CN1004005B - The method and apparatus of cracking naphtha and heavy hydrocarbon simultaneously - Google Patents
The method and apparatus of cracking naphtha and heavy hydrocarbon simultaneously Download PDFInfo
- Publication number
- CN1004005B CN1004005B CN85105709.8A CN85105709A CN1004005B CN 1004005 B CN1004005 B CN 1004005B CN 85105709 A CN85105709 A CN 85105709A CN 1004005 B CN1004005 B CN 1004005B
- Authority
- CN
- China
- Prior art keywords
- oil
- gas
- splitting gas
- quenching
- tower
- 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.)
- Expired
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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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/002—Cooling of cracked gases
-
- 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
- C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
- C10G51/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (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
Present method is for cracking naphtha and a kind of final boiling point are at least the heavy hydrocarbon of 500 ℃ simultaneously.Splitting gas is by a kind of oil quenching, and mix after chilling, from formed splitting gas mixture, separate a liquid distillate and as the quenching oil of heavy hydrocarbon splitting gas, after separating heavy liquid cut, remaining mixed pyrolysis gas first carries out primary fractionation, and the tower bottom distillate separating is as the quenching oil of naphtha splitting gas.
Description
The present invention relates to a kind of a kind of method that while cracking naphtha and its final boiling point are at least the heavy hydrocarbon of 500 ℃, a kind of oil quenching of its splitting gas.
In recent years, require in a cracking apparatus both cracking naphtha also the situation of cracking heavy hydrocarbon had increase.So-called heavy hydrocarbon, thinks that its final boiling point at least should be 500 ℃.The splitting gas of discharging from pyrolyzer, is first undertaken coolingly by a splitting gas water cooler, then make it chilling with a kind of quenching oil again.
When cracking naphtha and other light material, splitting gas is passed to light oil tower and is carried out primary fractionation.The tower bottom distillate of light oil tower has at least a part to be used to chilling naphtha splitting gas and other light material splitting gases of chilling where necessary.Quenching oil boiling spread is generally 180～350 ℃.
Simultaneously the difficulty of cracking naphtha and heavy hydrocarbon is, the quenching oil taking out from light oil tower can not be used for chilling mink cell focus.The splitting gas of heavy hydrocarbon also has about 500～600 ℃ of temperature after splitting gas water cooler is cooling.The in the situation that of chilling, its temperature also needs to drop to about 200～250 ℃.Using while carrying out chilling from the lightweight oil of naphtha splitting gas, cause strong coking at chilling point.The splitting gas of heavy hydrocarbon is used to high boiling quenching oil, can avoid this situation.In view of this reason, in all occasions of wanting while cracking naphtha and heavy hydrocarbon, heavy hydrocarbon splitting gas can be passed to a heavy oil tower being separated, the tower bottom distillate of this heavy oil tower can be used as quenching oil for heavy hydrocarbon.The boiling spread of this heavy quenching oil is for example 200～500 ℃.
But, increase a heavy oil tower for producing a kind of desired quenching oil with higher scope, will mean the obvious increase of cost of equipment, especially when just once in a while when treatment of heavy hydrocarbon, very uneconomical.
Therefore, task of the present invention is exactly a kind of economically viable method that starts said that cracking naphtha simultaneously and heavy hydrocarbon of invention.
This task is solved like this by the present invention, after chilling, splitting gas is mixed, and isolates a kind of heavy liquid fraction from mixed splitting gas, the quenching oil by this heavy liquid fraction as heavy hydrocarbon splitting gas; Mixed pyrolysis gas remaining after separation of heavy liquid distillate is carried out to primary fractionation, therefrom extracts fraction at the bottom of tower out, and with it carry out chilling naphtha splitting gas.
By this method of the present invention, be separated prior to primary fractionation for the quenching oil of heavy hydrocarbon splitting gas.The remaining mixed pyrolysis gas getting off, only has lower final boiling point now, is conveyed to and carries out primary fractionation.When primary fractionation, can obtain a kind of lightweight oil as tower bottom distillate corresponding to its component, this lightweight oil is used to chilling naphtha splitting gas.
By method of the present invention, can carry out two kinds of splitting gases of chilling with a kind of quenching oil of boiling spread the best, so also avoid the coking phenomenon of chilling point, and in the time of splitting gas primary fractionation, only needed a light oil tower, and do not needed heavy oil tower.
By a preferred implementation method of the present invention be: the heavy liquid fraction of separating from mixed pyrolysis gas, its boiling spread is 200～400 ℃.
By another preferred implementation method of the present invention be: gas oil or the vacuum gas oil through hydrotreatment can be used as heavy hydrocarbon and use.
By the another preferred method of the present invention, the heavy liquid fraction of separating to be filtered, it is suitable that this way is also proved to be.Filtration can be played removing and sometimes remain in the effect of the coke granule in heavy oil.
For implementing the equipment of the inventive method; at least comprise two pyrolyzer; pyrolyzer has carries the charging line of the heavy hydrocarbon that needs cracking and the pipeline of discharge splitting gas; and be equipped with quenching oil input tube with respect to each splitting gas pipeline; it is characterized in that: after the too urgent cold spot of splitting gas device for cleaning pipeline, be connected together; and pass into light oil tower from its tie point, and a tripping device is housed between tie point and light oil tower, the bottom of tripping device is connected with quenching oil input tube; The bottom of light oil tower is connected with another quenching oil input tube.
An embodiment by equipment of the present invention: tripping device is made up of a sunk part on pipeline.
Sunk part is on the pipeline between junction and the light oil tower of two kinds of splitting gas pipelines.
The present invention and further details, will be described in detail by illustrated embodiment:
Fig. 1 is by the schema of an embodiment of the method for the invention.
Fig. 2 is by the schema of another embodiment of the method for the invention.
Method shown in Fig. 1, is used for cracking naphtha simultaneously and as if through the heavy hydrocarbon of the decompression oil of hydrotreatment, naphtha is inputted by pipeline 1, and heavy hydrocarbon is inputted by pipeline 2.The vacuum gas oil of naphtha and process hydrotreatment, cracking simultaneously in two pyrolyzer 3,4.Splitting gas is discharged from pyrolyzer 3,4 by pipeline 5,6.
For example, they can have following composition.
Naphtha splitting gas is through hydrotreatment
The vacuum gas oil of (full boiling range naphtha)
15 ℃ 0.720 0.863 of density
ASTM distillation test method ℃ 54～175 340～530
Aromatic series total amount % by weight 10 19.4
H
2″ 0.8 0.6
CH
4″ 13.8 10.8
C
2H
4″ 31.5 30.8
C
3H
6″ 13.3 12.9
C
4H
6″ 4.5 6.4
Pyrolysis gasoline " 23.5 20.6
Pyrolysis oil " 4.5 9.0
Splitting gas is for example cooled in splitting gas water cooler 7,8: 370～450 ℃ or 450～650 ℃.
Splitting gas is discharged from after splitting gas water cooler 7,8, at chilling point 9,10 by quenching oil chilling.Then two kinds of splitting gases are mixed mutually.Gained mixed pyrolysis gas enters light oil tower 12 through pipeline 11, and mixed pyrolysis gas carries out primary fractionation in light oil tower, and tripping device 13 is contained on pipeline 11, and tripping device can be made up of a cylindric or peviform groove that is positioned at pipeline 11 bottoms.From the heavy liquid fraction of mixed pyrolysis gas, accumulate in tripping device 13, its boiling range is generally as follows:
+205℃ 240℃ 300℃ 350℃ ＞380℃
Pyrolysis gasoline joins in light oil tower by pipeline 17, boiling spread is the bottom that the light oil fraction of 180～350 ℃ accumulates in light oil tower, and all the other components of the mixed pyrolysis gas of input, through piping 18, discharge from the top of light oil tower, the component of discharge for example also can be washed.
From the light oil of light oil tower bottom, discharge by pipeline 19, remove solid particulate through filter 21, again send its part back to light oil tower 12(pipeline 22 by pump 20), and its other part is transported to the chilling point 9 on naphtha splitting gas pipeline by pipeline 23.
Method shown in Fig. 2 is different from the part of method shown in Fig. 1, except cracking naphtha and gas oil, also adds the third material, and ethane carries out cracking.Ethane is inputted pyrolyzer 28 by pipeline 27, and the splitting gas of being discharged through pipeline 29 by pyrolyzer 28 for example, can have following composition:
H
23.23 % by weight
CO/CO
20.07 ″
CH
42.99 ″
C
2H
20.42 ″
C
2H
446.45 ″
C
2H
643.64 ″
C
3+3.2 ″
Splitting gas carries out chilling after splitting gas water cooler 30 is chilled to 350～400 ℃ again, and quenching oil used is sent to chilling point 32 via pipeline 31.Quenching oil in pipeline 31 is to divide and get the light oil in the pipeline 23 from light oil tower 12.The ethane cracking gas of chilling mixes with naphtha splitting gas by pipeline 33, and then mixes with gas oil cracking gas together.The splitting gas mixture producing after being mixed by these three kinds of splitting gases, for example, can have following composition:
H
21.01 % by weight
CO/CO
20.08 ″
CH
413.36 ″
C
2H
20.42 ″
C
2H
428.98 ″
C
2H
67.58 ″
C
313.74 ″
C
47.66 ″
Benzene-toluene-dimethylbenzene 13.22 "
C
5+13.95 ″
Claims (6)
1, while cracking naphtha and a kind of its final boiling point are at least the method for the heavy hydrocarbon of 500 ℃; while using this method; splitting gas is by a kind of oil quenching; it is characterized in that: after splitting gas chilling, mix; from formed mixed pyrolysis gas, isolate a kind of heavy liquid fraction, this fraction can be used as the quenching oil of heavy hydrocarbon splitting gas; Mixed pyrolysis gas remaining after separation of heavy liquid fraction is made to primary fractionation, therefrom extract fraction at the bottom of a kind of tower out, at the bottom of this tower, fraction can be used as the quenching oil of naphtha splitting gas.
2, by the method for claim 1, it is characterized in that: described heavy hydrocarbon is gas oil or a kind of vacuum gas oil through hydrotreatment.
3, by the method for claim 1 or 2, it is characterized in that: from mixed pyrolysis gas, isolate a kind of boiling spread and be the heavy liquid fraction of 200～400 ℃.
4, by the method for one of claims 1 to 3, it is characterized in that: the heavy liquid fraction being separated will pass through filtration treatment.
5, by the method device used of claim 1, comprise two pyrolyzer, pyrolyzer has carries the feed pipe of heavy hydrocarbon and the outlet conduit of splitting gas that need cracking, each splitting gas pipeline all has a quenching oil input tube, it is characterized in that: splitting gas pipeline (5, 6) through over-quenching point (9, 10) after, link together, and pass into light oil tower (12) from its tie point, between tie point and light oil tower, there is a tripping device (13), the bottom of tripping device is connected with quenching oil input tube (16), the bottom of light oil tower (12) is connected with another root quenching oil input tube (23).
6, by the equipment of claim 5, it is characterized in that: tripping device (13) is made up of a sunk part on pipeline (11).
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19843433863 DE3433863A1 (en) | 1984-09-14 | 1984-09-14 | Process and equipment for simultaneously cracking naphtha and a heavy hydrocarbon feedstock |
| CN85105709.8A CN1004005B (en) | 1984-09-14 | 1985-07-27 | The method and apparatus of cracking naphtha and heavy hydrocarbon simultaneously |
| NL8502501A NL8502501A (en) | 1984-09-14 | 1985-09-12 | METHOD AND APPARATUS FOR SIMULTANEOUS CRACKING OF NAFTA AND A HEAVY HYDROCARBON FRACTION |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19843433863 DE3433863A1 (en) | 1984-09-14 | 1984-09-14 | Process and equipment for simultaneously cracking naphtha and a heavy hydrocarbon feedstock |
| CN85105709.8A CN1004005B (en) | 1984-09-14 | 1985-07-27 | The method and apparatus of cracking naphtha and heavy hydrocarbon simultaneously |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85105709A CN85105709A (en) | 1987-01-28 |
| CN1004005B true CN1004005B (en) | 1989-04-26 |
Family
ID=76224746
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85105709.8A Expired CN1004005B (en) | 1984-09-14 | 1985-07-27 | The method and apparatus of cracking naphtha and heavy hydrocarbon simultaneously |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN1004005B (en) |
| DE (1) | DE3433863A1 (en) |
| NL (1) | NL8502501A (en) |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3414705A1 (en) * | 1984-04-18 | 1985-10-31 | Linde Ag, 6200 Wiesbaden | Process for thermally cracking hydrocarbons |
-
1984
- 1984-09-14 DE DE19843433863 patent/DE3433863A1/en active Granted
-
1985
- 1985-07-27 CN CN85105709.8A patent/CN1004005B/en not_active Expired
- 1985-09-12 NL NL8502501A patent/NL8502501A/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| DE3433863C2 (en) | 1992-10-01 |
| DE3433863A1 (en) | 1986-03-27 |
| NL8502501A (en) | 1986-04-01 |
| CN85105709A (en) | 1987-01-28 |
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