CN112341306B - Eluent and method for separating alkane and alkene by simulated moving bed - Google Patents
Eluent and method for separating alkane and alkene by simulated moving bed Download PDFInfo
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- CN112341306B CN112341306B CN201910715133.XA CN201910715133A CN112341306B CN 112341306 B CN112341306 B CN 112341306B CN 201910715133 A CN201910715133 A CN 201910715133A CN 112341306 B CN112341306 B CN 112341306B
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- 239000003480 eluent Substances 0.000 title claims abstract description 100
- 150000001335 aliphatic alkanes Chemical class 0.000 title claims abstract description 54
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 53
- 238000000034 method Methods 0.000 title claims abstract description 27
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 29
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000002994 raw material Substances 0.000 claims description 33
- 239000004711 α-olefin Substances 0.000 claims description 29
- 239000000203 mixture Substances 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 8
- 230000007423 decrease Effects 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 abstract description 42
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 21
- HFDVRLIODXPAHB-UHFFFAOYSA-N 1-tetradecene Chemical compound CCCCCCCCCCCCC=C HFDVRLIODXPAHB-UHFFFAOYSA-N 0.000 description 50
- BGHCVCJVXZWKCC-UHFFFAOYSA-N tetradecane Chemical compound CCCCCCCCCCCCCC BGHCVCJVXZWKCC-UHFFFAOYSA-N 0.000 description 50
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 48
- 238000001179 sorption measurement Methods 0.000 description 35
- 239000003463 adsorbent Substances 0.000 description 29
- YCOZIPAWZNQLMR-UHFFFAOYSA-N heptane - octane Natural products CCCCCCCCCCCCCCC YCOZIPAWZNQLMR-UHFFFAOYSA-N 0.000 description 25
- CRSBERNSMYQZNG-UHFFFAOYSA-N 1-dodecene Chemical compound CCCCCCCCCCC=C CRSBERNSMYQZNG-UHFFFAOYSA-N 0.000 description 22
- AFFLGGQVNFXPEV-UHFFFAOYSA-N 1-decene Chemical compound CCCCCCCCC=C AFFLGGQVNFXPEV-UHFFFAOYSA-N 0.000 description 20
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 19
- 239000007788 liquid Substances 0.000 description 18
- 239000002808 molecular sieve Substances 0.000 description 16
- 150000002894 organic compounds Chemical class 0.000 description 16
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 15
- 229910052760 oxygen Inorganic materials 0.000 description 15
- 239000001301 oxygen Substances 0.000 description 15
- 239000003053 toxin Substances 0.000 description 15
- 231100000765 toxin Toxicity 0.000 description 15
- 108700012359 toxins Proteins 0.000 description 15
- 239000000463 material Substances 0.000 description 13
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical compound CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 11
- 229940069096 dodecene Drugs 0.000 description 11
- 229940094933 n-dodecane Drugs 0.000 description 9
- 238000004587 chromatography analysis Methods 0.000 description 8
- 238000000605 extraction Methods 0.000 description 8
- 230000000694 effects Effects 0.000 description 4
- BKIMMITUMNQMOS-UHFFFAOYSA-N nonane Chemical compound CCCCCCCCC BKIMMITUMNQMOS-UHFFFAOYSA-N 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000003795 desorption Methods 0.000 description 3
- ZGEGCLOFRBLKSE-UHFFFAOYSA-N 1-Heptene Chemical compound CCCCCC=C ZGEGCLOFRBLKSE-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 238000006384 oligomerization reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000005673 monoalkenes Chemical class 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
An eluent and a method for simulated moving bed separation of alkanes and alkenes, the eluent comprising alpha-alkenes and normal alkanes, wherein the carbon numbers of the alpha-alkenes and normal alkanes are different from the carbon numbers of the alkenes to be separated, and the carbon numbers of the alpha-alkenes and normal alkanes are the same or different. The invention can effectively improve the yield of olefin and reduce the cost of eluent.
Description
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to an eluent and a method for separating alkane and alkene by a simulated moving bed.
Background
A simulated moving bed is a mass transfer device for liquid separation operations using the adsorption principle. The method is to change the material inlet and outlet positions of fixed bed adsorption equipment in a countercurrent continuous operation mode, so as to generate the effect equivalent to continuous downward movement of the adsorbent and continuous upward movement of the material. The separation of the different components in the material is achieved according to the different adsorption capacities of the different components in the material on the adsorbent, as shown in fig. 1.
Alpha-olefins are known to be mono-olefins with double bonds at the end of the molecular chain. The catalyst is an important chemical raw material and an organic synthesis intermediate, and has wide application in the chemical field. It can be used as the synthetic intermediate of surfactant, plasticizer and additive of synthetic hydrocarbon lubricating oil and oil product. Alpha-olefins are also of great use in the perfumery, paper, household chemistry and other industries.
The alpha-olefin in the current market mainly comes from methods such as ethylene oligomerization, paraffin cracking, fischer-Tropsch synthesis and the like. The alpha-olefin produced by the coal-based Fischer-Tropsch process has continuous carbon number, contains a large amount of high-carbon alpha-olefin, has obvious advantages over an ethylene oligomerization process which can only produce even carbon number, but the alpha-olefin produced by the coal-based Fischer-Tropsch process is simultaneously produced along with alkane, so that the alkane and the alkene can be effectively separated, and the added value of the coal-based Fischer-Tropsch synthesis product is significant.
One prior art method for olefin separation has proposed the use of a simulated moving bed apparatus wherein an eluent (desorbent) employs olefins to desorb the olefins adsorbed to the adsorbent in an alkylen mixture. The method has no specific implementation effect, but the residual liquid (raffinate) entrains olefin to reduce the product yield, and the eluent adopts olefin with higher cost.
In another existing olefin separation method, the eluent is cycloparaffin, which can effectively separate olefin, but when cycloparaffin is used as the eluent, the amount of the extract (extract) is extremely large to meet the purity requirement, so that the absorbed olefin can be desorbed from the adsorbent, thus the desorption efficiency of the eluent is low, and the olefin separation cost in the extract is increased.
In the prior simulated moving bed separation of alkane and olefin, the eluent adopts a single component, such as olefin or naphthene. Olefin is used as eluent, so that the desorption is too fast, olefin is carried in residual liquid, the yield is low, and the cost of eluent is high. The naphthene is used as eluent, which has the disadvantages of slow desorption, long separation time, low device efficiency and large eluent consumption.
Disclosure of Invention
The invention provides a novel eluent (desorbent) and a method for separating alkane and alkene by a simulated moving bed, which can prepare different eluents according to the concentration of alkene in raw materials, effectively improve the yield of alkene and reduce the cost of the eluent. In addition, the invention has wider application range and can reduce the energy consumption of the device.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
an eluent for simulated moving bed separation of alkanes and alkenes, comprising alpha-alkenes and normal alkanes, wherein the carbon numbers of the alpha-alkenes and normal alkanes are different from the carbon numbers of the alkenes in the feedstock to be separated, and the carbon numbers of the alpha-alkenes and normal alkanes are the same or different.
In some embodiments, the difference in carbon numbers of the α -olefins and the n-paraffins to the carbon number of the olefins in the feedstock to be separated is less than 7 (e.g., 1, 2, 3, 4, 5, 6), preferably greater than 1 and less than 5 (e.g., 2, 3, 4).
In some embodiments, the weight percentage of the normal alkane is 1-99%, e.g., 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%.
In some embodiments, the fraction of normal paraffins in the eluent increases as the fraction of olefins in the feedstock to be separated decreases.
In some embodiments, the alpha-olefin may be one alpha-olefin, or a mixture of a plurality of alpha-olefins.
In some embodiments, the n-alkane may be one n-alkane, or a mixture of n-alkanes.
A method for separating alkanes and alkenes using a simulated moving bed, comprising eluting with the eluent.
In some embodiments, the operating temperature is from 0 to 250 ℃, preferably from 20 to 100 ℃; the operating pressure is 0 to 2MPa, preferably 0 to 1MPa.
In some embodiments, the method includes the step of removing impurities in the eluent and the feedstock to be separated that affect the adsorption effect.
In some embodiments, the method includes the step of separating and recovering the eluent in the extract and the raffinate.
Compared with the prior art, the invention has the following advantages:
1. the eluent selected by the invention has almost no entrainment (less than 3%) in the simulated moving bed separation process, and the recovery rate of the product is provided.
2. The alkene and alkane in the eluent provided by the invention can be of different carbon numbers, and the eluent is easier to obtain and more flexible in proportioning.
3. The alkane in the eluent provided by the invention accounts for 1-99%, can be flexibly adjusted according to actual technological parameters, and has wide operating conditions.
4. The eluent provided by the invention has small dosage, reduces the control difficulty of the rectification process and saves energy consumption.
5. The eluent selected by the invention is cheap and easy to obtain.
Drawings
FIG. 1 is a schematic diagram of the principle of operation of a simulated moving bed;
FIG. 2 is a graph showing the distribution of C14 in an adsorption tube of a simulated moving bed in example 1 of the present invention;
FIG. 3 is a graph showing the distribution of C14 in an adsorption tube of a simulated moving bed in example 2 of the present invention;
FIG. 4 is a graph showing the distribution of C14 in an adsorption tube of a simulated moving bed in example 3 of the present invention;
FIG. 5 is a graph showing the distribution of C10 in a simulated moving bed adsorbent tube in example 4 of the present invention;
FIG. 6 is a graph showing the distribution of C12 in an adsorption tube of a simulated moving bed in example 5 of the present invention;
FIG. 7 is a graph showing the distribution of C12 in an adsorption tube of a simulated moving bed in example 6 of the present invention;
FIG. 8 is a graph showing the distribution of C14 in an adsorption tube of a simulated moving bed in example 7 of the present invention;
FIG. 9 is a graph showing the distribution of C14 in an adsorption tube of a simulated moving bed in example 8 of the present invention.
Detailed Description
The present invention will be further described in detail below with reference to specific embodiments and with reference to the accompanying drawings, in order to make the objects, technical solutions and advantages of the present invention more apparent.
The Fischer-Tropsch synthesis product mainly comprises a mixture of alkane and alkene, the alkane and the alkene with different carbon numbers can be separated by means of rectification and the like, and the alkane and the alkene with the same carbon number are not easy to completely separate. The invention utilizes a simulated moving bed device to separate alkane and alkene, wherein eluent is an important factor influencing the separation effect.
The eluent with different alkyl and alkene mixing ratios with different carbon numbers of the alkene in the separated material is selected, so that the entrainment of the alkene in the raffinate (raffinate) can be effectively reduced, and the alkene yield of the product is improved (more than 97 percent); reducing the dosage of the eluent, and improving the olefin ratio (more than 20 percent) in the extract liquid (extract liquid); the eluent cost can be reduced by adopting the ratio of a large amount of alkane to a small amount of alkene.
The invention provides a novel eluent for separating alkane and alkene by a simulated moving bed, which comprises alpha-alkene and normal alkane, wherein the carbon numbers of the alpha-alkene and the normal alkane are different from those of the alkene in a raw material to be separated, and the carbon numbers of the alpha-alkene and the normal alkane are the same or different.
The carbon number of the alpha-olefin and/or the normal alkane may be greater than the carbon number of the olefin in the raw material to be separated, or may be less than the carbon number of the olefin in the raw material to be separated. In some embodiments, the difference in carbon numbers of the α -olefins and the n-paraffins to the carbon number of the olefins in the feedstock to be separated is less than 7 (e.g., 1, 2, 3, 4, 5, 6), preferably greater than 1 and less than 5 (e.g., 2, 3, 4).
The weight percentage of the normal alkane is 1-99%, such as 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%.
In general, the smaller the proportion of olefins in the feed to be separated, the greater the proportion of normal paraffins in the eluate.
The alpha-olefin may be one alpha-olefin, or a mixture of a plurality of alpha-olefins. The n-alkane may be one n-alkane, or a mixture of n-alkanes.
Example 1
The feedstock to be separated in this example is a C14 component, and the eluent is a C10 alpha-olefin and normal alkane.
C14 raw materials: n-tetradecane 30% (w/w), 1-tetradecene 70% (w/w), and prior to separation of the alkane from the feedstock, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C10 eluent: 70% (w/w) n-decane, 30% (w/w) 1-decene, and pre-treating the eluent to remove toxic substances (such as oxygen-containing organic compounds, benzene, water, etc.) which may cause adsorption failure before the separation of the alkane and the alkene.
Separation of the C14 feed was performed in a simulated moving bed unit using a C10 eluent. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the temperature operation temperature is 250 ℃; the operating pressure was 2MPa.
The distribution of C14 in the simulated moving bed adsorption tube is shown in FIG. 2. The chromatographic analysis results are shown in Table 1.
TABLE 1
| Material | N-tetradecane (%, w/w) | 1-tetradecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.93 |
| Extraction liquid | 0.04 | 36.33 | 63.58 |
| Raffinate from the treatment of a plant | 57.90 | 0.55 | 41.52 |
As can be seen from Table 1, the content of n-tetradecane in the extract was only 0.04%, the content of 1-tetradecene was 36.33%, the content of n-tetradecane in the residual liquid was 57.90%, and the content of 1-tetradecene was only 0.55%, and it was found that the high-efficiency separation of n-tetradecane and 1-tetradecene in the raw material was achieved by using the eluent.
Example 2
The feedstock to be separated in this example is a C14 component, and the eluent is a C10 alpha-olefin and normal alkane.
C14 raw materials: n-tetradecane 30% (w/w), 1-tetradecene 70% (w/w), and prior to separation of the alkane from the feedstock, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C10 eluent: n-decane 99% (w/w), 1-decene 1% (w/w), and prior to separation of the alkane, the eluent is pretreated to remove toxins (e.g., oxygen-containing organic compounds, benzene, water, etc.) which may cause adsorption failure.
Separation of the C14 feed was performed in a simulated moving bed unit using a C10 eluent. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the temperature operation temperature is 150 ℃; the operating pressure was 1.5MPa.
The distribution of C14 in the simulated moving bed adsorption tube is shown in FIG. 3. The chromatographic analysis results are shown in Table 2.
TABLE 2
| Material | N-tetradecane (%, w/w) | 1-tetradecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.91 |
| Extraction liquid | 0.02 | 22.57 | 77.41 |
| Raffinate from the treatment of a plant | 49.38 | 0.31 | 50.31 |
As can be seen from Table 2, the content of n-tetradecane in the extract was only 0.02%, the content of 1-tetradecene was 22.57%, the content of n-tetradecane in the residual liquid was 49.38%, and the content of 1-tetradecene was only 0.31%, and it was found that the separation of n-tetradecane and 1-tetradecene in the raw material was achieved by using the eluent.
Example 3
The feedstock to be separated in this example is a C14 component, and the eluent is a C10 alpha-olefin and normal alkane.
C14 raw materials: n-tetradecane 30% (w/w), 1-tetradecene 70% (w/w), and prior to separation of the alkane from the feedstock, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C10 eluent: n-decane 1% (w/w), 1-decene 99% (w/w), and prior to separation of the alkane, the eluent is pretreated to remove toxins (e.g., oxygen-containing organic compounds, benzene, water, etc.) which may cause adsorption failure.
Separation of the C14 feed was performed in a simulated moving bed unit using a C10 eluent. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the operating temperature is 100 ℃; the operating pressure was 1Mpa.
The distribution of C14 in the simulated moving bed adsorption tube is shown in FIG. 4. The chromatographic analysis results are shown in Table 3.
TABLE 3 Table 3
| Material | N-tetradecane (%, w/w) | 1-tetradecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.96 |
| Extraction liquid | 0.31 | 41.76 | 57.93 |
| Raffinate from the treatment of a plant | 63.25 | 5.16 | 31.59 |
As can be seen from Table 3, the content of n-tetradecane in the extract was only 0.31%, the content of 1-tetradecene was 41.76%, the content of n-tetradecane in the residual liquid was 63.25%, and the content of 1-tetradecene was only 5.16%, and it was found that the separation of n-tetradecane and 1-tetradecene in the raw material was also achieved by using the eluent.
Example 4
The feedstock to be separated in this example is a C10 component, and the eluent is a C9 alpha-olefin and normal alkane.
C10 raw materials: n-decane 30% (w/w), 1-decene 70% (w/w), and prior to the separation of the alkane, the feedstock was pretreated to remove toxins (e.g., oxygen-containing organic compounds, benzene, water, etc.) that could cause adsorption failure.
C9 eluent: 70% (w/w) of n-nonane and 30% (w/w) of 1-nonene, and prior to separation of the alkane from the eluent, pretreatment is carried out to remove toxins (e.g., oxygen-containing organic compounds, benzene, water, etc.) which may cause adsorption failure.
Separation of the C10 feed was performed in a simulated moving bed unit using a C9 eluent. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the operating temperature is 20 ℃; the operating pressure was 0.5MPa.
The distribution of C10 in the simulated moving bed adsorption tube is shown in FIG. 5. The chromatographic analysis results are shown in Table 4.
TABLE 4 Table 4
| Material | N-decane (%, w/w) | 1-decene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.91 |
| Extraction liquid | 0.04 | 38.22 | 61.74 |
| Raffinate from the treatment of a plant | 53.98 | 0.77 | 45.25 |
As can be seen from Table 4, the content of n-decane in the extract was only 0.04%, the content of 1-decene was 38.22%, the content of n-decane in the raffinate was 53.98%, and the content of 1-decene was only 0.77%, and it was found that the efficient separation of n-decane and 1-decene in the raw material was achieved by using the eluent.
Example 5
The feedstock to be separated in this example is a C12 component, and the eluent is a C7 alpha-olefin and normal alkane.
And C12 raw materials: n-dodecane 30% (w/w), 1-dodecene 70% (w/w), and prior to alkane-alkene separation, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C7 eluent: 70% (w/w) n-heptane, 30% (w/w) 1-heptene, and pre-treating the eluate to remove toxins (e.g., oxygen-containing organic compounds, benzene, water, etc.) therein that may cause adsorption failure prior to alkane-alkene separation.
Separation of the C12 feed was performed in a simulated moving bed unit using a C7 eluent. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the operating temperature is 50 ℃; the operating pressure was 1Mpa.
The distribution of C12 in the simulated moving bed adsorption tube is shown in FIG. 6. The chromatographic analysis results are shown in Table 5.
TABLE 5
| Material | N-dodecane (%, w/w) | 1-dodecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.97 |
| Extraction liquid | 0.03 | 43.58 | 56.39 |
| Raffinate from the treatment of a plant | 59.16 | 0.62 | 40.22 |
As can be seen from Table 5, the content of n-dodecane in the extract was only 0.03%, while the content of 1-dodecene was 43.58%, the content of n-dodecane in the raffinate was 59.16%, and the content of 1-dodecene was only 0.62%, and it was found that the efficient separation of n-dodecane and 1-dodecene in the raw material was achieved by using the eluent.
Example 6
The raw material to be separated in the embodiment is a C12 component, and the eluent is the mixture ratio of C8 and C9 normal paraffins and C9 alpha-olefin.
And C12 raw materials: n-dodecane 30% (w/w), 1-dodecene 70% (w/w), and prior to alkane-alkene separation, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C8 and C9 ratio eluent: 30% (w/w) n-octane, 40% (w/w) n-nonane, 30% (w/w) 1-nonene, and prior to separation of the paraffins, the eluate is subjected to a pretreatment to remove toxins (e.g., oxygenated organic compounds, benzene, water, etc.) that may cause adsorption failure.
Separating C12 raw materials in a simulated moving bed device by using a C8 and C9 mixed eluent. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the operating temperature is 120 ℃; the operating pressure was 1Mpa.
The distribution of C12 in the simulated moving bed adsorption tube is shown in FIG. 7. The chromatographic analysis results are shown in Table 6.
TABLE 6
| Material | N-dodecane (%, w/w) | 1-dodecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.89 |
| Extraction liquid | 0.06 | 44.73 | 55.21 |
| Raffinate from the treatment of a plant | 54.33 | 0.85 | 44.82 |
As can be seen from Table 6, the content of n-dodecane in the extract was only 0.06%, while the content of 1-dodecene was 44.73%, the content of n-dodecane in the raffinate was 54.33%, and the content of 1-dodecene was only 0.85%, and it was found that the efficient separation of n-dodecane and 1-dodecene in the raw material was achieved by using the eluent.
Example 7
The raw material to be separated in the embodiment is a C14 component, and the eluent is the mixture ratio of C9 and C10 alpha-olefins and C10 normal paraffins.
C14 raw materials: n-tetradecane 30% (w/w), 1-tetradecene 70% (w/w), and prior to separation of the alkane from the feedstock, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C9, C10 alpha-olefins and C10 normal paraffins ratio eluent: n-decane 40% (w/w), 1-nonene 40% (w/w), 1-decene 20% (w/w), and prior to separation of the alkane, the eluate is subjected to a pretreatment to remove toxins (e.g., oxygen-containing organic compounds, benzene, water, etc.) therein that may cause adsorption failure.
Separation of the C14 feedstock was performed in a simulated moving bed unit using C9, C10 alpha olefins and C10 normal paraffins proportioned eluents. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the operating temperature is 100 ℃; the operating pressure was 1Mpa.
The distribution of C14 in the simulated moving bed adsorption tube is shown in FIG. 8. The chromatographic analysis results are shown in Table 7.
TABLE 7
| Material | N-tetradecane (%, w/w) | 1-tetradecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.96 |
| Extraction liquid | 0.44 | 39.58 | 59.98 |
| Raffinate from the treatment of a plant | 60.82 | 4.38 | 34.80 |
As can be seen from Table 7, the content of n-tetradecane in the extract was only 0.31%, the content of 1-tetradecene was 41.76%, the content of n-tetradecane in the residual liquid was 63.25%, and the content of 1-tetradecene was only 5.16%, and it was found that the separation of n-tetradecane and 1-tetradecene in the raw material was also achieved by using the eluent.
Example 8
The feedstock to be separated in this example is a C14 component, and the eluent is C10, C12 alpha-olefins and normal paraffins.
C14 raw materials: n-tetradecane 30% (w/w), 1-tetradecene 70% (w/w), and prior to separation of the alkane from the feedstock, the feedstock is pretreated to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
C10, C12 eluent: n-decane 35% (w/w), 1-decene 15% (w/w), n-dodecane 35% (w/w), 1-dodecene 15% (w/w), and prior to separation of the alkane, the eluate is subjected to a pretreatment to remove toxins therein (e.g., oxygen-containing organic compounds, benzene, water, etc.) that may cause adsorption failure.
Separation of the C14 feedstock was performed in a simulated moving bed unit using C10, C12 eluents. Simulated moving bed operating conditions: the adsorbent adopts a molecular sieve adsorbent and is not limited to the molecular sieve adsorbent; the temperature operation temperature is 250 ℃; the operating pressure was 2MPa. The distribution of C14 in the simulated moving bed adsorption tube is shown in FIG. 9. The chromatographic analysis results are shown in Table 8.
TABLE 8
| Material | N-tetradecane (%, w/w) | 1-tetradecene (%, w/w) | Eluent (%, w/w) |
| Raw materials | 29.98 | 70.01 | - |
| Eluent (eluent) | - | - | 99.93 |
| Extraction liquid | 0.17 | 34.98 | 64.85 |
| Raffinate from the treatment of a plant | 52.73 | 1.47 | 45.80 |
As can be seen from Table 8, the content of n-tetradecane in the extract was only 0.17%, while the content of 1-tetradecene was 34.98%, the content of n-tetradecane in the residual liquid was 52.73%, while the content of 1-tetradecene was only 1.47%, and it was found that the high-efficiency separation of n-tetradecane and 1-tetradecene in the raw material was achieved by using the eluent.
The foregoing description of the embodiments has been provided for the purpose of illustrating the general principles of the invention, and is not meant to limit the invention thereto, but to limit the invention thereto, and any modifications, equivalents, improvements and equivalents thereof may be made without departing from the spirit and principles of the invention.
Claims (9)
1. A process for separating alkanes and alkenes using a simulated moving bed comprising eluting with an eluent in a simulated moving bed apparatus;
the eluent for separating alkane and alkene by using a simulated moving bed comprises alpha-alkene and normal alkane, wherein the carbon numbers of the alpha-alkene and the normal alkane are different from those of alkene in a raw material to be separated, the carbon numbers of the alpha-alkene and the normal alkane are the same or different, the weight ratio of the normal alkane is 70-99%, and the carbon numbers of the alpha-alkene and the normal alkane are smaller than those of alkene in the raw material to be separated;
wherein the alpha-olefin is a mixture of a plurality of alpha-olefins;
the n-alkane is a mixture of a plurality of n-alkanes.
2. The process of claim 1, wherein the difference between the carbon numbers of the alpha-olefins and the normal paraffins and the carbon number of the olefins in the feedstock to be separated is less than 7.
3. The process of claim 1, wherein the difference between the carbon numbers of the alpha-olefins and the normal paraffins and the carbon number of the olefins in the feedstock to be separated is greater than 1 and less than 5.
4. The method of claim 1, wherein the fraction of normal paraffins in the eluent increases as the fraction of olefins in the feedstock to be separated decreases.
5. The process according to claim 1, wherein the operating temperature is 0 to 250 ℃ and the operating pressure is 0 to 2Mpa.
6. The method of claim 5, wherein the operating temperature is 20-100 ℃.
7. The method according to claim 5, wherein the operating pressure is 0-1 Mpa.
8. The method of claim 1, wherein the method further comprises the step of removing impurities from the eluent and the feedstock to be separated.
9. The method of claim 1, wherein the method comprises the step of separating and recovering the eluent in the extract and the raffinate.
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