CN106478335B - The method of the separation and coproduction ethylbenzene of alcohol and/or ether olefin product - Google Patents
The method of the separation and coproduction ethylbenzene of alcohol and/or ether olefin product Download PDFInfo
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Abstract
The present invention relates to a kind of alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene, mainly solve the problems, such as that energy consumption height, by-product utilize in alcohol in the prior art and/or ether olefin production process.The present invention is by using comprising the following steps: it is main reaction product that alkene is converted into alcohol and/or ether olefin hydrocarbon reactor, and reaction product obtains hydrocarbon mixture product after the concentration of product gas enrichment region；Hydrocarbon mixture product, which is sent into pre-separation tower, removes light dydrocarbon and more heavy constituent acquisition carbon four and more light component；Carbon four and more light component is sent into absorption and desorption system after being pressurized, is separated into absorption tail gas, three component of carbon, four component of carbon；It absorbs tail gas and reacts generation ethylbenzene in ethylbenzene reaction zone with external world's feeding material containing benzene；Technical solution of four component Parts of carbon as absorptive tower absorbent, preferably solves the above problem, can be used in the industrial production of alcohol and/or ether alkene.
Description
Technical field
The present invention relates to a kind of alcohol and/or the methods of ether olefin product separation and coproduction ethylbenzene.
Technical background
Ethylene, propylene are a kind of basic organic chemical industry raw materials being in great demand, by ethylene oxide, polyethylene, polypropylene,
The growth of the ethylene such as acrylonitrile, isopropylbenzene, propylene oxide, acryloyl derivative demand, corresponding ethylene, propylene demand also quickly increase
It is long.Traditional ethylene and propylene mostlys come from petroleum refining process, as the increasingly plaque of petroleum resources is weary, develops by coal or day
Non-oil resources prepare ethylene to right gas etc., the technology of propylene increasingly causes attention both domestic and external.It is usual by coal ethylene, propylene
Methanol, the again process route through alcohol and/or ether ethylene, propylene are produced using producing synthesis gas from coal, synthesis gas.Wherein coal system synthesizes
It is highly developed that gas and synthesis gas produce methanol technics technology.Alcohol and/or ether ethylene, propylene technology pass through years development,
Also industrialization is had been realized in, the technology represented has the S-MTO technology of Sinopec, Dalian materialization institute D-MTO technology, UOP
MTO technology, the MTP technology of Lurgi, the S-MTP technology of Sinopec etc..But since alcohol and/or ether ethylene, propylene produce
Object complicated composition, product include the component even more heavy to carbon nine of carbon one, and generally existing separating technology long flow path, plant energy consumption are high
The problem of.The energy consumption of alcohol and/or ether ethylene, propylene technique is how reduced, the product separation method of low energy consumption is especially developed,
As the project for needing primary study.
The separation of conventional hydrocarbon-based product generallys use rectifying separation.Typical separation process includes the sequence separation of front-end demethanization
Process, front-end deethanization separation process and predepropanization separation process.Such as in CN1431982A patent, alcohol and/or ether system third
For alkene reaction product after cooling and isolating hydro carbons and water, gas phase hydrocarbon isolates carbon two and lighter through front-end deethanization process first
Then component and carbon three and more heavy constituent are isolated three component of carbon and carbon four containing propylene in depropanizing tower and are more recombinated
Point, since carbon alkadienes and four C_5 olefins of carbon can be further converted to propylene in alcohol and/or ether propylene reactor,
The return of the carbon two and more light component that obtain from dethanizer and the carbon four obtained from depropanizing tower and more heavy constituent part is pure and mild/
Or ether propylene reactor.Traditional hydrocarbon product separation method is due to using distillation operation or to be high pressure improve essence
It evaporates the operation temperature of tower or is therefore the problem that generally existing energy consumption is high using cryogenic coolant.
United States Patent (USP) US5326929 proposes a kind of solvent absorption separation hydrogen, the method for two component of methane and carbon.But
This method regenerated solvent under the pressure greater than 3.2MPa, causes regeneration temperature very high, up to 150 DEG C, needs again after solvent reclamation
Cooling down is wanted, it is huge so as to cause the process energy consumption.
Chinese patent CN101353286 proposes a kind of non-copious cooling lower carbon number hydrocarbons separation method containing light gas.This method
Feed gas is boosted to 2.0 to 4.0MPa by compressor first, then by precut tower separation most of two groups of carbon
Point and methane separation, then with the carbon two carried secretly in solvent absorption methane in absorption tower.Due to most of carbon two and whole
Carbon three and more heavy constituent are cut out in pre-separation tower, the decline of the gas-phase feed load on absorption tower, under absorbent dosage is also corresponding
Drop, therefore, the patent claim the energy consumption of this method than existing oily absorption and separation technology low energy consumption.But contain when in feed gas
When carbon six and more heavy constituent, this method leads to a large amount of carbon six since carbon six and more heavy constituent are not cut out from absorbent
And more heavy constituent recycles in absorption and desorption system, so that energy consumption will increase dramatically, absorption efficiency decline absorbs in resolution system
Tower tower diameter increase, thus but also investment also increase accordingly.And in alcohol and/or ether olefin process, reaction product
In contain a certain amount of carbon six and more heavy constituent, therefore inevitably have using this method that energy consumption is high, investment is increased lacks
Point.
Since the prior art has that plant energy consumption height, by-product utilize, the present invention is targetedly solved
State problem.
Summary of the invention
The technical problem to be solved by the present invention is to which the problem of plant energy consumption is high, by-product utilizes exists in the prior art, mention
For a kind of alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene.This method is for alcohol and/or ether olefin product
Have the advantages that low energy consumption, good economy performance, by-product are using abundant when separation.
To solve the above problems, The technical solution adopted by the invention is as follows: a kind of alcohol and/or ether olefin product separation and
The method of coproduction ethylbenzene, comprises the following steps: alcohol and/or ether olefin hydrocarbon reactor export to obtain hydrocarbon mixture product, hydrocarbon mixture
Class product is sent into pre-separation tower and is separated into light dydrocarbon and more heavy constituent and carbon four and more light component；Carbon four and more light component are through being pressurized
After be sent into absorption and desorption system, be separated into absorb tail gas, three component of carbon, four component of carbon；Tail gas is absorbed as ethylbenzene reaction zone
One charging.
In above-mentioned technical proposal, the pre-separation tower operating pressure is 0.1~1.2MPa, and bottom temperature is 68~171 DEG C.
In above-mentioned technical proposal, pressure is 1.0~2.0MPa after the carbon four and the pressurization of more light component.
In above-mentioned technical proposal, the absorption and desorption system includes absorption tower, desorber and depropanizing tower.
In above-mentioned technical proposal, the depropanization tower reactor obtains four component of carbon, and four component of carbon is at least partly as absorption
The absorbent of tower.
In above-mentioned technical proposal, the absorption tail gas is sent into material containing benzene with the external world and reacts generation second in ethylbenzene reaction zone
Benzene.
In above-mentioned technical proposal, the absorption tower operating pressure is 1.0~1.6MPa, and operation temperature is 30~60 DEG C, is inhaled
Receive 1.0~3.0 times that agent dosage is absorption tower gas-phase feed mass flow.
In above-mentioned technical proposal, the desorber operating pressure is 1.0~2.0MPa, and tower reactor operation temperature is 60~100
℃。
In above-mentioned technical proposal, the depropanizing tower operating pressure be 0.6~1.5MPa, tower reactor operation temperature be 70~
110℃。
In above-mentioned technical proposal, in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent
For greater than 2.2%.
In above-mentioned technical proposal, in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent
For greater than 4.1%.
In above-mentioned technical proposal, the alcohol and/or ether are methanol and/or dimethyl ether；Preferred alcohol and/or ether are first
Alcohol.
In above-mentioned technical proposal, the separation method of a kind of alcohol and/or ether olefin product comprises the following steps methanol
Being converted into alkene in the reactor is main reaction product, and reaction product obtains hydrocarbon mixture after the concentration of product gas enrichment region and produces
Object, hydrocarbon mixture object are separated into low pressure carbon four and more light component and light dydrocarbon and more heavy constituent in pre-separation tower；Carbon four and lighter
Component is sent into desorber after pressurization；Three component of carbon produces to obtain depropanizing tower charging from tower reactor in desorber, whole
Ethylene from desorber overhead extraction be absorbed tower charging；In absorption tower, since from the four component conduct of carbon of depropanization tower reactor
Absorbent absorbs the propylene in charging, and absorbing liquid returns to desorber；It absorbs tail gas and is reacted with external world's feeding material containing benzene in ethylbenzene
Area's reaction generates ethylbenzene, and by-product is preferably utilized；Depropanizing tower charging is separated into three component of carbon and four groups of carbon by depropanizing tower
Point；Three component of carbon can further isolate polymerization-grade propylene product and propane in propylene rectification tower；Partial four component of carbon
Absorption tower is sent into after absorbent cooler is cooling as absorbent, rest part is discharged as four component of outlet carbon.
In above-mentioned technical proposal, when the operating pressure of the pre-separation tower is higher than the pressure of hydrocarbon mixture product, using increasing
Pressure equipment is sent into pre-separation tower hydrocarbon mixture product booster to after being higher than the operating pressure.
The present invention has broken the intrinsic thinking of those skilled in the art, is not readily conceivable that using those skilled in the art
By removing light dydrocarbon and more heavy constituent in absorption and desorption system, and be utilized in hydrocarbon mixture product and enter absorption and desorption system
The method that light dydrocarbon and more heavy constituent are directly therefrom removed before system avoids the carbon six and more heavy constituent from accumulating, to cause to inhale with this
The phenomenon that rate of producing effects decline, energy consumption will increase dramatically.Using method of the invention, hydrocarbon mixture product removes in pre-separation tower
Light dydrocarbon and more heavy constituent, avoid the accumulation and circulation of carbon six and more heavy constituent in absorption and desorption system, reduce desorption
The temperature of tower reactor and depropanization tower reactor, to reduce process energy consumption；On the other hand due to having lacked the tired of carbon six and more heavy constituent
Product and circulation, so that absorption and desorption system tower diameter also accordingly reduces, to also save equipment investment expense.
Using method of the invention, absorption and desorption system carries out at lower pressures, further reduced desorption tower reactor
With the temperature of depropanization tower reactor, process energy consumption further reduced.Absorption tower uses higher absorption temperature, operation temperature 30
~60 DEG C, it further reduced the consumption of cooling capacity.Depropanization tower reactor, which obtains four component of carbon, at least partly can be used as absorbent.It adopts
With method of the invention, the rate of recovery of propylene is 99.99%, and low energy consumption, and utilizes by-product dry gas coproduction ethylbenzene, achieve compared with
Good technical effect.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for the invention.
In Fig. 1,1 is hydrocarbon mixture product；2 be low pressure carbon four and more light component；3 be high pressure carbon four and more light component；4 are
Absorption tower charging；5 feed for depropanizing tower；6 be absorbent；7 be absorption tail gas；8 be absorbing liquid；9 be three component of carbon；10 be carbon
Four components；11 be four component of outlet carbon；12 be light dydrocarbon and more heavy constituent；T1 is pre-separation tower；101 be the stream stock containing benzene；102
Stream stock containing ethylbenzene；C1 is supercharging equipment；T2 is desorber；T3 is absorption tower；T4 is depropanizing tower；E1 is cooling for absorbent
Device；R1 is ethylbenzene reaction zone.
The process flow of Fig. 1 is as follows: alcohol and/or ether are converted into propylene for main reaction product, through product in the reactor
Hydrocarbon mixture product 1 is obtained after gas enrichment region S1 concentration.Hydrocarbon mixture logistics 1 be separated into pre-separation tower T1 low pressure carbon four and
More light component 2 and light dydrocarbon and more heavy constituent 12.Low pressure carbon four and more light component 2 obtain high pressure carbon after supercharging equipment C1 pressurization
Four and more light component 3 after be sent into desorber T2.Carbon three and component more heavy constituent produce to obtain de- third from tower reactor in desorber T2
Alkane tower charging 5, whole ethylene from desorber T2 overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since autospasy third
Four component 6 of carbon of alkane tower reactor absorbs the propylene in charging 4 as absorbent, and absorbing liquid 8 returns to desorber T2.Absorb 7 He of tail gas
Benzene-containing stream stock 101 is sent into ethylbenzene reaction zone R1 together, and the stock of stream containing ethylbenzene 102 is obtained after reaction.Depropanizing tower T4, which will be fed in 5, to be divided
Separate out four component 10 of three component 9 of carbon and carbon.Partial four component 10 of carbon is sent into absorption tower T2 after absorbent cooler E1 is cooling
Propylene is absorbed as absorbent, rest part is discharged as four component 11 of outlet carbon.
Fig. 2 is the flow diagram using four or more component of carbon as absorbent.
In Fig. 2,1 is hydrocarbon mixture product；2 feed for desorber；3 feed for absorption tower；4 feed for depropanizing tower；5 are
Carbon four and more heavy constituent；6 be absorbent；7 be absorption tail gas；8 be absorbing liquid；9 be three component of carbon；10 be outlet carbon four and heavier
Component；C1 is supercharging equipment；T1 is desorber；T2 is absorption tower；T3 is depropanizing tower；E1 is absorbent cooler.
The process flow of Fig. 2 is as follows: alcohol and/or ether are converted into propylene in the reactor as main reaction product, be dehydrated,
Gas phase hydrocarbon mixture product 1 is obtained after oxygenatedchemicals and carbon dioxide.Gas phase hydrocarbon logistics 1 through supercharging equipment C1 pressurization after,
It is sent into desorber T1.In desorber T1 tower reactor extraction depropanizing tower charging 4, whole ethylene is obtained from desorber T1 overhead extraction
Absorption tower charging 3.In the T2 of absorption tower, since from the part carbon four of depropanization tower reactor and more heavy constituent 5 through absorbent cooler
Absorption tower T2 is sent into as absorbent as absorbent 6 after E1 is cooling and absorbs propylene, and absorbing liquid 8 returns to desorber T1.Absorb tail
Absorption and desorption system is discharged in gas 7.Depropanizing tower T3 charging 4 is separated into three component 9 of carbon and carbon four and heavier in depropanizing tower T3
Component 5.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
Using process of the present invention, by taking the methanol or/and dimethyl ether olefin hydrocarbon apparatus of 300,000/year propylene as an example,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, is dehydrated and is obtained after sour gas carbon dioxide
Obtain gas phase hydrocarbon material flow 1.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.10MPa.Gas phase hydrocarbon logistics 1 is in pre-separation tower
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into T1.Low pressure carbon four and more light component 2 pass through compressor
C1 is pressurized to after 1.3MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.70% mass fraction in desorber
Three component of carbon produces to obtain depropanizing tower charging 5 from tower reactor, and whole ethylene is absorbed tower charging 4 from overhead extraction.It is inhaling
Receive in tower T3, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorbing liquid 8, which returns, to be solved
Inhale tower T2.It absorbs tail gas 7 and benzene-containing stream stock 101 is sent into ethylbenzene reaction zone R1 together, the stock of stream containing ethylbenzene 102 is obtained after reaction.It is de-
Propane tower T4 will feed in 5 and isolate four component 10 of three component 9 of carbon and carbon.Three component 9 of carbon is divided in subsequent propylene rectification tower
Separate out polymerization-grade propylene product and propane.Four component 10 of carbon of 88% mass fraction is after absorbent cooler E1 is cooled to 40 DEG C
Absorption tower is sent into as absorbent, rest part is discharged as four light dydrocarbon component 11 of outlet carbon.The process flow propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.In table energy consumption be compressor, pump, heat exchanger, rectifying column energy consumption summation.
[embodiment 2]
Using process of the present invention, by taking the methanol or/and dimethyl ether olefin hydrocarbon apparatus of 300,000/year propylene as an example,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, is dehydrated and is obtained after sour gas carbon dioxide
Obtain gas phase hydrocarbon material flow 1.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.12MPa.Gas phase hydrocarbon logistics 1 is in pre-separation tower
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into T1.Low pressure carbon four and more light component 2 pass through compressor
C1 is pressurized to after 1.6MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.72% mass fraction in desorber
Three component of carbon produces to obtain depropanizing tower charging 5 from tower reactor, and whole ethylene is absorbed tower charging 4 from overhead extraction.It is inhaling
Receive in tower T3, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorbing liquid 8, which returns, to be solved
Inhale tower T2.It absorbs tail gas 7 and benzene-containing stream stock 101 is sent into ethylbenzene reaction zone R1 together, the stock of stream containing ethylbenzene 102 is obtained after reaction.It is de-
Propane tower T4 will feed in 5 and isolate four component 10 of three component 9 of carbon and carbon.Three component 9 of carbon is divided in subsequent propylene rectification tower
Separate out polymerization-grade propylene product and propane.Four component 10 of carbon of 90% mass fraction is after absorbent cooler E1 is cooled to 40 DEG C
Absorption tower is sent into as absorbent, rest part is discharged as four light dydrocarbon component 11 of outlet carbon.The process flow propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.In table energy consumption be compressor, pump, heat exchanger, rectifying column energy consumption summation.
[embodiment 3]
Using process of the present invention, by taking the methanol or/and dimethyl ether olefin hydrocarbon apparatus of 300,000/year propylene as an example,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, is dehydrated and is obtained after sour gas carbon dioxide
Obtain gas phase hydrocarbon material flow 1.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.14MPa.Gas phase hydrocarbon logistics 1 is in pre-separation tower
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into T1.Low pressure carbon four and more light component 2 pass through compressor
C1 is pressurized to after 1.8MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.73% mass fraction in desorber
Three component of carbon produces to obtain depropanizing tower charging 5 from tower reactor, and whole ethylene is absorbed tower charging 4 from overhead extraction.It is inhaling
Receive in tower T3, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorbing liquid 8, which returns, to be solved
Inhale tower T2.It absorbs tail gas 7 and benzene-containing stream stock 101 is sent into ethylbenzene reaction zone R1 together, the stock of stream containing ethylbenzene 102 is obtained after reaction.It is de-
Propane tower T4 will feed in 5 and isolate four component 10 of three component 9 of carbon and carbon.Three component 9 of carbon is divided in subsequent propylene rectification tower
Separate out polymerization-grade propylene product and propane.Four component 10 of carbon of 92% mass fraction is after absorbent cooler E1 is cooled to 40 DEG C
Absorption tower is sent into as absorbent, rest part is discharged as four light dydrocarbon component 11 of outlet carbon.The process flow propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.In table energy consumption be compressor, pump, heat exchanger, rectifying column energy consumption summation.
[embodiment 4]
Using process of the present invention, by taking the methanol or/and dimethyl ether olefin hydrocarbon apparatus of 300,000/year propylene as an example,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, is dehydrated and is obtained after sour gas carbon dioxide
Obtain gas phase hydrocarbon material flow 1.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.16MPa.Gas phase hydrocarbon logistics 1 is in pre-separation tower
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into T1.Low pressure carbon four and more light component 2 pass through compressor
C1 is pressurized to after 2.0MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.74% mass fraction in desorber
Three component of carbon produces to obtain depropanizing tower charging 5 from tower reactor, and whole ethylene is absorbed tower charging 4 from overhead extraction.It is inhaling
Receive in tower T3, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorbing liquid 8, which returns, to be solved
Inhale tower T2.It absorbs tail gas 7 and benzene-containing stream stock 101 is sent into ethylbenzene reaction zone R1 together, the stock of stream containing ethylbenzene 102 is obtained after reaction.It is de-
Propane tower T4 will feed in 5 and isolate four component 10 of three component 9 of carbon and carbon.Three component 9 of carbon is divided in subsequent propylene rectification tower
Separate out polymerization-grade propylene product and propane.Four component 10 of carbon of 94% mass fraction is after absorbent cooler E1 is cooled to 40 DEG C
Absorption tower is sent into as absorbent, rest part is discharged as four light dydrocarbon component 11 of outlet carbon.The process flow propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.In table energy consumption be compressor, pump, heat exchanger, rectifying column energy consumption summation.
[comparative example 1]
Fig. 2 is shown in process flow, using with the identical hydrocarbon mixture product of embodiment 1, after compressor boost to 1.6MPa,
It is sent into desorber T1.Desorber operating pressure 1.5MPa, 96 DEG C of bottom temperature.The carbon of 73.2% mass fraction in desorber T1
Three components produce to obtain depropanizing tower charging 4 from tower reactor, and whole ethylene is absorbed tower charging 3 from overhead extraction.Absorption tower
Operating pressure 1.25MPa absorbs 43 DEG C of temperature.In the T2 of absorption tower, since make from the carbon four of depropanization tower reactor and more heavy constituent 5
The propylene in charging 3 is absorbed for absorbent, absorbing liquid 8 returns to desorber T1.It absorbs tail gas 7 and absorption and desorption system is discharged.De- third
Alkane tower charging 4 is separated into three component 9 of carbon and carbon four and more heavy constituent 5, depropanizing tower operating pressure in depropanizing tower T3
1.15MPa, 81 DEG C of bottom temperature, three component 9 of carbon obtains polymerization-grade propylene product and propane through propylene rectifying.85% mass fraction
Carbon four and more heavy constituent 5 be sent into absorption tower after absorbent cooler E1 is cooling and be used as absorbent 6, rest part discharge is
System.The propylene recovery rate 98.2% of the process flow, energy consumption is shown in Table 1.
[comparative example 2]
Fig. 2 is shown in process flow, using with the identical hydrocarbon mixture product of embodiment 1, after compressor boost to 1.4MPa,
It is sent into desorber T1.Desorber operating pressure 1.3MPa, 74 DEG C of bottom temperature.The carbon of 71.2% mass fraction in desorber T1
Three components produce to obtain depropanizing tower charging 4 from tower reactor, and whole ethylene is absorbed tower charging 3 from overhead extraction.Absorption tower
Operating pressure 1.45MPa absorbs 44 DEG C of temperature.In the T2 of absorption tower, since make from the carbon four of depropanization tower reactor and more heavy constituent 5
The propylene in charging 3 is absorbed for absorbent, absorbing liquid 8 returns to desorber T1.It absorbs tail gas 7 and absorption and desorption system is discharged.De- third
Alkane tower charging 4 is separated into three component 9 of carbon and carbon four and more heavy constituent 5, depropanizing tower operating pressure in depropanizing tower T3
0.9MPa, 86 DEG C of bottom temperature, three component 9 of carbon obtains polymerization-grade propylene product and propane through propylene rectifying.80% mass fraction
Carbon four and more heavy constituent 5 be sent into absorption tower after absorbent cooler E1 is cooling and be used as absorbent 6, rest part discharge is
System.The propylene recovery rate 98.4% of the process flow, energy consumption is shown in Table 1.
Table 1
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Comparative example 1 | Comparative example 2 | |
| Pre-separation tower operating pressure | 0.11 | 0.55 | 0.8 | 1.2 | - | - |
| Pre-separation tower top operation temperature | -13 | 21 | 41 | 56 | - | - |
| Pre-separation tower reactor operation temperature | 72 | 103 | 144 | 167 | - | - |
| Absorptive tower absorbent dosage | 2.01 | 2.85 | 2.55 | 1.24 | 2.23 | 2.58 |
| Absorption tower operating pressure | 1.05 | 1.25 | 1.35 | 1.55 | 1.25 | 1.45 |
| Absorb tower reactor operation temperature | 35 | 43 | 47 | 58 | 43 | 44 |
| Desorber operating pressure | 1.25 | 1.55 | 1.75 | 1.95 | 1.5 | 1.3 |
| Desorb tower reactor operation temperature | 63 | 78 | 86 | 95 | 96 | 74 |
| Depropanizing tower operating pressure | 0.6 | 1.1 | 1.2 | 1.5 | 1.15 | 0.9 |
| Depropanization tower top operation temperature | 6 | 23.3 | 27 | 47 | 25 | 16 |
| Depropanization tower reactor operation temperature | 73 | 92 | 97 | 109 | 81 | 86 |
| Energy consumption (kg marks oil/kg propylene) | 0.168 | 0.172 | 0.180 | 0.182 | 0.226 | 0.231 |
Claims (10)
1. a kind of alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene, comprise the following steps: alcohol and/or ether alkene
Hydrocarbon reactor exports to obtain hydrocarbon mixture product, hydrocarbon mixture product be sent into pre-separation tower be separated into light dydrocarbon and more heavy constituent and
Carbon four and more light component；Carbon four and more light component is sent into absorption and desorption system after being pressurized is separated into and absorbs tail gas, three groups of carbon
Divide, four component of carbon；Absorb one charging of tail gas as ethylbenzene reaction zone；The alcohol and/or ether are methanol and/or dimethyl ether；
The alkene includes ethylene and/or propylene.
2. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 1, it is characterised in that described
Pre-separation tower operating pressure is 0.1~1.2MPa, and bottom temperature is 68~171 DEG C.
3. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 1, it is characterised in that described
Pressure is 1.0~2.0MPa after carbon four and the pressurization of more light component.
4. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 1, it is characterised in that described
Absorption and desorption system includes absorption tower, desorber and depropanizing tower.
5. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 4, it is characterised in that from institute
It states depropanization tower reactor and obtains four component of carbon, absorbent of four component of carbon at least partly as absorption tower.
6. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 1, it is characterised in that from institute
It states absorption tail gas and reacts generation ethylbenzene in ethylbenzene reaction zone with external world's feeding material containing benzene.
7. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 4, it is characterised in that described
Absorption tower operating pressure is 1.0~1.6MPa, and operation temperature is 30~60 DEG C, and absorbent dosage is absorption tower gas-phase feed quality
1.0~3.0 times of flow.
8. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 4, it is characterised in that described
Depropanizing tower operating pressure is 0.6~1.5MPa, and tower reactor operation temperature is 70~110 DEG C.
9. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 1, it is characterised in that described
In hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent is greater than 2.2%.
10. alcohol and/or the method for ether olefin product separation and coproduction ethylbenzene according to claim 9, it is characterised in that institute
It states in hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent is preferably greater than 4.1%.
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| WO2000053548A1 (en) * | 1999-03-09 | 2000-09-14 | Bp Chemicals Limited | Process for the production of olefins |
| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
| CN103880577A (en) * | 2014-03-20 | 2014-06-25 | 中国石油集团东北炼化工程有限公司吉林设计院 | Reaction product separation system for production of propylene and olefins by using methanol |
| CN203794811U (en) * | 2014-03-20 | 2014-08-27 | 中国石油集团东北炼化工程有限公司吉林设计院 | Reaction product separation system for methanol-to-propylene and methanol-to-olefin |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000053548A1 (en) * | 1999-03-09 | 2000-09-14 | Bp Chemicals Limited | Process for the production of olefins |
| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
| CN103880577A (en) * | 2014-03-20 | 2014-06-25 | 中国石油集团东北炼化工程有限公司吉林设计院 | Reaction product separation system for production of propylene and olefins by using methanol |
| CN203794811U (en) * | 2014-03-20 | 2014-08-27 | 中国石油集团东北炼化工程有限公司吉林设计院 | Reaction product separation system for methanol-to-propylene and methanol-to-olefin |
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