CN106631664A - Separation method for methanol-to-olefin reaction gas - Google Patents
Separation method for methanol-to-olefin reaction gas Download PDFInfo
- Publication number
- CN106631664A CN106631664A CN201510711458.2A CN201510711458A CN106631664A CN 106631664 A CN106631664 A CN 106631664A CN 201510711458 A CN201510711458 A CN 201510711458A CN 106631664 A CN106631664 A CN 106631664A
- Authority
- CN
- China
- Prior art keywords
- tower
- gas
- temperature
- absorbent
- content
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- 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
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a separation method for methanol-to-olefin reaction gas. The separation method has the advantages that component containing C4-C5 hydrocarbons is used as an absorbent for removing light components such as methane in the methanol-to-olefin (MTO/DMTO) reaction gas and removing the methane and light fractions in the methanol-to-olefin (MTO/DMTO) reaction gas in an operation temperature range above 10 DEG C so as to inhibit that water and the hydrocarbons form hydrates effectively; a drying process does not need to be conducted at a compressed unit outlet, and only overhead gas of a dethanizing column needs to be subjected to drying treatment, so that drying liquid-phase condensate at the compressed unit outlet is avoided, treatment capacity of the drying process is reduced substantially, and public engineering nitrogen consumption and energy consumption are reduced substantially; optimization of a heat exchanger network is facilitated by means of converting a demethanation process into a heat separation process without injection of refrigerants below minus 40 DEG C; the separation method is low in investment and high in material recovery ratio.
Description
Technical field
The present invention relates to methanol-to-olefins field, in particular it relates to a kind of methanol to olefins reaction gas point
From method.
Background technology
Based on coal, coal is for a long time as China's basic energy resource and important industrial chemicals for China's energy resource structure.
Modern Coal-based Chemical is important directions that coal high-efficiency clean conversion is utilized based on clean coal technology.
2014, China produced ethylene volume per year and has been added to more than 1,700 ten thousand tons.National economy is to ethene and propylene
Wilderness demand rely primarily on oil, the average annual consumption figure of China's oil is improved to more than 500,000,000 tons.With coal
Alkene technology processed undoubtedly becomes national economy and social development and provides important for the Modern Coal-based Chemical of representative
Support, is also the needs for ensureing national energy security.The breakthrough of preparing low carbon olefinic hydrocarbon with methanol technology and its industry
Change, 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 ground with catalyst
System and reactor development are designed as core；Isolation technics then with product as raw material, Jing impurity removals,
The ethene and propylene product of the process production polymer grade such as compression, separation, its core is impurity removal and separation
The exploitation and design of flow process.
The separation of polymer grade ethylene and propylene is obtained from methanol-to-olefins (MTO/DMTO) product gas
Technique is generally divided into four units：Compression unit, imurity-removal unit, cold separative element and thermal release list
Unit.Wherein, compression unit main task is (MTO/DMTO) product gas to be improved to subsequent technique
Desirable pressure.Imurity-removal unit main task is unreacted in removing (MTO/DMTO) product gas
Raw material is methyl alcohol, and intermediate reaction product is dimethyl ether (DME), sour gas such as carbon dioxide, NOx
Deng, according to action required condition difference can between compressor section Jing washings, alkali cleaning etc. operation remove wherein
Partial impurities.Cold separative element is the separative element of the temperature range below 0 DEG C, such as demethanation, de-
The process such as ethane and ethylene distillation.Thermal separation process is the separative element bag of the temperature range more than 0 DEG C
Include the processes such as depropanization, propylene rectifying.
The removal of the light components methane in impurity is the key for obtaining high-purity polymer grade ethylene.At this stage
Commonplace method is separation by deep refrigeration and absorption and separation method.Patent application CN200810201217.3
A kind of separation method of light hydrocarbon product in MTO/MTP product is disclosed, the method is made using ethane
The light components in product are successively excluded through absorption tower and domethanizing column two-stage absorption process for absorbent,
About -65 DEG C of chilling temperature, finally by rectifying the ethene of 90%-99.99% can be obtained.Using ethane
Relatively low as the absorption temperature required for absorbent, the ethene that -100 DEG C are needed in engineer applied freezes compression
Machine, in addition -135 DEG C methane compressor provide cold, improve the investment of equipment and increased energy consumption.
Patent application CN201110279313.1 discloses a kind of low-carbon (LC) separation of hydrocarbons and methanol-to-olefins
(M-OS/MTO) gas separating technology flow process, the method is using front-end demethanization tower, depropanizing tower and takes off
Butane tower tower reactor effluent absorbs carbon two and the component of carbon three in product gas as absorbent, by methane etc.
Light ends are separated from product gas.The method needs the temperature demethanation at -40 DEG C or so, and the party
It is front-end deethanization in method.
Patent application CN201310216950.3 discloses one kind and reclaims from MTO/DMTO product gas
The system and method for ethene, the method sets up cold recovery device after domethanizing column, reduces system energy
Consumption, and Recovery rate of ethylene is more than 99.7%, however it is necessary that ice chest, energy consumption is larger.
The method of patent application WO2009/015507 preparing low-carbon olefin of polymerization-grade of pyrolysis gas separation of methanol,
Methane is removed using the method for absorption and separation, 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 below 0 DEG C, and be front ethane or
Person's propane, therefore, methane and other lighter hydrocarbons such as ethane, ethene and propylene etc. can be caused easily to be formed with water
Hydrocarbon hydrate, this kind of hydrate easily makes valve below 0 DEG C and pipeline occurs the phenomenon of frozen block, and
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 that methanol to olefins reaction gas is separated in prior art
Consumption is larger, easily causes the defect of line clogging etc., there is provided a kind of 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,
The method includes：
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed process；
(2) compression is processed the gas phase for obtaining to be cooled down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is taken off in domethanizing column
Methane process；
(4) demethanation is processed the tower kettle product for obtaining carries out depropanization process in depropanizing tower；
(5) deethanization process is carried out in dethanizer after the overhead product of depropanization process is dried；
Wherein, it is 3.2-6.0MPa that the compression processes the gaseous pressure for obtaining, in step (2),
Described to be cooled to temperature for 10-30 DEG C, the absorbent contains C4-C5 hydrocarbon, what the demethanation was processed
Condition includes：Domethanizing column number of theoretical plate is 20-60 blocks, and operating pressure is 3.0-5.8MPa, tower top temperature
Spend for 10-40 DEG C, bottom temperature is 60-120 DEG C.
Methanol-to-olefins (MTO/DMTO) the method gas separation method of the present invention has advantages below：
(1) in the method for the present invention, using the component containing C4-C5 hydrocarbon as absorbent methanol removal alkene
The light components such as the methane in hydrocarbon (MTO/DMTO) reaction gas, raw sorbent is readily available, into
This is cheap；
(2) operation temperature interval methanol removal alkene (MTO/DMTO) product more than 10 DEG C
Methane and light ends in gas, effectively inhibits water and hydro carbons to form hydrate；
(3) in the method for the present invention, dry run need not be placed on compression unit outlet, it is only necessary to
Process is dried to deethanizer overhead gas, it is to avoid compression unit outlet liquid phase lime set is done
It is dry, significantly reduce the consumption and energy consumption of public work nitrogen.
(4) in the method for the present invention, overall process minimum temperature is not less than -40 DEG C, it is not necessary to use ethene
Refrigeration unit, material can select general low temperature carbon steel, and energy consumption is low, reduce investment outlay；
(5) method of the present invention can obtain the very high polymer grade ethylene of purity and propylene product, and second
The alkene rate of recovery is more than 95%, and 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.
Description of the drawings
Fig. 1 is a kind of compression process flow chart of specific embodiment of the invention.
Fig. 2 is a kind of methanol to olefins reaction gas separating technology flow chart of specific embodiment of the invention.
Specific embodiment
The specific embodiment of the present invention is described in detail below.It should be appreciated that this place is retouched
The specific embodiment stated is merely to illustrate and explains the present invention, is not limited to the present invention.
The reaction gas of methanol-to-olefins (MTO/DMTO) reactor per se with a large amount of saturation waters, and
And subtractive process commonly uses the operation such as alkali cleaning and washing, this causes to satisfy in a large number in the material of separation process
And water.Below 0 DEG C, operating pressure is more than 2.0MPa to the operation temperature of existing demethanation process.This
Under the conditions of kind, methane and other lighter hydrocarbons such as ethane, ethene and propylene etc. easily form hydrocarbon hydrate with water,
This kind of hydrate easily makes valve and pipeline that frozen block phenomenon occurs below 0 DEG C.So, typically in methyl alcohol
Alkene (MTO/DMTO) reaction gas processed needs dried process just to enter follow-up point after compression unit
From unit.It is due to traditional methanol-to-olefins product to select in compression unit port of export dry feedstock gas
The separating technology of gas is usually from the beginning of deethanization process.First by ethane and more light component from unstripped gas
Separate, the component of natural gas such as methane, carbon monoxide, nitrogen is needed in follow-up separation in this case
During remove in the ethene of relative lightweight, ethane from product gas, and this process is below 0 DEG C
Cold separation process in complete, so having to remove saturation water in the compression unit port of export.
Another problem of product gas elder generation deethanization through being dried and compressing is detrimental to heat-exchange network
Optimization.Because the operating pressure of general dethanizer is 2.5MPa or so, tower top operation temperature is -20 DEG C
Left and right, tower reactor operation temperature is 65 DEG C or so.Deethanizer overhead gas starts to take off into cold separative element
Ethene and demethanation process, tower reactor liquid starts depropanization process into thermal release unit.De- ethene and de-
The pressure of the cold separation process of methane is typically in 2.3MPa or so, and operation temperature is for -35 DEG C and following.For
The deep cooling process is avoided to need to use the tower bottoms of depropanizing tower as absorbent.The operation pressure of depropanizing tower
Power 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 temperature that the tower bottoms of 90 DEG C or so depropanizing towers is cooled to -35 DEG C of temperature below
Scope.And the logistics of the needs heating in thermal release unit is less with the temperature difference of depropanizing tower tower bottoms, no
Beneficial to heat recovery and utilization, and need to put into a large amount of colds.
Therefore, in order to overcome prior art in the drawbacks described above that exists because of first deethanization.
The invention provides a kind of separation method of methanol to olefins reaction gas, the method includes：
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed process；
(2) compression is processed the gas phase for obtaining to be cooled down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is taken off in domethanizing column
Methane process；
(4) demethanation is processed the tower kettle product for obtaining carries out depropanization process in depropanizing tower；
(5) deethanization process is carried out in dethanizer after the overhead product of depropanization process is dried；
Wherein, it is 3.2-6.0MPa that the compression processes the gaseous pressure for obtaining, in step (2),
Described to be cooled to temperature for 10-30 DEG C, the absorbent contains C4-C5 hydrocarbon, what the demethanation was processed
Condition includes：Domethanizing column number of theoretical plate is 20-60 blocks, and operating pressure is 3.0-5.8MPa, tower top temperature
Spend for 10-40 DEG C, bottom temperature is 60-120 DEG C.
Preferably, the condition that the demethanation is processed includes：Domethanizing column number of theoretical plate is 30-50 blocks,
Operating pressure is 3.0-4.5MPa, and tower top temperature is 10-40 DEG C, and bottom temperature is 60-120 DEG C, so as to
The rate of recovery of ethene and propylene can be improved and system energy consumption is reduced.
In the present invention, in methanol to olefins reaction gas can containing hydrogen, nitrogen, oxynitrides, one
Carbonoxide, carbon dioxide, dimethyl ether, water, methane, methyl alcohol, ethane, ethene, acetylene, propane,
Propylene, allene, normal butane, 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.Wherein, the content of ethene can be with
For 25-95 mole of %, the content of propylene can be 5-49 mole of %, and the content of methane can rub for 0-10
You are %, and the content of hydrogen can be 0-10 mole of %, and the total content of other components can be 0-30 mole of %.
According to method of the present invention, it is preferable that in step (1), the compression unit includes 3-5
Section compressor section, methanol to olefins reaction gas pressure after compression unit compression process rises to step by step
3.2-6.0MPa.Wherein, every section of outlet temperature of compressor section is usually no more than 140 DEG C according to technological requirement,
Every section of inlet temperature is 40 DEG C or so, generally adopts 25-35 DEG C of circulating water.
According to method of the present invention, it is preferable that the compression process during carry out alkali cleaning and
Washing, wherein, the order for washing alkali cleaning is not specially required, when sour gas is more in unstripped gas,
Can first alkali cleaning wash again, when methyl alcohol, dimethyl ether etc. are more in unstripped gas, can first wash alkalescence again.
According to method of the present invention, it is highly preferred that the alkali cleaning and washing are in 0.3-3.0MPa operating pressures
Under carry out.Usually, alkali cleaning and water-washing step can be carried out in 1-3 section compressor sections exit.
In the present invention, washing be in order to remove unstripped gas in organic oxygen compound, such as methyl alcohol, dimethyl ether.
Typically sprayed into from washing column overhead using demineralized water and be fully contacted with unstrpped gas in tower.According to operating pressure
Difference, water-washing process is possible to that a part of hydrocarbon component in unstripped gas can be absorbed, and therefore, it can using existing
There is known technology first to reclaim after wherein most methyl alcohol and DME, wherein hydrocarbon is reclaimed by methods such as strippings
Class material, returns compression unit.Wherein, washing process is the conventional technique in this area.
In the present invention, alkali cleaning be in order to remove unstripped gas in the sour gas such as carbon dioxide.It is general to adopt
Alkali lye is sprayed into from alkali cleaning column overhead and is fully contacted with unstrpped gas in tower.Caustic wash tower has neutralizing treatment section and washing
Section, caustic wash tower overhead gas 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,
Also need to carry out the operation such as alkali cleaning and washing, the rising and the drop of chilling temperature with pressure between compressor section
It is low to produce water phase lime set, or the three-phase effluent containing gas phase, water phase and oil phase.Wherein gas
Phase component is the hydrocarbons containing a small amount of saturation water, and water is mutually the water containing very small amount hydrocarbons, oil
It is mutually the hydrocarbons containing C2-C5 heavier components.Every section of compressor section produces water mutually can return one
Section compressor section entrance, and be ultimately delivered to stripper reclaim hydrocarbons avoid significant loss.It is compressed
Depropanizing tower, compressor outlet gas can be entered after the oil phase pressurization that the intersegmental gas of journey is produced after cooling
After cooling produced oil phase can enter domethanizing column.
It is described to be cooled to temperature for 15-20 according to method of the present invention, it is preferable that in step (2)
℃.Unstrpped gas after cooling is gas-liquid two-phase, it is not necessary to which drying can be sent directly into domethanizing column.Its
In, cold-producing medium used can be 5 DEG C or so of cold water, and cold water can be carried by lithium-bromide absorption-type refrigerating machine
For.And lithium bromide refrigerator uses absorption refrigeration technology, the waste hot steam with factory has as thermal source
Have the advantages that energy consumption is low.
According to method of the present invention, it is preferable that in step (3), absorbent is C4-C5 hydrocarbon,
It is highly preferred that the absorbent contains normal butane, iso-butane, 1- butylene, Trans-2-butene, cis- 2-
Butylene, pentane, isopentane, 1- amylenes；
It is highly preferred that on the basis of the gross weight of absorbent, the content of normal butane is 10-50 weight %,
The content of iso-butane is 5-15 weight %, Trans-2-butene for the content of 10-50 weight %, 1- butylene
Content be 5-35 weight %, the content of cis-2-butene be 5-35 weight %, pentane 5-35 weight %,
The content of isopentane for 5-35 weight %, 1- amylenes content be 5-35 weight %, each component content sum
Less than 100% such that it is able to improve the rate of recovery and reducing energy consumption of ethene and propylene.
The consumption of absorbent is not specially required in the present invention, for example：The consumption of absorbent and step (2)
The mol ratio of the gas-liquid two-phase obtained after cooling can be 1:5 to 3:1, preferably 1:4 to 2:1, it is more excellent
Elect 1 as:3 to 1.5:1.
According to method of the present invention, wherein, the absorption temperature more low absorption effect of absorbent is better,
I.e. demethanizer column overhead C2 and the loss of more heavy constituent are fewer, but energy consumption is higher, it is preferable that the suction
The temperature for receiving agent is 10-30 DEG C, most preferably 15-20 DEG C.
According to method of the present invention, wherein, domethanizing column can be divided into absorber portion and stripping section.Inhale
The effect for receiving section is to absorb the C2 and more heavy constituent in gas phase, in reducing the light components such as tower top methane
C2 constituent contents, it is preferable that domethanizing column absorber portion can increase intercooler to ensure to absorb effect
Really, it is highly preferred that the temperature of intercooler is 10-30 DEG C, most preferably 15-20 DEG C.Stripping section
Effect is to control the methane content in tower bottoms, and methane content is lower to advantageously ensure that final obtained ethene
The purity of product.But, increase as domethanizing column tower reactor methane content reduces bottom temperature, tower
C2 and more heavy constituent is consequently increased that top is lost, methane content control in preferred tower bottoms exists
1-10000ppm。
According to method of the present invention, in step (3), it is preferable that demethanation is processed into what is obtained
Overhead product carries out PSA hydrogen manufacturing, obtains hydrogen.Demethanation specifically can be processed the tower top for obtaining
Product is passed through in surge tank and prepares hydrogen and methane using PSA hydrogen producing technologies again.PSA hydrogen producing technologies are
Techniques well known, will not be described here.The purity of the isolated hydrogen of the present invention is
99-99.999%.
According to method of the present invention, in step (4), the condition of depropanization process can be ability
The conventional depropanization condition in domain, it is preferable that the condition that the depropanization is processed includes：Depropanizing tower is theoretical
Plate number is 15-50 blocks, and operating pressure is 1.5-3.5MPa, and tower top temperature is 10-50 DEG C, bottom temperature
For 100-160 DEG C such that it is able to further improve the rate of recovery for being finally recovered the ethene and propylene for obtaining.
According to method of the present invention, in step (4), depropanizing tower tower top is C2 and C3 components,
Tower reactor is mainly C4 and more heavy constituent simultaneously containing a small amount of C3 components, depropanizing tower top gaseous phase by
In being entrained with a certain amount of C4 and more heavy constituent, so need cooling to make it flow back, tower top temperature can be with
Control in the range of 10-50 DEG C, preferably in the range of 15-35 DEG C.Wherein, depropanizing tower tower reactor is mainly controlled
The content of C3 components processed, the content of C3 components is lower in tower reactor, C2 the and C3 components of system return
Yield is higher, while bottom temperature is higher；Bottom temperature is higher, and tower top C4 entrainment is higher, required
Energy consumption is higher.Therefore, the molar content of tower reactor C3 component is controlled in the range of 1-25%, preferably in 5-20%
In the range of.
According to method of the present invention, in step (4), it is preferable that depropanization process is obtained into tower reactor
Liquid is recycled as the absorbent that demethanation is processed, due to depropanizing tower kettle liquid and domethanizing column and de- second
There is certain temperature difference in alkane tower, it is highly preferred that circulating as absorbent depropanization process is obtained into tower bottoms
Using front, the thermal source that its elder generation is processed as demethanation process and deethanization, most after Jing recirculated waters and freezing
Water is cooled to step by step 10-30 DEG C, is preferably cooled to 15-20 DEG C such that it is able to reducing energy consumption, cost-effective.
In addition, wherein have small part absorbent to discharge with demethanizer column overhead gas phase, therefore, the present invention's
In method, preferably depropanization process is obtained being passed through after tower bottoms mixes with a part of fresh absorbent de-
In methane tower, with absorptive tower absorbent flow in guarantee system, wherein, take off to being recycled as absorbent
There is no particular limitation for the ratio of the propane tower bottoms that obtains of process and fresh absorbent, for example both
Weight ratio can be 1：0-0.1.
According to method of the present invention, in step (5), the drying is the conventional back tender in this area
Skill, it is intended to remove the saturation water in depropanizing tower tower overhead gas.It can be dried using molecular sieve drying system
Method, concrete grammar can include：Drier needs one to open one for alternate run, previous during alternate run
One of operation needs to carry out regenerative operation.During regenerative operation, need nitrogen through high pressure steam heating
It is used for afterwards regenerating drier.Dry run gas pressure only produces a small amount of pressure drop, is usually no more than
200kPa。
According to method of the present invention, it is preferable that in step (5), the tower top of depropanization process is produced
Thing is cooled to -10 DEG C～30 DEG C and carries out deethanization process again after being dried.The cooling can be returned by ethylene distillation
The cold produced during receipts is carried out, in order to further reducing energy consumption.
According to method of the present invention, it is preferable that the condition of deethanization process can be this area routine
The condition that processes of deethanization, it is preferable that the condition that the deethanization is processed includes：Dethanizer is theoretical
Plate number is 25-120 blocks, and operating pressure is 1.0-3.0MPa, and tower top temperature is -30～-10 DEG C, tower reactor temperature
Spend for 50-80 DEG C such that it is able to further improve the rate of recovery for being finally recovered the ethene and propylene for obtaining.
According to method of the present invention, dethanizer can clearly separate C2 and C3 components, pass through
The condition of control dethanizer can cause propylene in deethanizer overhead in above-mentioned preferred scope
Molar content be not higher than 0.5%, preferably no greater than 0.1%.
According to method of the present invention, it is preferable that by step (5) deethanization process overhead product according to
It is secondary to be hydrogenated with and ethylene distillation, according to process requirements select by conventional method or middle extraction method from
Ethylene rectifying column obtains ethene, and ethylene distillation tower reactor product is ethane, and ethylene distillation tower top product is returned
The close compressor section of back pressure.Wherein, hydrogenation is that, in order to acetylene is converted into ethene, the technology can be with
There is provided by known technology.It is a certain amount of due to being likely present in the material of dethanizer feeding ethylene rectifying column
Methane, the method that can select middle extraction obtains polymer grade ethylene product in ethylene rectifying column, one
As produce position can select to count the 2nd piece to 8 blocks column plates from top to bottom.
According to method of the present invention, it is preferable that by the overhead product of step (5) deethanization process
- 35 DEG C～-10 DEG C are cooled to after hydrogenation being passed through ethylene rectifying column again carries out ethylene distillation.Wherein, the cooling
Can be carried out by the cold produced in ethylene distillation removal process, in order to further reducing energy consumption.
According to method of the present invention, the condition of ethylene distillation can be the conventional ethylene distillation in this area
Condition, for example can include：The number of theoretical plate of ethylene rectifying column is 100-150 blocks, and operating pressure is
0.8-2.6MPa, tower top temperature is -39 DEG C～-15 DEG C, and bottom temperature is -20 DEG C～0 DEG C.
According to method of the present invention, it is preferable that by the tower kettle product of step (5) deethanization process
Propylene rectifying is carried out, propylene, propylene rectification tower kettle product are obtained from propylene rectification tower by middle extraction method
For propane.Can be with the middle extraction method for obtaining ethene in the concrete grammar of this middle extraction method for being adopted
It is identical, except that extraction position selects to count from top to bottom between 2-15 block column plates.
According to method of the present invention, the condition of propylene rectifying can be the conventional propylene rectifying in this area
Condition, for example can include：The number of theoretical plate of propylene rectification tower is 110-400 blocks, and operating pressure is
0.8-2.6MPa, tower top temperature is 10 DEG C -55 DEG C, and bottom temperature is 35 DEG C -60 DEG C.
The isolated Recovery rate of ethylene of the method for the present invention be more than 95%, propylene recovery rate be 95% with
On.
Embodiment
Methanol to olefins reaction gas is by ethene, propylene, methane, hydrogen and other component (nitrogen, nitrogen oxygen
Compound, carbon monoxide, carbon dioxide, dimethyl ether, water, methyl alcohol, ethane, acetylene, propane, third
Diene, normal butane, iso-butane, 1- butylene, 2- butylene, 1,3- butadiene, cis-2-butene, trans- 2- fourths
Alkene, pentane, isopentane, 1- amylenes, n-hexane, isohexane, hexene, benzene, toluene, to diformazan
Benzene, meta-xylene, ortho-xylene and 1,3,5- trimethylbenzenes) composition, wherein, the content of methane is 4.1
Mole %, the content of hydrogen are 1.8 moles of %, and the content of ethene is 40.7 moles of %, the content of propylene
For 37.5 moles of %, water is 5.7 moles of %, and other components are 10.2 moles of %.
Embodiment 1
The present embodiment is used for the separation method of the methanol to olefins reaction gas for illustrating the present invention.
(1) process is compressed as shown in figure 1, methanol to olefins reaction gas is passed through in compression unit,
The compression unit is made up of 3 sections of compressor sections, and every section of outlet temperature of compressor section is less than 140 DEG C,
Every section of inlet temperature is 40 DEG C, and using 30 DEG C of circulating waters, methanol to olefins reaction gas is through described
Pressure rises to step by step 3.8MPa after compression unit compression is processed, wherein, in the 1st section of compressor section outlet
(pressure is 0.55MPa) is disposed with caustic wash tower and water scrubber and carries out alkali cleaning process and water after drain tank
Process is washed, alkali lye is sprayed into from alkali cleaning column overhead and is fully contacted with unstrpped gas in tower in alkali cleaning processing procedure,
Sprayed into from washing column overhead using demineralized water during washing process and be fully contacted with unstrpped gas in tower, pressed
In contracting processing procedure, gas phase, water phase and oil-phase product can be produced, every section of compressor section be produced into water and is mutually returned
The entrance of the preceding paragraph compressor section is returned, and is ultimately delivered to stripper recovery hydrocarbons and avoid significant loss,
The oil phase that 3rd section of compressor outlet gas is produced after cooling enters domethanizing column, does not produce between compressor section
Oil generation phase；
(2) compression is processed the gas phase for obtaining to be carried out being cooled to 15 DEG C, and the unstrpped gas after cooling is gas
Liquid two-phase, it is not necessary to which drying can be sent directly into domethanizing column, cold-producing medium used is 5 DEG C or so of cold water,
Cold water can be provided by lithium-bromide absorption-type refrigerating machine；
(3) as shown in Fig. 2 (content of normal butane is 35 weight %, and iso-butane contains by absorbent
Measure the content for 15 weight %, 1- butylene be 6 weight %, the content of Trans-2-butene be 14 weight %,
The content of cis-2-butene is 10 weight %, and the content of pentane is that 5 weight %, the content of isopentane are
The content of 5 weight %, 1- amylenes is 10 weight %) 15 DEG C, in then passing to domethanizing column are cooled to,
The gas-liquid two-phase logistics obtained after above-mentioned cooling is passed through in domethanizing column carries out demethanation process, absorbent
Consumption and compressor outlet gas be after cooling 1 into the mol ratio of the logistics of domethanizing column:1.5, take off
Methane tower absorber portion is provided with intercooler, and the temperature of intercooler is 15 DEG C, by controlling piptonychia
The number of theoretical plate of alkane tower is 50 pieces, and operating pressure is 3.6MPa, and tower top temperature is 25 DEG C, by control
Bottom temperature is 70.5 DEG C so that methane content is controlled to 30ppm in tower bottoms；In addition, by demethanation
The overhead product that process is obtained is passed through in surge tank and prepares hydrogen and methane using PSA hydrogen producing technologies again,
The purity of obtained hydrogen is 99.99%；
(4) tower bottoms that demethanation process is obtained is passed through in depropanizing tower carries out depropanization process；It is de-
The number of theoretical plate of propane tower is 40 pieces, and operating pressure is 2.6MPa, and tower top temperature is 31.7 DEG C, tower reactor
Temperature is 128.2 DEG C, wherein, the molar content of C3 components is 7.6% in tower bottoms；
(5) depropanization process is obtained the thermal source that tower bottoms is processed as demethanation process and deethanization,
Jing recirculated waters and cold water are cooled to step by step 15 DEG C after most, first a portion are sent into battery limit (BL) and are sent to debutanization
Tower, then remaining circulating solvent is mixed and is passed through in domethanizing column (circulation with a part of fresh absorbent
The ratio of solvent and fresh absorbent is 1:0.03), it is ensured that the consumption of absorbent and compressor outlet gas
After cooling the mol ratio into the logistics of domethanizing column is 1:1.5.The overhead product of depropanization process is adopted
Carry out being cooled to 6.9 DEG C after being dried with molecular sieve drying system, the cooling passes through ethylene distillation removal process
The cold of middle generation is carried out, and the concrete operation method of molecular sieve drying system is：Drier needs one to open one
Standby alternate run, previously of operation needs to carry out regenerative operation during alternate run.During regenerative operation,
Need nitrogen after high pressure steam heating for regenerating to drier.By the depropanization after cooling
The overhead product of process is passed through in dethanizer carries out deethanization process, and the number of theoretical plate of dethanizer is 80
Block, operating pressure is 2.3MPa, and tower top temperature is -22.3 DEG C, and bottom temperature is 55.1 DEG C so that de-
The molar content of propylene is 0.005% in ethane tower overhead；
(6) it is cooled to -22.7 DEG C after the overhead product of step (5) deethanization process is hydrogenated with to be passed through
Ethylene rectifying column carries out ethylene distillation, and the cooling can be cold by what is produced in ethylene distillation removal process
Amount is carried out, and the number of theoretical plate of ethylene rectifying column is 100 pieces, and operating pressure is 1.9MPa, tower top temperature
For -30.7 DEG C, bottom temperature is -9.2 DEG C, and ethylene distillation tower reactor product is ethane, and tower overhead gas product is second
Alkene；
(7) tower kettle product of step (5) deethanization process is carried out into propylene rectifying, using middle extraction
Method obtains propylene from propylene rectification tower, and propylene rectification tower kettle product is propane, and propylene rectification tower tower top is produced
The close compressor section of thing returning pressure, propylene extraction position selects to count the 15th piece of 2- from top to bottom
Between column plate, the number of theoretical plate of propylene rectification tower is 170 pieces, and operating pressure is 1.95MPa, tower top temperature
For 18.9 DEG C, bottom temperature is 53.7 DEG C.
Embodiment 2
The present embodiment is used for the separation method of the methanol to olefins reaction gas for illustrating the present invention.
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed process, the compression is single
Unit is made up of 3 sections of compressor sections, and every section of outlet temperature of compressor section is less than 140 DEG C, every section of entrance temperature
Spend for 40 DEG C, using 30 DEG C of circulating waters, methanol to olefins reaction gas is through the compression unit pressure
Pressure rises to step by step 3.8MPa after contracting is processed, wherein, (the pressure after the 2nd compressor section outlet drain tank
Power is 1.8MPa) it is disposed with caustic wash tower and water scrubber and carries out alkali cleaning process and washing process, alkali cleaning
Alkali lye is sprayed into from alkali cleaning column overhead and is fully contacted with unstrpped gas in tower in processing procedure, washing process process
Middle employing demineralized water is sprayed into from washing column overhead and is fully contacted with unstrpped gas in tower, compression process
In, gas phase, water phase and oil-phase product can be produced, every section of compressor section is produced into water and mutually returns the preceding paragraph pressure
The entrance of contracting machine section, and be ultimately delivered to stripper and reclaim hydrocarbons to avoid significant loss, the 3rd section of compression
The oil phase that machine exit gas is produced after cooling enters domethanizing column, and oil phase is not produced between compressor section；
(2) compression is processed the gas phase for obtaining to be carried out being cooled to 15 DEG C, and the unstrpped gas after cooling is gas
Liquid two-phase, it is not necessary to which drying can be sent directly into domethanizing column, cold-producing medium used is 5 DEG C or so of cold water,
Cold water can be provided by lithium-bromide absorption-type refrigerating machine；
(3) as shown in Fig. 2 (content of normal butane is 10 weight %, and iso-butane contains by absorbent
Measure the content for 25 weight %, 1- butylene be 15 weight %, the content of Trans-2-butene be 24 weight %,
The content of cis-2-butene is 6 weight %, and it is 5 that the content of pentane is 5 weight %, the content of isopentane
The content of weight %, 1- amylene is 10 weight %) 15 DEG C, in then passing to domethanizing column are cooled to, will
The gas-liquid two-phase logistics obtained after above-mentioned cooling is passed through in domethanizing column carries out demethanation process, absorbent
Consumption is after cooling 1.5 into the mol ratio of the logistics of domethanizing column with compressor outlet gas:1, piptonychia
Alkane tower absorber portion is provided with intercooler, and the temperature of intercooler is 15 DEG C, by controlling demethanation
The number of theoretical plate of tower is 35 pieces, and operating pressure is 3.6MPa, and tower top temperature is 28.3 DEG C, bottom temperature
For 69.5 DEG C so that methane content is controlled to 30ppm in tower bottoms；In addition, demethanation is processed obtaining
Overhead product be passed through in surge tank and again hydrogen and methane, obtained hydrogen prepared using PSA hydrogen producing technologies
The purity of gas is 99.9%；
(4) tower bottoms that demethanation process is obtained is passed through in depropanizing tower carries out depropanization process；It is de-
The number of theoretical plate of propane tower is 35 pieces, and operating pressure is 2.4MPa, and tower top temperature is 28.4 DEG C, tower reactor
Temperature is 117 DEG C, wherein, the molar content of C3 components is 15.3% in tower bottoms；
(5) depropanization process is obtained the thermal source that tower bottoms is processed as demethanation process and deethanization,
Jing recirculated waters and cold water are cooled to step by step 15 DEG C after most, first a portion are sent into battery limit (BL) and are sent to debutanization
Tower, then remaining circulating solvent is mixed and is passed through in domethanizing column (circulation with a part of fresh absorbent
The ratio of solvent and fresh absorbent is 1:0.02), it is ensured that the consumption of absorbent and compressor outlet gas
After cooling the mol ratio into the logistics of domethanizing column is 1.5:1, the overhead product of depropanization process is adopted
Carry out being cooled to 6.7 DEG C after being dried with molecular sieve drying system, the cooling passes through ethylene distillation removal process
The cold of middle generation is carried out, and the concrete operation method of molecular sieve drying system is：Drier needs one to open one
Standby alternate run, previously of operation needs to carry out regenerative operation during alternate run.During regenerative operation,
Need nitrogen after high pressure steam heating for regenerating to drier.By the depropanization after cooling
The overhead product of process is passed through in dethanizer carries out deethanization process, and the number of theoretical plate of dethanizer is 70
Block, operating pressure is 2.3MPa, and tower top temperature is -22.3 DEG C, and bottom temperature is 55.1 DEG C so that de-
The molar content of propylene is 0.005% in ethane tower overhead；
(6) it is cooled to -22.7 DEG C after the overhead product of step (5) deethanization process is hydrogenated with to be passed through
Ethylene rectifying column carries out ethylene distillation, and the cooling can be cold by what is produced in ethylene distillation removal process
Amount is carried out, and the number of theoretical plate of ethylene rectifying column is 110 pieces, and operating pressure is 1.9MPa, tower top temperature
For -30.7 DEG C, bottom temperature is -9.2 DEG C, and ethylene distillation tower reactor product is ethane, and tower overhead gas product is second
Alkene；
(7) tower kettle product of step (5) deethanization process is carried out into propylene rectifying, using middle extraction
Method obtains propylene from propylene rectification tower, and propylene rectification tower kettle product is propane, and propylene rectification tower tower top is produced
The close compressor section of thing returning pressure, propylene extraction position selects to count the 15th piece of 2- from top to bottom
Between column plate, the number of theoretical plate of propylene rectification tower is 180 pieces, and operating pressure is 1.85MPa, tower top temperature
For 19.2 DEG C, bottom temperature is 51.2 DEG C.
Embodiment 3
The present embodiment is used for the separation method of the methanol to olefins reaction gas for illustrating the present invention.
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed process, the compression is single
Unit is made up of 3 sections of compressor sections, and every section of outlet temperature of compressor section is less than 140 DEG C, every section of entrance temperature
Spend for 40 DEG C, using 30 DEG C of circulating waters, methanol to olefins reaction gas is through the compression unit pressure
Pressure rises to step by step 3.8MPa after contracting is processed, wherein, (the pressure after the 2nd compressor section outlet drain tank
Power is 1.8MPa) it is disposed with caustic wash tower and water scrubber and carries out alkali cleaning process and washing process, alkali cleaning
Alkali lye is sprayed into from alkali cleaning column overhead and is fully contacted with unstrpped gas in tower in processing procedure, washing process process
Middle employing demineralized water is sprayed into from washing column overhead and is fully contacted with unstrpped gas in tower, compression process
In, gas phase, water phase and oil-phase product can be produced, every section of compressor section is produced into water and mutually returns the preceding paragraph pressure
The entrance of contracting machine section, and be ultimately delivered to stripper and reclaim hydrocarbons to avoid significant loss, the 3rd section of compression
The oil phase that machine exit gas is produced after cooling enters domethanizing column, and oil phase is not produced between compressor section；
(2) compression is processed the gas phase for obtaining to be carried out being cooled to 15 DEG C, and the unstrpped gas after cooling is gas
Liquid two-phase, it is not necessary to which drying can be sent directly into domethanizing column, cold-producing medium used is 5 DEG C or so of cold water,
Cold water can be provided by lithium-bromide absorption-type refrigerating machine；
(3) as shown in Fig. 2 (content of normal butane is 35 weight %, and iso-butane contains by absorbent
Measure the content for 15 weight %, 1- butylene be 14 weight %, the content of Trans-2-butene be 6 weight %,
The content of cis-2-butene is 10 weight %, and the content of pentane is that 5 weight %, the content of isopentane are
The content of 10 weight %, 1- amylenes is 5 weight %) 15 DEG C, in then passing to domethanizing column are cooled to,
The gas-liquid two-phase logistics obtained after above-mentioned cooling is passed through in domethanizing column carries out demethanation process, absorbent
Consumption and compressor outlet gas be after cooling 1 into the mol ratio of the logistics of domethanizing column:1, take off
Methane tower absorber portion is provided with intercooler, and the temperature of intercooler is 15 DEG C, by controlling piptonychia
The number of theoretical plate of alkane tower is 30 pieces, and operating pressure is 3.6MPa, and tower top temperature is 24.4 DEG C, tower reactor temperature
Spend for 68.9 DEG C so that methane content is controlled to 300ppm in tower bottoms；In addition, demethanation is processed
The overhead product for obtaining is passed through in surge tank and prepares hydrogen and methane using PSA hydrogen producing technologies again, is obtained
Hydrogen purity be 99.9%；
(4) tower bottoms that demethanation process is obtained is passed through in depropanizing tower carries out depropanization process；It is de-
The number of theoretical plate of propane tower is 35 pieces, and operating pressure is 2.6MPa, and tower top temperature is 30.8 DEG C, tower reactor
Temperature is 128.1 DEG C, wherein, the molar content of C3 components is 7.6% in tower bottoms；
(5) depropanization process is obtained the thermal source that tower bottoms is processed as demethanation process and deethanization,
Jing recirculated waters and cold water are cooled to step by step 15 DEG C after most, first a portion are sent into battery limit (BL) and are sent to debutanization
Tower, then remaining circulating solvent is mixed and is passed through in domethanizing column (circulation with a part of fresh absorbent
The ratio of solvent and fresh absorbent is 1:0.02), it is ensured that the consumption of absorbent and compressor outlet gas
After cooling the mol ratio into the logistics of domethanizing column is 1:1.The overhead product of depropanization process is adopted
Carry out being cooled to 5.8 DEG C after being dried with molecular sieve drying system, the cooling passes through ethylene distillation removal process
The cold of middle generation is carried out, and the concrete operation method of molecular sieve drying system is：Drier needs one to open one
Standby alternate run, previously of operation needs to carry out regenerative operation during alternate run.During regenerative operation,
Need nitrogen after high pressure steam heating for regenerating to drier.By the depropanization after cooling
The overhead product of process is passed through in dethanizer carries out deethanization process, and the number of theoretical plate of dethanizer is 60
Block, operating pressure is 2.3MPa, and tower top temperature is -22.4 DEG C, and bottom temperature is 55.1 DEG C so that de-
The molar content of propylene is 0.003% in ethane tower overhead；
(6) it is cooled to -22.9 DEG C after the overhead product of step (5) deethanization process is hydrogenated with to be passed through
Ethylene rectifying column carries out ethylene distillation, and the cooling can be cold by what is produced in ethylene distillation removal process
Amount is carried out, and the number of theoretical plate of ethylene rectifying column is 110 pieces, and operating pressure is 1.9MPa, tower top temperature
For -31.3 DEG C, bottom temperature is -9.2 DEG C, and ethylene distillation tower reactor product is ethane, using middle extraction method
Ethene is obtained from ethylene rectifying column, by the close compressor section of ethylene distillation tower top product returning pressure, second
Alkene extraction position selects to count from top to bottom between 2-8 block column plates；
(7) tower kettle product of step (5) deethanization process is carried out into propylene rectifying, using middle extraction
Method obtains propylene from propylene rectification tower, and propylene rectification tower kettle product is propane, and propylene rectification tower tower top is produced
The close compressor section of thing returning pressure, propylene extraction position selects to count the 15th piece of 2- from top to bottom
Between column plate, the number of theoretical plate of propylene rectification tower is 260 pieces, and operating pressure is 1.95MPa, tower top temperature
For 18.9 DEG C, bottom temperature is 53.7 DEG C.
Embodiment 4
The present embodiment is used for the separation method of the methanol to olefins reaction gas for illustrating the present invention.
Method according to embodiment 1 separates methanol to olefins reaction gas, and except for the difference that, the compression is processed
The chilling temperature of the gas phase, absorbent and domethanizing column intercooler that obtain is 25 DEG C.
Embodiment 5
The present embodiment is used for the separation method of the methanol to olefins reaction gas for illustrating the present invention.
Method according to embodiment 3 separates methanol to olefins reaction gas, except for the difference that, by controlling piptonychia
The number of theoretical plate of alkane tower is 20 pieces, and operating pressure is 5.0MPa, and tower top temperature is 33.7 DEG C, tower reactor temperature
Spend for 93.7 DEG C so that methane content is controlled to 608ppm in tower bottoms.
Comparative example 1
Method according to embodiment 1 separates methanol to olefins reaction gas, except for the difference that, by controlling piptonychia
The number of theoretical plate of alkane tower is 35 pieces, and operating pressure is 2.9MPa, and tower top temperature is 41 DEG C, bottom temperature
For 60.6 DEG C so that methane content is controlled to 30ppm in tower bottoms.
Table 1
Note：Steam is the saturated vapor of 0.4MPa.
By the data of table 1 can be seen that the isolated Recovery rate of ethylene of the method for the present invention for 95% with
On, purity is more than 99.95%, and propylene recovery rate is more than 95%, and purity is more than 99.5%, and should
Method energy consumption is low, operating flexibility big, can be according to product adjustment of yield energy consumption technological parameter.
This method is by the use of the component containing C4-C5 hydrocarbon as absorbent methanol removal alkene
(MTO/DMTO) light components such as methane in reaction gas, and the operation temperature more than 10 DEG C
Methane and light ends in interval methanol removal alkene (MTO/DMTO) product gas, effectively
Water and hydro carbons is inhibited to form hydrate.In addition, the dry run of the present invention need not be placed on compression list
Unit's outlet, it is only necessary to process is dried to deethanizer overhead gas, it is to avoid oral fluid is gone out to compression unit
Phase lime set is dried, and significantly reduces dry run treating capacity, and public work is considerably reduced therewith
The consumption and energy consumption of journey nitrogen.Demethanation process is switched to thermal release process and is conducive to the net that exchanges heat by this method
Network optimizes, it is not necessary to put into less than -40 DEG C of cryogen.With small investment, the features such as material recovery rate is high.
The preferred embodiment of the present invention described in detail above, but, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, can be to the technical side of the present invention
Case carries out various simple variants, and these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique described in above-mentioned specific embodiment is special
Levy, in the case of reconcilable, can be combined by any suitable means, in order to avoid need not
The repetition wanted, the present invention is no longer separately illustrated to various possible combinations.
Additionally, can also be combined between a variety of embodiments of the present invention, as long as its
Without prejudice to the thought of the present 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 the method includes：
(1) methanol to olefins reaction gas is passed through in compression unit and is compressed process；
(2) compression is processed the gas phase for obtaining to be cooled down；
(3) in the presence of absorbent, the gas-liquid two-phase obtained after cooling is taken off in domethanizing column
Methane process；
(4) demethanation is processed the tower kettle product for obtaining carries out depropanization process in depropanizing tower；
(5) deethanization process is carried out in dethanizer after the overhead product of depropanization process is dried；
Wherein, it is 3.2-6.0MPa that the compression processes the gaseous pressure for obtaining, in step (2),
Described to be cooled to temperature 10-30 DEG C, the absorbent contains C4-C5 hydrocarbon, the bar that the demethanation is processed
Part includes：Domethanizing column number of theoretical plate is 20-60 blocks, and operating pressure is 3.0-5.8MPa, tower top temperature
For 10-40 DEG C, bottom temperature is 60-120 DEG C.
2. method according to claim 1, wherein, the absorbent is C4-C5 hydrocarbon, preferably
Ground, the absorbent contain normal butane, iso-butane, 1- butylene, Trans-2-butene, cis-2-butene,
Pentane, isopentane, 1- amylenes；
It is highly preferred that on the basis of the gross weight of absorbent, the content of normal butane is 10-50 weight %,
The content of iso-butane is 5-15 weight %, Trans-2-butene for the content of 10-50 weight %, 1- butylene
Content be 5-35 weight %, the content of cis-2-butene be 5-35 weight %, pentane 5-35 weight %,
The content of isopentane for 5-35 weight %, 1- amylenes content be 5-35 weight %, each component content sum
Less than 100%.
3. method according to claim 1, wherein, the temperature of the absorbent is 10-30 DEG C,
Preferably 15-20 DEG C.
4. method according to claim 1, wherein, it is described to be cooled to temperature in step (2)
For 15-20 DEG C.
5. method according to claim 1, wherein, the compression unit includes the compression of 3-5 sections
Machine section, methanol to olefins reaction gas pressure after compression unit compression process rises to step by step
3.2-6.0MPa。
6. method according to claim 5, wherein, carry out during the compression is processed
Alkali cleaning and washing；
Preferably, the alkali cleaning and washing is carried out under 0.3-3.0MPa operating pressures.
7. method according to claim 1, wherein, the method also includes：Demethanation is processed
The overhead product for obtaining carries out PSA hydrogen manufacturing, obtains hydrogen.
8. method according to claim 1, wherein, the condition that the depropanization is processed includes：
Depropanizing tower number of theoretical plate is 15-50 blocks, and operating pressure is 1.5-3.5MPa, and tower top temperature is 10-50 DEG C,
Bottom temperature is 100-160 DEG C.
9. method according to claim 1, wherein, the condition that the deethanization is processed includes：
Dethanizer number of theoretical plate is 25-120 blocks, and operating pressure is 1.0-3.0MPa, and tower top temperature is
- 30～-10 DEG C, bottom temperature is 50-80 DEG C.
10. method according to claim 1, wherein, the method also includes：In step (5),
Being cooled to -10 DEG C～30 DEG C after the overhead product of depropanization process is dried carries out again deethanization process.
11. methods according to claim 1, wherein, the method also includes：By step (5)
The overhead product of deethanization process is hydrogenated with successively and ethylene distillation, is adopted by conventional method or centre
Go out method and obtain ethene from ethylene rectifying column, and ethylene distillation tower reactor product is ethane, by ethylene distillation tower top
The close compressor section of product returning pressure.
12. methods according to claim 11, wherein, the condition of the ethylene distillation includes：
The number of theoretical plate of ethylene rectifying column is 100-150 blocks, and operating pressure is 0.8-2.6MPa, and tower top temperature is
- 39 DEG C～-15 DEG C, bottom temperature is -20 DEG C～0 DEG C.
13. methods according to claim 1, wherein, the method also includes：By step (5)
The tower kettle product of deethanization process carries out propylene rectifying, and third is obtained from propylene rectification tower by middle extraction method
Alkene, propylene rectification tower kettle product is propane.
14. methods according to claim 13, wherein, the condition of the propylene rectifying includes：
The number of theoretical plate of propylene rectification tower is 110-400 blocks, and operating pressure is 0.8-2.6MPa, and tower top temperature is
10 DEG C -55 DEG C, bottom temperature is 35 DEG C -60 DEG C.
15. methods according to claim 1, wherein, the method also includes：Compression process is intersegmental
Depropanizing tower is entered after gas oil phase pressurization produced after cooling, compressor outlet gas is after cooling
Produced oil phase enters domethanizing column.
16. methods according to claim 1, wherein, the method also includes：Depropanization is processed
Obtain tower bottoms to recycle as the absorbent that demethanation is processed.
17. methods according to claim 16, wherein, before recycling as absorbent,
Depropanization process is obtained the thermal source that tower bottoms is first processed as demethanation process and deethanization.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510711458.2A CN106631664B (en) | 2015-10-28 | 2015-10-28 | A kind of separation method of methanol to olefins reaction gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510711458.2A CN106631664B (en) | 2015-10-28 | 2015-10-28 | A kind of separation method of methanol to olefins reaction gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106631664A true CN106631664A (en) | 2017-05-10 |
| CN106631664B CN106631664B (en) | 2019-06-28 |
Family
ID=58815919
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510711458.2A Active CN106631664B (en) | 2015-10-28 | 2015-10-28 | A kind of separation method of methanol to olefins reaction gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106631664B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN115210207A (en) * | 2020-02-28 | 2022-10-18 | 环球油品有限责任公司 | Method and apparatus for separating methanol from other oxygenates |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2015
- 2015-10-28 CN CN201510711458.2A patent/CN106631664B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115210207A (en) * | 2020-02-28 | 2022-10-18 | 环球油品有限责任公司 | Method and apparatus for separating methanol from other oxygenates |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106631664B (en) | 2019-06-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109912380B (en) | Pyrolysis gas separation method and device | |
| CN109912379B (en) | Refinery dry gas separation method and device | |
| CN109678635B (en) | Saturated hydrocarbon cracking gas separation system and utilization method of ethane/propane-rich saturated hydrocarbon | |
| CN104557387B (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN103304358B (en) | Low-carbon olefin separation method and equipment beneficial to product recovery | |
| CN103333039B (en) | Light olefin separation method and device for reducing dosage of absorbent | |
| CN101759518B (en) | Method for absorbing and separating refinery catalytic dry gas by adopting oil | |
| CN104557384B (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN108017499B (en) | Comprehensive utilization system and comprehensive utilization method for methanol-to-olefin reaction product | |
| CN103087772A (en) | Device and method for separating refinery dry gas through oil absorption | |
| CN110092701B (en) | Light hydrocarbon separation method for MTO product mixed gas | |
| US20210348071A1 (en) | Method and system for separating light hydrocarbons | |
| CN101759516A (en) | Method for refining catalysis drying gas by using oil absorption extraction | |
| CN105441130B (en) | One kind reclaims hydro carbons tail gas method | |
| CN104557386A (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN109678641A (en) | A kind of separation method and device of Catalyst for Oxidative Coupling of Methane reaction gas | |
| CN110950733B (en) | Separation device and method for preparing olefin gas from methanol | |
| CN107602325B (en) | Separation method of methanol-to-olefin reaction gas | |
| CN104560194B (en) | Refinery saturated dry gas recovery system and recovery method | |
| CN106631664A (en) | Separation method for methanol-to-olefin reaction gas | |
| CN107602333B (en) | Separation method of methanol-to-olefin reaction gas | |
| CN107602331B (en) | Separation method of methanol-to-olefin reaction gas | |
| CN111004079A (en) | Separation method and device for preparing ethylene reaction gas through oxidative coupling of methane | |
| CN106631672B (en) | A kind of separation method of methanol to olefins reaction gas | |
| CN107602326B (en) | Separation method of methanol-to-olefin reaction gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |