CN114470836B - Separation device and separation method for coal-to-ethanol liquid-phase product based on ethyl acetate cutting - Google Patents
Separation device and separation method for coal-to-ethanol liquid-phase product based on ethyl acetate cutting Download PDFInfo
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Abstract
The invention discloses a separation device and a separation method of a coal-to-ethanol liquid product based on cutting ethyl acetate. The coal-to-ethanol liquid phase product pipeline is used as a feeding pipeline of a light component removal tower, and a tower top material extraction pipeline of the light component removal tower is used as a feeding pipeline of an ethyl methyl ester separation tower; a tower bottom material extraction pipeline is used as a feeding pipeline of the methanol tower; taking a material extraction pipeline at the top of the ethanol tower as a first extraction pipeline of the methanol product, and extracting the methanol product meeting the purity requirement; the side discharge pipeline extracts an ethanol-water mixture with the ethanol concentration of 97.5 weight percent to obtain an ethanol product meeting the product requirement; the tower bottom material extraction pipeline is used as a feeding pipeline of the ethanol recovery tower. The method comprises the core steps of separating a coal-to-ethanol liquid-phase product by adopting a strategy of cutting ethyl acetate, optimizing the whole flow by utilizing an evolutionary algorithm, and obtaining the heat exchange relationship among towers. The invention obtains the ethanol, methanol, ethyl acetate and methyl acetate products meeting the national standard purity requirements, and has obvious energy-saving effect.
Description
Technical Field
The invention belongs to the technical field of rectification, relates to an energy-saving process for rectification and purification in a coal-to-ethanol liquid product separation process, and in particular relates to a separation device and a separation method for a coal-to-ethanol liquid product based on cutting ethyl acetate.
Background
Ethanol is widely applied to the fields of food manufacture, chemical industry, transportation and the like, and is an important basic chemical product. Moreover, ethanol can be used as an ideal green energy source with high octane number and an additive thereof due to the pollution-free characteristic of the ethanol as a vehicle fuel. Chinese petroleum resources are relatively insufficient, and coal resources are relatively rich. Based on the actual national conditions, the coal-to-ethanol production process has a natural competitive advantage in the field of ethanol preparation. Moreover, compared with biomass ethanol, coal ethanol has good energy-saving effect and economic competitiveness even under the condition of fluctuating raw material price.
The method is characterized in that the method comprises the steps of firstly dehydrating methanol to prepare dimethyl ether, then carrying out carbonylation reaction on the dimethyl ether to generate methyl acetate, and finally hydrogenating to obtain ethanol, and the method is considered as the most economical coal-to-ethanol process path at present because the process flow is relatively short, the equipment investment is low, the selectivity is high, the catalyst is low in cost and easy to obtain. The coal-to-ethanol technology has been developed continuously in the present year, and the whole process of producing 10 ten thousand tons of coal-to-ethanol in year is successfully opened up in 2017, 1 and 11 days. The reaction and the separation procedure of the coal-to-ethanol are optimized, the quality of the obtained ethanol product is improved, the energy consumption generated in the process is reduced, and a more novel and effective energy integration means is adopted, so that an important research direction of the coal-to-ethanol is formed.
The liquid phase product obtained by the coal-to-ethanol technology comprises, besides the target product ethanol, reactants which are not completely reacted in each step and various side reaction products, such as methanol, methyl acetate, ethyl acetate, water andalcohols, and the like. Although there are azeotropes of methyl acetate and methanol and azeotropes of ethyl acetate and methanol in this system, the boiling point difference between the azeotropes and pure substances is large, and the composition of these two azeotropes varies greatly with pressure, so that the above various substances can be separated one by a multi-column rectification process combining conventional rectification with pressure swing rectification.
The traditional separation process of the coal-to-ethanol liquid phase product has larger energy consumption, and the comprehensive energy consumption is generally more than 3 tons of saturated steam/ton of ethanol product, so that the new coal-to-ethanol rectification energy-saving method is particularly important.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a separation device and a separation method for a coal-to-ethanol liquid phase product based on cutting ethyl acetate, and the specific technical scheme is as follows:
the first aspect of the invention relates to a separation device for a coal-to-ethanol liquid-phase product based on cutting ethyl acetate, which comprises a light component removal tower T1, an ethanol tower T2, an ethanol recovery tower T3, a methanol tower T4, an ethyl ester normal pressure tower T5, an ethyl ester pressurizing tower T6, a methyl ethyl ester separation tower T7, a methyl ester pressurizing tower T8 and a methyl ester normal pressure tower T9, wherein the connection relation among the towers is as follows:
the coal-to-ethanol liquid-phase product pipeline S1 is used as a feeding pipeline of a light component removal tower T1, and a tower top material extraction pipeline S2 of the light component removal tower T1 is used as a feeding pipeline of a methyl ethyl ester separation tower T7; a tower bottom material extraction pipeline S3 is used as a feeding pipeline of a methanol tower T4;
the tower top material extraction pipeline S4 of the ethanol tower T2 is used as a first extraction pipeline of the methanol product, and the methanol product meeting the purity requirement is extracted; the side discharge pipeline S5 is used for extracting an ethanol-water mixture with the ethanol concentration of 97.5 weight percent, and an ethanol product meeting the product requirement can be obtained through a subsequent molecular sieve dehydration device; a tower bottom material extraction pipeline S6 is used as a feeding pipeline of the ethanol recovery tower T3;
an ethanol product meeting the requirements is extracted from a material extraction pipeline S7 at the top of the ethanol recovery tower T3; the bottom material extraction line S8 eliminates heavy components;
the tower top material extraction pipeline S9 of the methanol tower T4 is used as one of the feeding pipelines of the ethyl ester atmospheric tower T5, and the tower bottom material extraction pipeline S10 is used as the feeding pipeline of the ethanol tower T2;
the top material extraction pipeline S11 of the ethyl ester atmospheric tower T5 is used as a feeding pipeline of the ethyl ester pressurizing tower T6; the tower bottom material extraction pipeline S12 is used as a second methanol product extraction pipeline to extract a methanol product meeting the purity requirement;
the material extraction pipeline S13 at the top of the ethyl ester pressurizing tower T6 returns to the ethyl ester atmospheric tower T5 as a lateral line feeding pipeline thereof, so as to form a first circulation; the ethyl acetate product meeting the purity requirement is extracted from the tower bottom material extraction pipeline S14;
the tower top material extraction pipeline S15 of the methyl ethyl ester separation tower T7 is used as a feeding pipeline of the methyl ester pressurizing tower T8; a tower bottom material extraction pipeline S16 is used as one of feeding pipelines of the ethyl ester atmospheric tower T5; the products of the line S9 and the line S16 are mixed by a mixer M1 and then enter an ethyl ester atmospheric tower T5 through a line S21;
the tower top material extraction pipeline S17 of the methyl ester pressurizing tower T8 is used as a feeding pipeline of the methyl ester atmospheric tower T9; the tower bottom material extraction pipeline S18 extracts methyl acetate products meeting the purity requirement;
the tower top material extraction pipeline S19 of the methyl ester atmospheric tower T9 returns to the methyl ester pressurizing tower T8 as a side line feeding pipeline thereof to form a second circulation; the bottom material extraction line S20 is used as a third extraction line of the methanol product.
The ethanol recovery tower T3, the ethyl ester pressurizing tower T6 and the methyl ester pressurizing tower T8 supply heat to the methanol tower T4 together; the ethanol tower T2 supplies heat to the light component removal tower T1; the ethanol tower T2 and the methanol tower T4 supply heat to the ethyl ester atmospheric tower T5 together; the methanol tower T4 supplies heat to two towers, namely a methyl ethyl ester separation tower T7 and a methyl ester atmospheric tower T9.
As mentioned above, the coal-to-ethanol liquid phase product of the present invention comprises methanol, ethanol, methyl acetate, ethyl acetate, water andalcohols. Still further, the present invention is particularly suited for various combinations of such coal-to-ethanol liquid phase products.
Wherein the light component removing tower T1, the ethanol tower T2, the ethanol recovery tower T3, the methanol tower T4, the ethyl ester atmospheric tower T5, the ethyl ester pressurizing tower T6, the methyl ethyl ester separating tower T7, the methyl ester pressurizing tower T8 and the methyl ester atmospheric tower T9 are respectively and independently a packing rectifying tower or a tray rectifying tower.
A second aspect of the invention relates to a method for separating a coal-to-ethanol liquid phase product based on cut ethyl acetate, the coal-to-ethanol liquid phase product comprising methanol, ethanol, methyl acetate, ethyl acetate, water andalcohol separation method the separation device according to the first aspect of the present invention comprises the steps of:
the coal-to-ethanol liquid phase product enters a light component removal tower T1 through a coal-to-ethanol liquid phase product pipeline S1, and the composition of a tower top material extraction pipeline S2 comprises an azeotrope of methyl acetate and methanol and an azeotrope of ethyl acetate and methanol; the composition of the line S3 from the bottom stream comprises methanol, ethanol, ethyl acetate, water andalcohols;
the tower top material extraction pipeline S4 of the ethanol tower T2 extracts methanol products meeting the purity requirement; the side discharge pipeline S5 is used for extracting an ethanol-water mixture with the ethanol concentration of 97.5 weight percent, and an ethanol product meeting the product requirement can be obtained through a subsequent molecular sieve dehydration device; the composition of the bottom material extraction line S6 comprises ethanol, water andalcohols;
an ethanol product meeting the requirements is extracted from a material extraction pipeline S7 at the top of the ethanol recovery tower T3; the bottom material extraction pipeline S8 discharges waterHeavy components of alcohols;
the composition of the overhead offtake line S9 of the methanol column T4 comprises an azeotrope of methyl acetate and methanol; the composition of the bottom material extraction line S10 comprises methanol, ethanol, water andalcohols;
the composition of the overhead extraction line S11 of the ethyl acetate atmospheric tower T5 comprises an azeotrope of ethyl acetate and methanol; a tower bottom material extraction pipeline S12 extracts methanol products meeting the purity requirement;
the material extraction line S13 at the top of the ethyl ester pressurizing tower T6 circulates to the ethyl ester normal pressure tower T5 to form an azeotrope containing ethyl acetate and methanol; the ethyl acetate product meeting the purity requirement is extracted from the tower bottom material extraction pipeline S14;
the composition of the overhead material extraction line S15 of the methyl ethyl acetate separation column T7 comprises an azeotrope of methyl acetate and methanol; the bottom material extraction pipeline S16 is used as one of the feeding pipelines of the ethyl ester atmospheric tower T5 to form an azeotrope containing ethyl acetate and methanol; the products of the line S9 and the line S16 are mixed by a mixer M1 and then enter an ethyl ester atmospheric tower T5 through a line S21;
the composition of the overhead offtake line S17 of the methyl ester pressurization column T8 comprises an azeotrope of methyl acetate and methanol; the tower bottom material extraction pipeline S18 extracts methyl acetate products meeting the purity requirement;
the tower top material extraction line S19 of the methyl ester atmospheric tower T9 is recycled to the methyl ester pressurizing tower T8 to form an azeotrope containing methyl acetate and methanol; the bottom material extraction pipeline S20 extracts methanol products meeting the purity requirement.
The material flows in the tower top material extraction pipeline S7 of the ethanol recovery tower T3, the tower top material extraction pipeline S13 of the ethyl ester pressurizing tower T6 and the tower top material extraction pipeline S17 of the methyl ester pressurizing tower T8 enter a tower kettle reboiler of the methanol tower T4 in a gas phase mode for condensation heat exchange; the material flow in the tower top material extraction pipeline S4 of the ethanol tower T2 enters a tower kettle reboiler of the light component removal tower T1 in a gas phase mode for condensation heat exchange; the material flows in the tower top material extraction pipeline S4 of the ethanol tower T2 and the tower top material extraction pipeline S9 of the methanol tower T4 enter a tower kettle reboiler of the ethyl ester atmospheric tower T5 in a gas phase mode for condensation heat exchange; the material flow in the tower top material extraction pipeline S9 of the methanol tower T4 enters a tower kettle reboiler of the methyl ethyl ester separation tower T7 and a tower kettle reboiler of the methyl ester atmospheric tower T9 in a gas phase mode for condensation heat exchange.
Further, the separation method will take off an ethanol-water mixture having an ethanol concentration of 97.5wt% from a side offtake line S5 of the ethanol column T2 in the form of a gas phase, entering the subsequent molecular sieve dehydration section.
There are a wide variety of separation parameters that are available to meet the separation task. One group of technological parameters capable of smoothly running is that the reflux ratio of the light component removal tower T1 is 4.4-6.0, the operating pressure is 101-110kpa, and the preferred operating pressure is normal pressure; the reflux ratio of the ethanol tower T2 is 5.0-5.5, and the operating pressure is 250-300kpa; the reflux ratio of the ethanol recovery tower T3 is 1.0-2.0, and the operating pressure is 280-300kpa; the reflux ratio of the methanol tower T4 is 4.0-5.0, and the operating pressure is 180-200kpa; the reflux ratio of the ethyl ester atmospheric tower T5 is 7.0-9.5, the operation pressure is 101-110kpa, and the preferred operation pressure is normal pressure; the reflux ratio of the ethyl ester pressurizing tower T6 is 1.5-2.0, and the operation pressure is 600-700kpa; the reflux ratio of the methyl ethyl ester separation tower T7 is 5.0-6.0, the operation pressure is 101-110kpa, and the preferred operation pressure is normal pressure; the reflux ratio of the methyl ester pressurizing tower T8 is 2.33-4.0, and the operating pressure is 765-800kpa; the reflux ratio of the methyl ester atmospheric tower T9 is 1.12-1.5, the operating pressure is 101-140kpa, and the preferred operating pressure is atmospheric.
The theoretical plate number of the light component removal tower is 90-102; the theoretical plate number of the ethanol tower is 181-220; the theoretical plate number of the ethanol recovery tower is 15-25; the theoretical plate number of the methanol tower is 120-150; the theoretical plate number of the ethyl ester atmospheric tower is 80-100; the theoretical plate number of the ethyl ester pressurizing tower is 37-50; the theoretical plate number of the methyl ethyl ester separation tower is 60-90; the theoretical plate number of the methyl ester pressurizing tower is 35-70; the theoretical plate number of the methyl ester atmospheric tower is 30-65.
The mass fraction of the separated methanol product is more than or equal to 99.9%, the mass fraction of the separated ethanol product is more than or equal to 99.8%, the mass fraction of the separated methyl acetate product is more than or equal to 99.9%, and the mass fraction of the separated ethyl acetate product is more than or equal to 99.9%.
The invention is characterized in that:
1. ethanol, methanol, ethyl acetate and methyl acetate products with higher quality purity than conventional separation schemes can be obtained.
2. The technology of the invention is different from the existing separation method in terms of the separation strategy, not the conventional method which takes ethanol and methanol as the focus, but the method which takes cut ethyl acetate as the focus, firstly, all methyl acetate and part of ethyl acetate are taken out from the top of the tower through a small part of methanol in a rectification process in a light component removal tower T1, and the part of ethyl acetate and methyl acetate only need to be separated from the small part of methanol; the other part of ethyl acetate is carried out from the top of the methanol tower T4 by a small part of methanol, and then is mixed with a material flow from the bottom of the methyl ethyl ester separation tower and enters the subsequent separation step, namely enters an ethyl ester normal pressure tower and an ethyl ester high pressure tower for pressure swing rectification separation.
3. After the optimization of the evolutionary algorithm, the energy-saving effect is remarkable, the comprehensive energy consumption is 1.98 tons of steam/ton of ethanol products, and the comprehensive energy consumption is far smaller than that of the traditional separation flow of the coal-to-ethanol liquid-phase products.
Description of the drawings:
FIG. 1 is a schematic flow diagram of a separation apparatus and separation method for a coal-to-liquids ethanol product based on cutting ethyl acetate;
wherein, the light component removing tower-T1, the ethanol tower-T2, the ethanol recovery tower-T3, the methanol tower-T4, the ethyl ester atmospheric tower-T5, the ethyl ester pressurizing tower-T6, the methyl ethyl ester separating tower-T7, the methyl ester pressurizing tower-T8 and the methyl ester atmospheric tower-T9.
Detailed Description
The following describes the technical scheme of the present invention with reference to the drawings and examples, but the examples are not intended to limit the scope of the present invention.
As shown in fig. 1, the methanol product related to the invention is extracted from the tower top of an ethanol tower T3, the tower bottom of an ethyl ester atmospheric tower T5 and the tower bottom of a methyl ester atmospheric tower T9; the ethanol crude product is extracted from the gas phase of the side line of the ethanol tower T2 and enters a subsequent molecular sieve dehydration device; the refined ethanol product is extracted from the top of the ethanol recovery tower T3; methyl acetate product is extracted from the tower kettle of a methyl ester pressurizing tower T8; ethyl acetate product is extracted from the T6 tower kettle.
Example 1:
in this example, the mass composition of the coal ethanol liquid phase product was: methyl acetate 3.4%, methanol 41.7%, ethyl acetate 1.4%, n-propanol 0.1% and water 1%. The reflux ratio r=4.40 of the light component removal column T1, the operating pressure is 101kpa, and the theoretical plate number is 102; ethanol column T2 reflux ratio r=5.50, operating pressure of 285kpa, theoretical plate number of 181; the reflux ratio r=1.23 of the ethanol recovery column T3, the operating pressure was 300kpa, and the theoretical plate number was 20; the reflux ratio r=4.07 of the methanol tower T4, the operating pressure is 190kpa, and the theoretical plate number is 138; the reflux ratio r=9.50 of the ethyl ester atmospheric tower T5, the operating pressure is 101kpa, and the theoretical plate number is 86; the ethyl ester pressurizing column T6 has reflux ratio r=1.76, operating pressure of 620kpa and theoretical plate number of 37; the reflux ratio R=5.56 of the ethyl methyl ester separation tower, the operating pressure is 101kpa, and the theoretical plate number is 90; methyl ester pressurizing tower reflux ratio R=2.33, operating pressure of 765kpa and theoretical plate number of 40; methyl ester atmospheric tower reflux ratio r=1.12, operating pressure 108kpa, theoretical plate number 33. The purity of the obtained methanol product is more than or equal to 99.9%, the purity of the ethanol product is more than or equal to 99.8%, the purity of the methyl acetate product is more than or equal to 99.9%, the purity of the ethyl acetate product is more than or equal to 99.9%, all the recovery rates of the products meet the national standard requirement or the front-end reaction process recycling requirement, wherein the recovery rate of the methanol is more than 99.98%, the recovery rate of the ethanol is 99.89%, the recovery rate of the methyl acetate is 99.99%, the recovery rate of the ethyl acetate is 99.53%, and the comprehensive energy consumption is 1.983 tons of saturated steam per ton of ethanol product. If the same separation effect is achieved in the existing technology, the comprehensive energy consumption is generally greater than 3 tons of saturated steam/ton of ethanol product.
Example 2:
in this example, the mass composition of the coal-to-ethanol liquid product was the same as in example 1. The reflux ratio r=6.00 of the light component removal column T1, the operating pressure is 110kpa, and the theoretical plate number is 90; ethanol column T2 reflux ratio r=5.00, operating pressure 250kpa, theoretical plate number 220; the reflux ratio r=1.00 of the ethanol recovery column T3, the operating pressure is 300kpa, and the theoretical plate number is 15; the reflux ratio r=4.00 of the methanol tower T4, the operating pressure is 200kpa, and the theoretical plate number is 120; the reflux ratio r=7.00 of the ethyl ester atmospheric tower T5, the operating pressure is 101kpa, and the theoretical plate number is 100; the ethyl ester pressurizing tower T6 has reflux ratio R=2.00, operating pressure of 600kpa and theoretical plate number of 40; the reflux ratio R=5.00 of the ethyl methyl ester separation tower, the operating pressure is 101kpa, and the theoretical plate number is 60; methyl ester pressurization tower reflux ratio r=3.00, operating pressure 800kpa, theoretical plate number 40; methyl ester atmospheric tower reflux ratio r=1.50, operating pressure 110kpa, theoretical plate number 30. The purity of the obtained methanol product is more than or equal to 99.9%, the purity of the ethanol product is more than or equal to 99.8%, the purity of the methyl acetate product is more than or equal to 99.9%, the purity of the ethyl acetate product is more than or equal to 99.9%, all the recovery rates of the products meet the national standard requirement or the front-end reaction process recycling requirement, wherein the recovery rate of the methanol is more than 99.99%, the recovery rate of the ethanol is 99.89%, the recovery rate of the methyl acetate is 99.99%, the recovery rate of the ethyl acetate is 99.37%, and the comprehensive energy consumption is 2.021 tons of saturated steam per ton of ethanol product. If the same separation effect is achieved in the existing technology, the comprehensive energy consumption is generally greater than 3 tons of saturated steam/ton of ethanol product.
Example 3:
in this example, the mass composition of the coal-to-ethanol liquid product was the same as in example 1. The reflux ratio r=5.70 of the light component removal column T1, the operating pressure is 110kpa, and the theoretical plate number is 90; ethanol column T2 reflux ratio r=5.00, operating pressure 250kpa, theoretical plate number 210; the reflux ratio r=2.00 of the ethanol recovery tower T3, the operating pressure is 300kpa, and the theoretical plate number is 20; the reflux ratio r=5.00 of the methanol tower T4, the operating pressure is 200kpa, and the theoretical plate number is 150; the reflux ratio r=9.00 of the ethyl ester atmospheric tower T5, the operating pressure is 110kpa, and the theoretical plate number is 100; the ethyl ester pressurizing column T6 has a reflux ratio r=1.50, an operating pressure of 700kpa and a theoretical plate number of 50; the reflux ratio of the ethyl methyl ester separation tower is R=6.00, the operating pressure is 110kpa, and the theoretical plate number is 60; methyl ester pressurization tower reflux ratio r=4.00, operating pressure 800kpa, theoretical plate number 70; methyl ester atmospheric tower reflux ratio r=1.50, operating pressure 140kpa, theoretical plate number 30. The purity of the obtained methanol product is more than or equal to 99.9%, the purity of the ethanol product is more than or equal to 99.8%, the purity of the methyl acetate product is more than or equal to 99.9%, the purity of the ethyl acetate product is more than or equal to 99.9%, all the recovery rates of the products meet the national standard requirement or the front-end reaction process recycling requirement, wherein the recovery rate of the methanol is more than 99.99%, the recovery rate of the ethanol is 99.90%, the recovery rate of the methyl acetate is 99.99%, the recovery rate of the ethyl acetate is 99.25%, and the comprehensive energy consumption is 2.106 tons of saturated steam per ton of ethanol product. If the same separation effect is achieved in the existing technology, the comprehensive energy consumption is generally greater than 3 tons of saturated steam/ton of ethanol product.
Example 4:
in this example, the mass composition of the coal-to-ethanol liquid product was the same as in example 1. The reflux ratio r=5.70 of the light component removal column T1, the operating pressure is 101kpa, and the theoretical plate number is 100; ethanol column T2 reflux ratio r=5.20, operating pressure 300kpa, theoretical plate number 200; the reflux ratio r=1.00 of the ethanol recovery column T3, the operating pressure is 280kpa, and the theoretical plate number is 25; the reflux ratio r=5.00 of the methanol tower T4, the operating pressure is 180kpa, and the theoretical plate number is 120; the reflux ratio r=7.50 of the ethyl ester atmospheric tower T5, the operating pressure is 101kpa, and the theoretical plate number is 80; the ethyl ester pressurizing tower T6 has reflux ratio R=2, operating pressure of 650kpa and theoretical plate number of 40; the reflux ratio R=5.00 of the ethyl methyl ester separation tower, the operating pressure is 110kpa, and the theoretical plate number is 70; methyl ester pressurization tower reflux ratio r=4.00, operating pressure 800kpa, theoretical plate number 35; methyl ester atmospheric tower reflux ratio r=1.50, operating pressure 130kpa, theoretical plate number 65. The purity of the obtained methanol product is more than or equal to 99.9%, the purity of the ethanol product is more than or equal to 99.8%, the purity of the methyl acetate product is more than or equal to 99.9%, the purity of the ethyl acetate product is more than or equal to 99.9%, all the recovery rates of the products meet the national standard requirement or the front-end reaction process recycling requirement, wherein the recovery rate of the methanol is more than 99.98%, the recovery rate of the ethanol is 99.91%, the recovery rate of the methyl acetate is 99.99%, the recovery rate of the ethyl acetate is 99.67%, and the comprehensive energy consumption is 2.107 tons of saturated steam per ton of ethanol product. If the same separation effect is achieved in the existing technology, the comprehensive energy consumption is generally greater than 3 tons of saturated steam/ton of ethanol product.
Claims (3)
1. Separation device based on coal-to-ethanol liquid phase product of cutting ethyl acetate, characterized by, including light ends removal tower (T1), ethanol tower (T2), ethanol recovery tower (T3), methanol tower (T4), ethyl ester atmospheric tower (T5), ethyl ester pressurization tower (T6), methyl ethyl ester separation tower (T7), methyl ester pressurization tower (T8) and methyl ester atmospheric tower (T9), the relation of connection between each tower is as follows:
a coal-to-ethanol liquid phase product pipeline (S1) is used as a feeding pipeline of a light component removal tower (T1), and a tower top material extraction pipeline (S2) of the light component removal tower (T1) is used as a feeding pipeline of a methyl ethyl ester separation tower (T7); a tower bottom material extraction pipeline (S3) is used as a feeding pipeline of the methanol tower (T4);
the tower top material extraction pipeline (S4) of the ethanol tower (T2) is used as a first extraction pipeline of the methanol product, and the methanol product meeting the purity requirement is extracted; an ethanol-water mixture with the ethanol concentration of 97.5 weight percent is extracted from a side line discharging pipeline (S5), and an ethanol product meeting the product requirement can be obtained through a subsequent molecular sieve dehydration device; a tower bottom material extraction pipeline (S6) is used as a feeding pipeline of the ethanol recovery tower (T3);
an ethanol product meeting the requirements is extracted from a material extraction pipeline (S7) at the top of the ethanol recovery tower (T3); a tower bottom material extraction pipeline (S8) eliminates heavy components;
the tower top material extraction pipeline (S9) of the methanol tower (T4) is used as one of the feeding pipelines of the ethyl ester atmospheric tower (T5), and the tower bottom material extraction pipeline (S10) is used as the feeding pipeline of the ethanol tower (T2);
a tower top material extraction pipeline (S11) of the ethyl ester atmospheric tower (T5) is used as a feeding pipeline of the ethyl ester pressurizing tower (T6); a tower bottom material extraction pipeline (S12) is used as a second methanol product extraction pipeline to extract a methanol product meeting the purity requirement;
the tower top material extraction pipeline (S13) of the ethyl ester pressurizing tower (T6) returns to the ethyl ester atmospheric tower (T5) as a side line feeding pipeline thereof, so as to form a first circulation; the ethyl acetate product meeting the purity requirement is extracted from the tower bottom material extraction pipeline (S14);
the tower top material extraction pipeline (S15) of the methyl ethyl ester separation tower (T7) is used as a feeding pipeline of the methyl ester pressurizing tower (T8); the bottom material extraction pipeline (S16) is used as one of the feeding pipelines of the ethyl ester atmospheric tower (T5); the products of the pipeline (S9) and the pipeline (S16) are mixed by a mixer (M1) and then enter an ethyl ester atmospheric tower (T5) from a pipeline (S21);
the top material extraction pipeline (S17) of the methyl ester pressurizing tower (T8) is used as a feeding pipeline of a methyl ester atmospheric tower (T9); a tower bottom material extraction pipeline (S18) extracts methyl acetate products meeting the purity requirement;
the tower top material extraction pipeline (S19) of the methyl ester atmospheric tower (T9) returns to the methyl ester pressurizing tower (T8) as a side line feeding pipeline thereof, so as to form a second circulation; a tower bottom material extraction pipeline (S20) is used as a third methanol product extraction pipeline;
the ethanol recovery tower (T3), the ethyl ester pressurizing tower (T6) and the methyl ester pressurizing tower (T8) supply heat to the methanol tower (T4); the ethanol tower (T2) supplies heat to the dehydrogenation tower (T1); the ethanol tower (T2) and the methanol tower (T4) supply heat to the ethyl ester atmospheric tower (T5); the methanol tower (T4) supplies heat to the methyl ethyl ester separation tower (T7) and the methyl ester atmospheric tower (T9).
2. The separation device for the liquid-phase product of ethanol from coal based on cutting ethyl acetate according to claim 1, wherein the light component removing tower (T1), the ethanol tower (T2), the ethanol recovery tower (T3), the methanol tower (T4), the ethyl ester atmospheric tower (T5), the ethyl ester pressurizing tower (T6), the ethyl methyl ester separating tower (T7), the methyl ester pressurizing tower (T8) and the methyl ester atmospheric tower (T9) are respectively independent and are all packed rectifying towers or tray rectifying towers.
3. Using a base as claimed in any one of claims 1 to 2The separation method of the separation device of the coal-to-ethanol liquid phase product for cutting the ethyl acetate is characterized in that the coal-to-ethanol liquid phase product comprises methanol, ethanol, methyl acetate, ethyl acetate, water and C 3+ Alcohols; the method comprises the following steps:
the coal-to-ethanol liquid phase product enters a light component removal tower (T1) through a coal-to-ethanol liquid phase product pipeline (S1), and the composition of a tower top material extraction pipeline (S2) comprises an azeotrope of methyl acetate and methanol and an azeotrope of ethyl acetate and methanol; the composition of the bottom material extraction pipeline (S3) comprises methanol, ethanol, ethyl acetate, water and C 3+ Alcohols;
a tower top material extraction pipeline (S4) of the ethanol tower (T2) extracts methanol products meeting the purity requirement; an ethanol-water mixture with the ethanol concentration of 97.5 weight percent is extracted from a side line discharging pipeline (S5), and an ethanol product meeting the product requirement can be obtained through a subsequent molecular sieve dehydration device; the composition of the bottom material extraction pipeline (S6) comprises ethanol, water and C 3+ Alcohols;
an ethanol product meeting the requirements is extracted from a material extraction pipeline (S7) at the top of the ethanol recovery tower (T3); the bottom material extraction pipeline (S8) discharges water and C 3+ Heavy components of alcohols;
the composition of the overhead extraction line (S9) of the methanol column (T4) comprises an azeotrope of methyl acetate and methanol; the composition of the bottom material extraction pipeline (S10) comprises methanol, ethanol, water and C 3+ Alcohols;
the composition of the overhead material extraction line (S11) of the ethyl acetate atmospheric tower (T5) comprises an azeotrope of ethyl acetate and methanol; a tower bottom material extraction pipeline (S12) extracts methanol products meeting the purity requirement;
the tower top material extraction pipeline (S13) of the ethyl ester pressurizing tower (T6) is recycled to the ethyl ester normal pressure tower (T5) to form an azeotrope containing ethyl acetate and methanol; the ethyl acetate product meeting the purity requirement is extracted from the tower bottom material extraction pipeline (S14);
the composition of the overhead material extraction line (S15) of the methyl ethyl acetate separation column (T7) comprises an azeotrope of methyl acetate and methanol; the bottom material extraction pipeline (S16) is used as one of the feeding pipelines of the ethyl ester atmospheric tower (T5) to form an azeotrope containing ethyl acetate and methanol; the products of the pipeline (S9) and the pipeline (S16) are mixed by a mixer (M1) and then enter an ethyl ester atmospheric tower (T5) from a pipeline (S21);
the composition of the overhead feed withdrawal line (S17) of the methyl ester pressurizing column (T8) comprises an azeotrope of methyl acetate and methanol; a tower bottom material extraction pipeline (S18) extracts methyl acetate products meeting the purity requirement;
the top material extraction line (S19) of the methyl ester atmospheric tower (T9) is recycled to the methyl ester pressurizing tower (T8) to form an azeotrope containing methyl acetate and methanol; a tower bottom material extraction pipeline (S20) extracts methanol products meeting the purity requirement;
the material flows in the tower top material extraction pipeline (S7) of the ethanol recovery tower (T3), the tower top material extraction pipeline (S13) of the ethyl ester pressurizing tower (T6) and the tower top material extraction pipeline (S17) of the methyl ester pressurizing tower (T8) enter a tower kettle reboiler of the methanol tower (T4) in a gas phase form for condensation heat exchange; the material flow in the tower top material extraction pipeline (S4) of the ethanol tower (T2) enters a tower kettle reboiler of the dehydrogenation tower (T1) in a gas phase form for condensation heat exchange; the material flows in the tower top material extraction pipeline (S4) of the ethanol tower (T2) and the tower top material extraction pipeline (S9) of the methanol tower (T4) enter a tower kettle reboiler of the ethyl ester atmospheric tower (T5) in a gas phase form for condensation heat exchange; the material flow in the tower top material extraction pipeline (S9) of the methanol tower (T4) enters a tower kettle reboiler of the methyl ethyl ester separation tower (T7) and a tower kettle reboiler of the methyl ester atmospheric tower (T9) in a gas phase form for condensation heat exchange;
ethanol-water mixture with ethanol concentration of 97.5wt% is extracted from a side discharge pipeline (S5) of an ethanol tower (T2) in a gas phase form and enters a subsequent molecular sieve dehydration section;
the reflux ratio of the light component removal tower (T1) is 4.4-6.0, the operation pressure is 101-110kpa, and the preferable operation pressure is normal pressure; the reflux ratio of the ethanol tower (T2) is 5.0-5.5, and the operating pressure is 250-300kpa; the reflux ratio of the ethanol recovery tower (T3) is 1.0-2.0, and the operating pressure is 280-300kpa; the reflux ratio of the methanol tower (T4) is 4.0-5.0, and the operation pressure is 180-200kpa; the reflux ratio of the ethyl ester atmospheric tower (T5) is 7.0-9.5, the operation pressure is 101-110kpa, and the preferred operation pressure is normal pressure; the reflux ratio of the ethyl ester pressurizing tower (T6) is 1.5-2.0, and the operation pressure is 600-700kpa; the reflux ratio of the methyl ethyl ester separation tower (T7) is 5.0-6.0, the operation pressure is 101-110kpa, and the preferable operation pressure is normal pressure; the reflux ratio of the methyl ester pressurizing tower (T8) is 2.33-4.0, and the operating pressure is 765-800kpa; the reflux ratio of the methyl ester atmospheric tower (T9) is 1.12-1.5, the operating pressure is 101-140kpa, and the preferred operating pressure is atmospheric.
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