CN104226379B - A kind of renovation process of continuous reforming catalyst - Google Patents
A kind of renovation process of continuous reforming catalyst Download PDFInfo
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- CN104226379B CN104226379B CN201310247248.3A CN201310247248A CN104226379B CN 104226379 B CN104226379 B CN 104226379B CN 201310247248 A CN201310247248 A CN 201310247248A CN 104226379 B CN104226379 B CN 104226379B
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Abstract
A kind of renovation process of continuous reforming catalyst, including reacted reclaimable catalyst is passed through regenerator, scorch region, oxychlorination area and roast area are passed sequentially through, regeneration gas of the part without any processing that scorch region is exported to discharge is directly injected into oxychlorination area.This method can reduce the note chlorine dose to oxychlorination area, and be effectively improved the regeneration effect of catalyst using the regeneration gas regulation oxychlorination area atmosphere of heat.
Description
Technical field
The present invention is a kind of renovation process of catalyst, specifically, be a kind of naphtha continuous reforming catalyst again
Generation method.
Background technology
Naphtha continuous catalytic reforming receives the features such as high, hydrogen production is high and aromatics yield is high with its liquid, in high-knock rating gasoline
With the very big attention in aromatics production by people, and leading role will be played in reforming process evolution from now on.Even
The core of continuous reforming process is catalyst regeneration techniques, conventional regenerative process generally comprise burn, oxychlorination, roasting（Dry）
With four steps of reduction.
The purpose burnt is that the coke on catalyst is burnt up, and its process is that coke burns at a certain temperature with oxygen,
Carbon dioxide and water are produced, and releases heat.Because the part chlorine element in catalyst carrier can be lost under the conditions of burning, institute
With the flue gas after burning（Regeneration gas）In except containing moisture and CO2Outside, also containing a certain amount of HCL and Cl2.The mesh of oxidation chlorination
Be to adjust the chlorinity on catalyst, it is and the metal on catalyst is fully oxidized and scattered, platinum crystal grain is disperseed again, from
And recover the activity of catalyst.Oxychlorination process is reacted by oxygen and metal and organic chloride to complete, and the process needs
Want suitable water chlorine ratio.
CN1136056C discloses a kind of aromatic compounds preparation or the regeneration of reforming catalyst for improving oxidative chlorination
Method and apparatus.Including burning, oxychlorination and calcination stepses, at least one of this renovation process chlorination reagent, at least one
Kind oxygen-containing gas and water are transported to oxychlorination step, and it is 3~50 to make water cl molar ratio, and oxychlorination step is containing less than 21%
Oxygen and at least 50ppm chlorine（On the basis of HCl）Gas exist and temperature be 350~600 DEG C under conditions of carry out,
And operated under 3.0~8.0MPa pressure.Described oxygen-containing gas by washing dechlorination and is done to be a part of from scorch region
The dry regeneration gas for being dehydrated and supplementing oxygen, the roast area of another part from below.
CN1100852C discloses the renovation process and its equipment of a kind of hydrocarbon conversion catalyst, and reclaimable catalyst is from top to bottom
Pass sequentially through scorch region, chlorine oxidation zone, predrying area and the roast area of regenerator, the predrying area set up will can pass through dechlorination and
Dry regeneration recycle gas is used for the predrying of oxychlorination rear catalyst, so as to reduce the dry gas dosage of roast area, makes roasting
The oxygen-containing gas inlet oxygen demand needed for burning for burning area determines that the gas into roast area can fully enter chlorine oxidation zone,
Regeneration gas circulation loop is entered back into, to burn oxygen supply, the calcining zone of regenerator can be made to be vented without unnecessary oxygen-containing gas, so as to cancel
It is calcined the control techniques of area's emptying gas.
CN101835877A discloses the renovation process and container of a kind of reforming catalyst, containing Pd/carbon catalyst in a regenerator
Pass through one section of scorch region, two sections of scorch regions, oxychlorination area and roast area successively.A part of gaseous emission from oxychlorination area
The entrance of above-mentioned two scorch region is recycled to via at least one scrubbing section.A part from oxychlorination area is not scrubbed
, the gaseous emission that oxygen content is higher be recycled to two sections of scorch regions, pass through and improve the methods of two sections of scorch region oxygen contents and drop
The aggregation extent of low two sections of scorch region metal platinums, wherein after the discharge gas of two sections of scorch regions discharges gas mixing with oxychlorination area
Oxychlorination area is recirculated back to after scrubbed, dry.
CN101835878A discloses a kind of renovation process of reforming catalyst, i.e., containing Pd/carbon catalyst in a regenerator successively
By one section of scorch region, two sections of scorch regions, oxychlorination area and roast area.A part of gaseous emission from oxychlorination area via
At least one scrubbing section is recycled to the entrance of above-mentioned two scorch region.A part from oxychlorination area is not scrubbed, oxygen
The higher gaseous emission of content is recycled to two sections of scorch regions, and two sections are reduced by the method for improving two sections of scorch region oxygen contents
The aggregation extent of scorch region metal platinum.
USP6153091 proposes a kind of method for reducing chloride emission in moving bed regeneration recycle gas.Burnt in regenerator
Jiao Qu upstreams set the adsorption zone equipped with reclaimable catalyst, and the flue gas generated that scorch region carbon deposit is burnt is passed through adsorption zone, contains
The regenerated flue gas of chloride contacts with reclaimable catalyst, adsorbs most of chloride in flue gas using spent agent, and part is straight
Connect emptying.On the other hand, this method effectively utilizes the chlorine in the chloride supplement reclaimable catalyst being lost in burning process, so as to
Reduce the amount for injecting chloride in oxychlorination process outside system.
The content of the invention
It is an object of the invention to provide a kind of renovation process of continuous reforming catalyst, this method utilizes hot regeneration controlled atmosphere
Oxychlorination area atmosphere is saved, the note chlorine dose to oxychlorination area can be reduced, and be effectively improved the regeneration effect of catalyst.
The renovation process of continuous reforming catalyst provided by the invention, including reacted reclaimable catalyst is passed through regeneration
Device, scorch region, oxychlorination area and roast area are passed sequentially through, a part for the regeneration gas of scorch region discharge is directly injected into oxychlorination
Area.
Part scorch region regeneration gas is directly returned to oxychlorination area by the inventive method without any processing, using in regeneration gas
Moisture and chloride, the water chlorine ratio in supplement regulation oxychlorination area, so as to reduce the note chlorine dose in oxychlorination area and water injection rate, simultaneously
Oxychlorination effect can also be improved, lift catalyst regenerability, and reduce device operating cost.
Brief description of the drawings
Fig. 1 is that the present invention will inject oxychlorination area using one section of regeneration gas burnt, and regeneration cycle gas return path is using wet
The schematic flow sheet of thermal cycling profile.
Fig. 2 is that the present invention will inject oxychlorination area using one section of regeneration gas burnt, and regeneration cycle gas return path is using dry
The schematic flow sheet of SAPMAC method pattern.
Fig. 3 will be injected separately into oxychlorination area for the present invention using two sections of regeneration gases burnt, and regeneration cycle gas return path is adopted
With the schematic flow sheet of dry and cold circulation pattern.
Embodiment
In naphtha continuous reforming process, the cyclic process of catalyst is：Reduction rear catalyst passes through first reactor
Contacted to the 4th reactor with naphtha, it is carried out reforming reaction, contain Pd/carbon catalyst from what the 4th reactor bottom came out（Claim
For reclaimable catalyst）, it is thus lifted to the regenerator of catalyst regenerating section；Catalyst in regenerator through burning, chlorine monoxid
After changing and being calcined three steps（Referred to as regenerated catalyst）, into reducing zone, the reduction of catalyst is completed, is then returned again again
To the first reactor of reactive moieties, continue the circulation of a new round.
In regenerator, burn successively, oxychlorination and roasting are regenerated by process for reclaimable catalyst, then restores.Burn
Jiao is that the coke on carbon deposited catalyst is burnt up, and its process is that coke reacts at a certain temperature with oxygen, produces carbon dioxide
And water, and release heat.Because the part chlorine element in catalyst carrier can be lost under the conditions of burning, so, after burning
Regeneration gas（Flue gas）In except containing moisture and CO2Outside, also containing a certain amount of HCL and Cl2, wherein water content is up to 10000 μ g/g
More than, chlorinity is up to 500~5000 μ g/g.Oxidation chlorination is to adjust the chlorinity on catalyst, and makes the gold on catalyst
Belong to fully oxidized and scattered, platinum crystal grain is disperseed again.Oxidation chlorination process is reacted by oxygen and metal and organic chloride
And complete, the process needs suitable water chlorine ratio.Roasting is by the moisture removal on catalyst, because burning and chloride oxidation
Process can all generate water, in these water adsorptions to catalyst surface, can produce harmful effect to catalyst activity.Reduction be by
Oxidation state metal on catalyst is converted into as-reduced metal, needs starvation.Catalyst metal components reduction is more thorough, catalysis
Agent performance recovery is better.
The inventive method be continuous reformer reaction and catalyst cyclic regeneration system normal operation under, will again
A part for the regeneration gas of raw device scorch region discharge is directly injected into oxychlorination area, as oxychlorination area entrance without any processing
A part for gas, there is provided a part of chlorine needed for oxychlorination area note chlorine.Both the note chlorine dose in oxychlorination area can have been reduced, and can improves
The regenerability of catalyst.In the case of the dry and cold circulation of regeneration gas, moreover it is possible to reduce the dechlorination for the regeneration gas for being recycled back to scorch region
Amount.
The regeneration gas in the injection oxychlorination area can be separately injected into oxychlorination area, inject oxygen after preferably being mixed with chlorine-containing gas
Chlorination area.
Injected in the inventive method the regeneration gas in oxychlorination area with the volume ratio of catalyst in oxychlorination area be 5~200, it is excellent
Select 50~200.It is 1 to inject the regeneration gas in oxychlorination area and the volume ratio of the regeneration gas total amount of scorch region discharge：10~100, it is excellent
Select 1：10~50.
In the present invention, the regeneration gas that oxychlorination area is discharged into from regenerator is without heat exchange, dechlorination and drying process
Thermal current, its temperature are 400~550 DEG C, and wherein chlorinity is 500~5000 μ g/g, and water content is 10000~100000 μ g/
G, commonly reach 11000~50000 μ g/g.
The temperature in described oxychlorination area is 450~600 DEG C, is preferably 500~560 DEG C；Pressure is 0.1~2.0MPa,
It is preferred that 0.2~1.0MPa（Gauge pressure）, H2O/HCl mol ratios are 3~30, preferably 5~15.
In the inventive method, regenerator scorch region can be one section and burn, or two sections burn.Described scorch region is two
During section scorch region, there is partial regeneration gas injection oxychlorination area the outlet of every section of scorch region.
In the present invention, when being recycled from the regeneration gas of scorch region discharge in return scorch region, it can use " damp and hot to follow
The mode of ring ", the pattern of " dry and cold circulation " can also be used." moisture and hot ageing " refers to the regeneration gas of scorch region discharge
A part introduces oxychlorination area, and remaining returns to scorch region." the dry and cold circulation " refers to one of the regeneration gas of scorch region discharge
Separate into oxychlorination area, remaining returns to scorch region through alkali cleaning and after drying.The alkali cleaning is to use the chlorine in alkali lye zeolite regeneration gas.
Described continuous reforming catalyst is platinum-tin catalyst, including carrier and what is calculated on the basis of butt carrier contain
Measure following active component：
The mass % of platinum group metal 0.01~2.0
The mass % of tin 0.01~5.0
The mass % of halogen 0.1~10,
Active metallic content is preferably in above-mentioned catalyst：
The mass % of platinum group metal 0.1~1.0
The mass % of tin 0.1~2.0
The mass % of halogen 0.1~5.0.
Can also contain the third and fourth metal constituent element in above-mentioned catalyst, the preferred europium of the third and fourth metal constituent element, cerium and
One or more in titanium, its content are 0.01~5.0 mass %, preferably 0.1~2.0 mass %.
The preferred platinum in platinum group metal in the catalyst, the preferred chlorine of halogen, the more preferably preferred aluminum oxide of carrier, gamma oxidation
Aluminium.
The present invention is further illustrated below in conjunction with the accompanying drawings.
In Fig. 1, using catalyst, one section burns, regeneration gas moisture and hot ageing mode.In this mode, regeneration gas is entirely circulating
During without dry and dechlorination process.Catalyst flow path is：Reclaimable catalyst from pipeline 1 and 1a sequentially enters
Scorch region A, oxychlorination area B, roast area C and the cooling zone D of regenerator 2, enter catalyst reduction area by pipeline 20, complete to urge
The regenerative process of agent.
It is from the regeneration gas trend of scorch region discharge：Reclaimable catalyst completes burning process in the A of scorch region, after burning
Caused flue gas is regeneration gas through the discharge of pipeline 3, is divided into three parts after regenerating blower fan 4, Part I is through pipeline 5, air cooler
6th, pipeline 7, scorch region electric heater 8, catalyst scorch region is returned to by pipeline 11.Part II enters scorch region A through pipeline 10
The reheating area of bottom, Part III enter oxygen chlorine after pipeline 9 mixes with the chlorine-containing compound from pipeline 12 by pipeline 13
Change area B, oxychlorination processing is carried out to the catalyst after burning.
Dry air from pipeline 17 enters cooling zone D through pipeline 18, from the hot-air that cooling zone comes out with coming from pipe
After the dry air mixing of line 19, roast area C is entered after pipeline 16, roast area electric heater 15 and pipeline 14, to oxychlorination
Catalyst after processing is calcined.The gas come out from roast area C is discharged through pipeline 21.
In Fig. 2, using catalyst, one section burns, the dry and cold endless form of regeneration gas.In this mode, regeneration gas is in cyclic process
It is middle to pass through alkali cleaning dechlorination and drying and dehydrating process.Catalyst flow path is：Reclaimable catalyst from pipeline 1 sequentially enters again
Scorch region A, oxychlorination area B and the roast area C of raw device 2, enter catalyst reduction area after the discharge of pipeline 20, complete whole catalysis
The regenerative process of agent.
It is from the regeneration gas trend of scorch region discharge：Reclaimable catalyst completes burning process in scorch region A, burns generation
Regeneration gas after regenerator discharge, divide two parts, a part is through pipeline 3, heat exchanger 21, pipeline 5, caustic wash tower 22, drier
23rd, regeneration cycle air compressor 24 returns to heat exchanger 21.The stock-traders' know-how pipeline 7a of regeneration gas one, scorch region through the heat exchange of heat exchanger 21 enter
Mouth electric heater 8a, pipeline 11a return to catalyst scorch region A top, another stock-traders' know-how pipeline 7b, reheat area's electric heater
8b, pipeline 11b return to scorch region A bottom.Another part regeneration gas enters oxychlorination area B through pipeline 19 by pipeline 14.Part
Regeneration gas after dechlorination is directly discharged in air by pipeline 36.
Dry air through pipeline 17, roast area electric heater 15, pipeline 26 enter roast area C, complete catalyst roasting,
Dehydration.The hot-air come out from roast area C mixes through pipeline 16 with the chlorine-containing compound from pipeline 12, through oxychlorination area
Entrance electric heater 25 through pipeline 14 enters oxychlorination area B after being mixed with the regeneration gas from pipeline 19.Discharged from oxychlorination area B
Gas through pipeline 30 enter regeneration gas washing, drying, the circulatory system.
In Fig. 3, using catalyst, two sections burn, the dry and cold endless form of regeneration gas.In this mode, regeneration gas is in cyclic process
It is middle to pass through alkali cleaning dechlorination and drying and dehydrating process.Catalyst flow path is：Reclaimable catalyst from pipeline 1 sequentially enters again
One section of scorch region A1, two sections of scorch region A2, oxychlorination area B, the roast area C of raw device 2, are discharged, through pipeline 20 into catalyst also
Former area, complete the regenerative process of whole catalyst.
It is from the regeneration gas trend of scorch region discharge：The regeneration gas come from two sections of scorch region A2 outlets, a part is through pipe
Line 33, pipeline 14 enter oxychlorination area B；Remaining is through pipeline 3a, heat exchanger 21, caustic wash tower 22, drier 23, regeneration cycle air pressure
Divide three parts after contracting machine 24, a part exchanges heat and then by one section of scorch region entrance electric heater 8 and pipeline 11 through heat exchanger 21 again
Into one section of scorch region, another part is after pipeline 34, heat exchanger 35, with the dry air from pipeline 17 and from pipeline 12
Chlorine-containing compound mixing, produced after oxychlorination area entrance electric heater 25, then with the one section of scorch region in part from pipeline 31
Raw hot recycling gas mixing, enter oxychlorination area B through pipeline 14, Part III is burnt through pipeline 27 by pipeline 32 into two sections
Area A2 entrance.Discharged from the regeneration gas of one section of scorch region outlet discharge through pipeline 3b, a part and the circulation from pipeline 27
Enter two sections of scorch region A2 entrance after regeneration gas mixing through pipeline 32, another part then enters oxygen chlorine through pipeline 31 by pipeline 14
Change area B.Regeneration gas of the part after dechlorination is directly discharged in air by pipeline 36.
The gas come out from oxychlorination area B is after heat exchanger 35 and pipeline 30, into the regeneration gas circulatory system.Dry air
Enter roast area C through pipeline 17, roast area electric heater 15, pipeline 26.
The present invention is further illustrated below by example, but the present invention is not limited thereto.
Example 1
Technological process as shown in Fig. 1 of the present invention is regenerated to catalyst, i.e., from scorch region, extension regeneration gas is gone
Oxychlorination area, regeneration gas are " moisture and hot ageing ".
CONTINUOUS REFORMER used catalyst is the catalyst that the trade mark that the production of long catalyst Co. is built in Hunan is RC011, carrier
For aluminum oxide, each component content calculated on the basis of aluminum oxide is：Pt0.28 mass %, Sn0.41 mass %, by reactor
The carbon content of reclaimable catalyst be 4.5 mass %.
The operating condition of regenerator is：Catalyst internal circulating load is 907kg/h；480 DEG C of scorch region A inlet temperatures, scorch region
Pressure 0.25MPa（Gauge pressure）, gas/agent volume ratio 2000：1, it is nitrogen that oxygen content is 0.7 volume % to burn gases used.
Oxychlorination area B inlet temperatures are 510 DEG C, pressure 0.25MPa（Gauge pressure）, gas/agent volume ratio 450：1, H2O/HCl
Mol ratio is 7, and the chloride that oxychlorination area is injected from pipeline 12 is tetrachloro-ethylene, injection rate 450ml/h, will regenerate blower fan 4
The regeneration qi leel three parts of discharge, a part return to scorch region, another part warp after air cooler 6 and scorch region electric heater 8
Pipeline 10 enters the reheating area of scorch region A bottoms, and the tetrachloro-ethylene that Part III is injected through pipeline 9 with outside by pipeline 12 mixes
After conjunction, oxychlorination area is injected by pipeline 13, the regeneration gas temperature drawn by pipeline 9 is 480 DEG C, and wherein chlorinity is 1200 μ g/
G, water content are 35000 μ g/g, and it is 50 that it, which injects flow and the volume ratio of catalyst in oxychlorination area, the regeneration that pipeline 9 is drawn
The volume ratio of gas and the regeneration gas total amount discharged by pipeline 3 is 1：50.
Roast area C inlet temperatures are 550 DEG C, pressure 0.25MPa（Gauge pressure）, gas/agent volume ratio 450：1.After regeneration
Catalyst is in 480 DEG C, 0.50MPa（Gauge pressure）, gas/agent volume ratio 800：Hydrogen reducing 2h is used under conditions of 1.
In 100 milliliters of fixed bed reactors, the catalyst after 50 milliliters of reduction is loaded, with the refined stone brain listed by table 1
Oil is catalytic reforming raw material, reaction mass inlet temperature is 530 DEG C, reaction pressure 0.7MPa, hydrogen/hydrocarbon mol ratio are 6.7,
Feed volume air speed is 2.0h-1Under conditions of carry out reforming reaction, reaction result is shown in Table 2.
Example 2
Technological process as shown in Fig. 2 of the present invention regenerates to catalyst, and regeneration gas is " dry and cold circulation ".From scorch region
Regeneration qi leel two parts of discharge, a part is through pipeline 3, heat exchanger 21, pipeline 5, caustic wash tower 22, drier 23, regeneration cycle
Air compressor 24 returns to heat exchanger 21.The stock-traders' know-how pipeline 7a of regeneration gas one, the scorch region entrance electric heater to be exchanged heat through heat exchanger 21
8a, pipeline 11a return to catalyst scorch region A top, and another stock-traders' know-how pipeline 7b, reheating area electric heater 8b, pipeline 11b are returned
Go back to scorch region A bottom.Another part regeneration gas injects oxychlorination area B through pipeline 19 by pipeline 14.Drawn again through pipeline 19
Angry temperature is 490 DEG C, and it is 100 that it, which injects flow and the volume ratio of catalyst in oxychlorination area, the regeneration gas that pipeline 19 is drawn
The volume ratio of regeneration gas total amount with being discharged by pipeline 3 is 1：20.Tetrachloro-ethylene is injected by pipeline 12, injection rate 525ml/h,
The other control conditions of regenerator are identical with example 1.
For regenerated catalyst by reactivity worth evaluation is carried out after the method reduction of example 1, reaction result is shown in Table 2.
Example 3
Technological process as shown in Fig. 3 of the present invention carries out two sections of coke burning regenerations to catalyst, and regeneration gas is " dry and cold circulation ".
The regeneration gas come from two sections of scorch region A2 outlets, a part is through pipeline 3a, heat exchanger 21, caustic wash tower 22, drier
23rd, three strands are separated into after regeneration cycle air compressor 24, wherein two strands respectively enter one section of scorch region and two sections of scorch regions, it is another
Stock-traders' know-how pipeline 14 enters oxychlorination area B；Another part enters oxychlorination area B through pipeline 33, pipeline 14.What one section of scorch region was discharged
Regeneration gas enters oxychlorination area B by pipeline 31 through pipeline 14.The temperature for the regeneration gas that pipeline 33 and pipeline 31 are drawn is 470 DEG C,
The total flows of two pipelines and the volume ratio of catalyst in oxychlorination area are 75, the regeneration gas that two pipelines are drawn with by pipeline 3a
The volume ratio of the regeneration gas total amount of discharge is 1：28.Tetrachloro-ethylene is injected by pipeline 12, injection rate 515ml/h, regenerator its
Its control condition is identical with example 1.
For regenerated catalyst by reactivity worth evaluation is carried out after the method reduction of example 1, reaction result is shown in Table 2.
Comparative example 1
Catalyst is regenerated by the method for example 1, the difference is that regeneration gas is not introduced into oxychlorination area, from pipeline 12
The injection rate for injecting tetrachloro-ethylene is 520ml/h.
For regenerated catalyst by reactivity worth evaluation is carried out after the method reduction of example 1, reaction result is shown in Table 2.
Comparative example 2
Catalyst is regenerated by the method for example 2, the difference is that regeneration gas is not introduced into oxychlorination area, from pipeline 12
The note chlorine dose for injecting tetrachloro-ethylene is 595ml/h.
For regenerated catalyst by reactivity worth evaluation is carried out after the method reduction of example 1, reaction result is shown in Table 2.
Comparative example 3
Catalyst is regenerated by the method for example 3, the difference is that regeneration gas is not introduced into oxychlorination area, from pipeline 12
The injection rate for injecting tetrachloro-ethylene is 601ml/h.
For regenerated catalyst by reactivity worth evaluation is carried out after the method reduction of example 1, reaction result is shown in Table 2.
As can be known from Table 2, using the inventive method, can obviously reduce in regenerative process by injection oxychlorination outside device
The note chlorine dose in area, that is, the injection rate of additional tetrachloro-ethylene is reduced, and regenerated catalyst is than the renovation process of routine, reaction
Performance improves, and aromatics yield and hydrogen yield dramatically increase.
Table 1
Table 2
Claims (5)
1. a kind of renovation process of continuous reforming catalyst, including reacted reclaimable catalyst is passed through regenerator, lead to successively
Scorch region, oxychlorination area and roast area are crossed, injects oxygen after a part for the regeneration gas of scorch region discharge is mixed with chlorine-containing gas
Chlorination area, the regeneration gas that oxychlorination area is discharged into from regenerator is the thermal current without heat exchange, and its temperature is 400~550 DEG C,
Chlorinity from the regeneration gas of regenerator discharge is 500~5000 μ g/g, and water content is 10000~100000 μ g/g, into oxygen
The volume ratio of the regeneration gas in chlorination area and the regeneration gas total amount of scorch region discharge is 1：10~100, the temperature in described oxychlorination area
Spend for 450~600 DEG C, pressure is 0.1~2.0MPa, H2O/HCl mol ratios are 3~30.
2. in accordance with the method for claim 1, it is characterised in that the regeneration gas in injection oxychlorination area in oxychlorination area with being catalyzed
The volume ratio of agent is 5~200.
3. in accordance with the method for claim 1, it is characterised in that described scorch region is two sections and burnt that every section of scorch region exports
There is partial regeneration gas injection oxychlorination area.
4. in accordance with the method for claim 1, it is characterised in that the part injection oxychlorination of the regeneration gas of scorch region discharge
Area, remaining returns to scorch region.
5. in accordance with the method for claim 1, it is characterised in that the part injection oxychlorination of the regeneration gas of scorch region discharge
Area, remaining returns to scorch region through alkali cleaning and after drying.
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| FR2651154A1 (en) * | 1989-08-25 | 1991-03-01 | Inst Francais Du Petrole | Equipment for the regeneration of a reforming catalyst or of a catalyst for the production of aromatic hydrocarbons and for the recycling of the gaseous effluents |
| WO1994005418A1 (en) * | 1992-09-04 | 1994-03-17 | Exxon Research And Engineering Company | Improved method of regenerating deactivated catalyst |
| CN1197694A (en) * | 1997-04-14 | 1998-11-04 | 法国石油公司 | Process and vessel for regenerating catalyst for production of aromatic compounds or for reforming, with improved oxychlorination |
| CA2007707C (en) * | 1989-01-13 | 2000-07-18 | Jean-Claude Macaire | Process for regenerating a catalyst used for the production of aromatic of reforming hydrocarbons |
| CN101835878A (en) * | 2007-10-26 | 2010-09-15 | Ifp公司 | The method that is used for the generative reforming catalyzer |
| CN101835877A (en) * | 2007-10-26 | 2010-09-15 | Ifp公司 | The method and the container that are used for the generative reforming catalyzer |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2007707C (en) * | 1989-01-13 | 2000-07-18 | Jean-Claude Macaire | Process for regenerating a catalyst used for the production of aromatic of reforming hydrocarbons |
| FR2651154A1 (en) * | 1989-08-25 | 1991-03-01 | Inst Francais Du Petrole | Equipment for the regeneration of a reforming catalyst or of a catalyst for the production of aromatic hydrocarbons and for the recycling of the gaseous effluents |
| WO1994005418A1 (en) * | 1992-09-04 | 1994-03-17 | Exxon Research And Engineering Company | Improved method of regenerating deactivated catalyst |
| CN1197694A (en) * | 1997-04-14 | 1998-11-04 | 法国石油公司 | Process and vessel for regenerating catalyst for production of aromatic compounds or for reforming, with improved oxychlorination |
| CN101835878A (en) * | 2007-10-26 | 2010-09-15 | Ifp公司 | The method that is used for the generative reforming catalyzer |
| CN101835877A (en) * | 2007-10-26 | 2010-09-15 | Ifp公司 | The method and the container that are used for the generative reforming catalyzer |
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