CN209193845U - The separator of methanol-to-olefins gas - Google Patents
The separator of methanol-to-olefins gas Download PDFInfo
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- CN209193845U CN209193845U CN201821585168.3U CN201821585168U CN209193845U CN 209193845 U CN209193845 U CN 209193845U CN 201821585168 U CN201821585168 U CN 201821585168U CN 209193845 U CN209193845 U CN 209193845U
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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
- Y02P30/20—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
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Abstract
The utility model discloses a kind of separators of methanol-to-olefins gas, after being pre-processed by pre-processing assembly (1) to methanol-to-olefins gas, phase separation is carried out in separator (2), lime set is sent to lime set drier (3), gas phase is sent to the first gas phase drier (4), all it is sent into dethanizer (5) after drying, dethanizer (5) top gaseous phase passes through domethanizing column (6), solvent recovery tower (7), acetylene converter (8), ethylene rectifying column (9) isolated ethylene, the tower bottom of dethanizer (5) passes through depropanizing tower (10), propylene rectification tower (11) isolated propylene.The circulation loop of the device absorbent is domethanizing column (6)-solvent recovery tower (7)-domethanizing column (6), it is recycled back to short out, and it is not related to dethanizer (5) and propylene rectification tower (11), effectively reduce load, energy consumption and the equipment investment of dethanizer (5) and propylene rectification tower (11).
Description
Technical field
The utility model relates to technical field of petrochemical industry, in particular to a kind of separator of methanol-to-olefins gas.
Background technique
In recent years, although alkene production both at home and abroad shows the trend of development in pluralism, with methanol-to-olefins (MTO)
Non-steam cracking hydrocarbon mode for representative is still the important way for producing alkene.And methanol-to-olefins refer to coal base or natural
The methanol of gas base synthesis is raw material, by the fluidized-bed reaction form of similar catalytic cracking unit, produces the chemical industry of low-carbon alkene
Technology, major product are ethylene, propylene etc..
The separation process of current the most widely used MTO gas is the process flow of Lu Musi predepropanization.In the technique
Reaction gas enters depropanizing tower from MTO reactor, and depropanizing tower substrate streams to debutanizing tower and isolates mixing C4Component takes off
Propane overhead stream removes H component, C through domethanizing column1It is sent after component to dethanizer, the overhead materials of dethanizer are streamed to second
Alkene rectifying column isolates ethylene, and deethanizer bottoms send to propylene rectification tower and isolate propylene.The process characteristic is: using third
Alkene is cryogen, cold oil absorption process in the utilization of demethanation tower top, using the tower bottom C of part dethanizer3Fraction and propylene rectifying
The tower bottom propane of tower runs damage as absorbent, to reduce ethylene.
In the process of implementing the utility model, inventor discovery in the prior art the prior art has at least the following problems:
Due in the gas separation process of the prior art demethanation tower top utilize in cold oil absorption process, using part take off second
The tower bottom C of alkane tower3The tower bottom propane of fraction and propylene rectification tower recycles ethylene as absorbent, and the absorbent is from domethanizing column
Tower bottom separate after send to dethanizer, separate and sent to propylene rectification tower, finally from third from the tower bottom of dethanizer
The tower bottom of alkene rectifying column separates the tower top returned again to domethanizing column, that is to say, that the circulation loop of the absorbent is de-
Methane tower-dethanizer-propylene rectification tower-domethanizing column, this circulation loop is long, increase domethanizing column, dethanizer and
The load and energy consumption of propylene rectification tower easily lead to the separative unit fluctuation of service in circulation.
Utility model content
In consideration of it, the utility model provides a kind of separator of methanol-to-olefins gas, to solve to deposit in the prior art
The long problem of circulation loop of absorbent, reduce load, energy consumption and the equipment investment of dethanizer and propylene rectification tower.
Specifically, including technical solution below:
On the one hand, the utility model embodiment provides a kind of separator of methanol-to-olefins gas, described device packet
Include: pre-processing assembly, separator, lime set drier, the first gas phase drier, dethanizer, domethanizing column, solvent recovery tower,
Acetylene converter, ethylene rectifying column, depropanizing tower, propylene rectification tower and debutanizing tower, wherein
The inlet communication of the pre-processing assembly and the separator, the gaseous phase outlet of the separator and first gas
The inlet communication of phase drier, the inlet communication of the condensate outlet of the separator and the lime set drier, the lime set are dry
Dry device is connected to the fluid inlet of the dethanizer, the outlet and the gas phase import of the dethanizer of the first gas phase drier
Connection, the tower body inlet communication of the tower top outlet of the dethanizer and the domethanizing column, the tower top of the domethanizing column go out
Mouth is connected to fuel gas collector；
The inlet communication of the tower bottom outlet and the solvent recovery tower of the domethanizing column, the tower bottom of the solvent recovery tower
Outlet and the tower top inlet communication of the domethanizing column, the tower top outlet of the solvent recovery tower and the acetylene converter into
Mouth connection, the outlet of the acetylene converter and the inlet communication of the ethylene rectifying column, the tower top of the ethylene rectifying column go out
Mouth is connected to ethylene collector, and the tower bottom outlet of the ethylene rectifying column is connected to ethane collector；
The inlet communication of the tower bottom outlet and the depropanizing tower of the dethanizer, the tower top outlet of the depropanizing tower
With the inlet communication of the propylene rectification tower, the tower top outlet of the propylene rectification tower is connected to the propylene collector, described
The tower bottom outlet of propylene rectification tower is connected to propane collector；
The inlet communication of the tower bottom outlet and the debutanizing tower of the depropanizing tower, the tower top outlet of the debutanizing tower
It is connected to C4 fraction collector, the tower bottom outlet of the debutanizing tower is connected to C5 and C5 or more fraction collector.
Selectively, the pre-processing assembly includes chilling tower, water stripper, methanol distillation column, one section of compressor, compression
Two sections of machine, water scrubber, three sections of compressor, caustic wash tower and Spent caustic treatment tower；
The import of the chilling tower is connected to methanol to olefins reaction device, the tower top outlet and the methanol of the chilling tower
The inlet communication of recovery tower, the inlet communication of one section of the tower top outlet of the methanol distillation column and the compressor, the compression
One section of machine of outlet and the inlet communication of two sections of the compressor, the outlet and the import of the water scrubber of two sections of the compressor
Connection, the outlet of the water scrubber and the inlet communication of three sections of the compressor, the outlet of three sections of the compressor and the alkali
Wash the inlet communication of tower, the inlet communication of the tower top outlet of the caustic wash tower and the separator；
The inlet communication of the tower bottom outlet and the Spent caustic treatment tower of the caustic wash tower, the Spent caustic treatment tower
Outlet be connected to salkali waste collection；
The inlet communication of the tower bottom outlet and the water stripper of the chilling tower, the tower bottom outlet of the methanol distillation column
Outlet with the inlet communication of the water stripper, the water stripper is connected to water collector.
Selectively, the depropanizing tower includes high pressure depropanizer and low pressure depropanizer；
The inlet communication of the tower bottom outlet and the high pressure depropanizer of the dethanizer, the high pressure depropanizer
The inlet communication of tower top outlet and the propylene rectification tower；
The inlet communication of the tower bottom outlet and the low pressure depropanizer of the high pressure depropanizer, the low pressure depropanization
The inlet communication of the tower bottom outlet and the debutanizing tower of tower.
Selectively, described device further include: heat exchanger；
The inlet communication of the heat exchanger and the low pressure depropanizer is passed through in the tower bottom outlet of the high pressure depropanizer；
The inlet communication that the tower top outlet of the low pressure depropanizer passes through the heat exchanger and the high pressure depropanizer.
Selectively, the propylene rectification tower includes the first propylene rectification tower and the second propylene rectification tower；
The inlet communication of the tower top outlet of the high pressure depropanizer and first propylene rectification tower, first propylene
The tower top outlet of rectifying column is connected to the propylene collector；
Tower bottom outlet and the inlet communication of second propylene rectification tower of first propylene rectification tower, described the two the third
The tower bottom outlet of alkene rectifying column is connected to the propane collector；
The inlet communication of the tower top outlet of second propylene rectification tower and first propylene rectification tower.
Selectively, described device further include: four sections of compressor；
Four sections of the compressor are arranged between the dethanizer and the domethanizing column.
Selectively, described device further include: the second gas phase drier；
The second gas phase drier is arranged between the acetylene converter and the ethylene rectifying column.
Selectively, middle boiling device and reboiler are provided in the ethylene rectifying column；
The middle boiling device is arranged in from the 80-110 shelf theory column plate in the ethylene rectifying column from tower top to tower bottom；
The tower bottom of the ethylene rectifying column is arranged in the reboiler.
Selectively, it is provided with side line on 2-10 shelf theory column plate of the ethylene rectifying column from tower top to tower bottom, institute
Side line is stated to be connected to the ethylene collector.
The beneficial effect of technical solution provided by the embodiment of the utility model includes at least:
1, after pre-processing by pre-processing assembly to methanol-to-olefins gas, phase separation is carried out in the separator,
Lime set is sent to lime set drier, and gas phase is sent to the first gas phase drier, is all sent into dethanizer, deethanizer overhead after drying
Gas phase pass through domethanizing column, solvent recovery tower, acetylene converter, the isolated ethylene of ethylene rectifying column, the tower of dethanizer
Depropanizing tower, the isolated propylene of propylene rectification tower are passed through in bottom, realize the separation of methanol-to-olefins gas；
2, by setting solvent recovery tower, the absorbent used in domethanizing column can be mixed into the C2 component of tower bottom
When entering into solvent recovery tower, C2 component and absorbent separate in solvent recovery tower, tower top obtains C2 component, tower bottom obtains
Absorbent, and the absorbent of tower bottom can flow back into domethanizing column after cooling from solvent recovery tower, realize absorbent
Recycle, the circulation loop of the absorbent is domethanizing column-solvent recovery tower-domethanizing column, this be recycled back to it is short out, and
Be not related to dethanizer and propylene rectification tower, can effectively reduce the load of dethanizer and propylene rectification tower, energy consumption and
Equipment investment.
Detailed description of the invention
It, below will be to required in embodiment description in order to illustrate more clearly of the technical scheme in the embodiment of the utility model
Attached drawing to be used is briefly described, it should be apparent that, the accompanying drawings in the following description is only some realities of the utility model
Example is applied, it for those of ordinary skill in the art, without creative efforts, can also be according to these attached drawings
Obtain other attached drawings.
Fig. 1 is a kind of structural schematic diagram of the separator of methanol-to-olefins gas provided by the embodiment of the utility model；
Fig. 2 is the structural representation of the separator of another methanol-to-olefins gas provided by the embodiment of the utility model
Figure.
Appended drawing reference in figure respectively indicates are as follows:
1- pre-processing assembly, 101- chilling tower, 102- water stripper, 103- methanol distillation column, one section of 104- compressor,
Two sections of 105- compressor, 106- water scrubber, three sections of 107- compressor, 108- caustic wash tower, 109- Spent caustic treatment tower,
2- separator,
3- lime set drier,
4- the first gas phase drier,
5- dethanizer,
6- domethanizing column,
7- solvent recovery tower,
8- acetylene converter,
9- ethylene rectifying column,
10- depropanizing tower, 1001- high pressure depropanizer, 1002- low pressure depropanizer,
11- propylene rectification tower, the first propylene rectification tower of 1101-, the second propylene rectification tower of 1102-,
12- debutanizing tower,
13- fuel gas collector,
14- ethylene collector,
15- ethane collector,
16- propylene collector,
17- propane collector,
18-C4 fraction collector,
19-C5 and C5 or more fraction collector,
20- methanol to olefins reaction device,
21- salkali waste collection,
22- water collector,
23- heat exchanger,
Four sections of 24- compressor,
25- the second gas phase drier.
Specific embodiment
Unless otherwise defined, all technical terms used in the utility model embodiment all have and those skilled in the art
Normally understood identical meaning.To keep the purpose of this utility model, technical solution and advantage clearer, below in conjunction with attached
Figure is described in further detail the utility model embodiment.
The utility model embodiment provides a kind of separator of methanol-to-olefins gas, as shown in Figure 1, the device packet
Include: pre-processing assembly 1, separator 2, lime set drier 3, the first gas phase drier 4, dethanizer 5, domethanizing column 6, solvent return
Receive tower 7, acetylene converter 8, ethylene rectifying column 9, depropanizing tower 10, propylene rectification tower 11 and debutanizing tower 12.
Wherein, the inlet communication of pre-processing assembly 1 and separator 2, the gaseous phase outlet of separator 2 and the first gas phase drier
4 inlet communication, the condensate outlet of separator 2 and the inlet communication of lime set drier 3, the outlet of lime set drier 3 and de- second
The fluid inlet of alkane tower 5 is connected to, the outlet of the first gas phase drier 4 and the gas phase inlet communication of dethanizer 5, dethanizer 5
Tower top outlet and domethanizing column 6 tower body inlet communication, the tower top outlet of domethanizing column 6 is connected to fuel gas collector 13；
The inlet communication of the tower bottom outlet and solvent recovery tower 7 of domethanizing column 6, the tower bottom of solvent recovery tower 7 are exported and are taken off
The tower top inlet communication of methane tower 6, the tower top outlet of solvent recovery tower 7 and the inlet communication of acetylene converter 8, acetylene conversion
The outlet of device 8 and the inlet communication of ethylene rectifying column 9, the tower top outlet of ethylene rectifying column 9 are connected to ethylene collector 14, second
The tower bottom outlet of alkene rectifying column 9 is connected to ethane collector 15；
The inlet communication of the tower bottom outlet and depropanizing tower 10 of dethanizer 5, the tower top outlet and propylene of depropanizing tower 10
The tower top outlet of the inlet communication of rectifying column 11, propylene rectification tower 11 is connected to propylene collector 16, the tower of propylene rectification tower 11
Bottom outlet is connected to propane collector 17；
The inlet communication of the tower bottom outlet and debutanizing tower 12 of depropanizing tower 10, the tower top outlet and C4 group of debutanizing tower 12
Collector 18 is divided to be connected to, the tower bottom outlet of debutanizing tower 12 is connected to C5 and C5 or more fraction collector 19.
It is understood that being communicated with each other between each component in device by pipeline.
It should be noted that being polymer grade ethylene by the ethylene that ethylene rectifying column 9 obtains, obtained by propylene rectification tower 11
The propylene arrived is polymerization-grade propylene.
The working principle of the separator of the methanol-to-olefins gas of the utility model embodiment is described below:
The olefin mixed gas reacted in methanol to olefins reaction device 20 enters separation after pretreatment
Gas-liquid separation is carried out in device 2, obtains gaseous component and lime set component；
Gaseous component enters in the first gas phase drier 4 after the drying of progress gas from the upper outlet of separator 2, then
It enters in dethanizer 5, obtains the component of C2 and the C2 component below of tower top and the C3 and C3 or more of tower bottom；Tower top
C2 and C2 component below enters in domethanizing column 6 from the tower top outlet of dethanizer 5, to domethanizing column 6 inject C2 and
Absorbent is added while C2 component below, cold oil absorption process removes methane in utilization, obtains in the tower top of domethanizing column 6
Fuel gas (hydrogen, methane), and being collected by fuel gas collector 13, the tower bottom of domethanizing column 6 obtain C2 component with
The mixture of absorbent；
The C2 component of the tower bottom of domethanizing column 6 and the mixture of absorbent are exported from the tower bottom of domethanizing column 6 and are flowed out, and are entered
Into solvent recovery tower 7, C2 component separates in solvent recovery tower 7 with absorbent, and absorbent is dropped in the tower bottom of solvent recovery tower 7
Domethanizing column 6 is returned to after temperature, is entered in domethanizing column 6 from the tower top import of domethanizing column 6, is continued with middle cold oil and is absorbed
Method removes methane, realizes recycling for absorbent；
The C2 component that 7 tower top of solvent recovery tower obtains enter in acetylene converter 8 carry out hydrotreating after, enter back into
In ethylene rectifying column 9, ethylene is isolated, obtains ethylene in the tower top of ethylene rectifying column 9, and received by ethylene collector 14
Collection obtains ethane in the tower bottom of ethylene rectifying column 9, and is collected by ethane collector 15；
The component of the C3 and C3 or more of 5 tower bottom of dethanizer enter in depropanizing tower 9, obtain tower top C3 component and
The C3 component of the component of the C4 and C4 or more of tower bottom, tower top enters in propylene rectification tower 11, by propylene rectification tower 11, from
The propylene that the tower top of propylene rectification tower 11 is isolated, and be collected by propylene collector 16, propylene rectification tower 11
The propane that tower bottom is isolated, and collected by propane collector 17；
The component of C4 and C4 or more that 9 tower bottom of depropanizing tower obtains enter in debutanizing tower, from the tower of debutanizing tower 12
Top obtains C4 component, and is collected by C4 fraction collector 18, the C5 and C5 or more obtained from the tower bottom of debutanizing tower 12
Component, and collected by the collector 19 of C5 and C5 or more component.
Middle cold oil absorption process mentioned herein refers to -40 DEG C of propylene refrigerant refrigeration of use in conjunction with propane absorbent to reduce
The race of ethylene is damaged.
It should be noted that absorbent can select one of C3, C4 or C5 or a variety of, preferably propane, pass through gas
Liquid equilibrium principle absorbs ethylene, to improve the rate of recovery of ethylene；Propylene refrigerant is provided with 7 DEG C, -24 DEG C, -40 DEG C of three temperature
Grade.
Therefore, the separator of the methanol-to-olefins gas of the utility model embodiment utilizes pre-processing assembly 1, separator
2, lime set drier 3, the first gas phase drier 4, dethanizer 5, domethanizing column 6, solvent recovery tower 7, acetylene converter 8, second
Alkene rectifying column 9, depropanizing tower 10, propylene rectification tower 11 and debutanizing tower 12, realize the separation of methanol-to-olefins gas, simultaneously
The circulation loop of the absorbent used in domethanizing column 6 is become into domethanizing column 6- solvent recovery tower 7- domethanizing column 6, is shortened
Circulation loop, and it is not related to dethanizer 5 and propylene rectification tower 11, dethanizer 5 and propylene essence can be effectively reduced
Load, energy consumption and the equipment investment for evaporating tower 11, improve the stability of device.
The Each part of the separator of the methanol-to-olefins gas of the utility model embodiment is carried out into one below
Step ground description explanation:
For pre-processing assembly 1, play the role of the pretreated of the mixed gas obtained to methanol-to-olefins, specifically
Ground, the pre-processing assembly 1 include chilling tower 101, water stripper 102, methanol distillation column 103, one section 104 of compressor, compressor
Two section 105, water scrubber 106, three section 107 of compressor, caustic wash tower 108 and Spent caustic treatment tower 109, as shown in Figure 2.
Wherein, the import of chilling tower 101 is connected to methanol to olefins reaction device 20, the tower top outlet and first of chilling tower 101
The inlet communication of alcohol recovery tower 103, the tower top outlet of methanol distillation column 103 and one section 104 of compressor of inlet communication, compress
The outlet and two section 105 of compressor of inlet communication that one section 104 of machine, the import of the outlet and water scrubber 106 that two section 105 of compressor
Connection, the outlet of water scrubber 106 and three section 107 of compressor of inlet communication, the outlet and caustic wash tower 108 that three section 107 of compressor
Inlet communication, the inlet communication of the tower top outlet of caustic wash tower 108 and separator 2；
The inlet communication of the tower bottom outlet and Spent caustic treatment tower 109 of caustic wash tower 108, Spent caustic treatment tower 109
Outlet is connected to salkali waste collection 21；
Tower bottom outlet and the inlet communication of water stripper 102 of chilling tower 101, the tower bottom outlet of methanol distillation column 103 with
The outlet of the inlet communication of water stripper 102, water stripper 102 is connected to water collector 22.
So set, the olefin mixed gas reacted in methanol to olefins reaction device 20 enters in chilling tower 101
After carrying out heat recovery, is entered in methanol distillation column 103 from the tower top outlet of chilling tower 101 and recycle methanol, using compression
One section 104 of machine, two section 105 of compressor compression after enter in water scrubber 106 and washed, to remove oxide impurity, such as
Methanol, dimethyl ether etc., then wash after gas enter three section 107 of compressor carry out first compression again after, enter caustic wash tower
In 108, to remove sour gas, such as carbon dioxide；
Spent lye in caustic wash tower 108 is entered in Spent caustic treatment tower 109 by the tower bottom outlet of caustic wash tower 108,
It after pretreatment by Spent caustic treatment tower 109, is collected into salkali waste collection 21, in case in subsequent processing or making
With；
And by the liquid phase after cooling of chilling tower 101, it is entered in water stripper 102 by the tower bottom outlet of chilling tower 101,
Since the effect of water stripper 102 is to be stripped out the hydrocarbon component in water, it is purified water, thus, water stripper 102
Outlet can be connected to water collector 22, be collected to water.
It is understood that methanol distillation column 103 is after recycling methanol, liquid phase component can be recycled further, be led to
The inlet communication of the tower bottom outlet and water stripper 102 of methanol distillation column 103 is crossed, also available purified water.
Gas after above-mentioned cooling, compression, washing and alkali cleaning, as pretreated gas can be carried out into one
The separation of step ground.
For separator 2, separator 2 plays the role of each phase component of separation, in the utility model embodiment, point
It is gas-liquid water three-phase separator from device 2.
For depropanizing tower 10, depropanizing tower 10 plays the role of separating C3 with the component of C4 and C4 or more, tool
Body, depropanizing tower 10 includes high pressure depropanizer 1001 and low pressure depropanizer 1002, as shown in Figure 2.
Wherein, the inlet communication of the tower bottom outlet and high pressure depropanizer 1001 of dethanizer 5, high pressure depropanizer 1001
Tower top outlet and propylene rectification tower 11 inlet communication；
The inlet communication of the tower bottom outlet and low pressure depropanizer 1002 of high pressure depropanizer 1001, low pressure depropanizer
The inlet communication of 1002 tower bottom outlet and debutanizing tower 12.
By setting high pressure depropanizer 1001 and low pressure depropanizer 1002, temperature point in domethanizing column 6 can be made
Cloth and cryogen matching are more reasonable；Compared with single depropanizing tower 10, using high pressure depropanizer 1001 and low pressure depropanizer
1002 total load is lower, and the tower top of high pressure depropanizer 1001 does not need liquid phase discharging, and the tower of low pressure depropanizer 1002
Low-pressure steam dosage significantly reduces in the reboiler of bottom, can save energy consumption to a certain extent；In addition, using high pressure depropanizer
1001 and low pressure depropanizer 1002 combine, can also reduce C4 and C4 or more unsaturated hydrocarbons (such as butadiene) in depropanizing tower 10
The problem of generating polymer, fouling blockage column plate, separative efficiency reduction, segregational load caused to increase, so as to extend device fortune
The row period.
Based on high pressure depropanizer 1001 and low pressure depropanizer 1002, the methanol-to-olefins gas of the utility model embodiment
The separator of body further include: heat exchanger 23.
Wherein, the import of heat exchanger 23 and low pressure depropanizer 1002 is passed through in the tower bottom outlet of high pressure depropanizer 1001
Connection；The tower top outlet of low pressure depropanizer 1002 passes through the inlet communication of heat exchanger 23 and high pressure depropanizer 1001, such as schemes
Shown in 2.
By the way that heat exchanger 23 is arranged, the hot logistics of the tower bottom of high pressure depropanizer 1001 and low pressure depropanizer can be made
The cold logistics of 1002 tower top mutually exchanges heat, to meet the requirement of the technique in respective tower.
For propylene rectification tower 11, in order to preferably separate propylene and propane, propylene rectification tower 11 includes the one the third
Alkene rectifying column 1101 and the second propylene rectification tower 1102.
Wherein, the inlet communication of the tower top outlet of high pressure depropanizer 1001 and the first propylene rectification tower 1101, the one the third
The tower top outlet of alkene rectifying column 1101 is connected to propylene collector 16；
The inlet communication of the tower bottom outlet and the second propylene rectification tower 1102 of first propylene rectification tower 1101, the second propylene essence
The tower bottom outlet for evaporating tower 1102 is connected to propane collector 17；
The inlet communication of the tower top outlet of second propylene rectification tower 1102 and the first propylene rectification tower 1101, as shown in Figure 2.
Pass through the first propylene rectification tower 1101 of setting and the second propylene rectification tower 1102, after rectifying twice, Ke Yiti
The rate of recovery of high propylene.
It is understood that the propane that the tower bottom of the second propylene rectification tower 1102 obtains can pass out to the propane recovery phase 17
In, it can also be sent in solvent recovery tower 7, to supplement the loss of absorbent.
In order to which the removing of methane is better achieved, the separator of the methanol-to-olefins gas of the utility model embodiment is also
It include: four section 24 of compressor, four section 24 of compressor is arranged between dethanizer 5 and domethanizing column 6, as shown in Figure 2.
The C2 and C2 component below flowed out from the tower top outlet of dethanizer 5 can pass through four section 24 of compressor of pressure
After contracting, enters back into domethanizing column 6 and carry out further demethanation processing.
In order to preferably separate ethylene and ethane, due to being converted in acetylene converter 8 by hydrotreating, second is improved
The rate of recovery of alkene, the separator of the methanol-to-olefins gas of the utility model embodiment further include: the second gas phase drier 25；
Second gas phase drier 25 is arranged between acetylene converter 8 and ethylene rectifying column 9, as shown in Figure 2.
By the second gas phase drier 25, the product water after the conversion of acetylene converter 8 can be removed.
In order to further reduce plant energy consumption, in the utility model embodiment, middle boiling is provided in ethylene rectifying column 9
Device (not shown in figure) and reboiler (not shown in figure).
Wherein, middle boiling device is arranged in from the 80-110 shelf theory column plate in ethylene rectifying column 9 from tower top to tower bottom, then boils
The tower bottom of ethylene rectifying column 9 is arranged in device.
By in middle boiling device and reboiler use propylene refrigerant heat supply, can effective recovery waste heat, reduce propylene refrigerant use
Amount reduces propylene refrigeration compressor power consumption, further realizes the reduction of plant energy consumption.
For more convenient collection ethylene, ethylene rectifying column 9 is arranged on the 2-10 shelf theory column plate from tower top to tower bottom
There is side line, side line is connected to ethylene collector 14, and the collection to ethylene may be implemented.
The above is merely for convenience of it will be understood by those skilled in the art that the technical solution of the utility model, not to
Limit the utility model.Within the spirit and principle of the utility model, any modification, equivalent replacement, improvement and so on,
It should be included within the scope of protection of this utility model.
Claims (9)
1. a kind of separator of methanol-to-olefins gas, which is characterized in that described device includes: pre-processing assembly (1), separation
Device (2), lime set drier (3), the first gas phase drier (4), dethanizer (5), domethanizing column (6), solvent recovery tower (7),
Acetylene converter (8), ethylene rectifying column (9), depropanizing tower (10), propylene rectification tower (11) and debutanizing tower (12), wherein
The inlet communication of the pre-processing assembly (1) and the separator (2), the gaseous phase outlet of the separator (2) with it is described
The inlet communication of first gas phase drier (4), the import of the condensate outlet of the separator (2) and the lime set drier (3)
Connection, the lime set drier (3) are connected to the fluid inlet of the dethanizer (5), the outlet of the first gas phase drier (4)
With the gas phase inlet communication of the dethanizer (5), tower top outlet and the domethanizing column (6) of the dethanizer (5)
The tower top outlet of tower body inlet communication, the domethanizing column (6) is connected to fuel gas collector (13)；
The inlet communication of the tower bottom outlet and the solvent recovery tower (7) of the domethanizing column (6), the solvent recovery tower (7)
Tower bottom outlet and the tower top inlet communication of the domethanizing column (6), the tower top outlet of the solvent recovery tower (7) and the second
The inlet communication of alkynes converter (8), the outlet of the acetylene converter (8) and the inlet communication of the ethylene rectifying column (9), institute
The tower top outlet for stating ethylene rectifying column (9) is connected to ethylene collector (14), the tower bottom outlet of the ethylene rectifying column (9) and second
Alkane collector (15) connection；
The inlet communication of the tower bottom outlet and the depropanizing tower (10) of the dethanizer (5), the depropanizing tower (10)
The inlet communication of tower top outlet and the propylene rectification tower (11), the tower top outlet and propylene of the propylene rectification tower (11) are collected
The tower bottom outlet of device (16) connection, the propylene rectification tower (11) is connected to propane collector (17)；
The inlet communication of the tower bottom outlet and the debutanizing tower (12) of the depropanizing tower (10), the debutanizing tower (12)
Tower top outlet is connected to C4 fraction collector (18), tower bottom outlet and C5 and C5 or more the Fraction collection of the debutanizing tower (12)
Device (19) connection.
2. the separator of methanol-to-olefins gas according to claim 1, which is characterized in that the pre-processing assembly
It (1) include chilling tower (101), water stripper (102), methanol distillation column (103), one section of compressor (104), two sections of compressor
(105), water scrubber (106), three sections of compressor (107), caustic wash tower (108) and Spent caustic treatment tower (109)；
The import of the chilling tower (101) is connected to methanol to olefins reaction device (20), the tower top outlet of the chilling tower (101)
With the inlet communication of the methanol distillation column (103), one section of the tower top outlet and the compressor of the methanol distillation column (103)
(104) inlet communication, the inlet communication of the outlet of the compressor one section (104) and the compressor two sections (105) are described
The inlet communication of the outlet of compressor two sections (105) and the water scrubber (106), the outlet of the water scrubber (106) with it is described
The inlet communication of compressor three sections (107), the outlet of the compressor three sections (107) and the import of the caustic wash tower (108) connect
It is logical, the tower top outlet of the caustic wash tower (108) and the inlet communication of the separator (2)；
The inlet communication of the tower bottom outlet and the Spent caustic treatment tower (109) of the caustic wash tower (108), the spent lye are pre-
The outlet for the treatment of column (109) is connected to salkali waste collection (21)；
The inlet communication of the tower bottom outlet and the water stripper (102) of the chilling tower (101), the methanol distillation column
(103) inlet communication of tower bottom outlet and the water stripper (102), the outlet of the water stripper (102) and water are collected
Device (22) connection.
3. the separator of methanol-to-olefins gas according to claim 1, which is characterized in that the depropanizing tower (10)
Including high pressure depropanizer (1001) and low pressure depropanizer (1002)；
The inlet communication of the tower bottom outlet and the high pressure depropanizer (1001) of the dethanizer (5), the high pressure-off third
The tower top outlet of alkane tower (1001) and the inlet communication of the propylene rectification tower (11)；
The inlet communication of the tower bottom outlet and the low pressure depropanizer (1002) of the high pressure depropanizer (1001) is described low
Press the inlet communication of the tower bottom outlet and the debutanizing tower (12) of depropanizing tower (1002).
4. the separator of methanol-to-olefins gas according to claim 3, which is characterized in that described device further include:
Heat exchanger (23)；
The tower bottom outlet of the high pressure depropanizer (1001) is by the heat exchanger (23) and the low pressure depropanizer
(1002) inlet communication；
The tower top outlet of the low pressure depropanizer (1002) passes through the heat exchanger (23) and the high pressure depropanizer
(1001) inlet communication.
5. the separator of methanol-to-olefins gas according to claim 3, which is characterized in that the propylene rectification tower
It (11) include the first propylene rectification tower (1101) and the second propylene rectification tower (1102)；
The inlet communication of the tower top outlet of the high pressure depropanizer (1001) and first propylene rectification tower (1101), it is described
The tower top outlet of first propylene rectification tower (1101) is connected to the propylene collector (16)；
The inlet communication of the tower bottom outlet and second propylene rectification tower (1102) of first propylene rectification tower (1101), institute
The tower bottom outlet for stating the second propylene rectification tower (1102) is connected to the propane collector (17)；
The inlet communication of the tower top outlet of second propylene rectification tower (1102) and first propylene rectification tower (1101).
6. the separator of methanol-to-olefins gas according to claim 1, which is characterized in that described device further include:
Four sections of compressor (24)；
Four sections of the compressor (24) is arranged between the dethanizer (5) and the domethanizing column (6).
7. the separator of methanol-to-olefins gas according to claim 1, which is characterized in that described device further include:
Second gas phase drier (25)；
The second gas phase drier (25) is arranged between the acetylene converter (8) and the ethylene rectifying column (9).
8. the separator of methanol-to-olefins gas according to claim 1, which is characterized in that the ethylene rectifying column
(9) middle boiling device and reboiler are provided in；
The middle boiling device setting is at the 80-110 shelf theory column plate in the ethylene rectifying column (9) from tower top to tower bottom；
Tower bottom of the reboiler setting in the ethylene rectifying column (9).
9. the separator of methanol-to-olefins gas according to claim 1, which is characterized in that the ethylene rectifying column
(9) side line is provided on the 2-10 shelf theory column plate from tower top to tower bottom, the side line and the ethylene collector (14) are even
It is logical.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821585168.3U CN209193845U (en) | 2018-09-27 | 2018-09-27 | The separator of methanol-to-olefins gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821585168.3U CN209193845U (en) | 2018-09-27 | 2018-09-27 | The separator of methanol-to-olefins gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111238164A (en) * | 2020-02-11 | 2020-06-05 | 大连理工大学 | Intercooling separation device and process for catalytic cracking product gas |
| CN111336715A (en) * | 2020-03-17 | 2020-06-26 | 苏应玺 | Energy-saving refrigeration system suitable for olefin separation process |
-
2018
- 2018-09-27 CN CN201821585168.3U patent/CN209193845U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111238164A (en) * | 2020-02-11 | 2020-06-05 | 大连理工大学 | Intercooling separation device and process for catalytic cracking product gas |
| CN111336715A (en) * | 2020-03-17 | 2020-06-26 | 苏应玺 | Energy-saving refrigeration system suitable for olefin separation process |
| CN111336715B (en) * | 2020-03-17 | 2021-09-24 | 华亭煤业集团有限责任公司 | Energy-saving refrigeration system suitable for olefin separation process |
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