CN105085154B - Increase production the method for aroamtic hydrocarbon raw material by heavy aromatics inferior - Google Patents
Increase production the method for aroamtic hydrocarbon raw material by heavy aromatics inferior Download PDFInfo
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Abstract
The present invention relates to a kind of method for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, the problem of mainly solving that mononuclear aromatics raw material can not be increased production with the heavy aromatics inferior containing condensed-nuclei aromatics present in conventional art.The present invention is by comprising the following steps：A) the inferior heavy aroamtic hydrocarbon raw material rich in mixing condensed-nuclei aromatics removes sulphur therein, nitrogen impurity；B) selective hydrogenation cracking reaction occurs for condensed-nuclei aromatics；C) selective hydrogenation cracking reaction product obtains light fraction, light aromatics cut, heavy arene cut and heavy distillat through Oil-gas Separation, after fractionating system is by boiling point fractionation；D) enter heavy aromatic hydrocarbon light reactor after heavy arene cut is mixed with hydrogen, occur transalkylation and dealkylation, reaction product returns to fractionating system；E) light aromatics cut drains into technical scheme out-of-bounds as product, preferably resolves the problem, in the industrial production available for production benzene, toluene and dimethylbenzene.
Description
Technical field
Aroamtic hydrocarbon raw material method is directly produced by heavy aromatics inferior the present invention relates to one kind, will can be contained especially with regard to one kind
The mixture through catalytic for having hydrocarbon with condensed rings is converted into high-purity benzene,toluene,xylene, the mononuclear aromatics of carbon nine and the mixing of the mononuclear aromatics of carbon ten
The method of thing.
Background technology
Benzene and paraxylene (PX) are important basic organic chemical industry raw materials, are widely used in the products such as production polyester, chemical fibre,
Clothing, food, lodging and transportion -- basic necessities of life with the national economic development and people are closely related, and in strong demand in recent years, increment is rapid.The source of aroamtic hydrocarbon raw material
Mainly there are two process routes：One raw material route is that naphtha obtains aroamtic hydrocarbon raw material by catalytic reforming, Aromatics Extractive Project；It is another
Bar raw material route is that the byproduct of ethylene unit-cracking of ethylene gasoline is passed through into hydrogenation, Aromatics Extractive Project to obtain aroamtic hydrocarbon raw material, from
And low value-added raw material is converted into high added value aromatic hydrocarbon product.In petrochemical factory, Aromatic Hydrocarbon United Plant is generally with to two
Toluene (coproduction ortho-xylene) is purpose product, and raw material is provided for downstream PTA devices.The maximum amount of paraxylene is produced, is removed
Outside dimethylbenzene in catalytic reforming and cracking of ethylene gasoline, mainly using the process of disproportionation and transalkylation toluene
And C9Aromatic hydrocarbons (in addition to the monocyclic C in part10Aromatic hydrocarbons) disproportionation and transalkylation reaction generation are carried out under molecular sieve catalyst effect
Mixed xylenes and benzene, mixed xylenes are converted into paraxylene by dimethylbenzene hysomer technique again.
Ethylene unit and Aromatic Hydrocarbon United Plant are all using naphtha as raw material, and limited naphtha resource will also meet domestic fast
The motor petrol demand that speed increases.The degree of dependence to raw material naphtha is reduced, aroamtic hydrocarbon raw material resource is expanded, is current development stone
The important topic of oiling work, catalytic cracking light cycle oil (LCO), Aromatic Hydrocarbon United Plant heavy aromatics tower tail oil, coal tar or coal are straight
Connect the visual field that the Heavy Aromatic Hydrocarbons inferior containing condensed-nuclei aromatics such as liquefaction oil enter people.Wherein mainly contain the bicyclic virtue of naphthalene system
Hydrocarbon, anthracene, phenanthrene be thrcylic aromatic hydrocarbon etc. hydrocarbon, cut is wide, complicated components and can not isolate pure component, and value is not
It is high.After coal tar and coal direct liquefaction oil are by hydrotreating, available for production fuel oil and automobile-used petrol and diesel oil, but not yet it is used for
The production of high added value aromatic hydrocarbon product.Aromatic Hydrocarbon United Plant heavy aromatics tail oil is further sharp after the products such as durene are isolated
Value less, can only be used as hydrogenation plant raw material or fuel oil.
LCO total arene content is up to 80%, and naphthalene system double ring arene accounts for 70% or so, and mononuclear aromatics and thrcylic aromatic hydrocarbon are about
15% or so is respectively accounted for, other is alkane, cycloalkane and alkene etc..LCO 0.2~1.5wt% of sulfur content, nitrogen content 100~
750ppm, Cetane number only has 15~25, and ignition performance is poor, and the Technical Economy for processing derv fuel is not good.LCO usually as
A kind of second-rate diesel oil blending component is used in mixed way with straight-run diesel oil, or is directly used as fuel oil.In recent years, it is domestic
Catalytic cracking unit more than using maximizing iso-paraffins MIP techniques carry out technology upgrading, a large amount of by-product MIP light diesel fuels are (i.e.
LCO) there is the utilization of resources and increment problem.China's catalytic cracking (FCC) device year processing capacity is close to 100,000,000 tons, and LCO year gives birth to
Yield is more than 10,000,000 tons.
Current poor quality catalytic cracking diesel (mainly LCO) modification means generally used both at home and abroad are hydrofinishing, added
Hydrogen is modified and light oil type hydrogen cracking.Catalytic diesel oil hydrofinishing, be in, under conditions of low pressure, carry out olefins hydrogenation,
Desulfurization, denitrogenation and aromatic moiety saturated reaction, can improve its color and stability, and Cetane number increase rate is smaller, especially
It is the catalytic unit for processing inferior raw material, its catalytic diesel oil is also wanted far from meeting product by hydrofinishing to Cetane number
Ask.The Unicracking techniques (USP5026472) of hydrogenation modifying process, such as Uop Inc., with good aromatic hydrogenation saturability
Can and selectivity of ring-opening, aromatic hydrocarbons conversion level is very high, it is ensured that larger Cetane number increase rate and have higher diesel yield,
But the hydrogen consumption of the technique is very big, and high-pressure installation investment and operating cost are all higher.Light oil type hydrogen cracking is then by light bavin
Oily component is after refined, and violent saturated hydrogenation obtains the reforming material or gasoline fraction of naphtha cut, and this process similarly has
The problem of having aromatic hydrocarbons supersaturation and too high hydrogen consumption, and the cycloalkane and chain hydrocarbon that are generated after supersaturation will also be in reformers
Aromatic hydrocarbons is converted into, is not an economic route.The light oil type hydrogen cracking method that such as CN101684415 patents are proposed, not directly
Practice midwifery aromatic hydrocarbons, the virtue of heavy naphtha is dived relatively low.
In order to which light cycle oil is converted into the higher mononuclear aromatics of industrial added value, patent CN102227490 is described
A kind of to prepare clean fuel and the method for aromatic compound by light cycle oil, this process cuts into light cycle oil raw material
After 170-220 DEG C and 220-360 DEG C of cut, wherein light oil distillate are by hydrofinishing and hydrocracking reaction, then by special
Beds, liquid petroleum gas cut is cracked into by the non-aromatics in the reaction effluent for mainly containing aromatic hydrocarbons and non-aromatics,
So as to obtain the aromatic hydrocarbon product of higher degree.However, the light oil distillate Partial Conversion of only 170-220 DEG C cut produces for aromatic hydrocarbons
Product, the utilization rate of raw material is not high.Patent USP7265252 describes a kind of fuels from FCC LCO hydro-conversion-alkylation selectivity and turned
The method that colonization produces dimethylbenzene.This process is that first pre-hydrotreating removes the impurity such as sulphur, nitrogen in feedstock oil, is then being entered
Double ring arene is partially converted into mononuclear aromatics by the reaction of row catalytic hydrocracking, anti-finally by the transalkylation of mononuclear aromatics
Should, generation target product dimethylbenzene and benzene, while going back a part of liquefied gas of by-product, light naphthar and ultra-low-sulphur diesel component.So
And, because hydrofinishing and isocrackate are directly entered transalkylation reaction, the presence of a large amount of by-product non-aromaticss will be to alkane
The long-term operation of group-transfer catalyst brings adverse effect, and the purity of aromatic hydrocarbon product is not also high.
The content of the invention
The technical problems to be solved by the invention are not high inferior heavy aroamtic hydrocarbon raw material utilization rate, mononuclear aromatics low yield, virtue
There is provided a kind of new method that aroamtic hydrocarbon raw material is directly produced with heavy aromatics inferior for the problems such as hydrocarbon product purity is not high.This method is used
Aroamtic hydrocarbon raw material is directly produced in heavy aromatics inferior, with aroamtic hydrocarbon raw material utilization rate is high, mononuclear aromatics product yield is high and product is pure
The features such as having spent.
In order to solve the above-mentioned technical problem, the technical solution adopted by the present invention is as follows：One kind passes through hydrofinishing, selectivity
The method being combined with heavy aromatic hydrocarbon light is hydrocracked, is comprised the following steps：A) inferior heavy rich in mixing condensed-nuclei aromatics
Raw material mixed with hydrogen after by hydrofining reactor, remove sulphur therein, nitrogen impurity；B) come from hydrofining reactor
After logistics is mixed with appropriate amount of hydrogen again, pass through the selective hydrogenation cracker connected with hydrofining reactor, condensed ring virtue
Selective hydrogenation cracking reaction occurs for hydrocarbon；C) selective hydrogenation cracking reaction product presses boiling through Oil-gas Separation, in fractionating system
Light fraction, light aromatics cut, heavy arene cut and heavy distillat are obtained after point fractionation, wherein heavy distillat is partly or entirely followed
Loopback selective hydrogenation cracker, light fraction is drained into out-of-bounds；D) heavy virtue is entered after heavy arene cut is mixed with hydrogen
Hydrocarbon lighting reactor, occurs transalkylation and dealkylation, and reaction product returns to fractionating system；E) light aromatics evaporates
It is allocated as draining into out-of-bounds for product.
In above-mentioned technical proposal, raw material comes catalytic cracking light cycle oil, Aromatic Hydrocarbon United Plant heavy aromatics tower tail oil or coal
At least one of direct liquefaction oil, 180~370 DEG C of boiling spread, density is not less than 0.85g/ml at 20 DEG C, with percentage by weight
Meter, total aromatic ring content is between 50-98%, and Bicyclic aryl rings content is between 35-80%, and sulfur content is between 0~3%, and nitrogen contains
Amount is between 0~3%；The light aromatics cut that fractionating system is obtained is benzene, toluene, ethylbenzene and dimethylbenzene, also comprising cycloalkane
And alkane, by weight percentage, arene content is between 65-95%, and total sulfur content is less than 0.5ppm, and total nitrogen content is less than
0.5ppm；The boiling spread of heavy arene cut is 145~200 DEG C；The boiling spread of unconverted heavy distillat is 200~350 DEG C；
The operating pressure of hydrofining reactor is between 3.5~10.0MPa, and inlet temperature is between 330~400 DEG C, hydrogen oil volume
Than between 400~1000 (V/V)；Hydrotreated product is directly entered selective hydrogenation cracker, pressure and hydrogenation essence
Reactor processed is consistent, and inlet temperature is between 350-420 DEG C, and hydrogen to oil volume ratio is between 600~1200 (V/V)；Heavy arene
The operating pressure of lighting reactor is between 2.5~3.5MPa, and inlet temperature is at 360~450 DEG C, and hydrogen to oil volume ratio is 500
Between~1200 (V/V).
To contain the mixture of condensed-nuclei aromatics as raw material, by hydrofinishing unit, selective hydrogenation Cracking Unit and
Non-aromatic conversion unit, can be efficiently produced former including mononuclear aromatics such as benzene,toluene,xylene, C9 aromatic and monocyclic C10 aromartics
Material.The impurity such as hydrofinishing unit efficient removal sulphur, nitrogen, fractional saturation condensed-nuclei aromatics component.Mixture is in choosing after imurity-removal
Under the effect of selecting property hydrocracking catalyst, mononuclear aromatics product and a small amount of non-aromatics are selectively converted to.Benzene is fragrant to the lightweight of carbon eight
Hydrocarbon-fraction can be directly entered Aromatic Hydrocarbon United Plant, including the heavy arene cut of carbon nine and carbon ten reacts in heavy aromatic hydrocarbon light
De- alkyl and transalkylation reaction occur in device, so as to maximize the important basic organic chemical industries such as volume increase benzene, toluene and dimethylbenzene
Raw material.
As can be seen that such process route, can convert the relatively low mixture containing condensed-nuclei aromatics of the added value of industry
For the mononuclear aromatics mixture of high added value, the heavy arene cut for being hydrocracked by-product is further converted to benzene, toluene and two
Toluene, with volume increase benzene, toluene and dimethylbenzene, the features such as product value-added effect is good is maximized, achieves preferable technique effect.
Brief description of the drawings
Fig. 1 is the schematic diagram of the technique for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior according to the present invention.The figure is intended to signal
Property, which is illustrated rather than, to be limited.
Enter hydrofining reactor after raw material containing heavy aromatics inferior is mixed by the hydrogen of pipeline 1 and pipeline 9
2, reaction effluent mixes laggard selectable hydrocracking reactor 4 with the hydrogen partial in pipeline 9 again by pipeline 3, instead
Effluent is answered to send into high-pressure separator 6 through pipeline 5.Hydrogen gas-phase product enters circulating hydrogen compressor 8, part by pipeline 7
Drain into out-of-bounds.High pressure hydrogen from supplement hydrogen compressor 29 is incorporated in pipeline 9 by pipeline 32, and low pressure hydrogen passes through pipeline 31
It is incorporated in pipeline 27.Liquid product in high-pressure separator 6 sends into low pressure separator 11 by pipeline 10, and light hydrocarbon component is from pipeline
12 are drained into out-of-bounds, and liquid phase component sends into fractionating column 14 through pipeline 13, and less than 70 DEG C light components are drained into out-of-bounds through pipeline 16, bottom of towe weight
Component delivers to fractionating column 17 by pipeline 15, and boiling point is used as product by pipeline 19 between 70-145 DEG C of light aromatics cut and drained into
Out-of-bounds.Bottom of towe boiling point is more than 200 DEG C of ends fractions and returns to selective hydrogenation cracker 4 as charging, and part is outer to drain into boundary
Outside.It is light that 145-200 DEG C of component of boiling range of side take-off enters heavy arene after being mixed by pipeline 20 with the hydrogen in pipeline 27
Matter reactor 21, reaction effluent delivers to gas-liquid separator 23 by pipeline 22, and hydrogen gas-phase product enters by pipeline 25
Enter circulating hydrogen compressor 26, partly drain into out-of-bounds.Liquid product in gas-liquid separator 23 is back to pipeline 13 by pipeline 24,
Into fractionating system.
Below by embodiment, the invention will be further elaborated.
Embodiment
【Embodiment 1】
It is after 180-370 DEG C of heavy aromatics inferior is mixed with 6.0MPa hydrogen, into hydrofining reactor removing by boiling point
Sulphur nitrogen, surplus next aromatic ring is saturated to part condensed-nuclei aromatics, and table 1 lists catalyst and reaction condition used.Table 2 is listed
The sulphur nitrogen content of raw material and hydrofinishing product, density, aromatic content, naphthane system arene content and evaporate
Distribution.The nitrogen content of hydrotreated product is less than 20ppm.
Table 1
Table 2
【Embodiment 2】
After hydrotreated product is mixed with 6.0MPa hydrogen, into selective hydrogenation cracker, occurs naphthane
It is the selective hydrogenation ring-opening reaction and dealkylation of aromatic hydrocarbons and polycyclic aromatic hydrocarbon.Table 3 lists used catalyst and reaction
Condition.Selective hydrogenation cracked reaction product cuts into less than 70 DEG C light fractions, 70-145 in the fractionating column of series connection by boiling point
DEG C light aromatics cut, 145-200 DEG C of heavy arene cut and more than 200 DEG C heavy distillat.Less than 70 DEG C light fractions drain into boundary
Outside；70% heavy distillat is recycled back to selective hydrogenation cracker, and 30% heavy distillat is drained into out-of-bounds；70-145 DEG C of light aromatics evaporates
It is allocated as arranging outside product；145-200 DEG C of cut fed downstream.Table 4 lists the composition of light aromatics component, mainly benzene, first
Benzene, ethylbenzene and dimethylbenzene, also containing a small amount of cycloalkane and alkane.
Table 3
Table 4
| 70-145 DEG C of cut product |
| Below C6 is non-aromatic | 0.32 |
| C6-C8 is non-aromatic | 8.76 |
| Benzene | 13.72 |
| Toluene | 36.13 |
| Ethylbenzene | 7.48 |
| Dimethylbenzene | 33.5 |
| It is more than C9 hydro carbons | 0.09 |
【Embodiment 3】
After 145-200 DEG C of heavy arene cut is mixed with 3.0MPa hydrogen, into heavy aromatic hydrocarbon light reactor, carbon
Transalkylation and side chain dealkylation occur for nine aromatic hydrocarbons, carbon ten and above aromatic hydrocarbons.Table 5 lists heavy aromatics lighting used
Catalyst and reaction condition.Heavy aromatics lighting product is returned in fractionating system after Oil-gas Separation.
Table 5
Claims (7)
1. a kind of method for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, comprises the following steps：
A) after the inferior heavy aroamtic hydrocarbon raw material rich in mixing condensed-nuclei aromatics is mixed with hydrogen, by hydrofining reactor, it is removed
In sulphur, nitrogen impurity；The operating pressure of hydrofining reactor is between 6.0~10.0MPa, and inlet temperature is at 330~400 DEG C
Between, hydrogen to oil volume ratio is between 400~1000；
B) after the logistics come out from hydrofining reactor is mixed with hydrogen again, the selection connected with hydrofining reactor is passed through
Property hydrocracking reactor, condensed-nuclei aromatics occur selective hydrogenation cracking reaction；Hydrocracking reactor pressure and hydrofinishing
Reactor is consistent, and inlet temperature is between 350-420 DEG C, and hydrogen to oil volume ratio is between 600~1200；
C) selective hydrogenation cracking reaction product, after Oil-gas Separation, after fractionating system presses boiling point fractionation, is gently evaporated
Point, light aromatics cut, heavy arene cut and heavy distillat, wherein heavy distillat is partly or entirely recycled back to selective hydrogenation and splits
Change reactor, light fraction is drained into out-of-bounds；
D) after heavy arene cut is mixed with hydrogen, into heavy aromatic hydrocarbon light reactor, occur transalkylation and de- alkyl
Reaction, reaction product returns to fractionating system；
E) light aromatics cut is drained into out-of-bounds as product；
Hydrofining reaction catalyst is 3wt%NiO-18wt%MoO in wherein step a)3/Al2O3；Selectively add in step b)
Hydrogen Cracking catalyst is 2.5wt%NiO-24wt%WO3- 60wt%USY/Al2O3；
The boiling spread of light aromatics cut is 70-145 DEG C in step c), and the boiling spread of heavy arene cut is 145~200
℃。
2. the method according to claim 1 for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, it is characterised in that be that raw material comes from
At least one of catalytic cracking light cycle oil, Aromatic Hydrocarbon United Plant heavy aromatics tower tail oil or coal direct liquefaction oil, boiling spread 180
~370 DEG C, density is not less than 0.85g/ml at 20 DEG C, and by weight percentage, total aromatic ring content is bicyclic between 50-98%
Aromatic ring content is between 35-80%, and sulfur content is between 0~3%, and nitrogen content is between 0~3%.
3. the method according to claim 1 for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, it is characterised in that fractionating system is obtained
The light aromatics cut arrived is benzene, toluene, ethylbenzene and dimethylbenzene, also comprising cycloalkane and alkane.
4. the method according to claim 1 for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, it is characterised in that fractionating system is obtained
To light aromatics cut in, by weight percentage, arene content is between 65-95%.
5. the method according to claim 1 for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, it is characterised in that fractionating system is obtained
The light aromatics cut arrived, total sulfur content is less than 0.5ppm, and total nitrogen content is less than 0.5ppm.
6. the method according to claim 1 for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, it is characterised in that unconverted double distilled
The boiling spread divided is 200~350 DEG C.
7. the method according to claim 1 for increasing production aroamtic hydrocarbon raw material by heavy aromatics inferior, it is characterised in that heavy arene is light
The operating pressure of matter reactor between 2.5~3.5MPa, inlet temperature at 360~450 DEG C, hydrogen to oil volume ratio 500~
Between 1200.
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| CN109718760A (en) * | 2017-10-30 | 2019-05-07 | 中国石油化工股份有限公司 | A method of light aromatics is produced by raw material of catalytic cracking diesel oil |
| CN108179026A (en) * | 2018-02-09 | 2018-06-19 | 中国海洋石油集团有限公司 | A kind of heavy aromatic hydrocarbon light prepares the method and device of low-carbon aromatic hydrocarbons |
| CN114437818B (en) * | 2020-10-30 | 2023-04-07 | 宁波中金石化有限公司 | Heavy aromatic oil processing method |
| CN114437811B (en) * | 2020-10-30 | 2023-05-16 | 中国科学院宁波材料技术与工程研究所 | Processing method for lightening heavy aromatic oil |
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| CN101730673A (en) * | 2007-07-06 | 2010-06-09 | 环球油品公司 | Be used to produce the method for dimethylbenzene |
| CN103059917A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Light cycle oil selective hydrorefining method |
| CN103108849A (en) * | 2010-09-16 | 2013-05-15 | Sk新技术株式会社 | Method of producing valuable aromatics and olefins from hydrocarbonaceous oils derived from coal or wood |
| CN103121897A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing arene by mixture containing hydrocarbon with condensed rings |
| CN103121895A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing monocyclic aromatic hydrocarbons by polycyclic aromatic hydrocarbons |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101730673A (en) * | 2007-07-06 | 2010-06-09 | 环球油品公司 | Be used to produce the method for dimethylbenzene |
| CN103108849A (en) * | 2010-09-16 | 2013-05-15 | Sk新技术株式会社 | Method of producing valuable aromatics and olefins from hydrocarbonaceous oils derived from coal or wood |
| CN103059917A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Light cycle oil selective hydrorefining method |
| CN103121897A (en) * | 2011-11-18 | 2013-05-29 | 中国石油化工股份有限公司 | Method for preparing arene by mixture containing hydrocarbon with condensed rings |
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