CN106631664B - 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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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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- C07C7/005—Processes comprising at least two steps in series
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The present invention relates to a kind of separation methods of methanol to olefins reaction gas.This method is using the component of the hydrocarbon containing C4-C5 as light components such as methane in absorbent methanol removal alkene (MTO/DMTO) reaction gas, and methane and light fraction in 10 DEG C or more operation temperature section methanol removal alkene (MTO/DMTO) product gas effectively inhibit water and hydro carbons to form hydrate.In addition, drying process of the invention does not need to be placed on compression unit outlet, it only needs that deethanizer overhead gas is dried, it avoids and compression unit outlet liquid phase lime set is dried, drying process treating capacity is significantly reduced, considerably reduces the consumption and energy consumption of public work nitrogen therewith.Demethanation process is switched to thermal release process and is conducive to heat exchange network optimization by this method, does not need -40 DEG C of cryogens below of investment.With the features such as small investment, material recovery rate is high.
Description
Technical field
The present invention relates to methanol-to-olefins fields, and in particular, to a kind of separation method of methanol to olefins reaction gas.
Background technique
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
Increased to more than 1,700 ten thousand tons.National economy relies primarily on petroleum to the wilderness demand of ethylene and propylene, keeps China's oil average annual
Consumption figure is improved to 500,000,000 tons or more.Undoubtedly become national economy and society by the Modern Coal-based Chemical of representative of coal-to-olefin technology
Development provides important support, and ensures the needs of national energy security.The breakthrough and its production of preparing low carbon olefinic hydrocarbon with methanol technology
Industry indicates that China has entered world lead level in the field.
Methanol-to-olefins complete set technology is made 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 ethylene and propylene product of grade are closed, 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 unit 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 is methanol in product gas, and intermediate reaction product is dimethyl ether (DME), sour gas such as carbon dioxide, NOxDeng,
According to required operating condition difference part of impurity can be removed through operations such as washing, alkali cleanings between compressor section.Cold separation
Unit is the separative unit in 0 DEG C of temperature range below, such as demethanation, deethanization and ethylene distillation process.Thermal release work
It includes the processes such as depropanization, propylene rectifying that skill, which is in the separative unit of 0 DEG C or more of temperature range,.
The removal of light components methane in impurity is the key that obtain high-purity polymer grade ethylene.It is commonplace at this stage
Method be cryogenic separation method and absorption and separation method.Patent application CN200810201217.3 discloses a kind of MTO/MTP reaction
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 cooling temperature is about -65 DEG C, finally by the available 90%- of rectifying
99.99% ethylene.Use ethane lower as absorption temperature required for absorbent, -100 DEG C of second is needed in engineer application
Alkene refrigerant condenser, even -135 DEG C of methane compressor provide cooling capacity, improve the investment of equipment and increase 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 process, this method is using front-end demethanization tower, depropanizing tower and debutanizing tower tower reactor effluent as absorbent
Three component of carbon two and carbon in product gas is absorbed, the light fractions such as methane are separated from product gas.This method is needed -40
DEG C or so temperature demethanation, and be front-end deethanization in this method.
Patent application CN201310216950.3 disclose it is a kind of from MTO/DMTO product gas recycle ethylene system and
Method, this method add cold recovery device after domethanizing column, reduce system energy consumption, and Recovery rate of ethylene is greater than
99.7%, but ice chest is needed, energy consumption is larger.
The method of patent application WO2009/015507 preparing low-carbon olefin of polymerization-grade of pyrolysis gas separation of methanol, utilizes absorption
Isolated method removes methane, and 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 at 0 DEG C hereinafter, and ethane or propane before being, because
This will lead to methane and other lighter hydrocarbons such as ethane, ethylene and propylene etc. and is easy to form hydrocarbon hydrate with water, and this kind of hydrate exists
0 DEG C or less is easy to make valve and pipeline that there is a phenomenon where frozen blocks, and the energy consumption of above-mentioned each method is also larger.
Summary of the invention
The purpose of the invention is to overcome the method energy consumption for separating methanol to olefins reaction gas in the prior art larger, easily
The defect for causing line clogging etc. provides a kind of separation method of methanol to olefins reaction gas.
To achieve the goals above, the present invention provides a kind of separation method of methanol to olefins reaction gas, this method packets
It includes:
(1) methanol to olefins reaction gas is passed through in compression unit and carries out compression processing；
(2) gas phase for obtaining compression processing cools 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 demethanation carries out depropanization processing in depropanizing tower；
(5) deethanization processing will be carried out in dethanizer after the overhead product drying of depropanization processing；
Wherein, the gaseous pressure that the compression processing makes is 3.2-6.0MPa, described to be cooled in step (2)
Temperature is 10-30 DEG C, and the absorbent contains C4-C5 hydrocarbon, and the condition of the demethanation processing includes: domethanizing column number of theoretical plate
For 20-60 block, operating pressure 3.0-5.8MPa, tower top temperature is 10-40 DEG C, and bottom temperature is 60-120 DEG C.
Methanol-to-olefins (MTO/DMTO) method gas separation method of the invention has the advantage that
(1) in method of the invention, using the component of the hydrocarbon containing C4-C5 as absorbent methanol removal alkene (MTO/DMTO)
The light components such as the methane in reaction gas, raw sorbent are easy to get, low in cost；
(2) methane in 10 DEG C or more operation temperature section methanol removal alkene (MTO/DMTO) product gas and
Light fraction effectively inhibits water and hydro carbons to form hydrate；
(3) in method of the invention, drying process does not need to be placed on compression unit outlet, it is only necessary to dethanizer tower
Top gas is dried, and 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, does not need using ethylene refrigeration unit, material
General low temperature carbon steel can be selected in material, and low energy consumption, reduces investment outlay；
(5) the very high polymer grade ethylene of the available purity of method of the invention and propylene product, and Recovery rate of ethylene is
95% or more, propylene recovery rate is 95% or more.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
Fig. 1 is a kind of compression process flow chart of specific embodiment of the present invention.
Fig. 2 is a kind of methanol to olefins reaction gas separating technology flow chart of specific embodiment of the present invention.
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The reaction gas of methanol-to-olefins (MTO/DMTO) reactor is per se with a large amount of saturated waters, and subtractive process
The operation such as alkali cleaning and washing is commonly used, this makes a large amount of saturated waters in the material of separation process.The behaviour of existing demethanation process
Make temperature at 0 DEG C hereinafter, operating pressure is greater than 2.0MPa.Under the conditions of this, methane and other lighter hydrocarbons such as ethane, ethylene and propylene
Hydrocarbon hydrate is formed with water Deng easy, this kind of hydrate is easy to make valve and pipeline that frozen block phenomenon occur at 0 DEG C or less.Institute
Generally to need to be dried after compression unit just in methanol-to-olefins (MTO/DMTO) reaction gas into later separation list
Member.Selection is since the separating technology of traditional methanol-to-olefins product gas is general in compression unit outlet end dry feedstock gas
It is since deethanization process.Ethane and more light component are separated from unstripped gas first, make methane, an oxygen in this case
Change carbon, the component of natural gas such as nitrogen need to remove from the ethylene of relative lightweight in product gas, ethane in subsequent separation process,
And this process is completed in 0 DEG C of cold separation process below, so having in compression unit outlet end except desaturation
Water.
The optimization of heat-exchange network is detrimental to by another problem of product gas elder generation deethanization that is dry and compressing.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- ethylene into cold separative unit and demethanation process, tower reactor liquid enter thermal release
Unit starts depropanization process.The pressure of the cold separation process of de- ethylene and demethanation is generally 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
Making pressure is 1.5MPa or so, and 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 following temperature.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 to put into a large amount of cold
Amount.
Therefore, in order to overcome in the prior art because of first deethanization and existing drawbacks described above.
The present invention provides a kind of separation methods of methanol to olefins reaction gas, this method comprises:
(1) methanol to olefins reaction gas is passed through in compression unit and carries out compression processing；
(2) gas phase for obtaining compression processing cools 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 demethanation carries out depropanization processing in depropanizing tower；
(5) deethanization processing will be carried out in dethanizer after the overhead product drying of depropanization processing；
Wherein, the gaseous pressure that the compression processing makes is 3.2-6.0MPa, described to be cooled in step (2)
Temperature is 10-30 DEG C, and the absorbent contains C4-C5 hydrocarbon, and the condition of the demethanation processing includes: domethanizing column number of theoretical plate
For 20-60 block, operating pressure 3.0-5.8MPa, tower top temperature is 10-40 DEG C, and bottom temperature is 60-120 DEG C.
Preferably, it is 30-50 block that the condition of the demethanation processing, which includes: domethanizing column number of theoretical plate, and operating pressure is
3.0-4.5MPa, tower top temperature are 10-40 DEG C, and bottom temperature is 60-120 DEG C, so as to improve the recycling of ethylene and propylene
Rate simultaneously reduces system energy consumption.
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, ethylene, acetylene, propane, propylene, allene, normal butane, iso-butane, 1- fourth
Alkene, 2- butylene, 1,3- butadiene, cis-2-butene, Trans-2-butene, pentane, isopentane, 1- amylene, n-hexane, isohexane,
Hexene, benzene, toluene, paraxylene, meta-xylene, ortho-xylene and 1,3,5- trimethylbenzene.Wherein, the content of ethylene 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
It can be 0-10 moles of %, the total content of other components can be 0-30 moles of %.
Method according to the present invention, it is preferable that in step (1), the compression unit includes 3-5 sections of compressor sections,
Methanol to olefins reaction gas pressure after the 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 the technological requirements, and every section of inlet temperature is 40 DEG C or so, generallys use 25-
35 DEG C of circulating waters.
Method according to the present invention, it is preferable that alkali cleaning and washing are carried out during the compression processing,
In, the sequence 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.Method according to the present invention, it is highly preferred that described
Alkali cleaning and washing carry out under 0.3-3.0MPa operating pressure.Generally, alkali cleaning and water-washing step can be in 1-3 sections of compressors
Section exit carries out.
In the present invention, washing is to remove the organic oxide in unstripped gas, such as methanol, dimethyl ether.It is general to use
Demineralized water is sprayed into tower from washing column overhead and is come into full contact with unstrpped gas.According to operating pressure difference, water-washing process is possible to
A part of hydrocarbon component in unstripped gas can be absorbed, therefore, can use existing well-known technique first recycle wherein most methanol and
After DME, wherein hydrocarbons are recycled by the methods of stripping, return to compression unit.Wherein, washing process is that this field is conventional
Technique.
In the present invention, alkali cleaning is to remove the sour gas such as the carbon dioxide in unstripped gas.Generally use lye from alkali
It washes in column overhead penetrating tower and is come into full contact with unstrpped gas.Caustic wash tower has neutralizing treatment section and a washing section, caustic wash tower overhead gas into
Enter compression unit.Wherein, alkali washing process is the technique of this field routine.
In the present invention, due to containing a large amount of saturated 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 raising of pressure and the reduction of cooling temperature may generate water phase lime set, or
Person contains the three-phase effluent of gas phase, water phase and oily phase.Wherein gaseous component is the hydrocarbons containing a small amount of saturated water, water phase
It is the water containing minute quantity hydrocarbons, oil is mutually the hydrocarbons containing C2-C5 heavier component.Every section of compressor section generates water
The entrance of the preceding paragraph compressor section mutually can be returned, and is ultimately delivered to stripper recycling hydrocarbons and avoids significant loss.Compression
The oil that gas generates after cooling between procedure segment can enter depropanizing tower, compressor outlet gas institute after cooling after mutually pressurizeing
The oil of generation can mutually enter domethanizing column.
Method according to the present invention, it is preferable that in step (2), the temperature that is cooled to is 15-20 DEG C.After cooling
Unstrpped gas be gas-liquid two-phase, domethanizing column can be sent directly by not needing drying.Wherein, refrigerant used can be 5 DEG C
The cold water of left and right, cold water can be provided by lithium-bromide absorption-type refrigerating machine.And lithium bromide refrigerator is using absorption refrigeration work
Skill has the advantages that low energy consumption using the waste hot steam of factory as heat source.
Method according to the present invention, it is preferable that in step (3), absorbent is C4-C5 hydrocarbon, it is highly preferred that the suction
It receives agent and contains normal butane, iso-butane, 1- butylene, Trans-2-butene, cis-2-butene, pentane, isopentane, 1- amylene；
It is highly preferred that the content of normal butane is 10-50 weight %, and iso-butane contains on the basis of the total weight of absorbent
Amount be 10-50 weight %, 1- butylene content be 5-15 weight %, the content of Trans-2-butene is 5-35 weight %, cis- 2- fourth
The content of alkene is 5-35 weight %, pentane 5-35 weight %, isopentane content be that the content of 5-35 weight %, 1- amylene is
5-35 weight %, the sum of each component content is no more than 100%, so as to improve the rate of recovery of ethylene and propylene and reduce energy
Consumption.
The dosage of absorbent is not specially required in the present invention, such as: after the dosage of absorbent and step (2) are cooling
The molar ratio of the gas-liquid two-phase arrived can be 1:5 to 3:1, preferably 1:4 to 2:1, more preferably 1:3 to 1.5:1.
Method according to 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
It is 15-20 DEG C.
Method according to the present invention, wherein domethanizing column can be divided into absorber portion and stripping section.The effect of absorber portion
It is the C2 and more heavy constituent absorbed in gas phase, reduces the C2 constituent content in the light components such as tower top methane, it is preferable that demethanation
Tower absorber portion can increase intercooler to guarantee 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 the methane content controlled in tower bottoms, and methane content is lower to be advantageously ensured that most
The purity of ethylene product made from end.But it is increased as domethanizing column tower reactor methane content reduces bottom temperature, tower top
The C2 of loss and more heavy constituent is consequently increased, methane content control is in 1-10000ppm preferably in tower bottoms.
Method according to the present invention, in step (3), it is preferable that the overhead product for handling demethanation carries out
PSA hydrogen manufacturing, obtains hydrogen.The overhead product that demethanation can be specifically handled is passed through in surge tank again using PSA system
Hydrogen technology prepares hydrogen and methane.PSA hydrogen producing technology is techniques well known, and details are not described herein.The present invention is isolated
Hydrogen purity be 99-99.999%.
Method according to the present invention, in step (4), the condition of depropanization processing can for this field it is conventional de- third
Alkane condition, it is preferable that it is 15-50 block that the condition of the depropanization processing, which includes: depropanizing tower number of theoretical plate, and operating pressure is
1.5-3.5MPa, tower top temperature are 10-50 DEG C, and bottom temperature is 100-160 DEG C, are finally recovered so as to further increase
The rate of recovery of the ethylene and propylene that arrive.
Method according to the present invention, in step (4), depropanizing tower tower top is C2 and C3 component, and tower reactor is mainly C4
And more heavy constituent contains a small amount of C3 component simultaneously, depropanizing tower top gaseous phase is due to being entrained with a certain amount of C4 and more recombinating
Point, so cooling is needed to make its reflux, tower top temperature be can control within the scope of 10-50 DEG C, preferably within the scope of 15-35 DEG C.
Wherein, depropanizing tower tower reactor mainly controls the content of C3 component, and the content of C3 component is lower in tower reactor, C2 the and C3 component of system
The rate of recovery it is higher, while bottom temperature is higher；Bottom temperature is higher, and tower top C4 entrainment is higher, and required energy consumption is higher.Cause
This, the molar content of tower reactor C3 component controls within the scope of 1-25%, preferably within the scope of 5-20%.
Method according to the present invention, in step (4), it is preferable that depropanization is handled to obtain tower bottoms as piptonychia
The absorbent of alkane processing recycles, more excellent since depropanizing tower kettle liquid and domethanizing column and dethanizer are there are certain temperature difference
It is first used as demethanation to handle and de- second by selection of land before depropanization to be handled to obtain tower bottoms and is recycled as absorbent
The heat source of alkane processing, is most cooled to 10-30 DEG C through recirculated water and chilled water afterwards step by step, is preferably cooled to 15-20 DEG C, so as to
Reduce energy consumption, save the cost.In addition, wherein having small part absorbent that can be discharged with demethanizer column overhead gas phase, therefore, in this hair
In bright method, preferably depropanization is handled to obtain after tower bottoms is mixed 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 handled the depropanization for being recycled as absorbent
There is no particular limitation with the ratio of fresh absorbent, such as the weight ratio of the two can be 1:0-0.1.
Method according to the present invention, in step (5), the drying is the drying process of this field routine, it is intended to be removed
Remove the saturated water in depropanizing tower tower overhead gas.It can use molecular sieve drying system drying means, and specific method may include:
Drier needs one to open one for alternate run, and when alternate run, previously run one needed to carry out regenerative operation.Regenerative operation
When, it needs for nitrogen to be used to after high pressure steam heating to regenerate desiccant.Drying process gas pressure only generates few
Pressure drop is measured, 200kPa is usually no more than.
Method according to the present invention, it is preferable that, will be cold after the overhead product drying of depropanization processing in step (5)
But deethanization processing is carried out again to -10 DEG C~30 DEG C.The cooling can by the cooling capacity that is generated in ethylene distillation removal process into
Row, in order to further decrease energy consumption.
Method according to the present invention, it is preferable that the condition of deethanization processing can be the deethanization of this field routine
The condition of processing, it is preferable that the condition of the deethanization processing includes: that dethanizer number of theoretical plate is 25-120 block, operation pressure
Power is 1.0-3.0MPa, and tower top temperature is -30~-10 DEG C, and bottom temperature is 50-80 DEG C, final so as to further increase
The rate of recovery of isolated ethylene and propylene.
Method according to the present invention, dethanizer can clearly separate C2 and C3 component, by controlling dethanizer
Condition in above-mentioned preferred scope, the molar content of propylene in deethanizer overhead can be made not higher than 0.5%, it is excellent
Choosing is not higher than 0.1%.
Method according to the present invention, it is preferable that successively carry out the overhead product of step (5) deethanization processing to add hydrogen
And ethylene distillation, by conventional method or intermediate extraction method from ethylene rectifying column obtains ethylene according to process requirements selection, and
Ethylene distillation tower reactor product is ethane, by compressor section similar in ethylene distillation tower top product returning pressure.Wherein, add hydrogen to be for
Acetylene is converted into ethylene, which can be provided by well-known technique.Since dethanizer is sent into the material of ethylene rectifying column
In be likely present a certain amount of methane, the method that can choose intermediate extraction obtains polymer grade ethylene production in ethylene rectifying column
Product, the general position that produces can choose the 2nd piece to 8 blocks column plates of counting from top to bottom.
Method according to the present invention, it is preferable that cooled down after the overhead product of step (5) deethanization processing is added hydrogen
It is passed through ethylene rectifying column again to -35 DEG C~-10 DEG C and carries out ethylene distillation.Wherein, the cooling can be recycled by ethylene distillation
The cooling capacity generated in the process carries out, in order to further decrease energy consumption.
The condition of method according to the present invention, ethylene distillation can be the condition of the ethylene distillation of this field routine,
Such as may include: ethylene rectifying column number of theoretical plate be 100-150 block, operating pressure 0.8-2.6MPa, tower top temperature be-
39 DEG C~-15 DEG C, bottom temperature is -20 DEG C~0 DEG C.
Method according to the present invention, it is preferable that the tower kettle product of step (5) deethanization processing is subjected to propylene essence
It evaporates, propylene is obtained from propylene rectification tower by intermediate extraction method, propylene rectification tower kettle product is propane.It is intermediate used by herein
The specific method of extraction method can be identical as the intermediate extraction method of ethylene is obtained, except that the selection of extraction position is from top to bottom
It counts between 2-15 block column plate.
The condition of method according to the present invention, propylene rectifying can be the condition of the propylene rectifying of this field routine,
Such as may include: the number of theoretical plate of propylene rectification tower be 110-400 block, operating pressure 0.8-2.6MPa, tower top temperature is
10 DEG C -55 DEG C, bottom temperature is 35 DEG C -60 DEG C.
The isolated Recovery rate of ethylene of method of the invention is 95% or more, and propylene recovery rate is 95% or more.
Embodiment
Methanol to olefins reaction gas is by ethylene, propylene, methane, hydrogen and other components (nitrogen, oxynitrides, an oxygen
Change carbon, carbon dioxide, dimethyl ether, water, methanol, ethane, acetylene, propane, allene, normal butane, iso-butane, 1- butylene, 2- fourth
Alkene, 1,3- butadiene, cis-2-butene, Trans-2-butene, pentane, isopentane, 1- amylene, n-hexane, isohexane, hexene, benzene,
Toluene, paraxylene, meta-xylene, ortho-xylene and 1,3,5- trimethylbenzenes) composition, wherein the content of methane is rubbed for 4.1
Your %, hydrogen content be 1.8 moles of %, the content of ethylene is 40.7 moles of %, and the content of propylene is 37.5 moles of %, and water is
5.7 moles of %, other groups are divided into 10.2 moles of %.
Embodiment 1
The present embodiment is used to illustrate the separation method of methanol to olefins reaction gas of the invention.
(1) compression processing is carried out as shown in Figure 1, methanol to olefins reaction gas is passed through in compression unit, the compression is single
Member is made 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, using 30
DEG C circulating water, methanol to olefins reaction gas pressure after the compression unit compression processing rise to 3.8MPa step by step,
In, (pressure 0.55MPa) is disposed with caustic wash tower and water scrubber progress alkali cleaning after paragraph 1 compressor section exports drain tank
Processing and washing process, lye is sprayed into tower from alkali cleaning column overhead and is come into full contact with unstrpped gas in alkali cleaning treatment process, is washed
It is sprayed into tower using demineralized water from washing column overhead in treatment process and is come into full contact with unstrpped gas, in compression process, meeting
Gas phase, water phase and oil-phase product are generated, every section of compressor section is generated into the entrance that water phase returns to the preceding paragraph compressor section, and final
It is sent into stripper recycling hydrocarbons and avoids significant loss, the oil that the 3rd section of compressor outlet gas generates after cooling mutually enters
Domethanizing column does not generate oily phase between compressor section；
(2) gas phase that compression processing obtains is carried out being cooled to 15 DEG C, unstrpped gas after cooling is gas-liquid two-phase, is not required to
Will drying can be sent directly into domethanizing column, the cold water that refrigerant used is 5 DEG C or so, cold water can be by suction-type lithium bromide system
Cold provides；
(3) as shown in Fig. 2, by absorbent (content of normal butane is 35 weight %, the content of iso-butane be 15 weight %,
The content of 1- butylene is 6 weight %, the content of Trans-2-butene is 14 weight %, the content of cis-2-butene is 10 weight %, just
The content that the content of pentane is 5 weight %, the content of isopentane is 5 weight %, 1- amylenes is 10 weight %) 15 DEG C are cooled to,
It then passes in domethanizing column, the gas-liquid two-phase logistics obtained after above-mentioned cooling is passed through in domethanizing column and is carried out at demethanation
Reason, the molar ratio that the dosage and compressor outlet gas of absorbent enter the logistics of domethanizing column after cooling is 1:1.5, piptonychia
Alkane tower absorber portion is provided with intercooler, and the temperature of intercooler is 15 DEG C, by the number of theoretical plate for controlling domethanizing column
It is 50 pieces, operating pressure 3.6MPa, tower top temperature is 25 DEG C, is 70.5 DEG C by control bottom temperature, so that in tower bottoms
Methane content control is 30ppm；In addition, the overhead product that demethanation is handled is passed through in surge tank again using PSA hydrogen manufacturing
Technology prepares hydrogen and methane, and the purity of hydrogen obtained is 99.99%；
(4) tower bottoms for handling demethanation 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 31.7 DEG C, and bottom temperature is 128.2 DEG C, wherein tower bottoms
The molar content of middle C3 component is 7.6%；
(5) depropanization is handled to obtain tower bottoms as the heat source of demethanation processing and deethanization processing, most afterwards through recycling
Water and cold water are cooled to 15 DEG C step by step, and a portion submitting battery limit (BL) is first sent to debutanizing tower, then by remaining circulation solvent
It is mixed with a part of fresh absorbent and is passed through in domethanizing column (ratio of circulation solvent and fresh absorbent is 1:0.03),
The molar ratio for guaranteeing the logistics that the dosage of absorbent enters domethanizing column with compressor outlet gas after cooling is 1:1.5.It will
The overhead product of depropanization processing carries out being cooled to 6.9 DEG C after using molecular sieve drying system dry, which passes through ethylene essence
It evaporates the cooling capacity generated in removal process to carry out, the concrete operation method of molecular sieve drying system are as follows: it is standby that drier needs one open one
Alternate run, when alternate run, previously run one needed to carry out regenerative operation.When regenerative operation, need nitrogen through excessively high
It is used to regenerate desiccant after pressure steam heating.The overhead product that depropanization after cooling is handled is passed through in dethanizer
Deethanization processing is carried out, the number of theoretical plate of dethanizer is 80 pieces, operating pressure 2.3MPa, and tower top temperature is -22.3 DEG C, tower
Kettle temperature degree is 55.1 DEG C, so that the molar content of propylene is 0.005% in deethanizer overhead；
(6) by the overhead product of step (5) deethanization processing carry out plus hydrogen after be cooled to -22.7 DEG C and be passed through ethylene rectifying column
Ethylene distillation is carried out, the cooling can be carried out by the cooling capacity generated in ethylene distillation removal process, the reason of ethylene rectifying column
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 tower overhead gas product is ethylene；
(7) tower kettle product by the processing of step (5) deethanization carries out propylene rectifying, using intermediate extraction method from propylene rectifying
Tower obtains propylene, and propylene rectification tower kettle product is propane, by compressor section similar in propylene rectification tower overhead product returning pressure,
Between propylene extraction position selection counts the 15th block of column plate of 2- from top to bottom, the number of theoretical plate of propylene rectification tower is 170 pieces, operation
Pressure is 1.95MPa, and tower top temperature is 18.9 DEG C, and bottom temperature is 53.7 DEG C.
Embodiment 2
The present embodiment is used to illustrate the separation method of methanol to olefins reaction gas of the invention.
(1) methanol to olefins reaction gas is passed through in compression unit and carries out compression processing, the compression unit is compressed by 3 sections
Machine Duan Zucheng, every section of outlet temperature of compressor section are no more than 140 DEG C, and every section of inlet temperature is 40 DEG C, using 30 DEG C of recirculated water coolings
But, methanol to olefins reaction gas pressure after the compression unit compression processing rises to 3.8MPa step by step, wherein in the 2nd pressure
(pressure 1.8MPa) is disposed at caustic wash tower and water scrubber progress alkali cleaning processing and washing after contracting machine section outlet drain tank
It manages, lye is sprayed into tower from alkali cleaning column overhead and come into full contact with unstrpped gas in alkali cleaning treatment process, is adopted during washing process
It is sprayed into tower with demineralized water from washing column overhead and is come into full contact with unstrpped gas, in compression process, gas phase, water phase can be generated
And oil-phase product, every section of compressor section is generated into water phase and returns to the entrance of the preceding paragraph compressor section, and is ultimately delivered to stripper and returns
It receives hydrocarbons and avoids significant loss, the oil that the 3rd section of compressor outlet gas generates after cooling mutually enters domethanizing column, compression
Oily phase is not generated between machine section；
(2) gas phase that compression processing obtains is carried out being cooled to 15 DEG C, unstrpped gas after cooling is gas-liquid two-phase, is not required to
Will drying can be sent directly into domethanizing column, the cold water that refrigerant used is 5 DEG C or so, cold water can be by suction-type lithium bromide system
Cold provides；
(3) as shown in Fig. 2, by absorbent (content of normal butane is 10 weight %, the content of iso-butane be 25 weight %,
The content of 1- butylene is 15 weight %, the content of Trans-2-butene is 24 weight %, the content of cis-2-butene is 6 weight %, just
The content that the content of pentane is 5 weight %, the content of isopentane is 5 weight %, 1- amylenes is 10 weight %) 15 DEG C are cooled to,
It then passes in domethanizing column, the gas-liquid two-phase logistics obtained after above-mentioned cooling is passed through in domethanizing column and is carried out at demethanation
Reason, the molar ratio that the dosage and compressor outlet gas of absorbent enter the logistics of domethanizing column after cooling is 1.5:1, piptonychia
Alkane tower absorber portion is provided with intercooler, and the temperature of intercooler is 15 DEG C, by the number of theoretical plate for controlling domethanizing column
It is 35 pieces, operating pressure 3.6MPa, tower top temperature is 28.3 DEG C, and bottom temperature is 69.5 DEG C, so that methane contains in tower bottoms
Amount control is 30ppm；In addition, the overhead product that demethanation is handled is passed through in surge tank again using PSA hydrogen producing technology system
Standby hydrogen and methane, the purity of hydrogen obtained are 99.9%；
(4) tower bottoms for handling demethanation 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 117 DEG C, wherein in tower bottoms
The molar content of C3 component is 15.3%；
(5) depropanization is handled to obtain tower bottoms as the heat source of demethanation processing and deethanization processing, most afterwards through recycling
Water and cold water are cooled to 15 DEG C step by step, and a portion submitting battery limit (BL) is first sent to debutanizing tower, then by remaining circulation solvent
It is mixed with a part of fresh absorbent and is passed through in domethanizing column (ratio of circulation solvent and fresh absorbent is 1:0.02),
The molar ratio for guaranteeing the logistics that the dosage of absorbent enters domethanizing column with compressor outlet gas after cooling is 1.5:1, will
The overhead product of depropanization processing carries out being cooled to 6.7 DEG C after using molecular sieve drying system dry, which passes through ethylene essence
It evaporates the cooling capacity generated in removal process to carry out, the concrete operation method of molecular sieve drying system are as follows: it is standby that drier needs one open one
Alternate run, when alternate run, previously run one needed to carry out regenerative operation.When regenerative operation, need nitrogen through excessively high
It is used to regenerate desiccant after pressure steam heating.The overhead product that depropanization after cooling is handled is passed through in dethanizer
Deethanization processing is carried out, the number of theoretical plate of dethanizer is 70 pieces, operating pressure 2.3MPa, and tower top temperature is -22.3 DEG C, tower
Kettle temperature degree is 55.1 DEG C, so that the molar content of propylene is 0.005% in deethanizer overhead；
(6) by the overhead product of step (5) deethanization processing carry out plus hydrogen after be cooled to -22.7 DEG C and be passed through ethylene rectifying column
Ethylene distillation is carried out, the cooling can be carried out by the cooling capacity generated in ethylene distillation removal process, the reason of ethylene rectifying column
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 tower overhead gas product is ethylene；
(7) tower kettle product by the processing of step (5) deethanization carries out propylene rectifying, using intermediate extraction method from propylene rectifying
Tower obtains propylene, and propylene rectification tower kettle product is propane, by compressor section similar in propylene rectification tower overhead product returning pressure,
Between propylene extraction position selection counts the 15th block of column plate of 2- from top to bottom, the number of theoretical plate of propylene rectification tower is 180 pieces, operation
Pressure is 1.85MPa, and tower top temperature is 19.2 DEG C, and bottom temperature is 51.2 DEG C.
Embodiment 3
The present embodiment is used to illustrate the separation method of methanol to olefins reaction gas of the invention.
(1) methanol to olefins reaction gas is passed through in compression unit and carries out compression processing, the compression unit is compressed by 3 sections
Machine Duan Zucheng, every section of outlet temperature of compressor section are no more than 140 DEG C, and every section of inlet temperature is 40 DEG C, using 30 DEG C of recirculated water coolings
But, methanol to olefins reaction gas pressure after the compression unit compression processing rises to 3.8MPa step by step, wherein in the 2nd pressure
(pressure 1.8MPa) is disposed at caustic wash tower and water scrubber progress alkali cleaning processing and washing after contracting machine section outlet drain tank
It manages, lye is sprayed into tower from alkali cleaning column overhead and come into full contact with unstrpped gas in alkali cleaning treatment process, is adopted during washing process
It is sprayed into tower with demineralized water from washing column overhead and is come into full contact with unstrpped gas, in compression process, gas phase, water phase can be generated
And oil-phase product, every section of compressor section is generated into water phase and returns to the entrance of the preceding paragraph compressor section, and is ultimately delivered to stripper and returns
It receives hydrocarbons and avoids significant loss, the oil that the 3rd section of compressor outlet gas generates after cooling mutually enters domethanizing column, compression
Oily phase is not generated between machine section；
(2) gas phase that compression processing obtains is carried out being cooled to 15 DEG C, unstrpped gas after cooling is gas-liquid two-phase, is not required to
Will drying can be sent directly into domethanizing column, the cold water that refrigerant used is 5 DEG C or so, cold water can be by suction-type lithium bromide system
Cold provides；
(3) as shown in Fig. 2, by absorbent (content of normal butane is 35 weight %, the content of iso-butane be 15 weight %,
The content of 1- butylene is 14 weight %, the content of Trans-2-butene is 6 weight %, the content of cis-2-butene is 10 weight %, just
The content that the content of pentane is 5 weight %, the content of isopentane is 10 weight %, 1- amylenes is 5 weight %) 15 DEG C are cooled to,
It then passes in domethanizing column, the gas-liquid two-phase logistics obtained after above-mentioned cooling is passed through in domethanizing column and is carried out at demethanation
Reason, the molar ratio that the dosage and compressor outlet gas of absorbent enter the logistics of domethanizing column after cooling is 1:1, demethanation
Tower absorber portion is provided with intercooler, and the temperature of intercooler is 15 DEG C, and the number of theoretical plate by controlling domethanizing column is
30 pieces, operating pressure 3.6MPa, tower top temperature is 24.4 DEG C, and bottom temperature is 68.9 DEG C, so that methane content in tower bottoms
Control is 300ppm；It is prepared again using PSA hydrogen producing technology in addition, the overhead product that demethanation is handled is passed through in surge tank
Hydrogen and methane, the purity of hydrogen obtained are 99.9%；
(4) tower bottoms for handling demethanation 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 128.1 DEG C, wherein tower bottoms
The molar content of middle C3 component is 7.6%；
(5) depropanization is handled to obtain tower bottoms as the heat source of demethanation processing and deethanization processing, most afterwards through recycling
Water and cold water are cooled to 15 DEG C step by step, and a portion submitting battery limit (BL) is first sent to debutanizing tower, then by remaining circulation solvent
It is mixed with a part of fresh absorbent and is passed through in domethanizing column (ratio of circulation solvent and fresh absorbent is 1:0.02),
The molar ratio for guaranteeing the logistics that the dosage of absorbent enters domethanizing column with compressor outlet gas after cooling is 1:1.It will take off
The overhead product of propane processing carries out being cooled to 5.8 DEG C after using molecular sieve drying system dry, which passes through ethylene distillation
The cooling capacity generated in removal process carries out, the concrete operation method of molecular sieve drying system are as follows: drier needs one to open a standby friendship
For operation, when alternate run, previously run one needed to carry out regenerative operation.When regenerative operation, need nitrogen by high pressure
It is used to regenerate desiccant after steam heating.By the overhead product that depropanization after cooling is handled be passed through in dethanizer into
The processing of row deethanization, the number of theoretical plate of dethanizer are 60 pieces, operating pressure 2.3MPa, and tower top temperature is -22.4 DEG C, tower reactor
Temperature is 55.1 DEG C, so that the molar content of propylene is 0.003% in deethanizer overhead；
(6) by the overhead product of step (5) deethanization processing carry out plus hydrogen after be cooled to -22.9 DEG C and be passed through ethylene rectifying column
Ethylene distillation is carried out, the cooling can be carried out by the cooling capacity generated in ethylene distillation removal process, the reason of ethylene rectifying column
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, ethylene is obtained from ethylene rectifying column using intermediate extraction method, by ethylene distillation tower top product returning pressure phase
Close compressor section, ethylene extraction position selection are counted from top to bottom between 2-8 block column plate；
(7) tower kettle product by the processing of step (5) deethanization carries out propylene rectifying, using intermediate extraction method from propylene rectifying
Tower obtains propylene, and propylene rectification tower kettle product is propane, by compressor section similar in propylene rectification tower overhead product returning pressure,
Between propylene extraction position selection counts the 15th block of column plate of 2- from top to bottom, the number of theoretical plate of propylene rectification tower is 260 pieces, operation
Pressure is 1.95MPa, and tower top temperature is 18.9 DEG C, and bottom temperature is 53.7 DEG C.
Embodiment 4
The present embodiment is used to illustrate the separation method of methanol to olefins reaction gas of the invention.
Methanol to olefins reaction gas is separated according to the method for embodiment 1, unlike, the gas that the compression processing obtains
The cooling temperature of phase, absorbent and domethanizing column intercooler is 25 DEG C.
Embodiment 5
The present embodiment is used to illustrate the separation method of methanol to olefins reaction gas of the 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 20 pieces, operating pressure 5.0MPa, and tower top temperature is 33.7 DEG C, and bottom temperature is 93.7 DEG C, so that first in tower bottoms
The control of alkane content is 608ppm.
Comparative example 1
Methanol to olefins reaction gas is separated according to the method for embodiment 1, unlike, by the theory for controlling domethanizing column
Plate number is 35 pieces, operating pressure 2.9MPa, and tower top temperature is 41 DEG C, and bottom temperature is 60.6 DEG C, so that methane in tower bottoms
Content control is 30ppm.
Table 1
Note: steam is the saturated vapor of 0.4MPa.
Can be seen that the isolated Recovery rate of ethylene of method of the invention by 1 data of table is 95% or more, and purity is
99.95% or more, propylene recovery rate is 95% or more, and purity is 99.5% or more, and low energy consumption, operating flexibility is big for this method,
It can be according to product adjustment of yield energy consumption technological parameter.
This method is using the component of the hydrocarbon containing C4-C5 as in absorbent methanol removal alkene (MTO/DMTO) reaction gas
The light components such as methane, and in 10 DEG C or more operation temperature section methanol removal alkene (MTO/DMTO) product gas
Methane and light fraction, effectively inhibit water and hydro carbons to form hydrate.In addition, drying process of the invention does not need to place
It is exported in compression unit, it is only necessary to deethanizer overhead gas is dried, avoided solidifying to compression unit outlet liquid phase
Liquid is dried, and significantly reduces drying process treating capacity, considerably reduce therewith public work nitrogen consumption and
Energy consumption.Demethanation process is switched to thermal release process and is conducive to heat exchange network optimization by this method, and it is below not need -40 DEG C of investment
Cryogen.With the features such as small investment, material recovery rate is high.
The preferred embodiment of the present invention has been described above in detail, still, during present invention is not limited to the embodiments described above
Detail within the scope of the technical concept of the present invention can be with various simple variants of the technical solution of the present invention are made, this
A little simple variants all belong to the scope of protection of the present invention.
It is further to note that specific technical features described in the above specific embodiments, in not lance
In the case where shield, can be combined in any appropriate way, in order to avoid unnecessary repetition, the present invention to it is various can
No further explanation will be given for the combination of energy.
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 also be regarded as the disclosure of the present invention.
Claims (18)
1. a kind of separation method of methanol to olefins reaction gas, which is characterized in that this method comprises:
(1) methanol to olefins reaction gas is passed through in compression unit and carries out compression processing, during the compression processing into
Row alkali cleaning and washing；
(2) gas phase for obtaining compression processing cools down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is not needed into drying and is directly taken off in domethanizing column
Methane processing；
(4) tower kettle product for handling demethanation carries out depropanization processing in depropanizing tower；
(5) deethanization processing will be carried out in dethanizer after the overhead product drying of depropanization processing；
Wherein, the gaseous pressure that the compression processing makes is 3.2-6.0MPa, described to be cooled to temperature in step (2)
10-30 DEG C, the absorbent is C4-C5 hydrocarbon, and the temperature of the absorbent is 10-30 DEG C, the condition packet of the demethanation processing
Include: domethanizing column number of theoretical plate is 20-60 block, and operating pressure 3.0-5.8MPa, tower top temperature is 10-40 DEG C, bottom temperature
It is 60-120 DEG C.
2. according to the method described in claim 1, wherein, the absorbent contains normal butane, iso-butane, 1- butylene, trans- 2- fourth
Alkene, cis-2-butene, pentane, isopentane, 1- amylene.
3. according to the method described in claim 2, wherein, on the basis of the total weight of absorbent, the content of normal butane is 10-50
Weight %, the content of iso-butane be the content of 10-50 weight %, 1- butylene be 5-15 weight %, the content of Trans-2-butene is 5-
35 weight %, cis-2-butene content be 5-35 weight %, pentane 5-35 weight %, isopentane content be 5-35 weigh
The content for measuring %, 1- amylene is 5-35 weight %, and the sum of each component content is no more than 100%.
4. according to the method described in claim 1, wherein, the temperature of the absorbent is 15-20 DEG C.
5. according to the method described in claim 1, wherein, in step (2), the temperature that is cooled to is 15-20 DEG C.
6. methanol-to-olefins are anti-according to the method described in claim 1, wherein, the compression unit includes 3-5 sections of compressor sections
Should gas pressure after the compression unit compression processing rise to 3.2-6.0MPa step by step.
7. method according to claim 1 or 6, wherein the alkali cleaning and washing under 0.3-3.0MPa operating pressure into
Row.
8. according to the method described in claim 1, wherein, this method further include: the overhead product for handling demethanation into
Row PSA hydrogen manufacturing, obtains hydrogen.
9. according to the method described in claim 1, wherein, the condition of the depropanization processing includes: depropanizing tower number of theoretical plate
For 15-50 block, operating pressure 1.5-3.5MPa, tower top temperature is 10-50 DEG C, and bottom temperature is 100-160 DEG C.
10. according to the method described in claim 1, wherein, the condition of the deethanization processing includes: dethanizer number of theoretical plate
For 25-120 block, operating pressure 1.0-3.0MPa, tower top temperature is -30~-10 DEG C, and bottom temperature is 50-80 DEG C.
11. according to the method described in claim 1, wherein, this method further include: in step (5), by the tower top of depropanization processing
- 10 DEG C~30 DEG C, which are cooled to, after product is dry carries out deethanization processing again.
12. according to the method described in claim 1, wherein, this method further include: produce the tower top of step (5) deethanization processing
Object successively carries out plus hydrogen and ethylene distillation, and by conventional method or intermediate extraction method from ethylene rectifying column obtains ethylene, and second
Alkene rectifying tower reactor product is ethane, by compressor section similar in ethylene distillation tower top product returning pressure.
13. according to the method for claim 12, wherein the condition of the ethylene distillation includes: the theory of ethylene rectifying column
Plate number be 100-150 block, operating pressure 0.8-2.6MPa, tower top temperature be -39 DEG C~-15 DEG C, bottom temperature be -20 DEG C~
0℃。
14. according to the method described in claim 1, wherein, this method further include: produce the tower reactor of step (5) deethanization processing
Object carries out propylene rectifying, obtains propylene from propylene rectification tower by intermediate extraction method, propylene rectification tower kettle product is propane.
15. according to the method for claim 14, wherein the condition of the propylene rectifying includes: the theory of propylene rectification tower
Plate number is 110-400 block, 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.
16. according to the method described in claim 1, wherein, this method further include: gas is produced after cooling between compression process section
Raw oil enters depropanizing tower after mutually pressurizeing, generated oil mutually enters domethanizing column to compressor outlet gas after cooling.
17. according to the method described in claim 1, wherein, this method further include: depropanization is handled to obtain tower bottoms as de-
The absorbent of methane processing recycles.
18. according to the method for claim 17, wherein before recycling as absorbent, depropanization is handled to obtain
The heat source that tower bottoms is first used as demethanation processing and deethanization to handle.
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| US7714180B2 (en) * | 2003-04-04 | 2010-05-11 | Exxonmobil Chemical Patents Inc. | Process and apparatus for recovering olefins |
| CN102115355A (en) * | 2010-12-27 | 2011-07-06 | 东华工程科技股份有限公司 | Method for separating low-carbon olefins |
| CN103443059A (en) * | 2011-03-29 | 2013-12-11 | Mt创新中心名下斯塔米卡邦有限责任公司 | Method for olefins production |
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| US7714180B2 (en) * | 2003-04-04 | 2010-05-11 | Exxonmobil Chemical Patents Inc. | Process and apparatus for recovering olefins |
| CN102115355A (en) * | 2010-12-27 | 2011-07-06 | 东华工程科技股份有限公司 | Method for separating low-carbon olefins |
| CN103443059A (en) * | 2011-03-29 | 2013-12-11 | Mt创新中心名下斯塔米卡邦有限责任公司 | Method for olefins production |
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