CN106478347B - Alcohol and/or the separation of ether olefin product and the method for increasing production alkene using by-product - Google Patents
Alcohol and/or the separation of ether olefin product and the method for increasing production alkene using by-product Download PDFInfo
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Abstract
A kind of method for increasing production alkene the present invention relates to alcohol and/or the separation of ether olefin product and using by-product mainly solves the problems, such as that high energy consumption in alcohol in the prior art and/or ether olefin production process, by-product utilize.The present invention is by using comprising the following steps：It is main reaction product that alcohol and/or ether are converted into alkene in the reactor, and reaction product obtains hydrocarbon mixture product after the concentration of product gas enrichment region；Hydrocarbon mixture 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 is sent into absorption and desorption system after supercharging is separated into and absorbs tail gas, three component of carbon, four component of carbon；Four component of carbon at least partly returns to the technical solution of alcohol and/or ether olefin hydrocarbon reactor volume increase alkene, preferably solves the above problem, can be used in the industrial production of alcohol and/or ether alkene at least partly as the absorbent on absorption tower.
Description
Technical field
Increase production the method for alkene the present invention relates to a kind of alcohol and/or the separation of ether olefin product and using by-product.
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, weary with the increasingly plaque of petroleum resources, 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 technologies of Sinopec, Dalian materialization institute D-MTO technologies, UOP
MTO technologies, the MTP technologies of Lurgi, S-MTP technologies of Sinopec etc..But due to alcohol and/or ether ethylene, propylene production
Object composition is complicated, and product includes carbon one to the even more heavy component of carbon nine, 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 needing the project of primary study.
The separation of conventional hydrocarbon-based product generally uses rectifying to detach.Typical separation process includes the sequence separation of front-end demethanization
Flow, front-end deethanization separation process and predepropanization separation process.Such as in CN1431982A patents, 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 first through front-end deethanization flow
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 carbon two obtained from dethanizer and more light component and the carbon four obtained from depropanizing tower and the return alcohol of more heavy constituent part and/
Or ether propylene reactor.Traditional hydrocarbon product separation method is as a result of distillation operation or to be high pressure improve essence
It evaporates the operation temperature of tower or is to use cryogenic coolant, therefore the problem of generally existing high energy consumption.
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 more than 3.2MPa, causes regeneration temperature very high, up to 150 DEG C, is needed 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, and the gas-phase feed load on absorption tower declines, under absorbent dosage is also corresponding
Drop, therefore, which claims the energy consumption of this method, and 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 can be significantly increased, and absorption efficiency declines, and absorb in resolution system
Tower tower diameter increase, to but also investment is also corresponding increases.And in alcohol and/or ether olefin process, reaction product
In contain a certain amount of carbon six and more heavy constituent, therefore using this method inevitably have high energy consumption, investment it is increased lack
Point.
Since the prior art has that plant energy consumption height, by-product utilize, the present invention targetedly solves
State problem.
Invention content
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, carry
Increase production the method for alkene for a kind of new alcohol and/or the separation of ether olefin product and using by-product.This method is used for alcohol and/or ether
Have the advantages that low energy consumption, good economy performance, olefin yields are high when olefin product processed separation.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of alcohol and/or the separation of ether olefin product and
The method for being increased production alkene using by-product, is comprised the following steps：Alcohol and/or ether are converted into alkene and are produced for key reaction in the reactor
Object, reaction product obtain hydrocarbon mixture product after the concentration of product gas enrichment region；Hydrocarbon mixture product, which is sent into pre-separation tower, to be divided
From for 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 supercharging, point
From for absorb tail gas, three component of carbon, four component of carbon；Four component of carbon is at least partly returned at least partly as the absorbent on absorption tower
Return alcohol and/or ether olefin hydrocarbon reactor.
In above-mentioned technical proposal, one kind in the product gas enrichment region removing water, oxygenatedchemicals, carbon dioxide is several
Or all.
In above-mentioned technical proposal, the pre-separation tower operating pressure is 0.1~1.2MPa, and bottom temperature is 68~170 DEG C.
In above-mentioned technical proposal, pressure is 1.0~2.0MPa after the carbon four and the supercharging 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 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
To be more 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
To be more than 4.2%.
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, a kind of alcohol and/or the separation of ether olefin product and the side using by-product volume increase alkene
Method, it is main reaction product to comprise the following steps that methanol is converted into propylene in the reactor, and reaction product is through product gas enrichment region
Hydrocarbon mixture product is obtained after concentration；Hydrocarbon mixture object be separated into pre-separation tower low pressure carbon four and more light component and light dydrocarbon and
More heavy constituent；Carbon four and more light component is sent into desorber after supercharging；Three component of carbon produces to obtain from tower reactor in desorber
Depropanizing tower feed, whole ethylene from desorber overhead extraction be absorbed tower charging；In absorption tower, since from depropanization
Four component of carbon of tower reactor absorbs the propylene in charging as absorbent, and absorbing liquid returns to desorber；It absorbs tail gas discharge and absorbs solution
Desorption system；Depropanizing tower charging is separated into four component of three component of carbon and carbon by depropanizing tower；Three component of carbon can be further third
Polymerization-grade propylene product and propane are isolated in alkene rectifying column；It is sent into and inhales after partial four groups of lease making absorbent cooler coolings of carbon
Tower is received as absorbent, carbon four component in part is back to alcohol and/or ether olefin hydrocarbon reactor volume increase alkene, especially increasing output of ethylene
And propylene, remaining four component Parts of carbon are discharged as outer four component of row's 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
Equipment is pressed to be sent into pre-separation tower hydrocarbon mixture product booster to higher than after 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 declines, and energy consumption can be significantly increased.Method using the present invention, hydrocarbon mixture product remove in pre-separation tower
Light dydrocarbon and more heavy constituent, avoid the accumulation and cycle 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 cycle so that absorption and desorption system tower diameter also accordingly reduces, to also save equipment investment expense.
Method using the present invention, absorption and desorption system carry 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 cold.Depropanization tower reactor, which obtains four component of carbon, can at least partly be used as absorbent.It adopts
The rate of recovery with the method for the present invention, propylene is 99.99%, and low energy consumption, and utilizes the four component increasing output of ethylene of carbon of by-product, third
Alkene, ethylene, propene yield greatly improve, and achieve preferable technique effect.
Description of the drawings
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 is fed；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 outer four component of row's carbon；12 be light dydrocarbon and more heavy constituent；101 feed for methanol；102 be four component of carbon returned；
103 be methanol to propylene reaction product；104 be waste water；R1 is methanol to propylene reaction device；S1 is product gas enrichment region；T1 is
Pre-separation tower；C1 is supercharging equipment；T2 is desorber；T3 is absorption tower；T4 is depropanizing tower；E1 is absorbent cooler.
As shown in Figure 1, it is main reaction product that methanol is converted into alkene in methanol to propylene reaction device R1, through product gas
Obtain hydrocarbon mixture product 1 after enrichment region S1 concentration, hydrocarbon mixture logistics 1 is separated into low pressure carbon four and more in pre-separation tower T1
Light component 2 and light dydrocarbon and more heavy constituent 12.Low pressure carbon four and more light component 2 obtain high pressure carbon four after supercharging equipment C1 superchargings
And desorber T2 is sent into after more light component 3.Carbon three and component more heavy constituent produce to obtain depropanization from tower reactor in desorber T2
Tower T4 charging 5, whole ethylene are absorbed tower charging 4 from desorber T2 overhead extractions.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 tail gas part
Absorption and desorption system is discharged.Depropanizing tower T4 isolates four component 10 of three component 9 of carbon and carbon in feeding 5.Four groups of partial carbon
It is sent into absorption tower T2 after the E1 coolings of lease making absorbent cooler and absorbs propylene as absorbent 6, four component 102 of carbon of part returns
To alcohol and/or ether propylene reactor increasing output of ethylene, propylene, four component of rest part carbon is discharged as four component 11 of outer row's 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 outer row's 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 technological process of Fig. 2 is as follows：It is main reaction product that alcohol and/or ether are converted into propylene in the reactor, through being dehydrated,
Gas phase hydrocarbon mixture product 1 is obtained after oxygenatedchemicals and carbon dioxide.Gas phase hydrocarbon logistics 1 after supercharging equipment C1 supercharging,
It is sent into desorber T1.In desorber T1 tower reactors extraction depropanizing tower charging 4, whole ethylene is obtained from desorber T1 overhead extractions
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 being sent into as absorbent 6 after E1 coolings and absorbing propylene as absorbent, 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 implementation mode
【Embodiment 1】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.10MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 1.3MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 70% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates carbon in feeding 5
Four light dydrocarbon component 10 of three components 9 and carbon.Three component 9 of carbon isolates polymerization-grade propylene product and third in subsequent propylene rectification tower
Alkane.Four component 102 of carbon of 50% mass fraction is returned to reactor R1 volume increase alkene, and four component Parts of carbon are through absorbent cooler
E1 is sent into absorption tower as absorbent after being cooled to 40 DEG C, rest part is discharged as four light dydrocarbon component 11 of outer row's carbon.The technique
Flow increasing output of ethylene, propylene 10.2%, 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.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Embodiment 2】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.12MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 1.6MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 72% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates carbon in feeding 5
Four light dydrocarbon component 10 of three components 9 and carbon.Three component 9 of carbon isolates polymerization-grade propylene product and third in subsequent propylene rectification tower
Alkane.Four component 102 of carbon of 60% mass fraction is returned to reactor R1 volume increase alkene, and four component Parts of carbon are through absorbent cooler
E1 is sent into absorption tower as absorbent after being cooled to 40 DEG C, rest part is discharged as four light dydrocarbon component 11 of outer row's carbon.The technique
Flow increasing output of ethylene, propylene 12.2%, 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.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Embodiment 3】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.14MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 1.8MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 73% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates carbon in feeding 5
Four light dydrocarbon component 10 of three components 9 and carbon.Three component 9 of carbon isolates polymerization-grade propylene product and third in subsequent propylene rectification tower
Alkane.Four component 102 of carbon of 70% mass fraction is returned to reactor R1 volume increase alkene, and four component Parts of carbon are through absorbent cooler
E1 is sent into absorption tower as absorbent after being cooled to 40 DEG C, rest part is discharged as four light dydrocarbon component 11 of outer row's carbon.The technique
Flow increasing output of ethylene, propylene 14.2%, 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.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Embodiment 4】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.16MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 2.0MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 74% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates carbon in feeding 5
Four light dydrocarbon component 10 of three components 9 and carbon.Three component 9 of carbon isolates polymerization-grade propylene product and third in subsequent propylene rectification tower
Alkane.Four component 102 of carbon of 80% mass fraction is returned to reactor R1 volume increase alkene, and four component Parts of carbon are through absorbent cooler
E1 is sent into absorption tower as absorbent after being cooled to 40 DEG C, rest part is discharged as four light dydrocarbon component 11 of outer row's carbon.The technique
Flow increasing output of ethylene, propylene 16.2%, 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.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Comparative example 1】
Fig. 2 is shown in technological process, using with 1 identical hydrocarbon mixture product of embodiment, after compressor is pressurized 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 obtain 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 cooling and be used as the absorbent 6, rest part discharge to be
System.The propylene recovery rate 98.2% of the technological process, energy consumption is shown in Table 1.
【Comparative example 2】
Fig. 2 is shown in technological process, using with 1 identical hydrocarbon mixture product of embodiment, after compressor is pressurized 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 obtain 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 cooling and be used as the absorbent 6, rest part discharge to be
System.The propylene recovery rate 98.4% of the technological process, 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) | 0.169 | 0.175 | 0.181 | 0.184 | 0.226 | 0.231 |
Claims (10)
1. a kind of alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene, comprise the following steps：Alcohol and/
Or it is main reaction product that ether is converted into alkene in the reactor, reaction product obtains hydrocarbon mixture after the concentration of product gas enrichment region
Class product；Hydrocarbon mixture 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 is sent into absorption and desorption system after supercharging, is separated into and absorbs tail gas, three component of carbon, four component of carbon；Four component of carbon is extremely
Absorbent of the small part as absorption tower at least partly returns to alcohol and/or ether olefin hydrocarbon reactor；Wherein, the alcohol and/or ether
For methanol and/or dimethyl ether.
2. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is that one kind in product gas enrichment region removing water, oxygenatedchemicals, carbon dioxide is several or whole.
3. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is that the pre-separation tower operating pressure is 0.1~1.2MPa, bottom temperature is 68~170 DEG C.
4. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
Pressure is 1.0~2.0MPa after being the carbon four and the supercharging of more light component.
5. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is to obtain four component of carbon from the depropanization tower reactor, absorbent of four component of carbon at least partly as absorption tower.
6. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is that the absorption tower operating pressure is 1.0~1.6MPa, operation temperature is 30~60 DEG C, and absorbent dosage is absorption tower gas phase
1.0~3.0 times of feedstock quality flow.
7. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is that the desorber operating pressure is 1.0~2.0MPa, tower reactor operation temperature is 60~100 DEG C.
8. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is that the depropanizing tower operating pressure is 0.6~1.5MPa, tower reactor operation temperature is 70~110 DEG C.
9. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 1, feature
It is in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent is more than 2.2%.
10. alcohol and/or the separation of ether olefin product and the method using by-product volume increase alkene according to claim 9, special
Sign is in the hydrocarbon mixture product that by weight percentage, the content of light dydrocarbon and more heavy constituent is preferably greater than 4.2%.
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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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2015
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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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