CN218989173U - Device for preparing low-carbon olefin from methanol - Google Patents
Device for preparing low-carbon olefin from methanol Download PDFInfo
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- CN218989173U CN218989173U CN202123123470.1U CN202123123470U CN218989173U CN 218989173 U CN218989173 U CN 218989173U CN 202123123470 U CN202123123470 U CN 202123123470U CN 218989173 U CN218989173 U CN 218989173U
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
The utility model discloses a device for preparing low-carbon olefin from methanol, which comprises a methanol buffer tank, wherein the discharge end of the methanol buffer tank is communicated with a heat exchanger I through a feed pump, the discharge end of the heat exchanger I is communicated with a heat exchanger II, the discharge end of the heat exchanger II is communicated with a methanol-reaction gas vertical heat exchanger, the methanol outlet of the methanol-reaction gas vertical heat exchanger and the outlet end of a low-pressure dilution steam pipeline are both communicated with a feed pipeline, the discharge end of the feed pipeline is communicated with the feed end I of a reactor, the discharge end of the high-temperature reaction gas of the reactor is communicated with the feed end of a cyclone separator through the methanol-reaction gas vertical heat exchanger, the discharge end of the cyclone separator is sequentially communicated with a heat exchanger III and a quenching tower, and the discharge end of the quenching tower is communicated with a product collecting tank; the scheme has the beneficial effects of high catalyst activity, low production cost and high product yield.
Description
Technical Field
The utility model relates to the field of chemical product production, in particular to a device for preparing low-carbon olefin from methanol.
Background
The low-carbon olefin such as ethylene and propylene is an important basic chemical material of various resin materials such as synthetic plastics, synthetic fibers, synthetic rubber and the like, and plays a very important role in the field of modern chemical industry. In the traditional process, the low-carbon olefin is mainly obtained by converting refinery gas generated by industrial hydrocarbon cracking and petroleum catalytic cracking. With the rapid development of the economy in China, the demand for low-carbon olefin is gradually increased, but with the continuous increase of the market demand, the increasing exhaustion of petroleum resources and the increasing price of international crude oil are increasingly outstanding, so people continuously strive to find a new route which can replace petroleum to prepare olefin and can continuously develop. The reaction for preparing low-carbon olefin by converting methanol is considered to be one of the most promising routes for replacing the traditional petroleum route for preparing low-carbon olefin and sustainable development because the raw material methanol can be obtained from synthesis gas in a large amount. The low-carbon hydrocarbon device for preparing the methanol in the prior art has the defects of low catalyst activity, high processing load of the methanol, high production cost and low yield of low-carbon olefin products, and as a catalyst which is a key technology, the activity and the service life of the catalyst directly influence the conversion rate of the methanol and the yield of the low-carbon olefin, and according to the reaction characteristics of the catalyst, the improvement of the low-carbon olefin selectivity is facilitated under the conditions of low reaction pressure and high water-alcohol ratio, but the requirement of further improving the processing load of the methanol is limited, if the processing load cannot be improved, the efficiency of preparing the low-carbon olefin from the methanol is low, and the production cost is increased, so that the device which is beneficial to playing the roles of the catalyst, low production cost and high product yield is needed to be designed.
Disclosure of Invention
Aiming at the defects of the prior art, the utility model aims to provide a device for preparing low-carbon olefin from methanol, which has high catalyst activity, low production cost and high product yield.
In order to solve the problems, the utility model provides the following technical scheme:
the utility model provides a device of methyl alcohol preparation light olefin, including the methyl alcohol buffer tank, the discharge end of methyl alcohol buffer tank communicates with heat exchanger I through the charge pump, heat exchanger I's discharge end intercommunication has heat exchanger II, heat exchanger II's discharge end intercommunication has methyl alcohol-reaction gas vertical heat exchanger, methyl alcohol outlet and low pressure dilution steam pipeline's of reaction gas vertical heat exchanger give vent to anger the end all with the feed line intercommunication, feed line's discharge end and reactor's feed end I intercommunication, reactor's feed end II and regenerator's discharge end intercommunication, reactor's high temperature reaction gas discharge end passes through methyl alcohol-reaction gas vertical heat exchanger and cyclone's feed end intercommunication, cyclone's discharge end has heat exchanger III and quench tower to communicate in proper order, the discharge end of quench tower communicates the washing tower in proper order, the reaction gas compressor, product separator communicates with the product collection tank.
The methanol after heat exchange is mixed with low-pressure dilution steam in a low-pressure dilution steam mixing tank, the dilution steam can effectively reduce the partial pressure of oil gas in the reactor, reduce the contact time of methanol, reaction gas and a catalyst core, reduce side reaction, and further improve the catalytic effect and the product yield; the methanol enters a feeding distribution pipe of the reactor to be directly contacted with a high-temperature regenerated catalyst from a regenerator in the reactor, and the exothermic reaction is rapidly carried out under the action of the catalyst, wherein the reaction condition of the methanol in the reactor is that the reaction temperature is more than 300 ℃, and the methanol and the intermediate product dimethyl ether can be completely converted at the temperature higher than 400 ℃.
The technical scheme of this application is through rationalizing the setting to methyl alcohol system low carbon olefin device, and technological process is succinct, is making reactor methyl alcohol feeding effectively satisfy the reaction process demand, when promoting catalytic reaction process, along with temperature, pressure, methyl alcohol feeding dilution steam flow, the close looks stock etc. collaborative regulation of reaction in the actual process, can effectively promote catalyst catalytic effect, improves reflection product yield and reduction in production cost.
In addition, in order to realize the optimal effect of the device, the reaction temperature in the reactor is 478+/-1 ℃, and the temperature is in the range, thereby being beneficial to reducing the coke generation in the reactor and improving the yield of diene; the flow of the methanol feeding dilution steam is 16+/-4 t/h, the flow of the methanol feeding dilution steam is in the range, the water-alcohol ratio is reduced, the methanol processing amount is improved, and the higher diene yield is ensured; the feeding temperature of the methanol is regulated to 186 ℃, the control range is 176-230 ℃, the feeding temperature is reduced, and the occurrence of side reaction of the methanol in the reactor is effectively reduced; the reaction dense phase reserve is 20+/-3 t, and is controlled within the range, so that the reaction residence time is effectively reduced, the coke generation in the reactor is reduced, and the diene yield is improved.
The technical scheme of the utility model also comprises that the heat exchanger I comprises an in-reactor heat collector, a methanol purified water heat exchanger and a methanol-condensed water heat exchanger which are sequentially connected in series, and methanol sequentially passes through the heat exchangers after entering a buffer tank so as to exchange heat to 75 ℃.
In order to raise the temperature of the fed methanol and raise the heat exchange efficiency, the technological scheme of the present utility model includes also heat exchanger II comprising parallel methanol-stripping gas heat exchanger, methanol-steam heat exchanger and methanol booster pump, and the three said parts are mixed before entering the vertical methanol-reaction gas heat exchanger.
Preferably, the technical scheme of the utility model further comprises that an atomizing nozzle is arranged at the discharge end of the methanol booster pump.
In order to fully mix the methanol and the low-pressure dilution steam, the technical scheme of the utility model further comprises that the low-pressure dilution steam pipeline is tangentially communicated with the feeding pipeline, wherein the tangential communication means that the air outlet end of the low-pressure dilution steam pipeline is tangentially connected with the side wall of the feeding pipeline, the axial directions of the two pipelines form an included angle of 90 degrees, so that the low-pressure dilution steam enters along the side wall of the feeding pipeline and forms rotational flow along the pipe wall, and the low-pressure dilution steam is fully mixed with the methanol.
In order to effectively remove the catalyst carried by the reaction gas, the technical scheme of the utility model also comprises that the cyclone separator comprises a two-stage cyclone separator and a three-stage cyclone separator which are sequentially connected in series, and the reaction gas generated by the methanol in the reactor is discharged after most of the carried catalyst is removed by the two-stage cyclone separator and the entrained catalyst is removed by the three-stage cyclone separator of the reaction gas.
The beneficial effects of the utility model are as follows:
compared with the prior art, the utility model aims to provide the device for preparing the low-carbon olefin from the methanol, which has the advantages of high catalyst activity, low production cost and high product yield, and in order to achieve the effects, the methanol stored in the buffer tank is firstly subjected to heat exchange through the heat exchanger I, the heat exchanger II and the methanol-reaction gas vertical heat exchanger in sequence, so that the methanol meets the feeding temperature of the reaction gas; secondly, the methanol after heat exchange is communicated with a low-pressure dilution steam mixing tank, so that the catalytic reaction process is improved, the side reaction is reduced, and the product yield is improved; finally, the preparation of the low-carbon olefin is realized through heat exchange, cyclone separation and cooling treatment of the reaction gas; the equipment has reasonable design, can effectively improve the production efficiency and the product yield, and reduces the production cost.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are required to be used in the description of the embodiments or the prior art will be briefly described below, and it will be obvious to those skilled in the art that other drawings can be obtained from these drawings without inventive effort.
Fig. 1 is a schematic diagram of an apparatus for preparing light olefins from methanol in the embodiment.
Wherein 1 is a methanol buffer tank, 2 is a feed pump, 3 is a reactor internal heat collector, 4 is a methanol-purified water heat exchanger, 5 is a methanol-condensed water heat exchanger, 6 is a methanol-stripping gas heat exchanger, 7 is a methanol-steam heat exchanger, 8 is a methanol booster pump, 9 is a methanol-reaction gas vertical heat exchanger, 10 is a reactor, 11 is a low-pressure dilution steam pipeline, 12 is a regenerator, 13 is a two-stage cyclone, 14 is a three-stage cyclone, 15 is a heat exchanger III, 16 is a quench tower, 17 is a feed pipeline, 18 is a water scrubber, 19 is a reactor compressor, 20 is a product separation device, and 21 is a product collection tank.
Detailed Description
In order to make the technical solution of the present utility model better understood by those skilled in the art, the technical solution of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model, and it is apparent that the described embodiments are only some embodiments of the present utility model, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present utility model without making any inventive effort, shall fall within the scope of the present utility model.
In the description of the present utility model, it should be understood that the terms "center," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like indicate orientations or positional relationships based on the orientation or positional relationships shown in the drawings, merely to simplify the description of the present utility model, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model.
As can be seen from the attached drawing, the device for preparing the low-carbon olefin from the methanol comprises a methanol buffer tank 1, wherein the discharge end of the methanol buffer tank 1 is communicated with a heat exchanger I through a feed pump 2, and the heat exchanger I comprises an in-reactor heat collector 3, a methanol purified water heat exchanger 4 and a methanol-condensed water heat exchanger 5 which are sequentially connected in series;
the discharge end of the methanol-condensation water heat exchanger 5 is communicated with a heat exchanger II, and comprises three paths, namely a methanol-stripping gas heat exchanger 6, a methanol-steam heat exchanger 7 and a methanol booster pump 8 which are connected in parallel, wherein an atomizing nozzle is arranged at the discharge end of the methanol booster pump 8, methanol is boosted by the booster pump and atomized by the atomizing nozzle, and then is mixed with the gasified methanol in the first two paths; after mixing, the mixture enters a methanol-reaction gas vertical heat exchanger 9, a methanol outlet of the methanol-reaction gas vertical heat exchanger 9 and an air outlet end of a low-pressure dilution steam pipeline 11 are communicated with a feeding pipeline 17, a discharging end of the feeding pipeline 17 is communicated with a feeding end I of a reactor 10, a feeding end II of the reactor 10 is communicated with a discharging end of a regenerator 12, a high-temperature reaction gas discharging end of the reactor 10 is communicated with a two-stage cyclone separator 13 and a three-stage cyclone separator 14 which are sequentially connected in series through the methanol-reaction gas vertical heat exchanger 9, a discharging end of the three-stage cyclone separator 14 is sequentially communicated with a heat exchanger III 15 and a quenching tower 16, a discharging end of the quenching tower 16 is sequentially communicated with a water washing tower 18, a reaction gas compressor 19 and a product separation device 20, and the product separation device 20 is communicated with a product collecting tank 21.
The process flow of the application is as follows: methanol from outside the device enters a methanol buffer tank 1, is boosted by a methanol feed pump 2, is subjected to heat exchange to 75 ℃ by a heat collector 3, a methanol-purified water heat exchanger 4 and a methanol-condensed water heat exchanger 5 in the reactor, and is divided into three paths: the first path is subjected to heat exchange 6 by a methanol-stripping gas heat exchanger, the second path is subjected to heat exchange 7 by a methanol-steam heat exchanger, so that methanol is gasified, the third path is subjected to pressure boosting by a methanol booster pump 8 and is atomized by an atomization nozzle, and is mixed with the methanol after the first two paths of gasification before a methanol-reaction gas vertical heat exchanger 9, and then enters the methanol-reaction gas vertical heat exchanger 9 to be fully subjected to heat exchange with high-temperature reaction gas from a reactor 10 so as to recover high-temperature heat of the reaction gas, and the methanol after heat exchange is mixed with low-pressure dilution steam, so that the oil-gas partial pressure in the reactor 10 can be effectively reduced, the contact time of the methanol, the reaction gas and a catalyst core can be reduced, and side reactions can be reduced; the mixed methanol feed temperature is about 186 ℃, the methanol enters a reactor feed distribution pipe to be in direct contact with a high-temperature regenerated catalyst from a regenerator 12 in a reactor 10, the exothermic reaction is rapidly carried out on a reaction dense bed under the action of the catalyst, the reaction condition of the methanol in the reactor 10 is that the reaction temperature is more than 300 ℃, the methanol and intermediate product dimethyl ether can be completely converted at the temperature higher than 400 ℃, the reaction gas generated in the reactor 10 removes most of carried catalyst through a two-stage cyclone separator 13, the entrained catalyst is removed through a three-stage cyclone separator 14 of the reaction gas, the catalyst is discharged after heat exchange through a heat exchanger, and the product is collected after the heat exchange is carried out on a rear quenching tower 16.
The device of the embodiment, through actual measurement, compared with the prior art, the productivity is increased from 145t/h to 169t/h, and the product yield is not less than 34%.
Although the present utility model has been described in detail by way of preferred embodiments with reference to the accompanying drawings, the present utility model is not limited thereto. Various equivalent modifications and substitutions may be made in the embodiments of the present utility model by those skilled in the art without departing from the spirit and scope of the present utility model, and it is intended that all such modifications and substitutions be within the scope of the present utility model/be within the scope of the present utility model as defined by the appended claims. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.
Claims (6)
1. The utility model provides a device of methyl alcohol preparation light olefin which characterized in that: the device comprises a methanol buffer tank, wherein the discharge end of the methanol buffer tank is communicated with a heat exchanger I through a feed pump, the discharge end of the heat exchanger I is communicated with a heat exchanger II, the discharge end of the heat exchanger II is communicated with a methanol-reaction gas vertical heat exchanger, the methanol outlet of the methanol-reaction gas vertical heat exchanger and the outlet end of a low-pressure dilution steam pipeline are both communicated with a feed pipeline, the discharge end of the feed pipeline is communicated with the feed end I of a reactor, the feed end II of the reactor is communicated with the discharge end of a regenerator, the discharge end of the high-temperature reaction gas of the reactor is communicated with the feed end of a cyclone separator through the methanol-reaction gas vertical heat exchanger, the discharge end of the cyclone separator is sequentially communicated with a heat exchanger III and a quench tower, a reaction gas compressor and a product separation device, and the product separation device is communicated with a product collection tank.
2. The apparatus for preparing light olefins from methanol according to claim 1, wherein: the heat exchanger I comprises an in-reactor heat collector, a methanol purified water heat exchanger and a methanol-condensed water heat exchanger which are sequentially connected in series.
3. The apparatus for preparing light olefins from methanol according to claim 1, wherein: the heat exchanger II comprises a methanol-stripping gas heat exchanger, a methanol-steam heat exchanger and a methanol booster pump which are connected in parallel.
4. The apparatus for preparing light olefins from methanol according to claim 3, wherein: and an atomizing nozzle is arranged at the discharge end of the methanol booster pump.
5. The apparatus for preparing light olefins from methanol according to claim 1, wherein: the low-pressure dilution steam pipeline is tangentially communicated with the feeding pipeline.
6. The apparatus for preparing light olefins from methanol according to claim 1, wherein: the cyclone separator comprises a two-stage cyclone separator and a three-stage cyclone separator which are sequentially connected in series.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123123470.1U CN218989173U (en) | 2021-12-14 | 2021-12-14 | Device for preparing low-carbon olefin from methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202123123470.1U CN218989173U (en) | 2021-12-14 | 2021-12-14 | Device for preparing low-carbon olefin from methanol |
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| Publication Number | Publication Date |
|---|---|
| CN218989173U true CN218989173U (en) | 2023-05-09 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202123123470.1U Active CN218989173U (en) | 2021-12-14 | 2021-12-14 | Device for preparing low-carbon olefin from methanol |
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| CN (1) | CN218989173U (en) |
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- 2021-12-14 CN CN202123123470.1U patent/CN218989173U/en active Active
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