CN106390518B - A method of with liquid phase Simulation moving bed while adsorbing separation multiply raw material - Google Patents
A method of with liquid phase Simulation moving bed while adsorbing separation multiply raw material Download PDFInfo
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Abstract
A method of with liquid phase Simulation moving bed while adsorbing separation multiply difference constitutive material, including the liquid phase Simulation moving bed for containing n bed is divided into m adsorbing separation section, bed between two adjacent desorbing agent D decanting points is an adsorbing separation section, each adsorbing separation section fluid flow direction sequence along bed arranges, and the bed between the coupled taking-up logistics of injection logistics forms the functional areas of Simulation moving bed；Each adsorbing separation Duan Jun includes desorption area, purification section, adsorption zone and isolated area.The absorption raw material of a variety of different compositions can be injected separately into different adsorbing separation sections, while the high-purity component of isolated one or more by the method, to make full use of the processing capacity of existing Simulation moving bed.
Description
Technical field
The present invention relates to a kind of adsorption separating methods, specifically, being a kind of liquid phase Simulation moving bed adsorbing separation hydrocarbon
The method of class isomer.
Background technique
Using liquid phase Simulation moving bed (SMB) the adsorption separating method isomer minimum to boiling-point difference or have not
Separation with the component of structure feature is more effective method in the art.The method achieve liquid-solid two-phase adverse currents
Contact, improves separative efficiency.Usually there are at least three functional areas in SMB device, using more for four areas, also have
The case where a small number of five areas.Typical SMB adsorption separation process includes at least raw material F and two bursts of desorbing agent D chargings, at least wraps
E containing Extract and two bursts of raffinate R dischargings.
US2985589、US3201491、US3969223、US3626020、US3686342、US3997620、
Moving-bed adsorption separation equipment and method are disclosed in the patents such as US4006197, US4326092 and its for diformazan
The method that benzene separation, meta-xylene separation, alkene and n-alkane separate.The equipment of control material disengaging adsorption tower can be
Rotary valve is also possible to a series of switch valves.
CN201280028723.1 disclose it is a kind of by raw material and desorbing agent be equally divided into multiply logistics injection SMB absorption
The method of separator, while Extract and raffinate are also classified into multiply accordingly, functional areas are increased to 4N by 4
(N is natural number), reduces the pressure drop of adsorbent equipment with this, but its processing be same composition raw material.
US4381419 discloses the adsorption separation process using coupling two kinds of desorbing agents of lightweight and heavy, to reduce absorption point
From plant energy consumption；Lightweight and heavy desorbing agent is respectively adopted in two adsorption separation devices, and obtained Extract imports the same essence
Tower is evaporated, obtains lightweight desorbing agent by being fractionated tower top, tower bottom obtains heavy desorbing agent, and middle part obtains product.
US5093004 is disclosed using strong and weak two kinds of desorbing agents, obtains two strands of Extracts and one raffinate, by absorption point
6 regions are divided into from device, at least three kinds of components in absorption raw material are separated into three bursts of pure logistics.
Summary of the invention
The object of the present invention is to provide it is a kind of with liquid phase Simulation moving bed simultaneously adsorbing separation multiply raw material method, should
The absorption raw material of a variety of different compositions is injected separately into different adsorbing separation sections by method, can be isolated simultaneously a kind of or a kind of
Above high-purity component.
It is provided by the invention with liquid phase Simulation moving bed simultaneously adsorbing separation multiply difference constitutive material method, including
Liquid phase Simulation moving bed containing n bed is divided into m adsorbing separation section, the bed between two adjacent desorbing agent D decanting points
Layer is an adsorbing separation section, and each adsorbing separation section fluid flow direction sequence along bed arranges, and injection logistics is coupled
Taking-up logistics between bed formed Simulation moving bed functional areas；
Each adsorbing separation Duan Jun includes that desorption area, purification section, adsorption zone and isolated area, desorbing agent D are injected and extracted from liquid
Functional areas between E taking-up are desorption area, and it is purification section, raw material F note that Extract E, which takes out the functional areas between raw material F injection,
Enter raffinate R take out between functional areas be adsorption zone, raffinate R take out and desorbing agent D injection between functional areas be every
From area；
M gangs of desorbing agent D1、D2、……、DmIt is injected separately into the desorption area of each adsorbing separation section, the m stock absorption of difference composition
Separate raw material F1、F2、……、Fm, it is injected separately into the adsorption zone of each adsorbing separation section, after adsorbing separation, the group that is not adsorbed
Divide and be discharged respectively by the adsorption zone of each adsorbing separation section, is raffinate R1、R2、……、Rm, total m strands of raffinate be adsorbed component
E1、E2、……、EmIt is discharged respectively by the purification section of each adsorbing separation section,
The decanting point and off-take point of each logistics of liquid phase Simulation moving bed are every to pass through a stepping time tsSimultaneously to same
A bed is moved in one direction, and moving direction is identical as fluid flow direction in adsorbent bed, and decanting point and off-take point are along stream
Body flow direction is followed successively by D1、E1、F1、R1、D2、E2、F2、R2、……、 Dm、Em、Fm、Rm。
Liquid phase Simulation moving bed is divided into interconnected m section by the method for the present invention, and every section can be passed through different absorption originals
Material, using different desorbing agents, obtains different adsorbing separation purpose products.The method of the present invention can make full use of existing tool
There is the adsorption separation device of multiple adsorption beds, utilizes a variety of different absorption formed of adsorbing separation simultaneously of its design treatment amount
Material improves the utilization rate of device.
Detailed description of the invention
Fig. 1 is prior art adsorbing separation C8The schematic diagram of each area's injecting material of paraxylene and taking-up material in aromatic hydrocarbons.
Liquid phase Simulation moving bed is divided into m adsorbing separation section, each section of injecting material and taking-up material for the present invention by Fig. 2
Schematic diagram.
Fig. 3 is the C of the present invention two strands of different content paraxylene of adsorbing separation purification simultaneously8Pair in aromatic hydrocarbons mixture
The schematic diagram of dimethylbenzene.
Fig. 4 is the C of the present invention two strands of different components of adsorbing separation purification simultaneously8Paraxylene in aromatic hydrocarbons mixture and
The schematic diagram of ethylbenzene.
Specific embodiment
The existing bed of liquid phase Simulation moving bed is divided into multiple adsorbing separation sections, each adsorbing separation section by the method for the present invention
The absorption material that different compositions can individually be handled obtains identical or different separation purpose product, is taken off using identical or different
Attached dose.The method of the present invention can make full use of the design treatment ability of existing adsorption separation device, in adsorbing separation feedstock processing
In the case that amount is reduced, the processing capacity more than needed of original adsorption separation device is made full use of, the absorption for handling different compositions is former
Material；Absorption raw material with different content purpose product can also be each led into different adsorbing separation sections, according to raw material group
At the adsorption zone bed number of each processing section being distributed, to improve separative efficiency.
The mobile adsorbent bed of the simulation that the method for the present invention adsorption separation process uses includes one or more adsorption towers, each
Adsorption tower is divided into multiple adsorption beds by fluid collection distributor, and the function of the fluid collection distributor is: will come from upper
The logistics of one bed is redistributed to next bed, and the logistics being introduced from outside into is mixed with the logistics from a upper bed
It is even, a part in the logistics from a upper bed is drawn into adsorption tower.Fluid collection distributor allows liquid to pass through and intercept
Absorbent particles evolution is adsorbent bed, and upper and lower surface generally uses woven wire cloth, sintered metal mesh or Johnson Net
(Johnson Screen).The logistics being introduced from outside into is all logical to a certain bed, and the logistics for drawing adsorption tower from a upper bed
It crosses the pipeline being connected with the bed fluid collection distributor and enters and draw adsorption bed.
The bed number n of liquid phase Simulation moving bed of the present invention is 24~36, preferably 24, the integer that the m is 2~4,
Liquid phase Simulation moving bed is divided into 2 to 4 adsorbing separation sections.M stock desorbing agent into each adsorbing separation section can be identical or not
Together；The bed number that each adsorbing separation section is included can be the same or different；The purpose of each adsorbing separation section adsorbing separation
Product may be the same or different.
The liquid phase Simulation moving bed material decanting point and off-take point position are as follows:
In each adsorbing separation section, Extract EpOff-take point is located at desorbing agent DpDecanting point and raw material FpIt is former between decanting point
Expect FpDecanting point, Extract EpOff-take point, desorbing agent DpIt is continuous between decanting point three；
Raw material FpDecanting point is located at Extract EpOff-take point and raffinate RpBetween off-take point, Extract EpOff-take point, raw material
FpDecanting point, raffinate RpIt is continuous between off-take point three；
Raffinate RpOff-take point is located at raw material FpDecanting point and next section of p+1 sections of desorbing agent Dp+1Between decanting point, raw material
Fp, raffinate RpOff-take point, desorbing agent Dp+1It is continuous between decanting point three；
Next section of p+1 sections of desorbing agent Dp+1Decanting point is located at the preceding paragraph raffinate RpOff-take point and Extract Ep+1Off-take point it
Between, raffinate RpOff-take point, desorbing agent Dp+1Decanting point, Extract Ep+1It is continuous between off-take point three；
First segment desorbing agent D1Decanting point is located at m sections of raffinate R of final stagemOff-take point and Extract E1Between off-take point,
Raffinate RmOff-take point, desorbing agent D1Decanting point, Extract E1It is continuous between off-take point three；
Integer of the p between 1~m.
" continuous " between above-mentioned material decanting point and off-take point refer between the continuity point without other take out or
Decanting point exists.
In the method for the present invention, the raw material of different absorbed component contents is respectively fed to different adsorbing separation sections, according into
Enter the absorbed component content in the absorption raw material of each adsorbing separation section and adjusts each adsorbing separation section desorption area, purification section, adsorption zone
With the adsorbent bed number of plies of isolated area.Such as there is the raw material of different compositions to be respectively fed to the first segregation section, the second segregation section m kind
┄ m segregation section adsorbs raw material F1、F2And FmThere is notable difference comprising the two or more adsorption capacities on same adsorbent
Component, wherein in the first adsorbing separation section, through adsorbing separation, by raw material F1In strong absorbed component from Extract E1Middle taking-up,
Remaining weakly adsorbed components are from raffinate R1It takes out, in the second adsorbing separation section, through adsorbing separation, by F2In strong absorbed component
From Extract E2Middle taking-up, remaining weakly adsorbed components are again from raffinate R2It takes out, and so on, to the last one adsorbs raw material
FmIn strong absorbed component from Extract EmMiddle taking-up, remaining weakly adsorbed components are from raffinate RmIt takes out, the original of difference composition
Material goes out the strong absorbed component in each feed composition, desorbing agent D by separating-purifying respectively simultaneously1To DmIt is infused respectively from different location
Enter.
It is that paraxylene content or meta-xylene content are different that different absorption raw materials is formed described in the method for the present invention
C8Aromatic hydrocarbons, the purpose product of adsorbing separation are paraxylene or meta-xylene.
The desorbing agent of adsorption stripping dimethyl benzene is p-Diethylbenzene, and the desorbing agent of adsorption separation of m-Xylene is toluene.
The different absorption raw material of the composition is the C containing paraxylene8Aromatic hydrocarbons and without paraxylene and containing ethylbenzene
C8Aromatic hydrocarbons；For the C containing paraxylene8Aroamtic hydrocarbon raw material, the purpose product of adsorbing separation are paraxylene, and desorbing agent is to diethyl
Benzene；For without paraxylene and containing the raw material of ethylbenzene, the purpose product of adsorbing separation is ethylbenzene, and desorbing agent is toluene.
The method of the present invention is preferably applied to while the C of two strands of separating-purifying different compositions8In aromatic hydrocarbons mixture to diformazan
Benzene, or the C of two strands of separating-purifying different compositions is distinguished simultaneously8Paraxylene and ethylbenzene in aromatic hydrocarbons mixture.
It is also possible to apply the invention to the separation of n-alkane and mono-methyl branched alkanes and other structures hydro carbons, alkene with
The adsorbing separation of alkane.
Liquid phase Simulation moving bed is preferably divided into two when separating the hydrocarbon mixture of different compositions by the method for the present invention
Adsorbing separation section, every section of bed number are 12~18, can be according to the big ditty of content of purpose adsorbing separation component in different material
Whole adsorption zone bed number such as inhales tool there are two the adsorbing separation section of 12 bed numbers into purpose in the raw material of the first segregation section
Attached constituent content is low, then the bed ratio of the desorption area of the adsorbing separation section, purification section, adsorption zone and isolated area is adjusted to 2:5:
3:2, it is high into purpose absorbed component content in the raw material of the second adsorbing separation section, then area, purification is desorbed in the second segregation section
The bed ratio in area, adsorption zone and isolated area is adjusted to 2:4:4:2.
In the method for the present invention, the desorbing agent of each desorbing agent D decanting point of SMB adsorbing separation injection can it is identical can also
With not identical, preferably different desorbing agent.
Illustrate the present invention with reference to the accompanying drawing.
Fig. 1 is prior art adsorbing separation C8The schematic diagram of each area's injecting material of paraxylene and discharge material in aromatic hydrocarbons.
In Fig. 1, liquid flow direction is divided into four areas along bed, is followed successively by desorption area, purification section, adsorption zone and isolated area, C8Virtue
Hydrocarbon F enters adsorption zone, and through adsorbing separation, paraxylene is adsorbed in adsorbent, remaining component and desorbing agent exist as raffinate R
It is taken out below raw material decanting point, the paraxylene after being desorbed is with desorbing agent as Extract E by taking above raw material decanting point
Out, desorbing agent D injects above Extract E off-take point, is isolation between the injection phase desorbing agent D and raffinate extracting position
Area.
Fig. 2 is that Simulation moving bed is divided into the schematic diagram of m adsorbing separation section by the method for the present invention, in figure, with each desorbing agent
Boundary line of the injection phase as adsorbing separation section is an adsorbing separation section, each absorption between two bursts of desorbing agent injection phases
Segregation section is equipped with desorption area, purification section, adsorption zone and isolated area, the isolated area and the first adsorbing separation of m adsorbing separation section
The desorption area of section is connected.M adsorbing separation section is respectively enterd by m strands of different raw material, the m strands of desorbing agents formed, obtains m bursts of pumpings
Liquid and m strands of raffinates out.The m preferably 2 or 3.
Simulation moving bed is divided into 2 adsorbing separation section adsorbing separation C for the method for the present invention by Fig. 38Paraxylene in aromatic hydrocarbons
Schematic diagram.First mixing C8Aroamtic hydrocarbon raw material F1Into the adsorption zone of the first adsorbing separation section, taken below raw material injection phase
Raffinate R out1, Extract E is taken out above1, desorbing agent D1In Extract E1Injection above extracting position.Second mixing C8Virtue
Hydrocarbon raw material F2Into the adsorption zone of the second adsorbing separation section, raffinate R is taken out below raw material injection phase2, take out above
Extract E2, desorbing agent D2In Extract E2Raffinate R above extracting position1Injection, desorbing agent D below extracting position1It is extracting out
Liquid E1With raffinate R2Between extracting position.The purpose absorbed component of two stage adsorption Disengagement zone is paraxylene, and desorbing agent is equal
For p-Diethylbenzene.
Simulation moving bed is divided into 2 adsorbing separation section adsorbing separation C for the method for the present invention by Fig. 48Paraxylene in aromatic hydrocarbons
With the schematic diagram of ethylbenzene.First mixing C8Aroamtic hydrocarbon raw material F1Into the adsorption zone of the first adsorbing separation section, in raw material injection phase
Take out raffinate R in lower section1, the Extract E containing paraxylene is taken out above1, desorbing agent D1In Extract E1On extracting position
Side's injection.The second mixing C without paraxylene8Aroamtic hydrocarbon raw material F2Into the adsorption zone of the second adsorbing separation section, infused in raw material
Enter and takes out raffinate R below position2, the Extract E containing ethylbenzene is taken out above2, desorbing agent D2In Extract E2Extracting position
Top raffinate R1Injection, desorbing agent D below extracting position1In Extract E1With raffinate R2Between extracting position.First segment
The purpose absorbed component of adsorptive separation zone is paraxylene, and desorbing agent is p-Diethylbenzene；The purpose of second segment adsorptive separation zone is inhaled
Attached group is divided into ethylbenzene, and desorbing agent is toluene.
Below by example, present invention be described in more detail, but the present invention is not limited thereto.
Comparative example 1
As shown in Figure 1, with the separate mode of the prior art from C8Adsorption stripping dimethyl benzene in aromatic hydrocarbons mixture.Absorption
The composition of raw material are as follows: 15 mass % of ethylbenzene (EB), 20 mass % of paraxylene (PX), 50 mass % of meta-xylene (MX), neighbour two
15 mass % of toluene (OX).
Liquid phase Simulation moving bed has 24 adsorption beds, and each bed length is 1.1 meters, and diameter is 1.9 meters, and device is set
The feed throughput of meter is 498.4L/min.Entire adsorption separation device has one raw material F injection, one desorbing agent D note
Enter, one raffinate R taking-up, one Extract E taking-up, is divided into desorption area, purification section, adsorption zone and isolated area, each area's bed
It is allocated as follows:
Desorption area (is injected and extracted between liquid E taking-up) in desorbing agent D: 5 beds；
It (is taken out between raw material F injection in Extract E) purification section: 9 beds；
Adsorption zone (between raw material F injection and raffinate R are taken out): 7 beds；
Isolated area (is taken out between desorbing agent D injection) in raffinate R: 3 beds.
One stepping time is 85.0 seconds, each to pass in and out material liquid flow direction along bed every a stepping time
A mobile bed.177 DEG C of operation temperature, operating pressure 0.88MPa.Adsorbent contains the BaX zeolite and 5 matter of 95 mass %
Measure the kaolin of %.Desorbing agent used is p-Diethylbenzene (PDEB).
Each material flow is as follows:
Raw material F:249.2L/min；
Desorbing agent D:316.3L/min；
Extract E:119.4L/min；
Raffinate R:446.1L/min.
Desorbing agent in gained Extract and raffinate is removed, extraction oil is obtained and is raffinated oil, wherein right in extraction oil
Dimethylbenzene purity is 99.81 mass %, and yield is 98.9 mass % (PX content in relative adsorption raw material).
Example 1
As shown in Figure 3, the liquid phase Simulation moving bed device that comparative example 1 there are 24 adsorption beds is divided into two absorption point
From section, every section has 12 beds, and by liquid flow direction in bed, the first adsorbing separation section is located at the second adsorbing separation section
Upstream.Entire adsorption separation device has two bursts of raw material injections, two bursts of desorbing agent injections, two bursts of raffinates taking-ups, two bursts of extractions
Liquid takes out.Two adsorbing separation Duan Jun have desorption area, purification section, adsorption zone and isolated area, each area's bed to be allocated as follows:
First adsorbing separation section:
1:2, area bed is desorbed；The bed of purification section 1:5；
1:3 bed of adsorption zone；1:2 bed of isolated area；
Second adsorbing separation section
2:2, area bed is desorbed；The bed of purification section 2:4；
2:4 bed of adsorption zone；2:2 bed of isolated area.
First adsorbing separation section has two bursts of chargings, respectively raw material F1With desorbing agent D1, two bursts of dischargings, respectively Extract
E1With raffinate R1。
Second adsorbing separation section has two bursts of chargings, respectively raw material F2With desorbing agent D2, two bursts of dischargings, respectively Extract
E2With raffinate R2。
Raw material F1Each component content are as follows: 15 mass % of ethylbenzene (EB), 20 mass % of paraxylene (PX), meta-xylene
(MX) 50 mass %, 15 mass % of ortho-xylene (OX).
Raw material F2Each component content are as follows: 10 mass % of ethylbenzene (EB), 25 mass % of paraxylene (PX), meta-xylene
(MX) 50 mass %, 15 mass % of ortho-xylene (OX).
One stepping time is 170 seconds, each to pass in and out material liquid flow direction along bed every a stepping time
A mobile bed.177 DEG C of operation temperature, operating pressure 0.88MPa.Adsorbent contains the BaX zeolite and 5 matter of 95 mass %
Measure the kaolin of %.Desorbing agent D1And D2It is p-Diethylbenzene (PDEB).
Each material flow is as follows:
Desorbing agent in gained Extract and raffinate is removed, extraction oil is obtained and is raffinated oil, wherein the first absorption point
The p-xylene purity oily from the extraction that section obtains is 99.80 mass %, and paraxylene yield is 98.6 mass %；Second inhales
The p-xylene purity for the extraction oil that attached segregation section obtains is 99.79 mass %, and yield is 99.3 mass %.
Example 2
As shown in Figure 4, the liquid phase Simulation moving bed device that comparative example 1 there are 24 adsorption beds is divided into two absorption point
From section, every section has 12 beds, and by liquid flow direction in bed, the first adsorbing separation section is located at the second adsorbing separation section
Upstream.Entire adsorption separation device has two bursts of raw material injections, two bursts of desorbing agent injections, two bursts of raffinates taking-ups, two bursts of extractions
Liquid takes out.Two adsorbing separation Duan Jun have desorption area, purification section, adsorption zone and isolated area, each area's bed to be allocated as follows:
First adsorbing separation section:
1:2, area bed is desorbed；The bed of purification section 1:5；
1:3 bed of adsorption zone；1:2 bed of isolated area；
Second adsorbing separation section
2:2, area bed is desorbed；The bed of purification section 2:4；
2:4 bed of adsorption zone；2:2 bed of isolated area.
First adsorbing separation section has two bursts of chargings, respectively raw material F1With desorbing agent D1, two bursts of dischargings, respectively Extract
E1With raffinate R1。
Second adsorbing separation section has two bursts of chargings, respectively raw material F2With desorbing agent D2, two bursts of dischargings, respectively Extract
E2With raffinate R2。
Raw material F1Each component content are as follows: 15 mass % of ethylbenzene (EB), 20 mass % of paraxylene (PX), meta-xylene
(MX) 50 mass %, 15 mass % of ortho-xylene (OX).
Raw material F2Each component content are as follows: 18.75 mass % of ethylbenzene (EB), 62.5 mass % of meta-xylene (MX), adjacent diformazan
18.75 mass % of benzene (OX).
One stepping time is 170 seconds, each to pass in and out material liquid flow direction along bed every a stepping time
A mobile bed.177 DEG C of operation temperature, operating pressure 0.88MPa.Adsorbent contains the BaX zeolite and 5 matter of 95 mass %
Measure the kaolin of %.Desorbing agent D used1For p-Diethylbenzene, D2For toluene (TOL).
Each material flow is as follows:
Desorbing agent in gained Extract and raffinate is removed, extraction oil is obtained and is raffinated oil, wherein the first absorption point
The p-xylene purity oily from the extraction that section obtains is 99.72 mass %, and paraxylene yield is 99.0 mass %；Second inhales
The ethylbenzene purity for the extraction oil that attached segregation section obtains is 99.7 mass %, and yield is 83.7 mass %.
Claims (9)
1. a kind of method with liquid phase Simulation moving bed adsorbing separation multiply difference constitutive material simultaneously, including will contain n bed
Liquid phase Simulation moving bed be divided into m adsorbing separation section, the bed between two adjacent desorbing agent D decanting points be one absorption
Segregation section, each adsorbing separation section fluid flow direction sequence along bed arrange, the coupled taking-up logistics of injection logistics it
Between bed formed Simulation moving bed functional areas；
Each adsorbing separation Duan Jun includes desorption area, purification section, adsorption zone and isolated area, and desorbing agent D is injected and extracted from liquid E taking-up
Between functional areas be desorption area, Extract E take out and raw material F injection between functional areas be purification section, raw material F injection and take out
Functional areas between extraction raffinate R taking-up are adsorption zone, and it is isolated area that raffinate R, which takes out the functional areas between desorbing agent D injection,；
M gangs of desorbing agent D1、D2、……、DmIt is injected separately into the desorption area of each adsorbing separation section, the m stock adsorbing separation of difference composition is former
Expect F1、F2、……、Fm, be injected separately into the adsorption zone of each adsorbing separation section, after adsorbing separation, the component not being adsorbed respectively by
The adsorption zone of each adsorbing separation section is discharged, and is raffinate R1、R2、……、Rm, total m strands of raffinate be adsorbed component E1、
E2、……、EmIt is discharged respectively by the purification section of each adsorbing separation section；
The decanting point and off-take point of each logistics of liquid phase Simulation moving bed are every to pass through a stepping time tsSimultaneously to same direction
A mobile bed, and moving direction is identical as fluid flow direction in adsorbent bed, and decanting point and off-take point are flowed along fluid
Direction is followed successively by D1、E1、F1、R1、D2、E2、F2、R2、……、Dm、Em、Fm、Rm,
First segment desorbing agent D1Decanting point is located at m sections of raffinate R of final stagemOff-take point and Extract E1Between off-take point, raffinate
Liquid RmOff-take point, desorbing agent D1Decanting point, Extract E1It is continuous between off-take point three,
The raw material of different absorbed component contents is respectively fed to different adsorbing separation sections, according to the suction for entering each adsorbing separation section
Absorbed component content in attached raw material adjust each adsorbing separation section desorption area, purification section, adsorption zone and isolated area adsorption bed
Number.
2. according to the method for claim 1, it is characterised in that the n is 24~36, the integer that the m is 2~4.
3. according to the method for claim 1, it is characterised in that the liquid phase Simulation moving bed material decanting point and off-take point
Position is as follows:
In each adsorbing separation section, Extract EpOff-take point is located at desorbing agent DpDecanting point and raw material FpBetween decanting point, raw material FpNote
Access point, Extract EpOff-take point, desorbing agent DpIt is continuous between decanting point three；
Raw material FpDecanting point is located at Extract EpOff-take point and raffinate RpBetween off-take point, Extract EpOff-take point, raw material FpNote
Access point, raffinate RpIt is continuous between off-take point three；
Raffinate RpOff-take point is located at raw material FpDecanting point and next section of p+1 sections of desorbing agent Dp+1Between decanting point, raw material Fp, raffinate
Liquid RpOff-take point, desorbing agent Dp+1It is continuous between decanting point three；
Next section of p+1 sections of desorbing agent Dp+1Decanting point is located at the preceding paragraph raffinate RpOff-take point and Extract Ep+1Between off-take point, take out
Extraction raffinate RpOff-take point, desorbing agent Dp+1Decanting point, Extract Ep+1It is continuous between off-take point three；
Integer of the p between 1~m.
4. according to the method for claim 1, it is characterised in that the m stock desorbing agent for entering each adsorbing separation section is identical or not
Together.
5. according to the method for claim 1, it is characterised in that the bed number that each adsorbing separation section is included is identical or not
Together.
6. according to the method for claim 1, it is characterised in that the purpose product of each adsorbing separation section adsorbing separation
It is identical or different.
7. according to the method for claim 1, it is characterised in that the different absorption raw material of the composition contains for paraxylene
Amount or the different C of meta-xylene content8Aromatic hydrocarbons, the purpose product of adsorbing separation are paraxylene or meta-xylene.
8. according to the method for claim 7, it is characterised in that the desorbing agent of adsorption stripping dimethyl benzene is p-Diethylbenzene, is inhaled
The desorbing agent that Fufen sows discord dimethylbenzene is toluene.
9. according to the method for claim 1, it is characterised in that the different absorption raw material of the composition is containing paraxylene
C8Aromatic hydrocarbons and C without paraxylene and containing ethylbenzene8Aromatic hydrocarbons；For the C containing paraxylene8Aroamtic hydrocarbon raw material, the mesh of adsorbing separation
Product be paraxylene, desorbing agent is p-Diethylbenzene；For without paraxylene and containing the raw material of ethylbenzene, the mesh of adsorbing separation
Product be ethylbenzene, desorbing agent is toluene.
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| CN201510450363.XA CN106390518B (en) | 2015-07-28 | 2015-07-28 | A method of with liquid phase Simulation moving bed while adsorbing separation multiply raw material |
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| CN201510450363.XA CN106390518B (en) | 2015-07-28 | 2015-07-28 | A method of with liquid phase Simulation moving bed while adsorbing separation multiply raw material |
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| CN106390518B true CN106390518B (en) | 2019-11-15 |
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| CN1107381A (en) * | 1994-12-07 | 1995-08-30 | 中国石化扬子石油化工公司 | Improved adsorption separation process for simulation moving bed |
| CN1034069C (en) * | 1991-09-05 | 1997-02-19 | 法国石油公司 | Process and device for separation of para-xylene from octa-arene by adsorption and crystallization with analogue movable bed |
| US5750820A (en) * | 1995-09-15 | 1998-05-12 | Wei; Chiu N. | Multiple grade flush adsorption separation process |
| CN101903073A (en) * | 2007-12-21 | 2010-12-01 | Ifp公司 | The improved device that is used for simulation moving-bed separation |
| FR2953733A1 (en) * | 2009-12-11 | 2011-06-17 | Inst Francais Du Petrole | Reactive separation on simulated moving bed using a liquid catalyst/soluble in the liquid medium constituted by reagents and products, comprises producing a desired isomer A from a mixture of isomers bound by equilibrium catalytic reaction |
| CN103596654A (en) * | 2011-06-16 | 2014-02-19 | Ifp新能源公司 | Simulated countercurrent chromatographic separation process and device with low pressure drop and high number of zones |
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| CN1034069C (en) * | 1991-09-05 | 1997-02-19 | 法国石油公司 | Process and device for separation of para-xylene from octa-arene by adsorption and crystallization with analogue movable bed |
| CN1107381A (en) * | 1994-12-07 | 1995-08-30 | 中国石化扬子石油化工公司 | Improved adsorption separation process for simulation moving bed |
| US5750820A (en) * | 1995-09-15 | 1998-05-12 | Wei; Chiu N. | Multiple grade flush adsorption separation process |
| CN101903073A (en) * | 2007-12-21 | 2010-12-01 | Ifp公司 | The improved device that is used for simulation moving-bed separation |
| FR2953733A1 (en) * | 2009-12-11 | 2011-06-17 | Inst Francais Du Petrole | Reactive separation on simulated moving bed using a liquid catalyst/soluble in the liquid medium constituted by reagents and products, comprises producing a desired isomer A from a mixture of isomers bound by equilibrium catalytic reaction |
| CN103596654A (en) * | 2011-06-16 | 2014-02-19 | Ifp新能源公司 | Simulated countercurrent chromatographic separation process and device with low pressure drop and high number of zones |
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