CN103977843A - Methanol catalyst temperature-rising reduction method - Google Patents
Methanol catalyst temperature-rising reduction method Download PDFInfo
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- CN103977843A CN103977843A CN201410226974.1A CN201410226974A CN103977843A CN 103977843 A CN103977843 A CN 103977843A CN 201410226974 A CN201410226974 A CN 201410226974A CN 103977843 A CN103977843 A CN 103977843A
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Abstract
The invention relates to a catalyst temperature-rising reduction technology, in particular to a methanol catalyst temperature-rising reduction method, and the method is used for solving the technical problem that a methanol catalyst is easily burnt down in the reduction process at present. The operation method of catalyst temperature-rising reduction comprises the following steps: (a) a temperature rise stage; (b) an initial reduction stage; (c) a main reduction stage; (d) a final reduction stage; (e) a constant-temperature stage. The method can be used for temperature-rising reduction of the methanol catalyst in a methanol and alcohol alkylation process of chemical enterprises, can be used for effectively controlling the temperature-rising rate and the water yield, avoiding burning down of the catalyst, and ensuring the activity of the reduced catalyst.
Description
Technical field
The present invention relates to revivification of catalyst technology, be specially a kind of method of methyl alcohol catalyst heating reduction.
Background technology
Fertilizer enterprises is Cu-Zn-Al series catalysts what carry out generally using when methyl alcohol synthesizes now, before this series catalysts reduces, is not oxidation state, is by high-purity C u (NO
3)
2, Zn (NO
3)
2be dissolved in Na
2cO
3in solution, by coprecipitation, obtain (Cu, Zn)
2(OH)
2cO
3precipitation, then adds Al
2o
3and Cr
2o
3the cylinder granule of the loose structure forming through high temperature Deng element, needs elemental copper as reaction media and methyl alcohol is synthetic, after therefore need to being reduced, uses.Methyl alcohol catalyst heating reduction is exothermic reaction (other conversion, synthetic catalyst heating reduction are all the endothermic reaction), if can not control exactly heating rate and thermal discharge in heating reduction process, be easy to cause catalyst steep temperature rise and the situation of " burning ", this happens occasionally in many manufacturers, not that catalyst is scrapped, be exactly active not all right reduction of service life, and the heating reduction scheme that catalyst producer provides is controlled main points and heating rate is all fuzzyyer, be unfavorable for operation.
For these reasons, need to improve methyl alcohol catalyst heating reduction, make catalyst in reduction process, avoid " being burnt " and scrapping by high temperature, to extend its service life.
Summary of the invention
The present invention is the technical problem that the current methyl alcohol catalyst of solution easily " is burnt " in reduction process, and a kind of method of methyl alcohol catalyst heating reduction is provided.
The present invention realizes by the following technical solutions: a kind of method of operating of methyl alcohol catalyst heating reduction, comprises the following steps: (a) temperature rise period; Reaction system rises to 70 ℃ by room temperature, and catalyst stratification temperature is poor is 0 ℃, and heating rate 15-20 ℃/h, time 3 ~ 4h; (b) the reduction phase initial stage; First stage, catalyst layer hot(test)-spot temperature rises to 80 ℃ by 70 ℃, and catalyst stratification temperature differs from 5 ℃, 0-5 ℃/h of programming rate rate, and Chu Shui Liang≤1 ~ 3Kg/ ton catalyst/h, time 2 ~ 3h; Second stage, catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, the poor 10-15 ℃ of catalyst stratification temperature, 0-1 ℃/h of programming rate rate, Chu Shui Liang≤3 ~ 5Kg/ ton catalyst/h, time 20 ~ 25h; (c) reduce the main phase; First stage, catalyst layer hot(test)-spot temperature rises to 120 ℃ by 95 ℃, the poor 5-10 ℃ of catalyst stratification temperature, heating rate 1-3 ℃/h, Chu Shui Liang≤2 ~ 4Kg/ ton catalyst/h, time 15 ~ 20h; Second stage, catalyst layer hot(test)-spot temperature rises to 140 ℃ by 120 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 0-1 ℃/h, Chu Shui Liang≤3 ~ 5Kg/ ton catalyst/h, time 20 ~ 25h; Phase III, catalyst layer hot(test)-spot temperature rises to 160 ℃ by 140 ℃, the poor 0-5 ℃ of catalyst stratification temperature, 1 ~ 3 ℃/h of heating rate, Chu Shui Liang≤2 ~ 4Kg/ ton catalyst/h, time 10 ~ 15h; (d) reduce latter stage; First stage, catalyst layer hot(test)-spot temperature rises to 200 ℃ by 160 ℃, and catalyst stratification temperature differs from 0 ℃, and heating rate 3-10 ℃/h, Chu Shui Liang≤1 ~ 3Kg/ ton catalyst/h, time 5 ~ 10h; Second stage, catalyst layer hot(test)-spot temperature rises to 240 ℃ by 200 ℃, and catalyst stratification temperature differs from 0 ℃, 10 ℃/h of heating rate, Chu Shui Liang≤1 ~ 2Kg/ ton catalyst/h, time 4h; (e) the constant temperature stage; Temperature range is 240 ℃, and catalyst stratification temperature differs from 0 ℃, 0 ℃/h of heating rate, and Chu Shui Liang≤2Kg/h, the time keeps 2h.In each step, all requiring keeping system pressure is 5.0Mpa above, and systemic circulation tolerance keeps 2000h
-1volume space velocity, H in system gas
2content is calculated as 70% with volume fraction.
Heating reduction process is used qualified virgin gas (i.e. synthetic tonifying Qi), H in gas
2content 70% left and right (volume fraction), all the other compositions are N
2, CO and CO
2content does not almost have, and has avoided so dramatically catalyst to have active rear methyl alcohol heat of reaction to produce in partial reduction and has caused catalyst sudden temperature rise (if gas is used decarburization after-purification gas, to contain 1.0% ~ 2.0% CO% and CO in gas
2%, has CO+2H
2=CH
3oH+Q CO
2+ 3H
2=CH
3oH+H
2two strong exothermal reactions of O+Q occur).
According to metal active, sort: K, Ca, Na, Mg, Al, Zn, Fe, Se, Pb come before H.The specific activity H of Zn and Al is strong, and a little less than the specific activity H of Cu, the reduction reaction of CuO only occurs therefore general reduction reaction:
CuO+H
2=Cu+H
2O+86.5KJ/mol
In reduction process, generate 20% left and right that the water yield is about catalyst weight, various model catalyst are with Cu content difference to some extent, wherein chemical water accounts for 8% ~ 10%, mechanical water accounts for 10% ~ 13%, therefore the key of copper-based catalysts reduction is to control namely programming rate of reduction reaction speed, the amount that generates water by reduction reaction conversely namely water yield is controlled heating rate and system reducing reaction producing heat, especially in two water outlet peak periods that go out mechanical water and chemical water.Arrhenius equation: k=Ae
-Ea/RTit has described the relation between chemical reaction rate (k) and temperature (T) and reaction activity Ea.For its activation energy of certain chemical reaction, be certain, so when reaction temperature heat energy RT reaches or surmount the required reaction activity Ea of material, chemical reaction rate leaps, be swift in response and carry out, that is to say and will generate a large amount of water, emit a large amount of heats simultaneously, at this moment need strictly to control reaction rate, otherwise heat too much will cause catalyst temperature rise and accelerate, temperature rise stimulates again quickening reaction rate, produce more heat, form chain reaction, cause catalyst temperature to rise and " burning " very soon.According to a large amount of practical observations, the reduction process of catalyst of the present invention has 80 ℃ ~ 95 ℃ and 120 ℃ ~ 140 ℃ to be two water outlet peak period temperature ranges, therefore near these two temperature ranges, adopt temperature range of the present invention and heating rate can effectively control the speed of reduction reaction, make the catalyst can be because of the liberated heat in reaction " being burnt "; The heating rate and the temperature range that in other step, adopt are to be also whole reduction reaction service simultaneously, guarantee carrying out smoothly of whole reduction reaction; Catalyst layering is to rely on cold shock gas by force catalyst layer to be divided into two parts by temperature difference, avoid whole catalyst to reach reaction high peak temperature and water yield is excessive simultaneously, reaction heat gathers and catalyst sudden temperature rise, and circulating flow rate can not be taken reaction heat and " burning " catalyst out of in time.Catalyst is divided into two parts pulls open 10 ~ 15 ℃ of temperature difference intentionally, reduces water yield per hour, makes reduction reaction more easy to control.Along with 160 ℃ of water outlets later reduce and progressively turn down and close cold shock, eliminate axial temperature difference.
In the present invention, whole heating reduction process has regulations to abide by, and speed is moderate, can complete smoothly the work of catalyst heating reduction.
Further, in keeping system pressure and systemic circulation tolerance, stable in the situation that, should adjust heating rate speed in each stage according to water yield size, thereby within the scope of each phases-time, extend or shorten the heating reduction time; For reduction initial stage second stage, be that catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, and reduce main phase second stage, be that catalyst layer hot(test)-spot temperature rises to 140 ℃ of these two stages by 120 ℃, can, by keeping constant temperature and the mode that heats up and combine, make water yield can not exceed this stage water yield requirement; Described systemic circulation tolerance refers to by volume flow 0.5m
3/ min/ ton catalyst.
In actual heating reduction process, should determine according to the water yield of each stage of reaction the size of programming rate, in actual reduction process, discharge water and once weigh per half an hour, for each stage in reduction, once surpass 1.5 ~ 2Kg/ ton catalyst/half h, constant temperature half an hour is to observe water yield next time, generally only have to just there will be the situation of water yield sudden fast rush near two high peak temperatures of water outlet, therefore must note, would rather also to avoid temperature heat " surplus " and reaction is carried out in a large number by constant temperature, after water yield affects too greatly media reductive, active structure forms, impact is active, therefore each stage of heating up is particularly reduced initial stage second stage and the main phase second stage of reduction, and temperature-rise period is the process of an intensification and constant temperature dynamic bind, guarantees that water yield is no more than corresponding requirements.
This process is the Novel operating method in conjunction with working practice summary of experience according to reduction reaction principle, the heating reduction that can be used for methyl alcohol catalyst in chemical enterprise methyl alcohol, alcohol hydrocarbylation process, according to this scheme, can effectively control heating rate and water yield, avoid " burning " catalyst, guaranteeing the activity after media reductive, is a kind of simple and practical process.
The specific embodiment
The method of operating of 1 one kinds of methyl alcohol catalyst heating reductions of embodiment, comprises the following steps: (a) temperature rise period; Reaction system rises to 70 ℃ by room temperature, and catalyst stratification temperature is poor is 0 ℃, and heating rate 15-20 ℃/h, time 3h; (b) the reduction phase initial stage; First stage, catalyst layer hot(test)-spot temperature rises to 80 ℃ by 70 ℃, and catalyst stratification temperature differs from 5 ℃, 0-5 ℃/h of programming rate rate, Chu Shui Liang≤1Kg/ ton catalyst/h, time 3h; Second stage, catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, and catalyst stratification temperature differs from 10 ℃, 0-1 ℃/h of programming rate rate, Chu Shui Liang≤3Kg/ ton catalyst/h, time 25h; (c) reduce the main phase; First stage, catalyst layer hot(test)-spot temperature rises to 120 ℃ by 95 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 1-3 ℃/h, Chu Shui Liang≤2Kg/ ton catalyst/h, time 20h; Second stage, catalyst layer hot(test)-spot temperature rises to 140 ℃ by 120 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 0-1 ℃/h, Chu Shui Liang≤3Kg/ ton catalyst/h, time 25h; Phase III, catalyst layer hot(test)-spot temperature rises to 160 ℃ by 140 ℃, and catalyst stratification temperature differs from 0 ℃, 1 ~ 3 ℃/h of heating rate, Chu Shui Liang≤2Kg/ ton catalyst/h, time 15h; (d) reduce latter stage; First stage, catalyst layer hot(test)-spot temperature rises to 200 ℃ by 160 ℃, and catalyst stratification temperature differs from 0 ℃, and heating rate 3-10 ℃/h, Chu Shui Liang≤1Kg/ ton catalyst/h, time 10h; Second stage, catalyst layer hot(test)-spot temperature rises to 240 ℃ by 200 ℃, and catalyst stratification temperature differs from 0 ℃, 10 ℃/h of heating rate, Chu Shui Liang≤1Kg/ ton catalyst/h, time 4h; (e) the constant temperature stage; Temperature range is 240 ℃, and catalyst stratification temperature differs from 0 ℃, 0 ℃/h of heating rate, and Chu Shui Liang≤2Kg/h, the time keeps 2h.In each step, all requiring keeping system pressure is 5.0Mpa above, and systemic circulation tolerance keeps 2000h
-1volume space velocity, H in system gas
2content accounts for 70%(volume fraction).
The method of operating of 2 one kinds of methyl alcohol catalyst heating reductions of embodiment, comprises the following steps: (a) temperature rise period; Reaction system rises to 70 ℃ by room temperature, and catalyst stratification temperature is poor is 0 ℃, and heating rate 15-20 ℃/h, time 4h; (b) the reduction phase initial stage; First stage, catalyst layer hot(test)-spot temperature rises to 80 ℃ by 70 ℃, and catalyst stratification temperature differs from 5 ℃, 0-5 ℃/h of programming rate rate, Chu Shui Liang≤3Kg/ ton catalyst/h, time 2h; Second stage, catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, and catalyst stratification temperature differs from 15 ℃, 0-1 ℃/h of programming rate rate, Chu Shui Liang≤5Kg/ ton catalyst/h, time 20h; (c) reduce the main phase; First stage, catalyst layer hot(test)-spot temperature rises to 120 ℃ by 95 ℃, the poor 5-10 ℃ of catalyst stratification temperature, heating rate 1-3 ℃/h, Chu Shui Liang≤4Kg/ ton catalyst/h, time 15h; Second stage, catalyst layer hot(test)-spot temperature rises to 140 ℃ by 120 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 0-1 ℃/h, Chu Shui Liang≤5Kg/ ton catalyst/h, time 20h; Phase III, catalyst layer hot(test)-spot temperature rises to 160 ℃ by 140 ℃, and catalyst stratification temperature differs from 5 ℃, 1 ~ 3 ℃/h of heating rate, Chu Shui Liang≤4Kg/ ton catalyst/h, time 10h; (d) reduce latter stage; First stage, catalyst layer hot(test)-spot temperature rises to 200 ℃ by 160 ℃, and catalyst stratification temperature differs from 0 ℃, and heating rate 3-10 ℃/h, Chu Shui Liang≤3Kg/ ton catalyst/h, time 5h; Second stage, catalyst layer hot(test)-spot temperature rises to 240 ℃ by 200 ℃, and catalyst stratification temperature differs from 0 ℃, 10 ℃/h of heating rate, Chu Shui Liang≤2Kg/ ton catalyst/h, time 4h; (e) the constant temperature stage; Temperature range is 240 ℃, and catalyst stratification temperature differs from 0 ℃, 0 ℃/h of heating rate, and Chu Shui Liang≤2Kg/h, the time keeps 2h.In each step, all requiring keeping system pressure is 5.0Mpa above, and systemic circulation tolerance keeps 2000h
-1volume space velocity, H in system gas
2content accounts for 70%(volume fraction).
The method of operating of 3 one kinds of methyl alcohol catalyst heating reductions of embodiment, comprises the following steps: (a) temperature rise period; Reaction system rises to 70 ℃ by room temperature, and catalyst stratification temperature is poor is 0 ℃, and heating rate 15-20 ℃/h, time 3.5h; (b) the reduction phase initial stage; First stage, catalyst layer hot(test)-spot temperature rises to 80 ℃ by 70 ℃, and catalyst stratification temperature differs from 5 ℃, 0-5 ℃/h of programming rate rate, Chu Shui Liang≤2Kg/ ton catalyst/h, time 2.5h; Second stage, catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, and catalyst stratification temperature differs from 12 ℃, 0-1 ℃/h of programming rate rate, Chu Shui Liang≤4Kg/ ton catalyst/h, time 23h; (c) reduce the main phase; First stage, catalyst layer hot(test)-spot temperature rises to 120 ℃ by 95 ℃, and catalyst stratification temperature differs from 7 ℃, and heating rate 1-3 ℃/h, Chu Shui Liang≤3Kg/ ton catalyst/h, time 17h; Second stage, catalyst layer hot(test)-spot temperature rises to 140 ℃ by 120 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 0-1 ℃/h, Chu Shui Liang≤4Kg/ ton catalyst/h, time 23h; Phase III, catalyst layer hot(test)-spot temperature rises to 160 ℃ by 140 ℃, and catalyst stratification temperature differs from 3 ℃, 1 ~ 3 ℃/h of heating rate, Chu Shui Liang≤3Kg/ ton catalyst/h, time 12h; (d) reduce latter stage; First stage, catalyst layer hot(test)-spot temperature rises to 200 ℃ by 160 ℃, and catalyst stratification temperature differs from 0 ℃, and heating rate 3-10 ℃/h, Chu Shui Liang≤2Kg/ ton catalyst/h, time 7h; Second stage, catalyst layer hot(test)-spot temperature rises to 240 ℃ by 200 ℃, and catalyst stratification temperature differs from 0 ℃, 10 ℃/h of heating rate, Chu Shui Liang≤1.5Kg/ ton catalyst/h, time 4h; (e) the constant temperature stage; Temperature range is 240 ℃, and catalyst stratification temperature differs from 0 ℃, 0 ℃/h of heating rate, and Chu Shui Liang≤2Kg/h, the time keeps 2h.In each step, all requiring keeping system pressure is 5.0Mpa above, and systemic circulation tolerance keeps 2000h
-1volume space velocity, H in system gas
2content is calculated as 70% with volume fraction.
For above-mentioned each embodiment, in keeping system pressure and systemic circulation tolerance, stable in the situation that, should adjust heating rate speed in each stage according to water yield size, thereby within the scope of each phases-time, extend or shorten each heating reduction time in stage; For reduction initial stage second stage, be that catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, and to reduce main phase second stage be that catalyst layer hot(test)-spot temperature rises to 140 ℃ of these two stages by 120 ℃, can, by keeping constant temperature and the mode that heats up and combine, make water yield can not exceed this stage water yield requirement; Described systemic circulation tolerance refers to by volume flow 0.5m
3/ min/ ton catalyst.As risen in 95 ℃ of these temperature ranges by 80 ℃ for catalyst layer hot(test)-spot temperature, adopt 0 ℃ of constant temperature and heat 1 ℃ of mode combining, and keeping within water yield maintains the scope of stipulating separately.
Reduction reaction process regulation principle: reduction reaction is strictly followed " three low, three steady, three controls " principle, " three is low " is low temperature water outlet, low pressure delivery and underrun a period of time, " three is steady " is that temperature is steady, pressure is steady, water yield is steady, and " three controls " controlled temperature, controls water yield, controlled CO
2% content.These conditions influence each other, be therefore mainly keeping system pressure in 5.0 ± 0.1MPa, in reduction reaction due to H
2participate in reaction and be constantly consumed, in order to keep H in gas
2% content 70% left and right, needs with the special preferably DN15 being equipped with or the elevated temperature gas pipeline of DN20 at 80 ℃ later and is system continuous supplementation sub-fraction live gas, by emptying after tower, is realized substitution gas and maintained the stable object of system pressure.According to 2 tons of catalyst of practical experience, coordinate 1 m
3the internal circulating load of/min, is converted under 5.0MPa system pressure namely approximately 3000Nm
3/the internal circulating load of h, observes through using, and this internal circulating load is moderate, 10 tons of general 15000Nm of catalyst
3/h internal circulating load, should keep inconvenience in whole reduction process.Like this at pressure, H
2in the situation that % content and internal circulating load remain unchanged, control heating rate well, guarantee that temperature heat is supplied with just can guarantee that water yield is relatively stable in right amount, Gao Feng Qi≤3 ~ 5Kg/ ton catalyst/h, reduction reaction intensity stabilization is even, just can make catalyst when forming active lattice structure, have good activity.Owing to containing CO in catalyst
3radical ion, therefore will discharge sub-fraction CO in reduction process
2gas, why Here it is arrives the reason of reduction middle and later periods water outlet band alcohol taste.If supplement in virgin gas, contain ammonia, water outlet will be because containing Cu (NH so
3 ) 2+ion and aobvious blue is therefore avoided in gas containing ammonia as far as possible, in case copper runs off (this kind of tonifying Qi is mainly because the gas of washing through copper after refining contains Ammonia).
Because internal circulating load is large and obviously to reduction reaction intensity effect, therefore remain stable as far as possible, otherwise along with internal circulating load strengthens, reduces and water yield strengthens, reduces, be unfavorable for stablizing water outlet.In addition, owing to going out mechanical water reaction, be that molecular diffusion is controlled (under certain temperature conditions), so internal circulating load play controlled condition to water yield during 80 ℃ ~ 95 ℃.Therefore the variation of system pressure also directly affects separating out of water, will make every effort to internal circulating load, system pressure is stable.
Claims (2)
1. a method of operating for methyl alcohol catalyst heating reduction, comprises the following steps: (a) temperature rise period; Reaction system rises to 70 ℃ by room temperature, and catalyst stratification temperature is poor is 0 ℃, and heating rate 15-20 ℃/h, time 3 ~ 4h; (b) the reduction phase initial stage; First stage, catalyst layer hot(test)-spot temperature rises to 80 ℃ by 70 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 0-5 ℃/h, Chu Shui Liang≤1 ~ 3Kg/ ton catalyst/h, time 2 ~ 3h; Second stage, catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, the poor 10-15 ℃ of catalyst stratification temperature, 0-1 ℃/h of programming rate rate, Chu Shui Liang≤3 ~ 5Kg/ ton catalyst/h, time 20 ~ 25h; (c) reduce the main phase; First stage, catalyst layer hot(test)-spot temperature rises to 120 ℃ by 95 ℃, the poor 5-10 ℃ of catalyst stratification temperature, heating rate 1-3 ℃/h, Chu Shui Liang≤2 ~ 4Kg/ ton catalyst/h, time 15 ~ 20h; Second stage, catalyst layer hot(test)-spot temperature rises to 140 ℃ by 120 ℃, and catalyst stratification temperature differs from 5 ℃, and heating rate 0-1 ℃/h, Chu Shui Liang≤3 ~ 5Kg/ ton catalyst/h, time 20 ~ 25h; Phase III, catalyst layer hot(test)-spot temperature rises to 160 ℃ by 140 ℃, the poor 0-5 ℃ of catalyst stratification temperature, 1 ~ 3 ℃/h of heating rate, Chu Shui Liang≤2 ~ 4Kg/ ton catalyst/h, time 10 ~ 15h; (d) reduce latter stage; First stage, catalyst layer hot(test)-spot temperature rises to 200 ℃ by 160 ℃, and catalyst stratification temperature differs from 0 ℃, and heating rate 3-10 ℃/h, Chu Shui Liang≤1 ~ 3Kg/ ton catalyst/h, time 5 ~ 10h; Second stage, catalyst layer hot(test)-spot temperature rises to 240 ℃ by 200 ℃, and catalyst stratification temperature differs from 0 ℃, 10 ℃/h of heating rate, Chu Shui Liang≤1 ~ 2Kg/ ton catalyst/h, time 4h; (e) the constant temperature stage; Temperature range is 240 ℃, and catalyst stratification temperature differs from 0 ℃, 0 ℃/h of heating rate, and Chu Shui Liang≤2Kg/h, the time keeps 2h; In each step, all requiring keeping system pressure is 5.0Mpa above, and systemic circulation tolerance keeps 2000h
-1volume space velocity, H in system gas
2content is calculated as 70% with volume fraction.
2. the method for operating of a kind of methyl alcohol catalyst heating reduction as claimed in claim 1, it is characterized in that, in keeping system pressure and systemic circulation tolerance stable in the situation that, should adjust heating rate speed in each stage according to water yield size, thereby within the scope of each phases-time, extend or shorten the heating reduction time; For reduction initial stage second stage, be that catalyst layer hot(test)-spot temperature rises to 95 ℃ by 80 ℃, and to reduce main phase second stage be that catalyst layer hot(test)-spot temperature rises to 140 ℃ of these two stages by 120 ℃, can, by keeping constant temperature and the mode that heats up and combine, make water yield can not exceed this stage water yield requirement; Described systemic circulation tolerance refers to by volume flow 0.5m
3/ min/ ton catalyst.
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| CN104857997A (en) * | 2015-04-30 | 2015-08-26 | 临涣焦化股份有限公司 | Reduction method of methanol synthesis catalyst |
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