CN107879870A - The separator and method of C9 cuts in process of preparing propylene from coal-based methanol accessory substance - Google Patents
The separator and method of C9 cuts in process of preparing propylene from coal-based methanol accessory substance Download PDFInfo
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- CN107879870A CN107879870A CN201711221833.0A CN201711221833A CN107879870A CN 107879870 A CN107879870 A CN 107879870A CN 201711221833 A CN201711221833 A CN 201711221833A CN 107879870 A CN107879870 A CN 107879870A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 238000000034 method Methods 0.000 title claims abstract description 59
- 239000003245 coal Substances 0.000 title claims abstract description 45
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 30
- 239000000126 substance Substances 0.000 title abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 110
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 100
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 99
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 98
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 238000000926 separation method Methods 0.000 claims description 93
- 239000000047 product Substances 0.000 claims description 50
- 239000006227 byproduct Substances 0.000 claims description 41
- 239000007788 liquid Substances 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000007795 chemical reaction product Substances 0.000 claims description 19
- 230000006835 compression Effects 0.000 claims description 15
- 238000007906 compression Methods 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 14
- 150000001336 alkenes Chemical class 0.000 claims description 13
- 238000010791 quenching Methods 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 10
- 150000001925 cycloalkenes Chemical class 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 239000000470 constituent Substances 0.000 abstract 3
- 239000003502 gasoline Substances 0.000 description 7
- 238000009835 boiling Methods 0.000 description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 6
- 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
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 150000001924 cycloalkanes Chemical class 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- 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
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides the separator and method of C9 cuts in a kind of process of preparing propylene from coal-based methanol accessory substance, and the separator includes：Heavy constituent knockout tower, for receiving the C6+ hydrocarbon mixtures in process of preparing propylene from coal-based methanol accessory substance, and it is separated, obtain the C6 C9 hydrocarbon mixtures as overhead product and the C10+ hydrocarbon mixtures as tower bottom product；C9 knockout towers, for being separated to the overhead product from heavy constituent knockout tower, obtain the C6 C8 hydrocarbon mixtures as overhead product and the C9 cuts as tower bottom product.The separator and method, pass through the setting to heavy constituent knockout tower and C9 knockout towers, realization separates to the C6+ hydrocarbon mixtures in process of preparing propylene from coal-based methanol accessory substance, so as to isolate C9 cuts therein, so as to significantly improve the economic benefit of MTO technology, realize diversification production, extension Chemical Industry chain, raising coal conversion added value.
Description
Technical Field
The invention belongs to the technical field of preparing propylene from coal-based methanol, and particularly relates to a separation device and a separation method for C9 fraction in a byproduct in a process of preparing propylene from coal-based methanol.
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 cannot effectively separate the carbon nine fraction.
Disclosure of Invention
The invention aims to provide a separation device and a separation method for a C9 fraction in a coal-based methanol-to-propylene process byproduct, which can separate a C9 fraction from the coal-based methanol-to-propylene process byproduct to serve as a petroleum resin raw material and have a good separation effect.
In order to achieve the first purpose of the invention, 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.
Preferably, the C6+ hydrocarbon mixture in the coal-based methanol-to-propylene process byproduct comprises paraffin, naphthene, alkene, cycloolefine and C9+ heavy aromatic hydrocarbon.
Preferably, the C6+ hydrocarbon mixture has a C9+ heavy aromatics content of 10-20 wt%, preferably 12-16 wt%.
Preferably, the operating pressure of the heavies separation column is from 0.09 to 0.14MPa, preferably from 0.11 to 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 ℃; the reflux ratio is 1.0 to 1.4, preferably 1.1 to 1.2;
preferably, the operating pressure of the C9 splitter is in the range of from 0.09 to 0.14MPa, preferably from 0.11 to 0.12 MPa; the temperature at the top of the column is 110 ℃ to 115 ℃, preferably 112 ℃ for example; the bottom temperature is 150-; the reflux ratio is from 2.0 to 3.0, preferably from 2.5 to 2.8.
Preferably, the operating temperature of the methanol-to-propylene reactor is 480-;
the operation temperature of the pre-chilling tower is 55-96.2 ℃, and the operation pressure is 0.018-0.020 MPa;
the operation temperature of the chilling tower is 40-51 ℃, and the operation pressure is 0.007-0.0091 MPa;
the operating temperature of the compression device is 40-96.2 ℃, and the operating pressure is 0.005-2.190 MPa;
the operation temperature of the debutanizer is 81.3-161 ℃, the operation pressure is 2.18-2.22MPa, and the reflux ratio is 2.2-3.0;
the operation temperature of the dehexanizer is 87.3-157.4 ℃, the operation pressure is 0.305-0.324MPa, and the reflux ratio is 5.0-6.1.
In order to achieve the second object of the invention, the invention provides a method for separating the C9 fraction in the byproduct of the coal-based methanol-to-propylene process by using the separation device.
The invention has the beneficial effects that:
according to the separation device and method for the C9 fraction in the byproduct of the process for preparing propylene from coal-based methanol, disclosed by the invention, the C6+ hydrocarbon mixture in the byproduct of the process for preparing propylene from coal-based methanol is separated by arranging the component separation tower and the C9 separation tower, so that the C9 fraction is separated, the economic benefit of the process for preparing olefin from methanol (namely, MTP process) is obviously improved, the diversified production is realized, the industrial chain of coal chemical industry is prolonged, and the additional value of coal conversion is increased.
Drawings
FIG. 1 is a flow diagram of a separation device for C9 fraction in a byproduct of a coal-based methanol-to-propylene process of the invention in one embodiment;
fig. 2 is a flow chart of a separation device of a C9 fraction in a coal-based methanol to propylene process byproduct according to another embodiment of the invention.
Detailed Description
The technical solution and effects of the present invention will be further described below by way of specific embodiments. The following embodiments are merely illustrative of the present invention, and the present invention is not limited to the following embodiments or examples. Simple modifications of the invention applying the inventive concept are within the scope of the invention as claimed.
As shown in fig. 1, the separation device for the C9 fraction in the byproduct of the coal-based methanol-to-propylene process comprises 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.
According to the separation device and method for the C9 fraction in the byproduct of the coal-based methanol-to-propylene process, the C6+ hydrocarbon mixture in the byproduct of the coal-based methanol-to-propylene process is separated by arranging the component separation tower 1 and the C9 separation tower 2, so that the C9 fraction is separated, the economic benefit of the methanol-to-olefin process (namely, MTP process) is remarkably improved, diversified production is realized, the industrial chain of coal chemical industry is prolonged, and the additional value of coal conversion is improved.
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.
The arrangement enables the MTP reaction system to provide raw materials for the heavy component separation tower 1 while producing propylene, so that the separation device provided by the invention can separate C6+ hydrocarbon mixtures in byproducts in the process of preparing propylene from coal-based methanol, thereby obtaining C9 fractions.
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 separation device for the C9 fraction in the byproduct in the process of preparing propylene from coal-based methanol 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.
The invention also provides a method for separating the C9 fraction in the byproduct in the process of preparing propylene from coal-based methanol by using the separation device.
In one embodiment, the method comprises:
separating a C6+ hydrocarbon mixture in a byproduct in the process of preparing propylene from coal-based methanol by using a heavy component separation tower 1 to obtain a C6-C9 hydrocarbon mixture as a tower top product and a C10+ hydrocarbon mixture as a tower bottom product;
the overhead product from the heavy component separation column 1 is separated by means of a C9 separation column 2 to give a C6-C8 hydrocarbon mixture as overhead product and a C9 fraction as bottom product.
In one embodiment, the method further comprises:
a methanol-to-propylene reactor 3 is used for receiving raw material methanol to generate a methanol-to-propylene reaction, and a reaction product is obtained at the bottom;
the reaction product from the bottom of the methanol-to-propylene reactor 3 is subjected to water removal by a gas-liquid separation device 4 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;
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;
separating the bottom product from the debutanizer 5 by using a dehexanizer 6 to obtain a C6+ hydrocarbon mixture as the bottom product, namely a C6+ hydrocarbon mixture in the byproduct of the process for preparing propylene from coal-based methanol;
the bottoms of the dehexanizer 6 are received and separated by the heavies separation column 1.
In one embodiment, the method further comprises:
separating water from the reaction product from the bottom of the methanol-to-propylene reactor 3 by using the pre-quench tower 41 to obtain a crude hydrocarbon mixture;
the crude hydrocarbon mixture from the pre-quench tower 41 is received by the quench tower 42 and the residual water is separated to obtain a hydrocarbon mixture.
Examples
The separation device and the method of the invention are used for separating the C6+ hydrocarbon mixture in the byproduct of the coal-based methanol-to-propylene process. 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 (9)
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.
4. The separation device of any one of claims 1-3, wherein the C6+ hydrocarbon mixture in the coal-based methanol-to-propylene process byproduct comprises paraffins, naphthenes, alkenes, cycloalkenes, and C9+ heavy aromatics.
5. The separation device according to claim 4, characterized in that the C6+ hydrocarbon mixture has a content of C9+ heavy aromatics in the range of 10-20 wt.%, preferably 12-16 wt.%.
6. Separation device according to claim 1,
the operating pressure of the heavy component separation column (1) is between 0.09 and 0.14MPa, preferably between 0.11 and 0.12 MPa; the temperature at the top of the tower is 115-120 ℃; the temperature at the bottom of the tower is 180 ℃ and 185 ℃; the reflux ratio is from 1.0 to 1.4, preferably from 1.1 to 1.2.
7. The separation device according to any one of claims 1 to 3 or 5 to 6, wherein the operating pressure of the C9 separation column (2) is 0.09 to 0.14MPa, preferably 0.11 to 0.12 MPa; the temperature at the top of the tower is 110-115 ℃; the bottom temperature is 150-154 ℃; the reflux ratio is from 2.0 to 3.0, preferably from 2.5 to 2.8.
8. Separation device according to claim 3,
the operating temperature of the methanol-to-propylene reactor (3) is 480-;
the operation temperature of the pre-chilling tower (41) is 55-96.2 ℃, and the operation pressure is 0.018-0.020 MPa;
the operation temperature of the chilling tower (42) is 40-51 ℃, and the operation pressure is 0.007-0.0091 MPa;
the operating temperature of the compression device (7) is 40-96.2 ℃, and the operating pressure is 0.005-2.190 MPa;
the operation temperature of the debutanizer (5) is 81.3-161 ℃, the operation pressure is 2.18-2.22MPa, and the reflux ratio is 2.2-3.0;
the operation temperature of the dehexanizer (6) is 87.3-157.4 ℃, the operation pressure is 0.305-0.324MPa, and the reflux ratio is 5.0-6.1.
9. A method for separating a C9 fraction in a coal-based methanol-to-propylene process byproduct by using the separation device as claimed in any one of claims 1 to 8.
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| CN103864564A (en) * | 2014-02-24 | 2014-06-18 | 中国海洋石油总公司 | Technique for processing methanol-to-propylene by-products |
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| CN207632727U (en) * | 2017-11-29 | 2018-07-20 | 神华集团有限责任公司 | The separator of C9 fractions in process of preparing propylene from coal-based methanol by-product |
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