CN108299157A - A method of preparing ethyl alcohol using calcium carbide stove exhaust - Google Patents
A method of preparing ethyl alcohol using calcium carbide stove exhaust Download PDFInfo
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- CN108299157A CN108299157A CN201810081884.6A CN201810081884A CN108299157A CN 108299157 A CN108299157 A CN 108299157A CN 201810081884 A CN201810081884 A CN 201810081884A CN 108299157 A CN108299157 A CN 108299157A
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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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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/14—Handling of heat and steam
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1258—Pre-treatment of the feed
Abstract
The invention discloses a kind of methods preparing ethyl alcohol using calcium carbide stove exhaust, ethyl alcohol is prepared using calcium carbide stove exhaust, it is reacted by calcium carbide stove exhaust and generates hydrogen, hydrogen is purified again, reduce influence of the impurity to hydrogenation reaction in hydrogen, simultaneously by each state modulator of hydrogenation reaction, finally so that methyl acetate conversion ratio >=99.0%, ethanol selectivity >=99.0%.
Description
Technical field
The present invention relates to a kind of preparation method of ethyl alcohol, specifically a kind of side preparing ethyl alcohol using calcium carbide stove exhaust
Method.
Background technology
Carbon monoxide content is a kind of gas having very high utility value up to 70~80% in calcium carbide furnace gas.But due to stove
Gas is purified and is burnt up using, there are some more scabrous problems, furnace gas can only be vented by many calcium carbide manufacturers in method,
This processing mode had not only polluted environment but also had wasted valuable gas resource.China is in closed type calcium carbide furnace gas purification utilization at present
Aspect technology is still far from perfect, thus research and solve improve can in the flue gas cleaning utilization technology of national popularity, for
It realizes environmental protection, labour protection and realizes that energy recovery utilizes, reduces production cost, improves economy and environmental benefit, all
It has practical significance.
Ethyl alcohol is a kind of good solvent, can dissolve many inorganic matters and many organic matters of dissolving, therefore commonly use ethyl alcohol
Come dissolve phytochrome or in which medicinal ingredient, also commonly use ethyl alcohol as reaction solvent, make participation react organic matter with
Inorganic matter can dissolve, and increase contact area, improve reaction rate.
Ethyl alcohol can call in gasoline, as automobile-used dyestuff.It sells ethanol petrol and has 20 years history, ethanol petrol in the U.S.
It is known as E type gasoline, China using ethanol petrol is reconciled with 90% regular gasoline and 10% alcohol fuel.It can change
The performance and quality of kind oil product, reduce the discharges of major pollutant such as carbon monoxide, hydrocarbon.
The demand of China industrial ethyl alcohol is increased with annual 8~10% growth rate, and ethyl alcohol mainly passes through biology
Zymotechnique produces, and non-grain ethyl alcohol only accounts for 5% or so of ethyl alcohol production.In recent years, biology combustion is constantly lowered in state revenue
Expect that ethyl alcohol financial aid standard, grain alcohol manufacturing enterprise face huge loss risk.Stop the back of the body of development in grain alcohol
Under scape, China is furnace of calcium carbide with the limited deliverability of ethyl alcohol to alcohol fuel and the huge potential consumption demand of industrial alcohol
Tail gas prepares ethyl alcohol and brings the good market opportunity.
The present invention prepares ethyl alcohol using calcium carbide stove exhaust, on the one hand promotes the development of non-grain ethyl alcohol technology；On the other hand, it solves
The difficult problem of calcium carbide stove exhaust of having determined processing, for realizing that comprehensive utilization of energy, environmental protection have great significance.
Invention content
The present invention is intended to provide a kind of method preparing ethyl alcohol using calcium carbide stove exhaust, it is comprehensive effectively to solve calcium carbide stove exhaust
Utilizing question is closed, comprehensive utilization of energy is realized, promotes the development of non-grain ethyl alcohol technology.
The method that the present invention prepares ethyl alcohol using calcium carbide stove exhaust, includes the following steps：
Step 1：Pretreatment
Calcium carbide stove exhaust is first passed around into the tar in electrical tar precipitator removing calcium carbide stove exhaust, is added for one section by compressor
Compressed tail gas is sent into thick desulfurizing tower and top-down desulfuration solution counter current contacting after pressure, absorbs the H in calcium carbide stove exhaust2S、
HCN, then from thick desulfurizing tower, treated that calcium carbide stove exhaust is sent into two sections of compressor after gas-liquid separation pressurizes；
Calcium carbide stove exhaust is forced into 0.2~1.5MPa by one section of compressor；Calcium carbide stove exhaust is forced by two sections of compressor
1.6~3.0MPa.
The desulfuration solution is the mixed solution of one or both of anthraquinone disulphonate, double-core peptide cyanines cobalt sodium sulfonate,
It is arbitrary if ratio at two kinds.
Step 2：Gas conversion
It will be first fed into the first steam mixer through the pretreated calcium carbide stove exhaust of step 1, it is abundant with saturated vapor
It is sent into the first change furnace after mixing to be reacted, primary first-order equation gas is obtained；Primary first-order equation pneumatic transmission enters the second steam mixer and satisfies
It is mixed again with steam, the second change furnace is sent into after mixing and is reacted, secondary response gas is obtained；
The volume ratio of calcium carbide stove exhaust and saturated vapor is 1 in first steam mixer:4~8；Mixture temperature is 400
~500 DEG C.
The volume ratio of primary first-order equation gas and saturated vapor is 1 in second steam mixer:1.5~3.5.
Controlling reaction temperature is 350~420 DEG C in first change furnace, and pressure is 1.0~2.5MPa；Second change furnace internal control
Reaction temperature processed is 380~470 DEG C, and pressure is 2.0~4.0MPa.
Step 3：Fine de-sulfur
By the secondary response temperature degree that step 2 obtains be down to 50~120 DEG C, pressure be 0.2~0.6MPa after be sequentially sent to
Fine de-sulfur is carried out in desulfurizer one, desulfurizer two, obtains conversion gas；
Desulfurizer therefor is the mixing of one or more of iron oxide, lime, lime stone in desulfurizer one, if several
When ratio it is arbitrary；Desulfurizer therefor is one or more of mixing of zinc oxide, magnesia, activated carbon in desulfurizer two, if
Ratio is arbitrary when several.
Step 4：Decarburization, purification
It will be sent into CO after transformation air cooling that step 3 obtains2Absorption tower carries out washing decarburization, absorption tower using cleaning solution
Outlet carries out Pressure Swing Adsorption, obtains purification gas, is then fed into compressor pressurization；
The control of conversion gas cooling temperature is 50~100 DEG C.
The cleaning solution is that sterically hindered amines, methyl diethanolamine be one such or two kinds of mixing, when if two kinds
Ratio is arbitrary；A concentration of 30~75wt% of the cleaning solution.
H in the purification gas2Volumetric concentration is 99~100%, and gas pressure is 3.0~6.0MPa after compressor pressurization.
Step 5：Hydrogenation reaction
Purification gas after step 4 is pressurizeed is heated to 220~260 DEG C, is then fed into methyl acetate evaporator and is mixed
Gas, gaseous mixture, which enters, carries out hydrogenation reaction in reactor, obtain product ethyl alcohol.
Hydrogenation reaction carries out in the presence of catalyst and co-catalyst, the catalyst using copper and mickel as active component,
The mass ratio of nickel and copper is 1 in active component：15~20, active component quality accounts for the 10%~25% of catalyst gross mass；Institute
It is molybdenum, tin, cadmium, the combination of one or more of silver to state co-catalyst, if it is several when ratio it is arbitrary, co-catalyst quality is to urge
The 1%~5% of agent gross mass.
Reactor pressure is 3.0~6.0MPa.
The molar ratio of methyl acetate and hydrogen is 1 in gaseous mixture:3~8.
The present invention prepares ethyl alcohol using calcium carbide stove exhaust, is reacted by calcium carbide stove exhaust and generates hydrogen, then hydrogen is carried out
Purification reduces influence of the impurity to hydrogenation reaction in hydrogen, while by each state modulator of hydrogenation reaction, finally so that tumer
Ester conversion rate >=99.0%, ethanol selectivity >=99.0%.
Beneficial effects of the present invention are embodied in：
1, the present invention prepares ethyl alcohol using calcium carbide stove exhaust, effectively recycles calcium carbide stove exhaust, realizes resource circulation utilization, together
When promote the development of non-grain ethyl alcohol technology；
2, fine de-sulfur step of the present invention uses tandem desulfurizer, on the one hand improves desulfurization effect, on the other hand saves
Cost improves economy.
3, methyl acetate conversion ratio >=99.0% of the present invention, ethanol selectivity >=99.0% have broad application prospects.
Specific implementation mode
Below using calcium carbide stove exhaust, methyl acetate as primary raw material, ethyl alcohol, specific embodiment are prepared by the method for the invention
It is as follows：
Embodiment 1：
The method for preparing ethyl alcohol in the present embodiment using calcium carbide stove exhaust is as follows：
1, calcium carbide stove exhaust pre-processes
Calcium carbide stove exhaust is first passed around into the tar in electrical tar precipitator removing calcium carbide stove exhaust, is incited somebody to action for one section by compressor
Calcium carbide stove exhaust is forced into 0.2-0.6MPa, and compressed tail gas is sent into thick desulfurizing tower and top-down anthraquinone disulphonate desulfurization is molten
Liquid counter current contacting absorbs the H in calcium carbide stove exhaust2S, HCN, then from thick desulfurizing tower treated calcium carbide stove exhaust through gas-liquid point
It is forced into 1.6-2.0MPa from rear two sections of feeding compressor.
2, gas conversion
It will be first fed into the first steam mixer through the pretreated calcium carbide stove exhaust of step 1, body is pressed with saturated vapor
Product ratio 1:The ratio of 4-5 is sufficiently mixed, then is sent into the first change furnace after mixture temperature is adjusted to 400-420 DEG C and is carried out instead
It answers, controlling reaction temperature is 350-375 DEG C in the first change furnace, and pressure 1.0-1.5MPa obtains primary first-order equation gas；It is primary anti-
Pneumatic transmission is answered to enter the second steam mixer and saturated vapor by volume 1:The ratio of 1.5-2 mixes, and the second transformation is sent into after mixing
Stove is reacted, and controlling reaction temperature is 380-400 DEG C in the second change furnace, and pressure 2.0-3.0MPa obtains secondary response
Gas；
3, fine de-sulfur
By the secondary response temperature degree that step 2 obtains be down to 50-70 DEG C, pressure be 0.2-0.6MPa after be sequentially sent to desulfurization
Fine de-sulfur is carried out in slot one, desulfurizer two, obtains conversion gas；Desulfurizer therefor is iron oxide or lime in desulfurizer one；Desulfurization
Desulfurizer therefor is zinc oxide or magnesia in slot two.
4, decarburization, purification
It is sent into CO after the conversion gas that step 3 obtains is cooled to 50-70 DEG C2Absorption tower is 30- using mass concentration
The sterically hindered amines cleaning solution of 40wt% carries out washing decarburization, and absorption tower outlet carries out Pressure Swing Adsorption, obtains purification gas, carries
Density of hydrogen is 99.5% in pure gas, is then fed into compressor and is forced into 3.0-4.0MPa.
5, hydrogenation reaction
Purification gas after step 4 is pressurizeed is heated to 220-230 DEG C, is then fed into methyl acetate evaporator and is mixed
Gas, methyl acetate and hydrogen molar ratio are 1 in gaseous mixture:3-5, gaseous mixture, which enters, carries out hydrogenation reaction, reactor in reactor
Pressure 3.0-6.0MPa obtains product ethyl alcohol.Methyl acetate conversion ratio is 99.0%, ethanol selectivity 99.2%.
Hydrogenation reaction carries out in the presence of catalyst and co-catalyst, the catalyst using copper and mickel as active component,
The mass ratio of nickel and copper is 1 in active component：15~20, active component quality accounts for the 10%~25% of catalyst gross mass；Institute
It is molybdenum, tin, cadmium, the combination of one or more of silver to state co-catalyst, if it is several when ratio it is arbitrary, co-catalyst quality is to urge
The 1%~5% of agent gross mass.
Embodiment 2：
The method for preparing ethyl alcohol in the present embodiment using calcium carbide stove exhaust is as follows：
1, calcium carbide stove exhaust pre-processes
Calcium carbide stove exhaust is first passed around into the tar in electrical tar precipitator removing calcium carbide stove exhaust, is incited somebody to action for one section by compressor
Calcium carbide stove exhaust is forced into 0.8-1.2MPa, and compressed tail gas is sent into thick desulfurizing tower and top-down anthraquinone disulphonate desulfurization is molten
Liquid counter current contacting absorbs the H in calcium carbide stove exhaust2S, HCN, then from thick desulfurizing tower treated calcium carbide stove exhaust through gas-liquid point
It is forced into 2.2-2.6MPa from rear two sections of feeding compressor.
2, gas conversion
It will be first fed into the first steam mixer through the pretreated calcium carbide stove exhaust of step 1, body is pressed with saturated vapor
Product ratio 1:The ratio of 5-6 is sufficiently mixed, then is sent into the first change furnace after mixture temperature is adjusted to 420-450 DEG C and is carried out instead
It answers, controlling reaction temperature is 380-400 DEG C in the first change furnace, and pressure 1.0-1.5MPa obtains primary first-order equation gas；It is primary anti-
Pneumatic transmission is answered to enter the second steam mixer and saturated vapor by volume 1:The ratio of 2-2.5 mixes, and the second transformation is sent into after mixing
Stove is reacted, and controlling reaction temperature is 410-430 DEG C in the second change furnace, and pressure 2.0-3.0MPa obtains secondary response
Gas；
3, fine de-sulfur
By the secondary response temperature degree that step 2 obtains be down to 50-70 DEG C, pressure be 0.2-0.6MPa after be sequentially sent to desulfurization
Fine de-sulfur is carried out in slot one, desulfurizer two, obtains conversion gas；Desulfurizer therefor is iron oxide or lime in desulfurizer one；Desulfurization
Desulfurizer therefor is activated carbon or magnesia in slot two.
4, decarburization, purification
It is sent into CO after the conversion gas that step 3 obtains is cooled to 55-75 DEG C2Absorption tower is 45- using mass concentration
The methyl diethanolamine cleaning solution of 55wt% carries out washing decarburization, and absorption tower outlet carries out Pressure Swing Adsorption, obtains purification gas,
It is 99.3% to purify density of hydrogen in gas, is then fed into compressor and is forced into 4.5-5.5MPa.
5, hydrogenation reaction
Purification gas after step 4 is pressurizeed is heated to 235-245 DEG C, is then fed into methyl acetate evaporator and is mixed
Gas, methyl acetate and hydrogen molar ratio are 1 in gaseous mixture:3.5-5.5, gaseous mixture, which enters, carries out hydrogenation reaction in reactor, instead
Device pressure 3.0-6.0MPa is answered, product ethyl alcohol is obtained.Methyl acetate conversion ratio is 99.4%, ethanol selectivity 99.5%.
Hydrogenation reaction carries out in the presence of catalyst and co-catalyst, the catalyst using copper and mickel as active component,
The mass ratio of nickel and copper is 1 in active component：15~20, active component quality accounts for the 10%~25% of catalyst gross mass；Institute
It is molybdenum, tin, cadmium, the combination of one or more of silver to state co-catalyst, if it is several when ratio it is arbitrary, co-catalyst quality is to urge
The 1%~5% of agent gross mass.
Embodiment 3：
The method for preparing ethyl alcohol in the present embodiment using calcium carbide stove exhaust is as follows：
1, calcium carbide stove exhaust pre-processes
Calcium carbide stove exhaust is first passed around into the tar in electrical tar precipitator removing calcium carbide stove exhaust, is incited somebody to action for one section by compressor
Calcium carbide stove exhaust is forced into 1.3-1.5MPa, and compressed tail gas is sent into thick desulfurizing tower and top-down anthraquinone disulphonate and double-core
Peptide cyanines cobalt sodium sulfonate mixing desulfuration solution counter current contacting absorbs the H in calcium carbide stove exhaust2S, HCN, then from the processing of thick desulfurizing tower
Calcium carbide stove exhaust afterwards is sent into two sections of compressor and is forced into 2.8-3.6MPa after gas-liquid separation.
2, gas conversion
It will be first fed into the first steam mixer through the pretreated calcium carbide stove exhaust of step 1, body is pressed with saturated vapor
Product ratio 1:The ratio of 6-8 is sufficiently mixed, then is sent into the first change furnace after mixture temperature is adjusted to 450-500 DEG C and is carried out instead
It answers, controlling reaction temperature is 410-420 DEG C in the first change furnace, and pressure 1.0-1.5MPa obtains primary first-order equation gas；It is primary anti-
Pneumatic transmission is answered to enter the second steam mixer and saturated vapor by volume 1:The ratio of 2.5-3.5 mixes, and second is sent into after mixing and is become
It changes stove to be reacted, controlling reaction temperature is 440-460 DEG C in the second change furnace, and pressure 2.0-3.0MPa obtains secondary counter
It should gas；
3, fine de-sulfur
By the secondary response temperature degree that step 2 obtains be down to 50-70 DEG C, pressure be 0.2-0.6MPa after be sequentially sent to desulfurization
Fine de-sulfur is carried out in slot one, desulfurizer two, obtains conversion gas；Desulfurizer therefor is that iron oxide and lime stone mix in desulfurizer one
Object；Desulfurizer therefor is zinc oxide and magnesia mixture in desulfurizer two.
4, decarburization, purification
It is sent into CO after the conversion gas that step 3 obtains is cooled to 60-80 DEG C2Absorption tower is 60- using mass concentration
The methyl diethanolamine cleaning solution of 70wt% carries out washing decarburization, and absorption tower outlet carries out Pressure Swing Adsorption, obtains purification gas,
It is 99.3% to purify density of hydrogen in gas, is then fed into compressor and is forced into 5.2-6.0MPa.
5, hydrogenation reaction
Purification gas after step 4 is pressurizeed is heated to 250-260 DEG C, is then fed into methyl acetate evaporator and is mixed
Gas, methyl acetate and hydrogen molar ratio are 1 in gaseous mixture:6-7, gaseous mixture, which enters, carries out hydrogenation reaction, reactor in reactor
Pressure 3.0-6.0MPa obtains product ethyl alcohol.Methyl acetate conversion ratio is 99.7%, ethanol selectivity 99.8%.
Hydrogenation reaction carries out in the presence of catalyst and co-catalyst, the catalyst using copper and mickel as active component,
The mass ratio of nickel and copper is 1 in active component：15~20, active component quality accounts for the 10%~25% of catalyst gross mass；Institute
It is molybdenum, tin, cadmium, the combination of one or more of silver to state co-catalyst, if it is several when ratio it is arbitrary, co-catalyst quality is to urge
The 1%~5% of agent gross mass.
Claims (10)
1. a kind of method preparing ethyl alcohol using calcium carbide stove exhaust, it is characterised in that include the following steps：
Step 1：Pretreatment
Calcium carbide stove exhaust is first passed around into the tar in electrical tar precipitator removing calcium carbide stove exhaust, after one section of pressurization of compressor
Compressed tail gas is sent into thick desulfurizing tower and top-down desulfuration solution counter current contacting, absorbs the H in calcium carbide stove exhaust2S, HCN,
Then from thick desulfurizing tower, treated that calcium carbide stove exhaust is sent into two sections of compressor after gas-liquid separation pressurizes；
Step 2：Gas conversion
It will be first fed into the first steam mixer through the pretreated calcium carbide stove exhaust of step 1, be sufficiently mixed with saturated vapor
After be sent into the first change furnace and reacted, obtain primary first-order equation gas；Primary first-order equation pneumatic transmission enters the second steam mixer and is steamed with saturation
Vapour mixes again, and the second change furnace is sent into after mixing and is reacted, secondary response gas is obtained；
Step 3：Fine de-sulfur
By the secondary response temperature degree that step 2 obtains be down to 50~120 DEG C, pressure be 0.2~0.6MPa after be sequentially sent to desulfurization
Fine de-sulfur is carried out in slot one, desulfurizer two, obtains conversion gas；
Step 4：Decarburization, purification
It is sent into CO after the conversion gas that step 3 obtains is cooled to 50~100 DEG C2Absorption tower carries out washing decarburization using cleaning solution,
Absorption tower outlet carries out Pressure Swing Adsorption, obtains purification gas, is then fed into compressor pressurization；
Step 5：Hydrogenation reaction
Purification gas after step 4 is pressurizeed is heated to 220~260 DEG C, is then fed into methyl acetate evaporator and obtains gaseous mixture, mixes
Conjunction gas, which enters, carries out hydrogenation reaction in reactor, obtain product ethyl alcohol.
2. according to the method described in claim 1, it is characterized in that：
In step 1, calcium carbide stove exhaust is forced into 0.2~1.5MPa by one section of compressor；Two sections of compressor adds calcium carbide stove exhaust
It is depressed into 1.6~3.0MPa.
3. according to the method described in claim 1, it is characterized in that：
In step 1, the desulfuration solution is that the mixing of one or both of anthraquinone disulphonate, double-core peptide cyanines cobalt sodium sulfonate is molten
Liquid.
4. according to the method described in claim 1, it is characterized in that：
In step 2, the volume ratio of calcium carbide stove exhaust and saturated vapor is 1 in the first steam mixer:4~8；Mixture temperature is
400~500 DEG C；The volume ratio of primary first-order equation gas and saturated vapor is 1 in second steam mixer:1.5~3.5.
5. according to the method described in claim 1, it is characterized in that：
In step 2, controlling reaction temperature is 350~420 DEG C in the first change furnace, and pressure is 1.0~2.5MPa；Second change furnace
Interior controlling reaction temperature is 380~470 DEG C, and pressure is 2.0~4.0MPa.
6. according to the method described in claim 1, it is characterized in that：
In step 3, desulfurizer therefor is the mixing of one or more of iron oxide, lime, lime stone in desulfurizer one；Desulfurization
Desulfurizer therefor is one or more of mixing of zinc oxide, magnesia, activated carbon in slot two.
7. according to the method described in claim 1, it is characterized in that：
In step 4, the cleaning solution is that sterically hindered amines, methyl diethanolamine be one such or two kinds of mixing；It is described to wash
Wash a concentration of 30~75wt% of liquid.
8. according to the method described in claim 1, it is characterized in that：
In step 4, H in the purification gas2Volumetric concentration be 99~100%, compressor pressurization after gas pressure be 3.0~
6.0MPa。
9. according to the method described in claim 1, it is characterized in that：
In step 5, hydrogenation reaction carries out in the presence of catalyst and co-catalyst, and the catalyst is using copper and mickel as activearm
Point, the mass ratio of nickel and copper is 1 in active component：15~20, active component quality accounts for the 10%~25% of catalyst gross mass；
The co-catalyst is molybdenum, tin, cadmium, the combination of one or more of silver, co-catalyst quality be catalyst gross mass 1%~
5%.
10. according to the method described in claim 1, it is characterized in that：
In step 5, the molar ratio of methyl acetate and hydrogen is 1 in gaseous mixture:3~8.
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