CN1049301A - Noble metals load-carbon oxide accelerator - Google Patents
Noble metals load-carbon oxide accelerator Download PDFInfo
- Publication number
- CN1049301A CN1049301A CN 89106165 CN89106165A CN1049301A CN 1049301 A CN1049301 A CN 1049301A CN 89106165 CN89106165 CN 89106165 CN 89106165 A CN89106165 A CN 89106165A CN 1049301 A CN1049301 A CN 1049301A
- Authority
- CN
- China
- Prior art keywords
- cracking catalyst
- carrier
- combustion adjuvant
- matrix
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Catalysts (AREA)
Abstract
The present invention relates to noble metals load-carbon oxide accelerator, its active component is 1-1000ppm platinum or 50-1000ppm palladium, and carrier is by microsphere particle and (2) 0.5-50%Al of Cracking catalyst or its matrix of (1) 99.5-50%
2O
30-20%RE
2O
3And 0-15%ZrO
2Form, (2) are the external coatings of (1) particle.The preparation method coats aluminium colloidal sol with microspherical catalyst or its matrix or contains an amount of rare earth or/and the aluminium colloidal sol of zirconium, drying, roasting again, carries steps such as platinum or palladium and gets final product.This combustion adjuvant has good activity, stability, intensity and fluidizing performance, method for making is easy, economical.
Description
The present invention relates to noble metals load-carbon oxide accelerator.
In catalytic cracking process, contact with hydrocarbon molecule at catalyst in reactor, promote it to be cracked into less hydrocarbon molecule, catalyst self deposition has gone up coke simultaneously.The catalyst of these cokings is transported to regenerates in the regenerator to recover its activity.
In regenerator, long-pending burnt catalyst at high temperature contacts with oxygen-containing gas, Jiao of deposition changes into CO and CO
2If these CO emit with flue gas, the meeting contaminated air, and lost liberated heat by CO completing combustion institute; If rise to the dilute phase bed on regenerator top with catalyst, further burning (after-burning) is emitted a large amount of heats catalyst and regenerator device is damaged; Thereby CO concentration is very necessary in the reduction regenerator.
Adopting the CO combustion adjuvant is the effective means that reduces CO concentration, and it can promote CO completing combustion, reduces the carbon deposition quantity on the Cracking catalyst.The active component of general combustion adjuvant has metals such as Pt, Pd, Ir, Rh, Os, Ru, Cu, wherein the most frequently used Pt and Pd, and its occupation mode has following several:
(1) adds in the regenerator (USP4118339) with the solution form.Because corrosion device, operate dumbly, the platinum consumption is big, and institute is seldom use in this way.
(2) as one of catalytic component.The catalyst of reporting among the USP4151121 contains 2～20% molecular sieves, 2～100ppmPt and inorganic oxide carrier.The catalyst of reporting among the USP409741 is made up of REX or REY, the USY that contains 500～5000ppm noble metal and inorganic oxide carrier.The Pt consumption is big in this kind mode, and the CO oxidation stability is poor, and catalyst uses dumb.
(3) be stated from and make combustion adjuvant on the carrier, directly add in the regenerator or and use with catalyst mix.This kind mode platinum consumption is few, and flexible and convenient operation.
The carrier of combustion adjuvant has inorganic oxide, as (USP4341623, USP350615 such as aluminium oxide, silica, silica one aluminium oxide, USP4148751, USP4222856), clay (USP4171286, USP4214978, USP4214978), and A type molecular sieve (USP3364136) or the like.Wherein the most frequently used is aluminium oxide or salic inorganic oxide, and domestic also mostly is to adopt aluminium oxide as combustion-supporting carrier.
Best to the dispersion of Pt with aluminium oxide in the above carrier, gained combustion adjuvant oxidation activity is good.But its complicated process of preparation, price is expensive, and intensity is relatively poor, after the high-temperature roasting, is powdery substantially especially, and wear-resisting and fluidizing performance can not satisfy industrial requirements.If with the amorphous aluminum silicide is carrier, the decentralization of Pt can not show a candle to aluminium oxide, but its preparation method is simple, and cheap, intensity is good.When being carrier with salic inorganic oxide, combustion adjuvant has good active and stability, but generally will pass through high-temperature roasting in the preparation process, and this just has certain requirement to equipment, and power consumption is big, and product strength is also relatively poor.
The combustion adjuvant of reporting among the USP3870455 is that the platinum group metal with 0.1～20 heavy % is an active component, and its carrier can be 50～95 heavy % aluminium oxide, 2～25 heavy % rare earth oxides and 2～25 heavy % chromium oxide and/or zirconias.Its preparation method is: make the carrier that contains above-mentioned inorganic oxide with infusion process or coprecipitation, this carrier being not less than 850 ℃ (best 900～1200 ℃) following roasting 2 hours, is soaked platinum again.
In Preparation of Catalyst, people are in order to improve activity of such catalysts and stability is often handled carrier, reported among the US3231520 catalyst carrier surface has been coated with one deck method of alumina: carrier has been contacted with alkali-metal aluminate solution, make its surface form one deck coating, roasting again.Introduced a kind of cleaning catalyst for tail gases of automobiles among the J60025544A, its preparation method is that cordierite carrier is immersed by 300 parts of (weight) aluminium colloidal sols, 60 parts of aluminum nitrates, 300～400 parts of water are in the solution of 40 parts of lanthanum carbonates and 830 parts of δ and/or θ aluminium oxide, through 150 ℃ of dryings 3 hours, 600 ℃ of roastings 3 hours are immersed cerous nitrate solution, the platinum salting liquid again, then be in the rhodium chloride solution, last drying and roasting get final product.
At the deficiencies in the prior art, the purpose of this invention is to provide a kind of prior art that is different from, and the preparation method is easy, have the CO combustion promoter of excellent activity, stability and physical and chemical performance.
Combustion adjuvant active component provided by the invention is 1～1000ppm platinum or 50～1000ppm palladium, and carrier is by (it is heavy to account for carrier) (1) 99.5～50% Cracking catalyst or the microsphere particle of its matrix and (2) 0.5～50%Al
2O
3, 0～20%RE
2O
3With 0～15%ZrO
2Form, (2) exist as the coating of particle (1) outer surface.
Said Cracking catalyst is the complete synthetic or semi-synthetic Cracking catalyst of preparing with conventional method.Full synthesising cracking catalyst is made up of molecular sieve active component and inorganic oxide matrix, and molecular sieve can be one or more of each molecular sieve analog of being used for catalytic cracking catalyst such as faujasite, ZSM zeolite, modenite, clay molecular sieve with layer structure.Inorganic oxide matrix can be the inorganic oxide as full synthesising cracking catalyst carrier such as aluminium oxide silicon monoxide, silica one magnesia.Semi-synthetic Cracking catalyst can be made up of above-mentioned molecular sieve active component and matrix, this matrix contains inorganic oxide and clay, inorganic oxide can be aluminium oxide, silica, silica one aluminium oxide etc., their precursor is an employed bonding agent in the semi-synthetic Cracking catalyst preparation process, as aluminium colloidal sol, Ludox, hydrated alumina, silicon-aluminum sol or gel etc.; Clay can be the various clays as semi-synthetic cracking catalyst carrier such as kaolin, halloysite.
Combustion adjuvant provided by the invention can be made by following method:
(1) with microballoon Cracking catalyst or its matrix 500～800 ℃ of following roastings 1～4 hour.
(2) with (1) gains and an amount of aluminium colloidal sol or an amount of aluminium colloidal sol and rare earth or/and the mixed liquor of zirconium salt solution mix, the consumption of solution with the pore volume of saturated microballoon after after 0～10% degree of being of metering-orifice volume, placed 0～48 hour, ℃ following drying is more than 0.5 hour in room temperature～200, at 450～800 ℃, best 550～650 ℃, following roasting 0.5～4 hour promptly gets the carrier of combustion adjuvant provided by the present invention.
(3) press the preparation method of noble metal supported catalyst routine, load platinum or palladium on combustion-supporting carrier.
Said Cracking catalyst can be the dead catalyst that draws off from catalytic cracking unit in said method, also can be the poising agent of Cracking catalyst, can also be fresh dose.The matrix of said Cracking catalyst is to synthesize entirely or semi-synthetic production of cracking catalyst according to routine respectively, save the step that relates to molecular sieve, the slurries that will contain the precursor of the inorganic oxide that is used as full synthesising cracking catalyst carrier, or contain clay and bonding agent as semi-synthetic cracking catalyst carrier, obtain as the slurries spray-drying of aluminium colloidal sol, Ludox or silicon-aluminum sol or gel.
Because raw material of the present invention can be dead catalyst or balance Cracking catalyst, can also be the preparation carrier of cracking, thereby raw material sources be convenient, economical; The combustion adjuvant of being made is oxidation activity height (about 90% or more than) not only, good stability, and also fluidizing performance and anti-wear performance (its abrasion index is 0.3～1.3, and general Cracking catalyst＞2) satisfying the catalytic cracking process requirement, heap is than big (＞1.0).Use this combustion adjuvant can reduce the loss of platinum.
The following examples will the present invention will be further described.
Example 1
Prepare combustion adjuvant provided by the invention.
(1) 188 kilogram kaolin (the Suzhou machine selects 2#) adds the making beating of 533 liter deionized waters, add 15.6 kilograms of hydrochloric acid (technical grades, concentration 30 heavy %), stir, add 71 kilograms in the wet glue of boehmite (Zhou village catalyst plant, salic 35 heavy %), kept 1 hour down at 60 ℃, cooling, spray-drying promptly gets semi-synthetic aluminium oxide-kaolin microsphere.
With this microballoon 600 ℃ of following roastings 1 hour.
(2) 2.2 gram aluminum solutions glue (the Zhou village catalyst plant contains aluminium 11.6 heavy %) and 3.3 ml concns are that 16 mg/ml are (with RE
2O
3Meter) rare earth chloride (Shanghai Yuelong Chemical Plant, technical grade) solution mixes
(3) 5 gram (1) thus obtained microspheres are mixed with (2) gained solution, place half an hour, drying is 3 hours under 60 ℃, 550 ℃ of following roastings 2 hours, promptly gets by 89.9 heavy % kaolin-aluminum oxide micro-sphere particles and 9.1 heavy %Al
2O
3Reach 1 heavy %RE
2O
3The combustion-supporting carrier formed of the external coating that is coated in above-mentioned particle outer surface.
(4) 5 ml concns are that the platinum acid chloride solution of 0.5 mg/ml (in platinum) (is dissolved in the platinum bits in the chloroazotic acid, adds hydrochloric acid and be heated to NO
2Till catching up with to the greatest extent) in add the hydrochloric acid that 3 concentration are 15 heavy %, add (3) gained carrier again, mix, 90 ℃ dry 2 hours down, promptly get the combustion adjuvant A of platiniferous 500ppm.
Example 2
Prepare combustion adjuvant provided by the invention.
With 0.43 gram aluminium colloidal sol (containing the heavy % of Al11.6), 3.3 ml concns are that 15.3 mg/ml are (with RE
2O
3Meter) re chloride mixes, and adds 5 gram examples 1 (1) step gains, is mixed, placed 5 hours, 100 ℃ dry 2 hours down, 700 ℃ of following roastings 1 hour promptly get by 97 heavy % kaolin one alumina particles and 2 and weigh %Al
2O
3Reach 1 heavy %RE
2O
3The combustion-supporting carrier that external coating is formed.
Above-mentioned carrier is immersed in the platinum acid chloride solution that 5 ml concns are 0.5 mg/ml (in platinum), and 100 ℃ of dryings 2 hours promptly get the combustion adjuvant B of platiniferous 500ppm.
Example 3
Preparation combustion adjuvant of the present invention on middle-scale device.
The method of pressing example 1 prepares 400 kilograms of combustion adjuvant C on middle-scale device, just restrain the aluminium colloidal sols with 12.93 in (2) step, 3.3 liter re chlorides (concentration 106 gram RE
2O
3/ liter) and 12 liter zirconium oxychloride solutions (concentration 33 gram Zr/ liters, Beijing chemical reagent factory).(3) step restrained microspheroidal kaolin-aluminium oxide with 400 liters.(4) step platinum acid chloride solution 8 liters.
Gained combustion adjuvant C is by the particle of 93.16 heavy % kaolin-aluminium oxide and 5.7 heavy %Al
2O
3, 1.0 heavy %RE
2O
3Reach 0.14 heavy %ZrO
2The carrier loaded 100ppm platinum formed of external coating.
Example 4
Prepare combustion adjuvant of the present invention.
Preparing combustion adjuvant D by example 1 method, is the palladium chloride solution replacement platinum acid chloride solution of 0.5 milliliter/milliliter (in palladium) with 5 ml concns just, and combustion adjuvant D contains the 500ppm palladium.
Example 5
Prepare combustion adjuvant of the present invention.
5 grams are total to Y catalyst (the full synthesising cracking catalyst of Y-type rare earth from the discarded 3# that catalytic cracking unit draws off, the Wuhan oil plant), 700 ℃ of following roastings 2 hours, adding 2 gram aluminium colloidal sols (containing aluminium 12.73 heavy %) and 4 milliliters goes in the dried up mixed liquor, mix, after 2 hours 150 ℃ dry 2 hours down, 550 ℃ of following roastings 4 hours promptly get and contain 90.6 heavy % Cracking catalyst and 9.4 heavy %Al
2O
3Combustion-supporting carrier.
This carrier is immersed in 5 milliliters of platinum acid chloride solutions (platiniferous 0.5 mg/ml), and 100 ℃ of dryings 3 hours promptly get the combustion adjuvant E of platiniferous 500ppm.
Example 6
Prepare combustion adjuvant of the present invention.
Method preparation by example 5 contains 81.1 heavy % Cracking catalyst and 18.9 heavy %Al
2O
3Carrier and the combustion adjuvant F of 500ppm platinum, just replace 2 to restrain the aluminium colloidal sols with 4 gram aluminium colloidal sols.
Example 7
Prepare combustion adjuvant of the present invention.
5 gram 3# Y Cracking catalyst poising agent altogether (contain RE with 2 gram aluminium colloidal sols (containing the heavy % of Al12.73), 0.5 milliliter of rare earth chloride again 750 ℃ of following roastings 1 hour
2O
330.6 mg/ml) mixed liquor of solution and 4 ml waters mixes, after half an hour 50 ℃ dry 10 hours down, 550 ℃ of roastings 4 hours promptly get and contain 97.1 heavy % Y Cracking catalyst and 1.9 heavy %Al altogether
2O
3Reach 1 heavy %RE
2O
3The combustion-supporting carrier of external coating.
This carrier is soaked platinum by the method for example 4, promptly get the combustion adjuvant G of platiniferous 500ppm.
Example 8～9
Prepare combustion adjuvant of the present invention.
Prepare combustion adjuvant H and I by example 7 methods, just prepare 85.6 heavy % Cracking catalyst and 9.4 heavy %Al with 2.5 milliliters of re chlorides
2O
3Reach 5.0 heavy %RE
2O
3The carrier of combustion adjuvant H of external coating, contain 80.6 heavy % Cracking catalyst and 9.4 heavy %Al with 5 milliliters of re chlorides preparations
2O
3Reach 10 heavy %RE
2O
3The carrier of the combustion adjuvant I of external coating.
Example 10
Prepare combustion adjuvant of the present invention.
2.2 gram aluminum solutions (containing the heavy % of Al11.6) and 1.7 milliliters of re chlorides (contain RE
2O
315.3 mg/ml) mix, add through 550 ℃ of roastings after 2 hours partially-Y Cracking catalyst (Y-type rare earth contains synthesising cracking catalyst, Lanzhou Oil Refinery) 5 grams, mix, under the room temperature dry 5 days, 500 ℃ of following roastings 4 hours.Promptly get and contain inclined to one side Y Cracking catalyst of 91.9 heavy % and 7.6 heavy %Al
2O
3Reach 0.5 heavy %RE
2O
3The combustion-supporting carrier of external coating.
This carrier is immersed in 1 milliliter of platinum acid chloride solution, and 200 ℃ of dryings 2 hours promptly get combustion adjuvant J.
Example 11～12
Prepare combustion adjuvant of the present invention.
Method preparation by example 10 helps right agent K and L, just: with Y-4 (the full synthesising cracking catalyst of Y-type rare earth, Lanzhou Oil Refinery) Preparation of Catalyst combustion adjuvant K.(Lanzhou Oil Refinery contains 13 heavy %Al with the amorphous aluminum silicide microballoon
2O
3) preparation combustion adjuvant L.
Example 13
Estimate the oxidation activity and the stability of combustion adjuvant.
On the small fixed flowing bed device, estimate oxidation activity and the stability of combustion adjuvant A～L, and and contrast combustion adjuvant contrast-1. contrast-2, contrast-3, contrast-4 and contrast-5 make comparisons.The regenerative response condition is: catalyst to be regenerated 30 grams add an amount of combustion adjuvant makes the platinum amount account for the 0.2ppm (except the combustion adjuvant C) of catalyst, 600 ℃ of reaction temperatures, and air mass flow 1500 liters/minute, 2 minutes reaction time.The oxidation activity of combustion adjuvant is expressed as:
R in the base
BCO in the flue gas during for no combustion adjuvant
2/ CO ratio, R are the CO when combustion adjuvant is arranged
2/ CO ratio.
Oxidation activity after the aging activity that to be combustion adjuvant go out through 800 ℃, the burin-in process post-evaluation in 4 hours of 100% water vapour.Reaction result sees Table 1.
The activity of combustion adjuvant provided by the invention and stability all are higher than the not contrast combustion adjuvant of aluminising of carrier as can be seen from Table 1.
Contrast-1 combustion adjuvant is by 1000ppm platinum and r-Al
2O
3Microballoon is formed.
Contrast-2 combustion adjuvants are by 500ppm platinum and Al
2O
3-kaolin (Al
2O
325 heavy %, kaolin 75 heavy %) to form, its preparation method is: with the Al of the 1st step of example 1 gained
2O
3-kaolin support is by the 4th step method load platinum.Contrast-3 combustion adjuvants are by 500ppm platinum, 1 heavy %RE
2O
3And Al
2O
3-kaolin is formed, and its preparation method is: with the Al of the 1st step of example 1 gained
2O
3-kaolin support 5 grams immerse 5 milliliters of platinum acid chloride solutions (containing 0.5 milligram of platinum/milliliter), 3.3 milliliters of re chlorides (contain 15.3 milligrams of RE
2O
3/ milliliter) and in the mixed liquor of 2 hydrochloric acid (1 part of 35% concentrated hydrochloric acid dilutes with 1 part of water), placed 2 hours 100 ℃ of dryings 2 hours.Contrast-4 combustion adjuvants and form, carry platinum method and the 4th step of example 1 together by 500ppm platinum and inclined to one side Y Cracking catalyst.Contrast-5 combustion adjuvants are U.S. FILTROX-H combustion adjuvant (platiniferous 2000ppm).
Table 1
| Combustion adjuvant | Carrier is formed | The heavy ppm of Pt | Oxidation activity % | The aging active % in back | Remarks | |||
| Matrix | External coating, heavy % | |||||||
| Al 2O 3 | RE 2O 3 | ?ZrO 2 | ||||||
| A B C D E F G H I J K L contrast-1 contrast-2 contrasts-3 contrasts-4 contrasts-5 | Al 2O 3-kaolin | ?9.1????????????1?????????????0?????????500 | ????90 | ????82.5 | It is that Pd * * rare earth is dipped on the carrier with Pt that Pt accounts for catalyst 0.2ppm 0.1ppm 0.05ppm * active component | |||
| Al 2O 3-kaolin | ?2??????????????1?????????????0?????????500 | ????93 | ????70 | |||||
| Al 2O 3-kaolin | ?5.7????????????1?????????????0.14??????100 | ????97 ????92 ????86 | ????80 ????80 ????78 | |||||
| Al 2O 3-kaolin | ?9.1????????????1?????????????0?????????500* | ????86.7 | ????- | |||||
| Altogether-Y 3The # dead catalyst | ?9.4????????????0?????????????0?????????500 | ????89 | ????70 | |||||
| ?????″ | ?18.9???????????0?????????????0?????????500 | ????89 | ????70 | |||||
| Altogether-Y 3The # poising agent | ?1.9????????????1?????????????0?????????500 | ????89 | ????79 | |||||
| ?????″ | ?9.4????????????5?????????????0?????????500 | ????91 | ????72 | |||||
| ?????″ | ?9.4????????????10????????????0?????????500 | ????88 | ????80 | |||||
| Partially-Y | ?7.6????????????0.5???????????0?????????100 | ????97 | ????- | |||||
| Y-4 | ?7.6????????????0.5???????????0?????????100 | ????96 | ????- | |||||
| Amorphous aluminum silicide | ?7.6????????????0.5???????????0?????????100 | ????92 | ????- | |||||
| r-Al 2O 3Al 2O 3-kaolin Al 2O 3-kaolin-RE 2O 3* partially-Y | ?0??????????????0?????????????0?????????1000 ?0??????????????0?????????????0?????????500 ?0??????????????0?????????????0?????????500 ?0??????????????0?????????????0?????????500 ????????????????????????????????????????2000 | ????82 ????61 ????85 ????86 ????52 | ????50 ????53 ????60 ????43.3 ????40 | |||||
Example 14
Estimate the physical property of combustion adjuvant.
The semi-synthetic Al of combustion adjuvant C and raw material thereof
2O
3The physical property of-kaolin microsphere, contrast-1 combustion adjuvant and inclined to one side Y Cracking catalyst sees Table 2, the surface area determination of nitrogen adsorption, pore volume is to measure with the water droplet method, abrasion index is represented with the percentage (pneumatic) of per hour wearing and tearing, bulk density is represented by apparent bulk density, determines size distribution with the MALVERN3600E laser particle size analyzer.
As can be seen from Table 2, combustion adjuvant provided by the invention has kept the physical property close with Cracking catalyst, and its size distribution satisfies the needs of fluidisation attitude, and screening is concentrated, fine powder is few, and intensity is better than general Cracking catalyst (general Cracking catalyst abrasion index 2～4).Heap is than big.
| Surface area rice 2/ gram | Pore volume milliliter/gram | Abrasion index %/hour | The bulk density grams per milliliter | Size distribution, heavy % | |||||
| 0～ 160u | 0～ 113u | ?0～ ?84u | 0～ 39u | ?0～ ?19u | |||||
| Combustion adjuvant C Al 2O 3-kaolin microsphere contrast-1 inclined to one side-Y | ??61??????????0.16?????????0.3????????????＞1.0????????95.4????77.9?????46.8?????5.3??????0 ??70～100?????0.2??????????0.7????????????0.9～1.0?????94.7????82.7?????62.4?????20.3?????4.4 ???????????????????????????＞6????????????1～1.2???????84.4????71.9?????57.0?????26.2?????10.1 ??606?????????0.65?????????3.4????????????0.48?????????88.3????73.4?????57.8?????20.?7????4.8 | ||||||||
Claims (7)
1, a kind of noble metals load-carbon oxide accelerator, active component is platinum or the 50～1000ppm palladium of 1～1000ppm, it is characterized in that its carrier is by (it is heavy to account for carrier) (1) 99.5～50% Cracking catalyst or the microsphere particle of its matrix and (2) 0.5～50%Al
2O
3, 0～20%RE
2O
3With 0～15%ZrO
2Form, (2) exist as the coating of particle (1) outer surface, and its preparation method is:
(1) with microballoon Cracking catalyst or its matrix 500～800 ℃ of following roastings 1～4 hour.
(2) with (1) gains and an amount of aluminium colloidal sol or an amount of aluminium colloidal sol and rare earth or/and the mixed liquor of zirconium salt solution mix, the consumption of solution with saturated microballoon pore volume after after 0～10% degree of being of metering-orifice volume, placed 0～48 hour, ℃ following drying is more than 0.5 hour in room temperature～200,450～800 ℃ of following roastings 0.5～4 hour, promptly get carrier.
(3) press the conventional preparation method of noble metal carrier catalyst, load platinum or palladium on carrier.
2, according to the described combustion adjuvant of claim 1, it is characterized in that said Cracking catalyst is full synthesising cracking catalyst, it is by one or more molecular sieves in faujasite, ZSM zeolite, modenite and the clay molecular sieve with layer structure, form with inorganic oxide matrix, inorganic oxide matrix is aluminium oxide silicon monoxide or silica one magnesia.
3, according to the described combustion adjuvant of claim 1, it is characterized in that said Cracking catalyst is semi-synthetic Cracking catalyst, it is by one or more molecular sieves in faujasite, ZSM zeolite, modenite and the clay molecular sieve with layer structure, form with matrix, matrix is salic, a kind of inorganic oxide in silica and silica one aluminium oxide and comprise kaolin and the high mountain range of many water on a kind of clay.
4, by the said combustion adjuvant of claim 1, it is characterized in that the Cracking catalyst among the said preparation method is dead catalyst or the poising agent that draws off from catalytic cracking unit.
5, according to the described combustion adjuvant of claim 1, it is characterized in that the microspheroidal Cracking catalyst matrix among the said preparation method is complete routinely synthesising cracking catalyst preparation method, save the step that relates to molecular sieve, the slurries spray-drying that will contain the inorganic oxide precursor that is used as full synthesising cracking catalyst carrier obtains.
6, according to the described combustion adjuvant of claim 1, it is characterized in that the microspheroidal Cracking catalyst matrix among the said preparation method is semi-synthetic routinely production of cracking catalyst, save the step that relates to molecular sieve, to contain clay and inorganic oxide bonding agent as semi-synthetic cracking catalyst carrier, obtain as the slurries spray-drying of aluminium colloidal sol, Ludox, hydrated alumina, silicon-aluminum sol or gel.
7,, it is characterized in that the sintering temperature among the said preparation method is 550～650 ℃ according to the described combustion adjuvant of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89106165 CN1022843C (en) | 1989-08-09 | 1989-08-09 | Noble metals load-carbon oxide accelerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 89106165 CN1022843C (en) | 1989-08-09 | 1989-08-09 | Noble metals load-carbon oxide accelerator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1049301A true CN1049301A (en) | 1991-02-20 |
| CN1022843C CN1022843C (en) | 1993-11-24 |
Family
ID=4856648
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 89106165 Expired - Fee Related CN1022843C (en) | 1989-08-09 | 1989-08-09 | Noble metals load-carbon oxide accelerator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1022843C (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102294241A (en) * | 2011-06-30 | 2011-12-28 | 福州大学 | Preparation method and application of Pd/modified bauxite catalyst |
| CN105562031A (en) * | 2016-02-02 | 2016-05-11 | 青岛康洁聚能科技有限公司 | Catalyst for reducing content of NOx in FCC smoke |
| CN107022390A (en) * | 2017-06-21 | 2017-08-08 | 黄河三角洲京博化工研究院有限公司 | A kind of CO combustion promoter and preparation method thereof |
| CN117718040A (en) * | 2023-12-22 | 2024-03-19 | 青岛康洁聚能科技有限公司 | Carbon monoxide combustion improver and preparation method thereof |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1074449C (en) * | 1996-10-14 | 2001-11-07 | 中国石化洛阳石油化工工程公司炼制研究所 | Carbon monoxide bombustion adjuvant and preparing process thereof |
| TWI786147B (en) | 2017-07-05 | 2022-12-11 | 中國大陸商中國石油化工科技開發有限公司 | Composition capable of reducing CO and NOx emissions, its preparation method and application, and fluidized catalytic cracking method |
-
1989
- 1989-08-09 CN CN 89106165 patent/CN1022843C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102294241A (en) * | 2011-06-30 | 2011-12-28 | 福州大学 | Preparation method and application of Pd/modified bauxite catalyst |
| CN105562031A (en) * | 2016-02-02 | 2016-05-11 | 青岛康洁聚能科技有限公司 | Catalyst for reducing content of NOx in FCC smoke |
| CN105562031B (en) * | 2016-02-02 | 2018-02-02 | 青岛康洁聚能科技有限公司 | A kind of catalyst for being used to reduce NOx content in FCC flue gases |
| CN107022390A (en) * | 2017-06-21 | 2017-08-08 | 黄河三角洲京博化工研究院有限公司 | A kind of CO combustion promoter and preparation method thereof |
| CN117718040A (en) * | 2023-12-22 | 2024-03-19 | 青岛康洁聚能科技有限公司 | Carbon monoxide combustion improver and preparation method thereof |
| CN117718040B (en) * | 2023-12-22 | 2024-07-26 | 青岛康洁聚能科技有限公司 | Carbon monoxide combustion improver and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1022843C (en) | 1993-11-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1040422C (en) | Method for preparation of light alkene by dehydrogenation from relative paraffin | |
| CN1089024C (en) | Diesel engine exhaust gas catalyst and method of use thereof | |
| EP1879982B1 (en) | Co oxidation promoters for use in fcc processes | |
| US4587231A (en) | Method of producing monolithic catalyst for purification of exhaust gas | |
| CN1090533C (en) | Process for the preparation of fluid bed vinyl acetate catalyst | |
| EP0596552A1 (en) | Catalyst for treatment of diesel exhaust particulate | |
| CN1082018A (en) | Process for dehydrogenating light paraffins in the fluidized-bed reactor | |
| CN1684766A (en) | Cooxidation promoters for use in FCC processes | |
| JP2008540096A (en) | Catalyst for exhaust gas treatment and method for producing the same | |
| CN1909962A (en) | NOx reduction composition for use in FCC processes | |
| CN1055303A (en) | Carbonatoms is the catalytic composition of the paraffin dehydrogenation of 2-5 | |
| CN1575850A (en) | Catalyst for purifying diesel engine exhaust gas and method for production thereof | |
| CN101491758A (en) | Catalyst for H2 selective oxidation in styrene production | |
| CN1049301A (en) | Noble metals load-carbon oxide accelerator | |
| CN1021801C (en) | Waste gas purifying catalyst containing aluminium oxide and stabilized by solid barium sulfate and its preparation | |
| KR20000069323A (en) | Catalytic Metal Plate | |
| JPS59156438A (en) | Catalyst composition and production thereof | |
| CN1816608A (en) | Catalyst additives for the removal of nh3 and hcn in the regeneration zone during catalytic cracking process | |
| US4522792A (en) | Process for oxidizing a gas comprising carbon monoxide or an hydrocarbon | |
| CN1030285C (en) | Non-noble metal oxide-carbon oxide combustion improver and preparation method thereof | |
| CN1102433C (en) | Process for preparation of sulfur transfer catalyst | |
| EP1129774A1 (en) | Adsorbent for hydrocarbon and catalyst for exhaust gas purification | |
| JP3387417B2 (en) | Exhaust gas purification catalyst and method for producing the same | |
| WO2002055194A1 (en) | Catalyst for clarification of nitrogen oxides | |
| CN1210104C (en) | Sundex low-temperature catalytic combustion nanometre composite oxide catalyst and preparing method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |