CN108855168A - A kind of preparation method of phosgene decomposition catalyst - Google Patents
A kind of preparation method of phosgene decomposition catalyst Download PDFInfo
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- CN108855168A CN108855168A CN201810749852.9A CN201810749852A CN108855168A CN 108855168 A CN108855168 A CN 108855168A CN 201810749852 A CN201810749852 A CN 201810749852A CN 108855168 A CN108855168 A CN 108855168A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/20—Carbon compounds
- B01J27/22—Carbides
- B01J27/224—Silicon carbide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8678—Removing components of undefined structure
- B01D53/8687—Organic components
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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
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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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
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
- C01B7/035—Preparation of hydrogen chloride from chlorides
Abstract
The invention discloses a kind of preparation methods of phosgene decomposition catalyst, include the following steps：A, bamboo charcoal and silicon dioxide gel are mixed, is prepared into slurry；B, slurry obtained in a is dried in an oven, obtains pulvis；C, mixing powder is obtained after being mixed pulvis obtained in b with silicon carbide powder, dispersing agent, mixing powder is mixed with water again, and mixed slurry is made；D, binder is added into mixed slurry obtained in step c, be uniformly mixed, bonding slurry is made；E, slurry mist projection granulating will be bonded obtained in step d, obtain powder；F, step e medium silt is taken out, plasticiser is added, is mixed, obtains powder；G, powder is taken out, Al is added2O3, it is mixed, it is aging, obtain pug；H, aging rear pug extrusion molding, sintering obtain phosgene decomposition catalyst.The advantages that simple with the technological process of production, processing phosgene concentration is high, and the required residence time is short, by-product hydrochloric acid raising economy.
Description
Technical field
The present invention relates to a kind of preparation methods of efficient phosgene decomposition catalyst.
Technical background
Phosgene is a kind of irritative gas, and sucking easily causes pulmonary edema etc. to endanger.However phosgene is a kind of extremely important
Organic intermediate, all there are many purposes in pesticide, medicine, engineering plastics, polyurethane material and military affairs.In Chemical Manufacture
In the process, a large amount of exhaust gas containing phosgene can be generated, according to the difference of operating condition, phosgene concentration is different in tail gas.When normal operation, use
Phosgene concentration is generally in 10~1000mg/Nm in the product gas of phosgene3, during device driving and parking, such as in optical self-encoding
Workshop synthesizes start of run, is the incoagulable gas in exchange system, usually the tail gas containing phosgene is immediately discharged at tail gas
System destruction is managed, until the incoagulable gas displacement in system is complete, side imports phosgenation reaction process or phosgene liquefaction process,
The phosgene concentration being vented at this time reaches as high as 50000-100000mg/Nm3.It, need to be by the light in equipment when optical self-encoding furnace stops
Air-blowing just can be carried out maintenance after sweeping displacement completely, and concentration reaches as high as 1000000-2000000mg/ in the displacement gas being discharged at this time
Nm3.Phosgene direct emission will cause serious security risk, (need to be lower than 5mg/Nm through processing is qualified3) after could empty.It is common
Tail gas in phosgene destruction methods there is alkali cleaning to destroy method, catalytic decomposition etc..
Alkali wash refers to and uses NaOH solution or other lye as absorbing liquid, in packed tower or plate column and containing light
Tail-gas carries out acid-base neutralization reaction to destroy the phosgene in tail gas.There are acid-base neutralization heat releases seriously to lead to absorption tower for this method
It is difficult to stability contorting, reacts the deficiencies of a large amount of lye operating costs of consumption are high, when being chiefly used in emergency circumstances a large amount of phosgene leakage
Emergency measure.
The active charcoal of the common phosgene decomposition catalyst of catalytic decomposition, SN7501 etc..Active carbon in tail gas vulnerable to carrying secretly
Organic solvent (such as chlorobenzene, dichloro-benzenes) pollution, cause decomposition efficiency to reduce.Meanwhile the usual particle of active carbon is smaller, tower pressure drop
It is higher, need multitower to be used in series, and alkali cleaning must be set in final stage and protect tower more.SN7501 is that Shenyang Chemical Research Institute exists
The phosgene decomposition catalyst of exploitation in 1977, is a kind of skeleton surface catalysis membrane type sial type catalyst, has compared with active carbon lower
Tower pressure drop and higher catalytic activity, but decompose high concentration phosgene (such as concentration is in 2000000mg/Nm3Left and right) tail gas is extremely
Qualification needs the residence time longer, meanwhile, the catalytic activity of SN7501 is affected by temperature larger, and the thermal conductivity of catalyst itself
Can be bad, the amount of heat generated in decomposable process easily causes local tower temperature to increase, and resolution ratio is caused to reduce.In addition,
It is the hydrochloric acid no more than 5% as distintegrant that SN7501 catalyst, which generally uses concentration, decomposes a large amount of dilute hydrochloric acid disposition of generation
It is inconvenient.
Patent CN201410684532.1 discloses a kind of containing CO2、Cl2With the tail gas treatment process of the toxic gases such as phosgene
And device, the main absorbing liquid using the mixed aqueous solution of sodium thiosulfate and sodium hydroxide as sour gas, for low dense
It spends, the acid tail gas of low discharge has preferable treatment effect.But for high concentration, high flow capacity contain phosgene tail gas, because of thermal discharge
Cause greatly technique can not stability contorting, while quantity of alkali consumption is big, and disaggregated cost is high.
Patent CN201420216447.8 discloses a kind of optical self-encoding tail gas absorption processing unit, by falling-film tower, urges
Change the series design of tower, washing tower (for removing CO2), catalyst is SN7501 filler；Patent CN201610884886.X discloses a kind of alkali purification
Phosgene exhaust gas process, using the multi-stage treatment units such as solvent absorption, Diluted Acid Washing, SN7501 catalytic decomposition, alkali cleaning, processing stream
Journey is more complex；Patent CN201720137445.3 discloses a kind of phosgene tail gas processing unit, mainly uses SN7501 catalyst
Catalytic decomposition combines the treatment process of caustic wash tower, although catalytic decomposition part phosgene can reduce the consumption of lye, because
SN7501 catalytic decomposition generates a large amount of dilute hydrochloric acid, and no economic value still needs to further be concentrated.Meanwhile SN7501 catalyst pair
The decomposition of high concentration phosgene needs the longer residence time, i.e. equipment size is larger, to site requirements height.
The above patent combines the methods of alkali cleaning to decompose containing phosgene tail gas using alkali cleaning or catalytic decomposition, highly concentrated a large amount of handling
It is low that there are catalytic efficiencies when tail gas, and the required residence time is long, and equipment size is big, and alkali consumption is high, the economic valence of low concentrated hydrochloric acid of by-product
It is worth low deficiency, therefore a kind of efficient phosgene decomposition catalyst need to be developed.
Summary of the invention
High object of the present invention is to prepare a kind of decomposition efficiency, tower pressure drop is low, and the efficient of concentrated hydrochloric acid can be generated after decomposition
Phosgene decomposition catalyst absorbs efficient-decomposition of the decomposition technique realization to highly concentrated phosgene, tower bottom salt preferably in combination with multiple process phosgene
Acid, which is recycled in tower top and tower, decomposes phosgene, and preparation concentration has the by-product hydrochloric acid of economic value, simple production process, phosgene point
It is good to solve effect.
To achieve the above object, the preparation of a kind of phosgene decomposition catalyst provided by the present invention, includes the following steps：
A, by bamboo charcoal and silicon dioxide gel by certain mass ratio mixing, preferably through ultrasound and strength mechanical stirring, system
For at slurry；
B, slurry obtained in a is dried in an oven, obtains pulvis；
C, mixing powder is obtained after being mixed pulvis obtained in b with silicon carbide powder, dispersing agent, is mixed
Pulvis is closed again with water, and preferably for pure water by certain mass than mixing, mixed slurry is made in strength mechanical stirring；
D, a certain proportion of binder is added into mixed slurry obtained in step c, is uniformly mixed,
Bonding slurry is made；
E, slurry mist projection granulating will be bonded obtained in step d, obtain powder；
F, step e medium silt is taken out, certain proportion plasticiser is added, is mixed, obtains powder；
G, powder in step f is taken out, certain proportion Al is added2O3, it is mixed, it is aging, obtain pug；
H, pug extrusion molding after will be aging in step g, sintering obtain phosgene decomposition catalyst.
In the method for the present invention, the dioxide-containing silica of silicon dioxide gel described in step a is 15~41wt%, preferably 20
~25wt%.
In the method for the present invention, bamboo charcoal described in step a and silicon dioxide gel mixing quality ratio are 1:1~10:1, it is excellent
Select 2:1~6:1, more preferable 3:1~4:1.
In the method for the present invention, drying temperature described in step b be 100~200 DEG C, preferably 110~140 DEG C, more preferably
115-125℃.Drying time is 3-15h, preferably 5-10h, more preferable 6-8h.
In the method for the present invention, the mixing quality ratio of pulvis described in step c and silicon carbide powder is 2:1~8:1, preferably
3:1~7:1, more preferable 4:1~5:1.
In the method for the present invention, dispersing agent described in step c is one of alumina silicate, ammonium polymethacrylate, preferably silicon
The addition mass ratio of sour aluminium, dispersing agent and silicon carbide powder is 1:20~1:50, preferably 1:25~1:40, more preferable 1:30~
1:35。
In the method for the present invention, the addition mass ratio of mixing powder described in step c and pure water is 1:1~2:1, preferably
1.2:1~1.8:1, more preferable 1.4:1~1.6:1.
In the method for the present invention, binder described in step d be one of hydroxypropyl methyl cellulose, POLYPROPYLENE GLYCOL, it is excellent
Select hydroxypropyl methyl cellulose, the mass ratio of binder and mixed slurry is 1:20~1:60, preferably 1:30~1:50, it is more excellent
Select 1:35~1:45.The median particle diameter D50 control of manufactured bonding slurry is at 0.30~0.90 μm after stirring, preferably 0.40~
0.70 μm, more preferable 0.50~0.60 μm.
In the method for the present invention, the heating and temperature control of mist projection granulating described in step e at 150~200 DEG C, preferably 170~
180℃.Inlet air temperature is controlled at 100~120 DEG C, and preferably 105~110 DEG C.Leaving air temp control at 60~90 DEG C, preferably 70~
80℃.Pressure is controlled in 0.05~0.08MPaG, preferably 0.06~0.07MPaG.
In the method for the present invention, plasticiser described in step f is phthalic acid ester, preferably dibutyl phthalate, modeling
The mass ratio of agent and powder is 1:20~1:90, preferably 1:30~1:55, more preferably 1:35~1:45.
In the method for the present invention, Al described in step g2O3For nano particle, optional partial size is 20~100nm, preferably 25~
60nm, more preferable 30~40nm.
In the method for the present invention, powder described in step g and Al2O3Mass ratio optional 2:1~8:1, preferably 3:1~6:1,
More preferable 4:1~5:1.
In the method for the present invention, the aging optional 36~72h of duration, preferably 48~60h described in step g.
In the method for the present invention, extrusion molding described in step h is preferably cylindric, and cylinder height and cross-sectional dimension phase
Deng optional cylindric having a size of 5*5~30*30mm, preferably 8*8~20*20mm is cylindric, more preferable 10*10~15*15mm circle
Column.
In the method for the present invention, optional 1200~1800 DEG C of sintering temperature described in step h, preferably 1300~1600 DEG C, more
It is preferred that 1400~1500 DEG C.
In the method for the present invention, the sintering optional 40~100h of duration, preferably 50~80h, more preferable 60 described in step h~
70h。
Catalyst of the invention is used for the technique that phosgene decomposes：Catalyst uses two sections or more shapes in phosgene decomposition tower
Formula filling, preferably three sections fillings, the tail gas containing phosgene enter phosgene decomposition tower from bottom, and tower top is trapped using process water, light
Gas hydrolyzes under the catalytic action of catalyst to be generated hydrochloric acid and generates CO2Gas, tower bottom hydrochloric acid big flow circulation, is returned using multistage
It is flow to position in tower top or tower, is consistent with filling number of segment, the phosgene in decomposed tail gas generates concentrated hydrochloric acid, and small flow is adopted
It keeps balancing with technique water flow out.
In catalyst preparation process, CO gas overflowing is generated by bamboo charcoal and silicon dioxde reaction and generates hole abundant
The specific surface area of catalyst is improved in hole；The good thermal conductivity of SiC skeleton can quickly conduct reaction heat, avoid hot-spot, dimension
Hold higher phosgene resolution ratio；By high temperature sintering, by Al2O3It is fully converted to α-Al2O3Crystal form improves catalyst acid resistance.
The good effect of this method is：
The present invention provides a kind of preparation method of phosgene decomposition catalyst, has the technological process of production simple, handles phosgene
The advantages that concentration is high, and the required residence time is short, and by-product hydrochloric acid improves economy, can greatly improve the tail for relating to phosgene production device
Gas disposal ability and phosgene in emergency circumstances decompose emergency capability.Preferably, residence time item of the catalyst of preparation in 20s
Highest can decompose 2000000mg/Nm under part3The phosgene of concentration decomposes the hydrochloric acid that can produce 32% concentration, and phosgene decomposes in tail gas
Rate can reach 98.5% or more.
Detailed description of the invention
Fig. 1 is the phosgene decomposition tower structural schematic diagram that the specific embodiment of the invention uses.Wherein, 1：Phosgene decomposition tower；2：
Phosgene decomposition catalyst；3：Containing phosgene tail gas；4：Tail gas after processing；5：Supplement process water；6：Reflux cycle hydrochloric acid；7：By-product salt
Acid.
Specific embodiment
The present invention is further illustrated with embodiment below, but the present invention is not limited except as.Tool is not specified in the following example
The experimental method of concrete conditions in the establishment of a specific crime, usually according to normal condition.
Embodiment provided by the present invention is that light phosgenation prepares phosgene in methyl diphenylene diisocyanate process tail gas
Catalytic decomposition process.
Phosgene decomposition tower is three sections of packed towers, and phosgene decomposition catalyst is loaded in inside, and the tail gas containing phosgene enters from tower bottom,
Tower top is trapped using process water, the hydrochloric acid big flow circulation that tower bottom generates, using the phosgene in three sections of decomposed tail gas that flow back, control
The concentration of hydrochloric acid of tower bottom discharge is 32%, and small flow extraction keeps balancing with technique water flow.Deethanizer design diameter is 0.18m, high
1.0m, highly respectively 0.2m, 0.25m, 0.25m, two layers of the supportive grid upper berth in bottom silk screen, catalyst are total from top to bottom for filler
Need about 0.015m3。
Phosgene assay absorbs the tail gas containing phosgene using 10wt%NaOH solution, and absorbing liquid is into ion chromatography chlorine
Ion concentration, then it is converted into phosgene content in tail gas.
Calculation formula is as follows：
Wherein：c1Indicate phosgene content in tail gas, unit：mg/Nm3；
M indicates the quality of NaOH absorbing liquid, unit：g；
c2Indicate Cl in NaOH absorbing liquid-Content, unit：mg/kg；
Q indicates the tail gas absorption flow containing phosgene, unit：L/min；
T indicates the time of tail gas absorption, unit：min.
Ion chromatography instrument producer is Switzerland Wan Tong company, model 930Compact Flex, column model A
Supp 7-250/4.0, mobile phase are 3.6mmol/L Na2CO3, flow velocity 0.8ml/min.
Embodiment 1
It takes 10kg bamboo charcoal and 5kg 20wt% silicon dioxide gel to mix, by ultrasound and strength mechanical stirring, is prepared into
Slurry dries 6h in 115 DEG C of baking ovens, obtains pulvis, 2.75kg silicon carbide powder, 0.09kg alumina silicate is added, and add
Mixed slurry is made in 9.89kg pure water, strength mechanical stirring, adds 0.68kg hydroxypropyl methyl cellulose, is stirred to D50
It is 0.50 μm.Mist projection granulating temperature is set as 170 DEG C, 105 DEG C of inlet air temperature, 70 DEG C of leaving air temp, pressure 0.06MPaG, is granulated
Obtain powder.0.70kg dibutyl phthalate is added into powder, is mixed evenly to obtain powder.It is added into powder
The Al of 6.28kg 30nm2O3Powder, after being mixed evenly, aging 48h obtains pug, is 10*10mm by pug extrusion molding
Cylinder, 1400 DEG C of sintering 60h obtain efficient phosgene decomposition catalyst.By in packed tower shown in Catalyst packing to Fig. 1, it is passed through
Concentration is 2049347mg/Nm3Phosgene, residence time 18.8s, adjusting process water amount of collected and circulation hydrochloric acid content, control tower
The concentration of hydrochloric acid of bottom discharge is 32.0%, and the phosgene resolution ratio in tail gas is 98.89%.
Embodiment 2
10kg bamboo charcoal and 2.5kg 25wt% silicon dioxide gel is taken to mix, by ultrasound and strength mechanical stirring, preparation
At compound slurry, 8h is dried in 125 DEG C of baking ovens, obtains powder particle, 2.13kg silicon carbide powder, the poly- methyl of 0.06kg is added
Slurry is made in ammonium acrylate, and add 8.01kg pure water, strength mechanical stirring, adds 0.46kg POLYPROPYLENE GLYCOL, be stirred to
D50 is 0.60um.Mist projection granulating temperature is set as 180 DEG C, 110 DEG C of inlet air temperature, 80 DEG C of leaving air temp, pressure 0.07MPaG,
Granulation obtains powder.0.47kg dibutyl phthalate is added into powder, is mixed evenly to obtain powder.Into powder
The Al of 4.35kg40nm is added2O3Powder, after being mixed evenly, aging 60h obtains pug, is 15* by pug extrusion molding
The cylinder of 15mm, 1500 DEG C of sintering 70h obtain efficient phosgene decomposition catalyst.By in packed tower shown in Catalyst packing to Fig. 1,
Being passed through concentration is 1982754mg/Nm3Phosgene, residence time 19.5s, adjusting process water amount of collected and circulation hydrochloric acid content, control
The concentration of hydrochloric acid of tower bottom discharge processed is 32.0%, and the phosgene resolution ratio in tail gas is 98.56%.
Embodiment 3
It takes 10kg bamboo charcoal and 22% silicon dioxide gel of 3.4kg to mix, by ultrasound and strength mechanical stirring, is prepared into
Slurry dries 7h in 120 DEG C of baking ovens, obtains pulvis, 2.39kg silicon carbide powder, 0.07kg alumina silicate is added, and add
Mixed slurry is made in 8.81kg pure water, strength mechanical stirring, adds 0.55kg hydroxypropyl methyl cellulose, is stirred to D50
It is 0.55 μm.Mist projection granulating temperature is set as 175 DEG C, 108 DEG C of inlet air temperature, 75 DEG C of leaving air temp, pressure 0.065MPaG makes
Grain obtains powder.0.56kg dibutyl phthalate is added into powder, is mixed evenly to obtain powder.Add into powder
Enter the Al of 5.14kg 35nm2O3Powder, after being mixed evenly, aging 55h obtains pug, is 12* by pug extrusion molding
The cylinder of 12mm, 1450 DEG C of sintering 65h obtain efficient phosgene decomposition catalyst.By in packed tower shown in Catalyst packing to Fig. 1,
Being passed through concentration is 2013588mg/Nm3Phosgene, residence time 19.2s, adjusting process water amount of collected and circulation hydrochloric acid content, control
The concentration of hydrochloric acid of tower bottom discharge processed is 32.0%, and the phosgene resolution ratio in tail gas is 98.72%.
Comparative example 1
30kg column cocoanut active charcoal (specification 4*4mm) is taken, is loaded into packed tower shown in Fig. 1, being passed through concentration is
2013588mg/Nm3Phosgene, the adjustment residence time is 19.2s, and the concentration of hydrochloric acid of control tower bottom discharge is 32.0%, in tail gas
Phosgene resolution ratio be 45.72%；The adjustment residence time is 30.0s, and the concentration of hydrochloric acid of control tower bottom discharge is 32.0%, tail gas
In phosgene resolution ratio be 59.17%；The adjustment residence time is 19.2s, and the concentration of hydrochloric acid of control tower bottom discharge is 1.0%, tail
Phosgene resolution ratio in gas is 87.86%.
Comparative example 2
30kg SN7501 (specification 12*12mm) is taken to be loaded into packed tower shown in Fig. 1, being passed through concentration is
2013588mg/Nm3Phosgene, the adjustment residence time is 19.2s, and the concentration of hydrochloric acid of control tower bottom discharge is 32.0%, in tail gas
Phosgene resolution ratio be 51.22%；The adjustment residence time is 30.0s, and the concentration of hydrochloric acid of control tower bottom discharge is 32.0%, tail gas
In phosgene resolution ratio be 63.45%；The adjustment residence time is 19.2s, and the concentration of hydrochloric acid of control tower bottom discharge is 1.0%, tail
Phosgene resolution ratio in gas is 89.77%.
Claims (10)
1. a kind of preparation method of phosgene decomposition catalyst, which is characterized in that include the following steps：
A, bamboo charcoal and silicon dioxide gel are mixed, is prepared into slurry；
B, slurry obtained in a is dried in an oven, obtains pulvis；
C, obtain mixing powder after being mixed pulvis obtained in b with silicon carbide powder, dispersing agent, mixing powder again with water
Mixing, is made mixed slurry；
D, binder is added into mixed slurry obtained in step c, be uniformly mixed, bonding slurry is made；
E, slurry mist projection granulating will be bonded obtained in step d, obtain powder；
F, step e medium silt is taken out, plasticiser is added, is mixed, obtains powder；
G, powder in step f is taken out, Al is added2O3, it is mixed, it is aging, obtain pug；
H, pug extrusion molding after will be aging in step g, sintering obtain phosgene decomposition catalyst.
2. the method according to claim 1, wherein silica contains in silicon dioxide gel described in step a
Amount is 15~41wt%, preferably 20~25wt%；The bamboo charcoal and silicon dioxide gel mass ratio are 1:1~10:1, preferably 2:1
~6:1, more preferable 3:1~4:1.
3. method according to claim 1 or 2, which is characterized in that drying temperature described in step b is 100~200 DEG C,
It is preferred that 110~140 DEG C, more preferable 115-125 DEG C；Drying time is 3-15h, preferably 5-10h, more preferable 6-8h.
4. method according to any one of claim 1-3, which is characterized in that pulvis described in step c and carborundum powder
The mass ratio of body is 2:1~8:1, preferably 3:1~7:1, more preferable 4:1~5:1.
5. method according to any of claims 1-4, which is characterized in that dispersing agent described in step c be alumina silicate,
The mass ratio of one of ammonium polymethacrylate, preferably alumina silicate, dispersing agent and silicon carbide powder is 1:20~1:50, preferably
1:25~1:40, more preferable 1:30~1:35；The mass ratio of mixing powder described in step c and water is 1:1~2:1, preferably
1.2:1~1.8:1, more preferable 1.4:1~1.6:1.
6. method according to any one of claims 1-5, which is characterized in that binder described in step d is hydroxypropyl
The mass ratio of one of methylcellulose, POLYPROPYLENE GLYCOL, preferably hydroxypropyl methyl cellulose, binder and mixed slurry is 1:
20~1:60, preferably 1:30~1:50, more preferable 1:35~1:45；The median particle diameter D50 control of manufactured bonding slurry after stirring
System is at 0.30~0.90 μm, and preferably 0.40~0.70 μm, more preferable 0.50~0.60 μm.
7. method according to claim 1 to 6, which is characterized in that the heating of mist projection granulating described in step e
Temperature is controlled at 150~200 DEG C, and preferably 170~180 DEG C；Inlet air temperature is controlled at 100~120 DEG C, and preferably 105~110 DEG C；
Leaving air temp is controlled at 60~90 DEG C, and preferably 70~80 DEG C；Pressure control in 0.05~0.08MPaG, preferably 0.06~
0.07MPaG。
8. method according to any one of claims 1-7, which is characterized in that plasticiser described in step f is adjacent benzene two
The mass ratio of formic acid esters, preferably dibutyl phthalate, plasticiser and powder is 1:20~1:90, preferably 1:30~1:
55, more preferably 1:35~1:45.
9. method according to claim 1 to 8, which is characterized in that Al described in step g2O3For nano particle,
Partial size is 20~100nm, preferably 25~60nm, more preferable 30~40nm；Powder described in step g and Al2O3Mass ratio is 2:1
~8:1, preferably 3:1~6:1, more preferable 4:1~5:1；The aging time described in step g is 36~72h, preferably 48~60h.
10. method according to claim 1 to 9, which is characterized in that sintering temperature described in step h is 1200
~1800 DEG C, preferably 1300~1600 DEG C, more preferable 1400~1500 DEG C；The sintering time be 40~100h, preferably 50~
80h, more preferable 60~70h.
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| CN116371436A (en) * | 2023-02-08 | 2023-07-04 | 美瑞科技(河南)有限公司 | Catalyst capable of efficiently decomposing phosgene and resisting chlorobenzene poisoning, and preparation and application thereof |
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| CN116371436A (en) * | 2023-02-08 | 2023-07-04 | 美瑞科技(河南)有限公司 | Catalyst capable of efficiently decomposing phosgene and resisting chlorobenzene poisoning, and preparation and application thereof |
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