Patent
Pre-passivation process for a continuous reforming apparatus, and passivation process for a continuous reforming apparatus during the initial reaction
| العنوان: | Pre-passivation process for a continuous reforming apparatus, and passivation process for a continuous reforming apparatus during the initial reaction |
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| Patent Number: | 8,475,650 |
| تاريخ النشر: | July 02, 2013 |
| Appl. No: | 12/740458 |
| Application Filed: | October 30, 2008 |
| مستخلص: | The present invention relates to a pre-passivation process for a continuous reforming apparatus prior to the reaction, or a passivation process for a continuous reforming apparatus during the initial reaction, comprising loading a reforming catalyst into the continuous reforming apparatus, starting the gas circulation and raising the temperature of a reactor, injecting sulfide into the gas at a reactor temperature ranging from 100-650° C., controlling the sulfur amount in the recycle gas within a range of 0.5-100×10−6 L/L so as to passivate the apparatus. |
| Inventors: | Wang, Jieguang (Beijing, CN); Ma, Aizeng (Beijing, CN); Ren, Jianqiang (Beijing, CN); Ji, Changqing (Beijing, CN); Zhang, Xinkuan (Beijing, CN); Chen, Hengfang (Beijing, CN); Zhao, Yajun (Beijing, CN) |
| Assignees: | China Petroleum & Chemical Corporation (Beijing, CN), Research Institute of Petroleum Processing, Sinopec (Beijing, CN) |
| Claim: | 1. A pre-passivation process for a continuous reforming apparatus, said continuous reforming apparatus comprising a reactor, said process comprising loading a reforming catalyst into the continuous reforming apparatus, starting a gas circulation, said gas circulation including a recycle gas, and raising the temperature of the reactor, injecting sulfide into the gas circulation at a reactor temperature ranging from 100-650° C., controlling the sulfur amount in the recycle gas within a range of 3-20×10 −6 L/L so as to passivate the continuing reforming apparatus. |
| Claim: | 2. The process according to claim 1 , characterized in that the injected sulfide is hydrogen sulfide when the recycle gas is an inert gas. |
| Claim: | 3. The process according to claim 2 , characterized in that the inert gas is nitrogen gas. |
| Claim: | 4. The process according to claim 1 , characterized in that, after the passivation is finished, a purge gas is firstly introduced to replace the gas circulation in the apparatus; when the content of hydrogen sulfide in the recycle gas leaving from the outlet of the reactor is not greater than 5×10 −6 L/L, the feedstock is fed for normal reforming reaction operation, wherein the purge gas is hydrogen gas, inert gas or a mixture of inert gas and hydrogen gas. |
| Claim: | 5. The process according to claim 1 , characterized in that the recycle gas is hydrogen gas, inert gas or a mixture of inert gas and hydrogen gas. |
| Claim: | 6. The process according to claim 1 , characterized in that the sulfide is hydrogen sulfide, carbon bisulfide, dimethyl disulfide, a sulfur-containing aliphatic compound, a sulfur-containing alicyclic compound, a sulfur-containing aromatic compound, a thiophene compound, a morpholine compound or a mixture of two or more of said compounds. |
| Claim: | 7. The process according to claim 1 , characterized in that the catalyst comprises a support, 0.05-1.0 mass % of a platinum-group metal, 0.05-1.0 mass % of tin and 0.1-5.0 mass % of halogen, based on the dry basis support. |
| Claim: | 8. The process according to claim 7 , characterized in that, in the reforming catalyst, the platinum-group metal is platinum; the halogen is chlorine; and the support is alumina. |
| Claim: | 9. A passivation process for a continuous reforming apparatus during the initial reaction, said continuous reforming apparatus comprising a reaction system, said reaction system having more than one reactor including a reforming reactor, said process comprising (1) loading a reforming catalyst into the continuous reforming apparatus, starting a gas circulation, said gas circulation including a recycle gas, and raising the temperature of a reactor in said reaction system, feeding a reforming feedstock into the reaction system when the temperature of the reactor is increased to 300-460° C., introducing sulfide into the reaction system while or after the reforming feedstock is fed, controlling the ratio of the total sulfur amount introduced into the reaction system to the reforming feedstock within the range of 0.5 μg/g-50 μg/g, reducing the content of sulfide introduced into the reaction system when hydrogen sulfide concentration in the recycle gas reaches 2.0 μL/L˜30 μL/L; and (2) maintaining the reforming reactor at a temperature of 460-490° C., controlling the ratio of the total sulfur amount introduced into the reaction system to the reforming feedstock within the range of 0.2 μg/g-0.5 μg/g when the water content in the recycle gas is less than 50 μL/L, adjusting the amount of the reforming feedstock to the design value of the continuous reforming apparatus, increasing the reforming reactor temperature to 490-545° C. according to the requirements on the octane number of the liquid product, and letting the continuous reforming apparatus run under normal operating conditions. |
| Claim: | 10. The process according to claim 9 , characterized in that sulfide is introduced into the reaction system in the manner of adding sulfide into the reforming feedstock. |
| Claim: | 11. The process according to claim 9 , characterized in that sulfide is introduced into the reaction system in the manner of adding hydrogen sulfide or a hydrogen sulfide-containing gas into the recycle gas. |
| Claim: | 12. The process according to claim 11 , characterized in that the hydrogen sulfide-containing gas is a hydrogen-containing gas having a hydrogen sulfide content of 50-5000 μL/L. |
| Claim: | 13. The process according to claim 9 , characterized in that sulfide is introduced into the reaction system in the manner of adding hydrogen sulfide or a hydrogen sulfide-containing gas into the recycle gas and adding sulfide into the reforming feedstock. |
| Claim: | 14. The process according to claim 9 , characterized in that the reforming feedstock introduced in step (1) is in an amount of 50-75 mass % of the designed feed rate of the reforming apparatus. |
| Claim: | 15. The process according to claim 9 , characterized in that the sulfide initially introduced in step (1) should enable the ratio of the total sulfur amount introduced into the system to the reforming feedstock to be 0.6-20 μg/g. |
| Claim: | 16. The process according to claim 9 , characterized in that, when the concentration of hydrogen sulfide in the recycle gas reaches to 2.0-4.0 μL/L, the ratio of the total sulfur amount introduced into the system to the reforming feedstock is controlled to be 0.2˜0.5 μg/g. |
| Claim: | 17. The process according to claim 9 , characterized in that, after the ratio of the total sulfur amount introduced into the system to the reforming feedstock in step (1) is reduced to 0.2˜2.0 μg/g, a regeneration system is started for the cyclic regeneration of the catalyst when the hydrogen sulfide in the recycle gas is in a concentration of less than 5.0 μL/L. |
| Claim: | 18. The process according to claim 9 , characterized in that the recycle gas is hydrogen gas, inert gas or a mixture of inert gas and hydrogen gas. |
| Claim: | 19. The process according to claim 18 , characterized in that the inert gas is nitrogen gas. |
| Claim: | 20. The process according to claim 9 , characterized in that the sulfide is hydrogen sulfide, carbon bisulfide, dimethyl disulfide, a sulfur-containing aliphatic compound, a sulfur-containing alicyclic compound, a sulfur-containing aromatic compound, a thiophene compound, a morpholine compound or a mixture of two or more of said compounds. |
| Claim: | 21. The process according to claim 9 , characterized in that the catalyst comprises a support, 0.05-1.0 mass % of a platinum-group metal, 0.05-1.0 mass % of tin and 0.1-5.0 mass % of halogen, based on the dry basis support. |
| Claim: | 22. The process according to claim 21 , characterized in that, in the reforming catalyst, the platinum-group metal is platinum; the halogen is chlorine; and the support is alumina. |
| Current U.S. Class: | 208/133 |
| Patent References Cited: | 2863825 December 1958 Engel 3999961 December 1976 White et al. 4159938 July 1979 Lewis 4220520 September 1980 Carter et al. 5200059 April 1993 Bogdan et al. 6495487 December 2002 Bogdan 6780814 August 2004 Ma et al. 962210 February 1975 85106828 March 1987 1126607 November 2003 1160435 August 2004 1234455 January 2006 |
| Other References: | Baokun, L., “Industrial Application of a Continuous Reforming Catalyst GCR-100” Petroleum Processing and Petrochemicals (Aug. 2002) pp. 26-29, vol. 33, No. 8, together with English-language abstract. cited by applicant Lian, T. et al., “Commercial Application of PS-VI Continuous Reforming Catalyst” Industrial Catalysis (Sep. 2003) pp. 5-8, vol. 11, No. 9, together with English-language abstract. cited by applicant Catalytic Reforming Process and Engineering, 1st Edition (Nov. 2006) China Petrochemical Press, pp. 522-534, as described in the specification on p. 2, line 20. cited by applicant Catalytic Reforming, 1st Edition (Apr. 2004) China Petrochemical Press, pp. 200-202, as described in the specification on p. 3, line 16. cited by applicant |
| Primary Examiner: | McCaig, Brian |
| Attorney, Agent or Firm: | Scully, Scott, Murphy & Presser, P.C. |
| رقم الانضمام: | edspgr.08475650 |
| قاعدة البيانات: | USPTO Patent Grants |
| الوصف غير متاح. |