CN107602331A - A kind of separation method of methanol to olefins reaction gas - Google Patents
A kind of separation method of methanol to olefins reaction gas Download PDFInfo
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- CN107602331A CN107602331A CN201610546037.3A CN201610546037A CN107602331A CN 107602331 A CN107602331 A CN 107602331A CN 201610546037 A CN201610546037 A CN 201610546037A CN 107602331 A CN107602331 A CN 107602331A
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Abstract
The present invention relates to methanol-to-olefins field, discloses a kind of separation method of methanol to olefins reaction gas, and this method includes：Methanol to olefins reaction gas is passed through in compression unit and is compressed processing；The gas phase that compression handles to obtain is cooled down；In the presence of absorbent, the gas-liquid two-phase obtained after cooling is subjected to demethanation processing in domethanizing column；The tower kettle product that demethanation is handled to obtain carries out depropanization processing in depropanizing tower；Deethanization processing is carried out after the overhead product of depropanization processing is dried in dethanizer, the gaseous pressure that the compression processing obtains is 3.2 6.0MPa, and described to be cooled to 10 30 DEG C of temperature, the absorbent is gasoline.The method of the present invention by the use of gasoline component as absorbent methanol removal olefine reaction gas in the light components such as methane, be capable of the purity and the rate of recovery of significantly ethene and propylene, and system energy consumption can be significantly reduced.
Description
Technical field
The present invention relates to methanol-to-olefins field, in particular it relates to a kind of separation method of methanol to olefins reaction gas.
Background technology
For China's energy resource structure based on coal, coal is used as China's basic energy resource and important industrial chemicals for a long time.Modern coalification
Work is the important directions that coal high-efficiency clean conversion utilizes based on clean coal technology.2014, China produced ethylene volume per year
Through increasing to more than 1,700 ten thousand tons.National economy relies primarily on oil to the wilderness demand of ethene and propylene, makes China's oil average annual
Consumption figure is improved to more than 500,000,000 tons.Using the Modern Coal-based Chemical that coal-to-olefin technology is representative without suspected of national economy and social hair
Exhibition provides important support, and has ensured the needs of national energy security.The breakthrough of preparing low carbon olefinic hydrocarbon with methanol technology and its
Industrialization, indicate that China has been enter into world lead level in the field.
Methanol-to-olefins complete set technology is made up of reaction technology and isolation technics.Reaction technology is with catalyst preparation and reaction
Device exploitation is designed as core；Isolation technics produces poly- then using reaction product as raw material through processes such as impurity removal, compression, separation
The ethene and propylene product of level are closed, its core is the exploitation and design of impurity removal and separation process.
The separating technology that polymer grade ethylene and propylene are obtained from methanol-to-olefins (MTO/DMTO) product gas is generally divided into
Four units：Compression unit, imurity-removal unit, cold separative element and thermal release unit.Wherein, compression unit main task is
(MTO/DMTO) product gas is improved to pressure needed for subsequent technique.Imurity-removal unit main task is removing (MTO/DMTO)
Unreacting material such as methanol in product gas, intermediate reaction product such as dimethyl ether (DME), sour gas such as carbon dioxide, NOxDeng,
Which part impurity can be removed through operations such as washing, alkali cleanings between compressor section according to required operating condition difference.Cold separation
Unit is the separative element of the temperature range below 0 DEG C, such as demethanation, deethanization and ethylene distillation process.Thermal release work
Skill is the separative element of the temperature range more than 0 DEG C, including the process such as depropanization, propylene rectifying.
The removal of light components methane in impurity is to obtain the key of high-purity polymer grade ethylene.It is commonplace at this stage
Method be separation by deep refrigeration and absorption and separation method.Patent application CN200810201217.3 discloses a kind of MTO/MTP reactions
The separation method of light hydrocarbon product in product, this method is using ethane as absorbent successively by absorption tower and domethanizing column two-stage
Absorption process excludes the light components in product, and chilling temperature is about -65 DEG C, and 90%- can be obtained finally by rectifying
99.99% ethene.It is relatively low using the absorption temperature required for ethane as absorbent, -100 DEG C of second is needed in engineer applied
Alkene refrigerant condenser, even -135 DEG C of methane compressor provide cold, improve the investment of equipment and add energy consumption.
Patent application CN201110279313.1 discloses a kind of low-carbon separation of hydrocarbons and methanol-to-olefins (M-OS/MTO)
Gas separating technology flow, this method is using front-end demethanization tower, depropanizing tower and debutanizing tower tower reactor effluent as absorbent
The carbon two and the component of carbon three in product gas are absorbed, the light fractions such as methane are separated from product gas.This method is needed -40
DEG C or so temperature demethanation, and this method is front-end deethanization.
Patent application CN201310216950.3 disclose in a kind of product gas from MTO/DMTO reclaim ethene system and
Method, this method set up cold recovery device after domethanizing column, reduce system energy consumption, and Recovery rate of ethylene is more than
99.7%, but ice chest is needed, energy consumption is larger.
Patent application WO2009/015507 discloses a kind of side of preparing low-carbon olefin of polymerization-grade of pyrolysis gas separation of methanol
Method, this method removes methane using the method for absorption and separation, but technique minimum temperature is -91 DEG C or so, and energy consumption is also larger.
The method disclosed in the above-mentioned patent document demethanation process is carried out below 0 DEG C, and be front-end deethanization or
Propane, therefore, methane and other lighter hydrocarbons such as ethane, ethene and propylene etc. can be caused easily to form hydrocarbon hydrate with water, it is this kind of
Hydrate easily makes valve and pipeline that the phenomenon of frozen block occur below 0 DEG C, and the energy consumption of above-mentioned each method is also larger.
The content of the invention
The invention aims to overcome the method energy consumption for separating methanol to olefins reaction gas in the prior art larger, easily
A kind of the defects of causing line clogging etc., there is provided separation method of methanol to olefins reaction gas.
To achieve these goals, the invention provides a kind of separation method of methanol to olefins reaction gas, this method bag
Include：
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed processing；
(2) gas phase that compression handles to obtain is cooled down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is subjected to demethanation processing in domethanizing column；
(4) tower kettle product for handling to obtain by demethanation carries out depropanization processing in depropanizing tower；
(5) deethanization processing is carried out in dethanizer after the overhead product of depropanization processing is dried；
Wherein, the gaseous pressure that the compression processing obtains is 3.2-6.0MPa, and step is cooled to temperature in (2)
10-30 DEG C, the absorbent is gasoline, and the condition of the demethanation processing includes：Domethanizing column number of theoretical plate is 20-60 blocks,
Operating pressure is 3.0-5.8MPa, and tower top temperature is 10-40 DEG C, and bottom temperature is 40-120 DEG C.
Methanol-to-olefins (MTO/DMTO) reaction gas separation method of the present invention has advantages below：
(1) in method of the invention, absorbent methanol removal alkene (MTO/DMTO) reaction gas is used as using gasoline component
In light components, the raw sorbent such as methane be readily available, cost is cheap；
(2) methane in operation temperature section methanol removal alkene (MTO/DMTO) product gas more than 10 DEG C and
Light fraction, water and hydro carbons is effectively inhibited to form hydrate；
(3) in method of the invention, drying process need not be placed on compression unit outlet, it is only necessary to dethanizer tower
Processing is dried in top gas, avoids and compression unit outlet liquid phase lime set is dried, significantly reduce public work nitrogen
The consumption and energy consumption of gas；
(4) in method of the invention, overall process minimum temperature is not less than -40 DEG C, it is not necessary to uses ethylene refrigeration unit, material
In general low temperature carbon steel can be selected in material, and energy consumption is low, reduces investment outlay；
(5) method of the invention can obtain the very high polymer grade ethylene of purity and propylene product, and Recovery rate of ethylene is
More than 80%, propylene recovery rate is more than 95%.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Fig. 1 is a kind of compression process flow chart of embodiment of the present invention.
Fig. 2 is a kind of methanol to olefins reaction qi leel separating process flow chart of embodiment of the present invention.
Embodiment
The embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The end points of disclosed scope and any value are not limited to the accurate scope or value herein, these scopes or
Value should be understood to comprising the value close to these scopes or value.For number range, between the endpoint value of each scope, respectively
It can be combined with each other between the endpoint value of individual scope and single point value, and individually between point value and obtain one or more
New number range, these number ranges should be considered as specific open herein.
Pressure in the present invention refers to absolute pressure.
The reaction gas of methanol-to-olefins (MTO/DMTO) reactor is per se with a large amount of saturation waters, and subtractive process
The operation such as alkali cleaning and washing is commonly used, this to contain a large amount of saturation waters in the material of separation process.Existing demethanation process
Operation temperature below 0 DEG C, operating pressure is more than 2.0MPa.Under the conditions of this, methane and other lighter hydrocarbons such as ethane, ethene and
Propylene etc. easily forms hydrocarbon hydrate with water, and this kind of hydrate easily makes valve and pipeline that frozen block phenomenon occur below 0 DEG C.
So typically drying process is needed just to enter later separation after compression unit in methanol-to-olefins (MTO/DMTO) reaction gas
Unit.Select in compression unit port of export dry feedstock gas be due to traditional methanol-to-olefins product gas separating technology one
As be since deethanization process.Ethane and more light component are separated from unstripped gas first, cause methane, one in this case
The component of natural gas such as carbonoxide, nitrogen need to take off in the ethene of relative lightweight, ethane from product gas in follow-up separation process
Remove, and this process is completed in the cold separation process below 0 DEG C, is satisfied so having to remove in the compression unit port of export
And water.
The optimization of heat-exchange network is detrimental to by another problem for the product gas elder generation deethanization dried and compressed.Because
The operating pressure of general dethanizer is 2.5MPa or so, and tower top operation temperature is -20 DEG C or so, and tower reactor operation temperature is 65 DEG C
Left and right.Deethanizer overhead gas starts de- ethene and demethanation process, tower reactor liquid into cold separative element and enters thermal release
Unit starts depropanization process.The pressure of the cold separation process of de- ethene and demethanation is typically in 2.3MPa or so, operation temperature
It is for -35 DEG C and following.In order to avoid deep cooling process needs to use the tower bottoms of depropanizing tower as absorbent.The behaviour of depropanizing tower
Make pressure as 1.5MPa or so, tower top operation temperature is 45 DEG C or so, and tower reactor operation temperature is 90 DEG C or so.So system needs
The tower bottoms of 90 DEG C or so depropanizing towers is cooled to the temperature range of -35 DEG C of temperature below.And the need in thermal release unit
The logistics to be heated and the temperature difference of depropanizing tower tower bottoms are smaller, are unfavorable for heat recovery and utilization, and need input a large amount of cold
Amount.
Therefore, in order to overcome the existing drawbacks described above because of first deethanization in the prior art, the invention provides one kind
The separation method of methanol to olefins reaction gas, this method include：
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed processing；
(2) gas phase that compression handles to obtain is cooled down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is subjected to demethanation processing in domethanizing column；
(4) tower kettle product for handling to obtain by demethanation carries out depropanization processing in depropanizing tower；
(5) deethanization processing is carried out in dethanizer after the overhead product of depropanization processing is dried；
Wherein, the gaseous pressure that the compression processing obtains is 3.2-6.0MPa, and step is cooled to temperature in (2)
10-30 DEG C, the absorbent is gasoline, and the condition of the demethanation processing includes：Domethanizing column number of theoretical plate is 20-60 blocks,
Operating pressure is 3.0-5.8MPa, and tower top temperature is 10-40 DEG C, and bottom temperature is 40-120 DEG C.
In the present invention, hydrogen, nitrogen, oxynitrides, carbon monoxide, dioxy can be contained in methanol to olefins reaction gas
Change carbon, dimethyl ether, water, methane, methanol, ethane, ethene, acetylene, propane, propylene, allene, normal butane, iso-butane, 1- fourths
Alkene, 2- butylene, 1,3- butadiene, cis-2-butene, Trans-2-butene, pentane, isopentane, 1- amylenes, n-hexane, isohexane,
Hexene, benzene, toluene, paraxylene, meta-xylene, ortho-xylene and 1,3,5- trimethylbenzenes.Wherein, the content of ethene can be
25-95 moles of %, the content of propylene can be 5-49 moles of %, and the content of methane can be 0-10 moles of %, the content of hydrogen
Can be 0-10 moles of %, the total content of other components can be 0-30 moles of %.
According to method of the present invention, it is preferable that in step (1), the compression unit includes 3-5 section compressor sections,
Methanol to olefins reaction gas pressure after compression unit compression processing rises to 3.2-6.0MPa step by step.Wherein, compressor
Every section of outlet temperature of section is usually no more than 140 DEG C according to technological requirement, and every section of inlet temperature is 40 DEG C or so, generally use 25-
35 DEG C of circulating waters.
According to method of the present invention, it is preferable that alkali cleaning and washing are carried out during the compression is handled, its
In, the order for washing alkali cleaning does not specially require, when sour gas is more in unstripped gas, can first alkali cleaning wash again, work as original
When expecting that methanol, dimethyl ether etc. are more in gas, can first it wash again alkaline.According to method of the present invention, it is highly preferred that described
Alkali cleaning and washing are carried out under 0.3-3.0MPa operating pressures.Usually, alkali cleaning and water-washing step can be in 1-3 section compressors
Section exit is carried out.
In the present invention, washing is to remove the organic oxygen compound in unstripped gas, such as methanol, dimethyl ether.It is general to use
Demineralized water is sprayed into tower from washing column overhead and fully contacted with unstrpped gas.Different according to operating pressure, water-washing process is possible to
A part of hydrocarbon component in unstripped gas can be absorbed, therefore, can first be reclaimed using existing known technology wherein most methanol and
After DME, the methods of passing through stripping, reclaims hydrocarbons therein, and the hydrocarbons then are returned into compression unit again.Wherein, water
Technique is washed as the conventional technique in this area.
In the present invention, alkali cleaning is to remove the sour gas such as the carbon dioxide in unstripped gas.Alkali lye is typically used from alkali
Wash in column overhead penetrating tower and fully contacted with unstrpped gas.Caustic wash tower has neutralizing treatment section and washing section, and caustic wash tower overhead gas enter
Enter compression unit.Wherein, alkali washing process is the conventional technique in this area.
In the present invention, due to containing a large amount of saturation waters in methanol-to-olefins (MTO/DMTO) reaction gas, gone back between compressor section
Need to carry out the operation such as alkali cleaning and washing, as the rise of pressure and the reduction of chilling temperature may produce aqueous phase lime set, or
Person contains the three-phase effluent of gas phase, aqueous phase and oil phase.Wherein gaseous component is the hydrocarbons containing a small amount of saturation water, aqueous phase
It is the water containing very small amount hydrocarbons, oil phase is the hydrocarbons containing C2-C5 heavier components.Every section of compressor section produces water
The entrance of the preceding paragraph compressor section mutually can be returned, and is ultimately delivered to stripper recovery hydrocarbons and avoids significant loss.Compression
The intersegmental gas of process can enter depropanizing tower after the pressurization of caused oil phase after cooling, compressor outlet gas institute after cooling
Caused oil phase can enter domethanizing column.
According to method of the present invention, it is preferable that in step (2), be cooled to temperature as 15-20 DEG C.Original after cooling
Expect that gas is gas-liquid two-phase, it is not necessary to which drying can be sent directly into domethanizing column.Wherein, refrigerant used can be 5 DEG C or so
Cold water, cold water can provide by lithium-bromide absorption-type refrigerating machine.And lithium bromide refrigerator is using absorption refrigeration technology, with
The waste hot steam of factory is thermal source, has the advantages of energy consumption is low.
According to method of the present invention, in step (3), the absorbent is gasoline, predominantly C5-C8 hydro carbons and its is spread out
Biological and a small amount of more than C8 heavy constituents.The various gasoline that the gasoline can be known in the art, such as its performance can include：
Initial boiling point is 25-55 DEG C, is done as 120-250 DEG C, sulfur content is less than 50ppm, and it can come from light naphthar, scheelite brain
At least one in oil, catalytic reforming gasoline, catalytically cracked gasoline, fluid catalytic cracking FCC gasoline, coal liquifaction and biogasoline
Kind, but it is several to be not limited to the above.Preferably, the gasoline contains C6-C7 components, and C6-C7 components account for the 10- of gasoline gross weight
60%, and the sulfur content of gasoline is less than 50ppm, so as to improve assimilation effect.
The dosage of absorbent is not specially required in the present invention, for example, the dosage of absorbent after step (2) cooling with obtaining
The mol ratio of the gas-liquid two-phase arrived can be 1:10 to 10:1, preferably 1:5 to 5:1, more preferably 1:4 to 4:1.The gas-liquid
Two-phase refers to that the methanol to olefins reaction gas contains gas phase and liquid phase while compressed processing and cooling obtain afterwards successively
Mixture.Correspondingly, the mole of the gas-liquid two-phase refers to the total moles of gaseous substance and liquid phase substance in the mixture
Amount.
According to method of the present invention, wherein, the absorption temperature more low absorption effect of absorbent is better, i.e. domethanizing column
Tower top C2 and the loss of more heavy constituent are fewer, but energy consumption is higher, it is preferable that the temperature of the absorbent is 10-30 DEG C, most preferably
For 15-20 DEG C.
According to method of the present invention, wherein, domethanizing column can be divided into absorber portion and stripping section.The effect of absorber portion
It is to absorb the C2 and more heavy constituent in gas phase, reduces the C2 constituent contents in the light components such as tower top methane, it is preferable that demethanation
Tower absorber portion can increase intercooler to ensure assimilation effect, it is highly preferred that the temperature of intercooler is 10-30 DEG C,
Most preferably 15-20 DEG C.The effect of stripping section is to control the methane content in tower bottoms, and methane content is more low more advantageously ensures that
The purity of final obtained ethylene product.But increased as domethanizing column tower reactor methane content reduces bottom temperature, tower
Push up the C2 of loss and more heavy constituent is consequently increased, methane content control is in 1-10000ppm preferably in tower bottoms.
According to method of the present invention, in step (3), it is preferable that carry out the overhead product that demethanation handles to obtain
Pressure swing adsorption hydrogen production hydrogen manufacturing, obtains hydrogen.The overhead product that specifically demethanation can be handled to obtain is passed through in surge tank again
Hydrogen and methane are prepared using pressure swing adsorption hydrogen production technology.Pressure swing adsorption hydrogen production technology is known in the art technology, herein no longer
Repeat.The purity of the isolated hydrogen of the present invention is 99-99.999%.Pressure swing adsorption hydrogen production abbreviation PSA hydrogen manufacturing.
According to method of the present invention, in step (4), the condition of depropanization processing can be conventional de- third in this area
Alkane condition, it is preferable that the condition of the depropanization processing includes：Depropanizing tower number of theoretical plate is 15-50 blocks, and operating pressure is
1.5-3.5MPa, tower top temperature are 10-50 DEG C, and bottom temperature is 100-160 DEG C, is finally recovered so as to further improve
The ethene and the rate of recovery of propylene arrived.
According to method of the present invention, in step (4), depropanizing tower tower top is mainly C2 and C3 components, and tower reactor is main
Contain a small amount of C3 components simultaneously for C4 and more heavy constituent, depropanizing tower top gaseous phase is due to being entrained with a certain amount of C4 and heavier
Component, so needing cooling to make its backflow, tower top temperature can be controlled in the range of 10-50 DEG C, be preferably controlled in 15-35 DEG C of model
In enclosing.Wherein, the content of depropanizing tower tower reactor major control C3 components, the content of C3 components is lower in tower reactor, the C2 of system and
The rate of recovery of C3 components is higher, while bottom temperature is higher；Bottom temperature is higher, and tower top C4 entrainment is higher, and required energy consumption is got over
It is high.Therefore, the molar content of tower reactor C3 components can be controlled in the range of 1-25%, preferably in the range of 5-20%.
According to method of the present invention, in step (4), it is preferable that handle to obtain tower bottoms as piptonychia using depropanization
The absorbent of alkane processing recycles, more excellent because depropanizing tower kettle liquid and domethanizing column and dethanizer have certain temperature difference
Selection of land, before depropanization is handled obtain tower bottoms recycled as absorbent, it is first handled as demethanation and takes off second
The thermal source of alkane processing, is most cooled to 10-30 DEG C through recirculated water and chilled water afterwards, is preferably cooled to 15-20 DEG C step by step, so as to
Energy consumption is reduced, it is cost-effective.In addition, wherein there is small part absorbent to be discharged with demethanizer column overhead gas phase, therefore, in this hair
In bright method, preferably depropanization is handled to obtain after tower bottoms mixes with a part of fresh absorbent and be passed through domethanizing column
In, with absorptive tower absorbent flow in guarantee system, wherein, the tower bottoms for handling to obtain to the depropanization for being recycled as absorbent
There is no particular limitation with the ratio of fresh absorbent, such as both weight ratios can be 1：0-0.1.
According to method of the present invention, in step (5), the drying is the conventional drying process in this area, it is intended to is removed
The saturation water gone in depropanizing tower tower overhead gas.It can use molecular sieve drying system drying means, and specific method can include：
Drier needs one to open one for alternate run, and during alternate run, one previously run needs to carry out regenerative operation.Regenerative operation
When, it is necessary to by nitrogen after high pressure steam heating be used for drier is regenerated.Drying process gas pressure only produces few
Pressure drop is measured, is usually no more than 200kPa.
According to method of the present invention, it is preferable that cold after the overhead product of depropanization processing is dried in step (5)
But deethanization processing is carried out again to -10 DEG C to 30 DEG C.The cooling can be entered by caused cold in ethylene distillation removal process
OK, in order to further reducing energy consumption.
According to method of the present invention, it is preferable that the condition of deethanization processing can be the conventional deethanization in this area
The condition of processing, it is preferable that the condition of the deethanization processing includes：Dethanizer number of theoretical plate is 25-120 blocks, operation pressure
Power is 1.0-3.0MPa, and tower top temperature is -30 DEG C to -10 DEG C, and bottom temperature is 50-80 DEG C, so as to further improve most
The rate of recovery of isolated ethene and propylene eventually.
According to method of the present invention, dethanizer can clearly separate C2 and C3 components, by controlling dethanizer
Condition in above-mentioned preferred scope, can cause propylene in deethanizer overhead molar content be not higher than 0.5%, it is excellent
Choosing is not higher than 0.1%.
According to method of the present invention, it is preferable that the overhead product of step (5) deethanization processing is hydrogenated with successively
And ethylene distillation, selected to obtain ethene from ethylene rectifying column by conventional method or middle extraction method according to process requirements, by
A certain amount of methane is likely present in the material that dethanizer is sent into ethylene rectifying column, it is preferred to use middle extraction method, from
And polymer grade ethylene product can be obtained, among use during extraction method, ethylene distillation tower reactor product is ethane, and ethene is from tower reactor
Side extraction, the general position that produces can select to count the 2nd piece to 8 blocks column plates from top to bottom, preferably by ethylene distillation tower top
Compressor section similar in product returning pressure.When using conventional method, overhead product is ethene, and tower kettle product is ethane.Its
In, hydrogenation is in order to which acetylene is converted into ethene, and the technology can be provided by known technology.
According to method of the present invention, it is preferable that will be cooled down after the overhead product hydrogenation of step (5) deethanization processing
Ethylene rectifying column is passed through again to -35 DEG C to -10 DEG C carries out ethylene distillation.Wherein, the cooling can be reclaimed by ethylene distillation
During caused cold carry out, in order to further reduce energy consumption.
According to method of the present invention, the condition of ethylene distillation can be the condition of the conventional ethylene distillation in this area,
Such as it can include：The number of theoretical plate of ethylene rectifying column is 100-150 blocks, operating pressure 0.8-2.6MPa, tower top temperature for-
39 DEG C to -15 DEG C, bottom temperature is -20 DEG C to 0 DEG C.
According to method of the present invention, it is preferable that the tower kettle product of step (5) deethanization processing is carried out into propylene essence
Evaporate, select to obtain from the tower top of propylene rectification tower and/or middle part by conventional method or middle extraction method according to process requirements
Propylene, wherein, during using middle extraction method, propylene is obtained in the middle part of propylene rectification tower, propylene rectification tower kettle product is propane.
The specific method of used middle extraction method can be identical with obtaining the middle extraction method of ethene herein, except that extraction
Position selection counts between 2-15 block column plates from top to bottom.Correspondingly, referred in the middle part of aforesaid propylene rectifying column from propylene essence
Evaporate the position counted from top to bottom between 2-15 block column plates of tower.During using conventional method rectifying, overhead product is propylene, tower reactor
Product is propane.
According to method of the present invention, the condition of propylene rectifying can be the condition of the conventional propylene rectifying in this area,
Such as it can include：The number of theoretical plate of propylene rectification tower is 110-400 blocks, operating pressure 0.8-2.6MPa, and tower top temperature is
10 DEG C -55 DEG C, bottom temperature is 35 DEG C -60 DEG C.
The Recovery rate of ethylene that the method for the present invention is isolated is more than 95%, and propylene recovery rate is more than 95%.
In following examples and comparative example, methanol to olefins reaction gas is by ethene, propylene, methane, hydrogen and other components
(nitrogen, oxynitrides, carbon monoxide, carbon dioxide, dimethyl ether, water, methanol, ethane, acetylene, propane, allene, positive fourth
Alkane, iso-butane, 1- butylene, 2- butylene, 1,3- butadiene, cis-2-butene, Trans-2-butene, pentane, isopentane, 1- amylenes,
N-hexane, isohexane, hexene, benzene, toluene, paraxylene, meta-xylene, ortho-xylene and 1,3,5- trimethylbenzenes) composition, its
In, the content of methane is 4.1 moles of %, and the content of hydrogen is 1.8 moles of %, and the content of ethene is 40.7 moles of %, propylene
Content is 37.5 moles of %, and the content of water is 5.7 moles of %, and the content of other components is 10.2 moles of %.
Embodiment 1
The present embodiment is used for the separation method for illustrating the methanol to olefins reaction gas of the present invention.
(1) processing is compressed as shown in figure 1, methanol to olefins reaction gas raw material is passed through in compression unit, the pressure
Contracting unit is made up of 3 sections of compressor sections, and every section of outlet temperature of compressor section is no more than 140 DEG C, and every section of inlet temperature is 40 DEG C, is adopted
With 30 DEG C of circulating waters, methanol to olefins reaction gas pressure after compression unit compression processing rises to step by step
3.9MPa, wherein, after the 1st section of compressor section exports drain tank (pressure 0.55MPa) pass sequentially through setting caustic wash tower and
Water scrubber carries out alkali cleaning processing and washing process, and alkali lye is sprayed into tower and unstrpped gas from alkali cleaning column overhead in alkali cleaning processing procedure
Fully contact, sprayed into tower from washing column overhead using demineralized water during washing process and fully contacted with unstrpped gas, washed
Product afterwards is sent into the 2nd compressor section.In compression process, gas phase, aqueous phase and oil-phase product can be produced, by every section of compressor
Section produces aqueous phase lime set and returns to the entrance of the preceding paragraph compressor section, and is ultimately delivered to stripper recovery light hydrocarbon material and avoids raw material
Loss, caused oil phase enters domethanizing column to the 3rd section of compressor outlet gas after cooling, and oil phase is not produced between compressor section；
(2) gas phase for handling to obtain by compression carries out being cooled to 15 DEG C, and the unstrpped gas after cooling is gas-liquid two-phase, is not required to
Will drying can be sent directly into domethanizing column, refrigerant used is 5 DEG C or so of cold water, and cold water can be by suction-type lithium bromide system
Cold provides；
(3) as shown in Fig. 2 (initial boiling point is 42 DEG C, is done as 187 DEG C, C6-C7 components account in gasoline by absorbent gasoline
The 42.7% of gross weight, sulfur content are less than 50ppm) 15 DEG C are cooled to, then pass in domethanizing column, will be obtained after above-mentioned cooling
Gas-liquid two-phase logistics be passed through in domethanizing column progress demethanation processing, the dosage of absorbent is with compressor outlet gas through cooling
It is afterwards 1 into the mol ratio of the logistics of domethanizing column:1.74, domethanizing column absorber portion is provided with intercooler, cooling during rolling
The temperature of device is 15 DEG C, is 50 pieces, operating pressure 3.7MPa by controlling the number of theoretical plate of domethanizing column, tower top temperature is
21.4 DEG C, be 63.2 DEG C by controlling bottom temperature so that methane content control is 28ppm in tower bottoms；In addition, by demethanation
The overhead product that processing obtains is passed through in surge tank prepares hydrogen and methane (fuel gas) using PSA hydrogen producing technologies again, obtained
The purity of hydrogen is 99.99%；
(4) tower bottoms that demethanation handles to obtain is passed through progress depropanization processing in depropanizing tower；The reason of depropanizing tower
It is 40 pieces, operating pressure 2.6MPa by plate number, tower top temperature is 32.2 DEG C, and bottom temperature is 140.7 DEG C, wherein, tower bottoms
The molar content of middle C3 components is 1.6%；
(5) depropanization is handled to obtain thermal source of the tower bottoms as above-mentioned demethanation processing and the processing of following deethanizations, most
15 DEG C are cooled to step by step by recirculated water and cold water, and a portion tower bottoms (lighter hydrocarbons) submitting battery limit (BL) is first sent to debutanization
Tower, then mix and is passed through in domethanizing column (circulation solvent and newly as circulation solvent with a part of fresh absorbent using remaining
The weight ratio of fresh absorbent is 1:0.03) dosage and compressor outlet gas for, ensureing absorbent enter piptonychia after cooling
The mol ratio of the logistics of alkane tower is 1:1.74.Carried out after the overhead product of depropanization processing is dried using molecular sieve drying system
7.4 DEG C are cooled to, the cooling is carried out by caused cold in ethylene distillation removal process, the specific behaviour of molecular sieve drying system
It is as method：Drier needs one to open one for alternate run, and during alternate run, one previously run needs to carry out regeneration behaviour
Make., it is necessary to which nitrogen is used for regenerating drier after high pressure steam heating during regenerative operation.By de- third after cooling
The overhead product of alkane processing is passed through progress deethanization processing in dethanizer, and the number of theoretical plate of dethanizer is 80 pieces, operation pressure
Power is 2.3MPa, and tower top temperature is -22.3 DEG C, and bottom temperature is 55.1 DEG C so that propylene rubs in deethanizer overhead
Your content is 0.005%；
(6) -22.7 DEG C are cooled to after the overhead product of step (5) deethanization processing is hydrogenated with and is passed through ethylene rectifying column
Ethylene distillation is carried out, the cooling can be carried out by caused cold in ethylene distillation removal process, the reason of ethylene rectifying column
It it is 100 pieces, operating pressure 1.9MPa by plate number, tower top temperature is -30.7 DEG C, and bottom temperature is -9.2 DEG C, ethylene rectifying column
Kettle product is ethane, and ethene is obtained from ethylene rectifying column side using middle extraction method, and ethylene distillation tower top product is returned and pressed
Compressor section similar in power, ethene extraction position selection count between 2-8 block column plates from top to bottom；
(7) tower kettle product of step (5) deethanization processing is subjected to propylene rectifying, propylene rectification tower overhead product is third
Alkene, propylene rectification tower kettle product are propane, and the number of theoretical plate of propylene rectification tower is 170 pieces, operating pressure 1.95MPa, tower top
Temperature is 18.9 DEG C, and bottom temperature is 53.7 DEG C, and the purity of ethene is 99.96%, and the purity of propylene is 99.6%, ethene, third
The alkene rate of recovery and energy consumption parameter are shown in Table 1.
Embodiment 2
The present embodiment is used for the separation method for illustrating the methanol to olefins reaction gas of the present invention.
(1) methanol to olefins reaction gas raw material is passed through in compression unit and is compressed processing, the compression unit is by 3 sections
Compressor section forms, and every section of outlet temperature of compressor section is no more than 140 DEG C, and every section of inlet temperature is 40 DEG C, using 30 DEG C of circulations
Water cooling, methanol to olefins reaction gas pressure after compression unit compression processing rise to 3.9MPa step by step, wherein, the
2 compressor sections outlet drain tank after (pressure 1.8MPa) pass sequentially through setting caustic wash tower and water scrubber carry out alkali cleaning processing and
Washing process, alkali lye is sprayed into tower from alkali cleaning column overhead and fully contacted with unstrpped gas in alkali cleaning processing procedure, washing process mistake
Sprayed into tower from washing column overhead using demineralized water in journey and fully contacted with unstrpped gas, the product after washing is sent into the 3rd compression
Machine section.In compression process, gas phase, aqueous phase and oil-phase product can be produced, every section of compressor section is produced into aqueous phase lime set returns
The entrance of the preceding paragraph compressor section, and be ultimately delivered to stripper recovery light hydrocarbon material and avoid significant loss, the 3rd section of compressor goes out
Caused oil phase enters domethanizing column to gas after cooling, and oil phase is not produced between compressor section；
(2) gas phase for handling to obtain by compression carries out being cooled to 15 DEG C, and the unstrpped gas after cooling is gas-liquid two-phase, is not required to
Will drying can be sent directly into domethanizing column, refrigerant used is 5 DEG C or so of cold water, and cold water can be by suction-type lithium bromide system
Cold provides；
(3) as shown in Fig. 2 (initial boiling point is 32 DEG C, is done as 192 DEG C, C6-C7 components account in gasoline by absorbent gasoline
The 51.2% of gross weight, sulfur content are less than 50ppm) 15 DEG C are cooled to, then pass in domethanizing column, will be obtained after above-mentioned cooling
Gas-liquid two-phase logistics be passed through in domethanizing column progress demethanation processing, the dosage of absorbent is with compressor outlet gas through cooling
It is afterwards 1.5 into the mol ratio of the logistics of domethanizing column:1, domethanizing column absorber portion is provided with intercooler, intercooler
Temperature be 15 DEG C, by control domethanizing column number of theoretical plate be 35 pieces, operating pressure 3.7MPa, tower top temperature 28.3
DEG C, bottom temperature is 65.2 DEG C so that methane content control is 29ppm in tower bottoms；In addition, the tower that demethanation is handled to obtain
Top product is passed through in surge tank prepares hydrogen and methane (fuel gas) using PSA hydrogen producing technologies again, and the purity of obtained hydrogen is
99.9%；
(4) tower bottoms that demethanation handles to obtain is passed through progress depropanization processing in depropanizing tower；The reason of depropanizing tower
It is 35 pieces, operating pressure 2.4MPa by plate number, tower top temperature is 28.4 DEG C, and bottom temperature is 142.2 DEG C, wherein, tower bottoms
The molar content of middle C3 components is 3.22%；
(5) depropanization is handled to obtain thermal source of the tower bottoms as above-mentioned demethanation processing and the processing of following deethanizations, most
15 DEG C are cooled to step by step by recirculated water and cold water, and a portion tower bottoms (lighter hydrocarbons) submitting battery limit (BL) is first sent to debutanization
Tower, then mix and is passed through in domethanizing column (circulation solvent and newly as circulation solvent with a part of fresh absorbent using remaining
The weight ratio of fresh absorbent is 1:0.02) dosage and compressor outlet gas for, ensureing absorbent enter piptonychia after cooling
The mol ratio of the logistics of alkane tower is 1.5:1, carried out after the overhead product of depropanization processing is dried using molecular sieve drying system
6.7 DEG C are cooled to, the cooling is carried out by caused cold in ethylene distillation removal process, the specific behaviour of molecular sieve drying system
It is as method：Drier needs one to open one for alternate run, and during alternate run, one previously run needs to carry out regeneration behaviour
Make., it is necessary to which nitrogen is used for regenerating drier after high pressure steam heating during regenerative operation.By de- third after cooling
The overhead product of alkane processing is passed through progress deethanization processing in dethanizer, and the number of theoretical plate of dethanizer is 70 pieces, operation pressure
Power is 2.3MPa, and tower top temperature is -22.3 DEG C, and bottom temperature is 55.1 DEG C so that propylene rubs in deethanizer overhead
Your content is 0.005%；
(6) -22.7 DEG C are cooled to after the overhead product of step (5) deethanization processing is hydrogenated with and is passed through ethylene rectifying column
Ethylene distillation is carried out, the cooling can be carried out by caused cold in ethylene distillation removal process, the reason of ethylene rectifying column
It it is 110 pieces, operating pressure 1.9MPa by plate number, tower top temperature is -30.7 DEG C, and bottom temperature is -9.2 DEG C, ethylene rectifying column
Kettle product is ethane, and ethene is obtained from ethylene rectifying column side using middle extraction method, and ethylene distillation tower top product is returned and pressed
Compressor section similar in power, ethene extraction position selection count between 2-8 block column plates from top to bottom；；
(7) tower kettle product of step (5) deethanization processing is subjected to propylene rectifying, propylene rectification tower overhead product is third
Alkene, propylene rectification tower kettle product are propane, and the number of theoretical plate of propylene rectification tower is 180 pieces, operating pressure 1.85MPa, tower top
Temperature is 19.2 DEG C, and bottom temperature is 51.2 DEG C, and the purity of ethene is 99.96%, and the purity of propylene is 99.6%, ethene, third
The alkene rate of recovery and energy consumption parameter are shown in Table 1.
Embodiment 3
The present embodiment is used for the separation method for illustrating the methanol to olefins reaction gas of the present invention.
(1) methanol to olefins reaction gas raw material is passed through in compression unit and is compressed processing, the compression unit is by 3 sections
Compressor section forms, and every section of outlet temperature of compressor section is no more than 140 DEG C, and every section of inlet temperature is 40 DEG C, using 30 DEG C of circulations
Water cooling, methanol to olefins reaction gas pressure after compression unit compression processing rise to 3.9MPa step by step, wherein, the
2 compressor sections outlet drain tank after (pressure 1.8MPa) pass sequentially through setting caustic wash tower and water scrubber carry out alkali cleaning processing and
Washing process, alkali lye is sprayed into tower from alkali cleaning column overhead and fully contacted with unstrpped gas in alkali cleaning processing procedure, washing process mistake
Sprayed into tower from washing column overhead using demineralized water in journey and fully contacted with unstrpped gas, the product after washing is sent into the 3rd compression
Machine section.In compression process, gas phase, aqueous phase and oil-phase product can be produced, every section of compressor section is produced into aqueous phase lime set returns
The entrance of the preceding paragraph compressor section, and be ultimately delivered to stripper recovery light hydrocarbon material and avoid significant loss, the 3rd section of compressor goes out
Caused oil phase enters domethanizing column to gas after cooling, and oil phase is not produced between compressor section；
(2) gas phase for handling to obtain by compression carries out being cooled to 20 DEG C, and the unstrpped gas after cooling is gas-liquid two-phase, is not required to
Will drying can be sent directly into domethanizing column, refrigerant used is 5 DEG C or so of cold water, and cold water can be by suction-type lithium bromide system
Cold provides；
(3) as shown in Fig. 2 (initial boiling point is 51 DEG C, is done as 243 DEG C, C6-C7 components account in gasoline by absorbent gasoline
The 42.1% of gross weight, sulfur content are less than 50ppm) 20 DEG C are cooled to, then pass in domethanizing column, will be obtained after above-mentioned cooling
Gas-liquid two-phase logistics be passed through in domethanizing column progress demethanation processing, the dosage of absorbent is with compressor outlet gas through cooling
It is afterwards 1 into the mol ratio of the logistics of domethanizing column:1.87, domethanizing column absorber portion is provided with intercooler, cooling during rolling
The temperature of device is 20 DEG C, is 30 pieces, operating pressure 3.7MPa by controlling the number of theoretical plate of domethanizing column, tower top temperature is
24.4 DEG C, bottom temperature is 63.7 DEG C so that methane content control is 300ppm in tower bottoms；In addition, demethanation is handled
To overhead product be passed through in surge tank hydrogen and methane (fuel gas) prepared using PSA hydrogen producing technologies again, obtained hydrogen
Purity is 99.9%；
(4) tower bottoms that demethanation handles to obtain is passed through progress depropanization processing in depropanizing tower；The reason of depropanizing tower
It is 35 pieces, operating pressure 2.6MPa by plate number, tower top temperature is 30.8 DEG C, and bottom temperature is 140.4 DEG C, wherein, tower bottoms
The molar content of middle C3 components is 1.45%；
(5) depropanization is handled to obtain thermal source of the tower bottoms as above-mentioned demethanation processing and the processing of following deethanizations, most
20 DEG C are cooled to step by step by recirculated water and cold water, and a portion tower bottoms (lighter hydrocarbons) submitting battery limit (BL) is first sent to debutanization
Tower, then mix and is passed through in domethanizing column (circulation solvent and newly as circulation solvent with a part of fresh absorbent using remaining
The weight ratio of fresh absorbent is 1:0.02) dosage and compressor outlet gas for, ensureing absorbent enter piptonychia after cooling
The mol ratio of the logistics of alkane tower is 1:1.87.Carried out after the overhead product of depropanization processing is dried using molecular sieve drying system
5.8 DEG C are cooled to, the cooling is carried out by caused cold in ethylene distillation removal process, the specific behaviour of molecular sieve drying system
It is as method：Drier needs one to open one for alternate run, and during alternate run, one previously run needs to carry out regeneration behaviour
Make., it is necessary to which nitrogen is used for regenerating drier after high pressure steam heating during regenerative operation.By de- third after cooling
The overhead product of alkane processing is passed through progress deethanization processing in dethanizer, and the number of theoretical plate of dethanizer is 60 pieces, operation pressure
Power is 2.3MPa, and tower top temperature is -22.4 DEG C, and bottom temperature is 55.1 DEG C so that propylene rubs in deethanizer overhead
Your content is 0.003%；
(6) -22.9 DEG C are cooled to after the overhead product of step (5) deethanization processing is hydrogenated with and is passed through ethylene rectifying column
Ethylene distillation is carried out, the cooling can be carried out by caused cold in ethylene distillation removal process, the reason of ethylene rectifying column
It it is 110 pieces, operating pressure 1.9MPa by plate number, tower top temperature is -31.3 DEG C, and bottom temperature is -9.2 DEG C, ethylene rectifying column
Kettle product is ethane, and ethene is obtained from ethylene rectifying column side using middle extraction method, and ethylene distillation tower top product is returned and pressed
Compressor section similar in power, ethene extraction position selection count between 2-8 block column plates from top to bottom；
(7) tower kettle product of step (5) deethanization processing is subjected to propylene rectifying, propylene rectification tower overhead product is third
Alkene, propylene rectification tower kettle product are propane, and the number of theoretical plate of propylene rectification tower is 260 pieces, operating pressure 1.95MPa, tower top
Temperature is 18.9 DEG C, and bottom temperature is 53.7 DEG C, and the purity of ethene is 99.96%, and the purity of propylene is 99.6%, ethene, third
The alkene rate of recovery and energy consumption parameter are shown in Table 1.
Embodiment 4
The present embodiment is used for the separation method for illustrating the methanol to olefins reaction gas of the present invention.
Methanol to olefins reaction gas is separated according to the method for embodiment 1, unlike, the compression handles obtained gas
The chilling temperature of phase, absorbent and domethanizing column intercooler is 25 DEG C.
Comparative example 1
The present embodiment is used for the separation method for illustrating the methanol to olefins reaction gas of the present invention.
Methanol to olefins reaction gas is separated according to the method for embodiment 3, unlike, by the theory for controlling domethanizing column
Plate number is 18 pieces, operating pressure 5.0MPa, and tower top temperature is 26.3 DEG C, and bottom temperature is 75.9 DEG C so that by tower bottoms
Methane content control is 375pm.
Table 1
Note：Steam is 0.8MPa saturated vapor.
The Recovery rate of ethylene that the method for the present invention is isolated is more than 80%, and propylene recovery rate is more than 95%, and should
Method energy consumption is low, operating flexibility is big, can be according to product adjustment of yield energy consumption technological parameter.
This method by the use of gasoline component as absorbent methanol removal alkene (MTO/DMTO) reaction gas in methane etc.
Light components, and the methane in operation temperature section methanol removal alkene (MTO/DMTO) product gas more than 10 DEG C
And light fraction, effectively inhibit water and hydro carbons to form hydrate.In addition, the drying process of the present invention need not be placed on compression
Unit exports, it is only necessary to processing is dried to deethanizer overhead gas, avoids and compression unit outlet liquid phase lime set is carried out
Dry, significantly reduce drying process treating capacity, considerably reduce the consumption and energy consumption of public work nitrogen therewith.This
Demethanation process is switched to thermal release process and is advantageous to heat exchange network optimization by method, it is not necessary to puts into less than -40 DEG C of cryogen.Tool
There is the features such as small investment, material recovery rate is high.
The preferred embodiment of the present invention described in detail above, still, the present invention are not limited in above-mentioned embodiment
Detail, in the range of the technology design of the present invention, a variety of simple variants can be carried out to technical scheme, this
A little simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (17)
1. a kind of separation method of methanol to olefins reaction gas, it is characterised in that this method includes：
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed processing；
(2) gas phase that compression handles to obtain is cooled down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is subjected to demethanation processing in domethanizing column；
(4) tower kettle product for handling to obtain by demethanation carries out depropanization processing in depropanizing tower；
(5) deethanization processing is carried out in dethanizer after the overhead product of depropanization processing is dried；
Wherein, the gaseous pressure that the compression processing obtains is 3.2-6.0MPa, and step is cooled to temperature 10-30 in (2)
DEG C, the absorbent is gasoline, and the condition of the demethanation processing includes：Domethanizing column number of theoretical plate is 20-60 blocks, operation pressure
Power is 3.0-5.8MPa, and tower top temperature is 10-40 DEG C, and bottom temperature is 40-120 DEG C.
2. according to the method for claim 1, wherein, the gasoline contains C6-C7 components, and C6-C7 components account for gasoline gross weight
The 10-60% of amount, the sulfur content of the gasoline is less than 50ppm, and its initial boiling point is 25-55 DEG C, is done as 120-250 DEG C.
3. according to the method for claim 1, wherein, the temperature of the absorbent is 10-30 DEG C, preferably 15-20 DEG C.
4. according to the method for claim 1, wherein, in step (2), temperature is cooled to as 15-20 DEG C.
5. according to the method for claim 1, wherein, the compression unit includes 3-5 section compressor sections, and methanol-to-olefins are anti-
Should gas by the compression unit compression processing after pressure rise to 3.2-6.0MPa step by step.
6. according to the method for claim 5, wherein, alkali cleaning and washing are carried out during the compression is handled；
Preferably, the alkali cleaning and washing are carried out under 0.3-3.0MPa operating pressure.
7. according to the method for claim 1, wherein, this method also includes：The overhead product that demethanation handles to obtain is entered
Row pressure swing adsorption hydrogen production, obtains hydrogen.
8. according to the method for claim 1, wherein, the condition of the depropanization processing includes：Depropanizing tower number of theoretical plate
For 15-50 blocks, operating pressure 1.5-3.5MPa, tower top temperature is 10-50 DEG C, and bottom temperature is 100-160 DEG C.
9. according to the method for claim 1, wherein, the condition of the deethanization processing includes：Dethanizer number of theoretical plate
For 25-120 blocks, operating pressure 1.0-3.0MPa, tower top temperature is -30 DEG C to -10 DEG C, and bottom temperature is 50-80 DEG C.
10. according to the method for claim 1, wherein, this method also includes：In step (5), by the tower top of depropanization processing
Product is cooled to -10 DEG C to 30 DEG C after drying and carries out deethanization processing again.
11. according to the method for claim 1, wherein, this method also includes：The tower top of step (5) deethanization processing is produced
Thing is hydrogenated with successively and ethylene distillation, and uses middle extraction method to obtain ethene from ethylene rectifying column side, and ethylene distillation
Tower kettle product is ethane, by compressor section similar in ethylene distillation tower top product returning pressure.
12. according to the method for claim 11, wherein, the condition of the ethylene distillation includes：The theory of ethylene rectifying column
Plate number is 100-150 blocks, operating pressure 0.8-2.6MPa, and tower top temperature is -39 DEG C to -15 DEG C, bottom temperature for -20 DEG C extremely
0℃。
13. according to the method for claim 1, wherein, this method also includes：The tower reactor of step (5) deethanization processing is produced
Thing carries out propylene rectifying, and obtains propylene from propylene rectification tower tower top, and propylene rectification tower kettle product is propane.
14. according to the method for claim 13, wherein, the condition of the propylene rectifying includes：The theory of propylene rectification tower
Plate number is 110-400 blocks, and operating pressure 0.8-2.6MPa, tower top temperature is 10 DEG C -55 DEG C, and bottom temperature is 35 DEG C -60 DEG C.
15. according to the method for claim 1, wherein, this method also includes：The intersegmental gas of compression process is produced after cooling
Enter depropanizing tower after raw oil phase pressurization, caused oil phase enters domethanizing column to compressor outlet gas after cooling.
16. according to the method for claim 1, wherein, this method also includes：Depropanization is handled to obtain tower bottoms as de-
The absorbent of methane processing recycles.
17. according to the method for claim 16, wherein, before recycling as absorbent, depropanization is handled to obtain
The thermal source that tower bottoms is first handled as demethanation processing and deethanization.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110092701A (en) * | 2018-01-31 | 2019-08-06 | 中国寰球工程有限公司 | The lighter hydrocarbons separation system and method for MTO product mix gas |
| CN114409492A (en) * | 2021-12-15 | 2022-04-29 | 国家能源集团宁夏煤业有限责任公司 | Device and method for preparing low-carbon olefin from methanol |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103058812A (en) * | 2013-01-28 | 2013-04-24 | 神华集团有限责任公司 | Olefin separation system and olefin separation method |
| CN103787814A (en) * | 2014-01-23 | 2014-05-14 | 东华工程科技股份有限公司 | Low-hydrocarbon intercooled solvent washing separation method |
| CN104177214A (en) * | 2014-08-27 | 2014-12-03 | 惠生工程（中国）有限公司 | Method for separating mixture of catalytic cracking rich gas and methanol-to-olefin reaction product |
| CN104884413A (en) * | 2012-11-15 | 2015-09-02 | 鲁姆斯科技公司 | Recovery of ethylene from methanol to olefins process |
-
2016
- 2016-07-12 CN CN201610546037.3A patent/CN107602331B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104884413A (en) * | 2012-11-15 | 2015-09-02 | 鲁姆斯科技公司 | Recovery of ethylene from methanol to olefins process |
| CN103058812A (en) * | 2013-01-28 | 2013-04-24 | 神华集团有限责任公司 | Olefin separation system and olefin separation method |
| CN103787814A (en) * | 2014-01-23 | 2014-05-14 | 东华工程科技股份有限公司 | Low-hydrocarbon intercooled solvent washing separation method |
| CN104177214A (en) * | 2014-08-27 | 2014-12-03 | 惠生工程（中国）有限公司 | Method for separating mixture of catalytic cracking rich gas and methanol-to-olefin reaction product |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110092701A (en) * | 2018-01-31 | 2019-08-06 | 中国寰球工程有限公司 | The lighter hydrocarbons separation system and method for MTO product mix gas |
| CN110092701B (en) * | 2018-01-31 | 2023-08-15 | 中国寰球工程有限公司 | Light hydrocarbon separation method for MTO product mixed gas |
| CN114409492A (en) * | 2021-12-15 | 2022-04-29 | 国家能源集团宁夏煤业有限责任公司 | Device and method for preparing low-carbon olefin from methanol |
| CN114409492B (en) * | 2021-12-15 | 2023-12-22 | 国家能源集团宁夏煤业有限责任公司 | Device and method for preparing low-carbon olefin from methanol |
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