CN106478350B - Alcohol and/or the separation of ether propylene product and the method using by-product propylene enhancing - Google Patents
Alcohol and/or the separation of ether propylene product and the method using by-product propylene enhancing Download PDFInfo
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Abstract
The present invention relates to a kind of alcohol and/or the separation of ether propylene product and using the method for by-product propylene enhancing, high energy consumption, by-product utilization during alcohol in the prior art and/or ether production of propylene are mainly solved the problems, such as.The present invention is by using comprising the following steps：It is main reaction product that alcohol and/or ether are converted into propylene in the reactor, and reaction product obtains hydrocarbon mixture product after the concentration of product gas enrichment region；Hydrocarbon mixture product is sent into removing light dydrocarbon and more heavy constituent in pre-separation tower and obtains carbon four and more light component；Carbon four and more light component is sent into absorption and desorption system after supercharging, is separated into absorption tail gas, three component of carbon, four component of carbon；It absorbs tail gas and at least partly returns to alcohol and/or ether propylene reactor, four component of carbon at least partly returns to the technical solution of alcohol and/or ether propylene reactor propylene enhancing, preferably solves the above problem, can be used in the industrial production of alcohol and/or ether propylene.
Description
Technical field
The present invention relates to a kind of alcohol and/or the separation of ether propylene product and utilize the method for by-product propylene enhancing.
Technical background
Ethylene, propylene are a kind of basic organic chemical industry raw materials being in great demand, by ethylene oxide, polyethylene, polypropylene,
The growth of the ethylene such as acrylonitrile, isopropylbenzene, propylene oxide, acryloyl derivative demand, corresponding ethylene, propylene demand also quickly increase
It is long.Traditional ethylene and propylene mostlys come from petroleum refining process, weary with the increasingly plaque of petroleum resources, develops by coal or day
Non-oil resources prepare ethylene to right gas etc., the technology of propylene increasingly causes attention both domestic and external.It is usual by coal ethylene, propylene
Methanol, the again process route through alcohol and/or ether ethylene, propylene are produced using producing synthesis gas from coal, synthesis gas.Wherein coal system synthesizes
It is highly developed that gas and synthesis gas produce methanol technics technology.Alcohol and/or ether ethylene, propylene technology pass through years development,
Also industrialization is had been realized in, the technology represented has the S-MTO technologies of Sinopec, Dalian materialization institute D-MTO technologies, UOP
MTO technologies, the MTP technologies of Lurgi, S-MTP technologies of Sinopec etc..But due to alcohol and/or ether ethylene, propylene production
Object composition is complicated, and product includes carbon one to the even more heavy component of carbon nine, and generally existing separating technology long flow path, plant energy consumption are high
The problem of.The energy consumption of alcohol and/or ether ethylene, propylene technique is how reduced, the product separation method of low energy consumption is especially developed,
As needing the project of primary study.
The separation of conventional hydrocarbon-based product generally uses rectifying to detach.Typical separation process includes the sequence separation of front-end demethanization
Flow, front-end deethanization separation process and predepropanization separation process.Such as in CN1431982A patents, alcohol and/or ether system third
For alkene reaction product after cooling and isolating hydro carbons and water, gas phase hydrocarbon isolates carbon two and lighter first through front-end deethanization flow
Then component and carbon three and more heavy constituent are isolated three component of carbon and carbon four containing propylene in depropanizing tower and are more recombinated
Point, since carbon alkadienes and four C_5 olefins of carbon can be further converted to propylene in alcohol and/or ether propylene reactor,
The carbon two obtained from dethanizer and more light component and the carbon four obtained from depropanizing tower and the return alcohol of more heavy constituent part and/
Or ether propylene reactor.Traditional hydrocarbon product separation method is as a result of distillation operation or to be high pressure improve essence
It evaporates the operation temperature of tower or is to use cryogenic coolant, therefore the problem of generally existing high energy consumption.
United States Patent (USP) US5326929 proposes a kind of solvent absorption separation hydrogen, the method for two component of methane and carbon.But
This method regenerated solvent under the pressure more than 3.2MPa, causes regeneration temperature very high, up to 150 DEG C, is needed again after solvent reclamation
Cooling down is wanted, it is huge so as to cause the process energy consumption.
Chinese patent CN101353286 proposes a kind of non-copious cooling lower carbon number hydrocarbons separation method containing light gas.This method
Feed gas is boosted to 2.0 to 4.0MPa by compressor first, then by precut tower separation most of two groups of carbon
Point and methane separation, then with the carbon two carried secretly in solvent absorption methane in absorption tower.Due to most of carbon two and whole
Carbon three and more heavy constituent are cut out in pre-separation tower, and the gas-phase feed load on absorption tower declines, under absorbent dosage is also corresponding
Drop, therefore, which claims the energy consumption of this method, and than existing oily absorption and separation technology, low energy consumption.But contain when in feed gas
When carbon six and more heavy constituent, this method leads to a large amount of carbon six since carbon six and more heavy constituent are not cut out from absorbent
And more heavy constituent recycles in absorption and desorption system so that energy consumption can be significantly increased, and absorption efficiency declines, and absorb in resolution system
Tower tower diameter increase, to but also investment is also corresponding increases.And in alcohol and/or ether olefin process, reaction product
In contain a certain amount of carbon six and more heavy constituent, therefore using this method inevitably have high energy consumption, investment it is increased lack
Point.
Since the prior art has that plant energy consumption height, by-product utilize, the present invention targetedly solves
Problem is stated, by-product is made full use of.
Invention content
The technical problem to be solved by the present invention is to which the problem of plant energy consumption is high, by-product utilizes exists in the prior art, carry
For a kind of new alcohol and/or the separation of ether propylene product and utilize the method for by-product propylene enhancing.This method is used for alcohol and/or ether
Have the advantages that low energy consumption, good economy performance, propene yield are high when the separation of propylene hydrocarbon product processed.
To solve the above problems, the technical solution adopted by the present invention is as follows：A kind of alcohol and/or the separation of ether propylene product and
Using the method for by-product propylene enhancing, comprise the following steps：Alcohol and/or ether are converted into propylene and are produced for key reaction in the reactor
Object, reaction product obtain hydrocarbon mixture product after the concentration of product gas enrichment region；Hydrocarbon mixture product, which is sent into pre-separation tower, to be divided
From for light dydrocarbon and more heavy constituent and carbon four and more light component；Carbon four and more light component is sent into absorption and desorption system after supercharging, point
From for absorb tail gas, three component of carbon, four component of carbon；It absorbs tail gas and at least partly returns to alcohol and/or ether propylene reactor；Carbon four
Component at least partly returns to alcohol and/or ether propylene reactor.
In above-mentioned technical proposal, one kind in the product gas enrichment region removing water, oxygenatedchemicals, carbon dioxide is several
Or all.
In above-mentioned technical proposal, the pre-separation tower operating pressure is 0.1~1.2MPa, and bottom temperature is 70~172 DEG C.
In above-mentioned technical proposal, pressure is 1.0~2.0MPa after the carbon four and the supercharging of more light component.
In above-mentioned technical proposal, the absorption and desorption system includes absorption tower, desorber and depropanizing tower.
In above-mentioned technical proposal, the depropanization tower reactor obtains four component of carbon, and four component of carbon is at least partly as absorption
The absorbent of tower.
In above-mentioned technical proposal, the absorption tower operating pressure is 1.0~1.6MPa, and operation temperature is 30~60 DEG C, is inhaled
Receive 1.0~3.0 times that agent dosage is absorption tower gas-phase feed mass flow.
In above-mentioned technical proposal, the desorber operating pressure is 1.0~2.0MPa, and tower reactor operation temperature is 60~100
℃。
In above-mentioned technical proposal, the depropanizing tower operating pressure be 0.6~1.5MPa, tower reactor operation temperature be 70~
110℃。
In above-mentioned technical proposal, in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent
To be more than 2.3%.
In above-mentioned technical proposal, in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent
To be more than 4.2%.
In above-mentioned technical proposal, the alcohol and/or ether are methanol and/or dimethyl ether；Preferred alcohol and/or ether are first
Alcohol.
In above-mentioned technical proposal, the separation method of a kind of alcohol and/or ether olefin product comprises the following steps methanol
It is main reaction product to be converted into propylene in the reactor, and reaction product obtains hydrocarbon mixture production after the concentration of product gas enrichment region
Object；Hydrocarbon mixture object is separated into low pressure carbon four and more light component and light dydrocarbon and more heavy constituent in pre-separation tower；Carbon four and lighter
Component is sent into desorber after supercharging；Three component of carbon produces to obtain depropanizing tower charging from tower reactor in desorber, whole
Ethylene from desorber overhead extraction be absorbed tower charging；In absorption tower, since from the four component conduct of carbon of depropanization tower reactor
Absorbent absorbs the propylene in charging, and absorbing liquid returns to desorber；It at least partly absorbs tail gas and is back to alcohol and/or ether propylene
Reactor propylene enhancing partially absorbs tail gas discharge absorption and desorption system；Depropanizing tower charging is separated into carbon three by depropanizing tower
Four component of component and carbon；Three component of carbon can further isolate polymerization-grade propylene product and propane in propylene rectification tower；Portion
Absorption tower is sent into as absorbent after four groups of lease making absorbent coolers coolings of the carbon divided, and at least partly four component of carbon is back to alcohol
And/or ether propylene reactor propylene enhancing, remaining four component of carbon are discharged as outer four component of row's carbon.
In above-mentioned technical proposal, when the operating pressure of the pre-separation tower is higher than the pressure of hydrocarbon mixture product, using increasing
Equipment is pressed to be sent into pre-separation tower hydrocarbon mixture product booster to higher than after the operating pressure.
The present invention has broken the intrinsic thinking of those skilled in the art, is not readily conceivable that using those skilled in the art
By removing light dydrocarbon and more heavy constituent in absorption and desorption system, and be utilized in hydrocarbon mixture product and enter absorption and desorption system
The method that light dydrocarbon and more heavy constituent are directly therefrom removed before system avoids the carbon six and more heavy constituent from accumulating, to cause to inhale with this
The phenomenon that rate of producing effects declines, and energy consumption can be significantly increased.Method using the present invention, hydrocarbon mixture product remove in pre-separation tower
Light dydrocarbon and more heavy constituent, avoid the accumulation and cycle of carbon six and more heavy constituent in absorption and desorption system, reduce desorption
The temperature of tower reactor and depropanization tower reactor, to reduce process energy consumption；On the other hand due to having lacked the tired of carbon six and more heavy constituent
Product and cycle so that absorption and desorption system tower diameter also accordingly reduces, to also save equipment investment expense.
Method using the present invention, absorption and desorption system carry out at lower pressures, further reduced desorption tower reactor
With the temperature of depropanization tower reactor, process energy consumption further reduced.Absorption tower uses higher absorption temperature, operation temperature 30
~60 DEG C, it further reduced the consumption of cold.Depropanization tower reactor, which obtains four component of carbon, can at least partly be used as absorbent.It adopts
The rate of recovery with the method for the present invention, propylene is 99.99%, and low energy consumption, and utilizes four component of absorption tail gas and carbon of by-product
Propylene enhancing, propene yield greatly improve, and achieve preferable technique effect.
Description of the drawings
Fig. 1 is the flow diagram of the method for the invention.
In Fig. 1,1 is hydrocarbon mixture product；2 be low pressure carbon four and more light component；3 be high pressure carbon four and more light component；4 are
Absorption tower is fed；5 feed for depropanizing tower；6 be absorbent；7 be absorption tail gas；8 be absorbing liquid；9 be three component of carbon；10 be carbon
Four components；11 be outer four component of row's carbon；12 be light dydrocarbon and more heavy constituent；101 feed for methanol；102 be the absorption tail gas returned；
103 be four component of carbon returned；104 be methanol to propylene reaction product；105 be waste water；R1 is methanol to propylene reaction device；S1
For product gas enrichment region；T1 is pre-separation tower；C1 is supercharging equipment；T2 is desorber；T3 is absorption tower；T4 is depropanizing tower；
E1 is absorbent cooler.
As shown in Figure 1, it is main reaction product that methanol is converted into propylene in methanol to propylene reaction device R1, through product gas
Obtain hydrocarbon mixture product 1 after enrichment region S1 concentration, hydrocarbon mixture logistics 1 is separated into low pressure carbon four and more in pre-separation tower T1
Light component 2 and light dydrocarbon and more heavy constituent 12.Low pressure carbon four and more light component 2 obtain high pressure carbon four after supercharging equipment C1 superchargings
And desorber T2 is sent into after more light component 3.Carbon three and component more heavy constituent produce to obtain depropanization from tower reactor in desorber T2
Tower T4 charging 5, whole ethylene are absorbed tower charging 4 from desorber T2 overhead extractions.In the T3 of absorption tower, since autospasy third
Four component 6 of carbon of alkane tower reactor absorbs the propylene in charging 4 as absorbent, and absorbing liquid 8 returns to desorber T2.Partially absorb tail gas
7 discharge absorption and desorption systems, partially absorb tail gas 102 and are back to alcohol and/or ether propylene reactor propylene enhancing.Depropanizing tower
T4 isolates four component 10 of three component 9 of carbon and carbon in feeding 5.It is sent after partial four groups of lease making absorbent cooler E1 coolings of carbon
Enter absorption tower T2 and absorb propylene as absorbent 6, at least partly four component 103 of carbon is back to alcohol and/or ether propylene reactor
R1 propylene enhancings, rest part are discharged as four component 11 of outer row's carbon.
Fig. 2 is the flow diagram using four or more component of carbon as absorbent.
In Fig. 2,1 is hydrocarbon mixture product；2 feed for desorber；3 feed for absorption tower；4 feed for depropanizing tower；5 are
Carbon four and more heavy constituent；6 be absorbent；7 be absorption tail gas；8 be absorbing liquid；9 be three component of carbon；10 be outer row's carbon four and heavier
Component；C1 is supercharging equipment；T1 is desorber；T2 is absorption tower；T3 is depropanizing tower；E1 is absorbent cooler.
The technological process of Fig. 2 is as follows：It is main reaction product that alcohol and/or ether are converted into propylene in the reactor, through being dehydrated,
Gas phase hydrocarbon mixture product 1 is obtained after oxygenatedchemicals and carbon dioxide.Gas phase hydrocarbon logistics 1 after supercharging equipment C1 supercharging,
It is sent into desorber T1.In desorber T1 tower reactors extraction depropanizing tower charging 4, whole ethylene is obtained from desorber T1 overhead extractions
Absorption tower charging 3.In the T2 of absorption tower, since from the part carbon four of depropanization tower reactor and more heavy constituent 5 through absorbent cooler
Absorption tower T2 being sent into as absorbent 6 after E1 coolings and absorbing propylene as absorbent, absorbing liquid 8 returns to desorber T1.Absorb tail
Absorption and desorption system is discharged in gas 7.Depropanizing tower T3 charging 4 is separated into three component 9 of carbon and carbon four and heavier in depropanizing tower T3
Component 5.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific implementation mode
【Embodiment 1】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through product gas enrichment region S1 dehydrations and sour gas
Gas phase hydrocarbon logistics 1 is obtained after body carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.10MPa.Gas phase hydrocarbon
Logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and lighter
Component 2 is pressurized to after 1.3MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
Three component of carbon of 70% mass fraction produces to obtain depropanizing tower charging 5 from tower reactor, and whole ethylene is inhaled from overhead extraction
Receive tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.The absorption tail gas 102 of 70% mass fraction is returned to reactor R1, residual absorption tail gas 7
Absorption and desorption system is discharged.Depropanizing tower T4 isolates four light dydrocarbon component 10 of three component 9 of carbon and carbon in feeding 5.Three component 9 of carbon
Polymerization-grade propylene product and propane are isolated in subsequent propylene rectification tower.Four component 103 of carbon of 50% mass fraction is returned
Increase production alkene to reactor R1, four component Parts of carbon are sent into absorption tower as absorption after absorbent cooler E1 is cooled to 40 DEG C
Agent, rest part are discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process propylene enhancing 30.2%, propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Embodiment 2】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.12MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 1.6MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 72% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.The absorption tail gas 102 of 75% mass fraction is returned to reactor R1, residual absorption tail gas 7
Absorption and desorption system is discharged..Depropanizing tower T4 isolates four light dydrocarbon component 10 of three component 9 of carbon and carbon in feeding 5.Three component of carbon
9 isolate polymerization-grade propylene product and propane in subsequent propylene rectification tower.Four component 102 of carbon of 60% mass fraction is returned
Increase production alkene to reactor R1, four component Parts of carbon are sent into absorption tower as absorption after absorbent cooler E1 is cooled to 40 DEG C
Agent, rest part are discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process propylene enhancing 32.2%, propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Embodiment 3】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.14MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 1.8MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 73% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.The absorption tail gas 102 of 80% mass fraction is returned to reactor R1, residual absorption tail gas 7
Absorption and desorption system is discharged..Depropanizing tower T4 isolates four light dydrocarbon component 10 of three component 9 of carbon and carbon in feeding 5.Three component of carbon
9 isolate polymerization-grade propylene product and propane in subsequent propylene rectification tower.Four component 102 of carbon of 70% mass fraction is returned
Increase production alkene to reactor R1, four component Parts of carbon are sent into absorption tower as absorption after absorbent cooler E1 is cooled to 40 DEG C
Agent, rest part are discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process propylene enhancing 34.2%, propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Embodiment 4】
Using process of the present invention, by 300,000/year propylene methanol or/and dimethyl ether olefin hydrocarbon apparatus for,
It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through through product gas enrichment region S1 dehydrations and acidity
Gas phase hydrocarbon logistics 1 is obtained after atmospheric carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.16MPa.Gas phase hydrocarbon
Class logistics 1 is separated into low pressure carbon four and more light component 2 and light dydrocarbon and more heavy constituent 12 in pre-separation tower T1.Low pressure carbon four and more
Light component 2 is pressurized to after 2.0MPa obtains high pressure carbon four and more light component 3 by compressor C1 and is sent into desorber T2.In desorber
In three component of carbon of 74% mass fraction produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is obtained from overhead extraction
Absorption tower charging 4.In the T3 of absorption tower, since absorbed from four component 6 of carbon of depropanization tower reactor as absorbent in charging 4 third
Alkene, absorbing liquid 8 return to desorber T2.The absorption tail gas 102 of 85% mass fraction is returned to reactor R1, residual absorption tail gas 7
Absorption and desorption system is discharged..Depropanizing tower T4 isolates four light dydrocarbon component 10 of three component 9 of carbon and carbon in feeding 5.Three component of carbon
9 isolate polymerization-grade propylene product and propane in subsequent propylene rectification tower.Four component 102 of carbon of 70% mass fraction is returned
Increase production alkene to reactor R1, four component Parts of carbon are sent into absorption tower as absorption after absorbent cooler E1 is cooled to 40 DEG C
Agent, rest part are discharged as four light dydrocarbon component 11 of outer row's carbon.The technological process propylene enhancing 36.2%, propylene recovery rate
99.99%.
The operating condition and system energy consumption of each tower are shown in Table 1.Absorptive tower absorbent dosage is the quality stream of absorbent 6 in table
The ratio between the mass flow of amount and absorption tower charging 4.Energy consumption is the summation of compressor, pump, heat exchanger, rectifying column energy consumption in table.
【Comparative example 1】
Fig. 2 is shown in technological process, using with 1 identical hydrocarbon mixture product of embodiment, after compressor is pressurized to 1.6MPa,
It is sent into desorber T1.Desorber operating pressure 1.5MPa, 96 DEG C of bottom temperature.The carbon of 73.2% mass fraction in desorber T1
Three components produce to obtain depropanizing tower charging 4 from tower reactor, and whole ethylene is absorbed tower charging 3 from overhead extraction.Absorption tower
Operating pressure 1.25MPa absorbs 43 DEG C of temperature.In the T2 of absorption tower, since make from the carbon four of depropanization tower reactor and more heavy constituent 5
The propylene in charging 3 is absorbed for absorbent, absorbing liquid 8 returns to desorber T1.It absorbs tail gas 7 and absorption and desorption system is discharged.De- third
Alkane tower charging 4 is separated into three component 9 of carbon and carbon four and more heavy constituent 5, depropanizing tower operating pressure in depropanizing tower T3
1.15MPa, 81 DEG C of bottom temperature, three component 9 of carbon obtain polymerization-grade propylene product and propane through propylene rectifying.85% mass fraction
Carbon four and more heavy constituent 5 be sent into absorption tower after absorbent cooler E1 cooling and be used as the absorbent 6, rest part discharge to be
System.The propylene recovery rate 98.2% of the technological process, energy consumption is shown in Table 1.
【Comparative example 2】
Fig. 2 is shown in technological process, using with 1 identical hydrocarbon mixture product of embodiment, after compressor is pressurized to 1.4MPa,
It is sent into desorber T1.Desorber operating pressure 1.3MPa, 74 DEG C of bottom temperature.The carbon of 71.2% mass fraction in desorber T1
Three components produce to obtain depropanizing tower charging 4 from tower reactor, and whole ethylene is absorbed tower charging 3 from overhead extraction.Absorption tower
Operating pressure 1.45MPa absorbs 44 DEG C of temperature.In the T2 of absorption tower, since make from the carbon four of depropanization tower reactor and more heavy constituent 5
The propylene in charging 3 is absorbed for absorbent, absorbing liquid 8 returns to desorber T1.It absorbs tail gas 7 and absorption and desorption system is discharged.De- third
Alkane tower charging 4 is separated into three component 9 of carbon and carbon four and more heavy constituent 5, depropanizing tower operating pressure in depropanizing tower T3
0.9MPa, 86 DEG C of bottom temperature, three component 9 of carbon obtain polymerization-grade propylene product and propane through propylene rectifying.80% mass fraction
Carbon four and more heavy constituent 5 be sent into absorption tower after absorbent cooler E1 cooling and be used as the absorbent 6, rest part discharge to be
System.The propylene recovery rate 98.4% of the technological process, energy consumption is shown in Table 1.
Table 1
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Comparative example 1 | Comparative example 2 | |
| Pre-separation tower operating pressure | 0.11 | 0.55 | 0.8 | 1.2 | - | - |
| Pre-separation tower top operation temperature | -13 | 21 | 41 | 56 | - | - |
| Pre-separation tower reactor operation temperature | 72 | 103 | 144 | 167 | - | - |
| Absorptive tower absorbent dosage | 2.01 | 2.85 | 2.55 | 1.24 | 2.23 | 2.58 |
| Absorption tower operating pressure | 1.05 | 1.25 | 1.35 | 1.55 | 1.25 | 1.45 |
| Absorb tower reactor operation temperature | 35 | 43 | 47 | 58 | 43 | 44 |
| Desorber operating pressure | 1.25 | 1.55 | 1.75 | 1.95 | 1.5 | 1.3 |
| Desorb tower reactor operation temperature | 63 | 78 | 86 | 95 | 96 | 74 |
| Depropanizing tower operating pressure | 0.6 | 1.1 | 1.2 | 1.5 | 1.15 | 0.9 |
| Depropanization tower top operation temperature | 6 | 23.3 | 27 | 47 | 25 | 16 |
| Depropanization tower reactor operation temperature | 73 | 92 | 97 | 109 | 81 | 86 |
| Energy consumption (kg marks oil/kg propylene) | 0.171 | 0.176 | 0.184 | 0.186 | 0.226 | 0.231 |
Claims (10)
1. a kind of methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing, comprise the following steps：
It is main reaction product that methanol and/or dimethyl ether are converted into propylene in the reactor, and reaction product is concentrated through product gas enrichment region
Hydrocarbon mixture product is obtained afterwards；Hydrocarbon mixture product, which is sent into pre-separation tower, is separated into light dydrocarbon and more heavy constituent and carbon four and lighter
Component；Carbon four and more light component is sent into absorption and desorption system after supercharging is separated into and absorbs tail gas, three component of carbon, four component of carbon；
It absorbs tail gas and at least partly returns to methanol and/or dimethyl ether propylene reactor；Four component of carbon at least partly return methanol and/or
Dimethyl ether propylene reactor.
2. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that one or more of product gas enrichment region removing water, oxygenatedchemicals, carbon dioxide.
3. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that the pre-separation tower operating pressure is 0.1~1.2MPa, bottom temperature is 70~172 DEG C.
4. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that pressure is 1.0~2.0MPa after the carbon four and the supercharging of more light component.
5. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that the absorption and desorption system includes depropanizing tower, four component of carbon is obtained from the depropanization tower reactor, four groups of the carbon
Divide the absorbent at least partly as absorption tower.
6. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that the absorption and desorption system includes absorption tower, absorption tower operating pressure is 1.0~1.6MPa, operation temperature 30
~60 DEG C, absorbent dosage is 1.0~3.0 times of absorption tower gas-phase feed mass flow.
7. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that the absorption and desorption system includes desorber, desorber operating pressure is 1.0~2.0MPa, tower reactor operation temperature
It is 60~100 DEG C.
8. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that the absorption and desorption system includes depropanizing tower, the depropanizing tower operating pressure is 0.6~1.5MPa, tower reactor
Operation temperature is 70~110 DEG C.
9. methanol and/or the separation of dimethyl ether propylene product and the method using by-product propylene enhancing according to claim 1,
It is characterized in that in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent is more than 2.3%.
10. methanol and/or the separation of dimethyl ether propylene product and the side using by-product propylene enhancing according to claim 9
Method, it is characterised in that in the hydrocarbon mixture product by weight percentage, the content of light dydrocarbon and more heavy constituent be more than
4.2%.
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| WO2000053548A1 (en) * | 1999-03-09 | 2000-09-14 | Bp Chemicals Limited | Process for the production of olefins |
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| 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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| 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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