CN108017492A - The method of mixed light-hydrocarbon aromatization aromatic hydrocarbons - Google Patents
The method of mixed light-hydrocarbon aromatization aromatic hydrocarbons Download PDFInfo
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- CN108017492A CN108017492A CN201610961622.XA CN201610961622A CN108017492A CN 108017492 A CN108017492 A CN 108017492A CN 201610961622 A CN201610961622 A CN 201610961622A CN 108017492 A CN108017492 A CN 108017492A
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
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Abstract
The present invention relates to a kind of method of mixed light-hydrocarbon aromatization aromatic hydrocarbons, mainly solves the problems, such as that the easy coking and deactivation of aromatizing catalyst for light hydrocarbon is fast in the prior art and aromatics yield is low.The present invention is by using including the following steps：1) light hydrocarbon feedstocks are separated into absorption tower absorbs tail gas and absorbing liquid；2) absorbing tail gas goes ethylene recovery unit to isolate ethene, hydrogen and fuel gas, and wherein ethene removes light dydrocarbon aromatization reaction device；3) absorbing liquid is separated into aromatization raw material and heavy constituent logistics in depentanizer；4) heavy constituent logistics is divided into two streams, one logistics returns to absorption tower as absorbent, and another burst of logistics is as the first arene stream product；5) aromatization raw material and ethene are sent into light dydrocarbon aromatization reaction device；6) light dydrocarbon aromatization reaction product is separated into circulation lighter hydrocarbons and the second arene stream product in gas-liquid separator after cooling；7) circulate the technical solution that lighter hydrocarbons return to absorption tower and preferably solve the above problem, available in light-hydrocarbon aromatized industrial production.
Description
Technical field
The present invention relates to a kind of method of mixed light-hydrocarbon aromatization aromatic hydrocarbons.
Technical background
Aromatic hydrocarbons, particularly light aromatics BTX (benzene,toluene,xylene), are important basic organic chemical industry raw materials, it is produced
Amount is inferior to ethene and propylene with scale.Paraxylene is with high value-added product in aromatic hydrocarbons.Paraxylene is polyester work
The important source material of industry, mainly for the production of p-phthalic acid (PTA) or p-phthalic acid's dimethyl ester (DMT), and then by PTA
Production polyester (PET) is removed with DMT.
Light aromatics is usually made using naphtha as raw material through catalytic reforming and Aromatic Hydrocarbon United Plant.Methanol aromatic hydrocarbons is then
Technical strategies using coal-based methanol as raw material aromatic hydrocarbons.Rich coal resources in China, exploitation methanol aromatic hydrocarbons technology is pair
The important supplement of conventional petroleum chemical industry route preparing aromatic hydrocarbon.
Methanol aromatic hydrocarbons technology is using methanol as raw material, in the catalytic action of difunctional (acid and dehydrogenation) active catalyst
Under, by dehydrogenation, cyclisation and etc. production aromatic hydrocarbons process.In this aromatization process, benzene,toluene,xylene is generated
Deng aromatic hydrocarbons, and by-product includes hydro carbons and the hydrogen such as methane, ethene, propylene.In general, carbon-based aromatics yield only about 50%, by-product
The aromatisation of lighter hydrocarbons is of great significance for the total arenes yield and overall technology economy for improving methanol aromatic hydrocarbons.
Light-hydrocarbon aromatized technology is a kind of nonpetroleum processing technology developed in the past 20 years, it is characterized in that utilizing modification
Low molecular hydro carbons such as liquefied gas, tops etc. are converted into the light aromatics such as BTX or gasoline by zeolite molecular sieve catalyst.
ZSM-5 molecular sieve has obtained extensive industry since its special shape selectivity, good hydrothermal stability and carbon accumulation resisting ability are strong
Using.In ZSM-5 zeolite on the catalyst of main active component, low molecule alkane or alkene can be directly translated into aromatic hydrocarbons,
And the arene underwater content of raw material is not required.Using this characteristic, develop in succession both at home and abroad multinomial by different process, difference
Raw material directly produces the light-hydrocarbon aromatized industrial technology of the light aromatics such as BTX or high octane value gasoline blending component.
Foreign technology has Cyclar techniques, Alpha techniques and Z-Forming technologies, M2-forming techniques, Aro-
Forming techniques and Zeoforming techniques.Domestic technique has the GTA aromatization technologies of Luoyang engineering company, Shi Ke institutes aromatization
Change technology and great Qi scientific ＆ technical corporation Nano-forming aromatisation.The aromatics yield of above technology about 50%, while by-product 20~
30% liquefied gas, carbon three therein and above component can continue aromatisation to further provide for aromatic hydrocarbons total recovery.Process above
The carbon three in liquefied gas and above component are not recycled, therefore aromatics yield is not high.
Patent No. CN101759512A discloses a kind of method using high olefin content lighter hydrocarbons production aromatic hydrocarbons.This method pin
, carbon deposition quantity big to high olefin content light hydrocarbon feedstocks aromatization coking probability is greatly, catalyst inactivation speed is fast, the one way cycle is short
The defects of, there is provided a kind of method using high olefin content lighter hydrocarbons production aromatic hydrocarbons, includes the following steps：Through impurity pretreatment height
Olefin(e) centent lighter hydrocarbons are warming up to 450 after efficient anti-coking feeds and gasifies at 100~109 DEG C of evaporator into composite heating stove
~570 DEG C, then enter solid bed bed reactor from top to bottom under the drive for being recycled back into carrier gas, under the action of catalyst into
Row aromatization, 500 DEG C~600 DEG C of reaction temperature, 0~0.4MPa of pressure, 0.4~0.8h of air speed-1.The present invention uses anti-caking
The means such as burnt technical equipment, new aromatized catalyst, circulating air return solve the above problem.
Patent No. CN101759515A discloses a kind of method that light dydrocarbon aromatization reaction regeneration switches online.This method bag
Include identical two sets of reaction systems, often cover reaction system according to process sequence, including sequentially connected feeding vaporizer plus
Hot stove, reactor, the reaction product of two sets of reaction systems enter same gas-liquid separator, gas-liquid separator top after cooling
It is connected by gas phase pipeline with surge tank, heating furnace of the surge tank respectively with two sets of reaction systems is connected；Switch in reaction system
Before, then the reactor pre-heating temperature elevation that the circulation dry gas of gas-liquid separator is introduced to be switched system switches to 450~570 DEG C
Charging, completes on-line continuous switching production.The present invention draws dry gas in reactant vapor-liquid separation upper end, shortens return line,
Save switching time.
Although process above improves total fragrant yield by lighter hydrocarbons circulation, circulate and carry hydrogen and aromatic hydrocarbons in dry gas secretly,
These components are unprocessed, direct Returning reactor, and aromatics yield will be caused low, and catalyst inactivation accelerates, and influence the length of device
Phase stable operation.
Therefore, the prior art is there are catalyst inactivation soon and the problem of aromatic hydrocarbons total recovery is low, it is of the invention targetedly
Solves the above problem.
The content of the invention
Catalyst inactivation exists in the prior art soon for the technical problems to be solved by the invention and aromatic hydrocarbons total recovery is low
A kind of problem, there is provided method of new mixed light-hydrocarbon aromatization.The device has catalyst life length and high excellent of aromatics yield
Point.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of side of mixed light-hydrocarbon aromatization aromatic hydrocarbons
Method, includes the following steps：1) light hydrocarbon feedstocks are separated into absorption tower absorbs tail gas and absorbing liquid；2) absorbing tail gas goes ethene to return
Receive unit and isolate ethene, hydrogen and fuel gas, wherein ethene removes light dydrocarbon aromatization reaction device；3) absorbing liquid is in depentanizer
It is separated into aromatization raw material and heavy constituent logistics；4) heavy constituent logistics is divided into two streams, one logistics is as absorbent
Absorption tower is returned to, another burst of logistics is as the first arene stream product；5) aromatization raw material and ethene are sent into lighter hydrocarbons aromatization
Change reactor；6) light dydrocarbon aromatization reaction product is separated into circulation lighter hydrocarbons and the second aromatic hydrocarbons thing in gas-liquid separator after cooling
Miscarriage product；7) lighter hydrocarbons are circulated and returns to absorption tower.
In above-mentioned technical proposal, the light hydrocarbon feedstocks include hydrogen, methane, ethene, ethane, propylene, propane, carbon four, carbon
5th, the component such as benzene,toluene,xylene.
In above-mentioned technical proposal, mass fraction of the absorbent containing BTX is more than 80%.
In above-mentioned technical proposal, the absorption tower operating pressure is 1.5~2.5MPA.
In above-mentioned technical proposal, the depentanizer operating pressure is 0.5~0.8MPA.
In above-mentioned technical proposal, the light dydrocarbon aromatization reaction condition is：500~600 DEG C of reaction temperature, reaction pressure
0.1~0.6MPA, 0.1~3HR of reaction mass air speed-1。
In above-mentioned technical proposal, it is preferred that as absorbent stream and the weight ratio of the first arene stream 150 in step 4)
~50；It is furthermore preferred that as absorbent stream and the weight ratio of the first arene stream 120~80 in step 4).
In above-mentioned technical proposal, the circulation lighter hydrocarbons are pressurized to pressure more than after the operating pressure of absorption tower through compressor, into
Enter absorption tower.
In above-mentioned technical proposal, after the light hydrocarbon feedstocks are cooled below 10 DEG C, operated through gas-liquid separation, gas phase is gone
Absorption tower, liquid phase remove depentanizer.
In above-mentioned technical proposal, the light hydrocarbon feedstocks are sent into absorption tower after UF membrane removes hydrogen partial.
Method using the present invention, light hydrocarbon feedstocks include more than two hydro carbons of hydrogen, methane and carbon.Pass through absorption and desorption system
System, pre-processes light hydrocarbon feedstocks and circulation lighter hydrocarbons.Obtained in light hydrocarbon feedstocks and circulation lighter hydrocarbons through absorption tower and absorb tail gas, tail
Gas self-absorption top of tower is discharged, wherein including hydrogen, methane and ethylene-ethane.The absorbing liquid of absorption tower bottom discharge is in de- pentane
Heavy constituent (aromatic hydrocarbons such as including benzene,toluene,xylene) is effectively removed in tower, avoids these heavy constituents from being led in catalyst surface coking
Cause catalyst inactivation.Propylene, propane, four light dydrocarbon component of carbon, and in absorption tower are included from the material of depentanizer top extraction
The part ethylene-ethane absorbed by absorbent.These components can be effectively converted into virtue except ethane in aromatization reactor
Hydrocarbon.
Method using the present invention, is stripped of hydrogen in absorption tower, controls content of the hydrogen in reaction feed, carries
The conversion ratio of high lighter hydrocarbons.In ethylene recovery system, hydrogen product is isolated from absorbing in tail gas, is isolated from two component of carbon
Ethene and ethane, wherein ethane avoid the accumulation of ethane, wherein ethene goes light-hydrocarbon aromatized anti-as fuel gas discharge system
Device is answered, is converted into aromatic hydrocarbons, improves aromatic hydrocarbons total recovery.
Method using the present invention, reaction product are sent into gas-liquid separator, the gas phase discharging of gas-liquid separator after cooling
By returning to absorption tower after compressor boost, methane, hydrogen and part ethane in elimination reaction product.And through ethylene recovery system
System recycling ethene.
Method using the present invention, is operated by absorption and rectifying etc., hydrogen in the reaction feed of light dydrocarbon aromatization reaction device
The content of the impurity such as gas, methane, ethane, benzene, toluene is controlled under some controlling values, makes these trace impurities to catalyst
The influence in service life is reduced to receivable degree.
Method using the present invention, a kind of preferable scheme is that light hydrocarbon feedstocks are cooled to first before absorption tower is sent into
10 DEG C, operated through gas-liquid separation, gas phase goes to absorption tower, and liquid phase removes depentanizer, can effectively reduce absorption tower and depentanizer
Load.
Method using the present invention, a kind of preferable scheme is that light hydrocarbon feedstocks are before absorption tower is sent into, using UF membrane
Or adsorption separation technology removing hydrogen partial, the dosage of absorbent is reduced, while reduce energy consumption.
Method using the present invention, light hydrocarbon feedstocks are stripped of the component for causing catalyst coking by pretreatment, by returning
Receive using lighter hydrocarbons raising total arenes yield is circulated, achieve preferable technique effect.
Brief description of the drawings
Fig. 1 is the flow diagram of the method for the invention.
In Fig. 1,1 is light hydrocarbon feedstocks；2 be absorption tail gas；3 be absorbing liquid；4 be absorbent；5 be hydrogen and fuel gas；6 are
Ethene；7 be aromatization raw material；8 be aromatization reaction products；9 be the second arene stream；10 be the first arene stream；11
To circulate lighter hydrocarbons.I is absorption tower, and II is ethylene recovery unit, and III is depentanizer, and IV is light dydrocarbon aromatization reaction device, and V is
Gas-liquid separator.
The process description is as follows：Light hydrocarbon feedstocks and the light body of circulation are separated into after converging in absorption tower absorbs tail gas and absorption
Liquid；Absorb tail gas and be separated into two logistics of hydrogen, methane and carbon through the operation such as rectifying and/or UF membrane in ethylene recovery system,
Two logistics of carbon goes ethylene rectifying column to be separated into ethene and ethane, and wherein ethene removes light dydrocarbon aromatization reaction device；Absorbing liquid is de- penta
Aromatization raw material and heavy constituent are separated into alkane tower；Heavy constituent part returns to absorption tower as absorbent, remaining goes de- penta
Alkane tower；The aromatization raw material of depentanizer top extraction removes light dydrocarbon aromatization reaction device, and tower bottoms is the first arene stream；Gently
Hydrocarbon aromatizing reaction product is separated into circulation lighter hydrocarbons and the second arene stream in gas-liquid separator after cooling；Circulation lighter hydrocarbons return
Go back to absorption tower.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Embodiment
【Comparative example 1】
Light hydrocarbon feedstocks flow is 47 ton hours, and volume fraction composition is hydrogen 54%, methane 8%, carbon 2 12%, carbon three
And the above 26%.The mass content of aromatic hydrocarbons is 4.9% in light hydrocarbon feedstocks.It is sent directly into after light hydrocarbon feedstocks waste heat light-hydrocarbon aromatized anti-
Device is answered, reaction temperature is 560 DEG C, reaction pressure 0.25MPa, reaction mass air speed 1HR-1.Pass through absorption after reaction product cooling
The conventional separation means such as operation and distillation operation, obtain 17 ton hour of aromatic hydrocarbons, 7 ton hour of ethane, 38 ton hour of carbon, tail gas
15 ton hours.In the comparative example, carbon three does not recycle, aromatics yield (hydrogen, methane and ethane conduct in light hydrocarbon feedstocks
Can not aromatisation component not calculate) be 44.7%.
【Embodiment 1】
Flow as shown in Figure 1, light hydrocarbon feedstocks flow are 47 ton hours, and volume fraction composition is hydrogen 54%, methane 8%,
Carbon 2 12%, carbon three and the above 26%.The mass content of aromatic hydrocarbons is 4.9% in light hydrocarbon feedstocks.Absorption tower operating pressure is
1.6MPa, absorption exhaust flow are 28.6 ton hours.Absorbent dosage is 600 ton hours, absorbent stream and the first aromatic hydrocarbons
The weight ratio of logistics is 120, and wherein the mass fraction of BTX is 87%.Tail gas is absorbed after compressor is pressurized to 3.2MPa, in film
3.2 ton hour hydrogen are isolated in separator, 12.6 ton hour methane are isolated in domethanizing column, in ethylene rectifying column
Isolate 5.7 ton hour ethene and 7.1 ton hour ethane.Absorbing liquid separates in depentanizer.Depentanizer operating pressure
For 0.7MPa, overhead stream flow is 60.2 ton hours, and tower reactor flow is 605 ton hours, wherein 600 ton hours are absorption
Agent, remaining 5 ton hour are the first arene stream, discharge system.Ethene enters lighter hydrocarbons aromatization after mutually converging with depentanizer top gas
Change reactor.Light dydrocarbon aromatization reaction temperature is 560 DEG C, reaction pressure 0.25MPa, reaction mass air speed 1HR-1.Circulate lighter hydrocarbons
Pressure is 1.6MPa after compression, and flow is 47.5 ton hours.Second arene stream flow is 18 ton hours.The embodiment
Aromatics yield (hydrogen, methane in light hydrocarbon feedstocks and ethane as can not aromatisation component not calculate) is 60.5%.Catalysis
Agent regeneration period relatively example extends 33%.
【Embodiment 2】
According to the condition and step described in embodiment 1, light hydrocarbon feedstocks and circulation lighter hydrocarbons converge after, be sent into absorption tower it
Before, 10 DEG C are cooled to first, and gas phase goes to absorption tower after gas-liquid separation operates, and liquid phase removes depentanizer.The embodiment absorbent
Dosage is 450 ton hours, and the weight ratio of absorbent stream and the first arene stream is 90, can effectively reduce the negative of absorption tower
Lotus about 25%.Aromatics yield is 59.3%, and catalyst regeneration cycle relatively example extends 30%.
【Embodiment 3】
According to the condition and step described in embodiment 1, light hydrocarbon feedstocks and circulation lighter hydrocarbons converge after, be sent into absorption tower it
Before, 90% hydrogen is removed using membrane separation technique, improves and absorbs the partial pressure of carbon two and above component in charging, improves and absorbs effect
Rate, the dosage of absorbent are 560 ton hours, and the weight ratio of absorbent stream and the first arene stream is 112.Aromatics yield is
59.6%, catalyst regeneration cycle relatively example extends 31%.
【Embodiment 4】
According to the condition and step described in embodiment 1, after light hydrocarbon feedstocks converge with circulation lighter hydrocarbons, taken off using membrane separation technique
Except 90% hydrogen, 10 DEG C are subsequently cooled to, gas phase goes to absorption tower after gas-liquid separation operates, and liquid phase removes depentanizer.This implementation
The dosage of example absorbent be 420 ton hours, and the weight ratio of absorbent stream and the first arene stream is 84.Aromatics yield is
58.7%, catalyst regeneration cycle relatively example extends 33%.
【Embodiment 5】
Flow as shown in Figure 1, light hydrocarbon feedstocks flow are 47 ton hours, and volume fraction composition is hydrogen 54%, methane 8%,
Carbon 2 12%, carbon three and the above 26%.The mass content of aromatic hydrocarbons is 4.9% in light hydrocarbon feedstocks.Absorption tower operating pressure is
1.6MPa, absorption exhaust flow are 28.6 ton hours.Absorbent dosage is 590 ton hours, absorbent stream and the first aromatic hydrocarbons
The weight ratio of logistics is 59, and wherein the mass fraction of BTX is 78%.Tail gas is absorbed after compressor is pressurized to 3.2MPa, in film
3.2 ton hour hydrogen are isolated in separator, 12.6 ton hour methane are isolated in domethanizing column, in ethylene rectifying column
Isolate 5.7 ton hour ethene and 7.1 ton hour ethane.Absorbing liquid separates in depentanizer.Depentanizer operating pressure
For 0.9MPa, overhead stream flow is 65.2 ton hours, and tower reactor flow is 600 ton hours, wherein 590 ton hours are absorption
Agent, remaining 10 ton hour are the first arene stream, discharge system.Ethene enters lighter hydrocarbons virtue after mutually converging with depentanizer top gas
Structure reactor.Light dydrocarbon aromatization reaction temperature is 560 DEG C, reaction pressure 0.25MPa, reaction mass air speed 1HR-1.Circulation is light
Pressure is 1.6MPa to hydrocarbon after compression, and flow is 47.5 ton hours.Second arene stream flow is 18 ton hours.The embodiment
Aromatics yield (hydrogen, methane in light hydrocarbon feedstocks and ethane as can not aromatisation component not calculate) be 57.6%.Urge
Agent regeneration period relatively example extends 23%.
【Comparative example 2】
According to the condition and step described in embodiment 1, only change in ethylene recovery unit and be not provided with ethylene rectifying column, i.e., not
The gaseous mixture of separation ethene and ethane, ethene and ethane is directly entered aromatization reactor, and circulating air is first in dethanizer
Two component of carbon is removed, avoids ethane from accumulating in systems, then loops in absorption tower.The comparative example energy consumption is higher than embodiment 1,
The mixed gas flow of ethene and ethane is smaller, and the equipment scale of ethylene rectifying column is smaller, therefore energy consumption and equipment investment are all relatively low, and
The energy consumption and scale of dethanizer are then higher, this is because caused by propane largely mixes.In addition, the flow setting of this comparative example is not
Rationally, ethylene distillation pressure tower is higher than 2MPaG, and the pressure of aromatization reaction system is less than 0.6MPaG, the pressure of dethanizer
Then it is higher than 2MPaG, therefore ethane needs to be down to low pressure from high pressure on stream, and need to rise to high pressure from low pressure, exist serious
Energy loss.
【Comparative example 3】
Flow as shown in Figure 1, light hydrocarbon feedstocks flow are 47 ton hours, and volume fraction composition is hydrogen 54%, methane 8%,
Carbon 2 12%, carbon three and the above 26%.The mass content of aromatic hydrocarbons is 4.9% in light hydrocarbon feedstocks.Absorption tower operating pressure is
1.6MPa, absorption exhaust flow are 28.6 ton hours.Absorbent dosage is 600 ton hours, absorbent stream and the first aromatic hydrocarbons
The weight ratio of logistics is 120, and wherein the mass fraction of BTX is 87%.Tail gas is absorbed after compressor is pressurized to 3.2MPa, in film
3.2 ton hour hydrogen are isolated in separator, 12.6 ton hour methane are isolated in domethanizing column, in ethylene rectifying column
Isolate 5.7 ton hour ethene and 7.1 ton hour ethane.Absorbing liquid and ethene enter light dydrocarbon aromatization reaction device.Lighter hydrocarbons virtue
Structure reaction temperature is 560 DEG C, reaction pressure 0.25MPa, reaction mass air speed 1HR-1.Pressure is circulation lighter hydrocarbons after compression
1.6MPa, flow are 47.5 ton hours.Second arene stream flow is 18 ton hours.Aromatics yield (the lighter hydrocarbons of the embodiment
Hydrogen, methane in raw material and ethane as can not aromatisation component not calculate) be 45.5%.
Claims (10)
1. a kind of method of mixed light-hydrocarbon aromatization aromatic hydrocarbons, includes the following steps：1) light hydrocarbon feedstocks are separated into absorption tower
Absorb tail gas and absorbing liquid；2) absorbing tail gas goes ethylene recovery unit to isolate ethene, hydrogen and fuel gas, and wherein ethene is gone gently
Hydrocarbon aromatizing reactor；3) absorbing liquid is separated into aromatization raw material and heavy constituent logistics in depentanizer；4) heavy constituent
Logistics is divided into two streams, one logistics returns to absorption tower as absorbent, and another burst of logistics is as the first arene stream product；
5) aromatization raw material and ethene are sent into light dydrocarbon aromatization reaction device；6) light dydrocarbon aromatization reaction product is after cooling in gas-liquid
Circulation lighter hydrocarbons and the second arene stream product are separated into separator；7) lighter hydrocarbons are circulated and returns to absorption tower..
2. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the light hydrocarbon feedstocks include
Hydrogen, methane, ethene, ethane, propylene, propane, carbon four, light dydrocarbon, benzene,toluene,xylene component.
3. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that absorbent thing in step 4)
The weight ratio 150~50 of stream and the first arene stream.
4. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the absorbent is containing BTX's
Total mass fraction is more than 80%.
5. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the absorption tower operation pressure
Power is 1.5~2.5MPA.
6. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the depentanizer operation
Pressure is 0.5~0.8MPA.
7. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that described light-hydrocarbon aromatized anti-
The condition is answered to be：500~600 DEG C, 0.1~0.6MPA of reaction pressure of reaction temperature, 0.1~3HR of reaction mass air speed-1。
8. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the circulation lighter hydrocarbons are through pressure
Contracting machine is pressurized to pressure more than after the operating pressure of absorption tower, into absorption tower.
9. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the light hydrocarbon feedstocks cooling
After being less than 10 DEG C to temperature, operated through gas-liquid separation, gas phase goes to absorption tower, and liquid phase removes depentanizer.
10. the method for mixed light-hydrocarbon aromatization aromatic hydrocarbons according to claim 1, it is characterised in that the light hydrocarbon feedstocks are through film
Absorption tower is sent into after separation removal hydrogen partial.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114436746A (en) * | 2020-11-04 | 2022-05-06 | 中国石油化工股份有限公司 | Process and system for purifying an ethylene-containing feed gas |
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|---|---|---|---|---|
| JPH04230639A (en) * | 1990-08-29 | 1992-08-19 | Inst Fr Petrole | Method for conversion of aliphatic into aromatic hydrocarbon |
| CN201280527Y (en) * | 2008-10-09 | 2009-07-29 | 山东齐旺达集团海仲化工科技有限公司 | Aromatic hydrocarbon production equipment |
| WO2010107696A1 (en) * | 2009-03-16 | 2010-09-23 | Shell Oil Company | An integrated process to coproduce aromatic hydrocarbons and ethylene and propylene |
| CN104292067A (en) * | 2013-07-16 | 2015-01-21 | 中石化洛阳工程有限公司 | Method for producing aromatic hydrocarbons by using naphtha |
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2016
- 2016-11-04 CN CN201610961622.XA patent/CN108017492B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04230639A (en) * | 1990-08-29 | 1992-08-19 | Inst Fr Petrole | Method for conversion of aliphatic into aromatic hydrocarbon |
| CN201280527Y (en) * | 2008-10-09 | 2009-07-29 | 山东齐旺达集团海仲化工科技有限公司 | Aromatic hydrocarbon production equipment |
| WO2010107696A1 (en) * | 2009-03-16 | 2010-09-23 | Shell Oil Company | An integrated process to coproduce aromatic hydrocarbons and ethylene and propylene |
| CN104292067A (en) * | 2013-07-16 | 2015-01-21 | 中石化洛阳工程有限公司 | Method for producing aromatic hydrocarbons by using naphtha |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114436746A (en) * | 2020-11-04 | 2022-05-06 | 中国石油化工股份有限公司 | Process and system for purifying an ethylene-containing feed gas |
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