CN106478336A - The separation of alcohol and/or ether olefin product and the method for by-product process - Google Patents
The separation of alcohol and/or ether olefin product and the method for by-product process Download PDFInfo
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Abstract
The present invention relates to a kind of method that alcohol and/or ether olefin product separate and by-product is processed, mainly solves the problems, such as in prior art high energy consumption, by-product utilization in alcohol and/or ether olefin production process.The present invention passes through using comprising the steps of：Alcohol and/or ether are converted into alkene in the reactor for main product, and product obtains hydrocarbon mixture product after the concentration of product gas enrichment region；Hydrocarbon mixture product is sent in pre-separation tower and is separated into carbon six and more heavy constituent and carbon five and more light component；Send into absorption and desorption system after carbon five and more light component are intensified, be separated into absorption tail gas, carbon three component, carbon four carbon five component；Absorb tail gas as one charging of ethylbenzene reaction zone；Carbon four carbon five component at least partly returns alcohol and/or the technical scheme of ether olefin hydrocarbon reactor, 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 a kind of alcohol and/or ether olefin product separate the method processing with by-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.
Due to prior art all there is a problem of plant energy consumption high, by-product utilize, the present invention targetedly solves above-mentioned
Problem, makes full use of by-product.
Content of the invention
The technical problem to be solved is that there is a problem of in prior art that plant energy consumption height, by-product utilize, and provides one
Plant alcohol and/or ether olefin product separates the method processing with by-product.The method is used for the separation of alcohol and/or ether olefin product
When have that energy consumption is low, good economy performance, by-product utilize sufficient advantage.
For solving the above problems, the technical solution used in the present invention is as follows：A kind of alcohol and/or ether olefin product separate and by-product
The method processing, comprises the steps of：Alcohol and/or ether are converted into alkene in the reactor for main product, product
Hydrocarbon mixture product is obtained through product gas enrichment region after concentrating；Hydrocarbon mixture product is sent into and is separated into carbon six and more in pre-separation tower
Heavy constituent and carbon carbon five and more light component；Send into absorption and desorption system after carbon five and more light component are intensified, be separated into absorption tail
Gas, carbon three component, carbon four carbon five component；Absorb tail gas as one charging of ethylbenzene reaction zone；Carbon four carbon five component is at least
Part returns alcohol and/or ether olefin hydrocarbon reactor.
In technique scheme, described pre-separation tower operating pressure is 0.1～1.2MPa, and bottom temperature is 80～202 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 carbon five component, this carbon four carbon five component at least partly as
The absorbent on absorption tower.
In technique scheme, described absorption tail gas reacts generation ethylbenzene with extraneous feeding material containing benzene in ethylbenzene reaction zone.
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 six and more heavy constituent is big
In 2.0%.
In technique scheme, in described hydrocarbon mixture product by weight percentage, the content of carbon six and more heavy constituent is big
In 4.1%.
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-
Answering and being converted into propylene in device is main product, obtains hydrocarbon mixture and produce after dehydration, oxygenatedchemicalss and carbon dioxide
Thing, hydrocarbon mixture thing is separated into low pressure carbon five and more light component and carbon six and more heavy constituent in pre-separation tower；Carbon five and more
Light component sends into desorber after supercharging；In desorber, carbon three component obtains depropanizing tower charging from tower reactor extraction, entirely
The ethylene in portion from desorber overhead extraction be absorbed tower charging；In absorption tower, since from carbon four carbon of depropanization tower reactor
Five components absorb the propylene in charging as absorbent, and absorbing liquid returns desorber；Absorb tail gas and send into thing containing benzene with extraneous
Material reacts in ethylbenzene reaction zone and generates ethylbenzene, preferably make use of by-product；Depropanizing tower charging is separated into carbon by depropanizing tower
Three components and carbon four carbon five component；Carbon three component can isolate in propylene rectification tower further polymerization-grade propylene product and
Propane；Absorption tower is sent into as absorbent, at least part of carbon after the five groups of lease making absorbent cooler coolings of partial carbon four carbon
Four carbon five component returns alcohol and/or ether olefin hydrocarbon reactor, and remainder is discharged as outer row's carbon four carbon five 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 five and more light component；3 is high pressure carbon five 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 carbon five component；11 is absorbent；12 is outer row's carbon four carbon five component；13 recombinate for carbon six and more
Point；101 is methanol charging；102 is carbon four component returning；103 is preparing propylene from methanol product；104 is waste water；
105 is the stream stock containing benzene；106 stream stocks containing ethylbenzene；R1 is preparing propylene from methanol reactor；R2 is ethylbenzene reaction zone；
S1 is product gas enrichment region；T1 is pre-separation tower；C1 is supercharging equipment；T2 is desorber；T3 is absorption tower；T4
For 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 producing in reactor R1
Product gas enrichment region S1 obtains hydrocarbon mixture product 1 after concentrating.Hydrocarbon mixture logistics 1 is separated into low pressure in pre-separation tower T1
Carbon five and more light component 2 and carbon six and more heavy constituent 12.Low pressure carbon five and more light component 2 are after supercharging equipment C1 supercharging
Desorber T2 is sent into after obtaining high pressure carbon five and more light component 3.In desorber T2, carbon three and component more heavy constituent are from tower reactor
Extraction obtains depropanizing tower charging 5, and whole ethylene is absorbed tower charging 4 from desorber T2 overhead extraction.On absorption tower
In T3, since absorb propylene in charging 4, absorbing liquid 8 as absorbent from carbon four carbon five component 6 of depropanization tower reactor
Return desorber T2.Absorb tail gas 7 and send into ethylbenzene reaction zone R1 together with benzene-containing stream stock 101, obtain containing ethylbenzene after reaction
Stream stock 102.Depropanizing tower T4 will isolate carbon three component 9 and carbon four carbon five component 10 in charging 5.Partial carbon four carbon
Five components 10 are sent into absorption tower T2 after absorbent cooler E1 cooling and are absorbed propylene, the carbon of part as absorbent 11
Four carbon five component 102 is back to alcohol and/or ether in reactor R1, and remainder is discharged as outer row's carbon four carbon five component 12.
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
Alcohol and/or ether olefin hydrocarbon reactor R1 are converted into propylene be main product, through product gas enrichment region S1 dehydration and
Gas phase hydrocarbon logistics 1 is obtained after sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.10MPa.
Gas phase hydrocarbon logistics 1 is separated into low pressure carbon five and more light component 2 and carbon six and more heavy constituent 12 in pre-separation tower T1.Low
Pressure carbon five and more light component 2 are pressurized to after 1.3MPa obtains high pressure carbon five and more light component 3 through compressor C1 and send into desorbing
Tower T2.In desorber, carbon three component of 70% mass fraction obtains depropanizing tower charging 5, whole ethylene from tower reactor extraction
From overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since make from carbon four carbon five component 6 of depropanization tower reactor
Absorb the propylene in charging 4 for absorbent, absorbing liquid 8 returns desorber T2.Absorb tail gas 7 and benzene-containing stream stock 101 1
Rise and send into ethylbenzene reaction zone R1, after reaction, obtain the stock of stream containing ethylbenzene 102.Depropanizing tower T4 will isolate carbon three in charging 5
Component 9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and third in follow-up propylene rectification tower
Alkane.Carbon four carbon five component 103 of 50% mass fraction is returned to reactor R1 volume increase alkene, carbon four carbon five component Parts warp
Absorbent cooler E1 sends into absorption tower as absorbent after being cooled to 40 DEG C, and remainder is as outer row's carbon four carbon five component
11 discharges.This technological process propylene enhancing 15.2%, 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
Alcohol and/or ether olefin hydrocarbon reactor R1 are converted into propylene be main product, through product gas enrichment region S1 dehydration and
Gas phase hydrocarbon logistics 1 is obtained after sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.12MPa.
Gas phase hydrocarbon logistics 1 is separated into low pressure carbon five and more light component 2 and carbon six and more heavy constituent 12 in pre-separation tower T1.Low
Pressure carbon five and more light component 2 are pressurized to after 1.6MPa obtains high pressure carbon five and more light component 3 through compressor C1 and send into desorbing
Tower T2.In desorber, carbon three component of 72% mass fraction obtains depropanizing tower charging 5, whole ethylene from tower reactor extraction
From overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since make from carbon four carbon five component 6 of depropanization tower reactor
Absorb the propylene in charging 4 for absorbent, absorbing liquid 8 returns desorber T2.Absorb tail gas 7 and benzene-containing stream stock 101 1
Rise and send into ethylbenzene reaction zone R1, after reaction, obtain the stock of stream containing ethylbenzene 102.Depropanizing tower T4 will isolate carbon three in charging 5
Component 9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and third in follow-up propylene rectification tower
Alkane.Carbon four carbon five component 102 of 60% mass fraction is returned to reactor R1 volume increase alkene, carbon four carbon five component Parts warp
Absorbent cooler E1 sends into absorption tower as absorbent after being cooled to 40 DEG C, and remainder is as outer row's carbon four carbon five component
11 discharges.This technological process propylene enhancing 17.2%, 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
Alcohol and/or ether olefin hydrocarbon reactor R1 are converted into propylene be main product, through product gas enrichment region S1 dehydration and
Gas phase hydrocarbon logistics 1 is obtained after sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.14MPa.
Gas phase hydrocarbon logistics 1 is separated into low pressure carbon five and more light component 2 and carbon six and more heavy constituent 12 in pre-separation tower T1.Low
Pressure carbon five and more light component 2 are pressurized to after 1.8MPa obtains high pressure carbon five and more light component 3 through compressor C1 and send into desorbing
Tower T2.In desorber, carbon three component of 73% mass fraction obtains depropanizing tower charging 5, whole ethylene from tower reactor extraction
From overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since make from carbon four carbon five component 6 of depropanization tower reactor
Absorb the propylene in charging 4 for absorbent, absorbing liquid 8 returns desorber T2.Absorb tail gas 7 and benzene-containing stream stock 101 1
Rise and send into ethylbenzene reaction zone R1, after reaction, obtain the stock of stream containing ethylbenzene 102.Depropanizing tower T4 will isolate carbon three in charging 5
Component 9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and third in follow-up propylene rectification tower
Alkane.Carbon four carbon five component 102 of 70% mass fraction is returned to reactor R1 volume increase alkene, carbon four carbon five component Parts warp
Absorbent cooler E1 sends into absorption tower as absorbent after being cooled to 40 DEG C, and remainder is as outer row's carbon four carbon five component
11 discharges.This technological process propylene enhancing 19.2%, 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
Alcohol and/or ether olefin hydrocarbon reactor R1 are converted into propylene be main product, through product gas enrichment region S1 dehydration and
Gas phase hydrocarbon logistics 1 is obtained after sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.16MPa.
Gas phase hydrocarbon logistics 1 is separated into low pressure carbon five and more light component 2 and carbon six and more heavy constituent 12 in pre-separation tower T1.Low
Pressure carbon five and more light component 2 are pressurized to after 2.0MPa obtains high pressure carbon five and more light component 3 through compressor C1 and send into desorbing
Tower T2.In desorber, carbon three component of 74% mass fraction obtains depropanizing tower charging 5, whole ethylene from tower reactor extraction
From overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since make from carbon four carbon five component 6 of depropanization tower reactor
Absorb the propylene in charging 4 for absorbent, absorbing liquid 8 returns desorber T2.Absorb tail gas 7 and benzene-containing stream stock 101 1
Rise and send into ethylbenzene reaction zone R1, after reaction, obtain the stock of stream containing ethylbenzene 102.Depropanizing tower T4 will isolate carbon three in charging 5
Component 9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and third in follow-up propylene rectification tower
Alkane.Carbon four carbon five component 102 of 70% mass fraction is returned to reactor R1 volume increase alkene, carbon four carbon five component Parts warp
Absorbent cooler E1 sends into absorption tower as absorbent after being cooled to 40 DEG C, and remainder is as outer row's carbon four carbon five component
11 discharges.This technological process propylene enhancing 20.2%, 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 | -8 | 26 | 45 | 59 | - | - |
| Pre-separation tower reactor operation temperature | 80 | 113 | 164 | 187 | - | - |
| Absorptive tower absorbent consumption | 2.11 | 2.94 | 2.75 | 1.44 | 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 | 40 | 45 | 49 | 60 | 43 | 44 |
| Desorber operating pressure | 1.25 | 1.55 | 1.75 | 1.95 | 1.5 | 1.3 |
| Desorbing tower reactor operation temperature | 65 | 82 | 88 | 98 | 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) | 0.179 | 0.192 | 0.189 | 0.178 | 0.226 | 0.231 |
Claims (10)
1. a kind of alcohol and/or ether olefin product separate the method processing with by-product, comprise the steps of：Alcohol and/or ether are anti-
Answering and being converted into alkene in device is main product, and product obtains hydrocarbon mixture product after the concentration of product gas enrichment region；
Hydrocarbon mixture product is sent in pre-separation tower and is separated into carbon six and more heavy constituent and carbon five and more light component；Carbon five and more light component
Send into absorption and desorption system after intensified, be separated into absorption tail gas, carbon three component, carbon four carbon five component；Absorb tail gas conduct
One charging of ethylbenzene reaction zone；Carbon four carbon five component at least partly returns alcohol and/or ether olefin hydrocarbon reactor.
2. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method is it is characterised in that institute
Stating pre-separation tower operating pressure is 0.1～1.2MPa, and bottom temperature is 80～202 DEG C.
3. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method is it is characterised in that institute
State carbon four and more light component supercharging after pressure be 1.0～2.0MPa.
4. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method it is characterised in that from
Described depropanization tower reactor obtains carbon four carbon five component, and this carbon four carbon five component is at least partly as the absorbent on absorption tower.
5. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method it is characterised in that from
Described absorption tail gas reacts generation ethylbenzene with extraneous feeding material containing benzene in ethylbenzene reaction zone.
6. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method is it is characterised in that institute
Stating absorption tower operating pressure is 1.0～1.6MPa, and operation temperature is 30～60 DEG C, and absorbent consumption is absorption tower gas-phase feed matter
1.0～3.0 times of amount flow.
7. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method is it is characterised in that institute
Stating desorber operating pressure is 1.0～2.0MPa, and tower reactor operation temperature is 60～100 DEG C.
8. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method is it is characterised in that institute
Stating depropanizing tower operating pressure is 0.6～1.5MPa, and tower reactor operation temperature is 70～110 DEG C.
9. alcohol and/or ether olefin product separate and by-product is processed according to claim 1 method is it is characterised in that institute
State in hydrocarbon mixture product by weight percentage, the content of carbon five and more heavy constituent is more than 2.0%.
10. alcohol and/or ether olefin product separate and by-product is processed according to claim 9 method is it is characterised in that institute
State in hydrocarbon mixture product by weight percentage, the content of carbon five and more heavy constituent is preferably greater than 4.1%.
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Citations (4)
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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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