CN105732251B - The method of methanol oxidation conversion production aromatic hydrocarbons - Google Patents
The method of methanol oxidation conversion production aromatic hydrocarbons Download PDFInfo
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- CN105732251B CN105732251B CN201410768814.XA CN201410768814A CN105732251B CN 105732251 B CN105732251 B CN 105732251B CN 201410768814 A CN201410768814 A CN 201410768814A CN 105732251 B CN105732251 B CN 105732251B
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- aromatic hydrocarbons
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The present invention relates to a kind of methods that methanol oxidation converts production aromatic hydrocarbons, relate generally to a kind of method using fixed bed two-stage method technique productions aromatic hydrocarbons, include the following steps：One section of reaction is using methanol as raw material, using ZSM 5 and 11 eutectic molecular sieves of ZSM as catalyst, one section of reaction product based on ethylene, propylene, C4 alkene is made, condensation separation is carried out to one section of reaction product, gas-phase product containing low-carbon alkene is sent into second stage reactor, in the presence of 5 molecular sieve catalyst of modified ZSM-5, aromatic hydrocarbons is made.The first segment reactor methanol of the present invention is changed into using low-carbon alkene as primary product, and low-carbon alkene, into aromatic hydrocarbons, uses this technique that can effectively improve selectivity and yield of the methanol carbon conversion for aromatic hydrocarbons in second segment reactor aromatization.
Description
Technical field
The present invention relates to a kind of methods that aromatic hydrocarbons is produced using methanol as raw material.
Background technology
Methanol is one of primary product of coal chemical industry, and with the development of coal chemical industry, methanol output in the market will be rapid
Increase, active development Downstream Products of Methanol has great importance to the development of methanol industry.Preparing olefin by conversion of methanol (MTO) is
Years of researches are passed through in one direction of methanol conversion, at present, domestic bigization, develop the MTO with independent intellectual property right
Technology, which comes into Industrial demonstration experimental stage.Aromatic hydrocarbons is that modern chemical industry demand is only second to ethylene, propylene
Basic chemical industry raw material.Methanol aromatic hydrocarbons (MTA) technology is to may advantageously facilitate China to substitute Petroleum Production petrochemical industry by raw material of coal
The new technology of the new industry development of product.
The industrialization technology of methanol aromatic hydrocarbons still belongs to blank.Aromatization of methanol is to select the effect of type molecular sieve catalyst
Under, alkene is generated through methanol dehydration, alkene is using processes such as polymerization, alkylation, cracking, isomerization, cyclisation, hydrogen migrations, most
The process of aromatic hydrocarbons is converted into eventually.Final products are related with the selection of selecting property catalyst, and product is based on paraxylene.This is one
The process of deep conversion requires aromatic device high；Technically catalyst inactivation degree is difficult to grasp simultaneously.
The research of domestic catalyst and technology in relation to methanol conversion for preparing arene is it has been reported that Chinese Academy of Sciences Shanxi
Coalification patent CN200610012703.1 disclose the technique and method for preparing catalyst of a kind of methanol conversion for preparing arene, with
ZSM-5 molecular sieve is catalyst, loads La2O3、GaO2Etc. metal oxide modifieds, using the conversion process of two sections of fixed beds,
Product of one section of conversion based on aromatic hydrocarbons, after condensation, a small amount of lower carbon number hydrocarbons enters second stage reactor, and the reaction was continued.On Sinopec
The patent CN201010261717.3 of extra large Petroleum Chemical Engineering Institute discloses a kind of method of methanol conversion for preparing arene, the patent
Feature uses a segment process by methanol conversion for preparing arene, using ZSM-5 and ZSM-11 or β H molecular sieve mixtures as catalyst, load
La2O3、P2O5Oxide modifyings are waited, C1-C4 product assays are high in reaction process, and the yield of aromatic hydrocarbons is relatively low.
By the present invention and related patents comparative analysis, the two is using catalyst and technique difference.The present invention provides a kind of first
Alcohol converts the technique of highly selective aromatic hydrocarbons processed, and aromatic hydrocarbons is produced using fixed bed two-stage method, and one section is reacted using methanol as raw material, with
The molecular sieve of ZSM-5 and ZSM-11 eutectics be catalyst, loading ZnO, La2O3、CeO2Etc. metal oxide modifieds, using fixation
Bed two-stage method production aromatic hydrocarbons, changes into first segment reactor methanol using low-carbon alkene as primary product, low-carbon alkene is second
Section reactor aromatization is into aromatic hydrocarbons.
The research for showing domestic catalyst and technology in relation to methanol conversion for preparing arene through document comparative analysis has
Report, but had not been reported with the present invention using the methanol aromatics process technology of same catalyst.
The content of the invention
The present invention provides the new process that highly selective aromatic hydrocarbons processed is converted using coal-based methanol as raw material, and the purpose of the technique is to carry
For the route of Non oil-based route production basic organic chemical industry raw material, can reduce by naphtha reforming production aromatic hydrocarbons according to
Rely degree, reduce the external interdependency of China's oil, improve the energy, the strategic security of resource.This technique behaviour do mild condition,
The advantage that production cost is low, the market competitiveness is strong.
To achieve the above object, the present invention provides a kind of method of methanol oxidation conversion production aromatic hydrocarbons, includes the following steps：
A, using fixed bed two-stage method technique productions aromatic hydrocarbons, one section of reaction is total to using methanol as raw material with ZSM-5 and ZSM-11
Brilliant molecular sieve is catalyst, in operating pressure 0.1-1.0MPa, 380-480 DEG C of reaction temperature, air speed 0.5-6.0h-1Under, it is made
One section of reaction product based on ethylene, propylene, C4 alkene；
B, condensation separation is carried out to one section of reaction product, the gas-phase product containing low-carbon alkene is sent into second stage reactor
In；The operating pressure of second stage reactor is 0.1-1.0MPa, and reaction temperature is 360-480 DEG C, air speed 100-5000h-1, changing
Property ZSM-5 molecular sieve catalyst in the presence of, be made aromatic hydrocarbons.
The method of methanol oxidation conversion production aromatic hydrocarbons of the present invention, wherein in the eutectic molecular sieve of the step A
The preferred 0.06-18 of mass ratio of ZSM-5 and ZSM-11.
The method of methanol oxidation of the present invention conversion production alkene, wherein in the eutectic molecular sieve each ingredient matter
Amount is than preferred Al2O3:SiO2:TBA+:Seeds:H2O=60~700：1：0.08~0.18：0.5~5：10~20, wherein Seeds
Represent the crystal seed of ZSM-5 structures, TBA+Represent the lye of tetrabutylammonium bromide.
The method of methanol oxidation conversion production aromatic hydrocarbons of the present invention, wherein the modified ZSM-5 molecule in the step B
Sieve preferred silica alumina ratio 30-80：1 modified zsm-5 zeolite.
The method of methanol oxidation conversion production aromatic hydrocarbons of the present invention, wherein the modified ZSM-5 molecule in the step B
Sieve is to be handled, dried by soda acid, roasting back loading ZnO, La2O3、CeO2Wait metal oxides be modified, load capacity with point
Son sieve carrier meter, ZnO preferred 0.5-3 mass %, La2O3It is preferred that 0.1-1.5 mass %, CeO2It is preferred that 0.1-1.5 mass %.
The method of methanol oxidation conversion production aromatic hydrocarbons of the present invention, wherein the operating pressure in the step A is preferred
0.1-0.5MPa。
The method of methanol oxidation conversion production aromatic hydrocarbons of the present invention, wherein the operating pressure in the step B is preferred
0.1-0.5MPa。
Aromatic hydrocarbons is produced using fixed bed two-stage method, is changed into first segment reactor methanol using low-carbon alkene as main production
Object, low-carbon alkene is in second segment reactor aromatization into aromatic hydrocarbons.Use this technique that can effectively improve methanol carbon conversion as aromatic hydrocarbons
Selectivity and yield.Low-carbon alkene (C2, C3, C4 alkene) content 80% or so after one section of conversion provided by the present invention, 13-
15% C5+Liquid product, remaining is the alkane of C1-C4.One section of gas-phase product passes through two sections of aromatizations, aromatic hydrocarbons
Selectivity reaches more than the 80% of liquid product, and low-carbon alkene aromatization again is converted by methanol using two sections of conversion process, obtains
Target product aromatic hydrocarbons selectivity be more than 80%, C5+Liquid yield reaches more than 32%, and the selectivity and yield of aromatic hydrocarbons are significantly
Degree improves.
Specific embodiment
The present invention is described in further detail with reference to specific embodiment, but the present invention is from following embodiments
Limitation.It is any without departing from the present invention design and scope change, be within the scope of the present invention.
Embodiment 1：
Using methanol as raw material, first segment reactor loading catalyst 6g, catalyst uses the mass ratio of ZSM-5 and ZSM-11
1：1, control reaction pressure 0.1MPa, 475 DEG C of reaction temperature, air speed 2h-1, the modified ZSM-5 molecules of second segment reactor filling
Sieve catalyst, modified ZSM-5 molecular sieve carry out soda acid processing, drying, roasting back loading 2% using 50 molecular sieve of silica alumina ratio
ZnO, reaction pressure 0.1MPa, 400 DEG C of reaction temperature, methanol is by the production of the liquid and gas of first stage reactor and second stage reactor
Object composition such as table 1, table 2.
The liquid product composition of 1 two reactor of table
The gas-phase product composition of 2 one sections of table, second stage reactor
Embodiment 2：
Using methanol as raw material, first segment reactor loading catalyst 10g, catalyst uses the quality of ZSM-5 and ZSM-11
Than 2：1, control reaction pressure 0.5MPa, 450 DEG C of reaction temperature, air speed 2h-1, ZSM-5 points of the filling modification of second segment reactor
Sub- sieve catalyst, modified ZSM-5 molecular sieve carry out soda acid processing, drying, roasting back loading 2% using 50 molecular sieve of silica alumina ratio
ZnO, reaction pressure 0.5MPa, 400 DEG C of reaction temperature, methanol is by the production of the liquid and gas of first stage reactor and second stage reactor
Object composition such as table 3, table 4.
The liquid product composition of 3 two reactor of table
The gas-phase product composition of 4 one sections of table, second stage reactor
Embodiment 3：
Using methanol as raw material, using methanol as raw material, first segment reactor loading catalyst 10g, catalyst using ZSM-5 and
The mass ratio 2 of ZSM-11：1, control reaction pressure 0.1MPa, 475 DEG C of reaction temperature, air speed 2h-1, second segment reactor, which loads, to be changed
Property ZSM-5 molecular sieve catalyst, modified ZSM-5 molecular sieve carries out soda acid processing, drying, roasting using 50 molecular sieve of silica alumina ratio
Back loading 1%ZnO reaction pressure 0.1MPa are burnt, 360 DEG C of reaction temperature, methanol is by first stage reactor and the liquid of second stage reactor
Mutually and gas-phase product forms such as table 5, table 6.
The liquid product composition of 5 two reactor of table
The gas-phase product composition of 6 two reactor of table
| Methane | Ethylene | Ethane | Propylene | Propane | Iso-butane | N-butene | Normal butane | Anti- butylene | Maleic |
| 7.88 | 4.25 | 1.49 | 14.00 | 16.4 | 28.66 | 12.20 | 7.57 | 4.87 | 2.63 |
Embodiment 4：
Using methanol as raw material, first segment reactor loading catalyst 10g, catalyst uses the quality of ZSM-5 and ZSM-11
Than 1：1, control reaction pressure 0.5MPa, 470 DEG C of reaction temperature, air speed 1.5h-1, the modified ZSM-5 of second segment reactor filling
Molecular sieve catalyst, modified ZSM-5 molecular sieve carry out soda acid processing, drying, roasting back loading using 80 molecular sieve of silica alumina ratio
1%ZnO, reaction pressure 0.5MPa, 400 DEG C of reaction temperature, when catalyst operation 200 is small, methanol passes through first stage reactor and two
Liquid and gas the product composition such as table 7, table 8 of section reactor.
The liquid product composition of 7 two reactor of table
The gas-phase product composition of 8 two reactor of table
| Methane | Ethylene | Ethane | Propylene | Propane | Iso-butane | N-butene | Normal butane | Anti- butylene | Maleic |
| 7.88 | 4.25 | 1.49 | 14.00 | 16.4 | 28.66 | 12.20 | 7.57 | 4.87 | 2.63 |
Embodiment 5：
Using methanol as raw material, first segment reactor loading catalyst 10g, catalyst uses the quality of ZSM-5 and ZSM-11
Than 2：1, control reaction pressure 0.2MPa, 450 DEG C of reaction temperature, air speed 2h-1, ZSM-5 points of the filling modification of second segment reactor
Sub- sieve catalyst, modified ZSM-5 molecular sieve carry out soda acid processing, drying, roasting back loading 2% using 80 molecular sieve of silica alumina ratio
ZnO, reaction pressure 0.2MPa, 400 DEG C of reaction temperature, when catalyst operation 360 is small, methanol is anti-by first stage reactor and two sections
The liquid and gas product of device is answered to form such as table 9, table 10.
The liquid product composition of 9 two reactor of table
The gas-phase product composition of 10 two reactor of table
| Methane | Ethylene | Ethane | Propylene | Propane | Iso-butane | N-butene | Normal butane | Anti- butylene | Maleic |
| 7.88 | 4.25 | 1.49 | 14.00 | 16.4 | 28.66 | 12.20 | 7.57 | 4.87 | 2.63 |
Claims (8)
1. a kind of method of methanol oxidation conversion production aromatic hydrocarbons, includes the following steps：
A, using fixed bed two-stage method technique productions aromatic hydrocarbons, one section of reaction is using methanol as raw material, with ZSM-5 and ZSM-11 eutectics point
Son sieve is catalyst, in operating pressure 0.1-1.0MPa, 380-480 DEG C of reaction temperature, air speed 0.5-6.0h-1Under, it is made with second
Alkene, propylene, one section of reaction product based on C4 alkene；
B, condensation separation is carried out to one section of reaction product, the gas-phase product containing low-carbon alkene is sent into second stage reactor；Two
The operating pressure of section reactor is 0.1-1.0MPa, and reaction temperature is 360-480 DEG C, air speed 100-5000h-1, in modification
In the presence of ZSM-5 molecular sieve catalyst, aromatic hydrocarbons is made.
2. the method for methanol oxidation conversion production aromatic hydrocarbons according to claim 1, it is characterised in that the eutectic of the step A
The mass ratio of ZSM-5 and ZSM-11 is 0.06-18 in molecular sieve.
3. the method for methanol oxidation conversion production alkene according to claim 2, it is characterised in that the eutectic molecular sieve
In each ingredient mass ratio be Al2O3:SiO2:TBA+:Seeds:H2O=60~700：1：0.08~0.18：0.5~5：10~
20, wherein Seeds represents the crystal seed of ZSM-5 structures, TBA+Represent the lye of tetrabutylammonium bromide.
4. the method for the methanol oxidation conversion production aromatic hydrocarbons according to claims 1 to 3 any one, it is characterised in that described
Modified zsm-5 zeolite in step B is silica alumina ratio 30-80：1 modified zsm-5 zeolite.
5. the method for the methanol oxidation conversion production aromatic hydrocarbons according to claims 1 to 3 any one, it is characterised in that described
Modified zsm-5 zeolite in step B is to be handled, dried by soda acid, roasting back loading ZnO, La2O3、CeO2Metal oxide
It is modified, load capacity is in terms of molecular sieve carrier, ZnO：0.5-3 mass %, La2O3：0.1-1.5 mass %, CeO2：0.1-1.5
Quality %.
6. the method for methanol oxidation conversion production aromatic hydrocarbons according to claim 4, it is characterised in that changing in the step B
Property ZSM-5 molecular sieve is to be handled, dried by soda acid, roasting back loading ZnO, La2O3、CeO2Metal oxide is modified, and is born
Carrying capacity is in terms of molecular sieve carrier, ZnO：0.5-3 mass %, La2O3：0.1-1.5 mass %, CeO2：0.1-1.5 mass %.
7. the method for methanol oxidation conversion production aromatic hydrocarbons according to claim 1, it is characterised in that the behaviour in the step A
Make pressure as 0.1-0.5MPa.
8. the method for methanol oxidation conversion production aromatic hydrocarbons according to claim 1, it is characterised in that the behaviour in the step B
Make pressure as 0.1-0.5MPa.
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| CN106542947B (en) * | 2016-10-14 | 2019-04-02 | 中国科学院山西煤炭化学研究所 | A kind of technique of fixed bed methanol aromatic hydrocarbons |
| CN106866328B (en) * | 2017-01-16 | 2019-12-10 | 厦门大学 | Method for preparing aromatic hydrocarbon with high selectivity by using methanol |
| CN111097337B (en) * | 2018-10-25 | 2022-04-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
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| US3911041A (en) * | 1974-09-23 | 1975-10-07 | Mobil Oil Corp | Conversion of methanol and dimethyl ether |
| CN102078819A (en) * | 2009-11-26 | 2011-06-01 | 中国石油化工股份有限公司 | Light hydrocarbon aromatization catalyst and preparation method thereof |
| CN102153105A (en) * | 2010-12-31 | 2011-08-17 | 华东师范大学 | Method for preparing MFI/MEL (Mobil Fifth/Mobil Eleven) eutectic molecular sieve |
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| CN103694077A (en) * | 2013-12-03 | 2014-04-02 | 浙江大学 | Reaction technology for production of propylene and coproduction of high-octane value gasoline components |
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