CN203794811U - Reaction product separation system for methanol-to-propylene and methanol-to-olefin - Google Patents
Reaction product separation system for methanol-to-propylene and methanol-to-olefin Download PDFInfo
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- CN203794811U CN203794811U CN201420130896.0U CN201420130896U CN203794811U CN 203794811 U CN203794811 U CN 203794811U CN 201420130896 U CN201420130896 U CN 201420130896U CN 203794811 U CN203794811 U CN 203794811U
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- Prior art keywords
- tower
- depropanizing
- separation system
- methanol
- propylene
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- Expired - Lifetime
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- 238000000926 separation method Methods 0.000 title claims abstract description 35
- 239000007795 chemical reaction product Substances 0.000 title claims abstract description 19
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000005977 Ethylene Substances 0.000 claims abstract description 48
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 30
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 30
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 56
- 238000011084 recovery Methods 0.000 claims description 30
- 229930195733 hydrocarbon Natural products 0.000 claims description 25
- 150000002430 hydrocarbons Chemical class 0.000 claims description 25
- 239000003795 chemical substances by application Substances 0.000 claims description 24
- 238000010521 absorption reaction Methods 0.000 claims description 23
- 238000000605 extraction Methods 0.000 claims description 17
- 230000008929 regeneration Effects 0.000 claims description 17
- 238000011069 regeneration method Methods 0.000 claims description 17
- 230000002745 absorbent Effects 0.000 claims description 15
- 239000002250 absorbent Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 238000000746 purification Methods 0.000 claims description 10
- 238000000034 method Methods 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 150000001336 alkenes Chemical class 0.000 abstract description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 36
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 16
- 229910052799 carbon Inorganic materials 0.000 description 16
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 9
- 239000007789 gas Substances 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000001294 propane Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 230000037351 starvation Effects 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
Classifications
-
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a reaction product separation system for methanol-to-propylene and methanol-to-olefin. The system comprises a depropanizing tower (1), an ethylene rectification tower (7) and a propylene rectification tower (15), wherein the tower top of the depropanizing tower (1) is connected with a demethanizing tower (5); the tower bottom of the demethanizing tower (5) is connected with a deethanizing tower (6); the tower top of the deethanizing tower (6) is connected with the ethylene rectification tower (7); the tower bottom of the deethanizing tower (6) is connected with the propylene rectification tower (15). The utility model aims to provide a separation system, thus simplifying the process, reducing the energy consumption, and improving the olefin yield.
Description
Technical field
The utility model relates to chemical industry, gas chemical industry and field of petrochemical industry, more specifically, relates to a kind of reaction product separation system for preparing propylene from methanol and methanol-to-olefins.
Background technology
Ethene, propylene are the of paramount importance basic materials of petrochemical industry, and its conventional production methods mainly adopts petroleum naphtha thermo-cracking to make, and petroleum resources are relied on serious.Along with the growing tension of petroleum resources supplies, taking coal as raw material production synthetic gas, synthesising gas systeming carbinol, dimethyl ether by methanol dehydration, dme Dehydration alkene obtained significant progress.Traditionally, when taking propylene as major objective product, be called preparing propylene from methanol (MTP) technique, if be called methanol-to-olefins (MTO) technique during regardless of ethene and propylene product volume variance.MTO/MTP technology can be alleviated the pressure of petroleum resources supply to a certain extent, especially meets the national conditions of China's " oil starvation, weak breath, rich coal ".
Industrialized MTP technological reaction product separation flow process is generally: gas hydrocarbon and liquid hydrocarbon after four sections of compressions are sent into respectively depropanizing tower and debutanizing tower, and in debutanizing tower, carbon four separates with carbon five, and carbon four is sent into depropanizing tower together with gas hydrocarbon.The above hydrocarbon of carbon five is sent into dehexanizing column and is carried out carbon five and separate with carbon six and carbon six hydrocarbon, more than six hydrocarbon of carbon from the bottom of tower out, after cooling, become gasoline products.Depropanizing tower overhead product is sent into deethanizing column.Deethanizing column materials at bottom of tower is sent into carbon three knockout towers and is separated, and obtains propylene and propane product.Depropanizing tower substrate is sent into extraction tower, and extraction tower overhead materials and carbon three knockout tower bottoms propane are as LPG product.Deethanizer overhead steam is delivered to demethanizing tower and is separated after deethanizing column compressor pressurizes.Demethanizer column overhead thing is as fuel gas, and bottoms is sent into carbon two knockout towers.Carbon two knockout tower tower tops are ethylene product, and bottoms is as fuel gas.
Existing MTO/MTP reactor product separation system flow process complexity, construction investment is high, and energy consumption is high, the profit margin of reduction enterprise.
Utility model content
For the problem existing in correlation technique, the purpose of this utility model is to provide a kind of reaction product separation system for preparing propylene from methanol and methanol-to-olefins, with simple flow, reduction energy consumption, and improves olefin yields.
For achieving the above object, the utility model provides a kind of reaction product separation system for preparing propylene from methanol and methanol-to-olefins, comprise: depropanizing tower, ethylene rectification tower and propylene rectification tower, wherein, the tower top of depropanizing tower is connected with demethanizing tower, at the bottom of the tower of demethanizing tower, be connected with deethanizing column, the tower top of deethanizing column is connected with ethylene rectification tower, at the bottom of the tower of deethanizing column, is connected with propylene rectification tower.
According to the utility model, between depropanizing tower and demethanizing tower, be connected with lighter hydrocarbons moisture eliminator, lighter hydrocarbons pre-cooler and lighter hydrocarbons in turn and divide flow container, wherein, at the bottom of the tank deck that lighter hydrocarbons divide flow container and tank, be all connected with demethanizing tower.
According to the utility model, at the bottom of the tower of depropanizing tower, be connected with pre-cooler at the bottom of depropanizing tower tower, extractor and extraction tower in turn, wherein, at the bottom of depropanizing tower tower, pre-cooler is connected to the tank deck of extractor, at the bottom of the tank deck of extractor is also connected to the tower of extraction tower.
According to the utility model, the tower top of extraction tower and C
4purification tower connects, wherein, and C
4the tower top of purification tower is provided with the tower top of demethanizing tower the pipeline being connected with ethylene recovery.
According to the utility model, ethylene recovery is connected with absorbent regeneration tower by absorption agent water cooler, wherein, connects successively the pipe side of absorption agent water cooler and the tower top of absorbent regeneration tower at the bottom of the tower of ethylene recovery; At the bottom of the tower of absorbent regeneration tower, connect successively the shell-side of absorption agent water cooler and the tower top of ethylene recovery.
According to the utility model, the charging of depropanizing tower is from the outlet of four sections of compressors.
According to the utility model, difference output ethene and ethane at the bottom of the tower top of ethylene rectification tower and tower, difference output propylene and propane at the bottom of the tower top of propylene rectification tower and tower.
According to the utility model, the bottom product of extraction tower is the aqueous solution containing methyl alcohol, C
4the bottom product of purification tower is the hydro carbons such as carbon five and carbon six.
According to the utility model, at the bottom of the tower top of ethylene recovery and tower, obtain respectively the ethylene component of methane fuel gas and recovery.
Useful technique effect of the present utility model is:
In separation system of the present utility model, reaction product to be separated directly enters depropanizing tower, then successively via demethanizing tower and deethanizing column, further isolate ethylene product and propylene product by the ethylene rectification tower being connected with deethanizing column respectively and propylene rectification tower.Compared with prior art, simplify separation process, reduced construction investment and running cost.
In addition, in separation system of the present utility model is applied in to MTO/MTP technological reaction product separation time, because absorption agent in ethylene recovery can be regenerated in absorbent regeneration tower, and again return in ethylene recovery.Therefore, improved the utilising efficiency of absorption agent.
Brief description of the drawings
Fig. 1 is the structural representation of separation system of the present utility model.
Embodiment
Referring now to Fig. 1, the reaction product separation system for preparing propylene from methanol and methanol-to-olefins of the present utility model is described.Shown in Fig. 1 is the structural representation of this separation system, and it comprises: depropanizing tower 1, ethylene rectification tower 7 and propylene rectification tower 15.Wherein, the tower top of depropanizing tower 1 is connected with demethanizing tower 5, is connected with deethanizing column 6 at the bottom of the tower of demethanizing tower 5.Further, the tower top of deethanizing column 6 is connected with ethylene rectification tower 7, at the bottom of the tower of deethanizing column 6, is connected with propylene rectification tower 15.
Continue with reference to Fig. 1, particularly, between depropanizing tower 1 and demethanizing tower 5, be connected with lighter hydrocarbons moisture eliminator 2, lighter hydrocarbons pre-cooler 3 and lighter hydrocarbons in turn and divide flow container 4.Wherein, at the bottom of the tank deck that lighter hydrocarbons divide flow container 4 and tank, be all connected with demethanizing tower 5.
In addition, at the bottom of the tower of depropanizing tower 1, be connected with pre-cooler 11 at the bottom of depropanizing tower tower, extractor 12 and extraction tower 13 in turn.And pre-cooler 11 is connected to the tank deck of extractor 12 at the bottom of depropanizing tower tower, at the bottom of the tank deck of extractor 12 is also connected to the tower of extraction tower 13.In addition at the bottom of the tank of extractor 12, return in the washing step of the utility model separation system other operating systems before.
Further, the tower top of extraction tower 13 is connected to the C for carbon four is purified
4purification tower 14, and C
4the tower top of purification tower 14 is provided with the tower top of demethanizing tower 5 pipeline being connected with ethylene recovery 8.In other words, the overhead product of demethanizing tower 5 is connected by pipeline with ethylene recovery 8, and from C
4in the product transfer lime that purification tower 14 tower tops connect, extracting one out is connected by pipeline with ethylene recovery 8 as absorption agent.
Referring again to Fig. 1, ethylene recovery 8 is connected with absorbent regeneration tower 10 by absorption agent water cooler 9.
Particularly, at the bottom of the tower of ethylene recovery 8, connect successively the pipe side of absorption agent water cooler 9 and the tower top of absorbent regeneration tower 10; And at the bottom of the tower top of ethylene recovery 8 connects the shell-side of absorption agent water cooler 9 and the tower of absorbent regeneration tower 10 successively.
An example of concrete sepn process when separation system of the present utility model is applied in MTO/MTP technological reaction product separation is described now by reference to the accompanying drawings.
From the reaction product of reactor outlet, deviate from cooled reaction product through chilling, four-stage compressor compression and impurity and comprise water, methyl alcohol, dme, hydrogen, carbon monoxide, carbonic acid gas, C
1to C
5and a small amount of C
6.2.275MPaG with under the condition of 42 DEG C, enter depropanizing tower 1 together with washing methyl alcohol, wherein the throughput ratio of lower carbon number hydrocarbons and washing methyl alcohol remains between 3～9, to ensure that methyl alcohol can all deviate from the dme in reaction product.After separating, depropanizing tower 1 bottom product is mainly C
4, C
5and methyl alcohol, then bottom product pre-cooler 11 at the bottom of depropanizing tower tower is cooled to 38 DEG C to enter extractor 12, then enters extraction tower 13, further, at the bottom of the tank of extractor 12, is back in aforesaid washing step.
C
4and C
5hydrocarbon using water as extraction agent, extracts the methyl alcohol in depropanizing tower 1 bottom product in extraction tower 13 at 2.35MPaG and 38 DEG C, and extraction tower 13 tower tops obtain C
4and C
5cut.Then pass through C
4purification tower 14 obtains respectively liquefied gas product and C at the bottom of tower top and tower under 0.49MPaG
5/ C
6deng hydro carbons.Wherein part C
4in ethylene recovery 8, reclaim the ethene in demethanizing tower 5 overhead products, all the other C as absorption agent
4as liquefied gas product, and C
5be back to reactive system.In addition, the bottom product of extraction tower 13 is to be back to and to return to methanol recovery system containing the aqueous solution of methyl alcohol.
On the other hand, the overhead product of depropanizing tower 1 is mainly hydrogen, C
2and C
3above cut.In this light hydrocarbon stream stock-traders' know-how lighter hydrocarbons moisture eliminator 2, adopt molecular sieve drying dehydration, be then cooled to-8 DEG C via lighter hydrocarbons pre-cooler 3, then after lighter hydrocarbons divide flow container 4, enter demethanizing tower 5.
The bottom product C of demethanizing tower 5
2and C
3enter deethanizing column 6 and carry out C
2and C
3separation.The C of deethanizing column 6 tower tops
2cut enters ethylene rectification tower 7.The tower top of ethylene rectification tower 7 obtains ethylene product, and obtains ethane product at the bottom of its tower.
C at the bottom of deethanizing column 6 towers
3cut enters propylene rectification tower 15 under 2.3MPaG and 55 DEG C of conditions, obtains respectively propylene and propane product at the bottom of its tower top and tower.
Further, the tower top material C of demethanizing tower 5
1and C
2, and C
4the C of purification tower 14 tower tops
4under 2.0MPaG and-41 DEG C of conditions, enter together ethylene recovery 8.Then, in ethylene recovery 8, utilize C
4reclaim the ethene in demethanizing tower 5 products as absorption agent.
Wherein, ethylene recovery 8 overhead products are methane, are back to reactive system, and are absorption agent C at the bottom of tower
4and part C
2.Ethylene recovery 8 bottom products are heated to 2 DEG C through absorption agent water cooler 9 and enter absorbent regeneration tower 10, and absorbent regeneration tower 10 tower tops are the C reclaiming
2hydrocarbon, is back to compression section.At the bottom of the tower of absorbent regeneration tower 10, be the absorption agent C after regeneration
4, it again enters in ethylene recovery 8 as absorption agent in absorption agent water cooler 9 with after ethylene recovery 8 bottom product heat exchange.So far complete whole sepn process.
Table 1 is that calculation result shows that the mass concentration of ethylene product is 95% by the separating resulting of process described above, and yield is 26.59%; And the mass concentration of propylene product is 99.6%, yield is 99.1%.
| Logistics title | Unit | Depropanizing tower charging | Ethylene product | Propylene product |
| Temperature | ℃ | 42 | -13.8 | 40 |
| Pressure | MPaG | 2.275 | 2.8 | 1.82 |
| Mass rate | Kg/h | 186504.3 | 8910.4 | 77559.4 |
| Each constituent mass flow | Kg/h | ? | ? | ? |
| H 2O | ? | 246.38 | 0 | 0 |
| Methyl alcohol | ? | 161.38 | 0 | 0 |
| Dme | ? | 1031.63 | 0 | 0 |
| H 2 | ? | 22.44 | 0 | 0 |
| CO | ? | 932.24 | 0 | 0 |
| CO 2 | ? | 0.2 | 0 | 0 |
| Methane | ? | 4837.02 | 1.8 | 0 |
| Ethene | ? | 31841.19 | 8465.2 | 0.03 |
| Ethane | ? | 5086.68 | 438.94 | 39.77 |
| Propylene | ? | 77951.65 | 4.46 | 77249.22 |
| Propane | ? | 2247.36 | 0 | 270.39 |
| C 4 | ? | 51479.16 | 0 | 0 |
| C 5 | ? | 10214.18 | 0 | 0 |
| C 6And more than | ? | 452.76 | 0 | 0 |
Table 1
In sum, in separation system of the present utility model, reaction product to be separated directly enters depropanizing tower 1, then successively via demethanizing tower 5 and deethanizing column 6, further isolate ethylene product and propylene product by the ethylene rectification tower 7 being connected with deethanizing column 6 respectively and propylene rectification tower 15.Compared with prior art, separation system of the present utility model is applied in to MTO/MTP technique, can have effectively simplified the flow process of existing MTO/MTP technological reaction product separation system.That is, simplify separation process, reduced construction investment and running cost.
In addition, in separation system of the present utility model is applied in to MTO/MTP technological reaction product separation time, owing to interconnecting by absorption agent water cooler 9 between ethylene recovery 8 and absorbent regeneration tower 10, that is to say, in ethylene recovery 8 reacted absorption agent can be in absorbent regeneration tower 10 regeneration, and again return in ethylene recovery 8.Therefore, improved the utilising efficiency of absorption agent.
Further, in separation system of the present utility model is applied in to MTO/MTP technological reaction product separation time, because separation system of the present utility model has adopted predepropanization separation process, and can use C
4as absorption agent.Therefore, be conducive to low-grade utility and the cold recovery of cold sepn process, avoid adopting the deep cooling ice chest and the ethylene compressor that expend large energy, have technical process simple, investment and the low feature of energy consumption, have good applicability to MTO/MTP technology.
The foregoing is only preferred embodiment of the present utility model, be not limited to the utility model, for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any amendment of doing, be equal to replacement, improvement etc., within all should being included in protection domain of the present utility model.
Claims (5)
1. for a reaction product separation system for preparing propylene from methanol and methanol-to-olefins, it is characterized in that, comprising: depropanizing tower (1), ethylene rectification tower (7) and propylene rectification tower (15),
Wherein, the tower top of described depropanizing tower (1) is connected with demethanizing tower (5), is connected with deethanizing column (6) at the bottom of the tower of described demethanizing tower (5),
The tower top of described deethanizing column (6) is connected with described ethylene rectification tower (7), at the bottom of the tower of described deethanizing column (6), is connected with described propylene rectification tower (15).
2. separation system according to claim 1, is characterized in that,
Between described depropanizing tower (1) and described demethanizing tower (5), be connected with lighter hydrocarbons moisture eliminator (2), lighter hydrocarbons pre-cooler (3) and lighter hydrocarbons in turn and divide flow container (4),
Wherein, at the bottom of the tank deck that described lighter hydrocarbons divide flow container (4) and tank, be all connected with described demethanizing tower (5).
3. separation system according to claim 1, is characterized in that,
At the bottom of the tower of described depropanizing tower (1), be connected with pre-cooler (11) at the bottom of depropanizing tower tower, extractor (12) and extraction tower (13) in turn,
Wherein, at the bottom of described depropanizing tower tower, pre-cooler (11) is connected to the tank deck of described extractor (12), at the bottom of the tank deck of described extractor (12) is also connected to the tower of described extraction tower (13).
4. separation system according to claim 3, is characterized in that,
Tower top and the C of described extraction tower (13)
4purification tower (14) connects,
Wherein, described C
4the tower top of purification tower (14) is provided with the tower top of described demethanizing tower (5) pipeline being connected with ethylene recovery (8).
5. separation system according to claim 4, is characterized in that,
Described ethylene recovery (8) is connected with absorbent regeneration tower (10) by absorption agent water cooler (9),
Wherein, at the bottom of the tower of described ethylene recovery (8), connect successively the pipe side of absorption agent water cooler (9) and the tower top of described absorbent regeneration tower (10); At the bottom of the tower of described absorbent regeneration tower (10), connect successively the shell-side of described absorption agent water cooler (9) and the tower top of described ethylene recovery (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420130896.0U CN203794811U (en) | 2014-03-20 | 2014-03-20 | Reaction product separation system for methanol-to-propylene and methanol-to-olefin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420130896.0U CN203794811U (en) | 2014-03-20 | 2014-03-20 | Reaction product separation system for methanol-to-propylene and methanol-to-olefin |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203794811U true CN203794811U (en) | 2014-08-27 |
Family
ID=51377044
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420130896.0U Expired - Lifetime CN203794811U (en) | 2014-03-20 | 2014-03-20 | Reaction product separation system for methanol-to-propylene and methanol-to-olefin |
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| Country | Link |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106478350A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separate and the method using by-product propylene enhancing |
| CN106478335A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The separation of alcohol and/or ether olefin product and the method for coproduction ethylbenzene |
| CN106478344A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separation method |
| CN106478348A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or the separation method of ether propylene product |
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| CN106478343A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separate the method utilizing |
| CN106478346A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separate and the method using lighter hydrocarbons propylene enhancing |
| CN106478333A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or the separation method of ether olefin product |
| CN106478336A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The separation of alcohol and/or ether olefin product and the method for by-product process |
| CN106478334A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The separation of alcohol and/or ether olefin product and the method using by-product coproduction ethylbenzene |
| CN106478347A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether olefin product separate and the method using by-product volume increase alkene |
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- 2014-03-20 CN CN201420130896.0U patent/CN203794811U/en not_active Expired - Lifetime
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| CN106478350A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separate and the method using by-product propylene enhancing |
| CN106478335A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | The separation of alcohol and/or ether olefin product and the method for coproduction ethylbenzene |
| CN106478344A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separation method |
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| CN106478349A (en) * | 2015-08-28 | 2017-03-08 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product processing method |
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| CN106478344B (en) * | 2015-08-28 | 2018-10-23 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product separation method |
| CN106478333B (en) * | 2015-08-28 | 2018-10-23 | 中国石油化工股份有限公司 | The separation method of alcohol and/or ether olefin product |
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| CN106478349B (en) * | 2015-08-28 | 2018-11-20 | 中国石油化工股份有限公司 | Alcohol and/or ether propylene product processing method |
| CN106478348B (en) * | 2015-08-28 | 2018-11-20 | 中国石油化工股份有限公司 | The separation method of alcohol and/or ether propylene product |
| CN106478336B (en) * | 2015-08-28 | 2019-04-12 | 中国石油化工股份有限公司 | The method of the separation of alcohol and/or ether olefin product and by-product processing |
| CN106478334B (en) * | 2015-08-28 | 2019-05-14 | 中国石油化工股份有限公司 | The separation of alcohol and/or ether olefin product and the method for utilizing by-product coproduction ethylbenzene |
| CN106478335B (en) * | 2015-08-28 | 2019-05-14 | 中国石油化工股份有限公司 | The method of the separation and coproduction ethylbenzene of alcohol and/or ether olefin product |
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