CN109503326B - Process for indirectly producing ethanol by dimethyl ether - Google Patents
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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
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- C07C29/149—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 of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
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Abstract
The invention provides a process for indirectly producing ethanol by dimethyl ether, belonging to the technical field of ethanol preparation. The process comprises the steps of preparing methyl acetate and acetic acid by taking dimethyl ether and carbon monoxide as raw materials through carbonylation, carrying out catalytic hydrogenation on the methyl acetate and the acetic acid with hydrogen, and purifying the product to obtain an ethanol product. The process for indirectly producing the ethanol by the dimethyl ether comprises the steps of carrying out carbonylation reaction by taking the dimethyl ether and carbon monoxide as raw materials, and then carrying out catalytic reaction on a product methyl acetate and acetic acid together with hydrogen to produce the ethanol. The method for producing ethanol by co-hydrogenation of methyl acetate and acetic acid which are products after the carbonylation reaction avoids separate separation and treatment of acetic acid which is a byproduct as waste acid, reduces energy consumption and discharge of three wastes, and further reduces energy consumption of the device by adopting heat pump rectification for the methanol tower in the separation process of ethanol.
Description
Technical Field
The invention belongs to the technical field of ethanol preparation, and particularly relates to a process for indirectly producing ethanol by dimethyl ether.
Background
Ethanol is an important bulk chemical and energy chemical, and is widely used in the industries of medicine, food, chemical industry, fuel and the like. The absolute ethanol with the volume concentration of more than 99.5 percent can be used as fuel ethanol, and the fuel ethanol is clean high-octane fuel and is renewable energy. As a renewable energy source, the fuel ethanol can be directly used as a liquid fuel or mixed with gasoline for use, so that the dependence on non-renewable energy sources, namely petroleum, can be reduced, and the safety of energy sources is guaranteed. The fuel ethanol industry in China starts late, but develops rapidly, and in recent years, with the fluctuation of petroleum price and the further improvement of domestic petroleum demand, an energy supply diversification strategy represented by alternative energy such as ethanol becomes one direction of the energy policy in China.
China has become the third major biofuel ethanol producing country and country of application in the world after Brazil and the United states. It is desirable to avoid the construction of new fuel ethanol projects using corn as the primary feedstock and to strongly encourage the development of fuel ethanol from non-grain crops. The fuel ethanol moves to the way of non-grain ethanol development and is rapidly developed, and the fuel ethanol has wide prospect in China. On the other hand, the current domestic dimethyl ether device can produce about 1400 million tons, but the operating rate is only 38 percent. The carbonylation synthesis of methyl acetate by using carbon monoxide and dimethyl ether as raw materials can solve the current situation of low dimethyl ether market and excessive capacity at present and can promote enterprises to form a good industrial chain.
At present, the processes of 'synthesis gas → methanol → dimethyl ether' and 'methyl acetate → ethanol' at home and abroad are very mature, but the processes for preparing methyl acetate from dimethyl ether are rarely reported in documents, and the processes of 'dimethyl ether → methyl acetate → ethanol' are longer and have higher energy consumption, so that the problems of energy consumption of devices and emission of three wastes are involved in how to treat acetic acid generated by side reaction in the process of producing methyl acetate by carbonylation of dimethyl ether, and the processes need to be optimized, and the processes are energy-saving and emission-reducing so as to be beneficial to industrial device production.
Disclosure of Invention
The invention aims to provide a process for indirectly producing ethanol by dimethyl ether. The dimethyl ether and the methyl acetate and the acetic acid which are the products of the carbonylation reaction of the carbon monoxide are taken as the raw materials for producing the ethanol by the catalytic reaction with the hydrogen, so that the energy consumption for treating the acetic acid which is the byproduct and is taken as the waste acid can be reduced, and the discharge of three wastes can be reduced. The purpose of the invention is realized by the following technical scheme:
a process for indirectly producing ethanol by dimethyl ether comprises the steps of preparing methyl acetate and acetic acid by carbonylation reaction of dimethyl ether and carbon monoxide, carrying out catalytic hydrogenation on the methyl acetate and the acetic acid with hydrogen, and purifying the product to obtain an ethanol product.
Specifically, the process for indirectly producing the ethanol by the dimethyl ether comprises the following steps:
1) preheating dimethyl ether and carbon monoxide, fully mixing to form mixed reaction gas, and introducing the mixed reaction gas into a carbonylation reactor to carry out carbonylation reaction;
furthermore, the carbonylation reactor is a fixed bed reactor, and a catalyst is arranged in the carbonylation reactor; the molar ratio of the carbon monoxide to the dimethyl ether is 3-20. The carbonylation reactor is preferably a tubular fixed bed reactor.
Further, the liquid raw material dimethyl ether and the gas raw material carbon monoxide are respectively preheated by a preheater, then mixed and vaporized in a vaporization tower, and then heated to the required temperature by a heater and then enter a carbonylation reactor.
Specifically, dimethyl ether and carbon monoxide are preheated by a preheater respectively and then enter a vaporizer, the carbon monoxide is added from the top of the vaporizer, the dimethyl ether is added from the bottom of the vaporizer, mixed and vaporized in the vaporizer, heated to the temperature required by the reaction by a superheater and then added from the top of the carbonylation reactor, the reaction temperature is 200-260 ℃, and the reaction pressure is 3.0-6.0 MPa.
2) After the heat of the product after the carbonylation reaction is recycled, the product enters a gas-liquid separation device, and a liquid-phase crude product enters a rough separation tower to obtain a mixture of methyl acetate and acetic acid;
further, the product materials are discharged from the carbonylation reactor and then sequentially enter a carbon monoxide preheater and a dimethyl ether preheater, the reaction materials are heated by utilizing waste heat step by step and then enter an air cooler for cooling, gas-liquid separation is carried out, a part of inert gas is discharged from a gas-phase product and then circularly enters a reaction system, and a liquid-phase crude product is sent to a rough separation tower.
And further, the liquid phase crude product enters a rough separation tower, the top noncondensable gas is recycled and enters a reaction circulating system, the top produced liquid is circularly mixed into the dimethyl ether raw material, and the tower kettle liquid phase crude product is a mixture of methyl acetate and acetic acid and enters a catalytic hydrogenation device.
3) Preheating the mixture of methyl acetate and acetic acid obtained by the separation device and hydrogen, fully mixing to form mixed reaction gas, and entering a hydrogenation reactor for catalytic hydrogenation;
further, preheating the mixture of methyl acetate and acetic acid and hydrogen, then feeding the mixture into a vaporization tower, adding the mixture from the top of the vaporization tower, feeding the hydrogen into the reaction gas superheater after fully mixing and vaporizing the mixture, heating the mixture to the required reaction temperature, and then feeding the mixture into a hydrogenation reactor for catalytic hydrogenation.
4) And (3) recycling the heat of the product from the hydrogenation reactor, then feeding the product into a gas-liquid separation device, and sequentially passing the liquid-phase crude product through a rough separation tower, a methanol tower and an ethanol tower to obtain an ethanol product.
And further, the hydrogenated product sequentially passes through a reaction gas superheater, a circulating gas preheater and a raw material preheater, waste heat is utilized step by step to heat reaction materials, then the reaction materials enter an air cooler for cooling and gas-liquid separation, a part of inert gas discharged by a gas-phase product and the raw material hydrogen circulate together to enter a reaction system, and a liquid-phase crude product enters a rough separation tower.
And further, the liquid phase crude product enters a rough separation tower, the top noncondensable gas is discharged by removing tail gas, the produced liquid at the top of the tower contains the unreacted methyl acetate raw material and returns to the hydrogenation device, the liquid phase crude product at the bottom of the tower enters a methanol tower, the methanol product is produced at the top of the tower, the mixture at the bottom of the tower enters an ethanol tower together, the ethanol product is produced at the top of the tower, and the heavy impurities are produced at the bottom of the tower.
Further, the methanol tower adopts heat pump rectification, and the heat pump rectification comprises the following steps:
the method comprises the following steps that (1) a methanol tower is rectified under normal pressure, material steam at the top of the tower is pressurized by a heat pump and then enters a reboiler of the methanol tower and a reboiler of the ethanol tower as a heat source respectively, so that part of circulating material at the bottom of the tower is vaporized and then condensed, then enters a cooler of the methanol tower together for cooling, the last part of circulating material flows back, the other part of circulating material is extracted as a methanol product, and an ethanol crude product obtained at the bottom of the tower is refined in a subsequent ethanol;
the ethanol tower adopts normal pressure rectification, a reboiler heat source of the tower bottom is provided by a heat pump of the methanol tower, ethanol products are obtained from the tower top, and the tower bottom is heavy impurities.
Compared with the prior art, the invention has the following beneficial effects:
the process for indirectly producing the ethanol by the dimethyl ether comprises the steps of carrying out carbonylation reaction by taking the dimethyl ether and carbon monoxide as raw materials, and then carrying out catalytic reaction on a product methyl acetate and acetic acid together with hydrogen to produce the ethanol. The method for producing the ethanol by co-hydrogenation of the methyl acetate and the acetic acid which are the products of the carbonylation reaction avoids the separate separation and treatment of the acetic acid which is the byproduct, reduces the discharge of three wastes, reduces energy consumption, and further reduces the energy consumption of the device by adopting heat pump rectification to the methanol tower in the separation process of the ethanol.
Drawings
FIG. 1 is a process flow for the carbonylation of dimethyl ether to produce methyl acetate according to example 1;
FIG. 2 is a process flow of rectifying the produced liquid from the tower bottom of the rough separation tower to obtain refined methyl acetate in example 2;
FIG. 3 is a flow chart of example 3 for the production of ethanol by the catalytic hydrogenation of methyl acetate from the product of example 1;
FIG. 4 is a process flow diagram of the conventional rectification mode adopted by both the methanol and ethanol towers in example 4;
reference numerals: an E-heat exchanger, an F-vaporizer, an R-reactor, an AC-air cooler, a V-gas-liquid separator, a C-compressor and a T-rectifying tower.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example 1
The process for preparing methyl acetate by carbonylation of dimethyl ether is shown in figure 1.
The carbonylation reactor adopts a tubular fixed bed reactor, a modified hydrogen type zeolite molecular sieve catalyst is filled in the reactor, stainless steel magnetic rings with the same granularity are filled at the upper part and the lower part, dimethyl ether and CO are used as raw materials, and the molar ratio of the CO to the dimethyl ether in the inlet gas of the reactor is 6.0. The reaction temperature is 210 ℃ and the pressure is 5.6 MPa.
Carbon monoxide feed gas 1 with the temperature of 30 ℃ and the pressure of 5.6MPa and recycle gas 17 form mixed gas, the temperature of 60 ℃ and the pressure of 5.6MPa are preheated by a preheater E1 to form a material flow 2, and the material flow enters from the top of a vaporizer F1. The mixed raw material of dimethyl ether raw material liquid 3, temperature 45 ℃, pressure 5.6MPa and reclaimed material 18, temperature 46 ℃, pressure 5.6MPa is preheated by preheater E2 to form material flow 4, enters from the top of vaporizer F1, is fully mixed and vaporized in the vaporizer to form mixed reaction gas 6, is heated by a heater E3 to the temperature 210 ℃ required by the reaction to form material flow 7, and is added from the top of a carbonylation reactor R1 filled with a catalyst to carry out carbonylation reaction. The reaction is a strong exothermic reaction, the temperature of a reaction outlet is controlled not to exceed 210 ℃, a large amount of heat released by the reaction is removed by utilizing the steam generated by the vaporization of the deoxygenated water, and the byproduct steam can supplement the consumption of part of steam in the working section. The temperature of a material at the outlet of a reactor is 210 ℃, the pressure of the material is 5.0MPa, the material is used as a high-temperature heat source, the material sequentially passes through heat exchangers E1 and E2 to heat a raw material, a material flow 10 is formed after the heat is fully utilized and then is sent to an air cooler AC1 to be cooled to 60 ℃ to form a material flow 11, the material flow 11 enters a gas-liquid separator V1 to be subjected to gas-liquid separation, a part of gas 12 is used as a discharge gas 13 to be discharged to be subjected to tail gas treatment to prevent inert gas accumulation in a system, most of the gas is pressurized by a compressor C1 to form a material flow 14, the material flow 14 and supplementary carbon monoxide form a recycle gas to be circulated into a carbonylation reactor, and the liquid 15 discharged from the separator.
The operation pressure of the crude separation tower is 2.0MPa, the tower top temperature is 42 ℃, the tower bottom temperature is 186 ℃, the reflux ratio is 2, the tower top non-condensable gas 16 is pressurized by a supercharger C2 and then forms a material flow 17 together with the gas from a gas-liquid separator V1, and then returns to the reactor together with the CO make-up gas. The mixed solution of the produced liquid 18 at the top of the tower, which contains 98 percent of dimethyl ether, returns to the raw material of dimethyl ether for continuous reaction, the produced liquid 19 at the bottom of the tower has the temperature of 185 ℃ and the pressure of 2.0MPa, and the components and the mass fraction of the product are as follows: methyl acetate: 94.84%, acetic acid 5.14%, and the balance others.
Example 2
This example is a comparative example of example 1, and further rectifying the produced liquid 19 from the bottom of the crude separation column to obtain refined methyl acetate, and the process flow diagram is shown in fig. 2, and the specific implementation is as follows:
the temperature of the produced liquid 19 at the tower bottom of the rough separation tower is 185 ℃, the pressure is 2.0MPa, and the composition and the mass fraction of the product are as follows: methyl acetate: 94.84 percent and acetic acid 5.14 percent enter a refining tower, the operating pressure of the refining tower is 0.2MPa, the temperature at the top of the tower is 78 ℃, the temperature at the bottom of the tower is 128 ℃, and the reflux ratio is 2. After the steam at the top of the tower is condensed by a condenser at the top of the tower, one part of the steam flows back, and the other part of the steam is extracted as refined methyl acetate, wherein the content of methyl acetate is 99.9 percent. The produced liquid at the tower bottom is mainly acetic acid as heavy impurities to be treated outside.
Example 3
This example is a process scheme for the production of ethanol by the catalytic hydrogenation of methyl acetate from the product obtained in example 1 or example 2, the process scheme is schematically shown in FIG. 3. The specific implementation is as follows:
the hydrogenation reactor is filled with a modified Cu catalyst, stainless steel magnetic rings with the same particle size are used as filling materials at the upper part and the lower part, a mixed solution (example 1) of methyl acetate and acetic acid or refined methyl acetate (example 2) is used as a liquid raw material, a certain amount of hydrogen is introduced, the molar ratio of the hydrogen to the ester in the reaction gas is controlled to be 30, the reaction temperature is 205 ℃, and the pressure is 6.0 MPa.
A hydrogen raw material gas 20 with the temperature of 40 ℃, the pressure of 6.0MPa and a recycle gas 32 with the pressure of 60 ℃ and the pressure of 6.0MPa, a material flow 21 is formed after being preheated by a heat exchange gas E4, the material flow enters a vaporization tower F2 from the top and is mixed and vaporized with a methyl acetate mixed liquid 22, a material flow 23 formed from a vaporization tower F2 enters a heat exchanger E6 and is heated to the temperature 205 ℃ required by the reaction, the material flow enters a hydrogenation reactor R2 filled with a catalyst for hydrogenation reaction, the temperature of an outlet product material 25 is 234 ℃ (the reaction adiabatic temperature is raised to 29 ℃), the product material is a high-quality heat source gas, the product material is cooled to a product material 28 after being sequentially heated by the heat exchangers E4 and E5 and then is further cooled to 50 ℃ by an air cooler AC2 to form a material flow 29, the gas-liquid separation is carried out by a gas-liquid separator V2, a gas-phase material flow 30, most of the gas-liquid flow, mixing with the hydrogen as the supplementary material and returning to the hydrogenation reactor. The liquid product stream 33 from gas liquid separator separation V2 is passed to a subsequent rectification unit.
The liquid phase crude product firstly passes through a rough separation tower T2, the operation pressure of the rough separation tower is 0.2MPa, the temperature of the top of the tower is 50 ℃, the temperature of the bottom of the tower is 90 ℃, the reflux ratio is 15, the noncondensable gas 34 at the top of the tower is discharged to remove tail gas for centralized treatment, the produced liquid 35 at the top of the tower is mainly mixed liquid containing methyl acetate, the mixed liquid returns to a raw material supply system of the methyl acetate, and the produced liquid at the bottom of the tower is 36 methanol removal tower T. The operating pressure of a methanol tower is 0.12MPa, the temperature of the top of the methanol tower is 68 ℃, the temperature of the bottom of the methanol tower is 83 ℃, the reflux ratio is 8, the steam 37 at the top of the methanol tower is heated by a heat exchanger E7 to form a material flow 38, the material flow is pressurized by a heat pump C4 to form superheated steam 39, the superheated compressed steam is used as a heat source of a reboiler at the bottom of the methanol tower and the subsequent ethanol tower to replace steam for heating, the heat is utilized to form condensate 40, the condensate 40 is utilized again by the heat of the heat exchanger E7, a part of the condensate flows back to be used as produced liquid 41 at the top of the ethanol tower, the. The operation pressure of the ethanol tower T4 is 0.12MPa, the tower top temperature is 82 ℃, the tower bottom temperature is 85 ℃, the reflux ratio is 1, the produced liquid 43 at the tower top is an ethanol product, the ethanol content is more than 95 percent, and the produced liquid 44 at the tower bottom is heavy impurities.
Example 4
This example belongs to the comparative example of example 3, and the product obtained in example 1 or example 2 was also subjected to catalytic hydrogenation of methyl acetate to produce ethanol. The reaction part and the crude part are the same as those in example 3, except that the methanol and ethanol towers adopt a conventional rectification mode instead of a heat pump rectification mode, and the process flow diagram is shown in figure 4 and is implemented as follows:
and (3) feeding the material flow 36 from the tower bottom of the rough separation tower into a methanol tower, wherein the operating pressure of the methanol tower is 0.12MPa, the tower top temperature is 68 ℃, the tower bottom temperature is 83 ℃, the reflux ratio is 8, the tower top steam is condensed by a tower top condenser, part of the steam flows back, the material flow 37 is used as a methanol product, and the content of the methanol is over 99.9 percent. The tower bottom material flow 38 is rectified by an ethanol tower. The operation pressure of the ethanol tower T4 is 0.12MPa, the tower top temperature is 82 ℃, the tower bottom temperature is 85 ℃, the reflux ratio is 1, the produced liquid 39 at the tower top is an ethanol product, the ethanol content is more than 95 percent, and the produced liquid 40 at the tower bottom is heavy impurities.
TABLE 1 analysis of energy consumption for different treatment regimes (taking 10 million tons/year ethanol project as an example)
The invention adopts the embodiment 1 and the embodiment 3 to complete the whole process of preparing methyl acetate by carbonylation of dimethyl ether and preparing ethanol by hydrogenation of methyl acetate. The mixed hydrogenation of the carbonylation products in the example 1 reduces the steam consumption of the refined methyl ester hydrogenation after the mixed products in the example 2 are treated by about 6.9 t/h. The product after acetic ester hydrogenation is separated by conventional rectification (example 4), and the overhead condenser of the methanol tower has the extra heat load of 23.8 x 103kw needs additional cooling medium to cool, and the extra heat load of the tower kettle reboiler is 23.56 x 103kw requires an additional heat source for heat supply, if a heat pump is used for rectification (example 3), the overhead steam is used as the heat source of the reboiler at the column bottom, and the condenser and the reboiler do not consume additional energy, but the pressure increase of the heat pump can be increased by 2.15 x 103The power consumption of kw and the heat pump coefficient of heat supply COP can reach more than 10, so the energy-saving effect is obvious.
Compared with the traditional scheme (example 2+ example 4), the flow scheme of the invention reduces the steam consumption 46.96t/h and increases the power consumption 2152 x 103kwh to increase a certain electricity consumption to reduce steam consumption, which is very advantageous for areas where electricity prices are relatively cheap.
It should be noted that the heat pump rectification does not change the material balance calculation, and the above temperature and flow difference is caused by the simulation calculation error.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (7)
1. The process for indirectly producing ethanol by dimethyl ether is characterized by comprising the following steps:
1) preheating dimethyl ether and carbon monoxide, fully mixing to form mixed reaction gas, and introducing the mixed reaction gas into a carbonylation reactor to carry out carbonylation reaction; the carbonylation reactor is a fixed bed reactor, and a catalyst is arranged in the carbonylation reactor; the molar ratio of the carbon monoxide to the dimethyl ether is 3-20;
2) after the heat of the product after the carbonylation reaction is recycled, the product enters a gas-liquid separation device, and a liquid-phase crude product enters a rough separation tower to obtain a mixture of methyl acetate and acetic acid;
3) preheating the mixture of methyl acetate and acetic acid obtained by the separation device and hydrogen, fully mixing to form mixed reaction gas, and entering a hydrogenation reactor for catalytic hydrogenation;
4) after the heat of the product discharged from the hydrogenation reactor is recycled, the product enters a gas-liquid separation device, and a liquid phase crude product sequentially passes through a rough separation tower, a methanol tower and an ethanol tower to obtain an ethanol product;
the methanol tower adopts heat pump rectification, and the heat pump rectification comprises the following steps:
the method comprises the following steps that (1) a methanol tower is rectified under normal pressure, material steam at the top of the tower is pressurized by a heat pump and then enters a reboiler of the methanol tower and a reboiler of the ethanol tower as a heat source respectively, so that part of circulating material at the bottom of the tower is vaporized and then condensed, then enters a cooler of the methanol tower together for cooling, the last part of circulating material flows back, the other part of circulating material is extracted as a methanol product, and an ethanol crude product obtained at the bottom of the tower is refined in a subsequent ethanol;
the ethanol tower adopts normal pressure rectification, a reboiler heat source of the tower bottom is provided by a heat pump of the methanol tower, anhydrous ethanol products are obtained from the tower top, and the tower bottom is heavy impurities.
2. The process for indirectly producing ethanol by using dimethyl ether according to claim 1, wherein in the step 1), the liquid raw material dimethyl ether and the gaseous raw material carbon monoxide are preheated by a preheater respectively, then mixed and vaporized in a vaporization tower, and then heated to the required temperature by a heater and then enter a carbonylation reactor.
3. The process for indirectly producing ethanol by using dimethyl ether according to claim 1, wherein in the step 2), the product materials are discharged from the carbonylation reactor and then sequentially enter a carbon monoxide preheater and a dimethyl ether preheater, the reaction materials are heated by using waste heat step by step, then enter an air cooler for cooling, gas-liquid separation is carried out, a part of inert gas is discharged from the gas-phase product and then is circulated into a reaction system, and the liquid-phase crude product enters a rough separation tower.
4. The process for indirectly producing ethanol by dimethyl ether according to claim 1, wherein in the step 2), the liquid phase crude product enters a rough separation tower, the top noncondensable gas is recycled and enters a reaction circulating system, the top produced liquid is circularly mixed into the dimethyl ether raw material, and the liquid phase crude product in the bottom of the tower is a mixture of methyl acetate and acetic acid and enters a catalytic hydrogenation device.
5. The process for indirectly producing ethanol by dimethyl ether according to claim 1, wherein in the step 3), the mixture of methyl acetate and acetic acid and hydrogen are preheated and then enter a vaporization tower, the mixture is added from the top of the vaporization tower, the hydrogen enters from the bottom of the vaporization tower, the mixture is fully mixed and vaporized and then enters a reaction gas superheater, and the reaction gas superheater is heated to the required reaction temperature and then enters a hydrogenation reactor for catalytic hydrogenation.
6. The process for indirectly producing ethanol by dimethyl ether according to claim 1, wherein in the step 4), the hydrogenated product sequentially passes through a reaction gas superheater, a circulating gas preheater and a raw material preheater, the reaction material is heated by waste heat step by step, then the reaction material is cooled in an air cooler, gas and liquid are separated, a part of inert gas is discharged from a gas-phase product and then the gas-phase product and the raw material hydrogen are circulated together to enter a reaction system, and a liquid-phase crude product is sent to a rough separation tower.
7. The process for indirectly producing ethanol by dimethyl ether according to claim 1, wherein in the step 4), the liquid phase crude product enters a rough separation tower, the top noncondensable gas is discharged from the tail gas, the produced liquid at the top of the tower contains unreacted methyl acetate raw material and returns to a hydrogenation device, the liquid phase crude product at the bottom of the tower enters a methanol tower, the methanol product is produced at the top of the tower, the mixture at the bottom of the tower enters an ethanol tower together, the ethanol product is produced at the top of the tower, and the heavy impurities are produced at the bottom of the tower.
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| CN111001431B (en) * | 2019-12-06 | 2020-12-01 | 西南化工研究设计院有限公司 | Core-shell catalyst for preparing ethanol from dimethyl ether and synthesis gas by one-step method and preparation method and application thereof |
| CN111848344A (en) * | 2020-07-16 | 2020-10-30 | 南京延长反应技术研究院有限公司 | Reaction system and method for preparing ethanol by adopting synthesis gas |
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| CN112169712A (en) * | 2020-10-29 | 2021-01-05 | 北京石油化工工程有限公司 | Reactor for synthesizing methyl acetate by dimethyl ether carbonylation |
| CN112608232B (en) * | 2020-12-04 | 2023-01-20 | 兖矿鲁南化工有限公司 | System and method for recycling reaction heat in process of synthesizing acetic acid by methanol low-pressure carbonyl |
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| CN115197047B (en) * | 2022-08-22 | 2023-08-22 | 西南化工研究设计院有限公司 | Coupling reaction method for preparing ethanol from dimethyl ether |
| CN117599690B (en) * | 2024-01-23 | 2024-05-14 | 中建安装集团有限公司 | Device and method for producing methyl ethyl carbonate and diethyl carbonate |
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| CN106311336A (en) * | 2016-08-11 | 2017-01-11 | 西南化工研究设计院有限公司 | Method for making methyl acetate through carbonylation of dimethyl ether and the modified molecular sieve catalyst and modification method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103012062A (en) * | 2012-12-20 | 2013-04-03 | 上海戊正工程技术有限公司 | Process for indirectly producing alcohol with synthetic gas and application of process |
| CN203033918U (en) * | 2012-12-20 | 2013-07-03 | 上海戊正工程技术有限公司 | Process system for indirectly producing ethanol by using synthesis gases |
| CN103896768A (en) * | 2012-12-25 | 2014-07-02 | 中国科学院大连化学物理研究所 | Method used for preparing methyl acetate |
| CN103657715A (en) * | 2013-12-04 | 2014-03-26 | 中国科学院山西煤炭化学研究所 | Catalyst for methanol or dimethyl ether carbonylation synthesis of methyl acetate, preparation method and application thereof |
| CN106311336A (en) * | 2016-08-11 | 2017-01-11 | 西南化工研究设计院有限公司 | Method for making methyl acetate through carbonylation of dimethyl ether and the modified molecular sieve catalyst and modification method thereof |
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