CN106140324B - A kind of regeneration method of semi regeneration reforming catalyst - Google Patents
A kind of regeneration method of semi regeneration reforming catalyst Download PDFInfo
- Publication number
- CN106140324B CN106140324B CN201510133674.3A CN201510133674A CN106140324B CN 106140324 B CN106140324 B CN 106140324B CN 201510133674 A CN201510133674 A CN 201510133674A CN 106140324 B CN106140324 B CN 106140324B
- Authority
- CN
- China
- Prior art keywords
- sulfur
- catalyst
- passed
- naphtha
- regeneration
- 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.)
- Active
Links
Abstract
A kind of regeneration method of semi regeneration reforming catalyst, including reaction temperature is adjusted to 250~480 DEG C, sulfur-containing compound is passed through into reforming reactor, make 0.1~3.0 mass % of sulfur content in catalyst, then stop being passed through raw material into reforming reactor, it makes charcoal to catalyst, chlorination updates, reduction.The method regenerated catalyst, which is not required to presulfurization, can be used, and have good regenerability.
Description
Technical field
The present invention is a kind of regeneration method of catalyst for reforming naphtha, specifically, being a kind of naphtha semi regeneration weight
The regeneration method of whole catalyst.
Background technique
Catalytic reforming is with C6~C12Naphtha Cut be raw material, in certain temperature, pressure, face hydrogen and catalyst and exist
Under, make raw material hydrocarbon molecule that the reforming reactions such as cycloalkane dehydrogenation, linear alkanes dehydrogenation isomery, paraffin dehydrogenation cyclisation, production occur
High-knock rating gasoline blend component or aromatic hydrocarbons, and the process of the cheap hydrogen of by-product.It is widely used in catalytic reforming process at present
The heterogeneous acidic function that support type dual-function reforming catalyst, the hydrogenation/dehydrogenation function of providing including metal constituent element and carrier provide
Energy.Reforming catalyst be usually using activated alumina as carrier, Pt be main metal constituent element, and containing the second metal constituent element such as rhenium,
Bis- (more) metallic catalysts of tin or germanium.
For dual-function reforming catalyst, metal function and acid function are acted synergistically on certain matching degree and are catalyzed weight
Whole reaction.If metal hydrogenation/dehydrogenation activity function is too strong in the two, the carbon deposit on reforming catalyst surface can increase sharply, no
Conducive to continuing for reforming reaction, metal function is too weak, and catalyst activity reduces.If acid too strong, catalyst adds hydrogen to split
Change activity is stronger, and the liquid yield of reformate can reduce, and acid too weak, activity reduces.Therefore support acidity function and metal
The balance matching of function determines the activity, selectivity and stability of catalyst.
In addition, for platinum-rhenium catalyst used in semi-regenerating catalytic reforming, since rhenium metal has very high hydrogenolysis activity,
If not being passivated the activity of rhenium when going into operation, strong hydrogenolysis will occur at oil inlet initial stage, release a large amount of reaction heat, make to be catalyzed
Agent bed temperature increases rapidly, overheating problem occurs.Once there is this phenomenon, it often will cause serious consequence, gently then cause
The a large amount of carbon deposits of catalyst, damage the activity and stability of catalyst, heavy then burn out catalyst, reactor and inner member.Therefore
Platinum-rhenium reforming catalyst is needed before use by presulfurization, by presulfurization, the hydrogenolysis for inhibiting fresh catalyst excessive,
With the activity and stability of guard catalyst, improve the selectivity of catalyst.The method for carrying out presulfurization to platinum-rhenium catalyst has
Two kinds: one is H is introduced in hydrogen2S slowly carries out presulfurization to catalyst under certain temperature and pressure；It is another
Kind is that organic sulfur compound, such as dimethyl disulfide, dimethyl sulfide are injected in hydrogen under certain temperature, pressure, is used
The H that these organic sulfur compounds are formed after decomposing2S carries out presulfurization to catalyst.First method is generally used for laboratory research,
Second method is commonly used to going into operation for platinum-rhenium catalyst commercial plant.The essence of both methods is all to use H2S is to catalyst
Presulfurization is carried out, gas-phase presulfiding is belonged to.There are the environmental pollution of equipment burn into and safety are hidden for the presulfurization of platinum-rhenium reforming catalyst
The problems such as suffering from.
Existing reforming catalyst regeneration techniques, as disclosed in USP20120270724, including Burning Coke on Catalyst, chlorination are more
New and reduction.
Reforming catalyst use process needs sulfur content in stringent limitation charging, general to require to be less than 1ppm.If catalysis
Sulfur poisoning occurs for agent use process, and catalyst forms sulfate radical after burning, it is considered that can damage the performance of catalyst.Therefore,
The sulphur before Burning Coke on Catalyst on Removal of catalyst is needed, after usually device stops charging, is removed by the method that hot hydrogen recycles,
In order to avoid sulfate radical is generated in coke combustion, alternatively, needing to remove sulfate radical after the sulfate radical for having generated certain content.
CN98117895.2 discloses a kind of removal methods of sulfate radical on reforming catalyst, at 400~600 DEG C to because of sulphur
Acid group fouled catalyst bed, which is passed through, to be decomposited the organochlorine compound of hydrogen chloride under this condition and is removed, the method compared with
Conventional catalyst chlorination updates regeneration, can sulfate radical effectively in Removal of catalyst.
Summary of the invention
The object of the present invention is to provide a kind of regeneration methods of semi regeneration reforming catalyst, and the catalyst after method regeneration is not
Presulfurization is needed, there is better regeneration effect.
Regeneration method provided by the invention, including reaction temperature is adjusted to 250~480 DEG C, it is passed through into reforming reactor
Sulfur-containing compound makes 0.1~3.0 mass % of sulfur content in catalyst, then stops being passed through raw material into reforming reactor, right
Catalyst is made charcoal, and chlorination updates, reduction.
The method of the present invention is before the regeneration of semi regeneration reforming catalyst, and the catalyst that activity is reduced is first at sulfur-containing compound
Reason, then make charcoal, chlorination updates, reduction is regenerated, it is i.e. usable that regenerated catalyst does not need presulfurization, simplifies regeneration and opens
Work process, regenerated catalyst performance are better than conventional regeneration processes.
Specific embodiment
The method of the present invention is stopped work in platinum-rhenium catalyst before regeneration, makes to make to be catalyzed containing a certain amount of sulfur-containing compound in charging
A certain amount of sulphur is adsorbed in agent, and then again through making charcoal, chlorination updates and reduction, and regenerated catalyst performance is compared with conventional regeneration processes
It is good, and regenerated catalyst is using being preceding not required to presulfurization.
Platinum-rhenium catalyst regeneration method provided by the invention is to activity reduction or decaying catalyst (reclaimable catalyst)
Before being made charcoal, first reduce temperature, sulfur-containing compound be passed through into reactor, catalyst is handled, then stop again into
Material, regenerates catalyst, and the regeneration step includes making charcoal, and chlorination updates and reduction.
The present invention is handled catalyst with sulfur-containing compound before making charcoal, and preferably makes sulfur content 0.3 in catalyst
~1.5 mass %, more preferably 0.3~1.0 mass %.
The present invention is passed through what sulfur-containing compound handled reclaimable catalyst with sulfur-containing compound into reforming reactor
There are two types of modes, and one is Containing-sulfur Naphtha is passed through into reactor, second is that sulfur-containing compound is injected into circulating air.
The Containing-sulfur Naphtha being passed through into reactor can be sulfur-bearing crude naphtha, or the purification containing sulfur-containing compound
Naphtha.
The sulfur-bearing crude naphtha can be obtained by not carrying out pre-add hydrogen to feed naphtha, can also be by reducing naphtha
Raw material pre-add hydrogen severity obtains, if sulfur content contained in crude naphtha is inadequate, can also fill into sulfur-containing compound thereto.
The purification naphtha containing sulfur-containing compound is obtained by injecting sulfur-containing compound into purification naphtha.
Sulfur content in the Containing-sulfur Naphtha being passed through into reactor be 100~10000ppm, preferably 200~
2000ppm, more preferable 200~1000ppm.
The amount that sulfur-containing compound is injected into circulating air is to make 10~1000 μ g/L of sulfur content in circulating air, preferably
100~1000 μ g/L.
The preferred hydrogen sulfide of the sulfur-containing compound being added into naphtha or into circulating air, thioether, disulphide, thioaldehydes,
Thiophene and derivant.
The mass space velocity that Containing-sulfur Naphtha is passed through into reactor is 0.1~10.0 hour-1, it is preferably 1.0~3.0 small
When-1, being passed through the time is 1~100 hour, preferably 2~24 hours.
The present invention need to adjust reaction temperature before being handled with sulfur-containing compound catalyst, preferably by reaction temperature
It is down to 300~450 DEG C, more preferably 300~400 DEG C.
After being handled with sulfur-containing compound reclaimable catalyst, stops charging, regenerate according to a conventional method, that is, make charcoal,
Chlorination updates and reduction.
In above-mentioned regenerative process, charcoal temperature is 400~550 DEG C, preferably 450~500 DEG C, make charcoal using oxygen-containing nitrogen or
Air.It is made charcoal using oxygen-containing nitrogen, wherein oxygen content is 0.5~21 volume %, preferably 1~5 volume %.
In the chlorination renewal process, oxygen-containing Oxygen in Nitrogen content used preferably 13.0~21.0 volume %, and thereto
Chlorine-containing compound is injected, note chlorine dose is 0.1~1.5%, preferably the 0.2~0.8% of catalyst quality, is conventional chlorinating update note
1.0~1.5 times of chlorine dose.It is 400~550 DEG C, preferably 450~520 DEG C that chlorination, which updates temperature,.The chlorine-containing compound is selected from two
Chloroethanes, trichloroethanes, carbon tetrachloride or tetrachloro-ethylene.
After chlorination updates, restored with hydrogen, preferably 460~500 DEG C of reduction temperature.In reduction process, preferably low
It is passed through hydrogen under temperature, then increases temperature and is restored, the temperature that hydrogen is preferably passed through into catalyst is not higher than 250 DEG C,
It is preferred that 30~200 DEG C, it is then gradually heated to 420~520 DEG C and catalyst is restored.
Semi regeneration reforming catalyst of the present invention include alumina support and the content calculated on the basis of carrier such as
Under active component:
0.1~2.0 mass % of platinum,
0.1~2.0 mass % of rhenium,
0.5~5.0 mass % of chlorine.
Yttrium or rare earth metal in the reforming catalyst also containing 0.1~1.0 mass %, the rare earth metal are
Lanthanide series metal, preferably ytterbium, europium or cerium.
The catalyst the preparation method comprises the following steps: be configured to maceration extract by compound containing platinum, containing rhenium compound, contain in maceration extract
There is chlorine, with maceration extract oxide impregnation alumina supporter, by impregnated carrier drying, roasts up to catalyst.The compound containing platinum
It is preferred that chloroplatinic acid, the preferred perrhenic acid containing rhenium compound, the drying temperature are 100~120 DEG C, maturing temperature is 350~650
℃.If containing yttrium or rare earth metal in catalyst, the nitrate or chloride of yttrium or rare earth metal are added in maceration extract.
Below by the example in detail present invention, but the present invention is not limited thereto.
Comparative example 1
(1) catalytic reforming reaction is carried out
50g is taken to form reduction-state PRT-D catalyst (production of middle Effect of Catalysis In Petrochemistry agent Chang Ling branch company) as shown in Table 1, dress
Enter in 100mL stainless steel tube reactor, being passed through nitrogen and replacing to oxygen content in system is 0.2 volume %, then is passed through high-purity hydrogen
Displacement, until density of hydrogen reaches 95 volume %, pressure to 1.0MPa, starting compressor carries out gas circulation, internal circulating load 150L/
H, is warming up to 400 DEG C, and 0.12g dimethyl disulfide (DMDS) is slowly injected into circulating air and carries out presulfurization.It is fed with 110g/h
Measure (mass space velocity 2.2h-1) composition purification naphtha as shown in Table 2 is introduced, it is warming up to 500 DEG C and reacts 200 hours.
(2) catalyst regeneration is carried out
The above-mentioned reactor after reaction in 200 hours is cooled to 400 DEG C, stops charging, is purged with nitrogen to circulating air
Middle H2Total content with hydro carbons is less than 0.3 volume %.500 DEG C are warming up to, air is filled into from suction port of compressor, in control loop gas
Oxygen content is 0.8 volume %, and gas internal circulating load is 100L/h, is made charcoal 20 hours, and reactor in/out mouth oxygen content is identical, display
Burning Coke on Catalyst is complete.Continue to fill into air, oxygen content in circulating air is made to reach 10.5 volume %, maintains gas circulation, it is small 4
When interior point of 5 injection 0.45mL dichloroethanes, carry out chlorination update.Fill into high pure nitrogen into circulating air oxygen content less than 0.2
Volume % is cooled to 200 DEG C, introduces high-purity hydrogen to density of hydrogen and reaches 95 volume %, is warming up to 480 DEG C and restores 4 hours.Drop
Temperature injects dimethyl disulfide (DMDS) 0.12g in hydrogen and carries out presulfurization to 400 DEG C.Then with the inlet amount (matter of 110g/h
Measure air speed 2.2h-1) be passed through into reactor shown in table 2 and refine naphtha, it is warming up to 500 DEG C and reacts 200 hours.Measurement is urged
The liquid product yield and octane number of agent regeneration front and back are shown in Table 3.
Example 1
After reduction-state catalyst is carried out presulfurization by the method for comparative example 1 (1) step, it is passed through naphtha and carries out catalytic reforming
Reaction is warming up to 500 DEG C and reacts 200 hours, carries out catalyst regeneration as follows.
Reactor is cooled to 400 DEG C, stopping is passed through purification naphtha thereto, and it is as shown in Table 2 to be passed through composition instead
Crude naphtha without pre-add hydrogen maintains crude naphtha to feed 4 hours, and the crude naphtha sulfur content being passed through accounts for catalyst quality
0.34%.Stopping is passed through crude naphtha, is passed through nitrogen and purges into circulating air H2With hydro carbons total content less than 0.3 volume %.It rises
Temperature is passed through air to 500 DEG C, from suction port of compressor, and oxygen content is 0.8 volume % in control loop gas, is in gas internal circulating load
It makes charcoal under 100L/h 20 hours, reactor in/out mouth oxygen content is identical, and display Burning Coke on Catalyst is complete.Continue to be passed through air, make
Oxygen content reaches 10.5 volume % in circulating air, maintains gas circulation, in 4 hours point 5 injection 0.50mL dichloroethanes into
Row chlorination updates.It is passed through high pure nitrogen oxygen content into circulating air and is cooled to 200 DEG C less than 0.2 volume %, introduce high-purity hydrogen
Reach 95 volume % to density of hydrogen, is warming up to 480 DEG C and restores 4 hours.400 DEG C are cooled to, with the inlet amount (quality of 110g/h
Air speed 2.2h-1) be passed through shown in table 2 and refine naphtha, it is warming up to 500 DEG C and reacts 200 hours, before and after the catalyst regeneration of measurement
Liquid product yield and octane number be shown in Table 3.
Example 2
After reduction-state catalyst is carried out presulfurization by the method for comparative example 1 (1) step, it is passed through naphtha and carries out catalytic reforming
Reaction is warming up to 500 DEG C and reacts 200 hours, carries out catalyst regeneration as follows.
Reactor is cooled to 400 DEG C, dimethyl disulfide is added into the purification naphtha for being passed through reactor, makes wherein to contain
Sulphur 900ppm maintains charging 2 hours, and the amount of sulphur accounts for the 0.40% of catalyst quality in the purification naphtha being passed through.Stop charging,
H is purged into circulating air with nitrogen2With hydro carbons total content less than 0.3 volume %.500 DEG C are warming up to, is passed through from suction port of compressor
Air, oxygen content is 0.8 volume % in control loop gas, is made charcoal 20 hours in the case where gas internal circulating load is 100L/h, reactor goes out/
Entrance oxygen content is identical, and display Burning Coke on Catalyst is complete.Continue to be passed through air, oxygen content in circulating air is made to reach 10.5 bodies
Product % maintains gas circulation, and point 5 injection 0.52mL dichloroethanes in 4 hours carry out chlorination update.It is passed through high pure nitrogen
Into circulating air, oxygen content is cooled to 200 DEG C less than 0.2 volume %, introduces high-purity hydrogen to density of hydrogen and reaches 95 volume %,
480 DEG C are warming up to restore 4 hours.400 DEG C are cooled to, with inlet amount (the mass space velocity 2.2h of 110g/h-1) it is passed through group shown in table 2
At purification naphtha, be warming up to 500 DEG C and react 200 hours, liquid product yield before and after the catalyst regeneration of measurement and pungent
Alkane value is shown in Table 3.
Example 3
After reduction-state catalyst is carried out presulfurization by the method for comparative example 1 (1) step, it is passed through naphtha and carries out catalytic reforming
Reaction is warming up to 500 DEG C and reacts 200 hours, carries out catalyst regeneration as follows.
Reactor is cooled to 400 DEG C, methyl mercaptan (CH is added into the purification naphtha being passed through in reactor3SH), make
Wherein sulfur-bearing 500ppm maintains charging 4 hours, and the amount of sulphur accounts for the 0.44% of catalyst quality in the purification naphtha being passed through.Stop
It only feeds, purges into circulating air H with nitrogen2With hydro carbons total content less than 0.3 volume %.500 DEG C are warming up to, is entered from compressor
Mouth is passed through air, and oxygen content is 0.8 volume % in control loop gas, makes charcoal 20 hours in the case where gas internal circulating load is 100L/h, instead
Answer device in/out mouth oxygen content identical, display Burning Coke on Catalyst is complete.Continue to be passed through air, reaches oxygen content in circulating air
10.5 volume % maintain gas circulation, and point 5 injection 0.50mL dichloroethanes in 4 hours carry out chlorination update.It is passed through height
Pure nitrogen gas oxygen content into circulating air is cooled to 200 DEG C less than 0.2 volume %, introduces high-purity hydrogen to density of hydrogen and reaches 95
Volume % is warming up to 480 DEG C and restores 4 hours.400 DEG C are cooled to, with inlet amount (the mass space velocity 2.2h of 110g/h-1) it is passed through table
The purification naphtha formed shown in 2 is warming up to 500 DEG C and reacts 200 hours, and the liquid product before and after the catalyst regeneration of measurement is received
Rate and octane number are shown in Table 3.
Example 4
After reduction-state catalyst is carried out presulfurization by the method for comparative example 1 (1) step, it is passed through naphtha and carries out catalytic reforming
Reaction is warming up to 500 DEG C and reacts 200 hours, carries out catalyst regeneration as follows.
Reactor is cooled to 400 DEG C, stops charging, introducing sulfur content in suction port of compressor with the flow of 100L/h is
The hydrogen of 160 μ g/L continues 10 hours, and sulfur-bearing hydrogen introduction volume is 1000L, and the total sulfur content in sulfur-bearing hydrogen is catalyst quality
0.32%.Stop introducing sulfur-bearing hydrogen, purges into circulating air H with nitrogen2With hydro carbons total content less than 0.3 volume %.It rises
Temperature is passed through air to 500 DEG C, from suction port of compressor, and oxygen content is 0.8 volume % in control loop gas, is in gas internal circulating load
It makes charcoal under 100L/h 20 hours, reactor in/out mouth oxygen content is identical, and display Burning Coke on Catalyst is complete.Continue to be passed through air, make
Oxygen content reaches 10.5 volume % in circulating air, maintains gas circulation, point 5 injection 0.50mL dichloroethanes in 4 hours, into
Row chlorination updates.It is passed through high pure nitrogen oxygen content into circulating air and is cooled to 200 DEG C less than 0.2 volume %, introduce high-purity hydrogen
Reach 95 volume % to density of hydrogen, is warming up to 480 DEG C and restores 4 hours.400 DEG C are cooled to, with the inlet amount (quality of 110g/h
Air speed 2.2h-1) it is passed through the purification naphtha formed shown in table 2, it is warming up to 500 DEG C and reacts 200 hours, the catalyst regeneration of measurement
The liquid product yield and octane number of front and back are shown in Table 3.
As known from Table 3, conventional regeneration processes of the regeneration method of the present invention compared with comparative example 1, liquid after catalyst regeneration
Product yield and octane number increase.
Table 1
* catalyst activity component content is calculated on the basis of carrier.
Table 2
Table 3
Claims (14)
1. a kind of regeneration method of semi regeneration reforming catalyst, including reaction temperature is adjusted to 250~480 DEG C, to reforming reaction
It is passed through sulfur-containing compound in device, makes 0.3~1.5 mass % of sulfur content in catalyst, then stops leading into reforming reactor
Enter raw material, make charcoal to catalyst, chlorination updates, and uses hydrogen reducing.
2. according to the method for claim 1, it is characterised in that be passed through the mode of sulfur-containing compound into reforming reactor are as follows:
It is passed through Containing-sulfur Naphtha into reactor or injects sulfur-containing compound into circulating air.
3. according to the method for claim 2, it is characterised in that the Containing-sulfur Naphtha is the crude naphtha of sulfur-bearing or contains
There is the purification naphtha of sulfur-containing compound.
4. according to the method for claim 2, it is characterised in that the sulfur content of the Containing-sulfur Naphtha be 100~
10000ppm。
5. according to the method for claim 2, it is characterised in that the sulfur content of the Containing-sulfur Naphtha is 200~2000ppm.
6. according to the method for claim 2, it is characterised in that the amount for injecting sulfur-containing compound into circulating air is to make to recycle
Sulfur content is 10~10000 μ g/L in gas.
7. according to method described in claim 2 or 3, it is characterised in that the sulfur-containing compound is hydrogen sulfide, thioether, two sulphur
Compound, thioaldehydes, thiophene and derivant.
8. according to the method for claim 2, it is characterised in that the mass space velocity for being passed through Containing-sulfur Naphtha into reactor is
0.1~10.0 hour-1, being passed through the time is 1~100 hour.
9. according to the method for claim 1, it is characterised in that it is passed through before sulfur-containing compound into reforming reactor, it will be anti-
Temperature is answered to be adjusted to 350~450 DEG C.
10. according to the method for claim 1, it is characterised in that chlorination update note chlorine dose for catalyst quality 0.1~
1.5%.
11. according to the method for claim 1, it is characterised in that restoring method be not higher than 250 DEG C at a temperature of be passed through
Hydrogen is gradually heated to 420~520 DEG C and is restored.
12. according to the method for claim 1, it is characterised in that the semi regeneration reforming catalyst includes alumina support
The following active component with the content that is calculated on the basis of carrier:
0.1~2.0 mass % of platinum,
0.1~2.0 mass % of rhenium,
0.5~5.0 mass % of chlorine.
13. according to the method for claim 12, it is characterised in that also contain 0.1~1.0 matter in the reforming catalyst
Measure the rare earth metal of %.
14. according to the method for claim 13, it is characterised in that the rare earth metal is yttrium or lanthanide series metal.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510133674.3A CN106140324B (en) | 2015-03-25 | 2015-03-25 | A kind of regeneration method of semi regeneration reforming catalyst |
| TW105109083A TWI681816B (en) | 2015-03-25 | 2016-03-23 | Regeneration method of semi-regeneration recombination catalyst |
| RU2016110754A RU2731273C2 (en) | 2015-03-25 | 2016-03-24 | Method of regenerating partially regenerated reforming catalyst |
| US15/081,234 US9694356B2 (en) | 2015-03-25 | 2016-03-25 | Method for regenerating semi-regenerated reforming catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510133674.3A CN106140324B (en) | 2015-03-25 | 2015-03-25 | A kind of regeneration method of semi regeneration reforming catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106140324A CN106140324A (en) | 2016-11-23 |
| CN106140324B true CN106140324B (en) | 2019-09-24 |
Family
ID=57339587
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510133674.3A Active CN106140324B (en) | 2015-03-25 | 2015-03-25 | A kind of regeneration method of semi regeneration reforming catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106140324B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108097275B (en) * | 2016-11-24 | 2021-03-02 | 中国石油化工股份有限公司 | Start-up method of semi-regenerated catalytic reforming catalyst |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5508243A (en) * | 1993-02-26 | 1996-04-16 | Eurecat | Heat treatment of solid catalyst or adsorbent particles in the presence of fluid in a vibrating helical coil |
| CN1921942A (en) * | 2004-01-20 | 2007-02-28 | 国际壳牌研究有限公司 | Method of restoring catalytic activity to a spent hydroprocessing catalyst, a spent hydroprocessing catalyst having restored catalytic activity, and a hydroprocessing process |
| CN102140366A (en) * | 2010-01-29 | 2011-08-03 | 中国石油化工股份有限公司 | Initial reaction method of platinum-rhenium reforming catalyst |
| CN103285895A (en) * | 2012-02-29 | 2013-09-11 | 中国石油化工股份有限公司 | Preparation method of sulfurized state reforming catalyst |
| CN103285858A (en) * | 2012-02-29 | 2013-09-11 | 中国石油化工股份有限公司 | Sulfurized state naphtha reforming catalyst and preparation method thereof |
-
2015
- 2015-03-25 CN CN201510133674.3A patent/CN106140324B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5508243A (en) * | 1993-02-26 | 1996-04-16 | Eurecat | Heat treatment of solid catalyst or adsorbent particles in the presence of fluid in a vibrating helical coil |
| CN1921942A (en) * | 2004-01-20 | 2007-02-28 | 国际壳牌研究有限公司 | Method of restoring catalytic activity to a spent hydroprocessing catalyst, a spent hydroprocessing catalyst having restored catalytic activity, and a hydroprocessing process |
| CN102140366A (en) * | 2010-01-29 | 2011-08-03 | 中国石油化工股份有限公司 | Initial reaction method of platinum-rhenium reforming catalyst |
| CN103285895A (en) * | 2012-02-29 | 2013-09-11 | 中国石油化工股份有限公司 | Preparation method of sulfurized state reforming catalyst |
| CN103285858A (en) * | 2012-02-29 | 2013-09-11 | 中国石油化工股份有限公司 | Sulfurized state naphtha reforming catalyst and preparation method thereof |
Non-Patent Citations (3)
| Title |
|---|
| "THIORESISTANCE OF SUPPORTED METAL CATALYSTS: STRUCTURE SENSITIVITY OF HYDROGEN SULPHIDE ADSORPTION ON Pt/A12O3,Ir/A12O3 AND Pt-Ir/A12O3 CATALYSTS";J. BARBIER et al.;《Applied Catalysis》;19851216;第19卷(第2期);第375-385页 * |
| "半再生重整催化剂PRT-C、PRT-D的器内再生";温传忠 等;《山东化工》;20110228;第40卷(第2期);第47页第1节、第48页右栏第3段、第50页左栏第2段、第51页表5 * |
| "硫酸盐硫对铂铼钛重整催化剂反应性能的影响";孙逢铎 等;《石油学报（石油加工）》;19880331;第4卷(第1期);第40页的表2、第44页的结论 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106140324A (en) | 2016-11-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0071397B1 (en) | Process for regenerating coked noble metal-containing catalysts | |
| CN104023841A (en) | Catalytic composition and process for the dehydrogenation of butenes or mixtures of butanes and butenes to give 1,3-butadiene | |
| CN102139221A (en) | Method for preparing platinum-rhenium reforming catalyst | |
| CN102140366B (en) | Initial reaction method of platinum-rhenium reforming catalyst | |
| WO2001000318A1 (en) | Catalytic reforming catalyst activation | |
| NO137356B (en) | PROCEDURES FOR ISOMERIZATION OF PARAFINIC HYDROCARBONS | |
| CN106140324B (en) | A kind of regeneration method of semi regeneration reforming catalyst | |
| CN106147829A (en) | Start-up method containing molecular sieve gasoline hydrogenation modifying catalyst | |
| CN101376824B (en) | Reforming catalyst pretreatment and initial reaction method | |
| CN103285895B (en) | A kind of preparation method of sulphided state reforming catalyst | |
| CN102371186B (en) | Reduction method of semi-regenerative reforming catalyst | |
| CA2409117A1 (en) | Improved catalytic reforming process | |
| CN106140244B (en) | A kind of regeneration method of platinum-rhenium reforming catalyst | |
| CN103285858B (en) | A kind of sulphided state catalyst for reforming naphtha and preparation method thereof | |
| CN106140326B (en) | The regeneration method of semi regeneration reforming catalyst | |
| US9694356B2 (en) | Method for regenerating semi-regenerated reforming catalyst | |
| EP0037647A1 (en) | Startup procedure for reforming catalysts | |
| US20180119032A1 (en) | Removal of sulfur from naphtha | |
| CN103285859A (en) | Sulfurized multi-metal reforming catalyst and preparation method thereof | |
| CN109772474A (en) | A kind of start-up method of hydrotreating catalyst | |
| CN102139222B (en) | Platinum rhenium reforming catalyst and preparation method thereof | |
| CN110760337A (en) | Method and equipment for desulfurizing aromatic hydrocarbon raw material | |
| CN108097275A (en) | A kind of start-up method of semi-regenerating catalytic reforming catalyst | |
| CN102166534A (en) | Method for removing sulfate radicals from continuous reforming catalyst | |
| CN113272408B (en) | Hydrocarbon conversion process with recycle of reduction effluent |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |