CN111825529B - Method for separating ethylene glycol - Google Patents
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- CN111825529B CN111825529B CN202010728145.9A CN202010728145A CN111825529B CN 111825529 B CN111825529 B CN 111825529B CN 202010728145 A CN202010728145 A CN 202010728145A CN 111825529 B CN111825529 B CN 111825529B
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Abstract
The invention discloses a method for separating ethylene glycol. The separation method comprises the following steps: the method comprises the steps of cooling and condensing a gas material containing hydrogen, water, methanol and glycol obtained by a dimethyl oxalate hydrogenation unit step by step to obtain a crude glycol liquid material and a crude methanol liquid material, wherein at least one of the crude glycol liquid material and the crude methanol liquid material is partially gasified before being sent into a separation unit; the heat source for partial gasification is preferably a gas material obtained by a dimethyl oxalate hydrogenation unit. The method of the invention saves the energy consumption of the reaction gas condensation and the rectification separation tower.
Description
Technical Field
The invention belongs to the technical field of ethylene glycol separation, and particularly relates to a method for separating ethylene glycol.
Background
Ethylene Glycol (EG) is used for the production of polyester resins, antifreeze solutions and the like, of which about 95% is used for the production of polyester fiber products. The preparation method of the ethylene glycol can be divided into a petroleum route method and a non-petroleum route method, the non-petroleum route technology for preparing the ethylene glycol by using the coal synthesis gas has the advantages of less waste discharge, low energy consumption, low cost and the like, and is a better choice for the energy conditions of relatively rich coal resources, less oil and gas shortage in China, so that the technology for preparing the ethylene glycol from the coal is greatly developed in China in recent years.
The current common process for preparing ethylene glycol from coal-based syngas (coal-based ethylene glycol for short) comprises a synthesis step and a post-treatment step, wherein the synthesis step is to prepare pure H from syngas (for example, coal gasification 2 And CO gas, namely synthesis gas), preparing methyl nitrite, synthesizing dimethyl oxalate through CO gas-phase catalytic coupling, and preparing ethylene glycol through dimethyl oxalate hydrogenation, wherein the reaction process is shown in the following reaction equation:
2NO+1/2O 2 +2CH 3 OH＝2CH 3 ONO(MN)+H 2 O
2CH 3 ONO+2CO＝CH 3 OOCCOOCH 3 (DMO)+2NO
CH 3 OOCCOOCH 3 +4H 2 ＝(CH 2 OH) 2 (EG)+2CH 3 OH；
the post-treatment step includes steps of regeneration of Methyl Nitrite (MN), purification of Ethylene Glycol (EG), and the like.
However, the reaction of the coal-to-ethylene glycol process is complex, excessive side reactions cause too many impurities in the ethylene glycol product, the components are complex and difficult to separate, and the separation energy consumption is high. The energy consumption of the device for preparing the ethylene glycol from the coal is reduced, the economic and technical competitiveness of the process is improved, and the method is a necessary way for the development of the process for preparing the ethylene glycol from the coal.
Disclosure of Invention
The invention provides a method for separating ethylene glycol, which comprises the following steps: cooling and condensing the gas material obtained by the dimethyl oxalate hydrogenation unit step by step to obtain a crude glycol liquid material and a crude methanol liquid material, wherein at least one of the crude glycol liquid material and the crude methanol liquid material is partially gasified before being sent to the separation unit;
the gaseous feed contains hydrogen, water, methanol and ethylene glycol.
According to an embodiment of the invention, the source of heat for the partial gasification may be selected from at least one of steam, a gas feed from a separation column overhead in a separation unit, a gas feed from a dimethyl oxalate hydrogenation unit. Illustrative is the gaseous feed from a dimethyl oxalate hydrogenation unit.
According to an embodiment of the invention, the crude methanol liquid material and/or the crude ethylene glycol liquid material is heated in a heat exchange manner with at least one heat source of steam, a gas material at the top of a separation tower in the separation unit and a gas material obtained by a dimethyl oxalate hydrogenation unit before being sent into the separation unit, so that the materials are partially gasified.
Preferably, the temperature difference between the crude methanol liquid feed and/or the crude ethylene glycol liquid feed and the heat source is 50-200 ℃, such as 100-.
Preferably, the temperature of the crude methanol liquid stream and/or the crude ethylene glycol liquid stream after the heat exchange attemperation is 30 to 160 deg.C, such as 50 to 150 deg.C, illustratively 80 deg.C, 90 deg.C, 100 deg.C, 110 deg.C, 120 deg.C, 130 deg.C, 140 deg.C, 150 deg.C, 160 deg.C, relative to the temperature of the crude methanol liquid stream and/or the crude ethylene glycol liquid stream prior to the heat exchange attemperation.
More preferably, the temperature of the crude methanol liquid stream and/or the crude ethylene glycol liquid stream after heat exchange for warming is 70-170 deg.C, such as 120-160 deg.C, exemplary 120 deg.C, 130 deg.C, 140 deg.C, 145 deg.C, 150 deg.C, 155 deg.C, 160 deg.C.
Preferably, the separation column overhead gas stream is a pressurized overhead gas stream. Further, the pressurization may be achieved by a compressor.
Preferably, the temperature of the gas material obtained from the dimethyl oxalate hydrogenation unit is 180-210 ℃, such as 185-205 ℃, exemplarily 180 ℃, 185 ℃, 190 ℃, 195 ℃, 200 ℃, 205 ℃ and 210 ℃.
Preferably, the pressure of the gaseous feed from the dimethyl oxalate hydrogenation unit is 2.5-3.0MPa, such as 2.6-2.9MPa, exemplary 2.5MPa, 2.6MPa, 2.7MPa, 2.8MPa, 2.9MPa, 3.0 MPa.
According to the embodiment of the invention, the dimethyl oxalate hydrogenation unit is a reaction unit in the preparation of ethylene glycol from coal-based synthesis gas.
According to an embodiment of the present invention, the process of hydrogenating dimethyl oxalate comprises: dimethyl oxalate (DMO) is subjected to catalytic hydrogenation reaction at the temperature of 180-225 ℃ and under the pressure of 2.5-3.0MPa to obtain a reaction product containing ethylene glycol. Wherein the reaction product further contains unreacted raw material hydrogen and by-products. For example, the by-product contains at least one of Butanediol (BDO), ethanol, Propylene Glycol (PG), Methyl Glycolate (MG), water, and the like. Further, the reaction product may contain inert gases such as nitrogen and/or methane. Illustratively, the reaction products include, in mass percent: 5 to 25 weight percent of nitrogen and/or methane, 30 to 60 weight percent of hydrogen, 15 to 30 weight percent of methanol, 15 to 20 weight percent of ethylene glycol, 0.1 to 2 weight percent of propylene glycol, 0.05 to 2.0 weight percent of butanediol, 0.1 to 5 weight percent of methyl glycolate and 0.1 to 0.6 weight percent of ethanol.
According to an embodiment of the invention, the fractional desuperheating condensation is subjected to at least two condensation stages. For example, the first stage condensation temperature is 110-. For example, the temperature of the second stage condensation may range from 20 ℃ to 50 ℃, illustratively 20 ℃, 30 ℃, 40 ℃, 50 ℃.
According to the embodiment of the invention, the crude ethylene glycol liquid material is a liquid phase material obtained after the gas material obtained by the dimethyl oxalate hydrogenation unit is subjected to first-stage condensation. For example, the crude ethylene glycol liquid material contains 72-85 wt% of ethylene glycol, 1-10 wt% of methanol, 0.1-10 wt% of methyl glycolate, 0.1-4 wt% of propylene glycol and 0.1-5wt% of butanediol in percentage by mass. Preferably, a first condensed gas phase stream is also obtained after the first stage condensation.
According to an embodiment of the present invention, the crude methanol liquid material is a liquid phase obtained after the gas phase stream after the first stage condensation is subjected to the second stage condensation. For example, the crude methanol liquid material contains 50 to 70 wt% of methanol, 10 to 25wt% of ethylene glycol, 0.3 to 15 wt% of methyl glycolate, 0.1 to 2wt% of propylene glycol, and 0.05 to 2wt% of butylene glycol, in terms of mass percentage. Preferably, said second stage of condensation also results in a second stage of condensed vapour phase stream. For example, the gas phase material flow after the second stage condensation is hydrogen containing inert gases such as nitrogen, and the hydrogen is returned to the dimethyl oxalate hydrogenation unit for reuse after further treatment.
According to an embodiment of the present invention, at least one of the crude methanol liquid feed and the crude ethanol liquid feed is subjected to partial gasification and then enters a separation tower to be separated to obtain a methanol and alcohol ester mixture.
According to an embodiment of the present invention, the crude methanol liquid stream may be combined with a crude ethylene glycol liquid stream and then fed to a separation column for separation to produce a methanol and alcohol ester mixture. Specifically, the crude methanol liquid material is partially gasified and then combined with the crude glycol liquid material, and then the mixture enters a separation tower to be separated to obtain a methanol and alcohol ester mixture.
According to an embodiment of the invention, the crude methanol liquid feed and the crude ethylene glycol liquid feed may be fed to different separation columns, respectively. For example, the separation column may comprise two columns, namely a column for separating a crude methanol liquid feed and a column for separating a crude ethylene glycol liquid feed, to obtain methanol and an alcohol ester mixture, respectively.
According to the embodiment of the invention, the alcohol ester mixture is separated into the ethylene glycol through an ester separation tower, a light component removal tower and an ethylene glycol rectification tower.
According to the embodiment of the invention, the temperature of the top of the separation tower for separating the crude methanol liquid material is 40-70 ℃, the pressure of the top of the separation tower is 0.07-0.12MPa, the temperature of the bottom of the separation tower is 80-180 ℃, the pressure of the bottom of the separation tower is 0.1-0.15MPa, methanol is obtained at the top of the separation tower, and the alcohol ester mixture material is obtained at the bottom of the separation tower. For example, the alcohol ester mixture material contains 70-80 wt% of Ethylene Glycol (EG), 2-5 wt% of butanediol, 2-10 wt% of propylene glycol and 5-20wt% of glycolic acid in percentage by mass.
The invention has the beneficial effects that:
the invention provides a method for separating ethylene glycol, which comprises the steps of cooling and condensing high-temperature gas materials containing hydrogen, water, methanol and ethylene glycol obtained by a dimethyl oxalate (DMO) hydrogenation reaction unit step by step to respectively obtain crude ethylene glycol liquid materials with high ethylene glycol content and crude methanol liquid materials with high methanol content, wherein the crude ethylene glycol liquid materials and/or the crude methanol liquid materials are partially gasified by heat exchange with a heat source before being sent into a separation unit. Separating by a separation tower to obtain a mixture of methanol and alcohol ester (including high content of glycol), and further purifying and separating the alcohol ester mixture to obtain the glycol. The method of the invention saves the energy consumption of the reaction gas condensation and the rectification separation tower.
Drawings
Fig. 1 is a schematic structural diagram of an ethylene glycol separation device.
Reference numerals: r, a catalytic hydrogenation reactor, E, a heat exchanger, C1, a first-stage condenser, C2, a second-stage condenser, V1, a first fraction liquid tank, V2, a second fraction liquid tank, T and a separation tower.
1. 2, reacting gas-phase product after heat exchange, 3, reacting product after first-stage condensation, 4, gas-phase product after first-stage condensation, 5, reacting product after second-stage condensation, 6, hydrogen containing inert gas, 7, crude methanol liquid material, 8, crude glycol liquid material, 9, heated crude methanol liquid material, 10, alcohol ester mixture, 11 and methanol.
Detailed Description
The technical solution of the present invention will be further described in detail with reference to specific embodiments. It is to be understood that the following examples are only illustrative and explanatory of the present invention and should not be construed as limiting the scope of the present invention. All the techniques realized based on the above-mentioned contents of the present invention are covered in the protection scope of the present invention.
Unless otherwise indicated, the raw materials and reagents used in the following examples are all commercially available products or can be prepared by known methods.
Example 1
The ethylene glycol separation process was carried out in the apparatus shown in figure 1. The high-temperature reaction gas-phase product 1 containing ethylene glycol, methanol, hydrogen, water and other components from dimethyl oxalate catalytic hydrogenation is at the temperature of 180-210 ℃, heat exchange is carried out on the high-temperature reaction gas-phase product 1 and a crude methanol liquid material from the bottom of a second-stage condensation liquid separation tank V2 through a heat exchanger E, the obtained heat-exchanged reaction gas-phase product 2 with reduced temperature enters a first-stage condenser C1, the obtained first-stage condensed reaction product 3 enters a first-stage liquid separation tank V1 for gas-liquid separation, a crude ethylene glycol liquid material 8 is obtained at the bottom of the tank, and a first-stage condensed gas-phase product 4 is arranged at the top of the tank; and condensing the gas-phase product 4 after the first-stage condensation by using a second-stage condenser C2 to obtain a reaction product 5 after the second-stage condensation, introducing the reaction product 5 into a second-stage liquid separation tank V2 for gas-liquid separation, obtaining hydrogen 6 containing inert gases such as nitrogen at the top of the tank, and obtaining a crude methanol liquid material 7 at the bottom of the tank.
And (3) feeding the crude methanol liquid material 7 into a heat exchanger E, exchanging heat with the high-temperature reaction gas-phase product 1, heating to obtain a heated crude methanol liquid material 9, feeding the heated crude methanol liquid material into a separation tower T, obtaining methanol 11 at the tower top, and obtaining an alcohol ester mixture 10 with high glycol content at the tower bottom. The crude ethylene glycol liquid material 8 is sent to another separation tower for separation to obtain an alcohol ester mixture with high methanol and ethylene glycol contents. The alcohol ester mixture is further separated and purified to obtain the glycol.
In another embodiment, the crude ethylene glycol liquid feed and the warmed crude methanol liquid feed are combined and fed to a separation column to obtain methanol at the top of the column and an alcohol ester mixture with a high ethylene glycol content at the bottom of the column. The alcohol ester mixture is further separated and purified to obtain the ethylene glycol.
Example 2
Take a 20 ten thousand tons/year coal glycol making device as an example.
TABLE 1 DMO catalytic hydrogenation gas phase product composition Table
| Components | Content (wt%) |
| Hydrogen gas | 39.00 |
| Nitrogen gas | 20.00 |
| Methanol | 20.10 |
| Ethylene glycol | 16.00 |
| Ethanol | 0.60 |
| Water (I) | 0.90 |
| Glycolic acid methyl ester | 1.20 |
| 1, 2-propanediol | 1.30 |
| 1, 2-butanediol | 0.90 |
The gas-phase product of the catalytic hydrogenation reaction of dimethyl oxalate with the composition shown in the table 1 has the flow of 155800kg/h, the temperature of 190 ℃ and the pressure of 2.8MPa, enters a heat exchanger E to exchange heat with 24250kg/h of 40 ℃ crude methanol liquid material from the bottom of a second-stage condensation liquid separation tank V2 to obtain 167 ℃ heat-exchanged reaction gas-phase product 2, enters a first-stage condenser C1 to be condensed, the condensation temperature is controlled to be 120 ℃, the obtained first-stage condensed reaction product material 3 enters a first-stage liquid separation tank V1 to be subjected to gas-liquid separation, and 24790kg/h crude glycol liquid material 8 is obtained at the bottom of the tank, wherein the crude glycol liquid material contains 82 wt% of glycol, 4 wt% of methanol, 3 wt% of methyl glycolate, 6wt% of propylene glycol, 4.4 wt% of butanediol and 0.6wt% of water; the top of the tank is a gas-phase product 4, the gas-phase product 4 after the first-stage condensation enters a second-stage condenser C2 for condensation, the temperature of the second-stage condenser is controlled to be 40 ℃, a reaction product 5 after the second-stage condensation enters a second-stage liquid separation tank V2 for gas-liquid separation, 106760kg/h of hydrogen 6 containing inert gases such as nitrogen is obtained at the top of the tank, and a crude methanol liquid material 7 is obtained at the bottom of the tank.
The temperature of the crude methanol liquid material 7 is increased to 160 ℃ after heat exchange between the crude methanol liquid material E and the high-temperature reaction gas phase material 1, the crude methanol liquid material enters a separation tower T, the crude glycol liquid material also enters the separation tower T, and methanol 11 is obtained at the top of the separation tower, wherein the content of the methanol is 90.5 wt%, and the content of the ethanol and the water is 9.5 wt%; the alcohol ester mixture 10 with high content of ethylene glycol is obtained in the tower kettle, and the EG content of the alcohol ester mixture 10 is 86 wt%, the BDO content is 3.7 wt%, the PG content is 5.4 wt%, and the MG content is 4.9 wt%.
The alcohol ester mixture 10 is further separated and purified to obtain the ethylene glycol. The separation and purification to obtain the ethylene glycol refers to the separation of the ethylene glycol through an ester separation tower, a light component removal tower and an ethylene glycol rectification tower.
The thermal load of each apparatus is shown in Table 2.
TABLE 2 thermal load of the relevant apparatus in example 2
| Device | Heat load (kW) |
| First condenser C1 | -25107 |
| Second condenser C2 | -39546 |
| Reboiler of separation tower | 1240 |
| Separator condenser | -6994 |
| Aggregate energy consumption | 72887 |
Comparative example
The gas-phase product of the dimethyl oxalate catalytic hydrogenation reaction with the composition shown in the table 1 has the flow of 155800kg/h, the temperature of 190 ℃ and the pressure of 2.8MPa, enters a condenser for heat exchange to 40 ℃, then is subjected to gas-liquid separation, hydrogen containing inert gas obtained by gas-liquid separation is treated and then returned for reuse, the separated condensate enters a separation tower, methanol is obtained at the top of the tower, and an alcohol ester mixture is obtained at the top of the tower.
The alcohol ester mixture is further separated and purified to obtain the ethylene glycol.
The associated equipment heat load is shown in table 3.
TABLE 3 thermal load of the relevant apparatus in the comparative example
| Device | Heat load (kW) |
| Heat exchanger | -79022 |
| Reboiler of separation tower | 15879 |
| Separator condenser | -8313 |
| Aggregate energy consumption | 103214 |
As can be seen from the comparative example, in the example 2, the high-temperature reaction gas is condensed step by step, and the crude methanol liquid material and the gas-phase product of the dimethyl oxalate catalytic hydrogenation reaction enter the separation tower after heat exchange, so that the energy consumption can be reduced by 103214-72887-30327 kW. Compared with the comparative example, the energy is saved by 29 percent.
The embodiments of the present invention have been described above. However, the present invention is not limited to the above embodiment. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (13)
1. A method for separating ethylene glycol, characterized in that the method comprises the following steps:
cooling and condensing the gas material obtained by the dimethyl oxalate hydrogenation unit step by step to obtain a crude ethylene glycol liquid material and a crude methanol liquid material; the gaseous feed contains hydrogen, water, methanol and ethylene glycol;
before the crude methanol liquid material is sent into the separation unit, the crude methanol liquid material exchanges heat with at least one heat source of steam, gas material at the top of the separation tower in the separation unit and gas material obtained by the dimethyl oxalate hydrogenation unit to increase the temperature, so that the material is partially gasified; the temperature difference between the crude methanol liquid material and a heat source is 50-200 ℃; the temperature difference of the crude methanol liquid material after heat exchange and temperature increase is 30-160 ℃ compared with the temperature difference before heat exchange and temperature increase; the temperature of the crude methanol liquid material after heat exchange and temperature increase is 70-170 ℃;
the crude methanol liquid material is partially gasified and then is combined with the crude glycol liquid material, and then the mixture enters a separation tower to be separated to obtain a methanol and alcohol ester mixture;
and separating the alcohol ester mixture by an ester separation tower, a light component removal tower and an ethylene glycol refining tower to obtain ethylene glycol.
2. The separation process according to claim 1, wherein the source of heat for partial gasification is selected from the group consisting of a gaseous feed from a dimethyl oxalate hydrogenation unit.
3. The separation process of claim 1, wherein the separation column overhead gas stream is a pressurized overhead gas stream.
4. The separation process according to claim 3, wherein the pressurization is achieved by a compressor.
5. The separation method according to claim 1, wherein the dimethyl oxalate hydrogenation unit is a reaction unit in the preparation of ethylene glycol from coal-based synthesis gas.
6. The separation method according to claim 5, wherein the process of hydrogenating the dimethyl oxalate comprises: performing catalytic hydrogenation reaction on dimethyl oxalate (DMO) at the temperature of 180-225 ℃ and under the pressure of 2.5-3.0MPa to obtain a reaction product containing glycol;
and/or the temperature of the gas material obtained by the dimethyl oxalate hydrogenation unit is 180-210 ℃;
and/or the pressure of the gas material obtained by the dimethyl oxalate hydrogenation unit is 2.5-3.0 MPa.
7. The separation process of claim 6, wherein the reaction product further comprises unreacted feed hydrogen and by-products.
8. The separation process of claim 7, wherein the by-product comprises at least one of Butanediol (BDO), ethanol, Propylene Glycol (PG), Methyl Glycolate (MG), water;
and/or the reaction product also contains inert gas.
9. The separation method according to claim 7, wherein the reaction product comprises, in mass percent: 5 to 25 weight percent of nitrogen and/or methane, 30 to 60 weight percent of hydrogen, 15 to 30 weight percent of methanol, 15 to 20 weight percent of ethylene glycol, 0.1 to 2 weight percent of propylene glycol, 0.05 to 2.0 weight percent of butanediol, 0.1 to 5 weight percent of methyl glycolate and 0.1 to 0.6 weight percent of ethanol.
10. The separation method as claimed in claim 1, wherein the fractional temperature-reduction condensation is performed by at least two-stage condensation, the first stage condensation temperature is 110-150 ℃, and the second stage condensation temperature is 20-50 ℃.
11. The separation method according to claim 10, wherein the crude ethylene glycol liquid material is a liquid phase material obtained by first-stage condensation of a gas material obtained by the dimethyl oxalate hydrogenation unit; and gas phase material flow after the first condensation is also obtained after the first condensation.
12. The separation process of claim 10, wherein the crude methanol liquid feed is a liquid phase obtained by a second stage of condensation of the first stage condensed gas phase stream; and a second-stage condensed gas-phase material flow is also obtained after the second-stage condensation.
13. The separation method of claim 12, wherein the gas phase stream after the second stage condensation is hydrogen containing nitrogen gas, and the hydrogen is further treated and returned to the dimethyl oxalate hydrogenation unit for reuse.
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