CN106478344A - Alcohol and/or ether propylene product separation method - Google Patents
Alcohol and/or ether propylene product separation method Download PDFInfo
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Abstract
The present invention relates to a kind of alcohol and/or ether propylene product separation method, mainly solve the problems, such as in prior art high energy consumption during alcohol and/or ether production of propylene.The present invention passes through using comprising the steps of：Alcohol and/or ether propylene reactor outlet product removal water and sour gas, obtain hydrocarbon mixture product；Hydrocarbon mixture product is sent into removing carbon six and more heavy constituent in pre-separation tower and is obtained 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；Carbon three components separation is propylene and propane；Absorb tail gas and at least partly return alcohol and/or the technical scheme of ether propylene reactor, 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 separation method.
Technical background
Propylene is a kind of basic organic chemical industry raw material being in great demand, and mostlys come from petroleum refining process.With oil money
The increasingly plaque in source is weary, and development increasingly causes attention both domestic and external by the technology that the non-oil resources such as coal or natural gas prepare propylene.
Methanol, the again process route through preparing propylene from methanol are generally produced using producing synthesis gas from coal, synthesis gas by coal propylene.Wherein coal
It is highly developed that preparing synthetic gas and synthesis gas produce methanol technics technology.Preparing propylene from methanol technology through years development, also
Through achieving industrialization.But because preparing propylene from methanol product forms complexity, product includes carbon one to the even more heavy group of carbon seven
Point, the high problem of generally existing technological process length, plant energy consumption.How to reduce the energy consumption of process for preparing propylene from methanol, especially
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 flow process and predepropanization process.For example in CN1431982A patent, preparing propylene from methanol product is through supercool
But, after isolating hydro carbons and water, gas phase hydrocarbon isolates carbon two and more light component and carbon three and heavier first through front-end deethanization flow process
Component, then isolates carbon three component containing propylene and carbon four and more heavy constituent again in depropanizing tower, due to carbon alkadienes and
Carbon four C_5 olefins can be further converted to propylene in preparing propylene from methanol reactor, the carbon two obtaining from dethanizer and
More light component and the return preparing propylene from methanol reactor of the carbon four obtaining from depropanizing tower and more heavy constituent part.Traditional hydro carbons
Due to employing distillation operation, therefore there is high energy consumption in product separation method.
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 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 heavy
Component circulates in absorption and desorption system, and energy consumption is still higher.And in process for preparing propylene from methanol, in product, contain one
Quantitative carbon six and more heavy constituent, therefore inevitably have the shortcomings that high energy consumption using the method.
Prior art all has that plant energy consumption is high, and 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 height, economic effect are poor, provides
A kind of new alcohol and/or the separation method of ether propylene hydrocarbon product.The method is used for alcohol and/or ether propylene hydrocarbon product
Have the advantages that when separating that energy consumption is low, 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 ether propylene hydrocarbon product separation side
Method, comprises the steps of：Alcohol and/or ether propylene reactor outlet obtain hydrocarbon mixture product；Hydrocarbon mixture product is sent into pre-
It is separated into carbon six and more heavy constituent and carbon five and more light component in knockout tower；Send into after carbon five and more light component are intensified and absorb solution
Desorption system, is separated into absorption tail gas, carbon three component, carbon four carbon five component；Carbon three components separation obtains propylene and propane；Inhale
Ending gas at least partly returns alcohol and/or ether propylene reactor.
It is preferred that alcohol and/or ether are methanol and/or dimethyl ether in technique scheme；It is furthermore preferred that alcohol and/or ether are first
Alcohol.
It is preferred that the separation method of a kind of alcohol and/or ether propylene hydrocarbon product in technique scheme, comprise the steps of
It is main product that methanol is converted into propylene in preparing propylene from methanol reactor, after dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon mixture product, gas phase hydrocarbon mixture logistics be separated in pre-separation tower low pressure carbon five and more light component and
Carbon six and more heavy constituent；Low pressure carbon five and more light component are sent after obtaining high pressure carbon five and more light component after compressor boost
Enter desorber；In desorber, carbon three component obtains depropanizing tower charging from tower reactor extraction, and whole ethylene is from overhead extraction
The tower that is absorbed feeds；In absorption tower, since absorb charging from carbon four carbon five component of depropanization tower reactor as absorbent
In propylene, absorbing liquid return desorber；Absorb tail gas and discharge absorption and desorption system, wherein comprise methane, ethylene, second
Alkane, part Returning reactor propylene enhancing, remainder discharge system；Depropanizing tower is isolated from depropanizing tower charging
Carbon three component and carbon four carbon five component；Carbon three component isolates polymerization-grade propylene product and propane in propylene rectification tower；Portion
Absorption tower is sent into as absorbent, remaining is as outer row's carbon four carbon after five groups of lease making absorbent coolers coolings of carbon four carbon dividing
Five components are discharged, it is to avoid accumulate in system.
It is preferred that described pre-separation tower operating pressure is 0.1～1.2MPa in technique scheme, bottom temperature is 80～197
℃.
In technique scheme it is preferred that described carbon five and more light component supercharging after pressure be 1.3～2.0MPa.If carbon five
And more light component is gas phase, then can adopt compressor boost；If carbon five and more light component are liquid phases, pump can be adopted
Supercharging.
It is preferred that described absorption and desorption system comprises absorption tower, desorber and depropanizing tower in technique scheme.
It is preferred that described depropanization tower reactor obtains carbon four carbon five component in technique scheme, this carbon four carbon five component is at least
Part is as the absorbent on absorption tower.
In technique scheme it is preferred that described absorption tower operating pressure is 1.2～1.4MPa, and operation temperature is 40～60 DEG C,
Absorbent consumption is 1.6～2.6 times of absorption tower gas-phase feed mass flow.
It is preferred that described desorber operating pressure is 1.4～1.8MPa in technique scheme, tower reactor operation temperature is 70～90
℃.
It is preferred that described depropanizing tower operating pressure is 0.9～1.2MPa in technique scheme, tower reactor operation temperature is
80～100 DEG C.
In technique scheme it is preferred that in described hydrocarbon mixture product by weight percentage, carbon six and more heavy constituent
Content is more than 2.0%.
In technique scheme, it is furthermore preferred that in described hydrocarbon mixture product by weight percentage, carbon six and more heavy constituent
Content be more than 4.0%.
Using the method for the present invention, when the pressure that the operating pressure of pre-separation tower is higher than hydrocarbon mixture product, using compressor
Hydrocarbon mixture product booster is sent in pre-separation tower to higher than after this operating pressure.
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 six and more heavy constituent in absorption and desorption system to avoid the method that carbon six and more heavy constituent are accumulated, and be utilized in
Hydrocarbon mixture product directly therefrom removes carbon six and more heavy constituent method before entering absorption and desorption system.Side using the present invention
Method, hydrocarbon mixture product is stripped of carbon six and more heavy constituent in pre-separation tower, it is to avoid carbon six and more heavy constituent are absorbing solution
Accumulation in desorption system and circulation, reduce desorbing tower reactor and the temperature of depropanization tower reactor, thus reducing process energy consumption.
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 40～60 on absorption tower
DEG C, reduce further the consumption of cold.Absorb and in the absorption tail gas of tower top, contain ethylene, carbon four C_5 olefins, this absorption
Tail gas at least partly can circulate the charging as alcohol and/or ether propylene reactor, improves propylene total recovery.Depropanization tower reactor
, as the absorbent on absorption tower, another part is as carbon four carbon five component of absorption and desorption system for a part for logistics.Using this
The method of invention, the response rate of propylene and propane 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
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 carbon five component；11 is outer row's carbon four carbon five component；12 is carbon six and more heavy constituent；101 enter for methanol
Material；102 is the absorption tail gas returning；103 is preparing propylene from methanol product；104 is preparing propylene from methanol product；105
For waste water；R1 is preparing propylene from methanol reactor；S1 is gas-liquid separator；T1 is pre-separation tower, and C1 is compressor, T2
For desorber, T3 is absorption tower, and T4 is depropanizing tower, and E1 is absorbent cooler.
As shown in figure 1, methanol be converted in preparing propylene from methanol reactor R1 propylene be main product, through dehydration and
Gas phase hydrocarbon mixture product 1 is obtained, gas phase hydrocarbon mixture logistics separates in pre-separation tower T1 after sour gas carbon dioxide
For low pressure carbon five and more light component 2 and carbon six and more heavy constituent 12；Low pressure carbon five and more light component 2 increase through compressor C1
Desorber T2 is sent into after obtaining high pressure carbon five and more light component 3 after pressure；In desorber, carbon three component obtains from tower reactor extraction
Depropanizing tower charging 5, whole ethylene is absorbed tower charging from overhead extraction；In absorption tower, since from depropanizing tower
Carbon four carbon five component of kettle absorbs the propylene in charging as absorbent, and absorbing liquid returns desorber；Absorb tail gas and discharge and absorb
Desorption system, wherein comprises methane, ethylene, ethane, partial tail gas 102 Returning reactor propylene enhancing, remainder is arranged
Go out system；Depropanizing tower charging isolates carbon three component and carbon four carbon five component in depropanizing tower T4；Carbon three component is in propylene
Polymerization-grade propylene product and propane is isolated in rectifying column；Send into after the five groups of lease making absorbent cooler coolings of partial carbon four carbon
As absorbent 6, remaining is discharged as outer row's carbon four carbon five component on absorption tower.
Fig. 2 is the schematic flow sheet using carbon more than five 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；
6 is absorbent；7 is to absorb tail gas；8 is absorbing liquid；9 is carbon three carbon four component；5 is carbon five and more heavy constituent；10 are
Outer row's carbon five and more heavy constituent；11 is carbon three component；12 is carbon four component；C1 is compressor；T1 is desorber；T2
For absorption tower；T3 is debutanizing tower；E1 is absorbent cooler；T4 is depropanizing tower.
The technological process of Fig. 2 is as follows：It is main product that methanol is converted into propylene in preparing propylene from methanol reactor, through de-
Gas phase hydrocarbon mixture product 1 is obtained after water and sour gas carbon dioxide.After gas phase hydrocarbon logistics 1 is pressurized through compressor C1,
Send into desorber T1.In desorber T1 tower reactor extraction debutanizing tower charging 4, whole ethylene is absorbed from overhead extraction
Tower charging 3.In the T2 of absorption tower, since inhale from the part carbon five of debutanization tower reactor and more heavy constituent 5 as absorbent 6
Receive propylene, absorbing liquid 8 returns desorber T1.Absorb tail gas 7 and discharge absorption and desorption system.Debutanizing tower charging 4 is de-
It is separated into carbon three carbon four component 9 and carbon five and more heavy constituent 5 in butane tower T3.Carbon three carbon four component 9 is in depropanizing tower T4
In isolate carbon three component 11 and carbon four component 12.Carbon three component 11 obtains polymerization-grade propylene product and propane through propylene rectification.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
Fig. 1 is shown in technological process.Methanol be converted in preparing propylene from methanol reactor propylene be main product, through 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 0.13MPa,
Mole consist of 18.7% carbon one to carbon two component, 45.9% carbon three component, 27.5% carbon, four carbon five component, 7.9% carbon six and more
Heavy constituent.Gas phase hydrocarbon logistics 1 is separated into low pressure carbon five and more light component 2 and carbon six in pre-separation tower T1 and more recombinates
Divide 12.Low pressure carbon five and more light component 2 are pressurized to after 2MPa acquisition high pressure carbon five and more light component 3 through compressor C1
Send into desorber T2.In desorber, carbon three component of 70.5% 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 carbon of depropanization tower reactor
Five components 6 absorb the propylene in charging 4 as absorbent, and absorbing liquid 8 returns desorber T2.The absorption of 50% volume fraction
Tail gas returns preparing propylene from methanol reactor, comprises methane, ethylene, carbon four carbon five alkane alkene in the absorption tail gas 102 of return,
Wherein alkene is further converted to propylene in the reactor.Remaining absorbs tail gas and discharges absorption and desorption system, can divide further
Separate out ethylene product or as fuel.Depropanizing tower T4 isolates carbon three component 9 and carbon four carbon five component 10 from charging 5.
Carbon three component 9 isolates polymerization-grade propylene product and propane in propylene rectification tower.Carbon four carbon five component of 88% mass fraction
10 are cooled to feeding absorption tower after 40 DEG C through absorbent cooler E1, and, as absorbent, remainder is as outer row's carbon four carbon five
Component 11 is discharged.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.
Similarly hereinafter.
【Embodiment 2】
Using with embodiment 1 identical technological process.Being converted into propylene in preparing propylene from methanol reactor is main product,
Gas phase hydrocarbon logistics 1 is obtained after dehydration and sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is
0.12MPa, mole consists of 22.3% carbon one to carbon two component, 46.4% carbon three component, 24.3% carbon, four carbon five component, and 7.0%
Carbon six and more heavy constituent.Gas phase hydrocarbon logistics 1 be pressurized to through compressor be separated in pre-separation tower T1 after 0.55MPa low
Pressure 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 pressurized to through compressor C1
1.5MPa sends into desorber T2 after obtaining high pressure carbon five and more light component 3.The carbon three of 72.7% mass fraction in desorber
Component obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene is absorbed tower charging 4 from overhead extraction.Absorbing
In tower T3, since absorb propylene in charging 4, absorbing liquid as absorbent from carbon four carbon five component 6 of depropanization tower reactor
8 return desorber T2.The absorption tail gas of 60% volume fraction returns preparing propylene from methanol reactor, the absorption tail gas 102 of return
In comprise methane, ethylene, carbon four carbon five alkane alkene, wherein alkene is further converted to propylene in the reactor.Remaining absorbs
Tail gas discharges absorption and desorption system, can be further separated out ethylene product or as fuel.Depropanizing tower T4 is from charging 5
In isolate carbon three component 9 and carbon four carbon five component 10.Carbon three component 9 is isolated polymerization-grade propylene in propylene rectification tower and is produced
Product and propane.Carbon four carbon five component 10 of 92% mass fraction is cooled to feeding absorption tower after 40 DEG C through absorbent cooler E1
As absorbent 6, 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.
【Embodiment 3】
Using with embodiment 1 identical technological process.It is main that dimethyl ether is converted into propylene in dimethyl ether propylene reactor
Product, obtains gas phase hydrocarbon logistics 1 after dehydration and sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 temperature is 43
DEG C, pressure is 0.14MPa, mole consists of 21.5% carbon one to carbon two component, 46.9% carbon three component, 25.4% carbon four carbon
Five components, 6.2% carbon six and more heavy constituent.Gas phase hydrocarbon logistics 1 is separated into low pressure carbon five and lighter in pre-separation tower T1
Component 2 and carbon six and more heavy constituent 12.Low pressure carbon five and more light component 2 are pressurized to 1.7MPa through compressor C1 and obtain
Desorber T2 is sent into after high pressure carbon five and more light component 3.In desorber, carbon three component of 72.9% mass fraction is adopted from tower reactor
Go out to obtain depropanizing tower charging 5, whole ethylene is absorbed tower charging 4 from overhead extraction.In the T3 of absorption tower, since
Absorb the propylene in charging 4 from carbon four carbon five component 6 of depropanization tower reactor as absorbent, absorbing liquid 8 returns desorber
T2.The absorption tail gas of 70% volume fraction returns preparing propylene from methanol reactor, comprise in the absorption tail gas 102 of return methane,
Ethylene, carbon four carbon five alkane alkene, wherein alkene is further converted to propylene in the reactor.Remaining absorbs tail gas and discharges and absorbs
Desorption system, can be further separated out ethylene product or as fuel.Depropanizing tower T4 isolates carbon three from charging 5
Component 9 and carbon four carbon five component 10.Carbon three component 9 isolates polymerization-grade propylene product and propane in propylene rectification tower.89%
Carbon four carbon five component 10 of mass fraction is cooled to through absorbent cooler E1 after 40 DEG C sends into absorption tower as absorbent 6,
Remainder is discharged as outer row's carbon four carbon five component 11.
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.This technological process propylene recovery rate 99.99%.
【Embodiment 4】
Using with embodiment 1 identical technological process, the methanol with the dimethyl ether of 50% mass fraction and 50% mass fraction is
Raw material, being converted into propylene through preparing propylene from methanol reactor is main product, obtains after dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon material flow 1.Gas phase hydrocarbon logistics 1 temperature is 43 DEG C, and pressure is 0.14MPa, mole consists of 19.7% carbon
One to carbon two component, 46.8% carbon three component, 31.2% carbon, four carbon five component, 2.3% carbon six and more heavy constituent.Gas phase hydrocarbon thing
Stream 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 sends into desorber after compressor C1 is pressurized to 1.7MPa.The carbon three of 70.3% mass fraction in desorber
Component obtains depropanizing tower charging 5 from tower reactor extraction, and whole ethylene is absorbed tower charging 4 from overhead extraction.Absorbing
In tower T3, since absorb propylene in charging 4, absorbing liquid as absorbent from carbon four carbon five component 6 of depropanization tower reactor
8 return desorber T2.The absorption tail gas of 80% volume fraction returns preparing propylene from methanol reactor, the absorption tail gas 102 of return
In comprise methane, ethylene, carbon four carbon five alkane alkene, wherein alkene is further converted to propylene in the reactor.Remaining absorbs
Tail gas discharges absorption and desorption system, can be further separated out ethylene product or as fuel.Depropanizing tower T4 is from charging 5
In isolate carbon three component 9 and carbon four carbon five component 10.Carbon three component 9 is isolated polymerization-grade propylene in propylene rectification tower and is produced
Product and propane.Carbon four carbon five component 10 of 85% mass fraction is cooled to feeding absorption tower after 40 DEG C through absorbent cooler E1
As absorbent 6, 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.
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 | 89 | 143 | 174 | 195 | - | - |
| Absorptive tower absorbent consumption | 2.31 | 1.94 | 2.55 | 2.05 | 2.13 | 2.28 |
| Absorption tower operating pressure | 1.2 | 1.4 | 1.3 | 1.2 | 1.2 | 1.2 |
| Absorb tower top operation temperature | 52 | 53 | 53 | 52 | 56 | 52 |
| Absorb tower reactor operation temperature | 44 | 48 | 47 | 43 | 43 | 44 |
| Desorber operating pressure | 1.4 | 1.8 | 1.6 | 1.5 | 1.5 | 1.4 |
| Desorbing tower reactor operation temperature | 77 | 88 | 86 | 79 | 96 | 79 |
| Depropanizing tower operating pressure | 0.9 | 1.2 | 1.1 | 1.2 | 1.15 | 0.9 |
| Depropanization tower top operation temperature | 16 | 27 | 23.3 | 27 | 25 | 16 |
| Depropanization tower reactor operation temperature | 83 | 96 | 92 | 97 | 81 | 86 |
| Energy consumption (kg marks oil/kg propylene) | 0.163 | 0.162 | 0.187 | 0.184 | 0.213 | 0.251 |
【Comparative example 1】
Fig. 2 is shown in technological process.Using with embodiment 1 identical hydrocarbon mixture product, be pressurized to through compressor after 1.6MPa,
Send into desorber T1.Desorber operating pressure 1.5MPa, 40 DEG C of tower top temperature, 96 DEG C of bottom temperature.In desorber T1
In 73.2% mass fraction carbon three component from tower reactor extraction obtain debutanizing tower charging 4, whole ethylene obtains from overhead extraction
Feed 3 to absorption tower.Absorption tower operating pressure 1.2MPa, absorbs 56 DEG C of temperature.In the T2 of absorption tower, since autospasy fourth
The carbon five of alkane tower reactor and more heavy constituent 5 absorb the propylene in charging 3 as absorbent, and absorbing liquid 8 returns desorber T1.
Absorb tail gas 7 and discharge absorption and desorption system.Debutanizing tower charging 4 is separated into carbon three carbon four component 9 in debutanizing tower T3
With carbon five and more heavy constituent 5, debutanizing tower operating pressure 1.2MPa, 41 DEG C of tower top temperature, 165 DEG C of bottom temperature.Carbon three
Carbon four component 9 isolates carbon three component 11 and carbon four component 12 in depropanizing tower T4, depropanizing tower operating pressure 1.15MPa,
25 DEG C of tower top temperature, 81 DEG C of bottom temperature.Carbon three component 11 obtains polymerization-grade propylene product and propane through propylene rectification.85%
The carbon five of mass fraction and more heavy constituent 5 are cooled to through absorbent cooler E1 after 40 DEG C sends into absorption tower as absorbent 6,
Remainder discharge system.The energy consumption of this technological process is higher than that the energy consumption of embodiment 1～4 contains carbon mainly due in absorbent
Six and above heavier component, desorber, the tower reactor high energy consumption of debutanizing tower.The energy consumption of comparative example 1 is shown in Table 2.
【Comparative example 2】
Using with embodiment 1 identical hydrocarbon mixture product, the oily absorption technique stream being readily apparent that using those skilled in the art
Journey, that is, be not provided with pre-separation tower and arrange depentanizer in absorption and desorption system, makes in absorbent not carbon containing six and more recombinating
Point.The energy consumption of this technological process is higher than embodiment and the energy consumption of comparative example 1, exists a large amount of in main cause absorption and desorption system
Absorbent circulation, depentanizer feed loading is big, and the carbon six separating relatively small amount from substantial amounts of carbon four carbon five absorbent needs
Will substantial amounts of energy.
【Comparative example 3】
Using with embodiment 1 identical hydrocarbon mixture product, be pressurized to through compressor after 1.6MPa, send into front-end deethanization divide
From system, successively through dethanizer, depropanizing tower, depentanizer, obtain carbon two and more light component, carbon three component, carbon four
Carbon five component and carbon six and more heavy constituent.This technological process due to employing less than -40 DEG C of cryogenic coolant, cold high energy consumption,
Lead to total energy consumption higher.The energy consumption of this comparative example marks oil/kg propylene for 0.229kg.
【Comparative example 4】
Using with embodiment 1 identical hydrocarbon mixture product, be pressurized to through compressor after 1.6MPa, send into predepropanization divide
From system, through depropanizing tower, dethanizer, depentanizer, obtain carbon two and more light component, carbon three component, carbon four carbon five
Component and carbon six and more heavy constituent.This technological process needs also exist for the cryogenic coolant using less than -40 DEG C, cold high energy consumption,
Lead to total energy consumption higher.The energy consumption of this comparative example marks oil/kg propylene for 0.227kg.
Claims (10)
1. a kind of alcohol and/or ether propylene product separation method, comprise the steps of：Alcohol and/or ether propylene reactor outlet
Obtain hydrocarbon mixture product；Hydrocarbon mixture product is sent in pre-separation tower and is separated into carbon six and more heavy constituent and carbon five and lighter group
Point；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；Carbon three components separation obtains propylene and propane；Absorb tail gas and at least partly return alcohol and/or ether propylene reactor.
2. according to claim 1 alcohol and/or ether propylene product separation method it is characterised in that described pre-separation tower behaviour
Making pressure is 0.09～1.25MPa, and bottom temperature is 85～195 DEG C.
3. according to claim 1 alcohol and/or ether propylene product separation method it is characterised in that described carbon five and lighter
After component supercharging, pressure is 1.35 to 1.95MPA.
4. according to claim 1 alcohol and/or ether propylene product separation method it is characterised in that described absorption and desorption system
System comprises absorption tower, desorber and depropanizing tower.
5. according to claim 4 alcohol and/or ether propylene product separation method it is characterised in that from described depropanizing tower
Kettle obtains carbon four carbon five component, and this carbon four carbon five component is at least partly as the absorbent on absorption tower.
6. according to claim 4 alcohol and/or ether propylene product separation method it is characterised in that the operation of described absorption tower
Pressure is 1.2～1.4MPa, and operation temperature is 40～60 DEG C, and absorbent consumption is absorption tower gas-phase feed mass flow
1.5～2.5 times.
7. according to claim 4 alcohol and/or ether propylene product separation method it is characterised in that the operation of described desorber
Pressure is 1.3～1.8MPa, and tower reactor operation temperature is 70～95 DEG C.
8. according to claim 4 alcohol and/or ether propylene product separation method it is characterised in that described depropanizing tower behaviour
Making pressure is 0.9～1.2MPa, and tower reactor operation temperature is 80～100 DEG C.
9. according to claim 1 alcohol and/or ether propylene product separation method it is characterised in that described hydrocarbon mixture produces
In thing by weight percentage, the content of carbon six and more heavy constituent is more than 2.3%.
10. according to claim 9 alcohol and/or ether propylene product separation method it is characterised in that described hydrocarbon mixture produces
In thing by weight percentage, the content of carbon six and more heavy constituent is more than 4.1%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108218656A (en) * | 2018-01-08 | 2018-06-29 | 惠生工程（中国）有限公司 | A kind of separation method of the C_4 hydrocarbon containing light gas |
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 |
-
2015
- 2015-08-28 CN CN201510540795.XA patent/CN106478344B/en active Active
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 |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108218656A (en) * | 2018-01-08 | 2018-06-29 | 惠生工程（中国）有限公司 | A kind of separation method of the C_4 hydrocarbon containing light gas |
| CN108218656B (en) * | 2018-01-08 | 2021-06-29 | 惠生工程（中国）有限公司 | Method for separating carbon tetrahydrocarbon containing light gas |
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