CN106478346A - Alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing - Google Patents
Alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing Download PDFInfo
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Abstract
The present invention relates to a kind of alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing, mainly solves the problems, such as in prior art high energy consumption, by-product utilization during alcohol and/or ether production of propylene.The present invention comprises the steps of：Alcohol and/or ether are converted into propylene 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 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, carbon four component；Absorb tail gas and at least partly return alcohol and/or the technical scheme of ether propylene reactor propylene enhancing, preferably solve the problems referred to above, can be used in alcohol and/or the commercial production of ether propylene.
Description
Technical field
The present invention relates to a kind of alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing.
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 that plant energy consumption height, by-product utilize, the present invention targetedly solves above-mentioned asking
Topic.
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 new alcohol and/or ether propylene product separates and the method using lighter hydrocarbons propylene enhancing.The method is used for alcohol and/or ether system third
Have the advantages that during the separation of olefinic product that energy consumption is low, good economy performance, propene yield are high.
For solving the above problems, the technical solution used in the present invention is as follows：A kind of alcohol and/or ether propylene product separate and utilize
The method of lighter hydrocarbons propylene enhancing, comprises the steps of：Alcohol and/or ether are converted into propylene in the reactor for main product,
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 five and more heavy constituent and carbon four and more light component；Send into absorption and desorption system after carbon four and more light component are intensified, be separated into
Absorb tail gas, carbon three component, carbon four component；Absorb tail gas and at least partly return alcohol and/or ether propylene reactor.
In technique scheme, one of described product gas enrichment region removing water, oxygenatedchemicalss, carbon dioxide several or
All.
In technique scheme, described pre-separation tower operating pressure is 0.1～1.2MPa, and bottom temperature is 69～171 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 2.1%.
In technique scheme, in described hydrocarbon mixture product by weight percentage, the content of carbon five 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, and product obtains hydrocarbon mixture product after the concentration of product gas enrichment region,
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 lighter group
Lease making sends into desorber after crossing supercharging；In desorber, carbon three component obtains depropanizing tower charging from tower reactor extraction, whole
Ethylene from desorber overhead extraction be absorbed tower charging；In absorption tower, since be allocated as from four groups of the carbon of depropanization tower reactor
Absorb the propylene in charging for absorbent, absorbing liquid returns desorber；Absorb tail gas part and discharge absorption and desorption system, portion
Divide and be back to alcohol and/or ether propylene reactor propylene enhancing；Depropanizing tower by depropanizing tower charging be separated into carbon three component and
Carbon four component；Carbon three component can isolate polymerization-grade propylene product and propane further in propylene rectification tower；Partial
Absorption tower is sent into as absorbent, remainder is arranged as outer row's carbon four component after four groups of lease making absorbent cooler coolings of carbon
Go out.
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, and the absorption tail gas propylene enhancing using by-product,
Propene yield is greatly improved, and 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
For absorption tower charging；5 is depropanizing tower charging；6 is absorbent；7 is to absorb tail gas；8 is absorbing liquid；9 is three groups of carbon
Point；10 is carbon four component；11 is outer row's carbon four component；12 is carbon five and more heavy constituent；101 is methanol charging；102
For the absorption tail gas returning；103 is preparing propylene from methanol product；104 is waste water；R1 is preparing propylene from methanol reactor；
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.
As shown in figure 1, it is main product that methanol is converted into propylene in preparing propylene from methanol reactor R1, through product gas
Enrichment region S1 obtains hydrocarbon mixture product 1 after concentrating, and hydrocarbon mixture logistics 1 is separated into low pressure carbon four in pre-separation tower T1
And more light component 2 and carbon five and more heavy constituent 12.Low pressure carbon four and more light component 2 obtain after supercharging equipment C1 supercharging
Desorber T2 is sent into after high pressure carbon four and more light component 3.In desorber T2, carbon three and component more heavy constituent produce from tower reactor
Obtain depropanizing tower T4 charging 5, whole ethylene is absorbed tower charging 4 from desorber T2 overhead extraction.On absorption tower
In T3, since absorb propylene in charging 4 as absorbent from carbon four component 6 of depropanization tower reactor, absorbing liquid 8 returns
Desorber T2.Absorb tail gas part and discharge absorption and desorption system, be partly back to alcohol and/or ether propylene reactor volume increase third
Alkene；.Depropanizing tower T4 will isolate carbon three component 9 and carbon four component 10 in charging 5.Partial carbon four component 10 warp
Send into absorption tower T2 after absorbent cooler E1 cooling and absorb propylene as absorbent, remainder is as four groups of outer row's carbon
Divide 11 discharges.
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 preparing propylene from methanol reactor is main product, through product gas enrichment region S1 dehydration and sour gas
Gas phase hydrocarbon logistics 1 is obtained after carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.10MPa.Gas phase hydrocarbon
Class logistics 1 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 more light component 2 is pressurized to after 1.3MPa obtains high pressure carbon four and more light component 3 through compressor C1 and sends into desorber T2.
In desorber, carbon three component of 70% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene is from tower top
Produce the tower charging 4 that is absorbed.In the T3 of absorption tower, since inhale from carbon four component 6 of depropanization tower reactor as absorbent
Take in the propylene in material 4, absorbing liquid 8 returns desorber T2.The absorption tail gas 102 of 70% mass fraction is returned to reactor
R1, residual absorption tail gas 7 discharges absorption and desorption system.Depropanizing tower T4 will isolate carbon three component 9 and carbon in charging 5
Four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and propane in follow-up propylene rectification tower.88% matter
Carbon four component 10 of amount fraction is cooled to through absorbent cooler E1 after 40 DEG C sends into absorption tower as absorbent, its remaining part
It is allocated as discharging for outer row's carbon four carbon five component 11.This technological process propylene enhancing 22.5%, 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 preparing propylene from methanol reactor is main product, through through product gas enrichment region S1 dehydration and sour gas
Gas phase hydrocarbon logistics 1 is obtained after body carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.12MPa.Gas phase
Hydrocarbon material flow 1 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 more light component 2 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 desorber, carbon three component of 72% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, whole ethylene from
Overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since from carbon four component 6 of depropanization tower reactor as absorption
Agent absorbs the propylene in charging 4, and absorbing liquid 8 returns desorber T2.The absorption tail gas 102 of 75% mass fraction is returned to instead
Answer device R1, residual absorption tail gas 7 discharges absorption and desorption system..Depropanizing tower T4 will isolate carbon three component in charging 5
9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and propane in follow-up propylene rectification tower.
Carbon four component 10 of 90% mass fraction is cooled to through absorbent cooler E1 after 40 DEG C sends into absorption tower as absorbent, its
Remaining part is allocated as discharging for outer row's carbon four carbon five component 11.This technological process propylene enhancing 24.1%, 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 preparing propylene from methanol reactor is main product, through through product gas enrichment region S1 dehydration and sour gas
Gas phase hydrocarbon logistics 1 is obtained after body carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.14MPa.Gas phase
Hydrocarbon material flow 1 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 more light component 2 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 desorber, carbon three component of 73% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, whole ethylene from
Overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since from carbon four component 6 of depropanization tower reactor as absorption
Agent absorbs the propylene in charging 4, and absorbing liquid 8 returns desorber T2.The absorption tail gas 102 of 80% mass fraction is returned to instead
Answer device R1, residual absorption tail gas 7 discharges absorption and desorption system..Depropanizing tower T4 will isolate carbon three component in charging 5
9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and propane in follow-up propylene rectification tower.
Carbon four component 10 of 92% mass fraction is cooled to through absorbent cooler E1 after 40 DEG C sends into absorption tower as absorbent, its
Remaining part is allocated as discharging for outer row's carbon four carbon five component 11.This technological process propylene enhancing 25.7%, 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 preparing propylene from methanol reactor is main product, through through product gas enrichment region S1 dehydration and sour gas
Gas phase hydrocarbon logistics 1 is obtained after body carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.16MPa.Gas phase
Hydrocarbon material flow 1 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 more light component 2 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 desorber, carbon three component of 74% mass fraction obtains depropanizing tower charging 5 from tower reactor extraction, whole ethylene from
Overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since from carbon four component 6 of depropanization tower reactor as absorption
Agent absorbs the propylene in charging 4, and absorbing liquid 8 returns desorber T2.The absorption tail gas 102 of 85% mass fraction is returned to instead
Answer device R1, residual absorption tail gas 7 discharges absorption and desorption system..Depropanizing tower T4 will isolate carbon three component in charging 5
9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and propane in follow-up propylene rectification tower.
Carbon four component 10 of 94% mass fraction is cooled to through absorbent cooler E1 after 40 DEG C sends into absorption tower as absorbent, its
Remaining part is allocated as discharging for outer row's carbon four carbon five component 11.This technological process propylene enhancing 27.3%, 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) | 0.167 | 0.173 | 0.180 | 0.183 | 0.226 | 0.231 |
Claims (10)
1. a kind of alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing, comprise the steps of：Alcohol and/or ether are converted into propylene 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 five and more heavy constituent and 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, carbon four component；Absorb tail gas and at least partly return alcohol and/or ether propylene reactor.
2. alcohol and/or ether propylene product separately and utilize the method for lighter hydrocarbons propylene enhancing it is characterised in that one of product gas enrichment region removing water, oxygenatedchemicalss, carbon dioxide are several or whole according to claim 1.
3. alcohol and/or ether propylene product separately and utilize the method for lighter hydrocarbons propylene enhancing it is characterised in that described pre-separation tower operating pressure is 0.1～1.2MPa according to claim 1, and bottom temperature is 69～171 DEG C.
4. according to claim 1 alcohol and/or ether propylene product separate and using lighter hydrocarbons propylene enhancing method it is characterised in that after described carbon four and the supercharging of more light component pressure be 1.0～2.0MPa.
5. according to claim 1 alcohol and/or ether propylene product separate and using lighter hydrocarbons propylene enhancing method it is characterised in that obtaining carbon four component from described depropanization tower reactor, this carbon four component is at least partly as the absorbent on absorption tower.
6. alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing according to claim 1, it is characterized in that described absorption tower operating pressure is 1.0～1.6MPa, operation temperature is 30～60 DEG C, and absorbent consumption is 1.0～3.0 times of absorption tower gas-phase feed mass flow.
7. alcohol and/or ether propylene product separately and utilize the method for lighter hydrocarbons propylene enhancing it is characterised in that described desorber operating pressure is 1.0～2.0MPa according to claim 1, and tower reactor operation temperature is 60～100 DEG C.
8. alcohol and/or ether propylene product separately and utilize the method for lighter hydrocarbons propylene enhancing it is characterised in that described depropanizing tower operating pressure is 0.6～1.5MPa according to claim 1, and tower reactor operation temperature is 70～110 DEG C.
9. according to claim 1 alcohol and/or ether propylene product separate and using lighter hydrocarbons propylene enhancing method it is characterised in that in described hydrocarbon mixture product by weight percentage, the content of carbon five and more heavy constituent is more than 2.1%.
10. alcohol and/or ether propylene product separate and utilize the method for lighter hydrocarbons propylene enhancing it is characterised in that, the content of carbon five and more heavy constituent is preferably greater than 4.1% in described hydrocarbon mixture product by weight percentage according to claim 1.
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| 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 |
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