CN101130488A - Catalyst temperature raising method for producing dimethyl ether by gas phase method - Google Patents
Catalyst temperature raising method for producing dimethyl ether by gas phase method Download PDFInfo
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- CN101130488A CN101130488A CNA2007100496967A CN200710049696A CN101130488A CN 101130488 A CN101130488 A CN 101130488A CN A2007100496967 A CNA2007100496967 A CN A2007100496967A CN 200710049696 A CN200710049696 A CN 200710049696A CN 101130488 A CN101130488 A CN 101130488A
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- dme
- temperature
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- catalyzer
- nitrogen
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- 238000000034 method Methods 0.000 title claims abstract description 39
- 239000003054 catalyst Substances 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title abstract description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 50
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 25
- 239000012159 carrier gas Substances 0.000 claims abstract description 13
- 239000012808 vapor phase Substances 0.000 claims description 15
- 230000006837 decompression Effects 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 42
- 238000010438 heat treatment Methods 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 4
- 239000007789 gas Substances 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 2
- 208000019901 Anxiety disease Diseases 0.000 description 1
- 230000036506 anxiety Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Abstract
The invention discloses a catalyst heating method for producing dimethyl ether by a gas phase method, which is characterized in that factory air is used as carrier gas to heat a catalyst at the initial stage of catalyst heating, when the temperature of the catalyst is increased to 80-280 ℃, the carrier gas for heating is switched into superheated steam or heated nitrogen to continue heating to the initial reaction temperature range of the catalyst of 190-335 ℃. Compared with the traditional method for heating the dimethyl ether catalyst by using nitrogen, the method disclosed by the invention has the advantages that under the condition that the nitrogen source is short or the flow is insufficient, the requirement of the catalyst on the large flow of nitrogen at the initial heating stage is reduced, the heating cost is reduced, and the heating time is shortened. On the premise of ensuring the activity of the catalyst, the one-way conversion rate of the methanol is improved, and the methanol consumption of ton products is reduced.
Description
Technical field
The present invention relates to the chemical materials production field, be specifically related to a kind of method that vapor phase process is produced the catalyzer temperature-elevating of dme that is used for.
Background technology
Conventional gas-phase method dme production equipment is all done carrier gas with the nitrogen after the heating at the catalyzer temperature-elevating at the initial stage of driving, and the bed catalyzer is heated up.The weak point of this method is, along with the expansion of unit scale, the nitrogen amount of catalyzer temperature-elevating demand also increases thereupon, the also corresponding increase of required time that heats up, so the facility investment of producing nitrogen also is multiplied.
Summary of the invention
The technical problem to be solved in the present invention provides a kind of method that heats up to the catalyzer that is used for vapor phase process production dme, this method is when catalyzer temperature-elevating initial stage nitrogen is nervous, can save the driving time guaranteeing not influence under the prerequisite of catalyst activity, and the heating-up time can be shortened, reduce the intensification cost, improve the methyl alcohol per pass conversion, reduce the methanol consumption of ton product.
Technical problem proposed by the invention is to solve like this, a kind of catalyzer temperature-elevating method that vapor phase process is produced dme that is used for is provided, it is characterized in that, utilize factory air catalyzer to be heated up at the catalyzer temperature-elevating initial stage as carrier gas, after catalyst temperature rose to 80～280 ℃, will heat up switched to superheated vapour or heated nitrogen with carrier gas and continues to be warming up in 190～335 ℃ of the catalyzer initial reaction temperature scopes again.
According to the catalyzer temperature-elevating method that is used for vapor phase process production dme provided by the present invention, it is characterized in that, before entering dme building-up reactions tower, distinguish the air line and the vapour line of mounting strap valve behind the door with nitrogen valve.
Be used for the catalyzer temperature-elevating method that vapor phase process is produced dme according to provided by the present invention, it is characterized in that,, open the air line valve and make factory air through the driving heater heats with 3000m at the catalyzer temperature-elevating initial stage
3/ h flow velocity enters dme building-up reactions tower, and beds is heated up.
According to the catalyzer temperature-elevating method that is used for vapor phase process production dme provided by the present invention, it is characterized in that, after catalyst temperature rises to 80～280 ℃, close the valve on the air line, valve or the nitrogen valve opened simultaneously on the vapour line make superheated vapour or nitrogen enter dme building-up reactions tower, and beds is proceeded to heat up.
According to the catalyzer temperature-elevating method that is used for vapor phase process production dme provided by the present invention, it is characterized in that, when described superheated vapour pressure is higher than dme building-up reactions tower working pressure far away, should make carrier gas vapor pressure and dme building-up reactions tower working pressure keep pressure reduction about 2kg/h by the depressurized system decompression.
The present invention adopts the method for nitrogen temperature dimethyl ether catalyst to compare with tradition, and its advantage is:
(1) under the situation of nitrogen source anxiety or underfed, satisfies the catalyzer temperature-elevating condition and shorten the heating-up time.
(2) reduced the big traffic demand of catalyzer temperature-elevating initial stage, reduced the intensification cost nitrogen.
(3) under the prerequisite that guarantees catalyst activity, improve the methyl alcohol per pass conversion, reduced the methanol consumption of ton product.
Description of drawings
Below in conjunction with accompanying drawing embodiments of the present invention are elaborated.
Fig. 1 is the fundamental diagram that is used for the catalyzer temperature-elevating method of vapor phase process production dme provided by the invention.
Wherein, 1, the driving well heater, 2, dme building-up reactions tower.
Embodiment
As shown in Figure 1, be the fundamental diagram that is used for the catalyzer temperature-elevating method of vapor phase process production dme provided by the invention.Utilize factory air catalyzer to be heated up at the catalyzer temperature-elevating initial stage as carrier gas, after catalyst temperature rose to 80～280 ℃, will heat up switched to superheated vapour or heated nitrogen with carrier gas and continues to be warming up in 190～335 ℃ of the catalyzer initial reaction temperature scopes again.
Before entering dme building-up reactions tower 2, distinguish the air line and the vapour line of mounting strap valve behind the door with nitrogen valve.At the catalyzer temperature-elevating initial stage, open the air line valve and make the factory air that heats through driving well heater 1 with 3000m
3/ h flow velocity enters dme building-up reactions tower 2, and beds is heated up.After catalyst temperature rises to 80～280 ℃, close the valve on the air line, valve or the nitrogen valve opened simultaneously on the vapour line make superheated vapour or nitrogen enter dme building-up reactions tower 2, and beds is proceeded to heat up.When described superheated vapour pressure is higher than dme building-up reactions tower 2 working pressures far away, should make carrier gas vapor pressure and dme building-up reactions tower 2 working pressures keep pressure reduction about 2kg/h, could be used as carrier gas by the depressurized system decompression.
The present invention adopts the method for nitrogen temperature dimethyl ether catalyst to compare with tradition, under the prerequisite that guarantees catalyst activity, reduced the big traffic demand of catalyzer temperature-elevating initial stage to nitrogen, reduced the intensification cost, shortened the heating-up time, improve the methyl alcohol per pass conversion, reduced the methanol consumption of ton product.
Embodiment 1:
Reaction bed temperature in dme building-up reactions tower 2 is that air is with 3000m under 21 ℃
3/ h flow velocity enters dme building-up reactions tower 2 after driving well heater 1 is heated to 380 ℃.After 40 minutes, reaction bed temperature is raised to 270 ℃, closes pressure lock, drives steam valve, and superheat steam temperature is 480 ℃, and after 20 minutes, reaction bed temperature is raised to 300 ℃.Close steam valve, driving feeds intake.
This produces result data:
The methyl alcohol per pass conversion is 85%, 1.405 tons of methyl alcohol ton consumptions, and product purity can reach 99.99%.
Embodiment 2:
Reaction bed temperature in dme building-up reactions tower 2 is that air is with 3000m under 21 ℃
3/ h flow velocity enters dme building-up reactions tower 2 after driving well heater 1 is heated to 380 ℃.After 40 minutes, reaction bed temperature is raised to 268 ℃, closes pressure lock, drives steam valve, and superheat steam temperature is 480 ℃, and after 20 minutes, reaction bed temperature is raised to 301 ℃.Close steam valve, driving feeds intake.
This produces result data:
The methyl alcohol per pass conversion is 85%, 1.405 tons of methyl alcohol ton consumptions, and product purity can reach 99.99%.
Embodiment 3:
Reaction bed temperature in dme building-up reactions tower 2 is that air is with 3000m under 20 ℃
3/ h flow velocity enters dme building-up reactions tower 2 after driving well heater 1 is heated to 380 ℃.After 40 minutes, reaction bed temperature is raised to 267 ℃, closes pressure lock, drives steam valve, and superheat steam temperature is 480 ℃, and after 22 minutes, reaction bed temperature is raised to 300 ℃.Close steam valve, driving feeds intake.
This produces result data:
The methyl alcohol per pass conversion is 85%, 1.405 tons of methyl alcohol ton consumptions, and product purity can reach 99.99%.
Though described embodiments of the present invention in conjunction with the accompanying drawings, the protection domain that those of ordinary skills do not need various distortion that creativity work just can make or modification still to belong to this patent within the scope of the appended claims.
Claims (5)
1. one kind is used for the catalyzer temperature-elevating method that vapor phase process is produced dme, it is characterized in that, utilize factory air catalyzer to be heated up at the catalyzer temperature-elevating initial stage as carrier gas, after catalyst temperature rose to 80～280 ℃, will heat up switched to superheated vapour or heated nitrogen with carrier gas and continues to be warming up in 190～335 ℃ of the catalyzer initial reaction temperature scopes again.
2. according to claim 1ly be used for the catalyzer temperature-elevating method that vapor phase process is produced dme, it is characterized in that, entering the preceding and nitrogen valve of dme building-up reactions tower (2) air line and the vapour line of mounting strap valve respectively behind the door.
3. the catalyzer temperature-elevating method that is used for vapor phase process production dme according to claim 1 is characterized in that, at the catalyzer temperature-elevating initial stage, opens the air line valve and makes the factory air that heats through driving well heater (1) with 3000m
3/ h flow velocity enters dme building-up reactions tower (2), and beds is heated up.
4. the catalyzer temperature-elevating method that is used for vapor phase process production dme according to claim 1, it is characterized in that, after catalyst temperature rises to 80～280 ℃, close the valve on the air line, valve or the nitrogen valve opened simultaneously on the vapour line make superheated vapour or nitrogen enter dme building-up reactions tower (2), and beds is proceeded to heat up.
5. the catalyzer temperature-elevating method that is used for vapor phase process production dme according to claim 1, it is characterized in that, when described superheated vapour pressure is higher than dme building-up reactions tower (2) working pressure far away, should make carrier gas vapor pressure and dme building-up reactions tower (2) working pressure keep pressure reduction about 2kg/h by the depressurized system decompression.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007100496967A CN101130488A (en) | 2007-08-08 | 2007-08-08 | Catalyst temperature raising method for producing dimethyl ether by gas phase method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007100496967A CN101130488A (en) | 2007-08-08 | 2007-08-08 | Catalyst temperature raising method for producing dimethyl ether by gas phase method |
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| CN101130488A true CN101130488A (en) | 2008-02-27 |
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| CNA2007100496967A Pending CN101130488A (en) | 2007-08-08 | 2007-08-08 | Catalyst temperature raising method for producing dimethyl ether by gas phase method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288603A (en) * | 2013-06-06 | 2013-09-11 | 贵州天福化工有限责任公司 | Optimized dimethyl ether device driving method |
| CN110183301A (en) * | 2019-05-31 | 2019-08-30 | 国家能源投资集团有限责任公司 | Preparing propylene from methanol system and the method that feeds intake of driving is carried out using it |
-
2007
- 2007-08-08 CN CNA2007100496967A patent/CN101130488A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288603A (en) * | 2013-06-06 | 2013-09-11 | 贵州天福化工有限责任公司 | Optimized dimethyl ether device driving method |
| CN103288603B (en) * | 2013-06-06 | 2015-03-18 | 贵州天福化工有限责任公司 | Optimized dimethyl ether device driving method |
| CN110183301A (en) * | 2019-05-31 | 2019-08-30 | 国家能源投资集团有限责任公司 | Preparing propylene from methanol system and the method that feeds intake of driving is carried out using it |
| CN110183301B (en) * | 2019-05-31 | 2022-06-28 | 国家能源投资集团有限责任公司 | Methanol-to-propylene system and method for starting and feeding by using same |
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Open date: 20080227 |