CN101590419B - Activation method of inactivated super solid acidic catalyst for excessive water content of raw material - Google Patents
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Abstract
The invention discloses an activating method of inactivated super solid acidic catalyst for excessive water content of raw material in reaction process, comprising the following steps: the process of leading reaction raw material into a reactor stops; hydrogen or nitrogen is led into the reactor to serve as recycle gas after recycling; at the temperature of 180-280 DEG C and pressure of 0.1-1.0MPa, the recycle gas is used for activating inactivated catalyst; and during activation, the water content of the recycle gas is lowered to be below 50ppm with drying agent. The method can effectively restore activity of inactivated catalyst for excessive water content in reaction process.
Description
Technical field
The present invention is a kind of activation method of solid super acid catalyst, specifically, is because of the activation method of the solid super acid catalyst of raw water too high levels inactivation in a kind of course of reaction.
Background technology
Acidic catalyst plays an important role in petrochemical industry industry, and acid catalyst commonly used has: liquid acid catalyst, and as H
2SO
4, HF; And halogen-containing solid acid catalyst.All there are problems such as contaminated environment and etching apparatus in this two classes catalyst.Existing result of study shows, handle the oxide or the hydroxide of IVB family metal with sulfur-containing compound, and through 400～800 ℃ of roastings, can obtain containing the solid acid catalyst of sulfate radical, can be as the acid strength of disclosed this type of solid acid of the day disclosure special permission clear 59-6181 of communique above 100% sulfuric acid (H
0=-11.93), therefore be called as solid super-strong acid.Because solid super acid catalyst has that surface acidity is strong, heat endurance is higher, environmentally friendly, not etching apparatus, advantage such as can regenerate, and is considered to up-and-coming isomerization catalyst [K.Arata, Adv.Catal., 37 (1990) 0165].In addition, need in the reaction of acidic catalyst in the esterification of cracking, alkene oligomerization and the hydration of butylene-isobutane alkylation, hydro carbons, alcohols and etherificate etc., solid super-strong acid also demonstrates very high catalytic activity.
In the alkane isomerization course of reaction, SO
4 2-/ ZrO
2The acidity of solid super acid catalyst mainly is the equilibrium relation in B (Bronsted) acid site and L (Lewis) acid site, directly determines the reactivity worth of catalyst, and the water content of catalyst has appreciable impact to the acidity of catalyst.The water that enters system in the course of reaction is mainly brought into by raw material, and excessive water can cause the loss of L acid, catalyst acid intensity is reduced and causes catalysqt deactivation.CN1185325C requires to use SO
4 2-/ ZrO
2The raw material hydrocarbon water content of the alkane isomerization process of solid super acid catalyst is lower than 5ppm.But the excessive dehydration of catalyst then can make the B acid site of directly playing catalytic action transform to the L acid site, also causes catalyst activity reduction.US5837641 adopts the method for short-term water filling 5～15ppm in raw material, improves the activity of excessive dehydration catalyst.
In the course of reaction, SO
4 2-/ ZrO
2The water absorption of solid super acid catalyst and raw water content and reaction temperature have equilibrium relation, and hot conditions can reduce the catalyst equilibrium water content.Japanese patent laid-open 10-17872 discloses a kind of activation SO
4 2-/ ZrO
2The method of solid acid isomerization catalyst, adopt the set of reactors of changeable control, catalyst do not absorb water inactivation or the activation after reactor under the well-defined reaction temp condition, react, the reactor of inactivation of having absorbed water reacts under the condition that is higher than 60 ℃ of well-defined reaction temps, recover the part activity of catalyst loss, by each reactor heating-cooling handover operation, under the situation of raw water content superelevation, keep the operation of reaction system.Significantly improve reaction temperature and can reduce the catalyst equilibrium water content, but while selection of catalysts variation, the cracking accessory substance of reaction increases, and catalyst carbon deposit speed increases.
SO
4 2-Be SO
4 2-/ ZrO
2The main active component of solid super acid catalyst.Existing result of study shows, under anaerobic or hypoxic atmosphere and uniform temperature condition, and the SO on the catalyst
4 2-Be reduced and run off (occur about 280 ℃, raise with temperature and quicken) cause catalyst activity reduction.Therefore the traditional activation process of this class catalyst comprises the activation of decaying catalyst in preceding pre-treatment and activation of reaction and the course of reaction, mostly carries out under oxygen-containing atmosphere and higher temperature.CN1131105C discloses the typical activation method of such catalyst, the catalyst that reacts inactivation in preceding or the course of reaction is used air-treatment at 350～480 ℃, make the dry and oxidation of catalyst remove the material of absorption or deposition and activate, improve or recover catalyst activity.Propose simultaneously, catalyst property changes if treatment temperature is too high, and the too low catalyst that will cause of treatment temperature is fully not dry, and catalyst activity all descends under two kinds of situations.Adopt air-activated method to be similar to catalyst regeneration, begin reaction again through steps such as inert gas replacement, air-treatment, inert gas replacement, hydrogen reducings usually, operating procedure and media variations are many, and process time is long.
Japanese patent laid-open 10-15399 discloses a kind of renovation process of solid acid isomerization catalyst, this method in the course of reaction because of the catalyst of institute's sulfur compound in the raw material and benzene poisoning and deactivation, after stopping charging, handle the recovery catalyst activity at 250～300 ℃ with hydrogen.
Summary of the invention
The purpose of this invention is to provide the activation method that causes the solid super acid catalyst of inactivation in a kind of course of reaction because of water intoxication, this method can have the efficient recovery activity of such catalysts, makes it reach the not preceding level of inactivation.
In the course of reaction provided by the invention because of the activation method of the solid super acid catalyst of raw water too high levels inactivation, comprise and stop in reactor, to feed reaction raw materials, to wherein feeding hydrogen or nitrogen and circulation as circulating air, circulating air is reduced to below the 50ppm with the water content that drier will be wherein, under 180～280 ℃, 0.1～1.0MPa condition with the catalyst of circulating air activation inactivation.
The inventive method adopts comparatively dry recyclegas to the SO of course of reaction because of raw water content overproof inactivation
4 2-/ ZrO
2Solid super acid catalyst carries out activation processing under lower temperature, the activity of activation rear catalyst can return to the normal level before the inactivation.
The specific embodiment
We find that generally, raw material water content＜5ppm helps to keep SO
4 2-/ ZrO
2The alkane isomerization activity that solid super acid catalyst is good; The raw material water content can cause catalyst activity reduction at 5～10ppm, but along with the raw material water content drops to below the 5ppm, catalyst activity can progressively return to normal level; As raw material water content＞15ppm, when particularly significantly surpassing the content of its saturated dissolving water, catalyst is with serious inactivation, even again raw water content is dropped to below the 5ppm, catalyst activity can not return to normal level, needing this moment to adopt the method for activation to recover catalyst activity, mainly is to remove redundant moisture on the catalyst, the acidity of equilibrium catalyst.
The inventive method is carried out activation processing to the catalyst that causes inactivation because of the raw water too high levels, recovers its activity.Characteristics of the present invention are: before the decaying catalyst activation, stop to feed raw material in reactor, also do not contact with the low water content raw material; Activated gas is reduced to its water content the activation that is used further to decaying catalyst below the 50ppm through super-dry; The temperature of activating catalyst is lower.In addition, the gas of activating catalyst can adopt the reaction carrier gas, and is easy and simple to handle, and soak time is short, and activation rear catalyst activity can return to the preceding level of inactivation.
The inventive method is after catalyst is because of raw water too high levels inactivation, stop charging earlier, make circulating air with hydrogen or nitrogen, in reaction unit, circulate, reaction system circulating air pressure is preferably transferred to 0.2～0.8MPa, remove water in the circulating air with being connected in series with drier in the drying chamber in the circulating air pipeline simultaneously, make the activated media that is re-used as decaying catalyst after its drying.The preferred 3～25ppm of water content in the circulating air of dry back, more preferably 3～20ppm.
Be provided with the circulating air drying unit in the described reaction unit.This unit can adopt under certain pressure the cryogenic freezing dehydration, or with the water content in the method reduction circulating air of absorption such as adsorbent such as molecular sieve, aluminium oxide, silica gel, active carbon, preferably uses adsorbent (drier) to remove water in the circulating air.The preferred A type molecular sieve of described drier, silica gel, aluminium oxide or active carbon.The working pressure of drier should be consistent with the operating pressure of technical process respective stage device.When the decline of sorbent treatment effect can't reach requirement in the drier, can be changed or be carried out on-the-spot in-situ regeneration, preferred on-the-spot in-situ regeneration method.
When the present invention activates decaying catalyst with circulating air, preferred 200～270 ℃ of activation temperature, the preferred 0.3～0.5MPa of circulating air pressure, control circulating air is 300～3000: 1 with the catalyst volume ratio, preferred 800～1500: 1, the time that feeds the circulating air activating catalyst in decaying catalyst is 1～24 hour.The catalysqt deactivation that causes when water content in the raw material is 20～30ppm is with preferred 200～240 ℃ of the temperature of circulating air activation decaying catalyst, preferred 2～4 hours of activation processing time.The catalysqt deactivation that causes when water content in the raw material is surpassed 40ppm is with preferred 220～260 ℃ of the temperature of circulating air activation decaying catalyst, preferred 6～12 hours of activation processing time.
The described catalyst of the inventive method is the solid super acid catalyst that the sulfur loaded acid group makes on zirconium dioxide, for increasing the anti-carbon deposition ability of catalyst, can introduce VIII family metal in catalyst, in addition, also contains suitable binding agent in the catalyst.This type of solid super acid catalyst is applicable to hydrocarbon isomerization, alkylation, cracking, technical process such as superimposed.The device that above-mentioned technical process is used can be: fixed bed half regenerative device, and moving bed continuous regenerative device, the front is that fixed bed reactors, back are the combination cot devices of moving-burden bed reactor, fixed bed circular regeneration or last anti-switching regenerative device.
The preferred solid super acid catalyst of the inventive method comprises the mixed oxide carrier of the sulfur loaded acid group of the VIII family metal of 0.05～2.0 quality % and 98.0～99.5 quality %, described mixed oxide carrier comprises the zirconia of 20～49 quality %, the aluminium oxide of 9～50 quality % and the silica of 1～52 quality %, and the sulfur content in the catalyst is 0.5～3.5 quality %.The preferred platinum of described VIII family's metal, palladium or nickel.The preparation method that described catalyst is detailed can be with reference to CN1524616A.
Above-mentioned catalyst needs through preliminary treatment such as super-dry, activation, reduction before reaction.Preliminary treatment can be adopted modes such as reduction in the outer activating and reducing of reactor, the outer activator of reactor, the interior activating and reducing of reactor.If select the pretreatment mode of reduction in outer activating and reducing of reactor or the outer activator of reactor for use; when catalyst packing, reactor charge, should take corresponding measure; as pack, use dry inert gas shielding when loading reactor and shorten filling time etc., prevent the catalyst contact atmosphere moisture absorption.The preferred pretreatment mode that adopts activation in the reactor, reduction.
Described solid super acid catalyst can feed lighter hydrocarbons and carry out isomerization reaction through after reacting preceding preliminary treatment.Reaction condition is: 140～220 ℃, 1.0～4.0MPa, charging mass space velocity 0.5～5.0hr
-1Hydrogen/hydrocarbon molecule ratio is 0.5～5.0.
The preferred C of described light hydrocarbon feedstocks
4～C
7The light naphthar of hydro carbons, its main component are C
5～C
6N-alkane, and contain part cycloalkane.Raw material need be removed impurity such as most of sulphur, nitrogen and will fully remove wherein moisture content before use through hydrofinishing.Raw material dehydration can be adopted the method for absorption such as fractionating column fractionation or drier such as silica gel, molecular sieve, aluminium oxide, and under the normal running, raw water content is controlled at below the 5ppm.
When the raw material dewatering unit breaks down or be unusual, saturated as water fractionating column operation fluctuation or drier suction in the course of reaction, raw water content can raise rapidly and catalyst activity is obviously descended.At this moment, by the composition analysis of raw material water content and product being determined whether catalyst needs activation.Surpass 15ppm if cause the raw water content of catalysqt deactivation, particularly surpass the saturation water content that dissolves in the raw material, promptly water content surpasses 30ppm in the raw material, simultaneously product C
5Isomerization rate descends and surpasses more than the 6 quality % of normal value, just needs catalyst is activated, even otherwise raw water content is reduced to below the 5ppm, catalyst activity also can't return to normal level.
Stop reaction feed immediately after definite catalyst need activate, the activation procatalyst no longer contacts the raw material that water content is lower than 5ppm.After stopping charging, feed circulating air and continue circulation 0.5～5 hour under reaction temperature, preferred 1～2 hour so that take residual raw material reactor out of and discharge reaction unit fully.
The described preferred hydrogen of circulating air that is used to activate decaying catalyst, more preferably employed circulating hydrogen in the course of reaction.
Activation processing transfers to reaction temperature with reactor inlet temperature after finishing under the hydrogen cycling condition, the circulating air drier is broken away from from the circulating air pipeline, and reaction system boosts to reaction pressure with hydrogen.Press parameters such as reaction condition control temperature, pressure, air speed, hydrogen/oil ratio, the raw material introducing reaction system that water content is lower than 5ppm restarts reaction.
The inventive method is applicable to that light hydrocarbon isomerization reacts used solid super acid catalyst and causes in-situ activation behind the inactivation because of the raw water content overproof.
Further specify the present invention below by example, but the present invention is not limited to this.
Example 1
This example is settled drying chamber in the circulating air pipeline, and raw material is carried out processed.
The circulating air drying chamber is contacted in the circulating air pipeline, the 4A molecular sieve was carried out packing into wherein after the activation processing 450 ℃ of roastings in 2 hours.
With forming raw material as shown in table 1, under 0.2～0.3MPa, dewater by the container that the 3A molecular sieve is housed, control its water content and be no more than 5ppm.
Example 2
To SO
4 2-/ ZrO
2Solid super acid catalyst reacts preceding preliminary treatment.
Use air in 400 ℃ of roastings 1 hour the solid super acid catalyst that consists of table 2.With baked SO
4 2-/ ZrO
2Solid super acid catalyst is packed in the reactor of isomerization reaction device, and the catalyst loading amount is 50 milliliters.
Example 3～8
Recover water intoxication SO with the inventive method
4 2-/ ZrO
2The activity of solid super acid catalyst.
Reaction unit is boosted to 1.6MPa with hydrogen, start recycle compressor and carry out the hydrogen circulation, control hydrogen is 1000: 1 with the catalyst volume ratio, and temperature of reactor is risen to 180 ℃.
The example 1 described moisture raw material that is no more than 5ppm is introduced reaction unit, at 180 ℃, Hydrogen Vapor Pressure 1.6MPa, mass space velocity 2.0h
-1, hydrogen/hydrocarbon molecule is than being to carry out isomerization reaction under 2.5 the condition.The online detection of water content dew point hygrometer (Britain SHOW company produces the SD-R type) in the reactor inlet gas, product liquid and product flashed vapour are formed with chromatograph (Tianjin, island GC-8A) analysis, with product C
5Isomerization rate, C
6Isomerization rate is represented catalyst activity.
After obtaining raw water content and being no more than response data under the 5ppm condition, be converted into the oxygen molal quantity of water correspondence under the described conditions by ethanol, in raw material, add absolute ethyl alcohol (analyzing pure) respectively, water content in the raw material is increased to 30ppm (saturated dissolving water) or 50ppm (over-saturation dissolving water).Observe the catalyst activity reduction situation after the raw material water filling, as product C
5During isomerization rate≤60 quality %, stop in reactor, to feed reaction raw materials, the used carrier gas of reaction is circulated by the drying chamber that is connected in series with in the recycle hydrogen pipeline, remove moisture in the circulating hydrogen with example 1 described circulating air drying chamber, make the water content in the reactor inlet gas be no more than 25ppm.Under 0.4MPa, 220～260 ℃, circulating hydrogen and the condition of catalyst volume than 1000: 1 with circulating hydrogen to decaying catalyst activation 3～12 hours.
Activation finishes the back and presses initial reaction condition and method, again the raw material of the moisture 5ppm of being no more than is introduced the reaction result that reaction system reacts and obtain the activation rear catalyst.
Response data before and after each example catalyst inactivation, cause catalysqt deactivation the raw material water injection rate, with the condition of circulating hydrogen activating catalyst, water content in the recycle hydrogen and activation afterreaction the results are shown in Table 3, table 4, wherein example 6 be to example 3 activation rear catalysts carry out water filling second time inactivation and activate after the result.
From table 3, table 4 as can be seen, for the catalyst because of the moisture too high serious inactivation of raw material, after the activation of employing the inventive method, catalyst activity can return to the preceding level of inactivation.
Example 9
By the method for example 3 carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, activation recovers active experiment, the activation temperature of different is decaying catalyst is 180 ℃, the results are shown in Table 5.
Example 10
By the method for example 3 carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, activation recovers active experiment, the activation temperature of different is decaying catalyst is 300 ℃, the results are shown in Table 5.
Example 11
By the method for example 3 carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, activation recovers active experiment, the soak time of different is decaying catalyst is 3 hours, the results are shown in Table 5.
Example 12
By the method for example 7 carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, activation recovers active experiment, the activation temperature of different is decaying catalyst is 180 ℃, the results are shown in Table 5.
By table 5 data as can be known, when activation temperature lower (180 ℃) or too high (300 ℃), activation effect is relatively poor, and soak time is also influential to activation results, and soak time is short, and then effect is poor slightly.
Comparative Examples 1
Carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, the active experiment of activation recovery by the method for example 4, different is the recycle hydrogen undried that is used for activating catalyst, the average water content of reactor inlet hydrogen is 1420ppm in the activation process, the results are shown in Table 6.
Comparative Examples 2
Carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, the active experiment of activation recovery by the method for example 7, different is the recycle hydrogen undried that is used for activating catalyst, the average water content of reactor inlet hydrogen is 830ppm in the activation process, the results are shown in Table 6.
Table 6 data declaration does not reduce the water content in the circulating hydrogen in activation process, activation effect is very poor.
Comparative Examples 3
Carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, the active experiment of activation recovery by the method for example 3, different is the dried feed haptoreaction of decaying catalyst elder generation and the moisture 5ppm of being no more than, with the recycle hydrogen that reduces water content decaying catalyst is activated again, the results are shown in Table 6.
Comparative Examples 4
Carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, the active experiment of activation recovery by the method for example 7, different is the dried feed haptoreaction of decaying catalyst elder generation and the moisture 5ppm of being no more than, with the recycle hydrogen that reduces water content decaying catalyst is activated again, the results are shown in Table 6.
Example 13
After treating the catalyst activation experiment of Comparative Examples 3, water filling 50ppm in raw material stops charging behind the catalysqt deactivation once more, catalyst is activated after the water content in the recycle hydrogen is reduced with drier again, the results are shown in Table 7.
Example 14
After treating the catalyst activation experiment of Comparative Examples 4, water filling 30ppm in raw material stops charging behind the catalysqt deactivation once more, catalyst is activated after the water content in the recycle hydrogen is reduced with drier again, the results are shown in Table 7.
Contrast table 6, table 7 data as can be known, it is fine not contact the effect that the low water content raw material directly activates before the decaying catalyst activation, and the effect that activates again behind the contact low water content raw material is relatively poor.
Example 15
Carry out the evaluation of catalyst initial reaction performance, raw material water filling inactivation, the active experiment of activation recovery by the method for example 4, different is that employing nitrogen is that circulating air activates, nitrogen content is greater than 99.99 volume % in the nitrogen, oxygen content is less than 0.01 volume %, and water content is no more than 10ppm after drying.With the hydrogen emptying of reaction system, introduce drying nitrogen before the activation, activation end back is carried out catalyst and is recovered active investigation with nitrogen in the hydrogen exchange system, the results are shown in Table 7.
The result shows, with nitrogen decaying catalyst is activated, and the catalyst activated activity also can be near the level before the inactivation.
Table 1
Hydrocarbon system's kind content, quality %
Carbon 4 0.05
Isomery carbon 5 1.43
Positive structure carbon 5 57.67
Isomery carbon 6 7.02
Positive structure carbon 6 29.55
Carbon six cycloalkanes 4.13
Benzene 0.08
Carbon 7 0.07
Table 2
Constituent content, quality %
Pt 0.2
Sulphur 2.3
Al
2O
3 50.0
SiO
2 2.5
ZrO
2 45.0
Table 3
Table 4
Table 5
Table 6
Table 7
Claims (11)
- In the course of reaction because of the SO of raw water too high levels inactivation 4 2-/ ZrO 2The activation method of solid super acid catalyst, comprise and stop in reactor, to feed reaction raw materials, to wherein feeding hydrogen or nitrogen and circulation as circulating air, circulating air is reduced to the circulating air water content below the 50ppm with drier, under 180～280 ℃, 0.1～1.0MPa condition with the catalyst of circulating air activation inactivation.
- 2. in accordance with the method for claim 1, it is characterized in that the water content in the circulating air is 3～25ppm.
- 3. in accordance with the method for claim 1, it is characterized in that temperature with circulating air activation decaying catalyst is that 200～270 ℃, pressure are 0.3～0.5MPa.
- 4. in accordance with the method for claim 1, it is characterized in that described drier is A type molecular sieve, silica gel, aluminium oxide or active carbon.
- 5. in accordance with the method for claim 1, the catalysqt deactivation that causes when it is characterized in that water content in the raw material is 20～30ppm is 200～240 ℃ with the temperature of circulating air activation decaying catalyst.
- 6. in accordance with the method for claim 1, the catalysqt deactivation that causes when it is characterized in that water content in the raw material surpassed 40ppm is 220～260 ℃ with the temperature of circulating air activation decaying catalyst.
- 7. in accordance with the method for claim 1, it is characterized in that described solid super acid catalyst comprises the mixed oxide carrier of the sulfur loaded acid group of the VIII family metal of 0.05～2.0 quality % and 98.0～99.5 quality %, described mixed oxide carrier comprises the zirconia of 20～49 quality %, the aluminium oxide of 9～50 quality % and the silica of 1～52 quality %, and the sulfur content in the catalyst is 0.5～3.5 quality %.
- 8. in accordance with the method for claim 7, it is characterized in that described VIII family metal is platinum, palladium or nickel.
- 9. in accordance with the method for claim 1, it is characterized in that described raw material is C 4～C 7Light naphthar.
- 10. in accordance with the method for claim 1, it is characterized in that the raw water content that causes catalysqt deactivation surpasses 15ppm.
- 11. in accordance with the method for claim 1, it is characterized in that described circulating air is employed circulating hydrogen in the course of reaction.
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| CN102553658B (en) * | 2011-08-16 | 2014-04-09 | 中国海洋石油总公司 | Regeneration method of deacidification catalyst for refining biodiesel and refining of biodiesel |
| CN104437591B (en) * | 2013-09-23 | 2016-08-24 | 中国石油化工股份有限公司 | The activation method of the solid super acid catalyst inactivated because of raw water too high levels |
| CN107344124B (en) * | 2016-05-06 | 2020-02-28 | 中国石油化工股份有限公司 | In-situ regeneration method of solid super acidic catalyst |
| CN113791159B (en) * | 2021-09-07 | 2023-11-28 | 山东非金属材料研究所 | Device and method for detecting equivalent water content in nitrous oxide propellant |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1144141A (en) * | 1994-05-07 | 1997-03-05 | 环球油品公司 | Periodic regeneration of deactivated solid alkylation catalyst with hydrogen |
| CN101062485A (en) * | 2006-04-26 | 2007-10-31 | 上海博源精细化工有限公司 | Regeneration method for nickel-base hydrogenation catalyst |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1144141A (en) * | 1994-05-07 | 1997-03-05 | 环球油品公司 | Periodic regeneration of deactivated solid alkylation catalyst with hydrogen |
| CN101062485A (en) * | 2006-04-26 | 2007-10-31 | 上海博源精细化工有限公司 | Regeneration method for nickel-base hydrogenation catalyst |
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| JP特开平10-15399A 1998.01.20 |
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| GR01 | Patent grant | ||
| CI01 | Correction of invention patent gazette |
Correction item: Patentee|Address|Co-patentee Correct: Sinopec Corp.|100029 Beijing City, Chaoyang District Hui Street No. 6|SINOPEC Research Institute of Petroleum Processin False: SINOPEC Research Institute of Petroleum Processin|100083 No. 18, Haidian District, Beijing, Xueyuan Road Number: 06 Volume: 27 |
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| ERR | Gazette correction |
Free format text: CORRECT: PATENTEE; ADDRESS; CO-PATENTEE; FROM: SINOPEC RESEARCH INSTITUTE OF PETROLEUM PROCESSING;100083 NO. 18, XUEYUAN ROAD, HAIDIAN DISTRICT, BEIJING TO: CHINA PETROCHEMICAL CO., LTD.;100029 NO. A-6, HUIXIN EAST STREET, CHAOYANG DISTRICT, BEIJING; SINOPEC RESEARCH INSTITUTE OF PETROLEUM PROCESSING |