CN109503326A - A kind of technique that dimethyl ether produces ethyl alcohol indirectly - Google Patents
A kind of technique that dimethyl ether produces ethyl alcohol indirectly Download PDFInfo
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- CN109503326A CN109503326A CN201811462039.XA CN201811462039A CN109503326A CN 109503326 A CN109503326 A CN 109503326A CN 201811462039 A CN201811462039 A CN 201811462039A CN 109503326 A CN109503326 A CN 109503326A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- 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
- C07C29/147—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
- 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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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
- C07C51/12—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on an oxygen-containing group in organic compounds, e.g. alcohols
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/36—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates
- C07C67/37—Preparation of carboxylic acid esters by reaction with carbon monoxide or formates by reaction of ethers with carbon monoxide
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Abstract
The present invention provides the technique that a kind of dimethyl ether produces ethyl alcohol indirectly, belongs to ethyl alcohol preparation technical field.The technique first prepares methyl acetate and acetic acid using dimethyl ether and carbon monoxide as feedstock carbonyl reaction, and methyl acetate and acetic acid add hydrogen with hydrogen catalytic again, obtains alcohol product after product purification processing.Dimethyl ether of the present invention produces the technique of ethyl alcohol indirectly, first carries out carbonylation using dimethyl ether and carbon monoxide as raw material, acetic acid product methyl esters together reacts production ethyl alcohol with acetic acid with hydrogen catalytic.Acetic acid product methyl esters after carbonylation is avoided using altogether plus by the way of hydrogen production ethyl alcohol to being separately separated and handling as spent acid of by-product acetic acid with acetic acid, reduce energy consumption, the discharge of the three wastes is decreased, while further reduced the energy consumption of device using heat pump distillation to methanol column in the separation process of ethyl alcohol.
Description
Technical field
The invention belongs to ethyl alcohol preparation technical field, technique that specially a kind of dimethyl ether produces ethyl alcohol indirectly.
Background technique
Ethyl alcohol is important bulk chemical and energy chemistry product, is widely used in the industries such as medicine, food, chemical industry, fuel.
Volumetric concentration reaches 99.5% or more dehydrated alcohol, can be used as alcohol fuel, and alcohol fuel is the high-octane rating of combustion cleaning
Fuel is renewable energy.As renewable energy, alcohol fuel can make directly as liquid fuel or with gasoline mixing
With can reduce to the dependence of non-renewable energy resources-petroleum, ensure the safety of the energy.Chinese fuel ethanol industrial is started late, but
It quickly grows, recent years, with the fluctuation of oil price and further increasing for domestic oil needs, is substituted with ethyl alcohol etc.
The energy is that the energy supply diversification strategy of representative has become a direction of Chinese energy policy.
China has become in the world after Brazil, the third-largest bio-fuel ethyl alcohol producing country and using state after the U.S..It is required that
No longer construction it is new using corn as the alcohol fuel project of primary raw material, and encouraging development energetically using non-grain crop is raw material exploitation
Alcohol fuel.Alcohol fuel has moved towards the road of non-grain ethyl alcohol development and has been developed rapidly, and has bright prospects in China.
On the other hand, at present 14,000,000 tons of Domestic DME device capbility or so, but the utilization of capacity only has 38%.Pass through carbon monoxide and two
Methyl ether, which is combined to methyl acetate both for feedstock carbonyl, can solve current dimethyl ether recessed market, and the status of excess capacity can also push
Enterprise forms good industrial chain.
" synthesis gas → methanol → dimethyl ether " and " methyl acetate → ethyl alcohol " technique are highly developed both at home and abroad at present, but two
For methyl ether methyl acetate technique but less it has been reported that " dimethyl ether → methyl acetate → ethyl alcohol " process is longer, energy consumption is higher,
Dimethyl ether carbonylation production methyl acetate, which is crossed the acetic acid that side reaction generates in title and how to be handled, is related to the energy consumption and the three wastes of device
Emission problem, it is therefore desirable to optimize technique, energy-saving and emission-reduction are in favor of industrialized unit production.
Summary of the invention
The purpose of the present invention is to provide the techniques that a kind of dimethyl ether produces ethyl alcohol indirectly.With dimethyl ether and carbon monoxide carbonyl
The acetic acid product methyl esters of glycosylation reaction, collectively as the raw material for reacting production ethyl alcohol with hydrogen catalytic, can reduce by-product with acetic acid
Processing energy consumption and three waste discharge of the object acetic acid as spent acid.The object of the invention is achieved through the following technical solutions:
A kind of dimethyl ether produces the technique of ethyl alcohol indirectly, and the technique is first using dimethyl ether and carbon monoxide as feedstock carbonyl
Reaction prepares methyl acetate and acetic acid, and methyl acetate and acetic acid add hydrogen with hydrogen catalytic again, obtains ethyl alcohol after product purification processing and produce
Product.
Specifically, the technique that a kind of dimethyl ether produces ethyl alcohol indirectly, comprising the following steps:
1) it is sufficiently mixed after dimethyl ether and carbon monoxide preheating, forms hybrid reaction gas, carried out into carbonylation reactor
Carbonylation；
Further, the carbonylation reactor is that fixed bed reactors are excellent, and catalyst is provided in carbonylation reactor；
The molar ratio of the carbon monoxide and dimethyl ether is 3~20.The carbonylation reactor is preferably tubular fixed-bed reactor.
Further, liquid charging stock dimethyl ether and gas raw material carbon monoxide mix in vaporization tower after distinguishing preheated device preheating
It closes, vaporization, carbonylation reactor is then entered after superheater is heated to required temperature.
Specifically, dimethyl ether and carbon monoxide distinguish preheated device preheating, and subsequently into vaporizer, carbon monoxide is from vaporization
It is added at the top of device, dimethyl ether is added from vaporizer bottom, and mixing, vaporization are heated to reaction institute using superheater in vaporizer
It is added at the top of carbonylation reactor after needing temperature, 200-260 DEG C of reaction temperature, reaction pressure 3.0-6.0MPa.
2) product after carbonylation is after heat recovery and utilization, and into gas-liquid separation device, liquid phase crude product enters thick
Divide tower, obtains the mixture of methyl acetate and acetic acid；
Further, product material sequentially enters carbon monoxide preheater, dimethyl ether preheating after coming out from carbonylation reactor
Device step by step heats reaction mass using waste heat, cooling subsequently into aerial cooler, gas-liquid separation, gaseous products row
It is recycled into reaction system after putting a part of indifferent gas, liquid phase crude product removes crude tower.
Further, liquid phase crude product enters crude tower, and the recycling of tower top fixed gas enters recycle system of reaction, and overhead extraction liquid follows
Ring is mixed into dimethyl ether raw material, and tower reactor liquid phase crude product is the mixture of methyl acetate and acetic acid, removes catalytic hydrogenation device.
3) mixture and hydrogen of separator obtains methyl acetate and acetic acid are sufficiently mixed after preheating, are formed mixed
Reaction gas is closed, carries out catalytic hydrogenation into hydrogenator；
Further, the mixture and hydrogen of the methyl acetate and acetic acid by preheating after enter vaporization tower, mixture from
It is added at the top of vaporization tower, hydrogen enters from tower top, enters reaction gas superheater after being sufficiently mixed vaporization, reaction temperature needed for being heated to
Enter hydrogenator after degree and carries out catalytic hydrogenation.
4) product that hydrogenator comes out is after heat recovery and utilization, and into gas-liquid separation device, liquid phase crude product is successively
Through crude tower, methanol column and ethanol tower, alcohol product is obtained.
Further, the successively reacted gas superheater of the product after described plus hydrogen, circulating gas preheater, feed preheater, by
Grade heats reaction mass using waste heat, cooling subsequently into aerial cooler, and gas-liquid separation, gaseous products discharge one
Reaction system is recycled into together with raw hydrogen after dividing indifferent gas, liquid phase crude product removes crude tower.
Further, liquid phase crude product enters crude tower, and tower top fixed gas removes exhaust emissions, and overhead extraction liquid is complete containing unreacted
Methyl acetate raw material, return hydrogenation plant in, tower reactor liquid phase crude product enters methanol column, and overhead extraction is methanol product, tower reactor
Mixture enters ethanol tower, overhead extraction alcohol product together, and tower reactor is heavy seeds.
Further, the methanol column use heat pump distillation, heat pump distillation the following steps are included:
Methanol column uses atmospheric distillation, and tower top material steam respectively enters methanol column as heat source after heat pump pressurizes and boils again
Device and ethyl alcohol tower reboiler itself are condensed after vaporizing tower bottom recycle stock a part, then enter methanol tower cooler together
Device is cooling, and last part reflux, a part is produced as methanol product, and tower reactor obtains ethyl alcohol crude product and removes subsequent ethanol rectifying column
Purification；
Ethanol tower uses atmospheric distillation, and tower reactor reboiler heat source is provided by methanol column heat pump, and overhead extraction obtains ethyl alcohol
Product, tower reactor are heavy seeds.
Compared with prior art, the invention has the following advantages:
Dimethyl ether of the present invention produces the technique of ethyl alcohol indirectly, first be carbonylated using dimethyl ether and carbon monoxide as raw material anti-
It answers, acetic acid product methyl esters together reacts production ethyl alcohol with acetic acid with hydrogen catalytic.To the acetic acid product first after carbonylation
Ester, using avoiding being separately separated and handling to by-product acetic acid altogether plus by the way of hydrogen production ethyl alcohol, reduces three wastes row with acetic acid
It puts, energy consumption also decreases, while further reduced to methanol column using heat pump distillation in the separation process of ethyl alcohol
The energy consumption of device.
Detailed description of the invention
Fig. 1 is the process flow that 1 Dimethyl ether carbonylation of embodiment prepares methyl acetate；
Fig. 2 is that 2 crude tower tower reactor Produced Liquid rectifying of embodiment obtains the process flow of smart methyl acetate；
Fig. 3 is the process flow that embodiment 3 carries out that methyl acetate catalysis adds hydrogen to produce ethyl alcohol with 1 product of embodiment；
Fig. 4 is the process flow that 4 methanol of embodiment and ethanol tower are all made of conventional rectification mode；
Appended drawing reference: E- heat exchanger, F- vaporizer, R- reactor, AC- aerial cooler, V- gas-liquid separator, C- compression
Machine, T- rectifying column.
Specific embodiment
In order to make the objectives, technical solutions, and advantages of the present invention clearer, with reference to embodiments, to the present invention
It is further elaborated.It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, it is not used to
Limit the present invention.
Embodiment 1
The technique that Dimethyl ether carbonylation prepares methyl acetate is as shown in Figure 1.
Carbonylation reactor uses calandria type fixed bed reactor, is packed into modified h-type zeolite molecular sieve catalyst, on
Under use the comparable stainless steel magnet ring of granularity as filling, using dimethyl ether and CO as raw material, CO and diformazan in reactor air inlet
The molar ratio of ether is 6.0.210 DEG C of reaction temperature, pressure 5.6Mpa.
Feed gas containing carbon monoxide 1, forms gaseous mixture, temperature 60 C, pressure with circulating air 17 by 30 DEG C of temperature, pressure 5.6MPa
Power 5.6MPa forms logistics 2 after preheater E1 preheating, enters from the top of vaporizer F1.The material liquid 3 of dimethyl ether, temperature
The mixed raw material that 45 DEG C of degree, pressure 5.6MPa and reclaimed materials 18 form, 46 DEG C of temperature, pressure 5.6MPa is preheated by preheater E2
Logistics 4 is formed afterwards, is entered from the top of vaporizer F1, vaporization is sufficiently mixed in vaporizer, forms hybrid reaction gas 6, then pass through
Superheater E3 is heated to reacting required 210 DEG C of temperature, forms logistics 7, then from the carbonylation reactor R1 that catalyst is housed
Top be added, carry out carbonylation.Reaction is strong exothermal reaction, and control reaction outlet temperature is no more than 210 DEG C, and reaction is put
Amount of heat out is removed using deoxygenation water vapor producing steam, and the steam of by-product can feed the consumption of a part of steam of the workshop section.
210 DEG C, pressure 5.0MPa of 8 temperature of reactor outlet material successively passes through heat exchanger E1, E2 as high temperature heat source, heats raw material
Material forms logistics 10 after heat makes full use of and aerial cooler AC1 is gone to be cooled to 60 DEG C again, forms logistics 11, logistics 11
Into gas-liquid separator V1, gas-liquid separation is carried out, 12 a part of gas discharges vent gas treatment as discharge gas 13, to prevent system
Interior inert gas accumulation, the overwhelming majority form logistics 14 after compressor C1 pressurization, form circulating air with supplement carbon monoxide
It is recycled into carbonylation reactor, the liquid 15 that separator comes out, temperature 50 C, pressure 4.8MPa, into T1 crude tower together.
Crude separation tower operating pressure 2.0MPa, 42 DEG C of tower top temperature, 186 DEG C of bottom temperature, reflux ratio 2, tower top fixed gas
16 are formed together logistics 17 after supercharger C2 pressurization with the gas-liquid separator V1 gas come out, then return together with CO supplement gas
Return reactor.Mixed liquor of the overhead extraction liquid 18 containing dimethyl ether 98%, returning to the raw material of dimethyl ether, the reaction was continued, tower reactor Produced Liquid
19,185 DEG C of temperature, pressure 2.0MPa, the composition and mass fraction of product are as follows: methyl acetate: 94.84%, acetic acid 5.14%,
Remaining is other.
Embodiment 2
The present embodiment is the comparative example of embodiment 1, does further rectifying to crude tower tower reactor Produced Liquid 19, obtains essence
Methyl acetate, process flow diagram is as shown in Fig. 2, specific implementation is as follows:
Crude tower tower reactor Produced Liquid 19,185 DEG C of temperature, pressure 2.0MPa, the composition and mass fraction of product are as follows: tumer
Ester: 94.84%, acetic acid 5.14%, into treating column, treating column operating pressure 0.2MPa, 78 DEG C of tower top temperature, bottom temperature
128 DEG C, reflux ratio 2.Overhead vapours is after overhead condenser condenses, a part reflux, and a part is as smart methyl esters extraction, vinegar
Sour methyl ester content 99.9%.Tower reactor Produced Liquid is that predominantly acetic acid goes out-of-bounds to handle as heavy seeds.
Embodiment 3
The present embodiment is to carry out methyl acetate catalysis with product obtained in Example 1 or Example 2 hydrogen is added to produce ethyl alcohol, work
Skill general flow chart is as shown in Figure 3.It is embodied as follows:
Hydrogenator is packed into modified Cu series catalysts, use the comparable stainless steel magnet ring of granularity as filling up and down,
Using the mixed liquor (embodiment 1) or smart methyl acetate (embodiment 2) of methyl acetate and acetic acid as liquid charging stock, it is passed through a certain amount of
Hydrogen, control reaction gas in the molar ratio of hydrogen and ester be 30,205 DEG C of reaction temperature, pressure 6.0Mpa.
Hydrogen feed gas 20,40 DEG C of temperature, the circulating air that pressure 6.0MPa and return gas 32 form, temperature 60 C, pressure
6.0MPa forms logistics 21 after exchanging air E4 is preheated, vaporization tower F2 is entered from top, with methyl acetate mixing liquid
22 mixing vaporizations, come out the logistics 23 formed from vaporization tower F2 and enter heat exchanger E6, are heated to reaction required temperature 205
DEG C, it enters in the hydrogenator R2 equipped with catalyst and carries out hydrogenation reaction, 234 DEG C of the temperature of exported product material 25 is (anti-
Answer 29 DEG C of adiabatic temperature rise), product material be high product heat source gas, successively by heat exchanger E4, E5 heat feed product after itself
Becoming product material 28 by cooling goes aerial cooler AC2 progress to be cooled to 50 DEG C, logistics 29 is formed, using gas-liquid separator
V2 gas-liquid separation, gaseous stream 30 are most of to be pressurized to form logistics by recycle gas compressor C3 after discharging small part 31
32, it is mixed with system supplement raw hydrogen, returns to hydrogenator.The liquid product stream 33 that gas-liquid separator separates V2 comes out
Then remove subsequent rectifier unit.
Liquid phase crude product first passes around crude tower T2, crude tower operating pressure 0.2MPa, and 50 DEG C of tower top temperature, bottom temperature 90
DEG C, reflux ratio 15, the discharge of tower top fixed gas 34 goes tail gas to focus on, and overhead extraction liquid 35 is mainly the mixing containing methyl acetate
Liquid, returns to the raw material make-up system of methyl acetate, and tower reactor Produced Liquid 36 removes methanol column T3.Methanol column operating pressure 0.12MPa, tower
68 DEG C of temperature of top, 83 DEG C of bottom temperature, reflux ratio 8, overhead vapours 37 is heated to form logistics 38 through superheater E7, using heat
It pumps and forms superheated steam 39 after C4 is pressurized, reboiler heat source of the compressed steam of overheat as Ben Ta and subsequent ethanol tower tower reactor,
Steam heating is substituted, condensate liquid 40 is formed after heat utilization, and the reflux of heat utilization rear portion is a part of again through superheater E7
As overhead extraction liquid 41,99.9% or more methanol content, tower reactor distillate 42 removes ethanol tower T4.Ethanol tower T4 operating pressure
0.12MPa, 82 DEG C of tower top temperature, 85 DEG C of bottom temperature, reflux ratio 1, overhead extraction liquid 43 is alcohol product, ethanol content 95%
More than, tower reactor Produced Liquid 44 is that heavy seeds are gone out-of-bounds.
Embodiment 4
The present embodiment belongs to the comparative example of embodiment 3, equally with product obtained in Example 1 or Example 2 progress
Methyl acetate catalysis adds hydrogen to produce ethyl alcohol.Reactive moieties and rough segmentation part are same as Example 3, are not both methanol and ethanol tower
It is all made of conventional rectification mode rather than heat pump distillation mode, process flow diagram is as shown in figure 4, specific implementation is as follows:
From crude tower tower reactor logistics 36 enter methanol column, methanol column operating pressure 0.12MPa, 68 DEG C of tower top temperature, tower
83 DEG C of kettle temperature degree, reflux ratio 8, for overhead vapours after overhead condenser condenses, a part reflux, logistics 37 is used as methanol product
Extraction uses, 99.9% or more methanol content.Ethanol tower rectification process is gone in tower reactor logistics 38.Ethanol tower T4 operating pressure
0.12MPa, 82 DEG C of tower top temperature, 85 DEG C of bottom temperature, reflux ratio 1, overhead extraction liquid 39 is alcohol product, ethanol content 95%
More than, tower reactor Produced Liquid 40 is that heavy seeds are gone out-of-bounds.
1 Different treatments energy consumption analysis of table (by taking 100,000 tons/year of ethyl alcohol projects as an example)
The present invention completes Dimethyl ether carbonylation using embodiment 1+ embodiment 3 and prepares methyl acetate, and methyl acetate adds again
Hydrogen prepares the full-flow process of ethyl alcohol.1 carbonylation product mixed hydrogenation of embodiment compared to 2 mix products of embodiment treated essence
Methyl esters repeated hydrogenation steam consumption reduces about 6.9t/h.Product separation after Dichlorodiphenyl Acetate ester through hydrogenation uses conventional rectification (embodiment 4),
The thermic load 23.8*10 that methanol column overhead condenser has more3Kw needs additional cooling medium cooling, and the heat that tower reactor reboiler has more is negative
Lotus 23.56*103Kw needs extra heat source heat supply, and according to heat pump distillation (embodiment 3), overhead vapours is as tower reactor reboiler
Heat source, condenser and reboiler do not consume the energy additionally, for no other reason than that heat pump pressurization will increase 2.15*103The power consumption of kw,
Heat pump heat supply coefficient COP can achieve 10 or more, therefore energy-saving effect is obvious.
It using flow scheme of the present invention, compares traditional scheme (embodiment 2+ embodiment 4), reduces steam consumption
46.96t/h increases power consumption 2152*103Kwh, to increase certain power consumption, to reduce steam consumption, this is relatively cheap for electricity price
Area be very favorable.
It should be noted that do not change mass balance calculating using heat pump distillation, above-mentioned temperature, the difference of flow by
Simulation calculates error and causes.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Made any modifications, equivalent replacements, and improvements etc., should all be included in the protection scope of the present invention within mind and principle.
Claims (10)
1. the technique that a kind of dimethyl ether produces ethyl alcohol indirectly, which is characterized in that the technique is first to be with dimethyl ether and carbon monoxide
Feedstock carbonyl reaction prepares methyl acetate and acetic acid, and methyl acetate and acetic acid add hydrogen, product purification processing with hydrogen catalytic again
Alcohol product is obtained afterwards.
2. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as described in claim 1, which comprises the following steps:
1) it is sufficiently mixed after dimethyl ether and carbon monoxide preheating, forms hybrid reaction gas, carry out carbonyl into carbonylation reactor
Change reaction；
2) product after carbonylation is after heat recovery and utilization, and into gas-liquid separation device, liquid phase crude product enters crude tower,
Obtain the mixture of methyl acetate and acetic acid；
3) mixture and hydrogen of separator obtains methyl acetate and acetic acid are sufficiently mixed after preheating, and it is anti-to form mixing
Should gas, into hydrogenator carry out catalytic hydrogenation；
4) product that hydrogenator comes out is after heat recovery and utilization, and into gas-liquid separation device, liquid phase crude product is successively passed through slightly
Divide tower, methanol column and ethanol tower, obtains alcohol product.
3. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that in step 1), the carbonyl
Glycosylation reaction device is fixed bed reactors, and catalyst is provided in carbonylation reactor；The carbon monoxide and dimethyl ether
Molar ratio is 3~20.
4. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that in step 1), liquid is former
Expect that dimethyl ether and gas raw material carbon monoxide are distinguished after preheated device preheats mix, vaporize in vaporization tower, then through superheater
Enter carbonylation reactor after being heated to required temperature.
5. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that in step 2), product object
Material sequentially enters carbon monoxide preheater, dimethyl ether preheater after coming out from carbonylation reactor, step by step using waste heat to reaction
Material is heated, cooling subsequently into aerial cooler, gas-liquid separation, gaseous products discharge recycle after a part of indifferent gas into
Enter reaction system, liquid phase crude product removes crude tower.
6. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that in step 2), liquid phase is thick
Product enter crude tower, and the recycling of tower top fixed gas enters recycle system of reaction, and overhead extraction liquid circulation is mixed into dimethyl ether raw material, tower
Kettle liquid phase crude product is the mixture of methyl acetate and acetic acid, removes catalytic hydrogenation device.
7. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that in step 3), the vinegar
The mixture and hydrogen of sour methyl esters and acetic acid enter vaporization tower after preheating, and mixture is added at the top of the vaporization tower, hydrogen from
Tower top enters, and enters reaction gas superheater after being sufficiently mixed vaporization, be heated to entering after required reaction temperature hydrogenator into
Row catalytic hydrogenation.
8. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that described to add in step 4)
Product after hydrogen successively reacted gas superheater, circulating gas preheater, feed preheater, step by step using waste heat to reaction mass into
Row heating, gas-liquid separation cooling subsequently into aerial cooler, gaseous products discharge after a part of indifferent gas with raw hydrogen one
It rises and is recycled into reaction system, liquid phase crude product removes crude tower.
9. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 2, which is characterized in that in step 4), liquid phase is thick
Product enter crude tower, and tower top fixed gas removes exhaust emissions, and overhead extraction liquid complete methyl acetate raw material containing unreacted returns and adds
In hydrogen production device, tower reactor liquid phase crude product enters methanol column, and overhead extraction is methanol product, and tower reactor mixture enters ethanol tower together,
Overhead extraction alcohol product, tower reactor are heavy seeds.
10. a kind of technique that dimethyl ether produces ethyl alcohol indirectly as claimed in claim 9, which is characterized in that the methanol column uses
Heat pump distillation, heat pump distillation the following steps are included:
Methanol column use atmospheric distillation, tower top material steam after heat pump pressurizes as heat source respectively enter methanol tower reboiler and
Ethyl alcohol tower reboiler itself is condensed after vaporizing tower bottom recycle stock a part, and it is cold then to enter methanol column cooler together
But, last part flows back, and a part is produced as methanol product, and tower reactor obtains ethyl alcohol crude product and goes subsequent ethanol rectifying column smart
System；
Ethanol tower uses atmospheric distillation, and tower reactor reboiler heat source is provided by methanol column heat pump, and overhead extraction obtains alcohol product,
Tower reactor is heavy seeds.
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| CN111001431A (en) * | 2019-12-06 | 2020-04-14 | 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 |
| CN111777491A (en) * | 2020-07-16 | 2020-10-16 | 南京延长反应技术研究院有限公司 | Micro-interface reaction system and method for preparing ethanol from coal |
| CN111807926A (en) * | 2020-07-16 | 2020-10-23 | 南京延长反应技术研究院有限公司 | Reaction system and method for preparing ethanol from coal |
| CN112608232A (en) * | 2020-12-04 | 2021-04-06 | 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 |
| WO2022011865A1 (en) * | 2020-07-16 | 2022-01-20 | 南京延长反应技术研究院有限公司 | Reaction system and method for preparing ethanol using syngas |
| CN115197047A (en) * | 2022-08-22 | 2022-10-18 | 西南化工研究设计院有限公司 | Coupling reaction method for preparing ethanol from dimethyl ether |
| CN116410058A (en) * | 2021-12-29 | 2023-07-11 | 延长中科（大连）能源科技股份有限公司 | Process method for separating coal-based ethanol |
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