CN109200770A - The processing method of butane oxidation cis-butenedioic anhydride tail gas - Google Patents
The processing method of butane oxidation cis-butenedioic anhydride tail gas Download PDFInfo
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Abstract
A kind of processing method of butane oxidation cis-butenedioic anhydride tail gas, separates tail gas by membrane reactor, and the film in membrane reactor is cellulose acetate film, and membrane aperture is 0.1um~0.3um, and internal diameter is 0.4mm~0.8mm, and wall thickness is 0.1mm~0.3mm；Passing through toluene, methyl iso-butyl ketone (MIBK) and three stage of distilled water immersion treatment respectively using preceding.The membrane reactor of specially treated is utilized in exhaust gas treating method of the invention, eliminate the molecular weight polymers impurity in membrane module, keep membrane module pore-size distribution more uniform, active principle and impurity in tail gas can be efficiently separated, is more advantageous to the enrichment for seeping butane-component in residual air；The present invention also has the advantages that equipment investment expense is low, service life is long, easy to operate, low energy consumption.
Description
Technical field
The present invention relates to the processing methods of butane oxidation cis-butenedioic anhydride tail gas.
Background technique
Maleic anhydride (cis-butenedioic anhydride, MA) also known as maleic anhydride are a kind of particularly important Organic Chemicals, consumption figure
It is only second to phthalic anhydride and aceticanhydride.Cis-butenedioic anhydride is very widely used, mainly for the production of unsaturated polyester resin (UPR), 1,4-butanediol
(BDO), the series such as coating resin, span polyimides, tetrahydrofuran (THF), gamma-butyrolacton, maleic acid and tetrahydro acid anhydrides essence
The raw material of thin chemicals and textile auxiliary, lube oil additive, medicine, food additives etc..Wherein, cis-butenedioic anhydride is maximum
Purposes be production UPR and BDO, account for about the 41.7% and 17.4% of total quantity consumed respectively.Cis-butenedioic anhydride 2012 annual output in China's reaches about
800kt increased 5 times than 2000.The nearly 400kt/a of production capacity will be increased newly to the end of the year 2014.
The production process route of cis-butenedioic anhydride can be divided into phthalic anhydride by-product method, benzene oxidatoin method, C by its raw material4Olefin oxidation method, just
4 kinds of butane oxidation method.The maleic anhydride yield of phthalic anhydride plant by-product is very limited, only accounts for the 5% of phthalic anhydride by-product yield, 60 years 20th century
Before generation, cis-butenedioic anhydride is produced through catalysis oxidation as raw material using benzene and is in the great majority.But since benzene catalytic oxidation technique generates sternly environment
Heavily contaminated, the utilization rate of benzene is low in addition and price is higher and higher, is ground with raw material cheap, that pollution is small to produce the technique of cis-butenedioic anhydride
Hair becomes hot spot concerned by people.
In the early 1960s, starting with the C of low cost4Fraction (mainly containing n-butene) is that raw material produces the new of cis-butenedioic anhydride
Technical study, but since certain embodiments belong to the endothermic reaction and by-product is more, cause technology development to delay.1974, beauty
On original benzene method process units, it is raw for raw material to use normal butane instead in succession for Monsanto company of state and Texas oil company
It produces cis-butenedioic anhydride and obtains success, then, U.S. Ha Kang (Halcon) company and scientific design technology (SD) company have developed jointly just
The new catalyst and production technology of butane oxidation cis-butenedioic anhydride so that preparing cis-anhydride by n-butane oxidation new technology obtain it is more rapid
Development.
The rate constant of the reaction of preparing cis-anhydride by n-butane oxidation is K=11.44 × 105exp (- 7180/T), studies have shown that
(VO) in the catalyst2P2O7A V atom and ligand hole on (020) crystal face of object phase, another V atom and offer alkene
The active O atom bonding of propyl forms (VO) since V2O2 and P2OX is combined2P2O7When, an O atom is lacked in structure and is caused
(VO)2P2O7(020) malformation of crystal face forces the position V-O to reverse or adjust bond strength, is formed by coordination chemistry
High activity V-V ion pair.V-V bond length is 0.333nm, exactly corresponds to C in normal butane1And C3Bond length between atom and H original,
To illustrate in catalyst (VO)2P2O7Effect of the object with respect to normal butane and V2O5-P2OXBetween interaction.
In butane oxidation cis-anhydride production process, the conversion ratio of normal butane about 82% is unreacted containing 18% in tail gas
Normal butane is said from angle of cutting down the consumption of raw materials is recycled, and unreacted normal butane should be isolated from tail gas, is recycled to reaction system
System recycles.But also containing carbon monoxide, acrylic acid, acetic acid, solvent etc., at belonging to, toxic, burn into is inflammable in tail gas
Explosive medium.If tail gas is not handled well, into blower inlet, it is recycled, is situated between in tail gas containing water, acid etc.
Matter, it will the leaf of the air blower equipment such as fall are caused to corrode, drastically influence the operational safety of device.
In butane oxidation maleic anhydride production, the method for tail gas separation recycling normal butane has absorption process, condensation method and absorption
Method etc.: 1) absorption process: absorption process is that the characteristic of special solvent (or solution of addition chemical agent) is dissolved in using a certain tail gas
A kind of method handled；2) condensation method: condenser can be made it through for high-content tail gas, available gas is dropped
As low as boiling point hereinafter, condensing into liquid with recycling and reusing；3) absorption method: absorption method is that have using certain from gas phase mixture
In adsorb the porous solid (adsorbent) of certain component abilities selectively to remove a kind of method of impurity in tail gas.At present
To handle the active charcoal of the most common adsorbent of impurity in tail gas and activated carbon fiber, device used is valve transfer formula two
Bed (or more) absorber.
" chemical industry and engineering technology " the 4th phase of volume 23 in 2006 reports n butane oxidation production cis-butenedioic anhydride vent gas treatment
Technology, with the tail gas of flame combustion formula oxidator method processing butane oxidation cis-butenedioic anhydride, main body is incinerator, including burning
Device, mixing section, burning zone and exhaust section generate steam equipped with waste heat boiler recycling heat.Such method is to butane oxidation system
A kind of processing method of cis-butenedioic anhydride tail gas, and do not achieve the purpose that recycling.
" petrochemical technology and application " the 1st phase of volume 32 in 2014 reports n butane oxidation method maleic anhydride production work
Skill tail gas recycles, and the principle of exhaust gas circulation process is by processes such as cooling, separation, washings by reactive absorption tower tail gas
The impurity such as solvent, acrylic acid, acetic acid, the water of middle entrainment separation, to recycle the complete normal butane of wherein unreacted.The method work
Skill process complexity and high production cost, in addition can generate a large amount of scrub raffinate, pollute environment.
To sum up, the generally existing complex technical process of method in the prior art and the shortcomings that high production cost, and butane is pure
Rate is low, in the prior art without using film come the technical solution of separating treatment butane oxidation cis-butenedioic anhydride tail gas.
Summary of the invention
To solve butane oxidation cis-butenedioic anhydride tail gas in the prior art, there are complex treatment process, at high cost and vent gas treatment effect
Fruit problem not up to standard, the present invention is quasi- to provide a kind of processing method of butane oxidation cis-butenedioic anhydride tail gas, with limited means process film
Component simultaneously controls operating condition to tail gas progress separating treatment, and the isolated higher butane-component of purity can direct circulation benefit
With.
To realize the above-mentioned technical purpose, the present invention uses following technological means:
The present invention provides the processing methods of butane oxidation cis-butenedioic anhydride tail gas, comprising the following steps: leads to after tail gas is dehydrated dedusting
It crosses membrane reactor and carries out UF membrane, the operating condition of UF membrane are as follows: pressure 0.5MPa~1.0MPa, 40 DEG C~100 DEG C of temperature, into
Gas velocity degree 0.1m/s~5.0m/s is obtained rich in carbon monoxide, propionic acid, acetic acid, solvent, the infiltration gas of vapor and rich in butane
The infiltration residual air of gas, nitrogen；
Wherein, the film in the membrane reactor be cellulose acetate film, membrane aperture be 0.1um~0.3um, internal diameter be 0.4mm~
0.8mm, wall thickness are 0.1mm~0.3mm；
The membrane reactor is handled in the following manner using preceding:
8h~for 24 hours is first impregnated at 40 DEG C~80 DEG C with toluene, then impregnated at 40 DEG C~60 DEG C with methyl iso-butyl ketone (MIBK) 4h~
12h, then immersion treatment is carried out using oxygen content≤5mg/L distilled water in three stages: first stage treatment conditions is pressure
0.5MPa~0.8Mpa, temperature 60 C~75 DEG C, soaking time 8h~for 24 hours；Second stage treatment conditions be pressure 0.9MPa~
1.5Mpa, 85 DEG C~100 DEG C of temperature, soaking time 12h~for 24 hours；Phase III treatment conditions are pressure 1.3MPa~1.5Mpa,
120 DEG C~150 DEG C of temperature, soaking time 12h~48h；Above three stage is passed through inert gas or nitrogen simultaneously, finally carries out
It is dry.
In above-mentioned processing method, it will be apparent to a skilled person that in the butane oxidation cis-butenedioic anhydride tail gas
Containing the complete butylene of unreacted, recoverable carries out reproduction, but wherein also containing water, carbon monoxide, nitrogen, oxygen,
The impurity such as carbon dioxide, acetic acid, propionic acid, cis-butenedioic anhydride, each component content is different because of respective process distinction in tail gas, to make
Those skilled in the art are more fully understood by the present invention, and processing method of the present invention is particularly suitable for following impurity content
Exhaust gas treating method: by weight, water content 1.0%-10.0%, carbon monoxide content 0.5%-3.0%, nitrogen content is
65.0%-85.0%, oxygen content 5.0%-25.0%, carbon dioxide content 0.5%-3.5%, acetic acid content 0.001%-
0.1%, propionic acid content 0.001%-0.05%, cis-butenedioic anhydride content are 0.001%-0.05%, and surplus is butane.Wherein preferred group
Cheng Shi: by weight, water content 3.0%-7.0%, carbon monoxide content 0.5%-2.5%, nitrogen content 70.0%-
80.0%, oxygen content 10.0%-20.0%, carbon dioxide content 0.5%-2.0%, acetic acid content 0.001%-0.10%, third
Acid content is 0.01%-0.05%, and cis-butenedioic anhydride content is 0.001%-0.02%, and surplus is butane.And it should be strongly noted that above-mentioned
The tail gas of composition is handled using method of the invention, available more preferably separating resulting, in the gas after making separation
Butane content meets the requirement as feedstock circulation reproduction, and impurity therein is substantially achieved removal, will not influence technological reaction,
And it is not to say that the tail gas except this composition and is unsuitable for being handled with the method.
In above-mentioned processing method, the dehydration dedusting is to remove all diameters the consolidating greater than 0.01 μm carried secretly in tail gas
Body particle, water mist and aerosol, micronic dust content≤0.01mg/Nm in the tail gas that makes that treated3, water content≤1PPm.Processing side
Method is known to the skilled person, such as inertial dust collection method, wet dedusting method, Cottrell process, filtering type process of cleaning, monotubular rotation
Wind process of cleaning, multi-cyclone process of cleaning, centrifugal force separate, gravitational settling, baffling separation, silk screen separation, ultra-filtration and separation and filler
Separation etc., preferably centrifugal force separate, filtering type process of cleaning.
In above-mentioned processing method, tail gas can make tail by Pneumatic booster pump or gas-booster before being passed through membrane separator
Gas is pressurized to required pressure；Exhaust temperature is set to be down to required temperature by heat exchange mode, heat exchange mode includes various hybrid, storages
Hot type or dividing wall type heat exchanger, preferably dividing wall type heat exchanger, wherein dividing wall type heat exchanger can be jacket type, tubular type, it is board-like or
The custom design heat exchanger of various abnormal shape heat-transfer area compositions；The type of flow of the cold fluid and hot fluid in heat exchanger include fair current, adverse current,
Hand over stream, mixed flow again, preferably adverse current.
In above-mentioned processing method, as a further preference, the operating condition of the UF membrane are as follows: pressure 0.5MPa~
0.8MPa, temperature 50 C~80 DEG C, intake velocity be 0.1m/s~4.0m/s, wherein intake velocity be more preferably 0.1m/s~
3.0m/s。
In above-mentioned processing method, as a further preference, the temperature that toluene carries out immersion treatment to membrane reactor is
40 DEG C~60 DEG C, the time is 10h~20h；The temperature that methyl iso-butyl ketone (MIBK) carries out immersion treatment to membrane reactor is 40 DEG C~50
DEG C, the time is 4h~8h.
In above-mentioned processing method, as a further preference, the distilled water oxygen content impregnated to membrane module is preferred
≤ 3mg/L, more preferably≤1mg/L(is in terms of under the conditions of 20 DEG C, 100kPa).
In above-mentioned processing method, as a further preference, the three phases of distilled water immersion are carried out to membrane reactor
The flow velocity for being passed through inert gas or nitrogen is respectively 20m3/ h~25m3/h、10m3/ h~15m3/ h and 5m3/ h~8m3/h。
In above-mentioned processing method, immersion of the present invention is subject to liquid and there completely was not membrane module.
In above-mentioned processing method, the membrane reactor includes shell and membrane module, and membrane module is arranged in shell, in shell
One end of body and membrane module are equipped with gas inlet parallel, are equipped with parallel in the other end and membrane module of shell and seep residual air outlet, shell
Body side surface, which is equipped with, seeps vent outlet.
After above-mentioned vent gas treatment, obtain rich in carbon monoxide, propionic acid, acetic acid, solvent, vapor infiltration gas and
Infiltration residual air rich in butagas, nitrogen seeps residual air and returns to the butane oxidation stage as raw material, and permeating gas can further recycle respectively
Component.
Compared with prior art, butane oxidation cis-butenedioic anhydride exhaust gas treating method of the invention has the advantage that
1. the present invention membrane reactor is impregnated under given conditions with toluene and methyl iso-butyl ketone (MIBK), stage by stage with water into
The mode of row processing, eliminates the molecular weight polymers impurity in membrane module, keeps membrane module pore-size distribution more uniform, more favorably
In the enrichment for seeping butane-component in residual air.
2. butane oxidation cis-butenedioic anhydride exhaust gas treating method of the invention has equipment investment expense compared with other techniques
Low, the advantages of service life is long, easy to operate, low energy consumption；Membrane reactor gas separation selectivity after specially treated is good,
Separative efficiency is high, effectively excludes impurity acetic acid, propionic acid, cis-butenedioic anhydride and the moisture in tail gas, active principle butane contains in tail gas
Amount is promoted to 1.60% or more by 1.1, fully meets the requirement that direct circulation is used as raw material, and entire technique does not produce
Raw secondary pollution.
Other features and advantages of the present invention will the following detailed description will be given in the detailed implementation section.
Detailed description of the invention
The concrete technology flow process figure of butane oxidation cis-butenedioic anhydride tail gas is handled used in Fig. 1 embodiment；
The structural schematic diagram of Fig. 2 membrane reactor；
Wherein 1. gas centrifuge, 2. gas-boosters I, 3. high pressure storage tanks, 4. active carbon filters, 5. contra-flow heat exchangers, 6.
Accurate filter, 7. membrane reactors, 8. gas-boosters II, 9. gas inlets, 10. seep vent outlet, 11. membrane modules, 12. shells
Body, 13. seep residual air outlet, 14. pipelines I, 15. pipelines II, 16. pipelines III.
Specific embodiment
Following non-limiting embodiments can with a person of ordinary skill in the art will more fully understand the present invention, but not with
Any mode limits the present invention.
In the examples below, be all made of technological process device shown in FIG. 1 to butane oxidation cis-butenedioic anhydride tail gas at
Reason, the room temperature tail gas from butane oxidation technique first passes through gas centrifuge 1, it is preliminary remove the solid particle carried in tail gas and
Water, then 0.5MPa~1.0Mpa is pressurized to by gas-booster I 2, it is further through active carbon filter 4 into high pressure storage tank 3
It is dehydrated dedusting, then makes exhaust temperature up to 50 DEG C~80 DEG C after the heat exchange of counter-current pipe exchanger 5, again through accurate filter 6
Micronic dust content≤0.01mg/Nm is obtained after removing solid particle of all diameters greater than 0.01 μm3, water content≤1PPm enters film
It is anti-to enter film under conditions of pressure 0.5MPa~1.0MPa, temperature 50 C~80 DEG C, intake velocity 0.1m/s~5.0m/s for gas
Device 7 is answered, purified infiltration residual air is isolated and concentrates the infiltration gas of impurity.Residual air is wherein seeped from residual air outlet is seeped through pipeline II
15 draw return butane oxidation device, and partial penetration gas returns to activity by gas-booster II 8 and pipeline III 16 through pipeline I 14
Carbon filter 4, another part permeate the recycling that gas carries out acrylic acid, acetic acid, solvent.
Fig. 2 is membrane reactor structural schematic diagram used in the embodiment of the present invention.Membrane reactor has shell 12, in shell
Equipped with membrane module 11, it is equipped with gas inlet 9 parallel in one end of shell 12 and membrane module 11, in the other end and film group of shell 12
Part 11 is equipped with parallel seeps residual air outlet 13, and housing side, which is equipped with, seeps vent outlet 10.Tail gas is in membrane module internal flow, as slow
The butane-component of gas walks membrane module tube side and is seeped 13 discharge of residual air outlet, and the impurity gas as fast gas appears membrane module through permeating gas
10 discharge of outlet.The material that the membrane module uses is cellulose acetate film, membrane aperture 0.1um-0.3um, internal diameter 0.4mm-
0.8mm, wall thickness 0.1mm-0.3mm.
Film parameters used in embodiment are shown in Table 1, and the composition of used butane oxidation device exhaust is listed in table 2.
Table 1
Table 2
% in following embodiment is weight percentage unless otherwise specified.
Embodiment 1
Using butane oxidation device exhaust listed by table 2 as raw material, the solid carried in tail gas is tentatively removed through gas centrifuge 1
After grain and water, enter high pressure storage tank 3 after being pressurized to 0.5MPa by gas-booster I 2；It is further taken off through active carbon filter 4
Water dedusting, micronic dust content is 0.007mg/Nm in treated tail gas3, water content 0.6PPm, then through shell and tube counterflow heat exchange
Device 5 makes exhaust temperature up to 50 DEG C after exchanging heat, and membrane reactor 7 is entered under conditions of pressure 0.6MPa, intake velocity 0.6m/s, point
Separate out the infiltration residual air rich in butane and the infiltration gas containing acetic acid, propionic acid, cis-butenedioic anhydride and moisture.It seeps residual air and is sent into butane oxidation device
Raw material as synthesis cis-butenedioic anhydride；It permeates gas and adsorbs laggard one-step removal butane therein as backflow gas pressurization through different adsorbents
Membrane separator 7 is returned afterwards to continue to purify；Another part permeates the recycling that gas carries out acetic acid, propionic acid, cis-butenedioic anhydride.It seeps residual air and forms result
It is shown in Table 3.
Embodiment 2
According to the method for embodiment 1, high pressure storage tank 3 will be only entered after gas boosting to 0.8MPa；Through active carbon filter 4 into
One step is dehydrated dedusting, and micronic dust Content is 0.007mg/Nm in treated tail gas3, water content 0.6PPm countercurrently changed
Hot device 5 makes exhaust temperature up to 60 DEG C after exchanging heat, and membrane reactor 7 is entered under conditions of pressure 0.8MPa, intake velocity 3m/s, point
Separate out the infiltration residual air rich in butane and the infiltration gas containing acetic acid, propionic acid, cis-butenedioic anhydride and moisture.It seeps residual air and is sent into butane oxidation device
Raw material as synthesis cis-butenedioic anhydride；It permeates gas and adsorbs laggard one-step removal butane therein as backflow gas pressurization through different adsorbents
Membrane separator 7 is returned afterwards to continue to purify；Another part permeates the recycling that gas carries out acetic acid, propionic acid, cis-butenedioic anhydride.It seeps residual air and forms result
It is shown in Table 3.
Embodiment 3
According to the method for embodiment 1, high pressure storage tank 3 will be only entered after gas boosting to 1.0MPa；Make through active carbon filter 4
Obtaining micronic dust content in tail gas is 0.01mg/Nm3, water content is that 0.5PPm enters film gas, makes tail gas after the heat exchange of contra-flow heat exchanger 5
Temperature enters membrane reactor 7 under conditions of pressure 0.6MPa, intake velocity 5.0m/s, isolates rich in butane up to 60 DEG C
Seep residual air and the infiltration gas containing acetic acid, propionic acid, cis-butenedioic anhydride and moisture.It seeps residual air and is sent into butane oxidation device as synthesis cis-butenedioic anhydride
Raw material；Infiltration gas returns to membrane separator after different adsorbents adsorb laggard one-step removal butane therein as backflow gas pressurization
7 continue to purify；Another part permeates the recycling that gas carries out acetic acid, propionic acid, cis-butenedioic anhydride.Seeping residual air composition the results are shown in Table 3.
Embodiment 4
Following processing has been carried out to membrane module 11: membrane module 11 being impregnated into 10h at a temperature of 40 DEG C with toluene, then uses methyl again
Isobutyl ketone impregnates 8h at 50 °C, and above-mentioned membrane module is carried out in the distillation moisture three phases of oxygen content 1mg/L again
Processing: first stage treatment conditions are pressure 0.5MPa, impregnate 8h under temperature 60 C, and immersion while is passed through nitrogen, and flow velocity is
20m3/h；Second stage treatment conditions are pressure 0.9MPa；It is impregnated for 24 hours at 100 DEG C of temperature, immersion while is passed through nitrogen, flows
Speed is 15m3/h；Phase III treatment conditions are pressure 1.5MPa；Impregnate 12h at 120 DEG C of temperature, immersion while is passed through nitrogen
Gas, flow velocity 5m3/ h, the dry membrane module being made for butane oxidation tail gas clean-up of after treatment.
According to the condition of embodiment 1, with treated above, membrane module is used for vent gas treatment.Seeping residual air composition the results are shown in Table
3。
Embodiment 5
Following processing has been carried out to membrane module 11: membrane module is impregnated into 20h at a temperature of 60 DEG C with toluene, it is then different with methyl again
Butyl ketone impregnates 4h at a temperature of 60 DEG C.By above-mentioned membrane module again at the distillation moisture three phases of oxygen content 2mg/L
Reason: first stage treatment conditions are pressure 0.8Mpa, are impregnated for 24 hours at 75 DEG C of temperature, and immersion while is passed through nitrogen, and flow velocity is
25m3/h；Second stage treatment conditions are pressure 1.0MPa；Impregnate 12h at 85 DEG C of temperature, immersion while is passed through nitrogen, flow velocity
For 10m3/h；Phase III treatment conditions are pressure 1.3MPa；Impregnate 48h at 150 DEG C of temperature, immersion while, is passed through nitrogen,
Flow velocity is 8m3/ h, the dry membrane module being made for butane oxidation tail gas clean-up of after treatment.
According to the condition of embodiment 2, with treated above, membrane module is used for vent gas treatment.Seeping residual air composition the results are shown in Table
3。
Embodiment 6
Following processing has been carried out to membrane module 11: membrane module is impregnated into 12h at a temperature of 80 DEG C with toluene, it is then different with methyl again
Butyl ketone impregnates 4h at 50 DEG C.Above-mentioned membrane module is handled in the distillation moisture three phases of oxygen content 1mg/L again: the
One step processing conditions are pressure 0.6MPa；Impregnate 10h at 65 DEG C of temperature, immersion while is passed through nitrogen, flow velocity 22m3/h；
Second stage treatment conditions are pressure 1.0MPa；Impregnate 16h at 90 DEG C of temperature, immersion while is passed through nitrogen, flow velocity 12m3/
h；Phase III treatment conditions are pressure 1.5MPa；It is impregnated for 24 hours at 130 DEG C of temperature, immersion while is passed through nitrogen, and flow velocity is
6m3/ h, the dry membrane module being made for butane oxidation tail gas clean-up of after treatment.
According to the method for embodiment 3, with treated above, membrane module is used for vent gas treatment.Seeping residual air composition the results are shown in Table
3。
Table 3
From table 3 it can be seen that butane oxidation device exhaust is after the purification of not pretreated membrane separator, active principle in tail gas
Butane content still contains the impurity such as a small amount of acetic acid, propionic acid and cis-butenedioic anhydride 1.1% or so, and passes through pretreated UF membrane
After device purification, impurity acetic acid, propionic acid, cis-butenedioic anhydride and moisture in tail gas have obtained effective exclusion, active principle butane in tail gas
Content is 1.60% or more, can be used as the raw material of synthesis cis-butenedioic anhydride workshop section completely, has reached the requirement being recycled.
Claims (8)
1. the processing method of butane oxidation cis-butenedioic anhydride tail gas, comprising the following steps: pass through membrane reactor after tail gas is dehydrated dedusting
Carry out UF membrane, the operating condition of UF membrane are as follows: pressure 0.5MPa~1.0MPa, 40 DEG C~100 DEG C of temperature, intake velocity
0.1m/s~5.0m/s is obtained rich in carbon monoxide, propionic acid, acetic acid, solvent, the infiltration gas of vapor and rich in butagas, nitrogen
The infiltration residual air of gas；
Wherein, the film in the membrane reactor be cellulose acetate film, membrane aperture be 0.1um~0.3um, internal diameter be 0.4mm~
0.8mm, wall thickness are 0.1mm~0.3mm；
The membrane reactor is handled in the following manner using preceding:
8h~for 24 hours is first impregnated at 40 DEG C~80 DEG C with toluene, then impregnated at 40 DEG C~60 DEG C with methyl iso-butyl ketone (MIBK) 4h~
12h, then immersion treatment is carried out using oxygen content≤5mg/L distilled water in three stages: first stage treatment conditions is pressure
0.5MPa~0.8Mpa, temperature 60 C~75 DEG C, soaking time 8h~for 24 hours；Second stage treatment conditions be pressure 0.9MPa~
1.5Mpa, 85 DEG C~100 DEG C of temperature, soaking time 12h~for 24 hours；Phase III treatment conditions are pressure 1.3MPa~1.5Mpa,
120 DEG C~150 DEG C of temperature, soaking time 12h~48h；Above three stage is passed through inert gas or nitrogen simultaneously, finally carries out
It is dry.
2. processing method according to claim 1, which is characterized in that the operating condition of the UF membrane are as follows: pressure
0.5MPa~0.8MPa, temperature 50 C~80 DEG C, intake velocity are 0.1m/s~4.0m/s.
3. processing method according to claim 2, which is characterized in that the intake velocity of the UF membrane be 0.1m/s~
3.0m/s。
4. processing method according to claim 1, which is characterized in that toluene carries out the temperature of immersion treatment to membrane reactor
It is 40 DEG C~60 DEG C, the time is 10h~20h.
5. processing method according to claim 1, which is characterized in that methyl iso-butyl ketone (MIBK) carries out at immersion membrane reactor
The temperature of reason is 40 DEG C~50 DEG C, and the time is 4h~8h.
6. processing method according to claim 1, which is characterized in that carry out three ranks of distilled water immersion to membrane reactor
It is respectively 20m that section, which is passed through inert gas or the flow velocity of nitrogen,3/ h~25m3/h、10m3/ h~15m3/ h and 5m3/ h~8m3/h。
7. processing method according to claim 1, which is characterized in that micronic dust in the dehydration dedusting makes that treated tail gas
Content≤0.01mg/Nm3, water content≤1PPm.
8. processing method according to claim 1, which is characterized in that the composition of the tail gas are as follows: by weight, water content
For 1.0%-10.0%, carbon monoxide content 0.5%-3.0%, nitrogen content 65.0%-85.0%, oxygen content 5.0%-
25.0%, carbon dioxide content 0.5%-3.5%, acetic acid content 0.001%-0.1%, propionic acid content 0.001%-0.05% are suitable
Acid anhydride content is 0.001%-0.05%, and surplus is butane.
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| CN111140862A (en) * | 2019-12-27 | 2020-05-12 | 安徽海德化工科技有限公司 | High-purity n-butane production device |
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Effective date of registration: 20230921 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |