CN217367195U - MTO grade methanol production system - Google Patents
MTO grade methanol production system Download PDFInfo
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- CN217367195U CN217367195U CN202220830930.XU CN202220830930U CN217367195U CN 217367195 U CN217367195 U CN 217367195U CN 202220830930 U CN202220830930 U CN 202220830930U CN 217367195 U CN217367195 U CN 217367195U
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Abstract
The utility model provides a MTO level methyl alcohol production system, include: the system comprises a pre-rectifying tower, a reboiler, a preheater, a first multi-effect evaporator, a second multi-effect evaporator, a third multi-effect evaporator, an extraction cooler, a recovery tower, a tower top cooler, a pre-tower reflux tank, a recovery tower cooler and a recovery tower reflux tank. The utility model provides a MTO level methyl alcohol production system can long-term steady operation to, have MTO level methyl alcohol productivity height and the low advantage of energy consumption.
Description
Technical Field
The utility model belongs to the technical field of the methyl alcohol rectification, concretely relates to MTO level methyl alcohol production system.
Background
The MTO reaction has high requirement (less than or equal to 0.1X 10) on the content of metals in methanol, particularly alkali metals such as sodium, potassium and the like -6 Mass fraction), if the metal content is too high, it will cause poisoning of the MTO catalyst, affecting the olefin effect. In order to meet the requirement of MTO reaction, the rectification process different from the conventional refined methanol needs to be carried out on the crude methanol to prepare the MTO-grade methanol so as to meet the requirement of the MTO reaction on the purity of the methanol.
The prior method for preparing MTO-grade methanol has the problems of low yield of MTO-grade methanol and low resource utilization rate.
SUMMERY OF THE UTILITY MODEL
To the defect that prior art exists, the utility model provides a MTO level methyl alcohol production system can effectively solve above-mentioned problem.
The utility model adopts the technical scheme as follows:
the utility model provides a MTO level methyl alcohol production system, include: the system comprises a pre-rectifying tower (1), a reboiler (2), a preheater (3), a first multi-effect evaporator (4), a second multi-effect evaporator (5), a third multi-effect evaporator (6), a recovery cooler (7) and a recovery tower (8);
a methanol liquid outlet at the bottom of the pre-rectifying tower (1) is connected to a cold source liquid inlet of the preheater (3); a cold source liquid outlet of the preheater (3) is connected to a cold source liquid inlet of the first multi-effect evaporator (4); a cold source exhaust port of the first multi-effect evaporator (4) is connected to a heat source air inlet of the second multi-effect evaporator (5), and is connected to a feed inlet of the extraction cooler (7) after being condensed by the second multi-effect evaporator (5); a cold source liquid outlet of the first multi-effect evaporator (4) is connected to a cold source liquid inlet of the second multi-effect evaporator (5); a cold source exhaust port of the second multi-effect evaporator (5) is connected to a heat source air inlet of the third multi-effect evaporator (6), and is connected to a feed inlet of the extraction cooler (7) after being condensed by the third multi-effect evaporator (6); a cold source liquid outlet of the second multi-effect evaporator (5) is connected to a cold source liquid inlet of the third multi-effect evaporator (6); a cold source exhaust port of the third multi-effect evaporator (6) is connected to a hot source air inlet of the reboiler (2), and is connected to a feed inlet of the production cooler (7) after being condensed by the reboiler (2); the liquid outlet of the extraction cooler (7) is an MTO-grade methanol extraction outlet; a cold source liquid outlet of the third multi-effect evaporator (6) is divided into two branches, and one branch is connected with the pre-rectifying tower (1) in a backflow mode; the other branch is connected to the recovery column (8).
Preferably, the system also comprises an overhead cooler (9) and a pre-tower reflux tank (10);
the tower top methanol steam exhaust port of the pre-rectifying tower (1) is connected to the tower top cooler (9), and is connected to the liquid inlet of the pre-rectifying tower reflux tank (10) after being cooled by the tower top cooler (9); and the liquid outlet of the pre-rectifying tower reflux groove (10) is connected to the inside of the pre-rectifying tower (1) in a reflux mode.
Preferably, the system also comprises a recovery tower cooler (11) and a recovery tower reflux groove (12);
the tower top methanol steam exhaust port of the recovery tower (8) is connected to the recovery tower cooler (11), and is connected to the liquid inlet of the recovery tower reflux groove (12) after being cooled by the recovery tower cooler (11); the liquid outlet of the recovery tower reflux groove (12) is connected with the inside of the recovery tower (8) in a reflux mode.
The utility model provides a MTO level methyl alcohol production system has following advantage:
the utility model provides a MTO level methyl alcohol production system can long-term steady operation to, have MTO level methyl alcohol productivity height and the low advantage of energy consumption.
Drawings
FIG. 1 is a schematic structural diagram of the MTO-grade methanol production system provided by the present invention.
Detailed Description
In order to make the technical problem, technical solution and advantageous effects solved by the present invention more clearly understood, the following description is given in conjunction with the accompanying drawings and embodiments to further explain the present invention in detail. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention.
The utility model provides a MTO level methanol production system, refer to figure 1, include: the system comprises a pre-rectifying tower 1, a reboiler 2, a preheater 3, a first multi-effect evaporator 4, a second multi-effect evaporator 5, a third multi-effect evaporator 6, a recovery cooler 7 and a recovery tower 8;
a methanol liquid outlet at the bottom of the pre-rectifying tower 1 is connected to a liquid inlet of a cold source of the preheater 3; a cold source liquid outlet of the preheater 3 is connected to a cold source liquid inlet of the first multi-effect evaporator 4; a cold source air outlet of the first multi-effect evaporator 4 is connected to a heat source air inlet of the second multi-effect evaporator 5, and is connected to a feed inlet of the extraction cooler 7 after being condensed by the second multi-effect evaporator 5; a cold source liquid outlet of the first multi-effect evaporator 4 is connected to a cold source liquid inlet of the second multi-effect evaporator 5; a cold source air outlet of the second multi-effect evaporator 5 is connected to a heat source air inlet of a third multi-effect evaporator 6, and is connected to a feed inlet of a production cooler 7 after being condensed by the third multi-effect evaporator 6; a cold source liquid outlet of the second multi-effect evaporator 5 is connected to a cold source liquid inlet of the third multi-effect evaporator 6; a cold source exhaust port of the third multi-effect evaporator 6 is connected to a heat source air inlet of the reboiler 2, and is connected to a feed inlet of the extraction cooler 7 after being condensed by the reboiler 2; the liquid outlet of the extraction cooler 7 is an MTO grade methanol extraction outlet; a cold source liquid outlet of the third multi-effect evaporator 6 is divided into two branches, and one branch is connected with the pre-rectifying tower 1 in a backflow mode; the other branch is connected to the recovery column 8.
Also comprises a tower top cooler 9 and a pre-tower reflux groove 10;
the top methanol steam exhaust port of the pre-rectifying tower 1 is connected to a top cooler 9, and is connected to a liquid inlet of a pre-rectifying tower reflux groove 10 after being cooled by the top cooler 9; the liquid outlet of the preliminary distillation column reflux tank 10 is connected to the inside of the preliminary distillation column 1 by reflux.
Also comprises a recovery tower cooler 11 and a recovery tower reflux groove 12;
a tower top methanol steam exhaust port of the recovery tower 8 is connected to a recovery tower cooler 11, and is connected to a liquid inlet of a recovery tower reflux groove 12 after being cooled by the recovery tower cooler 11; the liquid outlet of the recovery column reflux drum 12 is connected to the inside of the recovery column 8 by reflux.
The utility model provides a MTO level methyl alcohol production system, its theory of operation is:
1) the crude methanol enters a pre-rectifying tower 1 for rectification, methanol gas is discharged from the top of the tower and enters a tower top cooler 9 for cooling, and noncondensable gas is sent to a boiler for blending combustion; the condensed methanol liquid enters a pre-rectifying tower reflux groove 10 and is sent into a pre-rectifying tower 1 by a reflux pump to carry out the circulating rectification and purification process;
2) the methanol liquid at the bottom of the pre-rectifying tower 1 is fed into a preheater 3 for preheating through a 1 st pipeline L1 under the action of a feed pump;
3) the preheated methanol liquid is sent to the first multi-effect evaporator 4 through a 2 nd pipeline L2;
the first multi-effect evaporator 4-tube-pass heat source is provided by inputting 1.27MPa steam through a 3 rd pipeline L3, and certain waste heat is still generated after the steam is subjected to heat exchange and temperature reduction, so that the heat source is input into the preheater 3 through a 4 th pipeline L4 to be used as a heat source of the preheater 3, is finally cooled through the preheater 3 and is discharged through a 5 th pipeline L4;
the methanol liquid is sent to the shell pass of the first multi-effect evaporator 4 and heated by 1.27MPa steam, and the methanol liquid is arranged at the bottom of the shell pass; the top of the shell side is methanol steam; wherein the purity of the methanol vapor is greater than the purity of the methanol liquid;
4) methanol vapor in the shell pass of the first multi-effect evaporator 4 is sent to the tube pass of the second multi-effect evaporator 5 through a 6 th pipeline L6 to be used as a heat source of the second multi-effect evaporator 5; after being cooled by the second multi-effect evaporator 5, the cooled water is conveyed into a production cooler 7 through a 7 th pipeline L7;
the methanol liquid of the shell pass of the first multi-effect evaporator 4 is sent to the shell pass of the second multi-effect evaporator 5 through a 8 th pipeline L8 to be further heated and purified, and the further purified methanol steam is arranged at the top of the shell pass; the bottom of the shell pass is methanol liquid;
the methanol vapor of the shell side of the second multi-effect evaporator 5 is sent to the tube side of the third multi-effect evaporator 6 through a 9 th pipeline L9 to be used as a heat source of the third multi-effect evaporator 6; after being cooled by the third multi-effect evaporator 6, the cooled water is conveyed into a production cooler 7 through a 10 th pipeline L10;
5) the methanol liquid in the shell pass of the second multi-effect evaporator 5 is sent to the shell pass of the third multi-effect evaporator 6 through a 11 th pipeline L11 to be further heated and purified, and the further purified methanol steam is arranged at the top of the shell pass; the bottom of the shell pass is methanol liquid;
the methanol steam of the shell pass of the third multi-effect evaporator 6 is sent to the reboiler 2 through a 12 th pipeline L12 to be used as a heat source, the temperature of the methanol steam is reduced after passing through the reboiler 2, and the methanol steam is sent to the extraction cooler 7 through a 13 th pipeline L13 to be cooled; thereby realizing the high-efficiency utilization of the heat of the methanol steam on the shell side;
for the reboiler 2, the methanol part at the bottom of the pre-rectifying tower 1 enters the reboiler 2, is heated and then flows back to the interior of the pre-rectifying tower 1;
6) for the methanol liquid of the shell pass of the third multi-effect evaporator 6, the methanol purity is lower after the continuous action of the three-stage multi-effect evaporator, and the methanol liquid is sent to the bottom of the pre-rectifying tower 1 through a 14 th pipeline L14 for re-rectification; when the 14 th line L14 methanol liquid purity is detected to be lower than a certain value, the methanol liquid purity is sent to the recovery tower 8 through a 15 th line L15;
the recovery tower 8 is still a rectifying tower in essence, and after the methanol liquid is purified by the recovery tower 8, the bottom of the tower is discharged as wastewater; the methanol vapor at the top of the tower flows back to the recovery tower 8 after passing through a recovery tower cooler 11 and a recovery tower reflux groove 12; when the purity meets the requirement, a pipeline is led out from the reflux tank 12 of the recovery tower to the pipeline of the recovery tower 8 and is used as a methanol product to be extracted.
The utility model provides a MTO level methanol production system has following innovation:
1) a three-stage multi-effect evaporator series structure is adopted, for the former two-stage multi-effect evaporator, methanol steam generated by the former two-stage multi-effect evaporator is used as a heat source of the next-stage multi-effect evaporator, and the methanol steam flows into the extraction cooler 7 after heat is recovered; for the last stage of multi-effect evaporator, the generated methanol steam is used as a heat source of the reboiler, and the recovered heat flows into the extraction cooler 7, so that the high-efficiency utilization of the methanol steam heat is realized;
2) the methanol liquid is continuously reduced in purity after being acted by the multi-effect evaporators at all levels, and finally flows back to the pre-rectifying tower through a pipeline, so that the cyclic purification of the methanol liquid is realized, and the yield of the final MTO-level methanol is improved; in addition, after the purity drops to a certain value, if flow back to the pre-rectifying tower, the condition of pipeline blockage is easy to occur, therefore, the recovery tower 8 is connected in series behind the pre-rectifying tower, the methanol liquid is rectified and purified through the recovery tower 8, and the shutdown phenomenon caused by the abnormal working conditions such as pipeline blockage can be avoided.
3)3 multi-effect evaporators are connected in series, a heat source of a tube pass of the primary evaporator is provided with heat by 1.27MPa steam, generated methanol steam enters a tube pass of the secondary evaporator to serve as a heat source of the secondary evaporator, liquid of a shell pass of the primary evaporator enters a shell pass of the secondary evaporator to be heated by the methanol steam of the tube pass, and the like.
Removing low boiling point impurities such as dimethyl ether and the like dissolved in the crude methanol and other heavy components such as water, ethanol, alcohol-based liquid fuel and the like by a mode of serially connecting multi-effect evaporators, concentrating and removing alkaline metal ions from the crude methanol to produce MTO-grade methanol meeting the (Q/LHHX001-2021) standard, sending the MTO-grade methanol to a recovery cooler 7, simultaneously sending the byproduct alcohol-based liquid fuel and the light fraction alkane oil of the pre-tower to an alcohol-based liquid fuel storage tank for sale, and sending wastewater to a sewage treatment.
4) Two pipelines are arranged on a methanol liquid conveying pipeline of a third multi-effect evaporator 6, and one pipeline flows back to the bottom of a pre-rectifying tower 1; the other pipeline is sent to a recovery tower 8 for further purification, and products meeting the alcohol-based fuel standard are produced. This way the problem of blocking the pipes can be solved, in addition a better economic benefit is created and part of the energy consumption is saved. And the problem of more impurities at the bottom of the pre-rectifying tower can be solved.
The energy saving statistics are as follows:
1. influence on the boiler: when the MTO is started, the boiler load is reduced by 24.1 tons per hour, the power generation is increased by 1666kwh per hour (reduced to 8.3 tons of high-pressure steam), and the boiler load is reduced by 32.4 tons per hour in terms of accumulated boiler load.
2. The device consumes steam: the steam consumption per ton of refined methanol is 0.69T/T (average value) at 1.27MPa, the steam consumption per ton of MTO grade methanol is 0.256T/T (average value) at 1.27MPa, and the steam consumption per ton of 1.27MPA is reduced by 0.434T; 0.2T/T of steam (average value) is consumed for 0.3MPa of refined methanol per ton, 0.3T/T of steam is consumed for 0.3MPa of methanol per ton of MTO grade methanol, and the consumption of 0.2T of steam is reduced for 0.3 MPA.
3. The device has the following power consumption: the power consumption of refined methanol is 139206KWH per month under the working condition of refined methanol, 179212KWH per month under the working condition of MTO-grade methanol, and the power is saved by 40006KWH per month.
4. The alkali consumption of the device is as follows: the refined methanol working condition consumes 825KG per month alkali, the MTO-grade methanol working condition consumes 0KG per month alkali, and the caustic soda flakes are saved 825KG per month.
Therefore, the multi-effect evaporation device can run for a long period, the bottleneck problems of pipeline blockage and the like are thoroughly solved, compared with three-tower rectification, the cost can be saved by more than 300 ten thousand yuan per month, and good economic benefit is generated.
The utility model provides a MTO level methyl alcohol production system can long-term steady operation to, have MTO level methyl alcohol productivity height and the low advantage of energy consumption.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and decorations can be made without departing from the principle of the present invention, and these improvements and decorations should also be viewed as the protection scope of the present invention.
Claims (3)
1. An MTO grade methanol production system, comprising: the system comprises a pre-rectifying tower (1), a reboiler (2), a preheater (3), a first multi-effect evaporator (4), a second multi-effect evaporator (5), a third multi-effect evaporator (6), a recovery cooler (7) and a recovery tower (8);
a methanol liquid outlet at the bottom of the pre-rectifying tower (1) is connected to a cold source liquid inlet of the preheater (3); a cold source liquid outlet of the preheater (3) is connected to a cold source liquid inlet of the first multi-effect evaporator (4); a cold source exhaust port of the first multi-effect evaporator (4) is connected to a heat source air inlet of the second multi-effect evaporator (5), and is connected to a feed inlet of the extraction cooler (7) after being condensed by the second multi-effect evaporator (5); a cold source liquid outlet of the first multi-effect evaporator (4) is connected to a cold source liquid inlet of the second multi-effect evaporator (5); a cold source exhaust port of the second multi-effect evaporator (5) is connected to a heat source air inlet of the third multi-effect evaporator (6), and is connected to a feed inlet of the extraction cooler (7) after being condensed by the third multi-effect evaporator (6); a cold source liquid outlet of the second multi-effect evaporator (5) is connected to a cold source liquid inlet of the third multi-effect evaporator (6); a cold source exhaust port of the third multi-effect evaporator (6) is connected to a hot source air inlet of the reboiler (2), and is connected to a feed inlet of the production cooler (7) after being condensed by the reboiler (2); the liquid outlet of the extraction cooler (7) is an MTO-grade methanol extraction outlet; a cold source liquid outlet of the third multi-effect evaporator (6) is divided into two branches, and one branch is connected with the pre-rectifying tower (1) in a backflow mode; the other branch is connected to the recovery column (8).
2. The MTO grade methanol production system according to claim 1, further comprising an overhead cooler (9) and a pre-column reflux drum (10);
the tower top methanol steam exhaust port of the pre-rectifying tower (1) is connected to the tower top cooler (9), and is connected to the liquid inlet of the pre-rectifying tower reflux tank (10) after being cooled by the tower top cooler (9); and the liquid outlet of the pre-rectifying tower reflux groove (10) is connected to the inside of the pre-rectifying tower (1) in a reflux mode.
3. The MTO grade methanol production system of claim 1, further comprising a recovery tower cooler (11) and a recovery tower reflux drum (12);
the tower top methanol steam exhaust port of the recovery tower (8) is connected to the recovery tower cooler (11), and is connected to the liquid inlet of the recovery tower reflux groove (12) after being cooled by the recovery tower cooler (11); the liquid outlet of the recovery tower reflux groove (12) is connected with the inside of the recovery tower (8) in a reflux mode.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220830930.XU CN217367195U (en) | 2022-04-11 | 2022-04-11 | MTO grade methanol production system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220830930.XU CN217367195U (en) | 2022-04-11 | 2022-04-11 | MTO grade methanol production system |
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| CN217367195U true CN217367195U (en) | 2022-09-06 |
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| CN202220830930.XU Active CN217367195U (en) | 2022-04-11 | 2022-04-11 | MTO grade methanol production system |
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- 2022-04-11 CN CN202220830930.XU patent/CN217367195U/en active Active
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