CN207632727U - The separator of C9 fractions in process of preparing propylene from coal-based methanol by-product - Google Patents
The separator of C9 fractions in process of preparing propylene from coal-based methanol by-product Download PDFInfo
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- CN207632727U CN207632727U CN201721622983.8U CN201721622983U CN207632727U CN 207632727 U CN207632727 U CN 207632727U CN 201721622983 U CN201721622983 U CN 201721622983U CN 207632727 U CN207632727 U CN 207632727U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 93
- 239000003245 coal Substances 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000006227 byproduct Substances 0.000 title claims abstract description 29
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 27
- 239000000203 mixture Substances 0.000 claims abstract description 91
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 83
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 82
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 81
- 239000000047 product Substances 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims description 64
- 239000007788 liquid Substances 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 239000007795 chemical reaction product Substances 0.000 claims description 16
- 150000001336 alkenes Chemical class 0.000 claims description 11
- 230000006835 compression Effects 0.000 claims description 11
- 238000007906 compression Methods 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 9
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000010791 quenching Methods 0.000 claims description 7
- 238000005516 engineering process Methods 0.000 abstract description 15
- 239000000126 substance Substances 0.000 abstract description 14
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000000470 constituent Substances 0.000 abstract 3
- 239000003502 gasoline Substances 0.000 description 7
- 238000009835 boiling Methods 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 150000001925 cycloalkenes Chemical class 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 150000001924 cycloalkanes Chemical class 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- -1 cyclic olefins Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 150000005199 trimethylbenzenes Chemical class 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
- 150000003738 xylenes Chemical class 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a kind of separator of C9 fractions in process of preparing propylene from coal-based methanol by-product, which includes：Heavy constituent knockout tower for receiving the C6+ hydrocarbon mixtures in process of preparing propylene from coal-based methanol by-product, and detaches it, obtains the C6 C9 hydrocarbon mixtures as overhead product and the C10+ hydrocarbon mixtures as tower bottom product；C9 knockout towers obtain the C6 C8 hydrocarbon mixtures as overhead product and the C9 fractions as tower bottom product for being detached to the overhead product from heavy constituent knockout tower.The separator passes through the setting to heavy constituent knockout tower and C9 knockout towers, realization detaches the C6+ hydrocarbon mixtures in process of preparing propylene from coal-based methanol by-product, to isolate C9 fractions therein, to significantly improve the economic benefit of MTO technology, realize that diversification production, extension Chemical Industry chain, raising coal convert added value.
Description
Technical Field
The utility model belongs to coal-based methanol-to-propylene technology field, especially the separator of C9 fraction in the coal-based methanol-to-propylene technology accessory substance.
Background
The lurgi methanol to olefin process (i.e., the MTP process) produces a gasoline product as a byproduct in addition to propylene. For example, in two sets of industrial methanol-to-propylene apparatuses (propylene yield 50 ten thousand tons/year) of the shenhuaning coal group at present, gasoline by-products (namely hydrocarbon by-products) are nearly 40 ten thousand tons/year, the main components of the hydrocarbon by-products comprise olefin, naphthenic hydrocarbon, aromatic hydrocarbon and the like, the impurity content is very small, S and N are hardly contained, the hydrocarbon by-products are directly wasted when being used as fuel for combustion, and expensive gasoline tax exists at the same time, so that the economic benefit of the existing separation process using gasoline as a main product is poor. The hydrocarbon by-products comprise a high-carbon hydrocarbon mixture (i.e., a C6+ hydrocarbon mixture) containing a carbon nine fraction (a C9 fraction), the C9 fraction includes a C9 component and a C8 fraction having a higher boiling point and a part of a boiling point within a range of the C9 component, which cannot be separated from the C9 component, and the C9 component in the C9 fraction can be used as a raw material of petroleum resin, so that the economic benefits of a lurgi methanol-to-olefin process (i.e., an MTP process) can be significantly increased, diversified production is realized, the coal chemical industry chain is prolonged, and the added value of coal conversion is of great significance. The prior separation process and the separation device can not effectively separate the carbon nine fraction.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a separator of C9 fraction in coal-based methanol system propylene technology accessory substance, this separator can follow the C9 fraction separation in the coal-based methanol system propylene technology accessory substance in order to regard as the petroleum resin raw materials, and separation effect is good.
In order to realize the purpose of the utility model, the following technical scheme is adopted:
a separation device for C9 fraction in coal-based methanol-to-propylene process byproducts comprises:
the heavy component separation tower is used for receiving and separating a C6+ hydrocarbon mixture in a byproduct in the process of preparing propylene from coal-based methanol to obtain a C6-C9 hydrocarbon mixture as a tower top product and a C10+ hydrocarbon mixture as a tower bottom product;
and the C9 separation tower is used for separating the overhead product from the heavy component separation tower to obtain a C6-C8 hydrocarbon mixture as the overhead product and a C9 fraction as the bottom product.
Preferably, the separation device further comprises:
the methanol-to-propylene reactor is used for receiving raw material methanol to perform a methanol-to-propylene reaction to obtain a reaction product;
the gas-liquid separation device is used for removing water from the reaction product from the methanol-to-propylene reactor to obtain a hydrocarbon mixture;
the compression device is used for compressing the hydrocarbon mixture from the gas-liquid separation device so as to separate and remove the gaseous C3-hydrocarbon mixture;
a debutanizer for separating the liquid hydrocarbon mixture from the compression unit to obtain a C4 olefin and C3-hydrocarbon mixture as an overhead product and a C4+ hydrocarbon mixture as a bottom product;
and the dehexanizer is used for separating the bottom product from the debutanizer to obtain a C6+ hydrocarbon mixture serving as the bottom product and serving as a feed of the heavy component separation tower.
Preferably, the gas-liquid separation device comprises a pre-chilling tower and a chilling tower; the pre-chilling tower is used for separating water from reaction products of the methanol-to-propylene reactor to obtain a crude hydrocarbon mixture; the chilling tower is used for receiving the crude hydrocarbon mixture from the pre-chilling tower and separating residual water in the crude hydrocarbon mixture to obtain the hydrocarbon mixture.
The beneficial effects of the utility model reside in that:
the utility model discloses a separator of C9 fraction in coal-based methanol system propylene technology accessory substance, through the setting to component knockout tower and C9 knockout tower, the realization is separated the C6+ hydrocarbon mixture in the coal-based methanol system propylene technology accessory substance, thereby separate C9 fraction wherein, thereby show the economic benefits who improves methyl alcohol system alkene technology (promptly, MTP technology), realize diversified production, extension coal chemical industry industrial chain, improve coal conversion added value.
Drawings
FIG. 1 is a flow diagram of an apparatus for separating a C9 fraction from a byproduct of a coal-based methanol-to-propylene process of the present invention in one embodiment;
fig. 2 is a flow chart of a separation device for a C9 fraction in a byproduct of a coal-based methanol-to-propylene process of the present invention in another embodiment.
Detailed Description
The technical solution and effects of the present invention will be further explained by the following embodiments. The following embodiments are merely illustrative of the present invention, and the present invention is not limited to the following embodiments or examples. Use the utility model discloses a think about right the utility model discloses the simple change that goes on is all in the utility model discloses the within range that claims.
As shown in fig. 1, the separation device for the C9 fraction in the byproduct of the coal-based methanol-to-propylene process of the present invention includes a heavy component separation tower 1 and a C9 separation tower 2.
The heavy component separation tower 1 is used for receiving and separating a C6+ hydrocarbon mixture in a byproduct in the process of preparing propylene from coal-based methanol to obtain a C6-C9 hydrocarbon mixture as a tower top product and a C10+ hydrocarbon mixture as a tower bottom product; preferably, the heavy ends separation column 1 is operated at a pressure of from 0.09 to 0.14MPa, preferably from 0.11 to 0.12MPa, such as 0.12 MPa; the temperature at the top of the tower is 115 ℃ and 120 ℃, such as 118 ℃; the temperature of the bottom of the tower is 180 ℃ and 185 ℃, such as 182 ℃; a reflux ratio of 1.0 to 1.4, preferably 1.1 to 1.2, such as 1.15; it will be appreciated by those skilled in the art that the heavy ends separation column 1 is provided with a first condenser 11 at the top and a first reboiler 12 at the bottom. Through the arrangement, the C6-C9 hydrocarbon mixture and the C10+ hydrocarbon mixture in the C6+ hydrocarbon mixture in the coal-based methanol-to-propylene process byproduct can be effectively separated.
A C9 separating tower 2 for separating the overhead product from the heavy component separating tower 1 to obtain a C6-C8 hydrocarbon mixture as the overhead product and a C9 fraction as the bottom product; preferably, the operating pressure of the C9 splitter 2 is in the range of from 0.09 to 0.14MPa, preferably from 0.11 to 0.12MPa, such as 0.12 MPa; the temperature at the top of the column is 110 ℃ to 115 ℃, preferably 112 ℃ for example; the bottom temperature is 150-; a reflux ratio of 2.0 to 3.0, preferably 2.5 to 2.8, such as 2.6; it will be understood by those skilled in the art that the C9 splitter 2 is provided with a second condenser 21 at the top and a second reboiler 22 at the bottom. Through the above arrangement, the C6-C8 hydrocarbon mixture and the C9 fraction in the overhead product C6-C9 hydrocarbon mixture of the C9 separation tower 2 can be effectively separated.
The heavy component separation column 1 and the C9 separation column 2 each separate the mixture into desired components by partially vaporizing the liquid mixture multiple times and partially condensing the resulting vapor multiple times, using the difference in the volatility of the substances. The heavy component separation column 1 and the C9 separation column 2 are tray columns.
The utility model discloses a separator of C9 fraction in coal-based methyl alcohol system propylene technology accessory substance, through the setting to component knockout tower 1 and C9 knockout tower 2, the realization is separated the C6+ hydrocarbon mixture in the coal-based methyl alcohol system propylene technology accessory substance, thereby separate C9 fraction wherein, thereby show the economic benefits who improves methyl alcohol system alkene technology (promptly, MTP technology), realize diversified production, extension coal chemical industry industrial chain, improve coal conversion added value.
In one embodiment, the separation device further comprises:
the methanol-to-propylene reactor 3 is used for receiving raw material methanol to perform a methanol-to-propylene reaction, and obtaining a reaction product at the bottom; preferably, the operating temperature of the methanol-to-propylene reactor 3 is 480-; operating at a pressure of 0.03 to 0.13MPa, preferably 0.06 to 0.10MPa, such as 0.08 MPa;
a gas-liquid separation device 4 for performing gas-liquid separation on the reaction product from the bottom of the methanol-to-propylene reactor 3 to remove water therein, so as to obtain a hydrocarbon mixture;
a compression device 7 for compressing the hydrocarbon mixture from the gas-liquid separation device 4 to separate and remove the gaseous C3-hydrocarbon mixture; preferably, the operating temperature of the compression device 7 is 40-96.2 ℃ and the operating pressure is 0.005-2.190 MPa.
A debutanizer column 5 for separating the liquid hydrocarbon mixture from the compression unit 7 to obtain a mixture of C4 olefins and C3-hydrocarbons as an overhead product and a mixture of C4+ hydrocarbons as a bottom product; preferably, the debutanizer column 5 is operated at a temperature of 81.3 to 161 deg.C, preferably 100 deg.C and 140 deg.C, such as 120 deg.C; an operating pressure of 2.18-2.22MPa, such as 2.20 MPa; a reflux ratio of 2.2 to 3.0, preferably 2.5 to 2.8, such as 2.6;
a dehexanizer 6 for separating the bottoms from the debutanizer 5 to obtain a mixture of C6+ hydrocarbons as bottoms which is fed to the heavies separator 1; preferably, the operating temperature of the dehexanizer 6 is between 87.3 and 157.4 ℃, preferably 100-; an operating pressure of 0.305 to 0.324MPa, preferably 0.310 to 0.320MPa, such as 0.315 MPa; the reflux ratio is from 5.0 to 6.1, preferably from 5.3 to 5.8, for example 5.5.
This setting makes MTP reaction system when producing propylene, can provide the raw materials for heavy ends knockout tower 1, makes the utility model discloses a separator can separate the C6+ hydrocarbon mixture in the coal-based methyl alcohol system propylene technology accessory substance to obtain C9 fraction.
As shown in FIG. 2, in one embodiment, the gas-liquid separation device 4 includes a pre-quench tower 41 and a quench tower 42;
the pre-chilling tower 41 is used for separating water from the reaction product of the methanol-to-propylene reactor 3 to obtain a crude hydrocarbon mixture; the operating temperature of the pre-quench tower 41 is 55-96.2 ℃, preferably 65-80 ℃, such as 72 ℃; the operating pressure is 0.018-0.020MPa, such as 0.019 MPa; the reaction product of the methanol to propylene reactor 3 is input from the middle upper part of the pre-chilling tower 41, the chilling water at the top of the pre-chilling tower 41 sprays the reaction product, and part of water vapor in the reaction product of the methanol to propylene reactor 3 is condensed along with the spraying of the chilling water, so that the water vapor is separated;
the chilling tower 42 is used for receiving the crude hydrocarbon mixture from the pre-chilling tower 41 and separating residual water in the crude hydrocarbon mixture to obtain a hydrocarbon mixture; the operating temperature of the quench tower 42 is in the range of 40 to 51 deg.C, preferably 43 to 48 deg.C, such as 45 deg.C; the operating pressure is 0.007-0.0091MPa, such as 0.008 MPa; the crude hydrocarbon mixture from the pre-chilling tower 41 is input from the middle upper part of the chilling tower 42, chilling water at the top of the chilling tower 42 sprays the crude hydrocarbon mixture, and partial water vapor in the crude hydrocarbon mixture from the pre-chilling tower 41 is condensed along with the chilling water spraying, so that the water vapor is separated.
The reaction product of the methanol to propylene reactor 3 contains byproducts such as cycloalkane, paraffin, aromatic hydrocarbon and light fraction besides olefin and process water, and the pre-chilling tower and the chilling tower mainly function to separate water from a hydrocarbon mixture in the reaction product of the methanol to propylene reactor 3.
In one embodiment, the C6+ hydrocarbon mixture in the coal-based methanol to propylene process byproduct comprises paraffins, naphthenes, alkenes, cycloalkenes, and C9+ heavy aromatics, preferably the C6+ hydrocarbon mixture has a C9+ heavy aromatics content of 10-20 wt%, preferably 12-16 wt%, such as 14 wt%.
The operation process of the separating device for the C9 fraction in the coal-based methanol-to-propylene process byproduct is shown in figure 2:
the methanol-to-propylene reactor 3 receives raw material methanol to perform a methanol-to-propylene reaction to obtain a reaction product; the reaction product of the methanol-to-propylene reactor 3 is input into a pre-chilling tower 41 in a gas-liquid separation device 4 to remove moisture, so as to obtain a crude hydrocarbon mixture; inputting the crude hydrocarbon mixture from the pre-chilling tower 41 into a chilling tower 42 in the gas-liquid separation device 4 for further removing moisture to obtain a hydrocarbon mixture; the hydrocarbon mixture from the quench tower 42 is fed to a compression unit 7 for compression to separate and remove the gaseous C3-hydrocarbon mixture; the liquid hydrocarbon mixture in the compression device 7 is input into a debutanizer 5 for separation to obtain C4 olefin and C3-hydrocarbon mixture as a top product and C4+ hydrocarbon mixture as a bottom product; the bottom product of the debutanizer 5 is input into a dehexanizer 6 for separation to obtain a C6+ hydrocarbon mixture as the bottom product; the bottom product of the dehexanizer 6 is input into the heavy component separation tower 1 for separation to obtain a C6-C9 hydrocarbon mixture as a top product and a C10+ hydrocarbon mixture as a bottom product; the top product of the heavy component separation tower 1 is input into a C9 separation tower 2 for separation, and a C6-C8 hydrocarbon mixture as the top product and a C9 fraction as the bottom product are obtained.
Examples
Utilize the utility model discloses a separation device separates the C6+ hydrocarbon mixture in the coal-based methanol-to-propylene technology accessory substance. Wherein,
(1) the C6+ hydrocarbon mixture in the byproduct of the coal-based methanol to propylene process was obtained under the following operating conditions, and the composition thereof is shown in table 1.
The operating conditions are as follows:
the operating temperature of the reactor for preparing propylene from methanol is 480 ℃, and the operating pressure is 0.08 MPa;
the operation temperature of a pre-chilling tower in the gas-liquid separation device is 72 ℃, and the operation pressure is 0.019 MPa; the operation temperature of a chilling tower in the gas-liquid separation device is 45 ℃, and the operation pressure is 0.008 MPa;
a compression device: the operation temperature is 60 ℃, and the operation pressure is 1.005 Mpa;
the operation temperature of the debutanizer is 120 ℃, the operation pressure is 2.20MPa, and the reflux ratio is 2.6;
the operation temperature of the dehexanizer is 120 ℃, the operation pressure is 0.315MPa, and the reflux ratio is 5.5.
TABLE 1 composition of C6+ hydrocarbon mixture in coal-based methanol to propylene process by-product
As can be seen from Table 1, the composition of the MTP process gasoline by-product (i.e., the mixture of C6+ hydrocarbons in the coal-based methanol to propylene process by-product) produced was 17.06 wt% paraffins (including 3.35 wt% normal paraffins and 13.71 wt% isoparaffins), 19.46 wt% alkenes, 11.30 wt% cycloalkenes, 14.67 wt% cycloalkanes, and 35.62 wt% aromatics. Wherein the cycloolefins are concentrated at C6-C8 and more at C7. The aromatics were concentrated in C7-C9, mostly C8-C9 (i.e., xylenes and trimethylbenzenes), in addition to 14.32 wt% heavy aromatics (i.e., C9 and above, including 12.13 wt% C9 aromatics, 1.85 wt% C10 aromatics, and 0.34 wt% C11 aromatics).
(2) The MTP process gasoline by-product produced in (1) (i.e., the C6+ hydrocarbon mixture in the coal-based methanol to propylene process by-product) was separated to separate a carbon nine fraction under the operating conditions as shown in table 2. The composition of the process stream during the separation is shown in table 3.
TABLE 2 operating conditions for the heavies splitter and the C9 splitter
Table 3 composition of process streams in separation process
As can be seen from Table 3, the hydrocarbon mixed component with the raw material of C6+ is separated by the heavy component separation tower, the lighter C6-C9 component is obtained from the top of the heavy component separation tower, the heavy component C10+ (containing a small amount of C9) is obtained at the bottom of the tower, and the separation effect is better; C6-C9 components at the top of the heavy component separation tower are separated by a C9 separation tower, light C6-C8 (without C9 components) is obtained at the top of the tower, C9 fractions (comprising C9 components and part of C8 components with higher boiling points) are obtained at the bottom of the tower, and the separation effect is good. The C9 fraction of the bottom product of the C9 splitter 2 finally obtained contains 52.32 wt% of C9 components and 46.89 wt% of higher boiling C8 components (the boiling point of the higher boiling C8 component is in the range of C9 components, which cannot be separated at present), wherein the C8 component contains 11 to 13 wt% of C8 cyclic olefins. The bottom product of the C9 separation tower 2 can be used as petroleum resin raw material and is C9 component, and the concentration of the C9 component is higher than 52 wt%; the C6-C8 hydrocarbon mixture as the overhead product of the C9 splitter 2 may be subjected to aromatic extraction or still sold as a gasoline blending component.
Claims (3)
1. A separation device for C9 fraction in coal-based methanol-to-propylene process byproducts is characterized by comprising:
the heavy component separation tower (1) is used for receiving and separating a C6+ hydrocarbon mixture in a byproduct in the process of preparing propylene from coal-based methanol to obtain a C6-C9 hydrocarbon mixture as a tower top product and a C10+ hydrocarbon mixture as a tower bottom product;
and the C9 separation tower (2) is used for separating the overhead product from the heavy component separation tower (1) to obtain a C6-C8 hydrocarbon mixture as the overhead product and a C9 fraction as the bottom product.
2. The separation device of claim 1, further comprising:
the methanol-to-propylene reactor (3) is used for receiving raw material methanol to perform a methanol-to-propylene reaction to obtain a reaction product;
a gas-liquid separation device (4) for performing gas-liquid separation on the reaction product from the methanol-to-propylene reactor (3) to remove water therein, thereby obtaining a hydrocarbon mixture;
a compression device (7) for compressing the hydrocarbon mixture from the gas-liquid separation device (4) to separate and remove the gaseous C3-hydrocarbon mixture;
a debutanizer (5) for separating the liquid hydrocarbon mixture from the compression unit (7) to obtain a mixture of C4 olefins and C3-hydrocarbons as an overhead product and a mixture of C4+ hydrocarbons as a bottom product;
a de-hexanizer (6) for separating the bottom product from the de-butaneizer (5) to obtain a mixture of C6+ hydrocarbons as the bottom product as feed to the heavies separation column (1).
3. A separation device according to claim 2, wherein the gas-liquid separation device (4) comprises a pre-quench tower (41) and a quench tower (42); the pre-chilling tower (41) is used for separating water from the reaction product of the methanol-to-propylene reactor (3) to obtain a crude hydrocarbon mixture; the chilling tower (42) is used for receiving the crude hydrocarbon mixture from the pre-chilling tower (41) and separating residual water in the crude hydrocarbon mixture to obtain the hydrocarbon mixture.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107879870A (en) * | 2017-11-29 | 2018-04-06 | 神华集团有限责任公司 | The separator and method of C9 cuts in process of preparing propylene from coal-based methanol accessory substance |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107879870A (en) * | 2017-11-29 | 2018-04-06 | 神华集团有限责任公司 | The separator and method of C9 cuts in process of preparing propylene from coal-based methanol accessory substance |
| CN107879870B (en) * | 2017-11-29 | 2023-10-20 | 神华集团有限责任公司 | Separation device and method for C9 fraction in byproduct of coal-based methanol-to-propylene process |
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