water of condensation.
(4) high methane gas that will feed from distillation tower bottom circulates with compressor compresses, thus have can the optional recycle amount advantage.
When (5) the present invention's method being used for crude distillation, at cat head high methane gas is separated, compresses, it is fed at the bottom of the tower of distillation tower, thereby can select the internal circulating load of high methane gas arbitrarily, can be in a distillation tower fractionation heavy volatile oil, kerosene, solar oil, heavy gas oil and Residual oil, and can in condensate trap, reclaim lightweight volatile oil.
Claims (4)
1, at the fractionating method of methane atmosphere PetroChina Company Limited., it is characterized in that, in the crude oil fractionation, contain gas and send into condenser being contained in methane in the oil, make it condensation, after in this condenser, high methane gas being separated from the distillation cat head, this high methane gas is boosted send in the distillation tower, recirculation is used.
2, the method according to claim 1 is characterized in that, can feed in right amount in addition from the gas that contains an amount of methane outside the system in above-mentioned circulation high methane gas.
3, the method according to claim 1 is characterized in that, the outer feeding of said system is to carry out in the air-flow of distillation tower or process furnace front.
4, the method according to claim 1, it is characterized in that, above-mentioned oil is generation oil, the liquefied coal coil from crude oil, coal tar, hydroeracking unit and hydrogenation a refining unit, contains choose in the multicomponent system gas, tar sand oils, summer rock oil of rare gas element at least a.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP255265/84 | 1984-12-03 | ||
| JP25526584A JPS61133289A (en) | 1984-12-03 | 1984-12-03 | Fractionation of oil under methane atmosphere |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85108736A true CN85108736A (en) | 1986-08-13 |
| CN85108736B CN85108736B (en) | 1988-12-07 |
Family
ID=17276345
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85108736A Expired CN85108736B (en) | 1984-12-03 | 1985-12-02 | Process for petroleum fractionating under methane atmosphere |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP0186617B1 (en) |
| JP (1) | JPS61133289A (en) |
| CN (1) | CN85108736B (en) |
| DE (1) | DE3562271D1 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0699694B2 (en) * | 1985-11-20 | 1994-12-07 | 三菱重工業株式会社 | Crude oil distillation method |
| US7172686B1 (en) | 2002-11-14 | 2007-02-06 | The Board Of Regents Of The University Of Oklahoma | Method of increasing distillates yield in crude oil distillation |
| RU2556006C1 (en) * | 2014-01-10 | 2015-07-10 | Федеральное государственное бюджетное образовательное учреждение высшего профессионального образования "Астраханский государственный технический университет" | Gas mixture separation method |
| US10421917B2 (en) * | 2017-11-22 | 2019-09-24 | Meg Energy Corp. | Steamless hydrocarbon processing (upgrading) facility with multiple and integrated uses of non-condensable gas for hydrocarbon processing |
| CN109628133B (en) * | 2018-12-12 | 2021-04-27 | 中石化炼化工程（集团）股份有限公司 | Atmospheric distillation method for reducing corrosion of common-roof cooling system |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3996129A (en) * | 1975-05-12 | 1976-12-07 | Universal Oil Products Company | Reaction product effluent separation process |
| SU724558A1 (en) * | 1978-06-27 | 1980-03-30 | Харьковский Ордена Ленина Политехнический Институт Им. В.И.Ленина | Method of oil raw material processing |
-
1984
- 1984-12-03 JP JP25526584A patent/JPS61133289A/en active Granted
-
1985
- 1985-12-02 EP EP19850730158 patent/EP0186617B1/en not_active Expired
- 1985-12-02 CN CN85108736A patent/CN85108736B/en not_active Expired
- 1985-12-02 DE DE8585730158T patent/DE3562271D1/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| DE3562271D1 (en) | 1988-05-26 |
| EP0186617B1 (en) | 1988-04-20 |
| CN85108736B (en) | 1988-12-07 |
| EP0186617A1 (en) | 1986-07-02 |
| JPS61133289A (en) | 1986-06-20 |
| JPH0542476B2 (en) | 1993-06-28 |
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