CN218742012U - Ethylene recovery system in methanol-to-olefin device - Google Patents
Ethylene recovery system in methanol-to-olefin device Download PDFInfo
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- CN218742012U CN218742012U CN202223289323.6U CN202223289323U CN218742012U CN 218742012 U CN218742012 U CN 218742012U CN 202223289323 U CN202223289323 U CN 202223289323U CN 218742012 U CN218742012 U CN 218742012U
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Abstract
The utility model belongs to the technical field of methanol-to-olefin, a ethylene recovery system in methanol-to-olefin device is disclosed, including deethanizing tower, demethanizing tower and ethylene recovery tower, the tower cauldron liquid export of ethylene recovery tower links to each other through the reflux entry of tower cauldron pump with deethanizing tower, and the top of the tower methane hydrogen tail gas export of ethylene recovery tower links to each other with the cold source entry of 1# lotion cooler, and the middle part circulating liquid export of ethylene recovery tower links to each other with the circulating pump entry, the circulating pump export links to each other with circulating liquid cooler heat source entry, circulating liquid cooler heat source export links to each other with the middle part circulating liquid entry of ethylene recovery tower. The utility model discloses a draw forth one lotion from the middle part of ethylene recovery tower, return the ethylene recovery tower after the cooling again, through cooling lotion temperature, increased the absorbed dose of C4 lotion, effectively reduced ethylene loss in the top of the tower methane hydrogen tail gas, the operation load of deethanization tower simultaneously also corresponding reduction, the energy consumption reduces, and economic benefits is showing.
Description
Technical Field
The utility model belongs to the technical field of the alkene is made to methyl alcohol, concretely relates to ethylene recovery system in methyl alcohol system alkene device.
Background
Ethylene and propylene are the basic raw materials for the petrochemical industry. Currently, olefins are obtained mainly by hydrocarbon cracking or catalytic cracking. Under the situation that the global petroleum supply is increasingly tense, a process for producing low-carbon olefins by using oxides (particularly methanol and ethanol as raw materials) is developed. Wherein, the raw materials such as alcohols and the like can be produced by natural gas or coal synthesis gas, thus well solving the problem of high dependence of China on foreign oil. The process for producing low-carbon olefins mainly comprising ethylene and propylene from oxygen-containing compounds represented by methanol mainly comprises the MTO technology of UOP/Hyro company in the United states, the DMTO technology of the Union of Chinese academy of sciences, the MTP technology of Lurgi company in Germany and the S-MTO technology of petrochemical industry in China.
MTO deviceThe method comprises a methanol conversion part and a light hydrocarbon recovery part, wherein the light hydrocarbon recovery part has the main functions of compressing, condensing, separating and purifying gas-phase reaction products obtained by the methanol conversion part so as to obtain valuable olefins (mainly ethylene and propylene), and the separation process comprises a deethanizer, a demethanizer, an ethylene tower, an ethylene recovery tower, a depropanizer, a propylene tower, a debutanizer and the like. The product gas enters a deethanizer after quenching and compression, and C comes out from the top of the deethanizer 2 The product enters a demethanizer, light component gas (mainly methane and hydrogen) from the top of the demethanizer is sent to an ethylene recovery tower, and the bottom product is sent to an ethylene tower; separating ethane and ethylene products in an ethylene tower, sending the ethylene product from the top to an ethylene storage tank, and sending the ethane material at the bottom to a fuel gas system after vaporizing and heating; c4 washing liquid from a depropanizing tower enters an ethylene recovery tower from the top of the ethylene recovery tower, methane-hydrogen tail gas at the tower top is sent to a fuel gas system, and ethane at the tower bottom is sent to a deethanizing tower; the bottom product of the deethanizer is sent to a depropanizer which rectifies propane from the C4 heavy components, the top product is sent to a propylene tower, and the bottom product of the depropanizer is sent to a debutanizer; in the propylene tower, propane and propylene products are separated, the propylene product from the top is pumped to a propylene storage tank, and the saturated propane product at the bottom is gasified and then sent to a fuel gas system; the debutanizer separates the butanes from the pentanes or other heavy hydrocarbon components.
In the light hydrocarbon recovery part, condensation and separation of light component olefins are generally required to be carried out under cryogenic temperature and high pressure conditions, propylene is generally used as a refrigerant, for example, in an ethylene recovery tower section, as shown in fig. 1, an ethylene recovery tower is a packed tower, a C4 washing liquid from a depropanizer needs to pass through a 1# washing liquid cooler, a 2# washing liquid cooler and a 3# washing liquid cooler, and then enters from the upper part of the ethylene recovery tower after being subjected to heat exchange with a gas phase discharge at the top of the ethylene recovery tower, 7 ℃ propylene refrigerant and-25 ℃ propylene refrigerant to-20 ℃ in sequence to absorb ethylene in the gas phase and reduce ethylene loss in the tail gas at the top of the tower, but in actual operation, the temperature of the C4 washing liquid entering the ethylene recovery tower after being subjected to three heat exchanges is still higher, and in a high-load operation state, ethylene in the methane-hydrogen tail gas at the top of the ethylene recovery tower cannot be effectively recovered, so that ethylene product loss is caused, so that in actual operation, the flow of the C4 washing liquid in the tower top of the ethylene recovery tower can only be continuously increased, a certain effect on reducing ethylene loss is caused, but the ethylene recovery tower, the ethylene recovery tower is not beneficial to increase of a high-load steam-boiling device, and the energy-saving device is not beneficial to be increased. Therefore, it is required to reduce the amount of C4 wash liquid in the ethylene recovery column and reduce the energy consumption of the apparatus without reducing the ethylene loss.
Disclosure of Invention
The utility model discloses when retrieving to ethylene in the methyl alcohol system alkene device, the lotion quantity is big, the technical problem of device energy consumption increase, ethylene recovery system in the methyl alcohol system alkene device is provided, draw forth one lotion through the middle part from ethylene recovery tower, return ethylene recovery tower after the cooling, through cooling lotion temperature, the absorbed dose of C4 lotion has been increased, ethylene loss in the top of the tower methane hydrogen tail gas has effectively been reduced, simultaneously the operation load of deethanization tower also correspondingly reduces, the energy consumption reduces, economic benefits is showing.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the utility model provides an ethylene recovery system in methyl alcohol system alkene device, includes deethanizer, demethanizer and ethylene recovery tower, the top of the tower reflux tank of deethanizer links to each other with the raw materials liquid import of demethanizer, the top of the tower reflux tank of demethanizer links to each other with the raw materials liquid import of ethylene recovery tower, the tower cauldron liquid outlet of ethylene recovery tower links to each other through the reflux entry of tower cauldron pump with deethanizer, and the top of the tower methane hydrogen tail gas export of ethylene recovery tower links to each other with the cold source entry of 1# lotion cooler, and the heat source export of 1# lotion cooler links to each other with the heat source entry of 2# lotion cooler, and the heat source export of 2# lotion cooler links to each other with the heat source entry of 3# lotion cooler, and the heat source entry of 3# lotion cooler links to each other with the absorption liquid entry of ethylene recovery tower, and the middle part circulation liquid export of ethylene recovery tower links to each other with the circulating pump entry, and the circulation pump export of circulation liquid cooler links to each other with the middle part circulation liquid entry of ethylene recovery tower.
In one technical scheme, the cooling medium of the No. 2 washing liquid cooler is a propylene refrigerant at 7 ℃.
In one technical scheme, the cooling medium of the No. 3 washing liquid cooler is a propylene refrigerant with the temperature of-25 ℃.
In one technical scheme, the cooling medium of the circulating liquid cooler is a propylene refrigerant with the temperature of minus 40 ℃.
In a technical scheme, compare prior art, the beneficial effects of the utility model reside in that:
the utility model discloses a draw forth one lotion from the middle part of ethylene recovery tower, in the circulation liquid cooler with-40 ℃ after the propylene refrigerant heat transfer, deliver to the middle part of ethylene recovery tower, thus, the temperature of C4 lotion in the ethylene recovery tower has been reduced once more, the absorbed quantity of C4 lotion has been increased, ethylene loss in the top of the tower methane hydrogen tail gas has effectively been reduced, simultaneously the operation load of deethanizer also correspondingly reduces, the energy consumption reduces, economic benefits is showing, the drawback that the deethanizer high load operation that the absorbed quantity brought is increased so that the power consumption increases through increase C4 lotion flow has been avoided.
Drawings
FIG. 1 is a schematic flow diagram of an ethylene recovery system in a crude methanol to olefins plant.
FIG. 2 is a schematic flow diagram of an ethylene recovery system in the methanol to olefin apparatus of the present invention.
In the drawings, the reference numbers: 1 is a deethanizer, 2 is a demethanizer, 3 is an ethylene recovery tower, 4 is a 1# washing liquid cooler, 5 is a 2# washing liquid cooler, 6 is a 3# washing liquid cooler, 7 is a tower kettle pump, 8 is a circulating pump, and 9 is a circulating liquid cooler.
Detailed Description
The following examples are intended to illustrate the invention, but are not intended to limit the scope of the invention.
As shown in fig. 2, the utility model relates to an ethylene recovery system in methyl alcohol system alkene device, including deethanizer 1, demethanizer 2 and ethylene recovery tower 3, the top of the tower reflux tank of deethanizer 1 links to each other with demethanizer 2's raw material liquid import, demethanizer 2's top of the tower reflux tank links to each other with ethylene recovery tower 3's raw material liquid import, ethylene recovery tower 3's tower bottom of the tower liquid export links to each other with deethanizer 1's reflux inlet through tower kettle pump 7, ethylene recovery tower 3's top of the tower methane hydrogen tail gas export links to each other with ethylene recovery tower 3's cold source entry, 1# washing liquid cooler 4's heat source export links to each other with 2# washing liquid cooler 5's heat source entry, 2# washing liquid cooler 5's heat source export links to each other with 3# washing liquid cooler 6's heat source entry, 3# washing liquid cooler 6's heat source entry links to each other with ethylene recovery tower 3's absorption liquid entry, ethylene recovery tower 3's middle part export links to each other with circulating pump 8 entries of circulating pump, circulating pump export links to each other with ethylene recovery tower 9 heat source circulating liquid inlet.
In one embodiment, the cooling medium of the 1# washing liquid cooler of the present invention is the methane hydrogen tail gas at the top of the ethylene recovery tower 3, the cooling medium of the 2# washing liquid cooler 5 is a propylene refrigerant of 7 ℃, the cooling medium of the 3# washing liquid cooler 6 is a propylene refrigerant of-25 ℃, and the cooling medium of the circulating liquid cooler 9 is a propylene refrigerant of-40 ℃.
In practical operation, the ethylene recovery tower is a packed tower, C4 washing liquid from the depropanizing tower passes through a No. 1 washing liquid cooler, a No. 2 washing liquid cooler and a No. 3 washing liquid cooler, and then enters the ethylene recovery tower 3 from the upper part of the ethylene recovery tower after being subjected to heat exchange with methane hydrogen tail gas at the top of the ethylene recovery tower 3, propylene refrigerant at 7 ℃ and propylene refrigerant at-25 ℃ to-20 ℃ in sequence, so that ethylene in the gas phase of the ethylene recovery tower 3 is absorbed, and the loss of ethylene in the tail gas at the top of the ethylene recovery tower is reduced. When the utility model discloses draw forth one lotion from the middle part of ethylene recovery tower 3 (specifically for second section filler lower part), in circulation liquid cooler 9 with-40 ℃ after the propylene refrigerant heat transfer, send to the middle part of ethylene recovery tower 3 (specifically for third section filler upper portion), like this, the temperature of C4 lotion in the ethylene recovery tower 3 has been reduced once more, the absorbed dose of C4 lotion has been increased, ethylene loss in the top of the tower methane hydrogen tail gas has effectively been reduced, the drawback that the deethanizer high load operation that brings through increase C4 lotion flow increase absorbed dose so that the power consumption increases has been avoided.
The utility model discloses an draw forth the operation of C4 lotion and cooling in the ethylene recovery tower 3, economic benefits is showing: 1) By calculation, about 75kg of ethylene can be recovered per hour, 0.075t multiplied by 24 multiplied by 30=54t of ethylene can be recovered per month, the ethylene price is calculated according to 7500 yuan/t, and 54t multiplied by 7500/10000=40.5 ten thousand yuan is increased per month; 2) As shown in fig. 2, since the bottoms of the ethylene recovery column 3 are used as reflux liquid of the deethanizer 1, the results of online and offline analysis of the overhead gas of the deethanizer 1 show that the ethylene content in the overhead gas of the deethanizer 1 is 0, and the ethylene content can be maintained for a long time; 3) After accounting, the flow of the C4 washing liquid entering the ethylene recovery tower 3 is reduced to 12t/h from 15.5t/h before transformation, the operation load of the deethanizer 1 is correspondingly reduced, and under the same load, a reboiler at the tower bottom of the deethanizer 1 reduces low-pressure steam by about 0.5t/h per hour, so that 360t of the low-pressure steam can be saved every month, and the cost is saved by 360t multiplied by 120/10000 per month by 4.32 ten thousand yuan.
The above-mentioned embodiments are only preferred embodiments of the present invention, and are not intended to limit the scope of the present invention, and it is obvious to those skilled in the art that other embodiments can be easily made by replacement or change according to the technical content disclosed in the present specification, and therefore, all changes and modifications made in the principle of the present invention should be included in the claims of the present invention.
Claims (4)
1. The utility model provides an ethylene recovery system in methyl alcohol system alkene device, includes deethanizer (1), demethanizer (2) and ethylene recovery tower (3), the top of the tower reflux tank of deethanizer (1) links to each other with the raw materials liquid import of demethanizer (2), the top of the tower reflux tank of demethanizer (2) links to each other with the raw materials liquid import of ethylene recovery tower (3), the tower kettle liquid export of ethylene recovery tower (3) links to each other through tower kettle pump (7) and the reflux liquid entry of deethanizer (1), the top of the tower methane hydrogen tail gas export of ethylene recovery tower (3) links to each other with the cold source entry of 1# lotion cooler (4), the heat source export of 1# lotion cooler (4) links to each other with the heat source entry of 2# lotion cooler (5), the heat source export of 2# lotion cooler (5) links to each other with the heat source entry of 3# lotion cooler (6), the heat source entry of 3# lotion cooler (6) links to each other with the absorption liquid entry of ethylene recovery tower (3), its characteristic is continuous at the absorption liquid entry of ethylene recovery tower (3), the export of ethylene recycle tower (8) links to each other with the heat source entry of ethylene recycle tower (8), the export of ethylene recycle tower (9), the heat source export of ethylene recycle tower (9) and the middle part of ethylene recycle tower (9) links to each other.
2. The ethylene recovery system in methanol to olefin plant as claimed in claim 1, wherein the cooling medium of the 2# washing liquid cooler (5) is propylene refrigerant of 7 ℃.
3. The ethylene recovery system in a methanol-to-olefin device as claimed in claim 1, wherein the cooling medium of the 3# washing liquid cooler (6) is a propylene refrigerant with a temperature of-25 ℃.
4. The ethylene recovery system in a methanol to olefin device as claimed in claim 1, wherein the cooling medium of the circulating liquid cooler (9) is a propylene refrigerant of-40 ℃.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223289323.6U CN218742012U (en) | 2022-12-08 | 2022-12-08 | Ethylene recovery system in methanol-to-olefin device |
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| CN202223289323.6U CN218742012U (en) | 2022-12-08 | 2022-12-08 | Ethylene recovery system in methanol-to-olefin device |
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| CN218742012U true CN218742012U (en) | 2023-03-28 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113788735A (en) * | 2021-09-30 | 2021-12-14 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period |
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2022
- 2022-12-08 CN CN202223289323.6U patent/CN218742012U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113788735A (en) * | 2021-09-30 | 2021-12-14 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period |
| CN113788735B (en) * | 2021-09-30 | 2024-05-10 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery start-up method suitable for short-time shutdown period of methanol-to-olefin reaction |
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