CN106478333B - The separation method of alcohol and/or ether olefin product - Google Patents
The separation method of alcohol and/or ether olefin product Download PDFInfo
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- CN106478333B CN106478333B CN201510537500.3A CN201510537500A CN106478333B CN 106478333 B CN106478333 B CN 106478333B CN 201510537500 A CN201510537500 A CN 201510537500A CN 106478333 B CN106478333 B CN 106478333B
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Abstract
The present invention relates to a kind of alcohol and/or the separation methods of ether olefin product, mainly solve the problems, such as high energy consumption in alcohol in the prior art and/or ether olefin production process.The present invention comprises the following steps：After alcohol and/or ether olefin hydrocarbon reactor outlets products removing water, oxygenatedchemicals and carbon dioxide, hydrocarbon mixture product is obtained；Hydrocarbon mixture product is sent into removing light dydrocarbon and more heavy constituent in pre-separation tower and obtains carbon four and more light component；Carbon four and more light component is sent into absorption and desorption system after supercharging, is separated into absorption tail gas, the technical solution of three component of carbon, four component of carbon 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 separation methods of ether olefin 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 the high problem of plant energy consumption, the present invention targetedly solves the above problem.
Invention content
The technical problem to be solved by the present invention is to which the high problem of plant energy consumption exists in the prior art, provide a kind of new
The separation method of alcohol and/or ether olefin product.There is energy consumption when separation of this method for alcohol and/or ether olefin product
Advantage low, Technical Economy is good.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of separation of alcohol and/or ether olefin product
Method comprises the following steps：Alcohol and/or ether olefin hydrocarbon reactor export to obtain hydrocarbon mixture product, and hydrocarbon mixture product is sent into
Light dydrocarbon and more heavy constituent and carbon four and more light component are separated into pre-separation tower；Carbon four and more light component are sent into absorption after supercharging
Desorption system is separated into and absorbs tail gas, three component of carbon, four component of carbon.
In above-mentioned technical proposal, the pre-separation tower operating pressure is 0.1~1.2MPa, and bottom temperature is 70~170 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 2.0%.
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 4.0%.
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
It is converted into ethylene, propylene in the reactor as main reaction product, is mixed after dehydration, oxygenatedchemicals and carbon dioxide
Hydrocarbon product, 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 more light component is sent into desorber after supercharging；Three component of carbon produces to obtain depropanizing tower charging from tower reactor in desorber,
Whole ethylene is absorbed tower charging from desorber overhead extraction；In absorption tower, since from the part carbon of depropanization tower reactor
Four components absorb the propylene in charging as absorbent, and absorbing liquid returns to desorber；It absorbs tail gas and absorption and desorption system is discharged；It is de-
Depropanizing tower charging is separated into four component of three component of carbon and carbon by propane tower；Three component of carbon can be further in propylene rectification tower
Isolate polymerization-grade propylene product and propane；Absorption tower is sent into as suction after partial four groups of lease making absorbent cooler coolings of carbon
Agent is received, rest part is 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, achieves 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；T1 is pre-separation tower；C1 is supercharging equipment；T2 is desorption
Tower；T3 is absorption tower；T4 is depropanizing tower；E1 is absorbent cooler.
The technological process of Fig. 1 is as follows：It is main reaction product that alcohol and/or ether are converted into propylene in reactor R1, through de-
Hydrocarbon mixture product 1 is obtained after water, oxygenatedchemicals and carbon dioxide.Hydrocarbon mixture logistics 1 is 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 are after supercharging equipment C1 superchargings
It is sent into desorber T2 after obtaining high pressure carbon four and more light component 3.Carbon three and component more heavy constituent are adopted from tower reactor in desorber T2
Go out to obtain depropanizing tower charging 5, whole ethylene from desorber T2 overhead extractions be absorbed tower charging 4.In the T3 of absorption tower,
Since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorbing liquid 8 returns to desorber T2.It inhales
Absorption and desorption system is discharged in the gas 7 that finishes up.Depropanizing tower T4 isolates four component 10 of three component 9 of carbon and carbon in feeding 5.Partial
Four component 10 of carbon is sent into absorption tower T2 after the E1 coolings of absorbent cooler and absorbs propylene as absorbent, and rest part is as outer
Arrange the discharge of four component 11 of 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 alcohol and/or ether olefin hydrocarbon reactor R1, through dehydration and sour gas dioxy
Gas phase hydrocarbon logistics 1 is obtained after changing carbon.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.10MPa.Gas phase hydrocarbon logistics 1 exists
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into pre-separation tower T1.Low pressure carbon four and more light component 2 warp
Overcompression machine C1 is pressurized to after 1.3MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.70% matter in desorber
Measure three component of carbon of score and produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene from overhead extraction be absorbed tower into
Material 4.In the T3 of absorption tower, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorb
Liquid 8 returns to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates three component 9 of carbon in feeding 5
With four light dydrocarbon component 10 of carbon.Three component 9 of carbon isolates polymerization-grade propylene product and propane in subsequent propylene rectification tower.88%
Four component 10 of carbon of mass fraction is sent into absorption tower as absorbent, rest part after absorbent cooler E1 is cooled to 40 DEG C
It is discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process 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 alcohol and/or ether olefin hydrocarbon reactor R1, through dehydration and sour gas dioxy
Gas phase hydrocarbon logistics 1 is obtained after changing carbon.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.12MPa.Gas phase hydrocarbon logistics 1 exists
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into pre-separation tower T1.Low pressure carbon four and more light component 2 warp
Overcompression machine C1 is pressurized to after 1.6MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.72% matter in desorber
Measure three component of carbon of score and produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene from overhead extraction be absorbed tower into
Material 4.In the T3 of absorption tower, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorb
Liquid 8 returns to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates three component 9 of carbon in feeding 5
With four light dydrocarbon component 10 of carbon.Three component 9 of carbon isolates polymerization-grade propylene product and propane in subsequent propylene rectification tower.90%
Four component 10 of carbon of mass fraction is sent into absorption tower as absorbent, rest part after absorbent cooler E1 is cooled to 40 DEG C
It is discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process 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 alcohol and/or ether olefin hydrocarbon reactor R1, through dehydration and sour gas dioxy
Gas phase hydrocarbon logistics 1 is obtained after changing carbon.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.14MPa.Gas phase hydrocarbon logistics 1 exists
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into pre-separation tower T1.Low pressure carbon four and more light component 2 warp
Overcompression machine C1 is pressurized to after 1.8MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.73% matter in desorber
Measure three component of carbon of score and produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene from overhead extraction be absorbed tower into
Material 4.In the T3 of absorption tower, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorb
Liquid 8 returns to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates three component 9 of carbon in feeding 5
With four light dydrocarbon component 10 of carbon.Three component 9 of carbon isolates polymerization-grade propylene product and propane in subsequent propylene rectification tower.92%
Four component 10 of carbon of mass fraction is sent into absorption tower as absorbent, rest part after absorbent cooler E1 is cooled to 40 DEG C
It is discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process 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 alcohol and/or ether olefin hydrocarbon reactor R1, through dehydration and sour gas dioxy
Gas phase hydrocarbon logistics 1 is obtained after changing carbon.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.16MPa.Gas phase hydrocarbon logistics 1 exists
Low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 are separated into pre-separation tower T1.Low pressure carbon four and more light component 2 warp
Overcompression machine C1 is pressurized to after 2.0MPa obtains high pressure carbon four and more light component 3 and is sent into desorber T2.74% matter in desorber
Measure three component of carbon of score and produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene from overhead extraction be absorbed tower into
Material 4.In the T3 of absorption tower, since from four component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorb
Liquid 8 returns to desorber T2.It absorbs tail gas 7 and absorption and desorption system is discharged.Depropanizing tower T4 isolates three component 9 of carbon in feeding 5
With four light dydrocarbon component 10 of carbon.Three component 9 of carbon isolates polymerization-grade propylene product and propane in subsequent propylene rectification tower.94%
Four component 10 of carbon of mass fraction is sent into absorption tower as absorbent, rest part after absorbent cooler E1 is cooled to 40 DEG C
It is discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process 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) | 0.165 | 0.171 | 0.178 | 0.181 | 0.226 | 0.231 |
Claims (10)
1. the separation method of a kind of alcohol and/or ether olefin product, comprises the following steps：Alcohol and/or ether olefin hydrocarbon reactor go out
Mouth obtains hydrocarbon mixture product, and hydrocarbon mixture product, which is sent into pre-separation tower, is separated into light dydrocarbon and more heavy constituent and carbon four and lighter
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；
Wherein, the alcohol is methanol, and the ether is dimethyl ether.
2. the separation method of alcohol and/or ether olefin product according to claim 1, which is characterized in that the pre-separation tower
Operating pressure is 0.1~1.2MPa, and bottom temperature is 70~170 DEG C.
3. the separation method of alcohol and/or ether olefin product according to claim 1, which is characterized in that the carbon four and more
Pressure is 1.0~2.0MPa after light component supercharging.
4. the separation method of alcohol and/or ether olefin product according to claim 1, which is characterized in that the absorption and desorption
System includes absorption tower, desorber and depropanizing tower.
5. the separation method of alcohol and/or ether olefin product according to claim 4, which is characterized in that from the depropanization
Tower reactor obtains four component of carbon, absorbent of four component of carbon at least partly as absorption tower.
6. the separation method of alcohol and/or ether olefin product according to claim 4, which is characterized in that the absorption tower behaviour
It is 1.0~1.6MPa to make pressure, and operation temperature is 30~60 DEG C, and absorbent dosage is absorption tower gas-phase feed mass flow
1.0~3.0 times.
7. the separation method of alcohol and/or ether olefin product according to claim 4, which is characterized in that the desorber behaviour
It is 1.0~2.0MPa to make pressure, and tower reactor operation temperature is 60~100 DEG C.
8. the separation method of alcohol and/or ether olefin product according to claim 4, which is characterized in that the depropanizing tower
Operating pressure is 0.6~1.5MPa, and tower reactor operation temperature is 70~110 DEG C.
9. the separation method of alcohol and/or ether olefin product according to claim 1, which is characterized in that the hydrocarbon mixture
In product by weight percentage, the content of light dydrocarbon and more heavy constituent is more than 2.0%.
10. the separation method of alcohol and/or ether olefin product according to claim 9, which is characterized in that the hydrocarbon mixture
In product by weight percentage, the content of light dydrocarbon and more heavy constituent is preferably greater than 4.0%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510537500.3A CN106478333B (en) | 2015-08-28 | 2015-08-28 | The separation method of alcohol and/or ether olefin product |
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|---|---|---|---|
| CN201510537500.3A CN106478333B (en) | 2015-08-28 | 2015-08-28 | The separation method of alcohol and/or ether olefin product |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106478333A CN106478333A (en) | 2017-03-08 |
| CN106478333B true CN106478333B (en) | 2018-10-23 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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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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