CN106831288A - The MTP methods of mixed alcohol side entry feed - Google Patents
The MTP methods of mixed alcohol side entry feed Download PDFInfo
- Publication number
- CN106831288A CN106831288A CN201710127573.4A CN201710127573A CN106831288A CN 106831288 A CN106831288 A CN 106831288A CN 201710127573 A CN201710127573 A CN 201710127573A CN 106831288 A CN106831288 A CN 106831288A
- Authority
- CN
- China
- Prior art keywords
- mtp
- dme
- reactors
- mixed alcohol
- mixed
- Prior art date
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- 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
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
Abstract
The invention belongs to Coal Chemical Industry and technical field of petrochemical industry, it is related to a kind of MTP methods of mixed alcohol side entry feed.Comprise the following steps：A. in DME reactors, with refined methanol as raw material, DME is generated in the presence of alumina base catalyst；B. DME reactor products DME points is three parts, and Part I enters MTP reactors, and reaction is generated based on propylene, the product of by-product ethene, gasoline and LPG；C. the Part II DME gases in DME reactor products enter MTP reactors and participate in reacting from side line；D. the Part III DME in DME reactor products isolates gas-liquid two-phase, and gas phase enters MTP reactors and participates in reaction, after undercooling, MTP reactors is entered from side line；E. mixed alcohol is caused into MTP reactors from side line and participates in reaction.The present invention is easily controlled course of reaction；Improve ethene, propene yield；Reduce cost of goods manufactured.
Description
Technical field
The invention belongs to Coal Chemical Industry and technical field of petrochemical industry, it is related to a kind of preparing propylene from methanol (MTP) process
Optimisation technique, specifically a kind of MTP methods of mixed alcohol side entry feed.
Background technology
The low-carbon alkenes such as ethene, propylene are important organic chemical industry's basic material, its cracking for being mainly derived from naphtha.
In recent years, domestic ethene and propylene demand sharp increase, but China's oil yield far can not meet the market demand, so
Situation under, the diversification of ethene and production of propylene raw material becomes the key subjects of relation national energy structural adjustment.
Under traditional handicraft, ethene and propylene are mainly derived from steam cracking device and oil plant catalytic cracking (FCC) device,
About 43% comes from steam cracking device at present, and about 57% comes from FCC apparatus, and low-carbon alkene is the main by-product of technical process
Thing, imbalance between supply and demand is very prominent, and is the new of raw materials for production in the urgent need to substituting oil with the increasingly depleted of petroleum resources
Type production technology.At present, in the efficient utilization of coal resource, methanol-to-olefins (MTO) and preparing propylene from methanol (MTP) are main two
Bar route.Uop Inc. fluid bed MTO techniques, Dalian materialization DMTO technologies, LURGI's fixed bed MTP techniques (with methyl alcohol
It is raw material production propylene) success of exploitation, imply that ethene and propylene can be prepared by reacting as principal product.In China,
Ripe, the methanol market production capacity surplus with the technology that coal prepares methyl alcohol as raw material, by MTO and MTP techniques, can be by surplus
Methanol conversion after base stock ethene, propylene, the product for obtaining more high values to be reacted by various.
The technology path of current main flow includes two kinds, i.e. fluidized-bed reaction technique and fixed bed reaction technique.Wherein fluidize
With the MTO of the DMTO techniques of the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences and Uop Inc. as representative, technique uses SAPO-34 molecular sieves to bed process
Catalyst, and catalyst needs cyclic regeneration because inactivation is very fast, raw material is the methyl alcohol of water content 5%, anti-using recirculating fluidized bed
Answer device to can be very good to solve the problems, such as the very exothermic during methanol-to-olefins, the substantially suitable ethene of yield and third can be produced
Alkene., with the MTP technologies of strange (Lurgi) company exploitation in German Shandong as representative, the ZSM-5 types catalyst for using is because of knot for fixed-bed process
Burnt rate is low and inactivation is relatively slow, and MTP techniques are based on insulation fix bed system, and raw material is refined methanol, methyl alcohol is fed first and is reacted in DME
In device react generation DME, product DME in the MTP reactors of six beds selectivity be converted into propylene, while generate second
The accessory substances such as alkene, gasoline and LPG.
Existing multinomial patent is related to the technology with methyl alcohol as raw material production low-carbon alkene particularly propylene at present both at home and abroad, main
Have EP0448000, WO2007/140844A1, DE10027159A1, CN101309886A, CN1431982A,
CN101811920B etc., belongs to the category of above-mentioned MTP technologies.The common feature of these patents is：The technique road for being used
Line is designed according to the strange MTP process routes in German Shandong, is reacted using two sections of fixed beds, with refined methanol as former
Material, converts methanol into DME first in one section of DME reactor under aluminium oxide catalyst effect, product DME and water,
Recycle hydrocarbons are blended, preheating, enter in heat-insulating fixed bed reactors from top MTP reactor heads and react, in ZSM-5 bases MTP
In the presence of catalyst, ultimately generate based on propylene, the accessory substance such as a small amount of ethene of by-product, a certain amount of gasoline and LPG.
Methanol-to-olefins (MTP) reaction is strong exothermal reaction, the extremely difficult control of reaction temperature, in order to maintain temperature curve in institute
Within the temperature range of needing, reaction is divided into DME and MTP two reactors to disperse reaction heat by technique, is entered in MTP reactor heads
Add vapor and recycle hydrocarbons in material, vapor can as the heat absorption material of exothermic reaction to control the temperature rise of beds,
The addition of vapor simultaneously can reduce the formation of carbon deposit；In order to improve propene yield and yield, C2 that refined unit is looped back,
C4, C5/C6 are also converted into alkene into the bed of reactor first together, while can act also as the heat absorption material control of exothermic reaction
The temperature of beds processed.In order to better control over reaction temperature, intermediate feed is added to enter between each bed of main reactor
Row cooling, enters next beds after the gas phase and liquid phase DME hybrid coolings of side entry feed.Most cold be by from
What the liquid gasification rich in water of the supercooling of the second to the 6th bed injection was provided.
Traditional MTP operational process of craft is complicated, and rate-determining steps are relatively complicated, while the technique is in industrialization running
In, Propylene Selectivity and yield are all relatively low, and unit consumption of product is high, production run high cost, so as to reduce the profitability of device；
There is certain defect in the control device for being used as each bed temperature of MTP reactors using DME lime sets in another technological process, due to
MTP reactions belong to strong exothermal reaction, it is necessary to lime set amount it is often very big, often occur to cause bed temperature runaway because lime set is not enough
Phenomenon, lime set pump is fragile also because of long-term heavy-duty service, therefore, how technological process to be optimized, reduce operation difficult
Degree, while the yield for improving the products such as ethene, propylene is great meaning.
The content of the invention
The purpose of the present invention is：For the deficiency of existing process technology, there is provided a kind of MTP methods of mixed alcohol side entry feed,
Enable the method to reduce reaction heat from thermodynamics source, so that rate；The process components such as nozzle, expansion joint can be reduced
Operation course of reaction be easier control；Cost of material can be reduced, the receipts load of the products such as ethene, propylene is improved, consumption is reduced
Material, reduces cost of goods manufactured, and the raw material that solution MTP commercial plants presently, there are is single to mix alcohol purified treatment with coal chemical technology
The problems such as method missing.
To achieve these goals, the inventive method is comprised the following steps：
A. with refined methanol as raw material, 250~280 DEG C are preheated to and are entered in DME reactors, in the work of alumina base catalyst
With lower generation dimethyl ether (DME) and water；
B.DME product DME points is three parts, and Part I DME is isolated with from follow-up MTP reactor outlets
Recycle hydrocarbons mixing, then mix with process steam, the heated stove heat of mixed material to 430-460 DEG C of entrance is divided equipped with ZSM-5
The MTP reactors of son sieve base catalyst, reaction is generated based on propylene, the product of by-product ethene, gasoline and LPG；
Part II DME gases enter MTP reactors and participate in reacting from side line in c.DME product；
Part III DME materials isolate gas-liquid two-phase in DME knockout drums in d.DME product, and wherein gas phase is rich
Containing DME, liquid phase is rich in process water；MTP reactors are directly entered after DME gas mixings in gas phase portion and step c and participate in anti-
Should；After liquid phase part supercooling, MTP reactors are entered from side line after being pressurizeed through DME lime sets pump, play reduction reactor batch temperature
Effect；
E. the mixed alcohol of C1~C10 is caused by MTP reactors from side line by pump and participates in reaction, using mixed alcohol catalyst work
With the strong endothermic reaction of lower generation producing olefin hydrocarbon with alcohols dehydration, the fuel factor of MTP reactions is neutralized, by MTP reactor batch temperature controls
System is within the scope of required temperature.
Preferably, the mixed alcohol of MTP reactor pump-arounds charging is originated from by-product in Fischer-Tropsch synthesis higher hydrocarbon technique
Mixed alcohol, or the mixed alcohol hydrocarbonaceous to be derived from rectifying side take-off in methanol synthesizing process, or the mixed alcohol in above two source are passed through
After crossing pretreatment, the mixed raw polyol obtained with water compounding, water content can be adjusted in 5-99%.(the typical case's composition for wherein mixing alcohol is shown in
Table 1)
Preferably, by methyl alcohol, the dimethyl ether in the mixed alcohol and original material of all side entry feeds in MTP reactors, roll over
It is counted as methyl alcohol and calculates weight (hourly) space velocity (WHSV), specific algorithm is that the DME of 1M is converted to the CH3OH of 2M；Mixed alcohol quality is rubbed divided by corresponding
That quality, obtains corresponding CH3OH molal quantitys；The weight (hourly) space velocity (WHSV) of raw material is 0.5-1.5kg methyl alcohol/(kg in MTP reactors
cat.h)。
Preferably, the mixed alcohol of MTP reactor pump-arounds charging, carries out pretreatment purification before charging, and preprocessing means include
But it is not limited to ion exchange, alkali process, absorption and other physical chemistry processing methods etc., pre-treatment step is：Desulfurization successively
Deodorant, sand filtration, highly basic are heated to 55~60 DEG C of hydrolysis and use NaBH except ester, deacidification, at 50~80 DEG C4Reduction treatment.
Preferably, MTP reactors used catalyst be ZSM-5 types or modified type ZSM 5 molecular sieve base catalyst, its into
Part includes molecular screen primary powder, binding agent, auxiliary agent, extruded moulding after each composition mixing.
It is an advantage of the invention that：
In conventional process for preparing propylene from methanol route, C is will be enriched in1~C10Mixed alcohol make jointly with methyl alcohol after pretreatment
It is raw material, is introduced through MTP technique side line liquid phase cold burdens entrance in the presence of ZSM-5 molecular sieve catalyst, dehydration occurs
Generate corresponding alkene, the product distribution of modulation methyl alcohol conversion process.The inventive method can be by technological design and theoretical meter
Calculate, on the premise of primary product distribution is not changed, introduce a certain amount of mixed alcohol from side line former as reaction to substitute part methyl alcohol
Material, into reactor mode by replace original side line rich in process water DME lime set liquid phase feeding systems, into second to
6th bed, it is therefore intended that the dehydration of alcohols endothermic reaction occurs in beds by mixed alcohol, generation low-carbon alkene (removes methyl alcohol system
Alkene is that outside exothermic reaction, the reaction of other senior dehydration of alcohols alkene is the endothermic reaction), the heat release of MTP reactions is neutralized, together
The yield of light olefins such as Shi Tigao ethene, propylene.The replacement of mixed raw polyol, reduces the reaction of methanol conversion mistake to a certain extent
Fuel factor in journey, while reducing the consumption of methanol feedstock, reduces operation difficulty and cost of material, improves the steady of operation
The actual recovery of qualitative and low-carbon alkene.Further, since mixed alcohol can derive from F- T synthesis, the accessory substance of methanol synthesizing process,
Both the load of environmentally friendly aftertreatment technology had been reduced, also for MTP techniques provide cheap raw material, coal had been utilized as mixed alcohol
Chemical industry cause provides good recycling approach, the profitability of lifting device.
Brief description of the drawings
Fig. 1 is a kind of process principle figure of existing MTP methods.
Fig. 2 is the process principle figure of the inventive method embodiment 1,2.
Specific embodiment
The method to comparative example and the embodiment of the present invention is described further below in conjunction with the accompanying drawings.
Comparative example：
As shown in figure 1, its technique is with refined methanol as raw material, and on middle pattern examination fixed-bed reactor, DME pre-reactions
260 DEG C of device R-111 inlet temperatures, 370 DEG C of outlet temperature, methyl alcohol weight (hourly) space velocity (WHSV) is 2.0h in R-111 reactors-1, MTP reactors
Methyl alcohol (and dimethyl ether) weight (hourly) space velocity (WHSV) is 1.5h in R-151-1, the reaction temperature of R-151 reactors is 475 DEG C, reactor outlet
Pressure 10kPa.Partial pressure of the methyl alcohol (dimethyl ether is converted to methyl alcohol) in main reactor is 23kPa, and diluent gas is vapor.Urge
Agent is ZSM-5 based molecular sieve catalyst, and Si/Al=100, reactor outlet product is shown in Table 1 through on-line chromatograph analysis result.
Embodiment one：
As shown in Fig. 2 comprising the following steps：
A. in DME reactors (single stage adiabatic fixed bed reactors R-111), with refined methanol as raw material, from anti-after preheating
Device R-111 its top feeds are answered, DME (dimethyl ether) is generated in the presence of alumina base catalyst；
B. DME reactor products DME points is three parts, and Part I DME divides with from follow-up MTP reactor outlets
The recycle hydrocarbons mixing for separating out, then mix with process steam, the heated stove heat of mixed material to after 450 DEG C from top into being equipped with
The bed of MTP reactors (R-151) first of ZSM-5 molecular sieve base catalyst, product is once by the second to the 6th catalysis
Agent bed, reaction is generated based on propylene, the product of by-product ethene, gasoline and LPG；
C. Part II DME gases are joined from side line into the bed of MTP reactors second to the 6th in DME reactor products
With reaction；
D. Part III DME materials isolate gas-liquid two-phase in DME knockout drums D-112 in DME reactor products, its
Middle gas phase is rich in DME, and liquid phase is rich in process water；MTP reactors are directly entered after gas phase portion and DME gas mixings in step c
Second to the 6th bed participates in reaction, and liquid phase part therein is crossed after being cooled to 60 DEG C, enters from side line after being pressurizeed through DME lime sets pump
The bed of MTP reactors second to the 6th, plays a part of to reduce reactor batch temperature；
E. by pump in the future from by-product in Fischer-Tropsch synthesis higher hydrocarbon techniqueC1~C10 Mix alcohol from head tank C-
111 cause the beds porch of MTP reactors R-151 second to the 6th through side line participates in reaction, using mixed alcohol in catalysis
There is the strong endothermic reaction of producing olefin hydrocarbon with alcohols dehydration in the presence of agent, the fuel factor of MTP reactions is neutralized, by MTP reactor beds
Temperature control is within the scope of required temperature.
In above-mentioned steps, 260 DEG C of DME pre-reactor R-111 inlet temperatures, 370 DEG C of outlet temperature, in R-111 reactors
Methyl alcohol weight (hourly) space velocity (WHSV) is 2.0h-1, methyl alcohol (and dimethyl ether) weight (hourly) space velocity (WHSV) is 1.0h in MTP reactors R-151-1, mix alcohol side line and enter
Material weight (hourly) space velocity (WHSV) is 0.5h-1, total carbon treatment air speed is equal to methyl alcohol weight (hourly) space velocity (WHSV) for 1.5h caused by both-1.R-151 reacts
The reaction temperature of device is 475 DEG C, reactor outlet pressure 10kPa.Methyl alcohol (dimethyl ether is converted to methyl alcohol) is in main reactor
Partial pressure is 23kPa, and diluent gas is vapor.Catalyst is ZSM-5 based molecular sieve catalyst, and Si/Al=100, reactor goes out
Mouth product is shown in Table 1 through on-line chromatograph analysis result.
Embodiment two：
The processing step and parameter of embodiment two are essentially identical with embodiment, the step of differ only in embodiment two in e,
Pretreatment purification is carried out to it before mixed alcohol is caused into MTP reactors, the material that can make catalyst poisoning is sloughed, in order to avoid cause catalysis
The agent lost of life, low-carbon alkene actual recovery are low；Pre-treatment step is：Desulfurization deodorant (gas liquid ratio 0.1), sand filtration, highly basic successively
60 DEG C of hydrolysis are heated to except ester, deacidification, NaBH is used at 70 DEG C4Reduction treatment.Reactor outlet product is analyzed through on-line chromatograph
The results are shown in Table 2.
Above-mentioned implementation comparative example is used for illustrative purposes only, rather than is limitation of the present invention, relevant technical field
Technical staff, on the premise of the spirit and scope of the invention is not departed from, can also make a variety of changes and deform, therefore used
Equivalent technical scheme should also belong to scope of the invention, and protection scope of the present invention should have various claims to limit.
Table 1 mixes alcohol typical case's constituent
(water content is adjustable in 5-99%)
The embodiment of table 2 is constituted with the product of comparative example
Claims (6)
1. a kind of MTP methods of mixed alcohol side entry feed, it is characterized in that：Comprise the following steps,
A. with refined methanol as raw material, 250~280 DEG C are preheated to and are entered in DME reactors, in the presence of alumina base catalyst
Generation DME；
B.DME reactor products DME point is three parts, Part I DME with isolated from follow-up MTP reactor outlets
Recycle hydrocarbons mix, then mix with process steam, and the heated stove heat of mixed material to 430-460 DEG C of entrance is equipped with ZSM-5 molecules
The MTP reactors of base catalyst are sieved, reaction is generated based on propylene, the product of by-product ethene, gasoline and LPG；
Part II DME gases enter MTP reactors and participate in reacting from side line in c.DME reactor products；
Part III DME materials isolate gas-liquid two-phase in DME knockout drums in d.DME reactor products, and wherein gas phase is rich in
DME, liquid phase is rich in process water；The participation reaction of MTP reactors, liquid are directly entered after gas phase portion and DME gas mixings in step c
After mutually part is crossed and is cooled to 60 DEG C, MTP reactors are entered from side line after being pressurizeed through DME lime sets pump, play reduction reactor bed temperature
The effect of degree；
E. the mixed alcohol of C1~C10 is caused by MTP reactors from side line by pump and participates in reaction, using mixed alcohol in the presence of catalyst
There is the strong endothermic reaction of producing olefin hydrocarbon with alcohols dehydration, neutralize the fuel factor of MTP reactions, the control of MTP reactor batch temperatures is existed
Within the scope of required temperature.
2. MTP methods of mixed alcohol side entry feed according to claim 1, it is characterized in that：It is mixed that MTP reactor pump-arounds feed
Alcohol is originated from the mixed alcohol of by-product in Fischer-Tropsch synthesis higher hydrocarbon technique, or to be derived from rectifying side line in methanol synthesizing process
The hydrocarbonaceous mixed alcohol of extraction, or the mixed alcohol that above two is originated is by after pretreatment, the mixed raw polyol obtained with water compounding is aqueous
Amount is in 5-99% adjustment.
3. MTP methods of mixed alcohol side entry feed according to claim 1, it is characterized in that：By all side lines in MTP reactors
Methyl alcohol, dimethyl ether in the mixed alcohol and original material of charging, are converted to methyl alcohol and calculate weight (hourly) space velocity (WHSV), and specific algorithm is 1M
DME is converted to the CH3OH of 2M；By mixed alcohol quality divided by corresponding molal weight, corresponding CH3OH molal quantitys are obtained；MTP is anti-
The weight (hourly) space velocity (WHSV) for answering raw material in device is 0.5-1.5kg methyl alcohol/(kg cat.h).
4. MTP methods of mixed alcohol side entry feed according to claim 1, it is characterized in that：It is mixed that MTP reactor pump-arounds feed
Alcohol, carries out pretreatment purification before charging, preprocess method include ion exchange, alkali process, one or more of adsorption method.
5. MTP methods of mixed alcohol side entry feed according to claim 4, it is characterized in that：Pre-treatment step is：Desulfurization successively
Deodorant, sand filtration, highly basic are heated to 55~60 DEG C of hydrolysis and use NaBH except ester, deacidification, at 50~80 DEG C4Reduction treatment.
6. MTP methods of mixed alcohol side entry feed according to claim 1, it is characterized in that：MTP reactor used catalysts are
ZSM-5 types or modified type ZSM 5 molecular sieve base catalyst, its composition include molecular screen primary powder, binding agent, auxiliary agent, each composition
Extruded moulding after mixing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710127573.4A CN106831288B (en) | 2017-03-06 | 2017-03-06 | The MTP method of mixed alcohol side entry feed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710127573.4A CN106831288B (en) | 2017-03-06 | 2017-03-06 | The MTP method of mixed alcohol side entry feed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106831288A true CN106831288A (en) | 2017-06-13 |
| CN106831288B CN106831288B (en) | 2019-07-26 |
Family
ID=59137999
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710127573.4A Active CN106831288B (en) | 2017-03-06 | 2017-03-06 | The MTP method of mixed alcohol side entry feed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106831288B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110054539A (en) * | 2019-05-10 | 2019-07-26 | 国家能源投资集团有限责任公司 | A kind of preparing propylene from methanol device and 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 |
| CN114409497A (en) * | 2022-01-24 | 2022-04-29 | 山西大学 | Method for simulating/predicting catalytic reaction mechanism and intermediate activity and application |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101417914A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Method for preparing propylene from methanol using hydrocarbons as part material |
| CN101723779A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing dimethyl ether and olefin by dehydration on mixed alcohol |
-
2017
- 2017-03-06 CN CN201710127573.4A patent/CN106831288B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101417914A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Method for preparing propylene from methanol using hydrocarbons as part material |
| CN101723779A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Method for producing dimethyl ether and olefin by dehydration on mixed alcohol |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110054539A (en) * | 2019-05-10 | 2019-07-26 | 国家能源投资集团有限责任公司 | A kind of preparing propylene from methanol device and method |
| CN110054539B (en) * | 2019-05-10 | 2022-05-20 | 国家能源投资集团有限责任公司 | Device and method for preparing propylene from methanol |
| 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 |
| CN114409497A (en) * | 2022-01-24 | 2022-04-29 | 山西大学 | Method for simulating/predicting catalytic reaction mechanism and intermediate activity and application |
| CN114409497B (en) * | 2022-01-24 | 2023-07-18 | 山西大学 | Method for simulating/predicting catalytic reaction mechanism and intermediate activity |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106831288B (en) | 2019-07-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101992046B (en) | Parallel combined riser circular reaction-regeneration device | |
| CN105949021B (en) | A kind of system and method that propylene is prepared by Catalytic dehydration of methanol | |
| CN103121894A (en) | Combined method for producing low-carbon olefin | |
| CN105349172A (en) | Naphtha raw material catalysis cracking method | |
| CN103571530B (en) | Wax catalysis cracking is for the method for low-carbon alkene | |
| CN106831288B (en) | The MTP method of mixed alcohol side entry feed | |
| CN101293801B (en) | Method for preparing dimethyl ether, low carbon olefin hydrocarbon with combination of methanol dehydration catalytic pyrolysis | |
| CN101875851B (en) | Non-hydrogenation upgrading method for liquefied gas fractions | |
| CN101928598B (en) | Method and system for producing gasoline and propylene by integrating heavy oil catalytic cracking with oxygen-containing compound conversion | |
| CN103333040B (en) | Low energy consumption propylene production technology | |
| CN102351629B (en) | Method for producing propylene and high-octane gasoline from methanol | |
| CN103382145A (en) | Preparation process for propylene from methanol or dimethyl ether | |
| CN108485704B (en) | Process for preparing chemical raw materials in maximized mode by combining millisecond-graded gas-phase catalytic cracking and hydrogenation of crude oil | |
| CN101585747B (en) | Method for transforming oxygenates into propylene | |
| CN101880212B (en) | A kind of technique being prepared propylene by oxygenatedchemicals | |
| CN104355960B (en) | A kind of method by preparing propylene from methanol and BTX | |
| CN103121891B (en) | Method for producing low-carbon olefin | |
| CN104557362B (en) | Methanol and/or dimethyl ether conversion aromatic hydrocarbons coproduction ethylene, the system and method for propylene | |
| CN104525057B (en) | A kind of synthesis gas two-step method prepares the device and technique of gasoline | |
| CN104557368A (en) | System for preparing ethylene, ethylene and arene from kinds of raw materials by coupling and transformation and method for system | |
| CN114989865B (en) | Method for producing low-carbon olefin by coupling Fischer-Tropsch synthetic oil with low-carbon alcohol ether oxygen-containing compound | |
| CN207347425U (en) | Prepare the device of ethene | |
| CN107540502A (en) | The method that oxygen-containing compound material is catalytically conveted to ethene, propylene and aromatic hydrocarbons | |
| CN103694077B (en) | A kind of propylene that produces can the reaction process of coproduction high octane gasoline component | |
| CN101659600B (en) | Method and device of a combined process for producing dimethyl ether by methanol and catalytic cracking |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: No. 90, Chengcheng Road, new area of Zhenjiang new area, Zhenjiang, Jiangsu Applicant after: Jiangsu national porcelain tin no new material Polytron Technologies Inc Address before: 212132 Chengcheng Road, new town, Zhenjiang City, Jiangsu Province, No. 90 Applicant before: JIANGSU TIANNUO NEW MATERIAL TECHNOLOGY CO., LTD. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 212000 No. 90 Chenglu Road, new town, Zhenjiang, Jiangsu Patentee after: Jiangsu guoci New Material Technology Co., Ltd Address before: 212000, 90, Cheng Cheng Road, Zhenjiang New District, Jiangsu, Zhenjiang Patentee before: JIANGSU GUOCI TIANNUO NEW MATERIAL TECHNOLOGY Co.,Ltd. |
|
| CP03 | Change of name, title or address |