CN112516730A - MTO product gas clean system - Google Patents
MTO product gas clean system Download PDFInfo
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- CN112516730A CN112516730A CN202011553031.1A CN202011553031A CN112516730A CN 112516730 A CN112516730 A CN 112516730A CN 202011553031 A CN202011553031 A CN 202011553031A CN 112516730 A CN112516730 A CN 112516730A
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- Prior art keywords
- product gas
- mto product
- purification system
- heat exchanger
- gas purification
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 239000000428 dust Substances 0.000 claims abstract description 59
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 54
- 238000011084 recovery Methods 0.000 claims abstract description 39
- 238000000746 purification Methods 0.000 claims abstract description 33
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 238000000034 method Methods 0.000 claims abstract description 29
- 238000005406 washing Methods 0.000 claims abstract description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 30
- 238000011144 upstream manufacturing Methods 0.000 claims description 7
- 239000000919 ceramic Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 239000012716 precipitator Substances 0.000 claims 2
- 239000007789 gas Substances 0.000 abstract description 79
- 239000002918 waste heat Substances 0.000 abstract description 10
- 230000000903 blocking effect Effects 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 56
- 239000006227 byproduct Substances 0.000 description 11
- 239000007921 spray Substances 0.000 description 8
- 239000010802 sludge Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 5
- 150000001336 alkenes Chemical class 0.000 description 4
- -1 ethylene, propylene Chemical group 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229920002313 fluoropolymer Polymers 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/60—Combinations of devices covered by groups B01D46/00 and B01D47/00
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention discloses an MTO product gas purification system which comprises a dust remover, a heat recovery part and a water washing tower which are sequentially connected, wherein the heat recovery part adopts a tubular heat exchanger taking process water as a heat exchange medium, the process water circulates in a heat exchange tube of the tubular heat exchanger, the MTO product gas circulates outside the heat exchange tube of the tubular heat exchanger, and the dust remover adopts a bag type dust remover. The MTO product gas purification system can effectively recycle the waste heat of the MTO product gas, the process water required by operation is less, the blocking risk is small, the recovery rate of the catalyst is high, and the operation cost is low.
Description
Technical Field
The invention relates to the technical field of MTO product gas purification, in particular to an MTO product gas purification system.
Background
Methanol To Olefins (MTO), namely Methanol To Olefins (MTO), is introduced into a reactor, and the Methanol gas is dehydrated under the action of a catalyst to form MTO product gas, wherein the main components of the MTO product gas are ethylene, propylene and water vapor, and of course, some byproducts and fine catalyst dust are mixed in the MTO product gas. The particle diameter of the catalyst dust is generally about 1 um-10 um, and the concentration is generally 400-600 mg/Nm3Left and right.
To avoid fouling and plugging of downstream equipment by fine catalyst dust and to ensure the purity of the MTO product gas, the MTO product gas needs to be cleaned to remove dust and by-products.
The existing MTO product gas purification system mainly adopts a cyclone dust collector to carry out primary dust removal, then adopts a spray tower to carry out secondary dust removal and separate out byproducts, and then adopts a water washing tower to further carry out dust removal and separate out the byproducts. The purification system has the defects of difficult waste heat recovery, high operation cost, easy blockage, low catalyst recovery rate and the like.
In view of the above, how to circumvent some or all of the above disadvantages of MTO product gas purification systems is a technical problem that needs to be solved by those skilled in the art.
Disclosure of Invention
In order to solve the technical problem, the invention provides an MTO product gas purification system which comprises a dust remover, a heat recovery part and a water washing tower which are sequentially connected, wherein the heat recovery part adopts a tubular heat exchanger which takes process water as a heat exchange medium, the process water circulates in a heat exchange tube of the tubular heat exchanger, and the MTO product gas circulates outside the heat exchange tube of the tubular heat exchanger.
In one embodiment, the heat recovery section comprises a plurality of sets of tubular heat exchangers, the product gas inlet and outlet of each set of tubular heat exchangers are connected in sequence, and the MTO product gas flows through each set of tubular heat exchangers in sequence.
In one embodiment, the process water inlet and outlet of each group of the tube heat exchangers are connected in sequence, and the process water flows through each group of the tube heat exchangers in sequence, and flows through the downstream tube heat exchanger first and then flows through the upstream tube heat exchanger.
In one embodiment, fins are arranged on the outer wall of the heat exchange tube of the upstream tube type heat exchanger.
In one embodiment, the duster is a bag duster.
In one embodiment, the filter bag of the bag house is a metal filter bag or a ceramic filter bag.
In one embodiment, the MTO product gas purification system further comprises a gas-gas heat exchanger using methanol gas as a heat exchange medium, the gas-gas heat exchanger being connected between the dust separator and the heat recovery section.
In one embodiment, the MTO product gas purification system further comprises a catalyst recovery storage tank, wherein an ash discharge port is formed in the bottom of the dust remover, and the catalyst recovery storage tank is arranged at the ash discharge port.
According to the MTO product gas purification system provided by the invention, in the heat recovery process, the process water does not directly contact the MTO product gas, so that oil sludge and wax substances are not mixed in the process water, and therefore, the wastewater discharged by the heat recovery part can be directly used for supplying heat to heat-using equipment without treatment, so that the waste heat of the system is effectively recycled.
Further, the heat exchange tubes of the heat recovery section can intercept the catalyst dust to have the effect of further removing dust and by-products, so that the catalyst dust content and by-product content in the MTO product gas entering the water wash column are low, so that the amount of sludge and wax formed in the water wash column is reduced, and the risk of system plugging is small.
In addition, the heat recovery part achieves the purpose of dust removal by means of interception of the heat exchange tubes, so that liquid-gas ratio does not need to be considered, the process water consumption can be controlled to be low, and the system operation cost can be controlled to be low.
In a further scheme, set up the dust remover into bag collector, can further reduce the risk of system blocking to can promote the rate of recovery of catalyst.
Drawings
FIG. 1 is a schematic diagram of one embodiment of an MTO product gas purification system provided by the present invention.
The reference numerals are explained below:
100MTO product gas purification system;
101 dust remover, 102 gas-gas heat exchanger, 103 first group of tubular heat exchanger, 104 second group of tubular heat exchanger, 105 water scrubber, 106 catalyst recovery storage tank;
200 reactors;
300 an olefin separation system.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the technical solution of the present invention is further described in detail below with reference to the accompanying drawings and the detailed description.
In the prior MTO product gas purification system 100, a cyclone dust collector 101 is mainly used for primary dust removal, then a spray tower is used for secondary dust removal and byproduct precipitation, and a water scrubber 105 is used for further dust removal and byproduct precipitation. The purification system 100 has the disadvantages of difficult waste heat recovery, easy blockage, high operation cost, low catalyst recovery rate and the like.
The inventors have intensively studied and analyzed the reasons why the above-mentioned drawbacks exist in the conventional MTO product gas purification system 100:
(1) MTO product gas can condense in spray column and scrubbing tower and precipitate oil matter, and oil matter that precipitates can combine with the catalyst dust and form fatlute and wax thing, consequently can mix fatlute and wax thing in the waste water of spray column and scrubbing tower discharge, leads to the unable reuse of throwing into use again of not handling of discharged waste water, consequently waste heat in the waste water can not obtain effective utilization, so can cause the waste heat of system to be unable by effective recycle.
(2) In order to achieve the purpose of further dedusting in the spray tower and the water washing tower, the liquid-gas ratio must be kept above a certain value, so that a large amount of spray water is needed, and the running cost of the system is high.
(3) The dust concentration at the outlet of the cyclone dust collector is as high as 100-150 mg/Nm3The MTO product gas still contains a large amount of catalyst dust when it reaches the spray tower and the water scrubber downstream of the dust separator, and therefore, a large amount of sludge and wax is generated in the spray tower and the water scrubber, which causes the system to be very easily clogged.
(4) The catalyst dust is not easily separated from the sludge and wax, so that the catalyst dust combined with the oil-based substances is not recycled, resulting in a low catalyst recovery rate.
In view of this, the present invention provides an MTO product gas purification system.
As shown in FIG. 1, the MTO product gas purification system 100 provided by the present invention is provided with a dust remover 101 and a water scrubber 105, and when in use, a product gas inlet of the dust remover 101 is connected with a reactor 200, and a product gas outlet of the water scrubber 105 is connected with an olefin separation system 300. The dust remover 101 is used for removing dust in the MTO product gas, and the water scrubber 105 is used for deeply scrubbing and separating out byproducts in the MTO product gas, so that the follow-up separation of the MTO product gas is facilitated.
As shown in FIG. 1, the MTO product gas purification system 100 is further provided with a heat recovery section connected between a dust remover 101 and a water scrubber 105.
The heat recovery part adopts a tubular heat exchanger which takes process water as a heat exchange medium, the process water circulates in a heat exchange tube of the tubular heat exchanger, and the MTO product gas circulates outside the heat exchange tube of the tubular heat exchanger.
When MTO product gas flows through the heat recovery part, the MTO product gas exchanges heat with process water in a heat exchange pipe of the heat recovery part, the process water recovers the waste heat of the MTO product gas, so the temperature is increased, and the process water does not directly contact the MTO product gas, so oil sludge and wax are not mixed in the process water, therefore, waste water discharged by the heat recovery part can be directly used for supplying heat for heat equipment without treatment, and therefore the waste heat of the system is effectively recycled.
Moreover, when the MTO product gas flows through the heat recovery section, the catalyst dust therein is condensed and grows along with the condensation of the water vapor, the heat exchange tubes of the heat recovery section can intercept the condensed and grown catalyst dust, so as to achieve the purpose of further dedusting, and part of byproducts in the MTO product gas can be removed in a coordinated manner while dedusting, so that the catalyst dust content and the byproduct content in the MTO product gas entering the water scrubber 105 are low, the amount of sludge and wax formed in the water scrubber 105 is reduced, and the risk of system blockage is low.
In addition, the heat recovery part achieves the purpose of dust removal by means of interception of the heat exchange tube, so that liquid-gas ratio does not need to be considered, the process water consumption can be controlled to be small, and the system operation cost can be controlled to be low.
Specifically, the heat recovery section may include a plurality of sets of tube heat exchangers. In the illustrated embodiment, two sets of tube heat exchangers are provided, namely a first set of tube heat exchangers 103 and a second set of tube heat exchangers 104.
The product gas inlet and outlet of each group of tube heat exchangers are connected in sequence, and the MTO product gas flows through each group of tube heat exchangers in sequence, flows through the upstream tube heat exchanger firstly and then flows through the downstream tube heat exchanger, so that the waste heat recovery rate can be improved. In the illustrated embodiment, the product gas outlet of the first tubular heat exchanger 103 is communicated with the product gas inlet of the second tubular heat exchanger 104, and the MTO product gas flows through the first tubular heat exchanger 103 and then through the second tubular heat exchanger 104.
The process water inlet and outlet of each group of tube heat exchangers can also be connected in sequence, the process water flows through each group of tube heat exchangers in sequence, and flows through the downstream tube heat exchanger firstly and then flows through the upstream tube heat exchanger, thus, the process water discharged from the upstream tube heat exchanger has higher temperature, and the requirement of heat-using equipment is easily met. In the illustrated scheme, the process water inlet of the first group of tube heat exchangers 103 is communicated with the process water outlet of the second group of tube heat exchangers 104, and the process water firstly flows through the second group of tube heat exchangers 104 and then flows through the first group of tube heat exchangers 103.
The process water fully absorbs the latent heat of the MTO product gas in the second group of tubular heat exchangers 104 and is heated to medium-temperature water, the medium-temperature water fully absorbs the sensible heat of the MTO product gas in the first group of tubular heat exchangers 103 and is heated to high-temperature water, and the MTO product gas is basically cooled to about dew point temperature (namely about 110 ℃) when flowing out of the first group of tubular heat exchangers 103.
In the second group of tubular heat exchangers 104, the water vapor content in the MTO product gas is high, the MTO product gas has a high latent heat value, condensation heat release is realized, and the heat exchange coefficient is high, so that the heat exchange tubes of the second group of tubular heat exchangers 104 can adopt common light tubes (i.e., the outer walls of the tubes are not provided with fins). The heat exchange coefficient in the first group of tubular heat exchangers 103 is low, and the heat exchange effect can be enhanced by arranging fins on the outer wall of the heat exchange tubes. That is, the first group of tube heat exchangers 103 may employ finned heat exchange tubes, and the second group of tube heat exchangers 104 may employ conventional non-finned heat exchange tubes. The heat exchange tube is made of high temperature resistant material with high heat conductivity coefficient, such as carbon steel, stainless steel, fluoroplastic, etc.
Specifically, the dust collector 101 of the MTO product gas purification system 100 may be a bag house dust collector. The filter bag of the bag-type dust collector can adopt a high-temperature-resistant filter bag, such as a metal filter bag (for example, a filter bag made of iron-chromium-aluminum alloy and the like) or a ceramic filter bag. The dust removal efficiency of the bag type dust collector is higher than that of a cyclone dust collector. The concentration of the catalyst dust at the outlet of the bag house is about 5mg to 10mg/Nm3。
With the bag house, the catalyst dust concentration is already low when the MTO product gas reaches the heat exchanging part and the water scrubber 105 downstream of the dust collector 101 due to high dust collection efficiency, and therefore, the amount of sludge and wax formed in the heat exchanging part and the water scrubber 105 is small, thereby further reducing the risk of system clogging.
Moreover, most of the catalyst dust is intercepted by the dust remover 101, and the catalyst can be directly recycled after being discharged from the dust discharge port at the bottom of the dust remover 101, so that the recycling rate of the catalyst is high. Specifically, the catalyst recovery storage tank 106 may be hermetically connected to the ash discharge port at the bottom of the dust collector 101, and the catalyst may be directly discharged into the catalyst recovery storage tank 106.
Specifically, as shown in fig. 1, the MTO product gas purification system 100 further comprises a gas-gas heat exchanger 102, and the gas-gas heat exchanger 102 is connected between the dust separator 101 and the heat recovery unit. The gas-gas heat exchanger 102 uses methanol gas as a heat exchange medium. The gas-gas heat exchanger 102 may specifically be a shell and tube heat exchanger. The gas-gas heat exchanger 102 preheats the methanol gas by using the waste heat of the MTO product gas, and the preheated methanol gas is introduced into the reactor 200, so that the reaction efficiency can be improved. Specifically, the methanol gas outlet of the gas-gas heat exchanger 102 may be directly communicated with the methanol gas inlet of the reactor 200.
The MTO product gas purification system provided by the present invention is described in detail above. The principles and embodiments of the present invention are explained herein using specific examples, which are presented only to assist in understanding the method and its core concepts. It should be noted that, for those skilled in the art, it is possible to make various improvements and modifications to the present invention without departing from the principle of the present invention, and those improvements and modifications also fall within the scope of the claims of the present invention.
Claims (8)
- The MTO product gas purification system is characterized in that the MTO product gas purification system (100) comprises a dust remover (101), a heat recovery part and a water washing tower (105) which are sequentially connected, wherein the heat recovery part adopts a tubular heat exchanger which takes process water as a heat exchange medium, the process water circulates in a heat exchange tube of the tubular heat exchanger, and the MTO product gas circulates outside the heat exchange tube of the tubular heat exchanger.
- 2. The MTO product gas purification system (100) according to claim 1, wherein the heat recovery section comprises a plurality of sets of tubular heat exchangers, wherein the product gas inlet and outlet of each set of tubular heat exchangers are connected in series, and wherein the MTO product gas flows through each set of tubular heat exchangers in series.
- 3. The MTO product gas purification system (100) according to claim 2, wherein the process water inlet and outlet of each group of the tubular heat exchangers are connected in series, and the process water flows through each group of the tubular heat exchangers in series, first through the downstream tubular heat exchanger and then through the upstream tubular heat exchanger.
- 4. The MTO product gas purification system (100) according to claim 2, wherein fins are provided on an outer wall of the heat exchange tubes of the upstream tube heat exchanger.
- 5. The MTO product gas purification system (100) according to any one of claims 1 to 4, wherein the precipitator (101) is a bag precipitator.
- 6. The MTO product gas purification system (100) according to claim 5, wherein the filter bag of the bag house (101) is a metal filter bag or a ceramic filter bag.
- 7. The MTO product gas purification system (100) according to claim 5, wherein the MTO product gas purification system (100) further comprises a gas-gas heat exchanger (102) using methanol gas as a heat exchange medium, the gas-gas heat exchanger (102) being connected between the dust separator (101) and the heat recovery section.
- 8. The MTO product gas purification system (100) according to claim 7, wherein the MTO product gas purification system (100) further comprises a catalyst recovery storage tank (106), wherein an ash discharge is provided at a bottom of the dust separator (101), and wherein the catalyst recovery storage tank (106) is disposed at the ash discharge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011553031.1A CN112516730A (en) | 2020-12-24 | 2020-12-24 | MTO product gas clean system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011553031.1A CN112516730A (en) | 2020-12-24 | 2020-12-24 | MTO product gas clean system |
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| CN112516730A true CN112516730A (en) | 2021-03-19 |
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| CN202011553031.1A Pending CN112516730A (en) | 2020-12-24 | 2020-12-24 | MTO product gas clean system |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103214333A (en) * | 2013-05-10 | 2013-07-24 | 神华集团有限责任公司 | System and process for gas-solid separation and heat exchange of alkene product prepared from organic oxygen-containing compound |
| US20150291484A1 (en) * | 2012-10-31 | 2015-10-15 | Shell Oil Company | Processes for the preparation of an olefinic product |
| US20160341499A1 (en) * | 2015-05-19 | 2016-11-24 | Uop Llc | Process for online cleaning of mto reactor effluent cooler |
| CN107324966A (en) * | 2017-07-17 | 2017-11-07 | 浙江大学 | The preprocess method and its device of product gas in oxygenatedchemicals olefin process |
| CN214209935U (en) * | 2020-12-24 | 2021-09-17 | 福建龙净环保股份有限公司 | MTO product gas clean system |
-
2020
- 2020-12-24 CN CN202011553031.1A patent/CN112516730A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150291484A1 (en) * | 2012-10-31 | 2015-10-15 | Shell Oil Company | Processes for the preparation of an olefinic product |
| CN103214333A (en) * | 2013-05-10 | 2013-07-24 | 神华集团有限责任公司 | System and process for gas-solid separation and heat exchange of alkene product prepared from organic oxygen-containing compound |
| US20160341499A1 (en) * | 2015-05-19 | 2016-11-24 | Uop Llc | Process for online cleaning of mto reactor effluent cooler |
| CN107324966A (en) * | 2017-07-17 | 2017-11-07 | 浙江大学 | The preprocess method and its device of product gas in oxygenatedchemicals olefin process |
| CN214209935U (en) * | 2020-12-24 | 2021-09-17 | 福建龙净环保股份有限公司 | MTO product gas clean system |
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