CN106478333A - Alcohol and/or the separation method of ether olefin product - Google Patents
Alcohol and/or the separation method of ether olefin product Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The present invention relates to the separation method of a kind of alcohol and/or ether olefin product, mainly solve the problems, such as in prior art high energy consumption in alcohol and/or ether olefin production process.The present invention comprises the steps of：After alcohol and/or ether olefin hydrocarbon reactor outlets products removing water, oxygenatedchemicalss and carbon dioxide, obtain hydrocarbon mixture product；Hydrocarbon mixture product is sent into removing carbon five and more heavy constituent in pre-separation tower and is obtained carbon four and more light component；Send into absorption and desorption system after carbon four and more light component are intensified, be separated into absorption tail gas, carbon three component, the technical scheme of carbon four component preferably solves the problems referred to above, can be used in alcohol and/or the commercial production of ether alkene.
Description
Technical field
The present invention relates to the separation method of a kind of alcohol and/or ether olefin product.
Technical background
Ethylene, propylene are a kind of basic organic chemical industry raw materials being in great demand, by oxirane, polyethylene, polypropylene,
The ethylene such as acrylonitrile, isopropylbenzene, expoxy propane, the growth of acryloyl derivative demand, corresponding ethylene, propylene demand also fast
Speed increases.Traditional ethylene and propylene mostly come from petroleum refining process, and the increasingly plaque with petroleum resources is weary, development by
The non-oil resource such as coal or natural gas prepares ethylene, the technology of propylene increasingly causes attention both domestic and external.By coal ethylene,
Propylene generally produces methanol, the again process route through alcohol and/or ether ethylene, propylene using producing synthesis gas from coal, synthesis gas.Its
It is highly developed that middle producing synthesis gas from coal and synthesis gas produce methanol technics technology.Alcohol and/or ether ethylene, propylene technology are passed through
Years development, also has been realized in industrialization, and the technology that it represents has the S-MTO technology of Sinopec, Dalian materialization institute
D-MTO technology, the MTO technology of UOP, the MTP technology of Lurgi, S-MTP technology of Sinopec etc..But
Because alcohol and/or ether ethylene, propylene product composition are complicated, product includes carbon one to the even more heavy component of carbon nine, generally deposits
In the high problem of separating technology long flow path, plant energy consumption.How to reduce alcohol and/or the energy consumption of ether ethylene, propylene technique, especially
It is the product separation method of exploitation low energy consumption, becomes the problem needing primary study.
Conventional hydrocarbon-based product separates commonly used rectification and separates.Typical separation process include front-end demethanization order separation process,
Front-end deethanization separation process and predepropanization separation process.For example in CN1431982A patent, alcohol and/or ether propylene
After cooling and isolating hydro carbons and water, gas phase hydrocarbon isolates carbon two and lighter group through front-end deethanization flow process to product first
Divide and carbon three and more heavy constituent, in depropanizing tower, then isolate carbon three component containing propylene and carbon four and more heavy constituent,
Because carbon alkadienes and carbon four C_5 olefins can be further converted to propylene in alcohol and/or ether propylene reactor, from de-
Carbon two and the return alcohol of more light component and the carbon four obtaining from depropanizing tower and more heavy constituent part and/or ether that ethane tower obtains
Propylene reactor processed.Traditional hydrocarbon product separation method, due to employing distillation operation, to improve rectifying column or being high pressure
Operation temperature, or being to adopt cryogenic coolant, the therefore problem of generally existing high energy consumption.
A kind of method that United States Patent (USP) US5326929 proposes solvent absorption separation hydrogen, methane and carbon two component.But should
Method regenerated solvent under the pressure more than 3.2MPa, leads to regeneration temperature very high, up to 150 DEG C, after solvent reclamation again
Need cooling down, thus leading to this process energy consumption huge.
Chinese patent CN101353286 proposes a kind of non-copious cooling lower carbon number hydrocarbons separation method containing light gas.The method is first
First feed gas are boosted to 2.0 to 4.0MPa by compressor, then pass through precut tower and separate most of two groups of carbon
Divide and methane separation, the then carbon two with carrying secretly in solvent absorption methane in absorption tower.Due to most of carbon two and whole
Carbon three and more heavy constituent cut out in pre-separation tower, and the gas-phase feed load on absorption tower declines, under absorbent consumption is also corresponding
Fall, therefore, this patent claims the energy consumption of the observable index of the method existing oil absorption and separation technology low.But work as and contain in feed gas
When having carbon six and more heavy constituent, the method, due to carbon six and more heavy constituent not being cut out from absorbent, leads to substantial amounts of carbon
Six and more heavy constituent circulates in absorption and desorption system so that energy consumption can be significantly increased, absorption efficiency declines, and absorbs parsing system
Tower tower diameter in system increases, thus also making investment also accordingly increase.And in alcohol and/or ether olefin process, reaction
Contain a certain amount of carbon six and more heavy constituent in product, therefore high energy consumption is inevitably had using the method, investment increases
Shortcoming.
Because prior art all has the high problem of plant energy consumption, the present invention targetedly solves the problems referred to above.
Content of the invention
The technical problem to be solved is that there is a problem of in prior art that plant energy consumption is high, provide a kind of new alcohol and
/ or ether olefin product separation method.The method is used for during the separation of alcohol and/or ether olefin product having that energy consumption is low, skill
The advantage of art good economy performance.
For solving the above problems, the technical solution used in the present invention is as follows：A kind of alcohol and/or the separation method of ether olefin product,
Comprise the steps of：Alcohol and/or the outlet of ether olefin hydrocarbon reactor obtain hydrocarbon mixture product, and hydrocarbon mixture product sends into pre-separation
It is separated into carbon five and more heavy constituent and carbon four and more light component in tower；Absorption and desorption system is sent into after carbon four and more light component are intensified
System, is separated into absorption tail gas, carbon three component, carbon four component.
In technique scheme, described pre-separation tower operating pressure is 0.1～1.2MPa, and bottom temperature is 70～170 DEG C.
In technique scheme, after described carbon four and the supercharging of more light component, pressure is 1.0～2.0MPa.
In technique scheme, described absorption and desorption system comprises absorption tower, desorber and depropanizing tower.
In technique scheme, described depropanization tower reactor obtains carbon four component, and this carbon four component is at least partly as absorption tower
Absorbent.
In technique scheme, described absorption tower operating pressure is 1.0～1.6MPa, and operation temperature is 30～60 DEG C, absorbent
Consumption is 1.0～3.0 times of absorption tower gas-phase feed mass flow.
In technique scheme, described desorber operating pressure is 1.0～2.0MPa, and tower reactor operation temperature is 60～100 DEG C.
In technique scheme, described depropanizing tower operating pressure is 0.6～1.5MPa, and tower reactor operation temperature is 70～110 DEG C.
In technique scheme, in described hydrocarbon mixture product by weight percentage, the content of carbon five and more heavy constituent is big
In 2.0%.
In technique scheme, in described hydrocarbon mixture product by weight percentage, the content of carbon five and more heavy constituent is big
In 4.0%.
In technique scheme, described alcohol and/or ether are methanol and/or dimethyl ether；Preferred alcohol and/or ether are methanol.
In technique scheme, the separation method of a kind of described alcohol and/or ether olefin product, comprise the steps of methanol anti-
Answer and in device, be converted into ethylene, propylene is main product, obtains mixing after dehydration, oxygenatedchemicalss and carbon dioxide
Hydrocarbon product, hydrocarbon mixture thing is separated into low pressure carbon four and more light component and carbon five and more heavy constituent in pre-separation tower；Carbon
Four and more light component through supercharging after send into desorber；In desorber, carbon three component obtains depropanizing tower and enters from tower reactor extraction
Material, whole ethylene is absorbed tower charging from desorber overhead extraction；In absorption tower, since from depropanization tower reactor
Part carbon four component absorbs the propylene in charging as absorbent, and absorbing liquid returns desorber；Absorb tail gas and discharge and absorb solution
Desorption system；Depropanizing tower charging is separated into carbon three component and carbon four component by depropanizing tower；Carbon three component can exist further
Polymerization-grade propylene product and propane is isolated in propylene rectification tower；Send after the four groups of lease making absorbent cooler coolings of partial carbon
Enter absorption tower as absorbent, remainder is discharged as outer row's carbon four component.
In technique scheme, when the operating pressure of described pre-separation tower is higher than the pressure of hydrocarbon mixture product, set using supercharging
Send in pre-separation tower to higher than after this operating pressure for hydrocarbon mixture product booster.
The present invention has broken the intrinsic thinking of those skilled in the art, and do not adopt that those skilled in the art are readily conceivable that is logical
Cross removing carbon five and more heavy constituent in absorption and desorption system, and before being utilized in hydrocarbon mixture product entrance absorption and desorption system
The method directly therefrom removing carbon five and more heavy constituent, to avoid carbon six and the accumulation of more heavy constituent with this, thus causing to absorb effect
Rate declines, the phenomenon that energy consumption can be significantly increased.Using the method for the present invention, hydrocarbon mixture product is stripped of in pre-separation tower
Carbon five and more heavy constituent, it is to avoid the accumulation in absorption and desorption system of carbon six and more heavy constituent and circulation, reduce desorber
Kettle and the temperature of depropanization tower reactor, thus reduce process energy consumption；On the other hand due to having lacked the accumulation of carbon six and more heavy constituent
With circulation so that absorption and desorption system tower diameter also accordingly reduces, thus also saving equipment investment expense.
Using the method for the present invention, absorption and desorption system is carried out at lower pressures, reduce further desorbing tower reactor and takes off
The temperature of propane tower reactor, reduce further process energy consumption.Using higher absorption temperature, operation temperature is 30～60 on absorption tower
DEG C, reduce further the consumption of cold.Depropanization tower reactor obtains carbon four component at least partly can be used as absorbent.Using
The method of the present invention, the response rate of propylene is 99.99%, and energy consumption is low, achieves preferable technique effect.
Brief description
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is hydrocarbon mixture product；2 is low pressure carbon four and more light component；3 is high pressure carbon four and more light component；
4 is absorption tower charging；5 is depropanizing tower charging；6 is absorbent；7 is to absorb tail gas；8 is absorbing liquid；9 is carbon three
Component；10 is carbon four component；11 is outer row's carbon four component；12 is carbon five and more heavy constituent；T1 is pre-separation tower；C1
For supercharging equipment；T2 is desorber；T3 is absorption tower；T4 is depropanizing tower；E1 is absorbent cooler.
The technological process of Fig. 1 is as follows：Alcohol and/or ether are converted into propylene for main product, through de- in reactor R1
Hydrocarbon mixture product 1 is obtained after water, oxygenatedchemicalss and carbon dioxide.Hydrocarbon mixture logistics 1 divides in pre-separation tower T1
From for low pressure carbon four and more light component 2 and carbon five and more heavy constituent 12.Low pressure carbon four and more light component 2 are through supercharging equipment
Desorber T2 is sent into after obtaining high pressure carbon four and more light component 3 after C1 supercharging.In desorber T2, carbon three and component are heavier
Component obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene is absorbed tower charging 4 from desorber T2 overhead extraction.
In the T3 of absorption tower, since absorb propylene in charging 4 as absorbent from carbon four component 6 of depropanization tower reactor, absorb
Liquid 8 returns desorber T2.Absorb tail gas 7 and discharge absorption and desorption system.Depropanizing tower T4 will isolate carbon three in charging 5
Component 9 and carbon four component 10.Partial carbon four component 10 is sent into absorption tower T2 after absorbent cooler E1 cooling and is made
Absorb propylene for absorbent, remainder is discharged as outer row's carbon four component 11.
Fig. 2 is the schematic flow sheet using carbon more than four component as absorbent.
In Fig. 2,1 is hydrocarbon mixture product；2 is desorber charging；3 is absorption tower charging；4 is depropanizing tower charging；
5 is carbon four and more heavy constituent；6 is absorbent；7 is to absorb tail gas；8 is absorbing liquid；9 is carbon three component；10 is outer
Row's carbon four and more heavy constituent；C1 is supercharging equipment；T1 is desorber；T2 is absorption tower；T3 is depropanizing tower；E1
For absorbent cooler.
The technological process of Fig. 2 is as follows：Alcohol and/or ether are converted into propylene in the reactor for main product, through being dehydrated,
Gas phase hydrocarbon mixture product 1 is obtained after oxygenatedchemicalss and carbon dioxide.The intensified equipment C1 of gas phase hydrocarbon logistics 1 is pressurized
Afterwards, send into desorber T1.In desorber T1 tower reactor extraction depropanizing tower charging 4, whole ethylene is from desorber T1 tower
Top extraction be absorbed tower charging 3.In the T2 of absorption tower, since from the part carbon four of depropanization tower reactor and more heavy constituent 5
Send into absorption tower T2 as absorbent 6 after absorbent cooler E1 cooling and absorb propylene, absorbing liquid 8 as absorbent
Return desorber T1.Absorb tail gas 7 and discharge absorption and desorption system.Depropanizing tower T3 charging 4 divides in depropanizing tower T3
From for carbon three component 9 and carbon four and more heavy constituent 5.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus as a example, methanol
Being converted into propylene in alcohol and/or ether olefin hydrocarbon reactor R1 is main product, through dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon logistics 1 afterwards.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.10MPa.Gas phase hydrocarbon logistics 1
It is separated into low pressure carbon four and more light component 2 and carbon five and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and lighter group
Divide 2 to be pressurized to after 1.3MPa obtains high pressure carbon four and more light component 3 through compressor C1 and send into desorber T2.In desorbing
In tower, carbon three component of 70% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene obtains from overhead extraction
Feed 4 to absorption tower.In the T3 of absorption tower, since absorb charging 4 from carbon four component 6 of depropanization tower reactor as absorbent
In propylene, absorbing liquid 8 return desorber T2.Absorb tail gas 7 and discharge absorption and desorption system.Depropanizing tower T4 will feed
Carbon three component 9 and carbon four carbon five component 10 is isolated in 5.Carbon three component 9 isolates polymerization in follow-up propylene rectification tower
Level propylene product and propane.Carbon four component 10 of 88% mass fraction is cooled to through absorbent cooler E1 to send into after 40 DEG C inhales
Receive tower as absorbent, remainder is discharged as outer row's carbon four carbon five component 11.This technological process propylene recovery rate 99.99%.
The operating condition of each tower and system energy consumption are shown in Table 1.In table, absorptive tower absorbent consumption is the mass flow of absorbent 6
Ratio with the mass flow of absorption tower charging 4.In table, energy consumption is compressor, pump, heat exchanger, the summation of rectifying column energy consumption.
【Embodiment 2】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus as a example, methanol
Being converted into propylene in alcohol and/or ether olefin hydrocarbon reactor R1 is main product, through dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon logistics 1 afterwards.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.12MPa.Gas phase hydrocarbon logistics 1
It is separated into low pressure carbon four and more light component 2 and carbon five and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and lighter group
Divide 2 to be pressurized to after 1.6MPa obtains high pressure carbon four and more light component 3 through compressor C1 and send into desorber T2.In desorbing
In tower, carbon three component of 72% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene obtains from overhead extraction
Feed 4 to absorption tower.In the T3 of absorption tower, since absorb charging 4 from carbon four component 6 of depropanization tower reactor as absorbent
In propylene, absorbing liquid 8 return desorber T2.Absorb tail gas 7 and discharge absorption and desorption system.Depropanizing tower T4 will feed
Carbon three component 9 and carbon four carbon five component 10 is isolated in 5.Carbon three component 9 isolates polymerization in follow-up propylene rectification tower
Level propylene product and propane.Carbon four component 10 of 90% mass fraction is cooled to through absorbent cooler E1 to send into after 40 DEG C inhales
Receive tower as absorbent, remainder is discharged as outer row's carbon four carbon five component 11.This technological process propylene recovery rate 99.99%.
The operating condition of each tower and system energy consumption are shown in Table 1.In table, absorptive tower absorbent consumption is the mass flow of absorbent 6
Ratio with the mass flow of absorption tower charging 4.In table, energy consumption is compressor, pump, heat exchanger, the summation of rectifying column energy consumption.
【Embodiment 3】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus as a example, methanol
Being converted into propylene in alcohol and/or ether olefin hydrocarbon reactor R1 is main product, through dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon logistics 1 afterwards.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.14MPa.Gas phase hydrocarbon logistics 1
It is separated into low pressure carbon four and more light component 2 and carbon five and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and lighter group
Divide 2 to be pressurized to after 1.8MPa obtains high pressure carbon four and more light component 3 through compressor C1 and send into desorber T2.In desorbing
In tower, carbon three component of 73% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene obtains from overhead extraction
Feed 4 to absorption tower.In the T3 of absorption tower, since absorb charging 4 from carbon four component 6 of depropanization tower reactor as absorbent
In propylene, absorbing liquid 8 return desorber T2.Absorb tail gas 7 and discharge absorption and desorption system.Depropanizing tower T4 will feed
Carbon three component 9 and carbon four carbon five component 10 is isolated in 5.Carbon three component 9 isolates polymerization in follow-up propylene rectification tower
Level propylene product and propane.Carbon four component 10 of 92% mass fraction is cooled to through absorbent cooler E1 to send into after 40 DEG C inhales
Receive tower as absorbent, remainder is discharged as outer row's carbon four carbon five component 11.This technological process propylene recovery rate 99.99%.
The operating condition of each tower and system energy consumption are shown in Table 1.In table, absorptive tower absorbent consumption is the mass flow of absorbent 6
Ratio with the mass flow of absorption tower charging 4.In table, energy consumption is compressor, pump, heat exchanger, the summation of rectifying column energy consumption.
【Embodiment 4】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus as a example, methanol
Being converted into propylene in alcohol and/or ether olefin hydrocarbon reactor R1 is main product, through dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon logistics 1 afterwards.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.16MPa.Gas phase hydrocarbon logistics 1
It is separated into low pressure carbon four and more light component 2 and carbon five and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and lighter group
Divide 2 to be pressurized to after 2.0MPa obtains high pressure carbon four and more light component 3 through compressor C1 and send into desorber T2.In desorbing
In tower, carbon three component of 74% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene obtains from overhead extraction
Feed 4 to absorption tower.In the T3 of absorption tower, since absorb charging 4 from carbon four component 6 of depropanization tower reactor as absorbent
In propylene, absorbing liquid 8 return desorber T2.Absorb tail gas 7 and discharge absorption and desorption system.Depropanizing tower T4 will feed
Carbon three component 9 and carbon four carbon five component 10 is isolated in 5.Carbon three component 9 isolates polymerization in follow-up propylene rectification tower
Level propylene product and propane.Carbon four component 10 of 94% mass fraction is cooled to through absorbent cooler E1 to send into after 40 DEG C inhales
Receive tower as absorbent, remainder is discharged as outer row's carbon four carbon five component 11.This technological process propylene recovery rate 99.99%.
The operating condition of each tower and system energy consumption are shown in Table 1.In table, absorptive tower absorbent consumption is the mass flow of absorbent 6
Ratio with the mass flow of absorption tower charging 4.In table, energy consumption is compressor, pump, heat exchanger, the summation of rectifying column energy consumption.
【Comparative example 1】
Fig. 2 is shown in technological process, adopts and embodiment 1 identical hydrocarbon mixture product, is pressurized to through compressor after 1.6MPa,
Send into desorber T1.Desorber operating pressure 1.5MPa, 96 DEG C of bottom temperature.In desorber T1,73.2% mass is divided
Carbon three component of number obtains depropanizing tower charging 4 from tower reactor extraction, 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 from the carbon four of depropanization tower reactor and
More heavy constituent 5 absorbs the propylene in charging 3 as absorbent, and absorbing liquid 8 returns desorber T1.Absorb tail gas 7 to discharge
Absorption and desorption system.Depropanizing tower charging 4 is separated into carbon three component 9 and carbon four and more heavy constituent 5 in depropanizing tower T3,
Depropanizing tower operating pressure 1.15MPa, 81 DEG C of bottom temperature, carbon three component 9 obtains polymerization-grade propylene through propylene rectification and produces
Product and propane.The carbon four of 85% mass fraction and more heavy constituent 5 send into absorption tower conduct after absorbent cooler E1 cooling
Absorbent 6, remainder discharge system.The propylene recovery rate 98.2% of this technological process, energy consumption is shown in Table 1.
【Comparative example 2】
Fig. 2 is shown in technological process, adopts and embodiment 1 identical hydrocarbon mixture product, is pressurized to through compressor after 1.4MPa,
Send into desorber T1.Desorber operating pressure 1.3MPa, 74 DEG C of bottom temperature.In desorber T1,71.2% mass is divided
Carbon three component of number obtains depropanizing tower charging 4 from tower reactor extraction, 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 from the carbon four of depropanization tower reactor and
More heavy constituent 5 absorbs the propylene in charging 3 as absorbent, and absorbing liquid 8 returns desorber T1.Absorb tail gas 7 to discharge
Absorption and desorption system.Depropanizing tower charging 4 is separated into carbon three component 9 and carbon four and more heavy constituent 5 in depropanizing tower T3,
Depropanizing tower operating pressure 0.9MPa, 86 DEG C of bottom temperature, carbon three component 9 obtains polymerization-grade propylene product through propylene rectification
And propane.The carbon four of 80% mass fraction and more heavy constituent 5 send into absorption tower as suction after absorbent cooler E1 cooling
Receive agent 6, remainder discharge system.The propylene recovery rate 98.4% of this 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 consumption | 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 |
| Desorbing 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 steps of：Alcohol and/or ether olefin hydrocarbon reactor go out
Mouth obtains hydrocarbon mixture product, and hydrocarbon mixture product is sent into and is separated into carbon five and more heavy constituent and carbon four and lighter in pre-separation tower
Component；Send into absorption and desorption system after carbon four and more light component are intensified, be separated into absorption tail gas, carbon three component, four groups of carbon
Point.
2. according to claim 1 the separation method of alcohol and/or ether olefin product it is characterised in that described pre-separation tower
Operating pressure is 0.1～1.2MPa, and bottom temperature is 70～170 DEG C.
3. according to claim 1 the separation method of alcohol and/or ether olefin product it is characterised in that described carbon four and more
After light component supercharging, pressure is 1.0～2.0MPa.
4. according to claim 1 the separation method of alcohol and/or ether olefin product it is characterised in that described absorption and desorption
System comprises absorption tower, desorber and depropanizing tower.
5. according to claim 1 the separation method of alcohol and/or ether olefin product it is characterised in that from described depropanization
Tower reactor obtains carbon four component, and this carbon four component is at least partly as the absorbent on absorption tower.
6. according to claim 1 alcohol and/or ether olefin product separation method it is characterised in that described absorption tower behaviour
Making pressure is 1.0～1.6MPa, and operation temperature is 30～60 DEG C, and absorbent consumption is absorption tower gas-phase feed mass flow
1.0～3.0 times.
7. according to claim 1 alcohol and/or ether olefin product separation method it is characterised in that described desorber behaviour
Making pressure is 1.0～2.0MPa, and tower reactor operation temperature is 60～100 DEG C.
8. according to claims 1 separation method of alcohol and/or ether olefin product it is characterised in that described de- third
Alkane tower operating pressure is 0.6～1.5MPa, and tower reactor operation temperature is 70～110 DEG C.
9. according to claim 1 the separation method of alcohol and/or ether olefin product it is characterised in that described hydrocarbon mixture
In product by weight percentage, the content of carbon five and more heavy constituent is more than 2.0%.
10. according to claim 9 the separation method of alcohol and/or ether olefin product it is characterised in that described hydrocarbon mixture
In product by weight percentage, the content of carbon five and more heavy constituent is preferably greater than 4.0%.
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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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