CN106478349B - Alcohol and/or ether propylene product processing method - Google Patents
Alcohol and/or ether propylene product processing method Download PDFInfo
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- CN106478349B CN106478349B CN201510540714.6A CN201510540714A CN106478349B CN 106478349 B CN106478349 B CN 106478349B CN 201510540714 A CN201510540714 A CN 201510540714A CN 106478349 B CN106478349 B CN 106478349B
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Abstract
The present invention relates to a kind of alcohol and/or ether propylene product processing methods, and energy consumption is high during mainly solving the problems, such as alcohol in the prior art and/or ether production of propylene.The present invention is by using comprising the following steps：Alcohol and/or ether propylene reactor outlet product removal water and sour gas obtain hydrocarbon mixture product；Hydrocarbon mixture product, which is sent into pre-separation tower, removes carbon six and more heavy constituent acquisition light dydrocarbon and more light component；Light dydrocarbon and more light component is sent into absorption and desorption system after being pressurized, is separated into absorption tail gas, three component of carbon, four light dydrocarbon component of carbon；Carbon three components separation is propylene and propane；It absorbs tail gas and four light dydrocarbon component of carbon at least partly returns to the technical solution of alcohol and/or ether propylene reactor, preferably solve 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 ether propylene product processing methods.
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 stone
The increasingly plaque of oily resource is weary, and development is increasingly caused both domestic and external by the technology that the non-oil resources such as coal or natural gas prepare propylene
Pay attention to.Producing synthesis gas from coal is generallyd use by coal propylene, synthesis gas produces methanol, again through the process route of preparing propylene from methanol.Its
It is highly developed that middle producing synthesis gas from coal and synthesis gas produce methanol technics technology.Preparing propylene from methanol technology passes through years development,
Also industrialization is had been realized in.But due to preparing propylene from methanol product complicated composition, product includes that carbon one is even more heavy to carbon seven
Component, the problem that generally existing process flow is long, plant energy consumption is high.How the energy consumption of process for preparing propylene from methanol is reduced, especially
It is the product separation method for developing low energy consumption, becomes the project for needing primary study.
The separation of conventional hydrocarbon-based product generallys use rectifying separation.Typical separation process includes the sequence separation of front-end demethanization
Process, front-end deethanization process and predepropanization process.Such as in CN1431982A patent, methanol to propylene reaction product passes through
After cooling and isolating hydro carbons and water, gas phase hydrocarbon isolates carbon two and more light component and carbon three and more through front-end deethanization process first
Then heavy constituent isolates three component of carbon containing propylene and carbon four and more heavy constituent, due to carbon alkadienes again in depropanizing tower
It can be further converted to propylene in methanol to propylene reaction device with four C_5 olefins of carbon, the carbon two obtained from dethanizer
And more light component and the carbon four obtained from depropanizing tower and the return methanol to propylene reaction device of more heavy constituent part.Traditional hydrocarbon
Class product separation method has that energy consumption is high due to using distillation operation.
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 greater than 3.2MPa, causes regeneration temperature very high, up to 150 DEG C, needs again after solvent reclamation
Cooling down is wanted, it is huge so as to cause 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, the decline of the gas-phase feed load on absorption tower, under absorbent dosage is also corresponding
Drop, therefore, the patent claim the energy consumption of this method 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 causes largely to recombinate due to not cutting out carbon six and more heavy constituent from absorbent
Divide and recycled in absorption and desorption system, energy consumption is still higher.And in process for preparing propylene from methanol, containing a certain amount of in reaction product
Carbon six and more heavy constituent, therefore inevitably have the shortcomings that energy consumption is high using this method.
The prior art has that plant energy consumption is high, and the present invention targetedly solves the above problem.
Summary of the invention
The technical problem to be solved by the present invention is to which the problem of plant energy consumption height, economic effect difference exists in the prior art,
The separation method of a kind of new alcohol and/or ether propylene hydrocarbon product is provided.This method is produced for alcohol and/or ether propylene hydro carbons
Have the advantages that low energy consumption, good economy performance when the separation of object.
To solve the above problems, the technical solution adopted by the present invention is as follows：At a kind of alcohol and/or ether propylene hydrocarbon product
Reason method, comprises the following steps：Alcohol and/or ether propylene reactor outlet obtain hydrocarbon mixture product；Hydrocarbon mixture product is sent
Enter to be separated into carbon six and more heavy constituent and light dydrocarbon and more light component in pre-separation tower；Light dydrocarbon and more light component are sent into suction after being pressurized
Desorption system is received, is separated into and absorbs tail gas, three component of carbon, four light dydrocarbon component of carbon；Carbon three components separation obtains propylene and propane；It inhales
Ending gas and four light dydrocarbon component of carbon at least partly return to alcohol and/or ether propylene reactor.
In above-mentioned technical proposal, it is preferred that alcohol and/or ether are methanol and/or dimethyl ether；It is furthermore preferred that alcohol and/or ether are
Methanol.
In above-mentioned technical proposal, it is preferred that the separation method of a kind of alcohol and/or ether propylene hydrocarbon product, comprising as follows
It is main reaction product that step methanol is converted into propylene in methanol to propylene reaction device, through dehydration and sour gas carbon dioxide
Obtain gas phase hydrocarbon mixture product afterwards, the logistics of gas phase hydrocarbon mixture be separated into pre-separation tower low pressure light dydrocarbon and more light component and
Carbon six and more heavy constituent；Low pressure light dydrocarbon and more light component are sent into after obtaining high pressure carbon five and more light component after compressor boost
Desorber；Three component of carbon produces to obtain depropanizing tower charging from tower reactor in desorber, and whole ethylene is obtained from overhead extraction
Absorption tower charging；In absorption tower, since absorb from the four light dydrocarbon component of carbon of depropanization tower reactor as absorbent in charging third
Alkene, absorbing liquid return to desorber；It absorbs tail gas and absorption and desorption system is discharged, wherein including methane, ethylene, ethane, part is returned
Reactor propylene enhancing, rest part discharge system；Depropanizing tower isolates three component of carbon and carbon four from depropanizing tower charging
Light dydrocarbon component；Three component of carbon isolates polymerization-grade propylene product and propane in propylene rectification tower；Partial four light dydrocarbon component of carbon
Absorption tower is sent into after absorbent cooler is cooling as absorbent, another part Returning reactor propylene enhancing, remaining conduct
The discharge of four light dydrocarbon component of outlet carbon, avoids accumulating in system.
In above-mentioned technical proposal, it is preferred that the pre-separation tower operating pressure is 0.1~1.2MPa, bottom temperature 80
~197 DEG C.
In above-mentioned technical proposal, it is preferred that pressure is 1.3~2.0MPa after the light dydrocarbon and the pressurization of more light component.If
Light dydrocarbon and more light component are gas phases, then can use compressor boost；If light dydrocarbon and more light component are liquid phases, can use
Pump pressurization.
In above-mentioned technical proposal, it is preferred that the absorption and desorption system includes absorption tower, desorber and depropanizing tower.
In above-mentioned technical proposal, it is preferred that the depropanization tower reactor obtains four light dydrocarbon component of carbon, and the four light dydrocarbon component of carbon is extremely
Absorbent of the small part as absorption tower.
In above-mentioned technical proposal, it is preferred that the absorption tower operating pressure be 1.2~1.4MPa, operation temperature be 40~
60 DEG C, absorbent dosage is 1.6~2.6 times of absorption tower gas-phase feed mass flow.
In above-mentioned technical proposal, it is preferred that the desorber operating pressure is 1.4~1.8MPa, and tower reactor operation temperature is
70~90 DEG C.
In above-mentioned technical proposal, it is preferred that the depropanizing tower operating pressure is 0.9~1.2MPa, tower reactor operation temperature
It is 80~100 DEG C.
In above-mentioned technical proposal, it is preferred that in the hydrocarbon mixture product by weight percentage, carbon six and more heavy constituent
Content be greater than 2.0%.
In above-mentioned technical proposal, it is furthermore preferred that in the hydrocarbon mixture product by weight percentage, carbon six and more recombinate
The content divided is greater than 4.0%.
Using method of the invention, when the operating pressure of pre-separation tower is higher than the pressure of hydrocarbon mixture product, using pressure
Contracting machine is sent into pre-separation tower hydrocarbon mixture product booster to after being higher than 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
The method for avoiding carbon six and more heavy constituent to accumulate by removing carbon six and more heavy constituent in absorption and desorption system, but adopt
Used in hydrocarbon mixture product enter absorption and desorption system before directly therefrom remove the method for carbon six and more heavy constituent.Using the present invention
Method, hydrocarbon mixture product is stripped of carbon six and more heavy constituent in pre-separation tower, avoids carbon six and more heavy constituent is being inhaled
The accumulation and circulation in desorption system are received, the temperature of desorption tower reactor and depropanization tower reactor is reduced, to reduce process energy consumption.
Using method of the invention, absorption and desorption system carries 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 40
~60 DEG C, it further reduced the consumption of cooling capacity.It absorbs and contains ethylene, four C_5 olefins of carbon, the suction in the absorption tail gas of tower top
Ending gas can at least partly recycle the charging as alcohol and/or ether propylene reactor.A part of depropanization tower reactor logistics
As the absorbent on absorption tower, carbon four light dydrocarbon component of the another part as absorption and desorption system.The four light dydrocarbon component of carbon is at least
Part returns to methanol aromatic hydrocarbons reactor, and four C_5 olefins of carbon contained therein can effectively improve the propylene of methanol to propylene reaction
Yield.Using method of the invention, the rate of recovery of propylene and propane is 99.99%, and low energy consumption, achieves preferable technology effect
Fruit.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for the invention.
In Fig. 1,1 is hydrocarbon mixture product；2 be low pressure light dydrocarbon and more light component；3 be high pressure carbon five and more light component；4 are
Absorption tower charging；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 light dydrocarbon components；11 be four light dydrocarbon component of outlet carbon；12 be carbon six and more heavy constituent；101 feed for methanol；102 be to return
Absorb tail gas；103 be the four light dydrocarbon component of carbon returned；104 be methanol to propylene reaction product；105 be waste water；R1 is methanol system
Propylene reactor；S1 is gas-liquid separator；T1 is pre-separation tower, and C1 is compressor, and T2 is desorber, and T3 is absorption tower, and T4 is
Depropanizing tower, E1 are absorbent cooler.
As shown in Figure 1, methanol be converted into methanol to propylene reaction device R1 propylene be main reaction product, through dehydration and
Gas phase hydrocarbon mixture product 1 is obtained after sour gas carbon dioxide, the logistics of gas phase hydrocarbon mixture is separated into pre-separation tower T1
Low pressure light dydrocarbon and more light component 2 and carbon six and more heavy constituent 12；Low pressure light dydrocarbon and more light component 2 obtain after compressor C1 pressurization
Desorber T2 is sent into after obtaining high pressure carbon five and more light component 3；Three component of carbon produces to obtain depropanizing tower from tower reactor in desorber
Charging 5, whole ethylene from overhead extraction be absorbed tower charging；In absorption tower, since from four carbon of carbon of depropanization tower reactor
Five components absorb the propylene in charging as absorbent, and absorbing liquid returns to desorber；It absorbs tail gas and absorption and desorption system is discharged,
In include methane, ethylene, ethane, 102 Returning reactor propylene enhancing of partial tail gas, rest part discharge system；Depropanizing tower
Charging isolates four light dydrocarbon component of three component of carbon and carbon in depropanizing tower T4；Three component of carbon isolates polymerization in propylene rectification tower
Grade propylene product and propane；Absorption tower is sent into after partial four light dydrocarbon group lease making absorbent cooler of carbon is cooling as absorbent 6,
Another four light dydrocarbon component of part carbon, 103 Returning reactor propylene enhancing, remaining is discharged as four light dydrocarbon component of outlet carbon.
Fig. 2 is the flow diagram using the above component of light dydrocarbon as absorbent.
In Fig. 2,1 is hydrocarbon mixture product；2 feed for desorber；3 feed for absorption tower；4 feed for depropanizing tower；6 are
Absorbent；7 be absorption tail gas；8 be absorbing liquid；9 be three carbon of carbon, four component；5 be light dydrocarbon and more heavy constituent；10 for outlet light dydrocarbon and
More heavy constituent；11 be three component of carbon；12 be four component of carbon；C1 is compressor；T1 is desorber；T2 is absorption tower；T3 is de- fourth
Alkane tower；E1 is absorbent cooler；T4 is depropanizing tower.
The process flow of Fig. 2 is as follows：It is main reaction product, warp that methanol is converted into propylene in methanol to propylene reaction device
Gas phase hydrocarbon mixture product 1 is obtained after dehydration and sour gas carbon dioxide.Gas phase hydrocarbon logistics 1 through compressor C1 pressurization after,
It is sent into desorber T1.Desorber T1 tower reactor extraction debutanizing tower charging 4, whole ethylene from overhead extraction be absorbed tower into
Material 3.In the T2 of absorption tower, since from the part light dydrocarbon of debutanization tower reactor and more heavy constituent 5 as absorbent 6 absorb propylene, inhale
It receives liquid 8 and returns to desorber T1.It absorbs tail gas 7 and absorption and desorption system is discharged.Debutanizing tower charging 4 is separated into debutanizing tower T3
Three carbon of carbon, four component 9 and light dydrocarbon and more heavy constituent 5.Three carbon of carbon, four component 9 isolates three component of carbon, 11 He in depropanizing tower T4
Four component 12 of carbon.Three component 11 of carbon obtains polymerization-grade propylene product and propane through propylene rectifying.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
Fig. 1 is shown in process flow.It is main reaction product that methanol is converted into propylene in methanol to propylene reaction device, through being dehydrated
With acquisition gas phase hydrocarbon logistics 1 after sour gas carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.13MPa,
Mole group becomes 18.7% carbon one to two component of carbon, 45.9% carbon, three component, 27.5% carbon, four light dydrocarbon component, 7.9% carbon six and
More heavy constituent.Gas phase hydrocarbon logistics 1 is separated into low pressure light dydrocarbon and more light component 2 and carbon six and more heavy constituent in pre-separation tower T1
12.Low pressure light dydrocarbon and more light component 2 are pressurized to after 2MPa obtains high pressure carbon five and more light component 3 by compressor C1 and are sent into desorption
Tower T2.Three component of carbon of 70.5% mass fraction produces to obtain depropanizing tower charging 5, whole ethylene from tower reactor in desorber
From overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since from the four light dydrocarbon component 6 of carbon of depropanization tower reactor as inhaling
It receives agent and absorbs the propylene fed in 4, absorbing liquid 8 returns to desorber T2.The absorption tail gas of 50% volume fraction returns to methanol system third
Alkene reaction device, includes methane, ethylene, four light dydrocarbon alkane alkene of carbon in the absorption tail gas 102 of return, wherein alkene in the reactor into
One step is converted into propylene.Remaining absorbs tail gas and absorption and desorption system is discharged, and can be further separated out ethylene product or as combustion
Material.Depropanizing tower T4 isolates four light dydrocarbon component 10 of three component 9 of carbon and carbon from charging 5.Three component 9 of carbon is in propylene rectification tower
Isolate polymerization-grade propylene product and propane.The depropanization tower reactor logistics of 10% mass fraction is as the four light dydrocarbon component of carbon returned
103 Returning reactor R1 propylene enhancings, rest part is as four light dydrocarbon component 10 of carbon.The four light dydrocarbon component of carbon of 88% mass fraction
10 are sent into absorption tower as absorbent after absorbent cooler E1 is cooled to 40 DEG C, and rest part is as four light dydrocarbon group of outlet carbon
Divide 11 discharges.The process flow 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.In table energy consumption be compressor, pump, heat exchanger, rectifying column energy consumption summation.Under
Together.
【Embodiment 2】
Using with the identical process flow of embodiment 1.It is key reaction that propylene is converted into methanol to propylene reaction device
Product is dehydrated and obtains gas phase hydrocarbon logistics 1 after sour gas carbon dioxide.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure
For 0.12MPa, mole group becomes 22.3% carbon one to two component of carbon, 46.4% carbon, three component, 24.3% carbon, four light dydrocarbon component,
7.0% carbon six and more heavy constituent.Gas phase hydrocarbon logistics 1 is separated into pre-separation tower T1 after compressor boost to 0.55MPa
Low pressure light dydrocarbon and more light component 2 and carbon six and more heavy constituent 12.Low pressure light dydrocarbon and more light component 2 are pressurized to by compressor C1
1.5MPa is sent into desorber T2 after obtaining high pressure carbon five and more light component 3.Three groups of the carbon of 72.7% mass fraction in desorber
Point produce to obtain depropanizing tower charging 5 from tower reactor, whole ethylene is absorbed tower charging 4 from overhead extraction.In absorption tower T3
In, since from the four light dydrocarbon component 6 of carbon of depropanization tower reactor as absorbent absorb the propylene in charging 4, absorbing liquid 8 returns to desorption
Tower T2.The absorption tail gas of 60% volume fraction returns to methanol to propylene reaction device, in the absorption tail gas 102 of return comprising methane,
Ethylene, four light dydrocarbon alkane alkene of carbon, wherein alkene is further converted to propylene in the reactor.Remaining absorbs tail gas discharge and absorbs solution
Desorption system can be further separated out ethylene product or as fuel.Depropanizing tower T4 isolates three component 9 of carbon from charging 5
With four light dydrocarbon component 10 of carbon.Three component 9 of carbon isolates polymerization-grade propylene product and propane in propylene rectification tower.5% mass point
Several depropanization tower reactor logistics is as four light dydrocarbon component of carbon, the 103 Returning reactor R1 propylene enhancing returned, rest part conduct
Four light dydrocarbon component 10 of carbon.The four light dydrocarbon component 10 of carbon of 92% mass fraction is sent into suction after absorbent cooler E1 is cooled to 40 DEG C
Tower is received as absorbent 6, rest part is discharged as four light dydrocarbon component 11 of outlet carbon.The process flow 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.
【Embodiment 3】
Using with the identical process flow of embodiment 1.Dimethyl ether is converted into propylene in dimethyl ether propylene reactor
Key reaction product is dehydrated and obtains gas phase hydrocarbon logistics 1 after sour gas carbon dioxide.1 temperature of gas phase hydrocarbon logistics is
43 DEG C, pressure 0.14MPa, mole group becomes 21.5% carbon one to two component of carbon, 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 light dydrocarbon and lighter group in pre-separation tower T1
Points 2 and carbon six and more heavy constituent 12.Low pressure light dydrocarbon and more light component 2 are pressurized to 1.7MPa by compressor C1 and obtain high pressure carbon five
And desorber T2 is sent into after more light component 3.Three component of carbon of 72.9% mass fraction is produced from tower reactor in desorber is taken off
Propane tower charging 5, whole ethylene from overhead extraction be absorbed tower charging 4.In the T3 of absorption tower, since from depropanization tower reactor
Four light dydrocarbon component 6 of carbon as absorbent absorb charging 4 in propylene, absorbing liquid 8 return desorber T2.70% volume fraction
It absorbs tail gas and returns to methanol to propylene reaction device, include methane, ethylene, four light dydrocarbon alkane alkene of carbon in the absorption tail gas 102 of return,
Wherein alkene is further converted to propylene in the reactor.Remaining absorbs tail gas and absorption and desorption system is discharged, and can further divide
Separate out ethylene product or as fuel.Depropanizing tower T4 isolates four light dydrocarbon component 10 of three component 9 of carbon and carbon from charging 5.Carbon
Three components 9 isolate polymerization-grade propylene product and propane in propylene rectification tower.The depropanization tower reactor logistics of 3% mass fraction is made
For four light dydrocarbon component of carbon, the 103 Returning reactor R1 propylene enhancing of return, rest part is as four light dydrocarbon component 10 of carbon.89% matter
The four light dydrocarbon component 10 of carbon of amount score is sent into absorption tower as absorbent 6 after absorbent cooler E1 is cooled to 40 DEG C, remaining
Part is discharged as four light dydrocarbon component 11 of outlet carbon.
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.The process flow propylene recovery rate 99.99%.
【Embodiment 4】
Using with the identical process flow of embodiment 1, with the first of the dimethyl ether of 50% mass fraction and 50% mass fraction
Alcohol is raw material, and being converted into propylene through methanol to propylene reaction device is main reaction product, through dehydration and sour gas carbon dioxide
Gas phase hydrocarbon logistics 1 is obtained afterwards.1 temperature of gas phase hydrocarbon logistics is 43 DEG C, pressure 0.14MPa, and mole group becomes 19.7% carbon
One to two component of carbon, 46.8% carbon, three component, 31.2% carbon, four light dydrocarbon component, 2.3% carbon six and more heavy constituent.Gas phase hydrocarbon object
Stream 1 is separated into low pressure light dydrocarbon and more light component 2 and carbon six and more heavy constituent 12 in pre-separation tower T1.Low pressure light dydrocarbon and lighter group
2 are divided to be sent into desorber after compressor C1 is pressurized to 1.7MPa.In desorber three component of carbon of 70.3% mass fraction from
Tower reactor produces to obtain depropanizing tower charging 5, and whole ethylene is absorbed tower charging 4 from overhead extraction.In the T3 of absorption tower, with
Four light dydrocarbon component 6 of carbon from depropanization tower reactor absorbs the propylene in charging 4 as absorbent, and absorbing liquid 8 returns to desorber T2.
The absorption tail gas of 80% volume fraction returns to methanol to propylene reaction device, in the absorption tail gas 102 of return comprising methane, ethylene,
Four light dydrocarbon alkane alkene of carbon, wherein alkene is further converted to propylene in the reactor.Remaining absorbs tail gas and absorption and desorption system is discharged
System, can be further separated out ethylene product or as fuel.Depropanizing tower T4 isolates three component 9 of carbon and carbon from charging 5
Four light dydrocarbon components 10.Three component 9 of carbon isolates polymerization-grade propylene product and propane in propylene rectification tower.1% mass fraction
The logistics of depropanization tower reactor is as four light dydrocarbon component of carbon, the 103 Returning reactor R1 propylene enhancing returned, and rest part is as carbon four
Light dydrocarbon component 10.The four light dydrocarbon component 10 of carbon of 85% mass fraction is sent into absorption tower after absorbent cooler E1 is cooled to 40 DEG C
As absorbent 6, rest part is discharged as four light dydrocarbon component 11 of outlet carbon.The process flow 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.
Table 1
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Comparative example 1 | Comparative example 2 | |
| Pre-separation tower operating pressure | 0.12 | 0.55 | 0.8 | 1.3 | - | - |
| Pre-separation tower top operation temperature | -13 | 21 | 41 | 56 | - | - |
| Pre-separation tower reactor operation temperature | 89 | 143 | 174 | 197 | - | - |
| Absorptive tower absorbent dosage | 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 |
| Desorb 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) | 0.164 | 0.163 | 0.188 | 0.185 | 0.216 | 0.251 |
【Comparative example 1】
Fig. 2 is shown in process flow.Using with the identical hydrocarbon mixture product of embodiment 1, after compressor boost to 1.6MPa,
It is sent into desorber T1.Desorber operating pressure 1.5MPa, 40 DEG C of tower top temperature, 96 DEG C of bottom temperature.In desorber T1
Three component of carbon of 73.2% mass fraction produces to obtain debutanizing tower charging 4 from tower reactor, and whole ethylene is obtained from overhead extraction
Absorption tower charging 3.Absorption tower operating pressure 1.2MPa absorbs 56 DEG C of temperature.In the T2 of absorption tower, since from debutanization tower reactor
Light dydrocarbon and more heavy constituent 5 absorb the propylene in charging 3 as absorbent, and absorbing liquid 8 returns to desorber T1.Tail gas 7 is absorbed to be discharged
Absorption and desorption system.Debutanizing tower charging 4 is separated into three carbon of carbon, four component 9 and light dydrocarbon and more heavy constituent 5 in debutanizing tower T3,
Debutanizing tower operating pressure 1.2MPa, 41 DEG C of tower top temperature, 165 DEG C of bottom temperature.Three carbon of carbon, four component 9 is in depropanizing tower T4
Isolate four component 12 of three component 11 of carbon and carbon, depropanizing tower operating pressure 1.15MPa, 25 DEG C of tower top temperature, bottom temperature 81
℃.Three component 11 of carbon obtains polymerization-grade propylene product and propane through propylene rectifying.The light dydrocarbon of 85% mass fraction and more heavy constituent 5
Absorption tower is sent into after absorbent cooler E1 is cooled to 40 DEG C as absorbent 6, rest part discharge system.The process flow
Energy consumption be higher than the energy consumption of Examples 1 to 4 mainly due in absorbent containing the heavier component of six or more carbon, desorber,
The tower reactor energy consumption of debutanizing tower is high.The energy consumption of comparative example 1 is shown in Table 2.
【Comparative example 2】
Using with the identical hydrocarbon mixture product of embodiment 1, using those skilled in the art be readily apparent that oil absorb work
Skill process is not provided with pre-separation tower and depentanizer is arranged in absorption and desorption system, make in absorbent not carbon containing six and more
Heavy constituent.The energy consumption of the process flow is higher than the energy consumption of embodiment and comparative example 1, exists in main cause absorption and desorption system big
The absorbent of amount recycles, and depentanizer feed loading is big, and the carbon six of relatively small amount is separated from a large amount of four light dydrocarbon absorbent of carbon
Need a large amount of energy.
【Comparative example 3】
Front-end deethanization point is sent into after compressor boost to 1.6MPa using with the identical hydrocarbon mixture product of embodiment 1
From system, successively through dethanizer, depropanizing tower, depentanizer, carbon two and more light component, three component of carbon, four light dydrocarbon of carbon are obtained
Component and carbon six and more heavy constituent.Due to having used -40 DEG C of cryogenic coolants below, cooling capacity energy consumption is high for the process flow, causes
Total energy consumption is higher.The energy consumption of this comparative example is that 0.229kg marks oil/kg propylene.
【Comparative example 4】
Predepropanization point is sent into after compressor boost to 1.6MPa using with the identical hydrocarbon mixture product of embodiment 1
Carbon two and more light component, three component of carbon, four light dydrocarbon component of carbon are obtained through depropanizing tower, dethanizer, depentanizer from system
With carbon six and more heavy constituent.The process flow is also needed using -40 DEG C of cryogenic coolants below, and cooling capacity energy consumption is high, is caused total
Energy consumption it is higher.The energy consumption of this comparative example is that 0.227kg marks oil/kg propylene.
Claims (10)
1. a kind of methanol and/or dimethyl ether propylene product processing method, comprise the following steps：Methanol and/or dimethyl ether third
Alkene reaction device exports to obtain hydrocarbon mixture product；Hydrocarbon mixture product be sent into pre-separation tower be separated into carbon six and more heavy constituent and
Light dydrocarbon and more light component；Light dydrocarbon and more light component is sent into absorption and desorption system after being pressurized is separated into and absorbs tail gas, three groups of carbon
Divide, four light dydrocarbon component of carbon；Carbon three components separation obtains propylene and propane；It absorbs tail gas and four light dydrocarbon component of carbon at least partly returns
Methanol and/or dimethyl ether propylene reactor.
2. methanol and/or dimethyl ether propylene product processing method according to claim 1, it is characterised in that the pre-separation
Tower operating pressure is 0.12~1.3MPa, and bottom temperature is 85~200 DEG C.
3. methanol and/or dimethyl ether propylene product processing method according to claim 1, it is characterised in that the light dydrocarbon and
Pressure is 1.4 to 1.9MPa after the pressurization of more light component.
4. methanol and/or dimethyl ether propylene product processing method according to claim 1, it is characterised in that the absorption solution
Desorption system includes absorption tower, desorber and depropanizing tower.
5. methanol and/or dimethyl ether propylene product processing method according to claim 4, it is characterised in that from described de- third
Alkane tower reactor obtains four light dydrocarbon component of carbon, absorbent of the four light dydrocarbon component of carbon at least partly as absorption tower.
6. methanol and/or dimethyl ether propylene product processing method according to claim 4, it is characterised in that the absorption tower
Operating pressure is 1.2~1.4MPa, and operation temperature is 40~60 DEG C, and absorbent dosage is absorption tower gas-phase feed mass flow
1.5~2.8 times.
7. methanol and/or dimethyl ether propylene product processing method according to claim 4, it is characterised in that the desorber
Operating pressure is 1.4~1.8MPa, and tower reactor operation temperature is 70~90 DEG C.
8. methanol and/or dimethyl ether propylene product processing method according to claim 4, it is characterised in that the depropanization
Tower operating pressure is 0.9~1.2MPa, and tower reactor operation temperature is 80~100 DEG C.
9. methanol and/or dimethyl ether propylene product processing method according to claim 1, it is characterised in that the hydrocarbon mixture
In class product by weight percentage, the content of carbon six and more heavy constituent is greater than 2.2%.
10. methanol and/or dimethyl ether propylene product processing method according to claim 9, it is characterised in that the mixing
In hydrocarbon product by weight percentage, the content of carbon six and more heavy constituent is greater than 4.2%.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000053548A1 (en) * | 1999-03-09 | 2000-09-14 | Bp Chemicals Limited | Process for the production of olefins |
| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
| CN103880577A (en) * | 2014-03-20 | 2014-06-25 | 中国石油集团东北炼化工程有限公司吉林设计院 | Reaction product separation system for production of propylene and olefins by using methanol |
| CN203794811U (en) * | 2014-03-20 | 2014-08-27 | 中国石油集团东北炼化工程有限公司吉林设计院 | Reaction product separation system for methanol-to-propylene and methanol-to-olefin |
-
2015
- 2015-08-28 CN CN201510540714.6A patent/CN106478349B/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 |
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