CN106281444A - A kind of operational approach producing more than 92% n-alkane product - Google Patents
A kind of operational approach producing more than 92% n-alkane product Download PDFInfo
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- CN106281444A CN106281444A CN201610721609.7A CN201610721609A CN106281444A CN 106281444 A CN106281444 A CN 106281444A CN 201610721609 A CN201610721609 A CN 201610721609A CN 106281444 A CN106281444 A CN 106281444A
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Classifications
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
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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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of operational approach producing more than 92% n-alkane product, it utilizes the advantage that normal paraffin content in Fischer-Tropsch synthesis oil is higher, produce the n-alkane stable light hydrocarbon more than 92% and liquid paraffin product, can use as the solvent naphtha of high-quality or be used as to produce linear alkylbenzene (LAB), chlorocosane, the industrial chemicals of petroleum albumen.Present invention process hydrofinishing charging is cut off heavy wax charging, the charge proportion of heavy distillate and light ends oil need not be adjusted, high n-alkane product can be produced.Deliver to intermediate tank farm outside fractionating system just vacuum fractionation tail oil, stop cracking reaction system.In F-T synthesis oil product, normal paraffin content is high, after hydrofinishing, can produce the normal paraffin content stable light hydrocarbon more than 92% and liquid paraffin product.
Description
Technical field
The invention belongs to alkane synthesis field, especially design one Inner Mongol coal liquifaction company of gouy Thailand F-T synthesis device
The light ends oil of output, heavy distillate do raw material, produce the n-alkane stable light hydrocarbon more than 92% and liquid paraffin produces
Product.
Background technology
The n-alkane product produced in currently available technology is more rough, and the content of n-alkane does not reaches wanting of client
Asking, only as thick production marketing, added value is low.In F-T synthesis oil product, normal paraffin content is high, after hydrofinishing,
The stable light hydrocarbon containing n-alkane and liquid paraffin product can be produced.And after the hydrogenated cracking of fractional distillation tail oil, produce a large amount of
Isohydrocarbon, the product produced after refined products mixes with crackate does not has advantage, and the market price is low, is equivalent to two
The Product mix of individual extreme high-quality together, becomes and does not has pluses and minuses product, is thus unfavorable for finding market, it is impossible to by public affairs
The benefit of department.
Summary of the invention
In order to solve drawbacks described above present in prior art, the present invention utilizes in Fischer-Tropsch synthesis oil normal paraffin content relatively
High advantage, produces the n-alkane stable light hydrocarbon more than 90% and liquid paraffin product, can be as the solvent of high-quality
Oil uses or is used as to produce linear alkylbenzene (LAB), chlorocosane, the industrial chemicals of petroleum albumen, increases the economic benefit of company.
The present invention specifically provides following technical scheme:
A kind of operational approach producing more than 92% n-alkane product, it is characterised in that comprise the technical steps that:
Light ends oil and heavy distillate, mix respectively after feed pump boosts to 8.0MPa, then mixes with from recycle hydrogen
After conjunction, enter hydrofining reactor, under catalyst action, carry out hydrofining reaction；
After generation product mixes with heavy wax, the most heated stove enters hydrofining reactor after being heated to 240 DEG C,
Carry out hydrofining reaction under catalyst action, by saturated for alkene in raw oil, and deviate from the nitrogen in raw oil, sulfur, oxygen and gold
Belong to impurity；
Refining reaction product enters refining reaction product high pressure hot separator and carries out oil, gas two-phase laminated flow；Liquid is through decompression
After, enter thermal low-pressure separators；
Gas, after refining reaction product air cooler cools down, enters refining reaction product cold high pressure separator, divides at high pressure
Carrying out the two-phase laminated flow of gas phase and oil water mixture in device, liquid phase product enters cold low separator, hydrogen after decompression
Enter cracker as recycle hydrogen to recycle；
Fractionating system tail oil enters cracking reaction charging heating furnace heating as cracked stock after pump is forced into 7.0MPa
To 330 DEG C, enter hydrocracking reactor and carry out hydrocracking reaction；
It is hydrocracked product entrance cracked reaction product high pressure hot separator and carries out oil, gas two-phase laminated flow；Liquid is through subtracting
After pressure, enter thermal low-pressure separators D-7109；After the cooling of gas cracked product air cooler, enter cracked reaction product cold
High-pressure separator, carries out the separation of profit, gas in high-pressure separator；Its gas phase recycles as recycle hydrogen, isolated
In sewage send factory, sewage-treatment plant processes；
Being gone out device by the isolated gas phase of thermal low-pressure separators goes Hydrogen Unit, liquid phase to mix with cold low point of oil, enter and divide
Evaporate system.
The operational approach of above-mentioned production more than 92% n-alkane product still further comprises following steps:
After low mitogenetic one-tenth oil entrance fractional distillation charging heating furnace is heated to 310 DEG C, enter product fractionating column, top gaseous phase warp point
After evaporating the condensation of tower top air cooler, cooling, entering fractional distillation return tank of top of the tower, gas phase goes out battery limit (BL) and goes to oil-washing apparatus production LPG, liquid phase
Being fractionated into overhead reflux pumped, a part is as fractional distillation overhead reflux, and another part is as Petroleum carrying device；Fractionating column
If a side line, its distillation enters diesel oil stripping tower, output Paraffin liquid heavy；
Fractionating column base oil enters vacuum tower and carries out decompression separation, and tower top oil gas after cooling, enters Top of Vacuum Tower water distributing can
Carrying out gas-liquid separation, gas phase enters air through vacuum pump, and liquid phase is sent outside as liquid paraffin；In extraction side, vacuum tower top
Line, extraction section goes out device as Paraffin liquid heavy product；
After the pressurization of the cracked reaction feed pump of tail oil at the bottom of tower, enter cracking reaction system.
The present invention has the advantage that relative to prior art
1) heavy wax charging is cut off in hydrofinishing charging, the charge ratio of heavy distillate and light ends oil need not be adjusted
Example, can produce high n-alkane product.Deliver to intermediate tank farm outside fractionating system just vacuum fractionation tail oil, stop cracking reaction system
System.
2) in F-T synthesis oil product, normal paraffin content is high, after hydrofinishing, can produce n-alkane and contain
Stable light hydrocarbon and the liquid paraffin product that amount is more than 92%.
Accompanying drawing explanation
Fig. 1 is present invention process schematic flow sheet
Detailed description of the invention:
Below in conjunction with the accompanying drawings the application is expanded on further, it should be noted that this elaboration is merely to better illustrate
Inventive technique scheme, is not to limit technical scheme.
Reactive moieties technological process
Light ends oil and heavy distillate, mix respectively after feed pump boosts to 8.0MPa, then mixes with from recycle hydrogen
After conjunction, enter hydrofining reactor, under catalyst action, carry out hydrofining reaction.Generate product to mix with heavy wax
After conjunction, the most heated stove enters hydrofining reactor after being heated to 240 DEG C, carries out hydrofinishing anti-under catalyst action
Should, by saturated for alkene in raw oil, and deviate from the nitrogen in raw oil, sulfur, oxygen and metal impurities.Refining reaction product enters refined
Product high pressure hot separator carries out oil, gas two-phase laminated flow.Liquid, after decompression, enters thermal low-pressure separators.Gas is through essence
Product air cooler processed cooling after, enter refining reaction product cold high pressure separator, carry out in high-pressure separator gas phase and
The two-phase laminated flow of oil water mixture, liquid phase product enters cold low separator after decompression, and hydrogen enters as recycle hydrogen and splits
Change reactor cycles to use.
Fractionating system tail oil enters cracking reaction charging heating furnace heating as cracked stock after pump is forced into 7.0MPa
To 330 DEG C, enter hydrocracking reactor and carry out hydrocracking reaction.It is hydrocracked product and enters cracked reaction product heat height
Pressure separator carries out oil, gas two-phase laminated flow.Liquid, after decompression, enters thermal low-pressure separators D-7109.The cracked reaction of gas
Product air cooler cooling after, enter cracked reaction product cold high pressure separator, carry out in high-pressure separator profit, gas point
From.Its gas phase recycles as recycle hydrogen, and in isolated sewage send factory, sewage-treatment plant processes.
Being gone out device by the isolated gas phase of thermal low-pressure separators goes Hydrogen Unit, liquid phase to mix with cold low point of oil, enter and divide
Evaporate system.
Fractionating section technological process
After low mitogenetic one-tenth oil entrance fractional distillation charging heating furnace is heated to 310 DEG C, enter product fractionating column, top gaseous phase warp point
After evaporating the condensation of tower top air cooler, cooling, entering fractional distillation return tank of top of the tower, gas phase goes out battery limit (BL) and goes to oil-washing apparatus production LPG, liquid phase
Being fractionated into overhead reflux pumped, a part is as fractional distillation overhead reflux, and another part is as Petroleum carrying device.Fractionating column
If a side line, its distillation enters diesel oil stripping tower, output Paraffin liquid heavy.
Fractionating column base oil enters vacuum tower and carries out decompression separation, and tower top oil gas after cooling, enters Top of Vacuum Tower water distributing can
Carrying out gas-liquid separation, gas phase enters air through vacuum pump, and liquid phase is sent outside as liquid paraffin.In extraction side, vacuum tower top
Line, extraction section goes out device as Paraffin liquid heavy product.
After the pressurization of the cracked reaction feed pump of tail oil at the bottom of tower, enter cracking reaction system
Relate to term to illustrate:
Light ends oil: with synthesis gas as raw material, under fischer-tropsch synthetic catalyst and suitable reaction condition, the one of synthesis
Planting based on linear paraffin, alkene, without a kind of thick product of coal base of the impurity such as sulfur, nitrogen, charcoal number is distributed as C3～C29, under room temperature it is
Liquid.
Heavy distillate: with synthesis gas as raw material, under fischer-tropsch synthetic catalyst and suitable reaction condition, the one of synthesis
Planting based on linear paraffin, alkene, without a kind of thick product of coal base of the impurity such as sulfur, nitrogen, charcoal number is distributed as C8～C56, under room temperature it is
Solid.
N-alkane: do not have the saturated hydrocarbons of carbon side chain.
Stable light hydrocarbon: carbon number distribution is the saturated hydrocarbons of C5～C9.
Claims (2)
1. the operational approach producing more than 92% n-alkane product, it is characterised in that comprise the technical steps that:
Light ends oil and heavy distillate, respectively after feed pump boosts to 8.0MPa mix, then with mix from recycle hydrogen after,
Enter hydrofining reactor, under catalyst action, carry out hydrofining reaction；
After generation product mixes with heavy wax, the most heated stove enters hydrofining reactor after being heated to 240 DEG C, in catalysis
Carrying out hydrofining reaction under agent effect, by saturated for alkene in raw oil, and it is miscellaneous to deviate from the nitrogen in raw oil, sulfur, oxygen and metal
Matter；
Refining reaction product enters refining reaction product high pressure hot separator and carries out oil, gas two-phase laminated flow；Liquid, after decompression, enters
Enter thermal low-pressure separators；
Gas, after refining reaction product air cooler cools down, enters refining reaction product cold high pressure separator, at high-pressure separator
In carry out the two-phase laminated flow of gas phase and oil water mixture, liquid phase product enters cold low separator, hydrogen conduct after decompression
Recycle hydrogen enters cracker and recycles；
Fractionating system tail oil enters cracking reaction charging heating furnace after pump is forced into 7.0MPa as cracked stock and is heated to 330
DEG C, enter hydrocracking reactor and carry out hydrocracking reaction；
It is hydrocracked product entrance cracked reaction product high pressure hot separator and carries out oil, gas two-phase laminated flow；Liquid through decompression after,
Enter thermal low-pressure separators D-7109；After the cooling of gas cracked product air cooler, enter cracked reaction product cold anticyclone
Separator, carries out the separation of profit, gas in high-pressure separator；Its gas phase recycles as recycle hydrogen, isolated sewage
In sending factory, sewage-treatment plant processes；
Being gone out device by the isolated gas phase of thermal low-pressure separators goes Hydrogen Unit, liquid phase to mix with cold low point of oil, enter fractionation train
System.
2. the operational approach producing more than 92% n-alkane product as claimed in claim 1, it is characterised in that the most further
Comprise the steps:
After low mitogenetic one-tenth oil entrance fractional distillation charging heating furnace is heated to 310 DEG C, entering product fractionating column, top gaseous phase is fractionated into tower
After the condensation of head space cooler, cooling, entering fractional distillation return tank of top of the tower, gas phase goes out battery limit (BL) and goes to oil-washing apparatus production LPG, liquid phase warp point
Evaporating overhead reflux pumped, a part is as fractional distillation overhead reflux, and another part is as Petroleum carrying device；Fractionating column sets one
Side line, its distillation enters diesel oil stripping tower, output Paraffin liquid heavy；
Fractionating column base oil enters vacuum tower and carries out decompression separation, and tower top oil gas after cooling, enters Top of Vacuum Tower water distributing can and carries out
Gas-liquid separation, gas phase enters air through vacuum pump, and liquid phase is sent outside as liquid paraffin；Extract a side line out on vacuum tower top, take out
Go out part and go out device as Paraffin liquid heavy product；
After the pressurization of the cracked reaction feed pump of tail oil at the bottom of tower, enter cracking reaction system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610721609.7A CN106281444A (en) | 2016-08-24 | 2016-08-24 | A kind of operational approach producing more than 92% n-alkane product |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610721609.7A CN106281444A (en) | 2016-08-24 | 2016-08-24 | A kind of operational approach producing more than 92% n-alkane product |
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| Publication Number | Publication Date |
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| CN106281444A true CN106281444A (en) | 2017-01-04 |
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| CN201610721609.7A Pending CN106281444A (en) | 2016-08-24 | 2016-08-24 | A kind of operational approach producing more than 92% n-alkane product |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110616084A (en) * | 2018-06-20 | 2019-12-27 | 中国石油化工股份有限公司 | Process for producing crude white oil |
| CN110616083A (en) * | 2018-06-20 | 2019-12-27 | 中国石油化工股份有限公司 | Process for producing crude white oil |
| CN115043693A (en) * | 2022-07-27 | 2022-09-13 | 内蒙古伊泰煤基新材料研究院有限公司 | Process suitable for preparing coal-based linear alkylbenzene |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007269901A (en) * | 2006-03-30 | 2007-10-18 | Nippon Oil Corp | Method for treating synthetic oil, hydrocarbon oil for producing hydrogen and hydrocarbon oil for base material of diesel fuel |
| CN101173190A (en) * | 2007-10-22 | 2008-05-07 | 中国石油集团工程设计有限责任公司抚顺分公司 | Feito synthetic oil processing line |
| CN104611059A (en) * | 2015-02-12 | 2015-05-13 | 武汉炼化工程设计有限责任公司 | Method for preparing liquid paraffin, paraffin precursor and lubricant base oil precursor from Fischer-Tropsch synthesis products |
-
2016
- 2016-08-24 CN CN201610721609.7A patent/CN106281444A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007269901A (en) * | 2006-03-30 | 2007-10-18 | Nippon Oil Corp | Method for treating synthetic oil, hydrocarbon oil for producing hydrogen and hydrocarbon oil for base material of diesel fuel |
| CN101173190A (en) * | 2007-10-22 | 2008-05-07 | 中国石油集团工程设计有限责任公司抚顺分公司 | Feito synthetic oil processing line |
| CN104611059A (en) * | 2015-02-12 | 2015-05-13 | 武汉炼化工程设计有限责任公司 | Method for preparing liquid paraffin, paraffin precursor and lubricant base oil precursor from Fischer-Tropsch synthesis products |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110616084A (en) * | 2018-06-20 | 2019-12-27 | 中国石油化工股份有限公司 | Process for producing crude white oil |
| CN110616083A (en) * | 2018-06-20 | 2019-12-27 | 中国石油化工股份有限公司 | Process for producing crude white oil |
| CN110616083B (en) * | 2018-06-20 | 2021-11-16 | 中国石油化工股份有限公司 | Process for producing crude white oil |
| CN110616084B (en) * | 2018-06-20 | 2022-04-12 | 中国石油化工股份有限公司 | Process for producing crude white oil |
| CN115043693A (en) * | 2022-07-27 | 2022-09-13 | 内蒙古伊泰煤基新材料研究院有限公司 | Process suitable for preparing coal-based linear alkylbenzene |
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Application publication date: 20170104 |