CN101569830B - Method for dechlorinating gas discharged from continuous reforming regenerator - Google Patents
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Abstract
The invention relates to a method for dechlorinating gas discharged from a continuous reforming regenerator, comprising the following steps: absorbing chloride in gas discharged from a coke-burning zone and an oxychlorination zone of the continuous reforming regenerator through a bed for catalyst to be regenerated and a bed for solid dechlorinating agent, wherein the bed for catalyst to be regenerated and the bed for solid dechlorinating agent are arranged between a gas-solid separator and a regenerator in sequence; eliminating one part of gas discharged from the bed for catalyst to be regenerated from a system, and returning the other part of the gas to the coke-burning zone of the continuous reforming regenerator; enabling gas discharged from a roasting zone of the continuous reforming regenerator to enter another dechlorinating pot filled with solid dechlorinating agent to absorb chloride therein and eliminating the gas from the system, wherein the solid dechlorinating agent comprises 50-88 percent of alkaline earth oxide by weight, 10-40 percent of alumina by weight and 2-30 percent of bentonite by weight. With the method for dechlorinating gas discharged from a continuous reforming regenerator, the gas discharged from the continuous reforming regenerator can be dechlorinated, and agent to be regenerated can absorb a certain amount of chlorine to reduce the amount of chlorine injected in the regeneration process.
Description
Technical field
The present invention discharges muriatic method in the gas for a kind of continuous reforming regenerator that removes, and specifically, is that a kind of reclaimable catalyst and antichlor of utilizing removes muriatic method in the reforming regenerator discharge gas.
Background technology
Characteristics such as height, hydrogen product height and aromatics yield height are received in the naphtha continuous catalytic reforming with its liquid, in the production of high-knock rating gasoline and aromatic hydrocarbons, receive people's very big attention, and will in reforming process evolution from now on, bring into play leading role.The core of continuous reforming process is the catalyst regeneration technology, and the chloride concentration in its regenerator exit gas is high, for satisfying the environment protection control index, just can be disposed in the atmosphere after needing to purify.
At present, the purification method of continuous reforming regenerator exit gas mainly contains alkali cleaning, solid dechlorinating agent adsorbs and reclaimable catalyst adsorbs three kinds.CN1045411A to the processing method of reforming regenerator regeneration recycle gas is: regeneration off gases is come out after heat exchange from regenerator; Further cool off through water cooler, advance caustic wash tower then, with certain density NaOH solution washing; Remove chloride and carbon dioxide in the regeneration gas; After washing section is removed alkali lye, get into drier again, reduce water content in the regeneration recycle gas, get into the regenerator scorch region again.If this method misoperation can cause equipment corrosion, even can take alkali lye in the drier to, cause drier to lose efficacy, regenerative system is compelled stops work; And the gas with alkali washing process is handled also needs washing, and the content of water in gas after the washing can not be controlled well, causes the drying system load to increase; The problems such as disposal of pollutants that also have alkali wash water have influenced the smooth operation of regenerative system long period.
CN86102807A to the processing method of reforming regenerator regeneration recycle gas is: regeneration recycle gas comes out to be divided into two-way from air blast, and one the tunnel directly removes regenerator scorch region superheat section, another road after aerial cooler cooling as one section scorch region inlet gas.This method is not carried out dechlorination to regeneration recycle gas and is handled, and adopts the method for thermal cycle, effluxes the direct emptying of regeneration off gases or through alkali cleaning emptying.
The subject matter that the alkali cleaning mode exists is: equipment investment is high, complicated operation; Increase dechlorination effect variation, the easy problem that the regenerative circuit equipment corrosion takes place the duration of runs with device.
CN1241453A and CN1241454A propose regeneration recycle gas to be handled with antichlor at low-temperature space; The gas that comes out from the chlorination district through the water cooler cooling, is handled through the dechlorination jar earlier then, mixes with the regeneration recycle gas of handling through cooling, dechlorination successively again; Again behind drier, filter, compressor and heat exchanger; Be divided into two-way and heat through two heaters respectively, a pass is gone into scorch region, and another road is that scorch region is crossed hot gas.
CN1461675A discloses a kind of purification method of circulated gas regenerated continuously by reforming catalyst; Gas behind the coke burning regeneration and the gas after the oxychlorination come out from regenerator; Use antichlor to remove chlorine wherein earlier; Then successively through cooling, dry, filter, boost, heat, all be circulated back to the section of burning of regenerator at last.The gas that the regenerator furnace zone is discharged and the gas that discharge on scorch region top mix the back and get into the dechlorination jar and contact with antichlor and remove discharge system emptying behind the chlorine.This method can regeneration recycle gas high temperature position with gas in chlorinity drop to below the 1ppm, solved the equipment corrosion problem that causes by chlorine-containing gas.
The method of the solid dechlorinating agent dechlorination that above-mentioned employing is single, because the chloride content in the regeneration recycle gas up to 1000～5000ppm, receives the restriction of the maximum chlorosity of antichlor, the replacing of antichlor is more frequent.From the result of industry operation, existing antichlor is prone to argillization, is prone to caking, influences the normal operation of device.
Above-mentioned alkali cleaning mode and single solid dechlorinating agent mode all can not be recycled the chlorine that runs off in the catalyst regeneration process.Therefore, in the regenerative process of catalyst, regeneration discharge gas is wanted dechlorination on the one hand, also will outside system, in regenerator, annotate chlorine in a large number owing to keep the needs of acidity of catalyst on the other hand, has increased operating cost undoubtedly.
US6034018 discloses a kind of method that reduces chloride content in the reforming catalyst moving bed regeneration discharge gas; This method with reclaimable catalyst before getting into regenerator earlier with contain muriatic regeneration recycle gas and contact; Behind the absorption chloride wherein; Part circulating air is by emptying, and all the other then get back to the reclaimable catalyst scorch region.This method use spent agent to be adsorbed on to burn with chlorination process in the chloride that produces, both reduced in the catalyst regeneration process muriatic injection rate outside the system, reduced the chlorinity of regenerator emission gases again.
Above-mentioned spent agent adsorption technology has only considered that spent agent can adsorb a certain amount of chloride, do not have to consider the variation owing to coke on regenerated catalyst and regeneration recycle gas component, and catalyst uses the middle and later periods specific surface to descend significantly (usually by 200m
2Drop to 130m about/g
2About/g) etc. the catalyst that causes of reason inhale the chlorine ability drop, cause muriatic content in the regeneration discharge gas to surpass the problem of environment control index request.In addition, this technology is not considered the muriatic problem that removes in the regenerator roast area excessive emissions gas yet.
Summary of the invention
The purpose of this invention is to provide a kind of continuous reforming regenerator and discharge the dechlorination method of gas, this method can be discharged the chloride in the gas at effective elimination regenerator under the high water content.
Continuous reforming regenerator provided by the invention is discharged the dechlorination method of gas; Comprise that the gas with continuous reforming regenerator scorch region and the discharge of oxychlorination district adsorbs chloride wherein through reclaimable catalyst bed and the solid dechlorinating agent bed that is arranged between gas-solid separating device and the regenerator successively; From the gas part discharge system that the antichlor bed is discharged, another part turns back to the scorch region of regenerator; After then getting into another dechlorination jar that solid dechlorinating agent is housed absorption chloride wherein, the gas of discharging from the regenerator roast area discharges system again; Described solid dechlorinating agent comprises the alkaline earth oxide of 50～88 quality %, the aluminium oxide of 10～40 quality % and the bentonite of 2～30 quality %.
The gas that the inventive method is discharged continuous reforming regenerator carries out dechlorination and purifies; Earlier with reforming catalyst to be generated and antichlor adsorbing and removing chloride wherein, the gas with the discharge of regenerator roast area also removes chloride wherein with antichlor simultaneously with the gas of regenerator scorch region discharging, has solved when only adopting in the spent agent adsorbed gas chloride; Because coke on regenerated catalyst and regeneration recycle gas atmosphere change; And catalyst uses degradation reason under the middle and later periods specific area, causes and holds the chlorine ability drop, causes chloride in the regeneration discharge gas not meet the problem of environment protection control index request; Can also recycle the chloride in the partial regeneration gas; Muriatic injection rate outside the system reduces operating cost in the minimizing catalyst regeneration process, improves the stability of regenerator operation simultaneously.Used antichlor is used for the dechlorination process of high water content gas, is difficult for argillization, has dechlorination effect preferably.
Description of drawings
Fig. 1 for the present invention with continuous reforming regenerator scorch region and oxychlorination district exit gas divide one the tunnel carry out dechlorination process flow diagram.
Fig. 2 divides two-way to carry out the process flow diagram of dechlorination continuous reforming regenerator scorch region and oxychlorination district exit gas for the present invention.
The specific embodiment
The inventive method is adsorbed the gas of continuous reforming regenerator scorch region and the discharge of oxychlorination district earlier with reclaimable catalyst; Adsorb with antichlor again; Make a part of directly chlorinity of the gas of emptying reach the environmental requirement of China; The gas chlorinity that promptly in air, discharges is back to the regenerator scorch region with the gas after a part of dechlorination simultaneously less than 100ppm.In addition, the excess air that another outlet roast area of regenerator is discharged also removes chloride wherein with antichlor, thereby whole regenerator chlorinity of emission gases in air all is up to state standards.
The inventive method is to the gas of reforming regenerator scorch region and the discharge of oxychlorination district; Be that flue gas carries out the dechlorination processing; Both can it all be sent into reformation reclaimable catalyst bed; Also can the gas that said regenerator scorch region and oxychlorination district discharge be divided into two-way, the one tunnel successively through being arranged on discharge system behind reclaimable catalyst adsorbent bed and the solid dechlorinating agent bed between gas-solid separating device and the regenerator, and another road is then through turning back to the scorch region of regenerator after heating.
In the methods of the invention; Described gas of discharging from regenerator scorch region and oxychlorination district is 50～480 ℃, preferred 120～300 ℃ through the temperature of reclaimable catalyst adsorbent bed; Pressure is 0.1～2.0MPa, preferred 0.1～0.7MPa, more preferably 0.1～0.4MPa, and volume space velocity is 5～5000h
-1, preferred 50～2000h
-1
Not only contain hydrogen chloride in the described flue gas, but also contain carbon dioxide and more water vapour and a spot of Cl
2Usually, contain the HCl of 100～5000ppm in the reformation regenerated flue gas, the CO of 0～20 volume %
2, 0.001～10 quality % water vapour.
Described solid dechlorinating agent absorption is 50～650 ℃, preferred 120～500 ℃ from discharge of reclaimable catalyst bed or the muriatic temperature from the gas that the regenerator roast area is discharged; Pressure is 0.1～2.0MPa, preferred 0.1～1.0MPa, and volume space velocity is 5～5000h
-1, preferred 50～3000h
-1For the chlorine-containing gas of from the reclaimable catalyst bed, discharging,, from the roast area excess air, adsorb preferred 250～500 ℃ of muriatic temperature with antichlor with preferred 120～300 ℃ of antichlor absorption muriatic temperature wherein.
The reforming catalyst to be generated that the present invention uses is to be carrier with aluminium oxide or the aluminium oxide that contains zeolite; The platinum tin catalyst series that contains halogen contains the platinum of 0.01～2.0 quality %, the tin of 0.01～5.0 quality %, the halogen of 0.1～10 quality % and the carrier of 83～99.88 quality % in the described catalyst.Also can further contain the 3rd, the 4th metal constituent element in the said catalyst, described the 3rd, the 4th constituent element is selected from one or more in lanthanide series metal or the titanium, preferred europium of described lanthanide series metal and/or cerium.Three, the content of the 4th metal constituent element is that benchmark is calculated as 0.01～10 quality % with the butt carrier, preferred 0.1～5.0 quality %.
Preferred 0.1～1.0 quality % of Pt content, preferred 0.1～2.0 quality % of Sn content, content of halogen are 0.1～5.0 quality % in the above-mentioned catalyst, preferred 92～99.7 quality % of vector contg.The preferred chlorine of described halogen, the preferred aluminium oxide of high-temperature inorganic oxide carrier.
Antichlor of the present invention preferably contains the alkaline earth oxide of 65～85 quality %, the aluminium oxide of 10～30 quality % and the bentonite of 2～15 quality %.
The preferred calcium oxide of alkaline earth oxide in the antichlor, the preferred gama-alumina of aluminium oxide, preferred sodium base of bentonite or calcium-base bentonite.
The preparation method of described solid dechlorinating agent comprises alkaline earth oxide or its precursor, aluminium oxide or its precursor and bentonite is mixed into raw material, add expanding agent again and mix, behind the extruded moulding 450～700 ℃ of roastings.
The preferred calcium oxide of alkaline earth oxide described in the said method, precursor preferably calcium hydroxide, calcium carbonate or the calcium bicarbonate of alkaline earth oxide.Preferred boehmite of the precursor of aluminium oxide or aluminium colloidal sol.
Described expanding agent preferable methyl cellulose or carbonic hydroammonium, the addition of expanding agent are 0.5～15 quality % of raw material total amount, preferred 1.0～10 quality %.
Among the said antichlor preparation method, after raw material being mixed and add expanding agent, be preferably and add extrusion aid again.The addition of extrusion aid is 0.5～3.0 quality % of raw material, preferred 1.0～3.0 quality %, the preferred sesbania powder of extrusion aid.Behind said solids mixing, add suitable quantity of water and mix the moulding of pinching bar, preferably in water, add peptizing agent, the dosage of peptizing agent is 0.5～15 quality % of solids total amount, preferred 1～10 quality %.Peptizing agent is selected from organic acid or inorganic acid, example hydrochloric acid, nitric acid, acetate or citric acid.Extruded moulding thing dry roasting is promptly got antichlor, preferred 50～130 ℃ of described baking temperature, sintering temperature is 450～700 ℃, preferred 450～680 ℃.
Below in conjunction with accompanying drawing the present invention is elaborated.
Among Fig. 1; Separate dedusting from the reclaimable catalyst entering gas-solid separating device 2 of lift line 1; The catalyst that separates gets into adsorbent bed 4 through catalyst blanking pipeline 3, behind the part chloride in the reclaimable catalyst absorption regeneration circulating air, gets into regenerator 6 through catalyst blanking pipeline 5.In regenerator 6, after reclaimable catalyst passes through scorch region 7, oxychlorination district 8 and roast area 9 at least successively, get into follow-up catalyst reduction district and reforming reaction district through pipeline 10.
Get into reclaimable catalyst adsorbent beds 4 through pipeline 11, heat exchanger 12, pipeline 13 successively from the regeneration gas of regenerator 6 scorch regions and the discharge of oxychlorination district.In adsorbent bed 4, contact, remove the regeneration gas behind the part chloride, get into dechlorination jars 15 through pipeline 14 with reclaimable catalyst.In dechlorination jar 15, contact with antichlor; Chloride concentration in the gas is reduced to below the 1ppm; A part gets into atmosphere through pipeline 16 direct discharge systems; Another part after pipeline 17, cooler 18, pipeline 19, drier 20, pipeline 21, circulating fan 22, pipeline 23 get into heat exchanger 12 and the regeneration gas heat exchange from pipeline 11, gets into heaters 25 heating through pipeline 24 successively, returns regenerator scorch region 7 through pipeline 26 again.
The gas of regenerator roast area 9 excessive emissions gets into dechlorination jar 28 through pipeline 27 and contacts with antichlor, removes chloride wherein, gets into atmosphere through pipeline 29 discharge systems.
The difference of Fig. 2 and Fig. 1 is that circular regeneration gas is divided into two-way.The regeneration gas of discharging from regenerator 6 is divided into two-way successively behind pipeline 11, circulating fan 22, pipeline 13, aerial cooler 14: the one tunnel gets into reclaimable catalyst adsorbent beds 4 and contacts with reclaimable catalyst through pipeline 19, heat exchanger 18, pipeline 17; Remove the regeneration gas behind the part chloride; Get into dechlorination jar 15 through pipeline 16 and contact, then through pipeline 27 direct discharge systems with antichlor; Regenerator scorch region 7 through pipeline 21, heater 25, is returned through pipeline 23 successively in another road.
The all available one or more dechlorination jars of dechlorination jar 15 and 28 among Fig. 1 and 2.When using a plurality of dechlorination jar, can carry out handover operation, this jar of when the dechlorination jar exit gas chlorinity that uses surpasses environment control index request, stopping using is launched the dechlorination jar that another is equipped with fresh antichlor simultaneously.
The inventive method be applicable to various types of use with aluminium oxide or the aluminium oxide that contains zeolite as carrier, contain the continuous regenerative reforming device of the platinum tin catalyst series of halogen.The antichlor prevented from caking that the present invention uses, be difficult for argillization, be easy to dismounting, can the chloride content that chloride content in the gas is no more than in the continuous reforming regenerator exit gas of 5000ppm be reduced to below the 0.5ppm.
Further specify the present invention through instance below, but the present invention is not limited to this.
Instance 1
The used antichlor of preparation the present invention.
(alumina content is 70 quality % to get 15 gram boehmites; PURAL
SB that Germany Sasol company produces), (the butt solid content is 90 quality % to 2 gram calcium-base bentonites; Xinyang, Henan great cause bentonite Co., Ltd) and 80 the gram calcium hydroxides be mixed and made into raw material; Add 2 gram methylcellulose (the auspicious safe chemical industry in Shandong Co., Ltd produces) and mix with 2 gram sesbania powder, add again nitric acid that 15ml concentration is 33 quality % and 45ml deionized water mix pinch even, extruded moulding; 120 ℃ of dryings 2 hours; 650 ℃ of roastings 4 hours make antichlor A, and it is formed and physical property is seen table 1; Wherein specific area and pore volume adopt low-temperature nitrogen adsorption method to measure on Micromeritics ASAP2400 analyzer, and its chlorosity that penetrates under different temperatures is seen table 2.The said chlorosity that penetrates is meant chlorine-containing gas is fed the antichlor bed, when the content of hydrogen chloride in the antichlor bed exit gas is higher than 0.5ppm, stops to feed gas, analyzes the chlorinity in the antichlor, and this value is antichlor and penetrates chlorosity.
Chlorinity is that 3052ppm, water content are 13000ppm in the regenerator outlet recyclegas.This gas is 1000h in 260 ℃, 0.35MPa, volume space velocity
-1Condition under in fixed bed, be that 4.1 quality %, specific area are 135m with carbon content
2The platinum-tin catalyst contact to be generated of/g wherein contains Pt 0.28 quality %, Sn 0.30 quality %, and all the other are alumina support; Chlorinity through reclaimable catalyst absorption back from the fixed bed discharge is the discharging gas of 285ppm, then get into one antichlor A is housed the dechlorination jar, be 1000h at 240 ℃, 0.35MPa, volume space velocity
-1Condition under contact with wherein antichlor A, the gas chlorinity＜0.5ppm after the dechlorination, antichlor A is argillization not.
With the chlorinity of continuous reforming regenerator roast area excessive emissions is that 156ppm, water content are that the gas of 650ppm is 1000h at 400 ℃, 0.35MPa, volume space velocity
-1Condition under feed the fixed bed that antichlor A is housed, absorption chlorine-containing gas wherein, the gas chlorinity＜0.5ppm after the dechlorination, antichlor A is argillization not.
Instance 4
Method by instance 1 prepares antichlor B, and different is that the bentonite amount that adds is 10 grams, and composition and the physical property of the antichlor B that makes are seen table 1, and its chlorosity that penetrates under different temperatures is seen table 2.
Instance 5
Remove the chlorine in the regenerator outlet recyclegas by instance 2 described methods, different is, and that to load in the dechlorination jar is antichlor B, the gas chlorinity＜0.5ppm after the dechlorination, and antichlor B is argillization not.
Remove the chlorine in the regenerator roast area excessive emissions gas by instance 3 described methods, different is, and that to load in the fixed bed is antichlor B, the gas chlorinity＜0.5ppm after the dechlorination, and antichlor B is argillization not.
Method by instance 1 prepares antichlor C, and different is the bentonite that adds 20 grams, and replaces methylcellulose with 10 gram carbonic hydroammonium, and composition and the physical property of the antichlor C that makes are seen table 1, and its chlorosity that penetrates under different temperatures is seen table 2.
Remove the chlorine in the regenerator outlet recyclegas by instance 2 described methods, different is, and that to load in the dechlorination jar is antichlor C, the gas chlorinity＜0.5ppm after the dechlorination, and antichlor C is argillization not.
Instance 9
Remove the chlorine in the regenerator roast area excessive emissions gas by instance 3 described methods, different is, and that to load in the fixed bed is antichlor C, the gas chlorinity＜0.5ppm after the dechlorination, and antichlor C is argillization not.
Comparative Examples 1
Chlorinity is that 3108ppm, water content are 14000ppm in the regenerator outlet recyclegas.This gas is 1000h at 260 ℃ of temperature, stagnation pressure 0.35MPa, volume space velocity
-1Condition under in fixed bed, be that 4.1 quality %, specific area are 135m with carbon content
2Platinum tin/γ to be generated-Al of/g
2O
3The catalyst contact wherein contains Pt 0.28 quality %, Sn0.30 quality %, and the chlorinity in the discharging gas is 305ppm.Chlorinity is 180ppm in the roast area excessive emissions gas.The two-way emission gases does not all meet the environment protection emission requirement of national regulation.
Table 1
Table 2
Claims (12)
1. a continuous reforming regenerator is discharged the dechlorination method of gas; Comprise that the gas with continuous reforming regenerator scorch region and the discharge of oxychlorination district adsorbs chloride wherein through reclaimable catalyst bed and the solid dechlorinating agent bed that is arranged between gas-solid separating device and the regenerator successively; From the gas part discharge system that the antichlor bed is discharged, another part turns back to the scorch region of regenerator; After then getting into another dechlorination jar that solid dechlorinating agent is housed absorption chloride wherein, the gas of discharging from the regenerator roast area discharges system again; Described solid dechlorinating agent is made up of the alkaline earth oxide of 50～88 quality %, the aluminium oxide of 10～40 quality % and the calcium-base bentonite of 2～30 quality %.
2. according to the described method of claim 1; It is characterized in that the gas of said regenerator scorch region and the discharge of oxychlorination district is divided into two-way; One the tunnel successively through being arranged on discharge system behind reclaimable catalyst adsorbent bed and the solid dechlorinating agent bed between gas-solid separating device and the regenerator, and another road is then through turning back to the scorch region of regenerator after the heating.
3. according to claim 1 or 2 described methods, the temperature of the gas that it is characterized in that discharging in described regenerator scorch region and oxychlorination district through the reclaimable catalyst adsorbent bed is that 50～480 ℃, pressure are that 0.1～2.0MPa, volume space velocity are 5～5000h
-1
4. according to the described method of claim 3, it is characterized in that the temperature of described gas through the reclaimable catalyst adsorbent bed is that 120～300 ℃, pressure are that 0.1～0.7MPa, volume space velocity are 50～2000h
-1
5. according to claim 1 or 2 described methods, it is characterized in that in the described solid dechlorinating agent adsorbed gas that muriatic temperature is that 50～650 ℃, pressure are that 0.1～2.0MPa, volume space velocity are 5-5000h
-1
6. according to the described method of claim 5, it is characterized in that in the described solid dechlorinating agent adsorbed gas that muriatic temperature is that 120～500 ℃, pressure are that 0.1～1.0MPa, volume space velocity are 50～3000h
-1
7. according to the described method of claim 1, it is characterized in that described antichlor is made up of the alkaline earth oxide of 65～85 quality %, the aluminium oxide of 10～30 quality % and the calcium-base bentonite of 2～15 quality %.
8. according to the described method of claim 1, it is characterized in that described alkaline earth oxide is a calcium oxide, described aluminium oxide is a gama-alumina.
9. according to the described method of claim 1; The preparation method who it is characterized in that described solid dechlorinating agent comprises alkaline earth oxide or its precursor, aluminium oxide or its precursor and calcium-base bentonite is mixed into raw material; Add expanding agent again and mix, behind the extruded moulding 450～700 ℃ of roastings.
10. according to the described method of claim 9, it is characterized in that described alkaline earth oxide is a calcium oxide, the precursor of alkaline earth oxide is calcium hydroxide, calcium carbonate or calcium bicarbonate.
11. according to the described method of claim 9, the precursor that it is characterized in that described aluminium oxide is boehmite or aluminium colloidal sol.
12. according to the described method of claim 9, it is characterized in that described expanding agent is methylcellulose or carbonic hydroammonium, the addition of said expanding agent is 0.5～15 quality % of raw material total amount.
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| CN107583417A (en) * | 2017-08-31 | 2018-01-16 | 沈阳三聚凯特催化剂有限公司 | A kind of normal temperature gas phase antichlor and preparation method and application |
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| CN105498858B (en) * | 2014-09-23 | 2018-06-19 | 中国石油化工股份有限公司 | The regeneration method of continuous reforming catalyst |
| CN104297425B (en) * | 2014-09-26 | 2016-01-20 | 洛阳三隆安装检修有限公司 | A kind of measuring method of continuous catalytic reforming device regeneration gas oxygen content |
| US20160175774A1 (en) * | 2014-12-18 | 2016-06-23 | Uop Llc | Process for adsorbing hydrogen chloride from a regenerator vent gas |
| CN110639598A (en) * | 2018-06-27 | 2020-01-03 | 中国石化工程建设有限公司 | Catalyst oxychlorination and drying method for catalyst regeneration process and catalyst regeneration process |
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| US6034018A (en) * | 1995-10-20 | 2000-03-07 | Uop Llc | Method for reducing chloride emissions from a moving bed catalyst regeneration process |
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