CN104725229A - Method for preparing polyoxymethylene dimethyl ether carboxylate and methyl methoxy acetate - Google Patents
Method for preparing polyoxymethylene dimethyl ether carboxylate and methyl methoxy acetate Download PDFInfo
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- C07C67/36—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates
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- C07C29/10—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of ethers, including cyclic ethers, e.g. oxiranes
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- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
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Abstract
The invention provides a method for preparing polyoxymethylene dimethyl ether carboxylate and/or methyl methoxy acetate which serves as an intermediate for producing ethylene glycol. The method comprises the step of enabling a raw material, namely polyoxymethylene dimethyl ether or methylal, together with carbon monoxide and hydrogen gas to react in a dealuminzation modified acidic molecular sieve catalyst loaded reactor under appropriate reaction conditions without adding other solvents, so as to prepare corresponding products, wherein a reaction process is of gas-liquid-solid three-phase reaction. According to the method provided by the invention, the conversion ratio of the raw material polyoxymethylene dimethyl ether or methylal is high, the selectivity of each product is high, the service life of a catalyst is long, external solvents are not required to be used, reaction conditions are relatively mild, and continuous production can be carried out, so that the method has industrial application potential. Furthermore, the obtained products can be used for producing ethylene glycol through hydrolyzing after hydrogenating or hydrogenating after hydrolyzing.
Description
Technical field
The present invention relates to a kind of the polymethoxy dimethyl ether carbonyl compound of intermediate and the preparation method of methoxy menthyl acetate as producing ethylene glycol.
Background technology
Ethylene glycol is the important industrial chemicals of country and strategic materials, for the manufacture of polyester (can produce terylene, PET bottle, film further), explosive, oxalic dialdehyde, and can be used as frostproofer, softening agent, hydraulic fluid and solvent etc.The ethylene glycol import volume of China in 2009 is more than 5,800,000 tons, estimate that China's ethylene glycol demand in 2015 will reach 1,120 ten thousand tons, throughput about 5,000,000 tons, insufficiency of supply-demand still reaches 6,200,000 tons, therefore, the Application and Development of China's ethylene glycol production new technology has good market outlook.Mainly adopt the ethene of petroleum cracking to obtain oxyethane through oxidation in the world, ethylene oxide hydration obtains ethylene glycol.In view of the present situation such as Energy resources structure and crude oil price long term maintenance run at high level of China's " rich coal oil starvation weak breath ", coal-ethylene glycol New Coal Chemical technology can ensure the energy security of country, taking full advantage of again the coal resources of China, is the most real selection of future coal chemical industry.
At present, domestic contrast proven technique by Chinese Academy of Sciences's Fujian thing structure develop " CO synthesis of oxalic ester by gaseous catalysis and barkite shortening synthesizing glycol packaged process." in early December, 2009; whole world head cover industrialization demonstration unit-Tongliao, Inner Mongolia gold Coal Chemical Industry company " coal-ethylene glycol project " first phase of construction attracted much industry attention, annual output 200000 tons of coal-ethylene glycol projects get through technical process completely smoothly, produce qualified ethylene glycol product.But technique unit is more, industrial gasses purity requirement is high, need to use noble metal catalyst in oxidative coupling process, need the oxynitrides etc. utilizing latency environment to pollute can restrict the economy of this flow process, the feature of environmental protection, energy saving and engineering amplification further.
The molecular formula of polymethoxy dimethyl ether (or being polymethoxy methylal, English Polyoxymethylene dimethyl ethers by name) is CH
3o (CH
2o)
ncH
3, wherein n>=2, generally referred to as DMM
n(or PODE
n).In the process preparing polymethoxy dimethyl ether, its products distribution generated is unreasonable, methylal and DMM
2higher, and the DMM of diesel-dope can be used as
3 ~ 4selectivity is lower, therefore, usually needs repeatedly to be separated the by product in its preparation process to react again, and such energy consumption is comparatively large, and economy is poor.Therefore, if can using the DMM as by product
2directly be processed into the economy that the higher product of economic worth will improve this process.
In recent years, the Alexis T.Bell teach problem group of U.S. UC, Berkeley proposes to utilize methylal vapor phase carbonylation legal system for methoxy menthyl acetate, and then hydrogenation hydrolyzation obtains a variation route of ethylene glycol, and wherein a step of most critical is gas carbonylation reaction.But catalyst life is short, in unstripped gas low, the methylal transformation efficiency of methylal concentration and methoxy menthyl acetate selectivity all not ideal enough, also have quite long distance [Angew.Chem.Iht.Ed., 2009,48,4813 ~ 4815 from industrialization; J.Catal., 2010,270,185 ~ 195; J.Catal., 2010,274,150 ~ 162; WO2010/048300A1].
Summary of the invention
The object of the present invention is to provide a kind of by carbonylation preparation as the production polymethoxy dimethyl ether carbonyl compound of intermediate of ethylene glycol and the method for methoxy menthyl acetate.
For this reason, the invention provides a kind of by the method for carbonylation preparation as the polymethoxy dimethyl ether carbonyl compound of the intermediate of production ethylene glycol, it is characterized in that, by raw material polymethoxy dimethyl ether CH
3o (CH
2o)
ncH
3together with carbon monoxide and hydrogen by being loaded with the reactor of the acid molecular sieve catalyst of Dealumination, be 0.2 ~ 10.0h at temperature of reaction 60 ~ 140 DEG C, reaction pressure 2 ~ 10MPa, polymethoxy dimethyl ether mass space velocity
-1and product polymethoxy dimethyl ether carbonyl compound is prepared in reaction under not adding the condition of other solvents, wherein under the cited reaction conditions, at least one in described raw material and described product is liquid phase, the acid molecular sieve catalyst of described Dealumination is solid phase, carbon monoxide and hydrogen are that gas phase is to make reaction process for gas-liquid-solid phase reaction, and the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 20: 1, the mol ratio of hydrogen and described raw material is 1: 1 ~ 5: 1, wherein n>=2 and be integer.
Present invention also offers a kind of by carbonylation preparation as producing the intermediate methoxy menthyl acetate of ethylene glycol and the method for polymethoxy dimethyl ether carbonyl compound, it is characterized in that, by raw material methylal CH
3o-CH
2-OCH
3together with carbon monoxide and hydrogen by being loaded with the reactor of the acid molecular sieve catalyst of Dealumination, be 0.2 ~ 10.0h at temperature of reaction 60 ~ 140 DEG C, reaction pressure 2 ~ 10MPa, methylal mass space velocity
-1and product methoxy menthyl acetate and polymethoxy dimethyl ether carbonyl compound are prepared in reaction under not adding the condition of other solvents, wherein under the cited reaction conditions, at least one in described raw material and described product is liquid phase, the acid molecular sieve catalyst of described Dealumination is solid phase, carbon monoxide and hydrogen are that gas phase is to make reaction process for gas-liquid-solid phase reaction, and the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 20: 1, the mol ratio of hydrogen and described raw material is 1: 1 ~ 5: 1.
In a preferred embodiment, described product polymethoxy dimethyl ether carbonyl compound is at polymethoxy dimethyl ether CH
3o (CH
2o)
ncH
3-the O-CH of molecular chain
2what formed after-O-structural unit inserting one or more carbonyl-CO-has-O-(CO)-CH
2-O-or-O-CH
2the product of-(CO)-O-structural unit, wherein n>=2.
In a preferred embodiment, described polymethoxy dimethyl ether is two polymethoxy dimethyl ether CH
3o (CH
2o)
2cH
3.
In a preferred embodiment, described polymethoxy dimethyl ether carbonyl compound be following in one or more:
CH
3-O-(CO)-CH
2-O-CH
2-O-CH
3，
CH
3-O-CH
2-(CO)-O-CH
2-O-CH
3，
CH
3-O-(CO)-CH
2-O-(CO)-CH
2-O-CH
3, and
CH
3-O-(CO)-CH
2-O-CH
2-(CO)-O-CH
3。
In a preferred embodiment, the acid molecular sieve catalyst of described Dealumination is by making acid molecular sieve catalyst through comprising steam treatment and prepared by acid-treated Dealumination.
In a preferred embodiment, the temperature of described steam treatment is 400 ~ 700 DEG C, and the time is 1 ~ 8h; The acid used in described acid treatment is one or more acid be selected from hydrochloric acid, sulfuric acid, nitric acid, acetic acid, oxalic acid, citric acid of 0.03 ~ 3.0mol/L, and described acid-treated temperature is 15 ~ 95 DEG C, and the time is 1 ~ 24h.
In a preferred embodiment, the structure type of the acid molecular sieve catalyst of described Dealumination is MWW, FER, MFI, MOR, FAU or BEA.
In a preferred embodiment, the acid molecular sieve catalyst of described Dealumination is one or more in MCM-22 molecular sieve, ferrierite, ZSM-5 molecular sieve, mordenite, Y zeolite or Beta molecular sieve.
In a preferred embodiment, temperature of reaction is 60 ~ 120 DEG C, and reaction pressure is 4 ~ 10MPa, and the mass space velocity of described raw material is 0.5 ~ 3.0h
-1, the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 15: 1, and the mol ratio of hydrogen and described raw material is 1: 1 ~ 3: 1.
In a preferred embodiment, temperature of reaction is 60 ~ 90 DEG C, and reaction pressure is 5 ~ 10MPa, and the mass space velocity of described raw material is 0.5 ~ 1.5h
-1, the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 10: 1, and the mol ratio of hydrogen and described raw material is 1: 1 ~ 2: 1.
In a preferred embodiment, described reactor realizes the fixed-bed reactor of successive reaction, tank reactor, moving-burden bed reactor or fluidized-bed reactor.
The transformation efficiency of the inventive method Raw polymethoxy dimethyl ether or methylal is high, and the selectivity of each product is high, and catalyst life is long, does not need to use plus solvent, and reaction conditions is gentleer, can continuous seepage, possesses industrial applications potentiality.And the product obtained can produce ethylene glycol by hydrolysis after hydrogenation or hydrolysis back end hydrogenation.
Embodiment
The invention provides a kind of method preparing polymethoxy dimethyl ether carbonyl compound, it is characterized in that, will containing polymethoxy dimethyl ether CH
3o (CH
2o)
ncH
3, carbon monoxide and hydrogen raw material by being loaded with the reactor of the acid molecular sieve catalyst of Dealumination, be 0.2 ~ 10.0h at temperature of reaction 60 ~ 140 DEG C, reaction pressure 2 ~ 10MPa, polymethoxy dimethyl ether mass space velocity
-1and react under not adding the condition of other solvents, prepare polymethoxy dimethyl ether carbonyl compound; Under reaction conditions, raw material polymethoxy dimethyl ether and product polymethoxy dimethyl ether carbonyl compound at least one are liquid phase, and catalyzer is solid phase, and raw material carbon monoxide and hydrogen are gas phase, and reaction process is gas-liquid-solid phase reaction; In raw material, the mol ratio of carbon monoxide and polymethoxy dimethyl ether is 2: 1 ~ 20: 1, and the mol ratio of hydrogen and polymethoxy dimethyl ether is 1: 1 ~ 5: 1, wherein n>=2 and be integer.
Described polymethoxy dimethyl ether is one-component or mixture, and molecular formula is CH
3o (CH
2o)
ncH
3, wherein n>=2 and be integer, preferred n=2, i.e. CH
3o (CH
2o)
2cH
3.
In a preferred embodiment, reaction process is gas-liquid-solid phase reaction, and temperature of reaction is 60 ~ 120 DEG C, and reaction pressure is 4 ~ 10MPa, and polymethoxy dimethyl ether mass space velocity is 0.5 ~ 3.0h
-1, the mol ratio of carbon monoxide and polymethoxy dimethyl ether is the mol ratio of 2: 1 ~ 15: 1 preferred hydrogen and polymethoxy dimethyl ether is 1: 1 ~ 3: 1.
In a preferred embodiment, reaction process is gas-liquid-solid phase reaction, and temperature of reaction is 60 ~ 90 DEG C, and reaction pressure is 5 ~ 10MPa, and polymethoxy dimethyl ether mass space velocity is 0.5 ~ 1.5h
-1, the mol ratio of carbon monoxide and polymethoxy dimethyl ether is 2: 1 ~ 10: 1, and the mol ratio of preferred hydrogen and polymethoxy dimethyl ether is 1: 1 ~ 2: 1.
In some embodiments of the invention, the transformation efficiency of polymethoxy dimethyl ether and the selectivity of polymethoxy dimethyl ether carbonyl compound all calculate based on polymethoxy dimethyl ether carbon mole number:
Polymethoxy dimethyl ether transformation efficiency=[(in charging polymethoxy dimethyl ether carbon mole number)-(discharging polymethoxy dimethyl ether carbon mole number)] ÷ (in charging polymethoxy dimethyl ether carbon mole number) × (100%)
Polymethoxy dimethyl ether carbonyl compound selectivity=(the carbon mole number in charging after polymethoxy dimethyl ether carbonyl compound removing carbonyl) ÷ [(in charging polymethoxy dimethyl ether carbon mole number)-(in discharging polymethoxy dimethyl ether carbon mole number)] × (100%)
The present invention also provides the preparation method of a kind of methoxy menthyl acetate and polymethoxy dimethyl ether carbonyl compound, it is characterized in that, will containing methylal CH
3o-CH
2-OCH
3, carbon monoxide and hydrogen raw material by being loaded with the reactor of the acid molecular sieve catalyst of Dealumination, be 0.2 ~ 10.0h at temperature of reaction 60 ~ 140 DEG C, reaction pressure 2 ~ 10MPa methylal mass space velocity
-1and react under not adding the condition of other solvents, prepare methoxy menthyl acetate and polymethoxy dimethyl ether carbonyl compound; Under reaction conditions, raw material methylal and product methoxy menthyl acetate and polymethoxy dimethyl ether carbonyl compound at least one are liquid phase, and catalyzer is solid phase, and raw material carbon monoxide and hydrogen are gas phase, and reaction process is gas-liquid-solid phase reaction; In raw material, the mol ratio of carbon monoxide and methylal is 2: 1 ~ 20: 1, and the mol ratio of hydrogen and methylal is 1: 1 ~ 5: 1.
In a preferred embodiment, reaction process is gas-liquid-solid phase reaction, and temperature of reaction is 60 ~ 120 DEG C, and reaction pressure is 4 ~ 10MPa, and methylal mass space velocity is 0.5 ~ 3.0h
-1, the mol ratio of carbon monoxide and methylal is the mol ratio of 2: 1 ~ 15: 1 preferred hydrogen and methylal is 1: 1 ~ 3: 1.
In a preferred embodiment, reaction process is gas-liquid-solid phase reaction, and temperature of reaction is 60 ~ 90 DEG C, and reaction pressure is 5.0 ~ 10MPa, and methylal mass space velocity is 0.5 ~ 1.5h
-1, the mol ratio of carbon monoxide and methylal is 2: 1 ~ 10: 1, and the mol ratio of preferred hydrogen and methylal is 1: 1 ~ 2: 1.
In certain embodiments, the transformation efficiency of methylal and the selectivity of product all calculate based on methylal carbon mole number:
Methylal transformation efficiency=[(in charging methylal carbon mole number)-(in discharging methylal carbon mole number)] ÷ (in charging methylal carbon mole number) × (100%)
Methoxy menthyl acetate selectivity=(the carbon mole number in discharging after methoxy menthyl acetate removing carbonyl) ÷ [(in charging methylal carbon mole number)-(in discharging methylal carbon mole number)] × (100%)
Polymethoxy dimethyl ether carbonyl compound selectivity=(the carbon mole number in discharging after polymethoxy dimethyl ether carbonyl compound removing carbonyl) ÷ [(in charging methylal carbon mole number)-(in discharging methylal carbon mole number)] × (100%)
The method of described Dealumination comprises steam treatment and acid treatment.
Described steam treatment temperature is 400 ~ 700 DEG C, and preferably 550 ~ 650 DEG C, the steam treatment time is not limit, preferably 1 ~ 8h; The acid used in acid treatment is 0.03 ~ 3.0mol/L, one or more mixing acid preferably in the hydrochloric acid of 0.1 ~ 1.0mol/L, sulfuric acid, nitric acid, acetic acid, oxalic acid, citric acid, acid treatment temperature is 15 ~ 95 DEG C, preferably 60 ~ 80 DEG C, the acid treatment time is not limit, preferably 1 ~ 24h.
The structure type of described acid molecular sieve catalyst is MWW, FER, MFI, MOR, FAU or BEA.Preferably, described acid molecular sieve catalyst is any one or mixing several arbitrarily in MCM-22 molecular sieve, ferrierite, ZSM-5 molecular sieve, mordenite, Y zeolite or Beta molecular sieve, and sial atomic ratio is 3: 1 ~ 150: 1.
In an embodiment, sodium form molecular sieve converts the Standard operation procedure SOP of acidic molecular sieve to and is: by dried for 50g Na
+the 0.8M NH of 400ml put into by type molecular sieve
4nO
3in solution, at 80 DEG C, stir 12h, filter the distilled water wash of rear 800ml.This ion exchange process obtains NH in triplicate
4 +the molecular sieve of type.After abundant drying, be placed in retort furnace, be elevated to 550 DEG C with 2 DEG C/min and keep calcining 4h to obtain acidic molecular sieve.
Described polymethoxy dimethyl ether carbonyl compound is at polymethoxy dimethyl ether molecular chain-O-CH
2what formed after-O-structural unit inserting carbonyl-CO-has-O-(CO)-CH
2-O-or-O-CH
2the product of-(CO)-O-structural unit, polymethoxy dimethyl ether carbonyl compound contains one or more carbonyl.
The polymethoxy dimethyl ether carbonyl compound produced in embodiment can be one or more in following:
CH
3-O-(CO)-CH
2-O-CH
2-O-CH
3referred to as C5-1,
CH
3-O-CH
2-(CO)-O-CH
2-O-CH
3referred to as C5-2,
CH
3-O-(CO)-CH
2-O-(CO)-CH
2-O-CH
3referred to as C6-1,
CH
3-O-(CO)-CH
2-O-CH
2-(CO)-O-CH
3referred to as C6-2.
Product methoxy menthyl acetate of the present invention or polymethoxy dimethyl ether carbonyl compound can obtain ethylene glycol by hydrolysis after hydrogenation or hydrolysis back end hydrogenation, and in addition, described product can also be used as vapour, diesel-dope.Such as, with two polymethoxy dimethyl ether (DMM
2) CH
3o (CH
2o)
2cH
3the reaction process briefly expressing generating glycol for example is:
In a preferred embodiment, described reactor is the fixed-bed reactor of continuous flow, tank reactor, moving-burden bed reactor or fluidized-bed reactor.
Below by embodiment in detail the present invention is described in detail, but the present invention is not limited to these embodiments.
Embodiment 1
The MCM-22 molecular sieve being 40: 1 by 50g sodium form silica alumina ratio utilizes Standard operation procedure SOP to convert acidic molecular sieve to, is designated as catalyst A, in table 1.
Embodiment 2
The MCM-22 molecular sieve being 40: 1 by 100g sodium form silica alumina ratio passes into steam treatment 4h under 550 DEG C of conditions, then utilizes Standard operation procedure SOP to change into acidic molecular sieve, is designated as catalyst B, in table 1.
Embodiment 3
Be process 1h in the 0.1mol/L hydrochloric acid soln of MCM-22 molecular sieve 500ml under 60 DEG C of conditions of 40: 1 by 100g sodium form silica alumina ratio, then utilize Standard operation procedure SOP to change into acidic molecular sieve, be designated as catalyzer C, in table 1.
Embodiment 4
The ferrierite being 10: 1 by 50g sodium form silica alumina ratio utilizes Standard operation procedure SOP to convert acidic molecular sieve to, is designated as catalyzer D, in table 1.
Embodiment 5
The ferrierite being 10: 1 by 100g sodium form silica alumina ratio passes into steam treatment 1h under 700 DEG C of conditions, then utilizes Standard operation procedure SOP to change into acidic molecular sieve, is designated as catalyzer E, in table 1.
Embodiment 6
Be process 4h in the 0.4mol/L sulphuric acid soln of ferrierite 500ml under 80 DEG C of conditions of 10: 1 by 100g sodium form silica alumina ratio, then utilize Standard operation procedure SOP to change into acidic molecular sieve, be designated as catalyzer F, in table 1.
Embodiment 7
The ZSM-5 molecular sieve being 150: 1 by 50g sodium form silica alumina ratio utilizes Standard operation procedure SOP to convert acidic molecular sieve to, is designated as catalyzer G, in table 1.
Embodiment 8
The ZSM-5 molecular sieve being 150: 1 by 100g sodium form silica alumina ratio passes into steam treatment 8h under 400 DEG C of conditions, then utilizes Standard operation procedure SOP to change into acidic molecular sieve, is designated as catalyzer H, in table 1.
Embodiment 9
Be process 8h in the 1.0mol/L acetum of ZSM-5 molecular sieve 500ml under 75 DEG C of conditions of 150: 1 by 100g sodium form silica alumina ratio, then utilize Standard operation procedure SOP to change into acidic molecular sieve, be designated as catalyst I, in table 1.
Embodiment 10
The mordenite being 3: 1 by 50g sodium form silica alumina ratio utilizes Standard operation procedure SOP to convert acidic molecular sieve to, is designated as catalyzer J, in table 1.
Embodiment 11
The mordenite being 3: 1 by 100g sodium form silica alumina ratio passes into steam treatment 3h under 650 DEG C of conditions, then utilizes Standard operation procedure SOP to change into acidic molecular sieve, is designated as catalyzer K, in table 1.
Embodiment 12
Be process 12h in the 3.0mol/L citric acid solution of mordenite 500ml under 60 DEG C of conditions of 3: 1 by 100g sodium form silica alumina ratio, then utilize Standard operation procedure SOP to change into acidic molecular sieve, be designated as catalyzer L, in table 1.
Embodiment 13
The Y molecular sieve being 20: 1 by 50g sodium form silica alumina ratio utilizes Standard operation procedure SOP to convert acidic molecular sieve to, is designated as catalyzer M, in table 1.
Embodiment 14
The Y molecular sieve being 20: 1 by 100g sodium form silica alumina ratio passes into steam treatment 2h under 500 DEG C of conditions, then utilizes Standard operation procedure SOP to change into acidic molecular sieve, is designated as catalyst n, in table 1.
Embodiment 15
Be process 5h in the 1.5mol/L oxalic acid solution of Y molecular sieve 500ml under 95 DEG C of conditions of 20: 1 by 100g sodium form silica alumina ratio, then utilize Standard operation procedure SOP to change into acidic molecular sieve, be designated as catalyzer O, in table 1.
Embodiment 16
The Beta molecular sieve being 15: 1 by 50g sodium form silica alumina ratio utilizes Standard operation procedure SOP to convert acidic molecular sieve to, is designated as catalyst P, in table 1.
Embodiment 17
The Beta molecular sieve being 15: 1 by 100g sodium form silica alumina ratio passes into steam treatment 4h under 600 DEG C of conditions, then utilizes Standard operation procedure SOP to change into acidic molecular sieve, is designated as catalyzer Q, in table 1.
Embodiment 18
Be process 24h in the 0.03mol/L salpeter solution of Beta molecular sieve 500ml under 15 DEG C of conditions of 15: 1 by 100g sodium form silica alumina ratio, then utilize Standard operation procedure SOP to change into acidic molecular sieve, be designated as catalyzer R, in table 1.
Method for preparing catalyst in table 1 embodiment 1 ~ 18
| Embodiment | Catalyzer is numbered | Molecular sieve classification | Silica alumina ratio | Dealumination process | Treatment temp, time, concentration |
| 1 | A | MCM-22 | 40∶1 | - | - |
| 2 | B | MCM-22 | 65∶1 | Water vapour | 550℃、4h |
| 3 | C | MCM-22 | 50∶1 | Hydrochloric acid | 60℃、1h、0.1mol／L |
| 4 | D | Ferrierite | 10∶1 | - | - |
| 5 | E | Ferrierite | 25∶1 | Water vapour | 700℃、1h |
| 6 | F | Ferrierite | 30∶1 | Sulfuric acid | 80℃、4h、0.4mol／L |
| 7 | G | ZSM-5 | 150∶1 | - | - |
| 8 | H | ZSM-5 | 170∶1 | Water vapour | 400℃、8h |
| 9 | I | ZSM-5 | 180∶1 | Acetic acid | 75℃、8h、1.0mol／L |
| 10 | J | Mordenite | 3∶1 | - | - |
| 11 | K | Mordenite | 8∶1 | Water vapour | 650℃、3h |
| 12 | L | Mordenite | 10∶1 | Citric acid | 60℃、12h、3.0mol／L |
| 13 | M | Y | 20∶1 | - | - |
| 14 | N | Y | 30∶1 | Water vapour | 500℃、2h |
| 15 | O | Y | 35∶1 | Oxalic acid | 95℃、5h、1.5mol／L |
| 16 | P | Beta | 15∶1 | - | - |
| 17 | Q | Beta | 25∶1 | Water vapour | 600℃、4h |
| 18 | R | Beta | 30∶1 | Nitric acid | 15℃、24h、0.03mol／L |
Embodiment 19
Catalyst A sample compressing tablet, be ground into 20 ~ 40 orders, for active testing.Take this catalyst A 10g, loading internal diameter is in the stainless steel reaction pipe of 8.5mm, normal pressure, at 550 DEG C with nitrogen activation 4 hours, then drop to temperature of reaction (T)=90 DEG C, pass into carbon monoxide: two polymethoxy dimethyl ethers: hydrogen (CO: DMM
2: H
2)=7: 1: 1, slowly boost to reaction pressure (P)=10MPa, two polymethoxy dimethyl ether mass space velocity (WHSV)=0.2h
-1, use gas chromatographic analysis product, react basicly stable after, calculate the transformation efficiency of two polymethoxy dimethyl ethers and the selectivity of polymethoxy dimethyl ether carbonyl compound, reaction result is in table 2.
Embodiment 20
Change the catalyzer in embodiment 19 into catalyst B, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 21
Change the catalyzer in embodiment 19 into catalyzer C, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 22
Change the catalyzer in embodiment 19 into catalyzer D, reaction conditions is changed to: T=60 DEG C, CO: DMM
2: H
2=13: 1: 3, P=4MPa, WHSV=1.5h
-1, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 23
Change the catalyzer in embodiment 22 into catalyzer E, all the other experimental procedures are consistent with embodiment 22, and reaction result is in table 2.
Embodiment 24
Change the catalyzer in embodiment 22 into catalyzer F, all the other experimental procedures are consistent with embodiment 22, and reaction result is in table 2.
Embodiment 25
Change the catalyzer in embodiment 19 into catalyzer G, reaction conditions is changed to: T=140 DEG C, CO: DMM
2: H
2=2: 1: 5, P=6.5MPa, WHSV=3.0h
-1, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 26
Change the catalyzer in embodiment 25 into catalyzer H, all the other experimental procedures are consistent with embodiment 25, and reaction result is in table 2.
Embodiment 27
Change the catalyzer in embodiment 25 into catalyst I, all the other experimental procedures are consistent with embodiment 25, and reaction result is in table 2.
Embodiment 28
Change the catalyzer in embodiment 19 into catalyzer J, reaction conditions is changed to: T=105 DEG C, CO: DMM
2: H
2=20: 1: 1, P=5.0MPa, WHSV=1.0h
-1, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 29
Change the catalyzer in embodiment 28 into catalyzer K, all the other experimental procedures are consistent with embodiment 28, and reaction result is in table 2.
Embodiment 30
Change the catalyzer in embodiment 28 into catalyzer L, all the other experimental procedures are consistent with embodiment 28, and reaction result is in table 2.
Embodiment 31
Change the catalyzer in embodiment 19 into catalyzer M, reaction conditions is changed to: T=73 DEG C, CO: DMM
2: H
2=10: 1: 2, P=2MPa, WHSV=10.0h
-1, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 32
Change the catalyzer in embodiment 31 into catalyst n, all the other experimental procedures are consistent with embodiment 31, and reaction result is in table 2.
Embodiment 33
Change the catalyzer in embodiment 31 into catalyzer O, all the other experimental procedures are consistent with embodiment 31, and reaction result is in table 2.
Embodiment 34
Change the catalyzer in embodiment 19 into catalyst P, reaction conditions is changed to: T=120 DEG C, CO: DMM
2: H
2=15: 1: 4, P=4.7MPa, WHSV=0.5h
-1, all the other experimental procedures are consistent with embodiment 19, and reaction result is in table 2.
Embodiment 35
Change the catalyzer in embodiment 34 into catalyzer Q, all the other experimental procedures are consistent with embodiment 34, and reaction result is in table 2.
Embodiment 36
Change the catalyzer in embodiment 34 into catalyzer R, all the other experimental procedures are consistent with embodiment 34, and reaction result is in table 2.
Embodiment 37
Catalyzer G sample compressing tablet, be ground into 20 ~ 40 orders, for active testing.Take catalyst sample 10g, loading internal diameter is in the stainless steel reaction pipe of 8.5mm, normal pressure, at 550 DEG C with nitrogen activation 4 hours, then drop to temperature of reaction (T)=88 DEG C, pass into raw material carbon monoxide: polymethoxy dimethyl ether: hydrogen (CO: DMM
n: H
2)=8: 1: 1, wherein DMM
nthe mass ratio of each component is: DMM
2: DMM
3: DMM
4: DMM
5: DMM
6=51.2: 26.6: 12.8: 6.5: 2.9, slowly boost to reaction pressure (P)=8MPa, polymethoxy dimethyl ether mass space velocity (WHSV)=1.5h
-1, use gas chromatographic analysis product, react basicly stable after, reaction result is in table 2.
Embodiment 38
Change the catalyzer in embodiment 37 into catalyzer H, other condition is constant, and reaction result is in table 2.
Embodiment 39
Change the catalyzer in embodiment 37 into catalyst I, other condition is constant, and reaction result is in table 2.
Embodiment 40
Catalyzer M sample compressing tablet, be ground into 20 ~ 40 orders, for active testing.Take catalyst sample 10g, loading internal diameter is in the stainless steel reaction pipe of 8.5mm, normal pressure, at 550 DEG C with nitrogen activation 4 hours, then drop to temperature of reaction (T)=95 DEG C, pass into raw material carbon monoxide: polymethoxy dimethyl ether: hydrogen (CO: DMM
n: H
2)=10: 1: 1, wherein DMM
nthe mass ratio of each component is: DMM
2: DMM
3: DMM
4: DMM
5: DMM
6=47.7: 26.9: 14.0: 7.8: 3.6, slowly boost to reaction pressure (P)=7MPa, polymethoxy dimethyl ether mass space velocity (WHSV)=2.0h
-1, use gas chromatographic analysis product, react basicly stable after, reaction result is in table 2.
Embodiment 41
Change the catalyzer in embodiment 40 into catalyst n, other condition is constant, and reaction result is in table 2.
Embodiment 42
Change the catalyzer in embodiment 40 into catalyzer O, other condition is constant, and reaction result is in table 2.
Comparative example 1
Change the gas ratio in embodiment 30 into CO: DMM
2: H
2=20: 1: 0, all the other experimental procedures are consistent with embodiment 30, and reaction result is in table 2.
Comparative example 2
Change the gas ratio in embodiment 32 into CO: DMM
2: H
2=10: 1: 0, all the other experimental procedures are consistent with embodiment 32, and reaction result is in table 2.
Embodiment 43
Catalyst A sample compressing tablet, be ground into 20 ~ 40 orders, for active testing.Take this catalyst A 10g, loading internal diameter is in the stainless steel reaction pipe of 8.5mm, normal pressure, at 550 DEG C with nitrogen activation 4 hours, then drop to temperature of reaction (T)=90 DEG C, pass into carbon monoxide: methylal: hydrogen (CO: DMM: H
2)=7: 1: 1, slowly boost to reaction pressure (P)=10MPa, control methylal mass space velocity (WHSV)=0.2h
-1, use gas chromatographic analysis product, react basicly stable after, calculate the transformation efficiency of methylal and the selectivity of product, reaction result is in table 3.
Embodiment 44
Change the catalyzer in embodiment 43 into catalyst B, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 45
Change the catalyzer in embodiment 43 into catalyzer C, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 46
Change the catalyzer in embodiment 43 into catalyzer D, T=60 DEG C, CO: DMM: H
2=13: 1: 3, P=4MPa, WHSV=1.5h
-1, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 47
Change the catalyzer in embodiment 46 into catalyzer E, all the other experimental procedures are consistent with embodiment 46, and reaction result is in table 3.
Embodiment 48
Change the catalyzer in embodiment 46 into catalyzer F, all the other experimental procedures are consistent with embodiment 46, and reaction result is in table 3.
Embodiment 49
Change the catalyzer in embodiment 43 into catalyzer G, reaction conditions is changed to: T=140 DEG C, CO: DMM: H
2=2: 1: 5, P=6.5MPa, WHSV=3.0h
-1, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 50
Change the catalyzer in embodiment 49 into catalyzer H, all the other experimental procedures are consistent with embodiment 49, and reaction result is in table 3.
Embodiment 51
Change the catalyzer in embodiment 49 into catalyst I, all the other experimental procedures are consistent with embodiment 49, and reaction result is in table 3.
Embodiment 52
Change the catalyzer in embodiment 43 into catalyzer J, reaction conditions is changed to: T=105 DEG C, CO: DMM: H
2=20: 1: 1, P=5.0MPa, WHSV=1.0h
-1, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 53
Change the catalyzer in embodiment 52 into catalyzer K, all the other experimental procedures are consistent with embodiment 52, and reaction result is in table 3.
Embodiment 54
Change the catalyzer in embodiment 52 into catalyzer L, all the other experimental procedures are consistent with embodiment 52, and reaction result is in table 3.
Embodiment 55
Change the catalyzer in embodiment 43 into catalyzer M, reaction conditions is changed to: T=73 DEG C, CO: DMM: H
2=10: 1: 2, P=2MPa, WHSV=10.0h
-1, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 56
Change the catalyzer in embodiment 55 into catalyst n, all the other experimental procedures are consistent with embodiment 55, and reaction result is in table 3.
Embodiment 57
Change the catalyzer in embodiment 55 into catalyzer O, all the other experimental procedures are consistent with embodiment 55, and reaction result is in table 3.
Embodiment 58
Change the catalyzer in embodiment 43 into catalyst P, reaction conditions is changed to: T=120 DEG C, CO: DMM: H
2=15: 1: 4, P=4.7MPa, WHSV=0.5h
-1, all the other experimental procedures are consistent with embodiment 43, and reaction result is in table 3.
Embodiment 59
Change the catalyzer in embodiment 58 into catalyzer Q, all the other experimental procedures are consistent with embodiment 58, and reaction result is in table 3.
Embodiment 60
Change the catalyzer in embodiment 58 into catalyzer R, all the other experimental procedures are consistent with embodiment 58, and reaction result is in table 3.
Comparative example 3
Gas ratio in embodiment 54 is changed to CO: DMM: H
2=20: 1: 0, all the other experimental procedures are consistent with embodiment 54, and reaction result is in table 3.
Comparative example 4
Gas ratio in embodiment 56 is changed to CO: DMM: H
2=10: 1: 0, all the other experimental procedures are consistent with embodiment 56, and reaction result is in table 3.
Beneficial effect of the present invention includes but not limited to: the catalyzer that method of the present invention adopts is the acid molecular sieve catalyst of Dealumination, and raw material is polymethoxy dimethyl ether or methylal together with the gas mixture of carbon monoxide and hydrogen.Under the reaction conditions of the present invention, raw material can produce the product polymethoxy dimethyl ether carbonyl compound of intermediate as production ethylene glycol or methoxy menthyl acetate by stability and high efficiency by catalyzer, and reaction process is gas-liquid-solid phase reaction.Methoxyl group dme or methylal carbonylation reaction are strong exothermal reaction, and in the present invention, temperature of reaction is lower, add the large and latent heat of phase change of liquid phase thermal capacitance, can control temperature of reaction very well, prevent the problem of temperature runaway in Industrial processes.The gas-liquid-solid phase reaction that the present invention simultaneously adopts can operate under high polymethoxy dimethyl ether or methylal concentration, improves one way reaction production capacity in industrial production, decreases the energy consumption in compression, circulation and sepn process, improve economic performance.
The transformation efficiency of Raw polymethoxy dimethyl ether of the present invention or methylal is high, product polymethoxy dimethyl ether carbonyl compound or methoxy menthyl acetate selectivity high, catalyzer single pass life is long.In addition, in the methods of the invention, liquid phase feed reactant or product inherently fine solvent, does not need to use plus solvent.Liquid phase reaction thing or product can pre-carbon distribution materials in catalytic dissolution reaction process in addition, and be conducive to the activity and the stability that improve catalyzer, reaction conditions is gentleer, can continuous seepage, possess industrial applications potentiality.
And, in the present invention, carbonylation reaction adopts the gas mixture of carbon monoxide and hydrogen as gas phase, produce ethylene glycol technology relative to existing Coal Chemical Industry and need high-purity carbon monooxide, the present invention does not need high-purity carbon monooxide, can significantly reduce synthetic gas separating energy consumption, improve the economy in production process.Add hydrogen in addition in reaction gas and can also improve polymethoxy dimethyl ether or methylal transformation efficiency and polymethoxy dimethyl ether carbonyl compound or methoxy menthyl acetate selectivity, extending catalyst single pass life.
Molecular sieve Dealumination method in the present invention is simple to operation, be applicable to industrial mass production, the single pass life of catalyzer can be extended 5 ~ 10 times through Dealumination, effectively decrease the number of times that annual catalyzer is lived again, be conducive to improving annual capacity, reduce wastage of material, reduce waste gas discharge of wastewater, reduce the loss that catalyzer causes because of pressure release and burning carbon distribution, extend production unit life cycle, improve economic performance.
In addition, the polymethoxy dimethyl ether carbonyl compound produced in the present invention or methoxy menthyl acetate can produce ethylene glycol by hydrogenation hydrolyzation or hydrolysis back end hydrogenation.
Below to invention has been detailed description, but the present invention is not limited to embodiment described herein.It will be appreciated by those skilled in the art that in the case without departing from the scope of the present invention, other changes and distortion can be made.Scope of the present invention is defined by the following claims.
Claims (12)
1., by the method for carbonylation preparation as the polymethoxy dimethyl ether carbonyl compound of the intermediate of production ethylene glycol, it is characterized in that, by raw material polymethoxy dimethyl ether CH
3o (CH
2o)
ncH
3together with carbon monoxide and hydrogen by being loaded with the reactor of the acid molecular sieve catalyst of Dealumination, be 0.2 ~ 10.0h at temperature of reaction 60 ~ 140 DEG C, reaction pressure 2 ~ 10MPa, polymethoxy dimethyl ether mass space velocity
-1and product polymethoxy dimethyl ether carbonyl compound is prepared in reaction under not adding the condition of other solvents, wherein under the cited reaction conditions, at least one in described raw material and described product is liquid phase, the acid molecular sieve catalyst of described Dealumination is solid phase, carbon monoxide and hydrogen are that gas phase is to make reaction process for gas-liquid-solid phase reaction, and the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 20: 1, the mol ratio of hydrogen and described raw material is 1: 1 ~ 5: 1, wherein n>=2 and be integer.
2. prepared as the production intermediate methoxy menthyl acetate of ethylene glycol and a method for polymethoxy dimethyl ether carbonyl compound by carbonylation, it is characterized in that, by raw material methylal CH
3o-CH
2-OCH
3together with carbon monoxide and hydrogen by being loaded with the reactor of the acid molecular sieve catalyst of Dealumination, be 0.2 ~ 10.0h at temperature of reaction 60 ~ 140 DEG C, reaction pressure 2 ~ 10MPa, methylal mass space velocity
-1and product methoxy menthyl acetate and polymethoxy dimethyl ether carbonyl compound are prepared in reaction under not adding the condition of other solvents, wherein under the cited reaction conditions, at least one in described raw material and described product is liquid phase, the acid molecular sieve catalyst of described Dealumination is solid phase, carbon monoxide and hydrogen are that gas phase is to make reaction process for gas-liquid-solid phase reaction, and the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 20: 1, the mol ratio of hydrogen and described raw material is 1: 1 ~ 5: 1.
3. method according to claim 1 and 2, is characterized in that, described product polymethoxy dimethyl ether carbonyl compound is at polymethoxy dimethyl ether CH
3o (CH
2o)
ncH
3-the O-CH of molecular chain
2what formed after inserting one or more carbonyl-CO-in-O-structural unit has-O-(CO)-CH
2-O-or-O-CH
2the product of-(CO)-O-structural unit, wherein n>=2.
4. method according to claim 1, is characterized in that, described polymethoxy dimethyl ether is two polymethoxy dimethyl ether CH
3o (CH
2o)
2cH
3.
5. method according to claim 1 and 2, is characterized in that, described polymethoxy dimethyl ether carbonyl compound be following in one or more:
CH
3-O-(CO)-CH
2-O-CH
2-O-CH
3，
CH
3-O-CH
2-(CO)-O-CH
2-O-CH
3，
CH
3-O-(CO)-CH
2-O-(CO)-CH
2-O-CH
3, and
CH
3-O-(CO)-CH
2-O-CH
2-(CO)-O-CH
3。
6. method according to claim 1 and 2, is characterized in that, the acid molecular sieve catalyst of described Dealumination is by making acid molecular sieve catalyst through comprising steam treatment and prepared by acid-treated Dealumination.
7. method according to claim 6, is characterized in that, the temperature of described steam treatment is 400 ~ 700 DEG C, and the time is 1 ~ 8h; The acid used in described acid treatment is one or more acid be selected from hydrochloric acid, sulfuric acid, nitric acid, acetic acid, oxalic acid, citric acid of 0.03 ~ 3.0mol/L, and described acid-treated temperature is 15 ~ 95 DEG C, and the time is 1 ~ 24h.
8. method according to claim 1 and 2, is characterized in that, the structure type of the acid molecular sieve catalyst of described Dealumination is MWW, FER, MFI, MOR, FAU or BEA.
9. method according to claim 8, is characterized in that, the acid molecular sieve catalyst of described Dealumination is one or more in MCM-22 molecular sieve, ferrierite, ZSM-5 molecular sieve, mordenite, Y zeolite or Beta molecular sieve.
10. method according to claim 1 and 2, is characterized in that, temperature of reaction is 60 ~ 120 DEG C, and reaction pressure is 4 ~ 10MPa, and the mass space velocity of described raw material is 0.5 ~ 3.0h
-1, the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 15: 1, and the mol ratio of hydrogen and described raw material is 1: 1 ~ 3: 1.
11. methods according to claim 1 and 2, is characterized in that, temperature of reaction is 60 ~ 90 DEG C, and reaction pressure is 5 ~ 10MPa, and the mass space velocity of described raw material is 0.5 ~ 1.5h
-1, the mol ratio of carbon monoxide and described raw material is 2: 1 ~ 10: 1, and the mol ratio of hydrogen and described raw material is 1: 1 ~ 2: 1.
12. methods according to claim 1 and 2, is characterized in that, described reactor realizes the fixed-bed reactor of successive reaction, tank reactor, moving-burden bed reactor or fluidized-bed reactor.
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