CN105985214B - A kind of method recycling ethylene and a kind of method of separation hydrocarbon mixture - Google Patents
A kind of method recycling ethylene and a kind of method of separation hydrocarbon mixture Download PDFInfo
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- CN105985214B CN105985214B CN201510045123.1A CN201510045123A CN105985214B CN 105985214 B CN105985214 B CN 105985214B CN 201510045123 A CN201510045123 A CN 201510045123A CN 105985214 B CN105985214 B CN 105985214B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
A method of it is used for recycling ethylene from the mixture comprising ethylene, this method includes：The mixture comprising ethylene is set to enter absorption tower from the entrance of absorb the bottom of the tower；The absorption tower includes the main absorber portion of lower part and the assist absorption section on top, in the main absorber portion, winner's absorbent is set to be contacted with the mixture, to which ethylene be detached from the mixture, in the assist absorption section, so that auxiliary absorbent is contacted with the mixture, main absorbent is recycled from the mixture.The present invention also provides a kind of methods for being detached to hydrocarbon mixture.
Description
Technical field
The invention belongs to light hydrocarbons separation technology fields, more particularly to ethylene is recycled from the hydrocarbon mixture containing ethylene
Isolation technics.
Background technology
Ethylene and propylene are the basic materials of petrochemical industry, the past all the time by hydrocarbon steam cracking or catalytic pyrolysis
It obtains.In the case where being becoming tight oil supply day, it is developed and is especially produced using methanol, ethyl alcohol as raw material with oxide
The process of low-carbon alkene.Alcohols can use the production of the synthesis gas of natural gas or coal, avoid to use petroleum resources in this way.Hydrocarbon
The separation of class is the key points and difficulties of naphtha pyrolysis ethylene and MTO/MTP techniques, equipment investment, energy consumption and operating cost
Account for 70% or more of entire technical process.
Since the relative volatility of methane and ethylene is very close to domethanizing column is difficult to realize clear point of methane and ethylene
It cuts, the separation of realization ethylene and methane is the core of separation of olefins.Conventional method generally using deep cooling come separation of methane and ethylene,
To improve yield of ethene.Typical deep cooling separating method includes sequence separation, front-end deethanization and predepropanization process, three kinds of flows
With respective advantage and disadvantage, but -100 DEG C of Cryogenic Conditions below are required to, need ethylene refrigeration compressor, or even need first
Alkane refrigeration compressor provides cold for it, more demanding to ice chest so that construction investment increases.
The lower carbon number hydrocarbons feature that Modern Coal-based Chemical is produced is that hydrogen, methane content are relatively low, ethylene, propylene and four content of carbon compared with
Height causes domethanizing column using cryogenic separation and improper.Therefore in now generally being used for the separation of olefins of MTO/MTP techniques
Cold separation process.
WO01/25174 discloses a kind of method of separation of olefins, and this method is mainly characterized by using front-end deethanization stream
Journey is compared with conventional naphtha pyrolysis production ethylene unit, improves the ethylene contents in demethanizer overhead, to
Demethanation tower top temperature is improved, avoids using ethylene cold；In order to recycle the ethylene in demethanation overhead gas, by the gas
It is sent into pressure-variable adsorption (PSA) facility, separation of methane, hydrogen and ethylene, by the ethylene Returning oxidation reactor outlet material of recycling
In.The separation method avoids cryogenic separation, but as a result of PSA technology, equipment investment is larger, and operation sequence is more complex
And it is unstable, the workload of system maintenance is larger.
Chinese patent CN101747128A develops a kind of alkene separation method of MTO.The core of this method is to make piptonychia
The gas phase that alkane tower top comes out cools to -60~-45 DEG C, and liquid phase is back to domethanizing column after gas-liquid separation, and gas phase enters
Expanding machine makes its temperature drop to -120~-90 DEG C.The gas of the low temperature is first that domethanizing column top gas cools down, then by cold
Case is the propane absorbent cooling from propylene rectification tower bottom, makes full use of its -120~-90 DEG C of low temperature cold.The party
The more traditional cryogenic separation of method can reduce ethylene loss rate, and energy consumption is relatively low, but still has the following disadvantages：(1) it increases a set of
Expander system and ice chest, and flow is more complex, propylene refrigerant dosage is also very big；(2) due to dropping to -120 by expansion temperature
~-90 DEG C, this needs to use a large amount of low-temperature steel, and investment is larger；(3) sequence separation process, all logistics is used all to pass through
Domethanizing column, domethanizing column load is big, is particularly unsuitable for forming heavier hydrocarbon products separation.
Therefore, the present invention wishes a kind of new technique, and hydrocarbon mixture, especially C2 and C3 hydro carbons are realized under middle cool condition
Efficiently separate, while avoiding all logistics all by domethanizing column or dethanizer so that technique is produced suitable for heavier hydro carbons
The separation of product, simplified process equipment is cost-effective, reduces the loss late of target product.
Invention content
In order to achieve the above technical purposes, the present invention develop a kind of novel rectifying-absorption be combined, main absorption and
Assist absorption cold separation process in being combined.This method is high with product recovery rate, investment is small, flow is simple and easy to operate
Many advantages, such as, it is particularly suitable for the separation of the heavier hydrocarbon products of product form.
The first aspect of the invention provides a kind of method for being used for recycling ethylene from the mixture comprising ethylene, should
Method includes：The mixture comprising ethylene is set to enter absorption tower from the entrance of absorb the bottom of the tower；Under the absorption tower includes
The main absorber portion in portion and the assist absorption section on top, in the main absorber portion so that main absorbent is contacted with the mixture,
To detach ethylene from the mixture, in the assist absorption section so that auxiliary absorbent connects with the mixture
It touches, main absorbent is recycled from the mixture；Including the main absorbent and auxiliary absorbent of ethylene are discharged from absorb the bottom of the tower,
And detach mixture discharge at the top of absorption tower after ethylene；The main absorbent be selected from following hydro carbons any one or it is more
Kind：C3 hydro carbons, C4 hydro carbons, C5-C8 hydro carbons；The auxiliary absorbent is selected from any one or more of following hydro carbons：C2 hydrocarbon
Class, C3 hydro carbons.
The present invention a preferred embodiment in, the main absorbent in following hydro carbons any one or
It is a variety of：C3 hydro carbons, C4 hydro carbons and C5 hydro carbons；Any one or more more preferable of the main absorbent in following hydro carbons：
C3 hydro carbons and C4 hydro carbons；The more preferable main absorbent is selected from following hydro carbons any one or more of：Propane, propylene, butane,
Butylene, pentane and amylene；The auxiliary absorbent is selected from the one or more of following components：Ethane and propane.
In another preferred embodiment of the present invention, on the basis of the total weight of the mixture comprising ethylene
Meter, the content of ethylene is 20-80 weight %, preferably 30-70 weight % in the mixture comprising ethylene, more preferably
40-65 weight %, more preferably 50-60 weight %；One kind selected from the following is additionally comprised in the mixture comprising ethylene
Or a variety of substance：Hydrogen, methane, ethane, ethylene, propylene, propane, butylene, butane, amylene, pentane, hexene, hexane, ether,
Alcohol；It is preferred that additionally comprising one or more substance selected from the following in the mixture comprising ethylene：Hydrogen, methane, second
Alkane, ethylene, propylene, propane, butylene, butane；Selected from the following one is additionally comprised in the more preferably described mixture comprising ethylene
Kind or a variety of substances：Hydrogen, methane, ethane, ethylene, propylene, propane；In the more preferably described mixture comprising ethylene in addition
Including one or more substance selected from the following：Methane, ethane, ethylene, propylene, propane.
In another preferred embodiment of the present invention, the tower of the assist absorption Duan Yuzhu absorber portions on the absorption tower
The ratio between diameter is 0.1~0.8:1, the absorption tower is plate column or packed tower；When the absorption tower is plate column, the auxiliary
The ratio between number of plates of absorber portion and main absorber portion is 0.1~0.5:1, the wherein number of plates of assist absorption section is 5~30.
In another preferred embodiment of the present invention, the main absorber portion is provided with 1-3 charge air cooler, it is described
Charge air cooler produces a part of material from the main absorber portion, reduces the temperature of the material, then returns it to the master again
Absorber portion is counted on the basis of the material total flow in the absorption tower, and the ratio of the material of extraction accounts for 10-80%, cold in described
The cooling temperature of device is -40 DEG C~-10 DEG C.
In another preferred embodiment of the present invention, entrance of the mixture comprising ethylene from absorb the bottom of the tower
Temperature when into absorption tower is -40 DEG C~-10 DEG C, preferably -40 DEG C~-20 DEG C；Described in the main absorbent enters
Temperature when absorption tower is -40 DEG C~-10 DEG C, preferably -40 DEG C~-20 DEG C；The auxiliary absorbent enters the suction
Temperature when receiving tower is -40 DEG C~-10 DEG C, preferably -40 DEG C~-20 DEG C；Pressure in absorption tower is 10-50 bars, excellent
It is selected as 15-40 bars, more preferably 25-35 bars.
The second aspect of the invention provides a kind of method detached to the mixture comprising hydro carbons, described to include
The mixture of hydro carbons includes following components：C1 hydrocarbon, C2 hydrocarbon, C3 hydrocarbon；The mixture comprising hydro carbons also optionally includes following
It is one or more in optional components：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, C7 hydrocarbon, C8 hydrocarbon, C9 hydrocarbon, C10 hydrocarbon, alcohol, ether, alkynes；It is preferred that
Ground, the mixture comprising hydro carbons also optionally include one or more in following optional components：Hydrogen, C4 hydrocarbon, C5 hydrocarbon,
C6 hydrocarbon, methanol, dimethyl ether, acetylene, propine；It is highly preferred that the mixture comprising hydro carbons also optionally includes following optional
It is one or more in component：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, methanol, dimethyl ether；
It the described method comprises the following steps：(1) mixture comprising hydro carbons is detached in high pressure depropanizer
Operation, obtains the logistics of high pressure depropanizer top and high pressure depropanizer kettle logistics, wherein high pressure depropanizer top logistics is not
It is equal to or more than four hydrocarbon containing carbon number, the high pressure depropanizer kettle logistics is equal to or less than two hydrocarbon without carbon number；(2) described
High pressure depropanizer kettle logistics carries out lock out operation in low pressure depropanizer, obtains the logistics of low pressure depropanizer top and low pressure is de-
Propane tower reactor logistics, wherein low pressure depropanizer top logistics includes the hydrocarbon that carbon number is equal to three, the low pressure depropanizer kettle
Logistics includes the hydrocarbon that carbon number is equal to or more than four；(3) high pressure depropanizer top logistics optionally carries out hydrogenation and removing alkynes
It is condensed with cooling, then part conveying returns to the high pressure depropanizer, and a part is delivered to domethanizing column and carries out separation behaviour
Make, obtain demethanation overhead stream and demethanation tower reactor logistics, the demethanation overhead stream includes C1 hydrocarbon, C2 hydrocarbon and optional
Hydrogen, the demethanation tower reactor logistics include C2 hydrocarbon and C3 hydrocarbon；(4) the demethanation tower reactor logistics is divided in dethanizer
From operation, deethanization overhead stream and deethanization tower reactor logistics are obtained, the deethanization overhead stream includes C2 hydrocarbon, the de- second
Alkane tower reactor logistics includes C3 hydrocarbon；(5) the deethanization overhead stream carries out lock out operation in ethylene rectifying column, is detached
Ethane is optionally delivered to absorption tower as auxiliary absorbent by ethane and ethylene；The deethanization tower reactor logistics is in propylene essence
It evaporates and carries out lock out operation in tower, the propane and propylene detached, optionally using delivery of propane to absorption tower as assist absorption
Agent；(6) demethanation overhead stream enters absorption tower from the entrance of absorb the bottom of the tower, and the absorption tower includes the main absorber portion of lower part
With the assist absorption section on top, in the main absorber portion so that main absorbent is contacted with the mixture, to by ethylene from
It is detached in the demethanation overhead stream, in the assist absorption section so that auxiliary absorbent and the demethanation overhead materials
Stream contact, recycles main absorbent, including the main absorbent of ethylene and auxiliary absorbent conduct from the demethanation overhead stream
It absorbs tower reactor logistics to be discharged from absorb the bottom of the tower, is delivered to the high pressure depropanizer or domethanizing column, and after detaching ethylene
Demethanation overhead stream be discharged as absorbing tower top tail gas at the top of the absorption tower, be delivered to gas ductwork；The main absorbent
Selected from any one or more of following hydro carbons：C3 hydro carbons, C4 hydro carbons, C5-C8 hydro carbons；The auxiliary absorbent is selected from following hydrocarbon
Any one or more of class：C2 hydro carbons, C3 hydro carbons；(7) the low pressure depropanizer top logistics part conveying is back to institute
High pressure depropanizer is stated, a part is delivered to propane and propylene that the propylene rectification tower carries out isolated separation, a part
The absorption tower is optionally delivered to as main absorbent or auxiliary absorbent；(8) the low pressure depropanizer kettle logistics delivery
Lock out operation is carried out to debutanizing tower, obtains debutanization overhead stream and debutanization tower reactor logistics, the debutanization overhead stream
Including C4 hydrocarbon, the deethanization tower reactor logistics includes the hydrocarbon that carbon number is equal to or more than five, optionally by the debutanization overhead materials
One or both of stream and debutanization tower reactor logistics are delivered to the absorption tower as main absorbent.
In another preferred embodiment of the present invention, in the step (1), with the mixing for including hydro carbons
It is counted on the basis of the total weight of C3 hydrocarbon in object, the C3 hydrocarbon of at least 60 weight % enters high pressure depropanizer kettle logistics.
It in step (2), is counted on the basis of the total weight of low pressure depropanizer top logistics, the low pressure depropanizer
It pushes up logistics and includes at least C3 hydrocarbon of 99.5 weight %；In step (7), the total weight with low pressure depropanizer top logistics is
The low pressure depropanizer top logistics of benchmark meter, 0-50 weight %, preferably 5-40 weight %, more preferable 10-30 weight % is defeated
It send and returns to the high pressure depropanizer；50-80 weight %, preferably the low pressure depropanizer top logistics of 50-60 weight % are defeated
It send to the propylene rectification tower；The low pressure depropanizer top logistics delivery of 10-40 weight %, preferably 20-30 weight % are extremely
The main absorber portion on absorption tower；In step (4), optionally by least part deethanization tower reactor logistics delivery to the suction
The main absorber portion of tower is received as main absorbent.
In another preferred embodiment of the present invention, the bottom temperature of (1) described high pressure depropanizer is 40-60
DEG C, tower top temperature is -5 DEG C to 15 DEG C, and pressure is 10-15 bars, number of plates 35-60；(2) tower reactor of the low pressure depropanizer
Temperature is 60-90 DEG C, and tower top temperature is 0-15 DEG C, and pressure is 5-9 bars, number of plates 30-50；(3) tower of the domethanizing column
Kettle temperature degree is 0-20 DEG C, and tower top temperature is -40 DEG C to -20 DEG C, and pressure is 25-35 bars, number of plates 40-70；(4) the de- second
The bottom temperature of alkane tower is 40-60 DEG C, and tower top temperature is -40 DEG C to -15 DEG C, and pressure is 17-24 bars, number of plates 40-70；(5)
The bottom temperature of the ethylene rectifying column is 0-20 DEG C, and tower top temperature is -40 to -34 DEG C, and pressure is 11-17 bars, the number of plates
60-90；The bottom temperature of the propylene rectification tower is 40-80 DEG C, and tower top temperature is 35-50 DEG C, and pressure is 15-20 bars, preferably
Double-Tower Structure；(6) bottom temperature on the absorption tower is -40 DEG C~-20 DEG C, and preferably -40 DEG C~-30 DEG C, pressure is
10-50 bars, preferably 15-40 bars, more preferably 25-35 bars；(7) bottom temperature of the debutanizing tower is 90-120 DEG C, tower
It is 38-45 DEG C to push up temperature, and pressure is 3-6 bars, number of plates 40-55.
Description of the drawings
The present invention is in conjunction with the following drawings described some embodiments of the present invention.
Fig. 1 shows absorption tower according to one embodiment of the present invention；
Fig. 2 shows separation of hydrocarbons flow chart according to one embodiment of the present invention, wherein using C3 hydrocarbon as main absorption
Agent is delivered to absorption tower；
Fig. 3 shows separation of hydrocarbons flow chart according to one embodiment of the present invention, wherein using C4 hydrocarbon as main absorption
Agent is delivered to absorption tower；
Fig. 4 shows separation of hydrocarbons flow chart according to one embodiment of the present invention, wherein using C5+ hydrocarbon as main absorption
Agent is delivered to absorption tower；
The meaning numbered in attached drawing is as follows：
T-01A-high pressure depropanizer T-01B-low pressure depropanizer
T-02-domethanizing column T-03-dethanizer
T-04-ethylene rectifying column T-05-propylene rectification tower
T-06-absorption tower T-07-debutanizing tower
E-01-heater E-02-cooling water cooler
E-03-cooler E-04-cooler
E-05-charge air cooler E-06-auxiliary absorbent cooler
The main absorbent cooler C-01-fourth stage compressors of E-07-
R-01-alkyne hydrogenation reactor V-01-flash tank
Specific implementation mode
" range " disclosed herein is in the form of lower and upper limit.Can be respectively one or more lower limits and one
Or multiple upper limits.Given range is defined by selecting a lower limit and a upper limit.Selected lower and upper limit limit
The boundary of special range is determined.All ranges that can be defined in this way comprising and can combine, i.e., any lower limit
It can combine to form a range with any upper limit.For example, the range of 60-120 and 80-110 are listed for special parameter, reason
Solution is that the range of 60-110 and 80-120 is also to expect.In addition, if the minimum zone value 1 and 2 listed, and if list
Maximum magnitude value 3,4 and 5, then below range can all expect：1-3,1-4,1-5,2-3,2-4 and 2-5.
In the present invention, unless otherwise indicated, numberical range " a-b " indicates the contracting of the arbitrary real combinings between a to b
Sketch form shows that wherein a and b are real numbers.Such as numberical range " 0-5 " indicates all to have listed herein between " 0-5 "
Whole real numbers, " 0-5 " are that the breviary of these combinations of values indicates.
If be not specifically stated, the term " two kinds " used in this specification refers to " at least two ".
In the present invention, if without particularly illustrating, all embodiments mentioned in this article and preferred implementation side
Formula can be combined with each other to form new technical solution.
In the present invention, if without particularly illustrating, all technical characteristics and preferred feature mentioned in this article can
New technical solution is formed to be combined with each other.
In the present invention, if without particularly illustrating, all steps mentioned in this article can be carried out sequentially, can also
It is random to carry out, it is preferred that being that sequence carries out.For example, the method includes the steps (a) and (b), indicate that the method can wrap
The step of sequence carries out (a) and (b) are included, can also include the steps that sequence carries out (b) and (a).For example, described mention the side
Method may also include step (c), indicate that step (c) can be added to the method with random order, for example, the method may include
Step (a), (b) and (c) may also comprise step (a), (c) and (b), can also include step (c), (a) and (b) etc..
In the present invention, if without particularly illustrating, " comprising " mentioned in this article indicates open, can also be envelope
Enclosed.For example, the " comprising " can indicate can also to include the other elements that do not list, can also only include the member listed
Part.
In the present invention, for simplicity, indicate straight with the carbon number with " hydrocarbon " or " hydro carbons " that carbon number limits
The combination of the alkane and alkene of chain and branch, but wherein do not include cycloalkane, cycloolefin, aromatic hydrocarbons and alkynes.It is of the present invention
" hydrocarbon " of certain carbon number may include the arbitrary isomers for having the straight chain of the carbon number and the alkane of branch and alkene.Example
Such as, C1 hydrocarbon indicates that methane, C2 hydrocarbon indicate that ethane and ethylene, C3 hydrocarbon indicate propane and propylene, such as n-propane, isopropyl alkane, positive third
Alkene and isopropyl alkene, C4 indicate normal butane, secondary butane, iso-butane, tertiary butane, n-butene, middle butylene, isobutene and tertiary butylene.?
In the present invention, hydro carbons of the carbon number more than the specific carbon number, such as C5+ hydrocarbon tables are indicated with mode of the specific carbon number with plus sige (+)
Show that the hydro carbons for including at least five carbon, C6+ indicate the hydro carbons for including at least six carbon.In an embodiment of the invention,
C5+ hydrocarbon indicates C5-C10 hydrocarbon.In yet another embodiment of the present invention, C5+ hydrocarbon indicates C5-C8 hydrocarbon.At one of the present invention
In embodiment, C6+ hydrocarbon indicates C6-C10 hydrocarbon.In yet another embodiment of the present invention, C6+ hydrocarbon indicates C6-C8 hydrocarbon.
The method of the present invention can be used for preferably returning C2 the and C3 hydrocarbon components in the mixture comprising hydro carbons
It receives, ideal recovering effect preferably is realized to ethylene and propylene.The mixture comprising hydro carbons can be prepared by this field
The mix products of the technique of lighter hydrocarbon products, such as methanol-to-olefins (MTO), preparing propylene from methanol (MTP), naphtha pyrolysis system
The product of the techniques such as ethylene, according to technology category and the difference of concrete technology condition, method of the invention is used for the packet that handles
May include C1-C10 hydro carbons, hydrogen, alcohol, ether, alkynes, cycloalkane, aromatic hydrocarbons, heterocyclic compound etc. in the mixture of hydrocarbon-containifirst.But
It is that in some embodiments, the object handled by method of the invention is also likely to be other mixing comprising ethylene or propylene
Object.In the present invention unless otherwise stated, all pressure is " absolute pressure ".
As shown in Figure 1, the present invention provides a kind of absorption tower T-06 for absorption and separation ethylene, which includes upper
Lower two sections, hypomere is primarily absorption section, and epimere is auxiliary absorber portion.In operation, including the mixture of ethylene is from absorption tower
Bottom enter in absorption tower, contacted with main absorbent while moving upwardly through main absorber portion, to main absorbent will
Ethylene absorption in the mixture.The material after ethylene is absorbed to continue to ascend into assist absorption section, wherein with it is auxiliary
Absorbefacient contacts so that main absorbent wherein included is absorbed by the auxiliary absorbent.Including ethylene, absorbent and auxiliary are inhaled
The absorption tower reactor logistics delivery of agent is received to the treatment process in downstream.In the embodiment shown in figure 1, it inputs in the absorption tower
Including the mixture of ethylene is demethanation overhead stream, and tower reactor logistics delivery is absorbed to high pressure depropanizer T-01A.But
In other embodiments of the present invention, the absorption tower can be connected with other equipment, be used for from others including ethylene
Mixture in recycle ethylene, and using the ethylene being recovered to as absorbing tower reactor logistics delivery to other techniques.
In an embodiment of the invention, the main absorbent is selected from least one of following substance：C3, C4 and
C5+ hydro carbons.The auxiliary absorbent is selected from least one of following substance：C2 hydrocarbon and C3 hydrocarbon, preferably in ethane and propane
At least one.The main absorbent and auxiliary absorbent of the present invention can be mutually the same either different from each other.At this
In one embodiment of invention, the main absorbent is different from the auxiliary absorbent, specifically, when the main absorbent
When the mixture for C3 hydrocarbon or comprising C3 hydrocarbon, the auxiliary absorbent is free of C3 hydrocarbon.Another embodiment party according to the present invention
Formula, the main absorbent and the auxiliary absorbent can be C3 hydrocarbon.Main absorbent as used in the present invention and auxiliary are inhaled
It can be provided by least one of system residing for the absorption tower other equipment to receive at least part in agent.Example
Such as in the embodiment of following figure 2-4, provides C3, C4 or C5+ hydrocarbon by knockout tower different in entire hydrocarbon mixture separation system and make
For main absorbent.
In an embodiment of the invention, 1-3 charge air cooler is set in the main absorber portion on the absorption tower.Charge air cooler
Heat-exchange device known in the art, by the main absorber portion in absorption tower a part of material draw, in the charge air cooler into
Row cooling, is preferably cooled to -55 DEG C to -10 DEG C, then material after cooling is back in main absorber portion again, in the present invention
In, the material of cold tower is known as the material of the extraction of cold tower " in " during this part is flowed through.In an embodiment of the invention, institute
The amount for stating the material of charge air cooler extraction accounts for the 10-80 weight %, preferably 15-75 weight % of mass flow in tower.The present invention's
In one embodiment, refrigeration effect is provided using propylene refrigerant in the charge air cooler.In an embodiment of the invention
Propylene refrigerant is only used, is provided by propylene refrigeration compressor, the temperature of propylene refrigerant is respectively 7 DEG C, -24 DEG C and -40 DEG C.
In an embodiment of the invention, the absorption tower is plate column or packed tower, preferably plate column.At this
In the another embodiment of invention, the absorption tower is plate column, wherein assist absorption section and assist absorption section and main absorption
The ratio between section number of plates is 0.1~0.5:1, the assist absorption section number of plates is 5~30, and the ratio between tower diameter is 0.1~0.8:1.
In yet another embodiment of the present invention, the feeding temperature of the main absorbent is -60 DEG C to -10 DEG C, preferably
It it is -40 DEG C to -10 DEG C, preferably -40 DEG C to -20 DEG C, the feeding temperature of the auxiliary absorbent is -60 DEG C to -10 DEG C, preferably
It is -40 DEG C to -10 DEG C, preferably -40 DEG C to -20 DEG C.In yet another embodiment of the present invention, the pressure in absorption tower is
10-50 bars, preferably 15-40 bars, more preferable 25-35 bars.
The present invention also provides a kind of method detached to the mixture comprising hydro carbons, the mixing for including hydro carbons
Object can be the arbitrary technique for preparing hydrocarbon product, such as the product of the techniques such as naphtha pyrolysis ethylene, MTO, MTP,
It wherein include following components：C1 hydrocarbon, C2 hydrocarbon, C3 hydrocarbon；The mixture comprising hydro carbons also optionally includes following optional components
In it is one or more：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, C7 hydrocarbon, C8 hydrocarbon, C9 hydrocarbon, C10 hydrocarbon, alcohol, ether, alkynes；Preferably, described
Including the mixture of hydro carbons also optionally includes one or more in following optional components：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, first
Alcohol, dimethyl ether, acetylene, propine；It is highly preferred that the mixture comprising hydro carbons also optionally includes in following optional components
It is one or more：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, methanol, dimethyl ether.
This method includes the steps that the above-described separation ethylene in absorption tower.An embodiment party according to the present invention
Formula can optionally be provided with one or more condensers, temperature detection before and after each tower as described below and within tower
Device, temperature controller, pressure detector, pressure controller, purifier etc..As in Figure 2-4, the method includes following steps
Suddenly：
(1) mixture comprising hydro carbons optionally carries out pretreatment and squeeze operation first.The pretreatment can be with
It is the operation for removing arbitrary solid particle or by-product in the mixture, such as solvent adsorption, depickling, dealkalize, desulfurization, solid
The operations such as body particle removal.The squeeze operation can be carried out using the pump of this field routine or compressor.By pretreatment
Lock out operation is carried out in high pressure depropanizer T-01A first with the mixture comprising hydro carbons after squeeze operation, obtains height
Pressure-off propane overhead stream and high pressure depropanizer kettle logistics, wherein high pressure depropanizer top logistics be equal to without carbon number or
Hydrocarbon more than four, the high pressure depropanizer kettle logistics are equal to or less than two hydrocarbon without carbon number, are achieved in C2 hydrocarbon and C4 hydrocarbon
Clear segmentation.High pressure depropanizer top logistics delivery is to subsequent domethanizing column and dethanizer, and high pressure depropanization
Tower reactor logistics delivery is to low pressure depropanizer.
An advantage of the present invention is that the C3 hydrocarbon of at least 60 weight % does not pass through in the mixture comprising hydro carbons
The processing of domethanizing column and dethanizer, in other words, with the total weight of C3 hydrocarbon in the mixture comprising hydro carbons, conveying
Amount to the C3 for including in the high pressure depropanizer top logistics of subsequent domethanizing column and dethanizer is less than 40 weight %.
In an embodiment of the invention, the bottom temperature of the high pressure depropanizer be 40-60 DEG C, tower top temperature be -5 DEG C extremely
15 DEG C, pressure is 10-15 bars, number of plates 35-60.According to embodiment of the present invention, high pressure depropanizer T-01A without
Overhead condenser, tower overhead gas condense after being compressed into the fourth stage, and lime set returning part liquid phase is as reflux.
(2) the high pressure depropanizer kettle logistics carries out lock out operation in low pressure depropanizer T-01B, and it is de- to obtain low pressure
Propane overhead stream and low pressure depropanizer kettle logistics, wherein low pressure depropanizer top logistics, which includes carbon number, is equal to three
Hydrocarbon, the hydrocarbon without being equal to or more than four containing carbon number, the low pressure depropanizer kettle logistics include the hydrocarbon that carbon number is equal to or more than four,
Hydrocarbon without being less than four containing carbon number, is achieved in the clear segmentation of C3 and C4+.In an embodiment of the invention, described
The bottom temperature of low pressure depropanizer is 60-80 DEG C, and tower top temperature is 0-15 DEG C, and pressure is 5-9 bars, number of plates 30-50.
(3) high pressure depropanizer top logistics optionally through the fourth stage be compressed to pressure be 25-35 bars, optionally into
Row hydrogenation and removing alkynes is condensed with cooling, and then a part is conveyed as overhead reflux returns to the high pressure depropanizer, one
Divide and be delivered to domethanizing column T-02 progress lock out operation, obtains demethanation overhead stream and demethanation tower reactor logistics, the piptonychia
Alkane overhead stream includes C1 hydrocarbon, C2 hydrocarbon and optional hydrogen, and the demethanation tower reactor logistics includes C2 hydrocarbon and C3 hydrocarbon.The piptonychia
Not higher than 100ppm (weight ratio), tower top temperature is not less than -40 DEG C for methane content control in the tower reactor logistics of alkane tower.According to
The bottom temperature of an embodiment of the invention, the domethanizing column is 0-20 DEG C, and tower top temperature is -40 DEG C to -20 DEG C, pressure
Power is 25-35 bars, number of plates 40-70.
(4) the demethanation tower reactor logistics carries out lock out operation in dethanizer T-03, obtains deethanization overhead stream
With deethanization tower reactor logistics, the deethanization overhead stream includes C2 hydrocarbon, and the deethanization tower reactor logistics includes C3 hydrocarbon, thus real
The clear segmentation of existing C2 and C3.According to embodiment of the present invention, in deethanization overhead stream and deethanization tower reactor logistics
Any one or two kinds be optionally delivered to absorber with making main absorbent or auxiliary absorbent.It is described according to the present invention
The bottom temperature of one embodiment, the dethanizer is 40-60 DEG C, and tower top temperature is -40 DEG C to -15 DEG C, pressure 17-
24 bars, number of plates 40-70.
(5) the deethanization overhead stream carries out lock out operation in ethylene rectifying column T-04, the ethane detached and
Ethylene.When the auxiliary absorbent in absorption tower is the mixture of ethane or ethane and propane, optionally ethane is conveyed
To absorption tower as auxiliary absorbent.The deethanization tower reactor logistics carries out lock out operation in propylene rectification tower T-05, obtains
The propane and propylene of separation.When the auxiliary absorbent in absorption tower is the mixture of propane or ethane and propane, optionally
Ground is using delivery of propane to absorption tower as auxiliary absorbent.According to embodiment of the present invention, the ethylene rectifying column
Bottom temperature be -20-0 DEG C, tower top temperature be -40 to -30 DEG C, pressure be 11-18 bars, preferably 13-17 bars, number of plates 60-
90.According to embodiment of the present invention, the bottom temperature of the propylene rectification tower be 40-80 DEG C, preferably 45-65 DEG C, tower
It is 35-50 DEG C to push up temperature, and preferably 35-45 DEG C, pressure is 15-20 bars.
(6) in the embodiment shown in Fig. 2-4, the overhead stream of domethanizing column T-02 includes mainly hydrogen, CH4With
C2H4, enter absorption tower T-06 from the entrance of absorb the bottom of the tower, the absorption tower as described above in conjunction with fig. 1, includes the master of lower part
The assist absorption section of absorber portion and top, in the main absorber portion so that main absorbent is contacted with the mixture, thus will
Ethylene is detached from the demethanation overhead stream, in the assist absorption section so that auxiliary absorbent and the demethanation
Overhead stream contacts, and recycles main absorbent from the demethanation overhead stream, includes the main absorbent and assist absorption of ethylene
Agent is discharged as tower reactor logistics is absorbed from absorb the bottom of the tower, is delivered to the high pressure depropanizer or domethanizing column (when using C3
When hydrocarbon is as main absorbent), and the demethanation overhead stream after ethylene is detached as absorbing tower top tail gas at the top of absorption tower
Discharge, is delivered to gas ductwork.The main absorbent is selected from any one or more of following hydro carbons：C3 hydro carbons, C4 hydro carbons, C5
+ hydrocarbon (preferably C5-C8 hydro carbons)；The auxiliary absorbent is selected from any one or more of following hydro carbons：C2 hydro carbons, C3 hydro carbons,
It is preferred that at least one of ethane and propane；And the type of the main absorbent is different from the auxiliary absorbent.
(7) the overhead stream part conveying that the low pressure depropanizer T-01B tower tops come out is back to the high pressure-off
Propane tower T-01A, a part are delivered to propane and propylene that the propylene rectification tower T-05 carries out isolated separation, work as absorption
When C3 hydrocarbon is used in tower T-06 as main absorbent or auxiliary absorbent, a part of low pressure depropanizer top logistics is appointed
Selection of land is delivered to the absorption tower.According to embodiment of the present invention, with the gross weight of low pressure depropanizer top logistics
It is counted on the basis of amount, the ratio for being delivered to high pressure depropanizer T-01A is 0-50 weight %, preferably 5-40 weight %, more preferable 10-
The low pressure depropanizer top logistics delivery of 30 weight % returns to the high pressure depropanizer；50-80 weight %, preferably 50-
The low pressure depropanizer top logistics delivery of 60 weight % is to the propylene rectification tower；10-40 weight %, preferably 20-30 weights
The low pressure depropanizer top logistics delivery of % is measured to the main absorber portion on absorption tower.According to embodiment of the present invention,
It is counted on the basis of the total weight of low pressure depropanizer top logistics, low pressure depropanizer top logistics includes at least 99.5 weights
Measure the C3 hydrocarbon of %.
(8) the low pressure depropanizer kettle logistics includes C4+ the hydrocarbon components, is delivered to debutanizing tower and carries out lock out operation, obtains
To debutanization overhead stream and debutanization tower reactor logistics, the debutanization overhead stream includes C4 hydrocarbon, the deethanization tower reactor object
Stream is equal to or more than five hydrocarbon comprising carbon number, is achieved in the clear segmentation of C4 and C5+.An embodiment party according to the present invention
The bottom temperature of formula, the debutanizing tower is 90-120 DEG C, and tower top temperature is 38-50 DEG C, and pressure is 3-6 bars, number of plates 40-
55。
Fig. 2 of the present invention shows that the C3+ using the logistics of low pressure depropanizer top is delivered to absorption tower as absorbent, Fig. 3
It shows and the C4 hydrocarbon of debutanization overhead stream is delivered to absorption tower as absorbent, Fig. 4 is shown debutanizing tower bottoms stream
C5+ hydrocarbon be delivered to absorption tower as absorbent.It should be understood that the Matter Transfer of the present invention is not limited only to this, it is real
On border, the present invention can be considered is delivered to absorption tower as main absorbent or auxiliary suction using the arbitrary C2-C5+ hydrocarbon materials of each tower
Receive agent.
Embodiment
Fig. 2 of the present invention to embodiment shown in Fig. 4 is further described with the following Examples.
Embodiment 1
Reaction system shown in flow chart of the present embodiment using Fig. 2.Domethanizing column T-02 overhead materials are streamed to absorption tower
T-06 recycles the C being wherein rich in2H4, absorption tower is divided into two sections, and the main absorber portion of hypomere is low pressure depropanizer T-01B
The C3 of tower top is as main absorbent, -37 DEG C of feeding temperature, the main absorber portion number of plates 30；Epimere be auxiliary absorber portion, with from
The ethane and propane of ethylene rectifying column and propylene rectification tower are as auxiliary absorbent, -37 DEG C of feeding temperature, assist absorption section tower
Plate number 10.Gas flow 2570kg/hr from T-02 tower tops, -37 DEG C of temperature.Charge air cooler E-05 quantity is 1, from the 22nd plate
Extraction, is back to the 20th plate, produced quantity 720kg/hr, using -40 DEG C of propylene refrigerants.The tower top tail gas of absorption tower T-06 passes through
It throttles and is sent to fuel gas pipe network after recycling cold, tower reactor absorbing liquid is sent to high pressure depropanizer T-01A.Concrete operations parameter is shown in
Table 1.
1 embodiment of table, 1 operating parameter
| Bottom temperature/DEG C | Tower reactor pressure/bar | Tower top temperature/DEG C | Tower top pressure/bar | |
| T-01A | 51.6 | 14.5 | 3.5 | 13.1 |
| T-01B | 71.4 | 8.0 | 8.9 | 7.5 |
| T-02 | 26.1 | 33.5 | -37.0 | 33.0 |
| T-03 | 54.6 | 22.5 | -23.1 | 22.0 |
| T-04 | -16.4 | 16.0 | -38.0 | 15.5 |
| T-05 | 54.3 | 19.1 | 43.8 | 18.0 |
| T-06 | -14.5 | 32.5 | -34.5 | 32.0 |
| T-07 | 101.2 | 5.0 | 41.7 | 4.5 |
The logistics that 01 to 17 place of number in figure is measured using gas chromatographic measurement instrument is formed, and composition and flow everywhere are shown in Table
2, ethylene product, propylene product and four purity of carbon obtained as main absorbent using C3 be respectively 99.98wt.%,
99.7wt.% and 99.6wt.%, the rate of recovery are respectively 99.98%, 99.93% and 99.58%.62% C3 does not pass through
Domethanizing column and dethanizer, directly by being sent at the top of low pressure depropanizer to propylene rectification tower, energy consumption significantly reduces.
2 embodiment of table, 1 operating parameter and result
Embodiment 2
Reaction system shown in flow chart of the present embodiment using Fig. 3.Domethanizing column T-02 overhead materials are streamed to absorption tower
T-06 recycles the C being wherein rich in2H4, absorption tower is divided into two sections, and the main absorber portion of hypomere is debutanizing tower T-07 tower tops
C4 is as main absorbent, -37 DEG C of feeding temperature, the main absorber portion number of plates 30；Epimere assist absorption section comes from ethylene distillation
The ethane and propane of tower T-04 and propylene rectification tower T-05 are as auxiliary absorbent, -37 DEG C of feeding temperature, assist absorption section tower
Plate number 10.Gas flow 2662kg/hr from T-02 tower tops, -37 DEG C of temperature.Charge air cooler E-05 quantity is 1, from the 22nd plate
Extraction, is back to the 20th plate, produced quantity 720kg/hr, using -40 DEG C of propylene refrigerants.The tower top tail gas on absorption tower is through throttling
And given to fuel gas pipe network after recycling cold, tower reactor absorbing liquid is sent to high pressure depropanizer T-01A.Concrete operations parameter is shown in Table 3.
3 embodiment of table, 2 operating parameter
| Bottom temperature/DEG C | Tower reactor pressure/bar | Tower top temperature/DEG C | Tower top pressure/bar | |
| T-01A | 50.2 | 14.5 | 6.1 | 13.1 |
| T-01B | 78.2 | 8.0 | 9.2 | 7.5 |
| T-02 | 26.5 | 33.5 | -37 | 33.0 |
| T-03 | 54.6 | 22.5 | -23.1 | 22.0 |
| T-04 | -18.4 | 16.0 | -37.5 | 15.5 |
| T-05 | 54.3 | 19.1 | 43.8 | 18.0 |
| T-06 | 2.5 | 32.5 | -32.5 | 32.0 |
| T-07 | 103.2 | 5.0 | 43.6 | 4.5 |
The carrying out practically parameter of embodiment 2 is shown in Table 4, the ethylene product that is obtained as main absorbent using C4, propylene product
It is respectively 99.98wt.%, 99.7wt.% and 99.6wt.% with four purity of carbon, the rate of recovery is respectively 99.97%, 99.90%
With 99.60%.66% C3 does not pass through domethanizing column and dethanizer, directly by being sent at the top of low pressure depropanizer to propylene essence
Tower is evaporated, energy consumption significantly reduces.
4 embodiment of table, 2 operating parameter and result
Embodiment 3
Reaction system shown in flow chart of the present embodiment using Fig. 4.Domethanizing column T-02 overhead materials are streamed to absorption tower
T-06 recycles the C being wherein rich in2H4, absorption tower is divided into two sections, and the main absorber portion of hypomere is debutanizing tower T-07 tower reactors
C5+ is as main absorbent, -37 DEG C of feeding temperature, the main absorber portion number of plates 35；Epimere assist absorption section comes from ethylene essence
Evaporate tower and propylene rectification tower ethane and propane as auxiliary absorbent, -37 DEG C of feeding temperature, the assist absorption section number of plates 10
Block.Gas flow 2363kg/hr from T-02 tower tops, -37 DEG C of temperature.Charge air cooler E-05 quantity is 1, is produced from the 22nd plate,
It is back to the 20th plate, produced quantity 720kg/hr, using -40 DEG C of propylene refrigerants.The tower top tail gas of absorption tower T-06 is through throttling simultaneously
It is sent to fuel gas pipe network after recycling cold, tower reactor absorbing liquid is sent to high pressure depropanizer T-07.Concrete operations parameter is shown in Table 5.
5 embodiment of table, 3 operating parameter
| Bottom temperature/DEG C | Tower reactor pressure/bar | Tower top temperature/DEG C | Tower top pressure/bar | |
| T-01A | 51.0 | 14.5 | 5.1 | 13.1 |
| T-01B | 65.8 | 8.0 | 8.8 | 7.5 |
| T-02 | 29.8 | 33.5 | -37.5 | 33.0 |
| T-03 | 51.5 | 22.5 | -23.1 | 22.0 |
| T-04 | -16.8 | 16.0 | -38.5 | 15.5 |
| T-05 | 54.3 | 19.1 | 43.8 | 18.0 |
| T-06 | 8.5 | 32.5 | -33.5 | 32.0 |
| T-07 | 105.8 | 5.1 | 45.4 | 4.5 |
The carrying out practically parameter of embodiment 3 is shown in Table 6, and ethylene product, the propylene obtained as main absorbent using C5+ is produced
Product and four purity of carbon are respectively 99.98wt.%, 99.7wt.% and 99.1wt.%, the rate of recovery is respectively 99.99%,
99.90% and 99.86%.63% C3 does not pass through domethanizing column and dethanizer, directly by being sent at the top of low pressure depropanizer
To propylene rectification tower, energy consumption significantly reduces.
6 embodiment of table, 3 operating parameter and result
Compared with prior art, the present invention does not have deep cooling ice chest and special absorptive agent desorber, and propylene refrigerant is used only.It adopts
99.96wt.% is reached with the ethylene product purity that this method obtains, Recovery rate of ethylene is more than 99.97%, and propylene product purity reaches
99.7wt.%, the rate of recovery are more than 99.88%, the C4+ rate of recovery and are more than 99.6%；C3 more than 60% does not pass through domethanizing column
And dethanizer, directly by being sent at the top of low pressure depropanizer to propylene rectification tower, energy consumption significantly reduces.The present invention has investment
Less, low energy consumption, material recovery rate is high, many advantages easy to operate and stable etc., is particularly suitable for product distribution weighting
Alkene production technology.
Claims (22)
1. a kind of method for being used for recycling ethylene from the mixture comprising ethylene, this method include：
The mixture comprising ethylene is set to enter absorption tower from the entrance of absorb the bottom of the tower, with the mixture for including ethylene
Total weight on the basis of count, in the mixture comprising ethylene the content of ethylene is 50-80 weight %, described comprising ethylene
One or more substance selected from the following is additionally comprised in mixture：Hydrogen, methane, ethane, ethylene, propylene, propane, fourth
Alkene, butane, amylene, pentane, hexene, hexane, ether, alcohol；
The absorption tower includes the main absorber portion of lower part and the assist absorption section on top, in the main absorber portion so that main suction
It receives agent to contact with the mixture, to detach ethylene from the mixture, in the assist absorption section so that auxiliary
Absorbent is contacted with the mixture, and main absorbent is recycled from the mixture；
Including the main absorbent and auxiliary absorbent of ethylene are discharged from absorb the bottom of the tower, and the mixture after ethylene is detached from suction
Receive top of tower discharge；
The main absorbent is selected from any one or more of following hydro carbons：C3 hydro carbons, C4 hydro carbons, C5-C8 hydro carbons；
The auxiliary absorbent is selected from any one or more of following hydro carbons：C2 hydro carbons, C3 hydro carbons；
The main absorbent and auxiliary absorbent are different from each other.
2. the method as described in claim 1, which is characterized in that the main absorbent in following hydro carbons any one or
It is a variety of：C3 hydro carbons, C4 hydro carbons and C5 hydro carbons；
The auxiliary absorbent is selected from the one or more of following components：Ethane and propane.
3. the method as described in claim 1, which is characterized in that the main absorbent in following hydro carbons any one or
It is a variety of：C3 hydro carbons and C4 hydro carbons；
The auxiliary absorbent is selected from the one or more of following components：Ethane and propane.
4. the method as described in claim 1, which is characterized in that the main absorbent in following hydro carbons any one or
It is a variety of：Propane, propylene, butane, butylene, pentane and amylene；
The auxiliary absorbent is selected from the one or more of following components：Ethane and propane.
5. the method as described in claim 1, which is characterized in that on the basis of the total weight of the mixture comprising ethylene
It counts, the content of ethylene is 50-70 weight % in the mixture comprising ethylene；
One or more substance selected from the following is additionally comprised in the mixture comprising ethylene：Hydrogen, methane, ethane,
Ethylene, propylene, propane, butylene, butane.
6. the method as described in claim 1, which is characterized in that on the basis of the total weight of the mixture comprising ethylene
It counts, the content of ethylene is 50-65 weight % in the mixture comprising ethylene；
One or more substance selected from the following is additionally comprised in the mixture comprising ethylene：Hydrogen, methane, ethane,
Ethylene, propylene, propane.
7. the method as described in claim 1, which is characterized in that on the basis of the total weight of the mixture comprising ethylene
It counts, the content of ethylene is 50-60 weight % in the mixture comprising ethylene；
One or more substance selected from the following is additionally comprised in the mixture comprising ethylene：Methane, ethane, ethylene,
Propylene, propane.
8. the method as described in claim 1, which is characterized in that the tower diameter of the assist absorption Duan Yuzhu absorber portions on the absorption tower
The ratio between be 0.1~0.8:1, the absorption tower is plate column or packed tower；
When the absorption tower is plate column, the ratio between number of plates of the assist absorption section and main absorber portion is 0.1~0.5:1,
Wherein the number of plates of assist absorption section is 5~30.
9. the method as described in claim 1, which is characterized in that
The main absorber portion is provided with 1-3 charge air cooler, the charge air cooler produces a part of material from the main absorber portion,
The temperature of the material is reduced, then returns it to the main absorber portion again, using the material total flow in the absorption tower as base
The ratio of quasi- meter, the material of extraction accounts for 10-80%, and the cooling temperature of the charge air cooler is -40 DEG C~-10 DEG C.
10. the method as described in claim 1, which is characterized in that the entering from absorb the bottom of the tower of the mixture comprising ethylene
Temperature when mouth enters absorption tower is -40 DEG C~-10 DEG C；Temperature when the main absorbent enters the absorption tower is -40
DEG C~-10 DEG C；The temperature when auxiliary absorbent enters the absorption tower is -40 DEG C~-10 DEG C；
Pressure in absorption tower is 10-50 bars.
11. the method as described in claim 1, which is characterized in that the entering from absorb the bottom of the tower of the mixture comprising ethylene
Temperature when mouth enters absorption tower is -40 DEG C~-20 DEG C；Temperature when the main absorbent enters the absorption tower is -40
DEG C~-20 DEG C；The temperature when auxiliary absorbent enters the absorption tower is -40 DEG C~-20 DEG C；
Pressure in absorption tower is 15-40 bars.
12. the method as described in claim 1, which is characterized in that the entering from absorb the bottom of the tower of the mixture comprising ethylene
Temperature when mouth enters absorption tower is -40 DEG C~-20 DEG C；Temperature when the main absorbent enters the absorption tower is -40
DEG C~-20 DEG C；The temperature when auxiliary absorbent enters the absorption tower is -40 DEG C~-20 DEG C；
Pressure in absorption tower is 25-35 bars.
13. a kind of method detached to the mixture comprising hydro carbons, the mixture comprising hydro carbons includes following components：
C1 hydrocarbon, C2 hydrocarbon, C3 hydrocarbon；
The mixture comprising hydro carbons also optionally includes one or more in following optional components：Hydrogen, C4 hydrocarbon, C5
Hydrocarbon, C6 hydrocarbon, C7 hydrocarbon, C8 hydrocarbon, C9 hydrocarbon, C10 hydrocarbon, alcohol, ether, alkynes；
It the described method comprises the following steps：
(1) mixture comprising hydro carbons carries out lock out operation in high pressure depropanizer, obtains high pressure depropanizer top object
Stream and high pressure depropanizer kettle logistics, wherein high pressure depropanizer top logistics is equal to or more than four hydrocarbon, institute without carbon number
State the hydrocarbon that high pressure depropanizer kettle logistics is equal to or less than two without carbon number；
(2) the high pressure depropanizer kettle logistics carries out lock out operation in low pressure depropanizer, obtains low pressure depropanizer top
Logistics and low pressure depropanizer kettle logistics, wherein low pressure depropanizer top logistics includes the hydrocarbon that carbon number is equal to three, it is described low
Pressure-off propane tower reactor logistics includes the hydrocarbon that carbon number is equal to or more than four；
(3) high pressure depropanizer top logistics optionally carries out hydrogenation and removing alkynes and cooling condenses, then part conveying
The high pressure depropanizer is returned to, a part is delivered to domethanizing column and carries out lock out operation, obtains demethanation overhead stream and takes off
Methane tower reactor logistics, the demethanation overhead stream include C1 hydrocarbon, C2 hydrocarbon and optional hydrogen, the demethanation tower reactor logistics packet
Hydrocarbon containing C2 and C3 hydrocarbon；
(4) the demethanation tower reactor logistics carries out lock out operation in dethanizer, obtains deethanization overhead stream and deethanization
Tower reactor logistics, the deethanization overhead stream include C2 hydrocarbon, and the deethanization tower reactor logistics includes C3 hydrocarbon；
(5) the deethanization overhead stream carries out lock out operation in ethylene rectifying column, the ethane and ethylene detached, optionally
Ethane is delivered to absorption tower as auxiliary absorbent by ground；The deethanization tower reactor logistics carries out separation behaviour in propylene rectification tower
Make, the propane and propylene detached, optionally using delivery of propane to absorption tower as auxiliary absorbent；
(6) demethanation overhead stream enters absorption tower from the entrance of absorb the bottom of the tower, and the absorption tower includes the main absorption of lower part
The assist absorption section of section and top, in the main absorber portion so that main absorbent is contacted with the mixture, thus by ethylene
It is detached from the demethanation overhead stream, in the assist absorption section so that auxiliary absorbent and the demethanation tower top
Logistics contacts, and main absorbent is recycled from the demethanation overhead stream, including the main absorbent and auxiliary absorbent of ethylene are made
Be absorb tower reactor logistics from absorb the bottom of the tower be discharged, be delivered to the high pressure depropanizer or domethanizing column, and detach ethylene it
Demethanation overhead stream afterwards is delivered to gas ductwork as the discharge at the top of absorption tower of tower top tail gas is absorbed；The main absorption
Agent is selected from any one or more of following hydro carbons：C3 hydro carbons, C4 hydro carbons, C5-C8 hydro carbons；The auxiliary absorbent is selected from following
Any one or more of hydro carbons：C2 hydro carbons, C3 hydro carbons；
(7) the low pressure depropanizer top logistics part conveying is back to the high pressure depropanizer, and a part is delivered to institute
Propane and propylene that propylene rectification tower carries out isolated separation are stated, a part is optionally delivered to the absorption tower as main suction
Receive agent or auxiliary absorbent；
(8) the low pressure depropanizer kettle logistics delivery to debutanizing tower carries out lock out operation, obtains debutanization overhead materials
Stream and debutanization tower reactor logistics, the debutanization overhead stream include C4 hydrocarbon, and the deethanization tower reactor logistics is equal to comprising carbon number
Or the hydrocarbon more than five, one or both of the debutanization overhead stream and debutanization tower reactor logistics are optionally delivered to institute
Absorption tower is stated as main absorbent；
The main absorbent and auxiliary absorbent are different from each other.
14. method as claimed in claim 13, which is characterized in that the mixture comprising hydro carbons also optionally includes following
It is one or more in optional components：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, methanol, dimethyl ether, acetylene, propine.
15. method as claimed in claim 13, which is characterized in that the mixture comprising hydro carbons also optionally includes following
It is one or more in optional components：Hydrogen, C4 hydrocarbon, C5 hydrocarbon, C6 hydrocarbon, methanol, dimethyl ether.
16. method as claimed in claim 13, which is characterized in that in the step (1), with the mixing for including hydro carbons
It is counted on the basis of the total weight of C3 hydrocarbon in object, the C3 hydrocarbon of at least 60 weight % enters high pressure depropanizer kettle logistics.
17. method as claimed in claim 13, which is characterized in that in step (2), with low pressure depropanizer top logistics
Total weight on the basis of count, low pressure depropanizer top logistics includes at least C3 hydrocarbon of 99.5 weight %；
It in step (7), is counted on the basis of the total weight of low pressure depropanizer top logistics, the low pressure of 0-50 weight %
Depropanization tower top logistics delivery returns to the high pressure depropanizer；The low pressure depropanizer top logistics of 50-80 weight % is defeated
It send to the propylene rectification tower；The low pressure depropanizer top logistics delivery of 10-40 weight % to absorption tower main absorber portion；
In step (4), optionally by the main absorption of at least part deethanization tower reactor logistics delivery to the absorption tower
The main absorbents of Duan Zuowei.
18. method as claimed in claim 13, which is characterized in that in step (2), with low pressure depropanizer top logistics
Total weight on the basis of count, low pressure depropanizer top logistics includes at least C3 hydrocarbon of 99.5 weight %；
It in step (7), is counted on the basis of the total weight of low pressure depropanizer top logistics, the low pressure of 5-40 weight %
Depropanization tower top logistics delivery returns to the high pressure depropanizer；The low pressure depropanizer top logistics of 50-60 weight % is defeated
It send to the propylene rectification tower；The low pressure depropanizer top logistics delivery of 20-30 weight % to absorption tower main absorber portion；
In step (4), optionally by the main absorption of at least part deethanization tower reactor logistics delivery to the absorption tower
The main absorbents of Duan Zuowei.
19. method as claimed in claim 13, which is characterized in that in step (2), with low pressure depropanizer top logistics
Total weight on the basis of count, low pressure depropanizer top logistics includes at least C3 hydrocarbon of 99.5 weight %；
It in step (7), is counted on the basis of the total weight of low pressure depropanizer top logistics, 10-30 weight %'s is described low
The conveying of pressure-off propane overhead stream returns to the high pressure depropanizer；The low pressure depropanizer top logistics of 50-60 weight %
It is delivered to the propylene rectification tower；The low pressure depropanizer top logistics delivery of 20-30 weight % to absorption tower main absorption
Section；
In step (4), optionally by the main absorption of at least part deethanization tower reactor logistics delivery to the absorption tower
The main absorbents of Duan Zuowei.
20. method as claimed in claim 13, which is characterized in that
(1) bottom temperature of the high pressure depropanizer is 40-60 DEG C, and tower top temperature is -5 DEG C to 15 DEG C, pressure 10-15
Bar, number of plates 35-60；
(2) bottom temperature of the low pressure depropanizer is 60-90 DEG C, and tower top temperature is 0-15 DEG C, and pressure is 5-9 bars, column plate
Number is 30-50；
(3) bottom temperature of the domethanizing column is 0-20 DEG C, and tower top temperature is -40 DEG C to -20 DEG C, and pressure is 25-35 bars, tower
Plate number is 40-70；
(4) bottom temperature of the dethanizer is 40-60 DEG C, and tower top temperature is -40 DEG C to -15 DEG C, and pressure is 17-24 bars,
Number of plates 40-70；
(5) bottom temperature of the ethylene rectifying column is 0-20 DEG C, and tower top temperature is -40 to -34 DEG C, and pressure is 11-17 bars, tower
Plate number 60-90；The bottom temperature of the propylene rectification tower is 40-80 DEG C, and tower top temperature is 35-50 DEG C, and pressure is 15-20 bars,
For Double-Tower Structure；
(6) bottom temperature on the absorption tower is -40 DEG C~-20 DEG C, and pressure is 10-50 bars；
(7) bottom temperature of the debutanizing tower is 90-120 DEG C, and tower top temperature is 38-45 DEG C, and pressure is 3-6 bars, the number of plates
40-55。
21. method as claimed in claim 13, which is characterized in that
(1) bottom temperature of the high pressure depropanizer is 40-60 DEG C, and tower top temperature is -5 DEG C to 15 DEG C, pressure 10-15
Bar, number of plates 35-60；
(2) bottom temperature of the low pressure depropanizer is 60-90 DEG C, and tower top temperature is 0-15 DEG C, and pressure is 5-9 bars, column plate
Number is 30-50；
(3) bottom temperature of the domethanizing column is 0-20 DEG C, and tower top temperature is -40 DEG C to -20 DEG C, and pressure is 25-35 bars, tower
Plate number is 40-70；
(4) bottom temperature of the dethanizer is 40-60 DEG C, and tower top temperature is -40 DEG C to -15 DEG C, and pressure is 17-24 bars,
Number of plates 40-70；
(5) bottom temperature of the ethylene rectifying column is 0-20 DEG C, and tower top temperature is -40 to -34 DEG C, and pressure is 11-17 bars, tower
Plate number 60-90；The bottom temperature of the propylene rectification tower is 40-80 DEG C, and tower top temperature is 35-50 DEG C, and pressure is 15-20 bars,
For Double-Tower Structure；
(6) bottom temperature on the absorption tower is -40 DEG C~-30 DEG C, and pressure is 15-40 bars；
(7) bottom temperature of the debutanizing tower is 90-120 DEG C, and tower top temperature is 38-45 DEG C, and pressure is 3-6 bars, the number of plates
40-55。
22. method as claimed in claim 13, which is characterized in that
(1) bottom temperature of the high pressure depropanizer is 40-60 DEG C, and tower top temperature is -5 DEG C to 15 DEG C, pressure 10-15
Bar, number of plates 35-60；
(2) bottom temperature of the low pressure depropanizer is 60-90 DEG C, and tower top temperature is 0-15 DEG C, and pressure is 5-9 bars, column plate
Number is 30-50；
(3) bottom temperature of the domethanizing column is 0-20 DEG C, and tower top temperature is -40 DEG C to -20 DEG C, and pressure is 25-35 bars, tower
Plate number is 40-70；
(4) bottom temperature of the dethanizer is 40-60 DEG C, and tower top temperature is -40 DEG C to -15 DEG C, and pressure is 17-24 bars,
Number of plates 40-70；
(5) bottom temperature of the ethylene rectifying column is 0-20 DEG C, and tower top temperature is -40 to -34 DEG C, and pressure is 11-17 bars, tower
Plate number 60-90；The bottom temperature of the propylene rectification tower is 40-80 DEG C, and tower top temperature is 35-50 DEG C, and pressure is 15-20 bars,
For Double-Tower Structure；
(6) bottom temperature on the absorption tower is -40 DEG C~-30 DEG C, and pressure is 25-35 bars；
(7) bottom temperature of the debutanizing tower is 90-120 DEG C, and tower top temperature is 38-45 DEG C, and pressure is 3-6 bars, the number of plates
40-55。
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| CN102304010A (en) * | 2011-07-11 | 2012-01-04 | 中国天辰工程有限公司 | Method for separating low carbon olefin mixed gas by rectifying and absorbing |
| CN102965143A (en) * | 2011-09-01 | 2013-03-13 | 富德（北京）能源化工有限公司 | Absorption separation method of cracking gas in low-carbon olefin preparation process |
| CN103242123A (en) * | 2012-02-10 | 2013-08-14 | 中国石油化工股份有限公司 | Method for separating low-carbon olefin gas |
| CN103333039A (en) * | 2013-05-29 | 2013-10-02 | 中建安装工程有限公司 | Lightweight alkene separation method reducing absorbent usage amount and device thereof |
| CN103787814A (en) * | 2014-01-23 | 2014-05-14 | 东华工程科技股份有限公司 | Low-hydrocarbon intercooled solvent washing separation method |
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| CN102304010A (en) * | 2011-07-11 | 2012-01-04 | 中国天辰工程有限公司 | Method for separating low carbon olefin mixed gas by rectifying and absorbing |
| CN102965143A (en) * | 2011-09-01 | 2013-03-13 | 富德（北京）能源化工有限公司 | Absorption separation method of cracking gas in low-carbon olefin preparation process |
| CN103242123A (en) * | 2012-02-10 | 2013-08-14 | 中国石油化工股份有限公司 | Method for separating low-carbon olefin gas |
| CN103333039A (en) * | 2013-05-29 | 2013-10-02 | 中建安装工程有限公司 | Lightweight alkene separation method reducing absorbent usage amount and device thereof |
| CN103787814A (en) * | 2014-01-23 | 2014-05-14 | 东华工程科技股份有限公司 | Low-hydrocarbon intercooled solvent washing separation method |
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