 Method of producing crystal aluminium phosphate
专利摘要:
A novel family of crystalline, microporous aluminophosphate compositions is synthesized by hydrothermal crystallization at elevated temperatures of aluminophosphate gels containing a molecular structure-forming template. The family comprises a number of distinct species, each with a unique crystal structure. Calcination removes volatile extraneous matter from the intracrystalline void space and yields microporous crystalline adsorbents with uniform pores, the dimensions of which vary, among the individual species, from about 3A to 10A in diameter. The compositions represent a new class of adsorbents of the molecular sieve type, and also exhibit properties somewhat analogous to zeolitic molecular sieves which render them useful as catalysts or catalyst bases in chemical reactions such as hydrocarbon conversions. 公开号:SU1461371A3 申请号:SU813317302 申请日:1981-07-06 公开日:1989-02-23 发明作者:Томас Вильсон Степен；Мейтак Лок Брент；Мари Фланиген Эдит 申请人:Юнион Карбид Корпорейшн (Фирма)； IPC主号:
专利说明:
one This invention relates to the technology of producing aluminophosphates and may find application in chemical technology. The purpose of the invention is to obtain aluminum phosphate, possessing its properties of molecular sieves. Example A1P04-5. 1. Preparation The reaction mixture was prepared by combining 46.1 g of 85% orthophosphoric acid (HjPO)) and 100.0 g of water, to which 27.5 g of hydrated alumina oxide (pseudo-boehmite phase 74.2 wt.% % AljOj, 25.8 wt.%) And mix until homogeneous. To this mixture, 176.8 g of an aqueous solution of 23% by weight of tetrag1p 1 hydroxide hydroxide was added. 3,146 nor (GTPA), the mixture is stirred until homogeneous. The composition of the final reaction mixture in molar ratios of oxides is as follows: 0.5 (T11A) 20:: Pr0.5-: where TPA is tetrapropylammonium. The reaction mixture is placed in a pressure vessel, and in stainless steel lined with polytetrafluoroethylene, and heated in an oven at autogenous pressure for 43 hours. The solid reaction product is filtered, washed with water and dried in air at room temperature. Example 2. Cooking. The reaction mixture is prepared; by combining 23.1 g of 85% and 44.0 g of water, to which 13.7 g of hydrated alumina used in Example 1 is added and stirred until homogeneous. 35.1 g are added to this mixture; of an aqueous solution of 58% htpa, the mixture is stirred until homogeneous. The composition of the resulting reaction mixture in. The molar ratio of oxides is as follows: 0.5 (TIIA.) i Al.O:::: 40 HgO. The reaction mixture is placed in a stainless steel pressure vessel, lined from the inside with polytetrafluoroethylene, and heated in an oven at 150 ° C with autogenous pressure for 65 hours. The solid reaction product is filtered off, washed with water and dried in air at room temperature. Part of the solid particles are subjected to x-ray and chemical akalizam. Chemical analysis, wt.%: C 7.5; N 0.67; 34.2; P20, f-46.5; rubbed and on ashing at for 4 h 17.7, which gives the following composition-; duct in a molar ratio of oxides of 0.08 (TPA) O i : 0.98 FjO.f: 1.3 yCi, Example 3. Preparation. The reaction mixture is prepared by combining 46.1 g of 85% water to 118.6 g of water, to which 27.5 g of the pseudo-boehmite phase 74.2 may be added. 25.8 wt.%) And mix thoroughly until homogeneous. To this mixture was added 29.2 g of tripropylamine (Prj N) and a mixture of pe stir until homogeneous. The resulting mixture has the following composition in the form of molar ratios g oxides: 1,0 PrjN:: R. 0:: 40. The reaction mixture is placed in a pressure vessel, lined with polytetrafluoroethylene, and 0 is heated in an oven at 50 ° C under autogenous pressure for 70 hours. The solid reaction product is removed by filtration, washed with water and dried in air at room temperature. Chemical anapiv, wt.%: C 5.7; N 0.72; 34.0; P 0 48; loss on ashing 16.4, which corresponds to the following composition of the product in 0 form of oxides molar ratios: 0.16PrjN: 1,: l, 02P,: 1.5 HiO. Example 4. Preparation A1P04-5. 25 The reaction mixture was prepared by combining 46.1 g of 85% and 119.2 g of water, to which 27.5 g of hydrated alumina (74.2% by weight, 25.8% by weight 30 IgO) and shaken to a homogeneous state. 30.4 g of triztilamine (EtjN) are added to this mixture and the mixture is again stirred until a homogeneous state. Composition received 25 The reaction mixture in the form of oxide molar ratios is as follows: 1.5 EtaN: AljO:: AO. The reaction mixture is placed in a pressurized pressure vessel made of stainless steel lined with polytetrafluoroethylene and heated in an oven at an autogenous pressure for 27 hours. The solid: product is reacted by 45 filtered, washed with water and dried in air at room temperature. Chemical analysis, wt.%: C 4.8; N 0.97; AliOj 35.3; PjOr49,7; gag tering for ashing to 13.6, which corresponds to the following composition in the form of oxide molar ratios: 0.19:: 1.00 AliOg: 1.01: 1.1 HjO. Examples 5-23. Preparation gg A1P04-5. The technology was repeated, similar to the technology of Example 3, but the time and reaction temperature are taken according to the table. 1. The composition of such each finite, mixture in the form of molar ratios of oxides is as follows: 1.0 R:,:: 40, where R is from table. one; Each solid part The reactions were subjected to X-ray examination and in each case a phase was observed, characterized by a Debat-Scherrer diffraction X-ray diffraction pattern, essentially the same as in Phase 1, alone or in (. mixture with other products. Example 24. Preparation. The reaction mixture is prepared by combining 8.9 g of 85% and 6 g of water and mixing until homogeneous. To this mixture was added 27.2 g of an aqueous solution of 37% tetrabutypammonium hydroxide (GOTVA) and 2.0 g of water, and the mixture was stirred until a homogeneous state. The composition of the resulting reaction mixture in molar ratios of oxides is as follows: 0.5 (TBA) gO::: 52 The reaction mixture is placed in a pressurized pressure vessel made of stainless steel, lined from the inside with an inert plastic / CMI material, and heated in an oven at autogenous pressure for 145 hours. The solid reaction product is filtered through, rinsed with water , dried in air at 1 15 C. Chemical analysis, wt.%: With 0.2; N 0.05; 34.7; 46.6; loss on ashing 18.4, which corresponds to the product with the following composition in the form of molar oxide ratios: 1.00: 0.97 P 0: : 3,00 HgO .. Examples 25-27. Preparation of A1P04-8. A procedure was carried out, analogously to Example 24, except for the parameters listed in Table. 2. The composition of each final reaction mixture in the form of oxide molar ratios is as follows: 1.0 R:: P2.0j-: : JSC HgO, where R from table. I. The varieties are crystalline metal phosphate, whose characteristic framework structure has a chemical composition that is expressed in the form of molar oxides: AHgOz: 1.0 and 0.2 P 0. Example 28. Preparation of A1P04-9. 0 5 0 5 0 5 0 45 9 five The reaction mixture is prepared by combining 27.6 g of 85% and 36.0 g of water, to which 16.5 g of hydrated alumina is added (pseudo-boehmite phase 74.2% by weight of AliOj, 25.8% by weight) and stirred until homogeneous. To this mixture was added 13.5 g of DABCO, dissolved in 24.0 g of water, then 11.7 g of water, and the mixture was stirred until homogeneous. The composition of the resulting reaction mixture in the form of oxide molar ratios is as follows: 1.0 DABO:: Pr Oj-: 40. The reaction mixture is placed in a hermetic vessel working under pressure, stainless steel, lined from the inside with an inert plastic material, and heated in an oven for 336 h under autogenous pressure. The solid reaction product is isolated and washed by repeated centrifugation with water and dried in air at. Part of the solid particles is subjected to x-ray and chemical analysis of the memory. Chemical analysis, wt.% C 10.6; 3.9; R2.05-46.5; loss on ashing to 19.0, which corresponds to the composition of the product with the molar ratio of oxides: 0.46 PENCO: 1.00:: 1.03 P, jOr: 0.44. Example 29. Manufacturing. The reaction mixture was prepared by combining 46.0 g of 85% HjPO- / and 119.2 g of water, to which 27.5 g of the same hydrated alumina as in Example 1 was added and stirred until homogeneous. condition To the resulting mixture, 20.3 g of di- (n-propyl) amine () was added and this mixture was stirred until a homogeneous state. The composition of the resulting final reaction mixture corresponds to the following form in molar ratios x: 1.0 WG; 2.H i (: P 0 0j-:: 40 2.0. The reaction mixture is placed in a pressurized, pressure-resistant stainless steel vessel, lined inside with polytetrafluoroethylene, and heated in an oven at 200 ° C under autogenous pressure for 24 hours. The solid reaction product is separated by filtration, washed with water and air dried in rooms .7 Noah temperature. Chemical analysis of solid particles obtained as a result of the reaction, C 5,1; N 1.00; AltOj 37.6; PjrO 51.6; ash loss 10.4; which corresponds in molar ratios of oxides to the product of the following composition: 0.19: i 1,00 AliOj; 0.98 30-33. : 0.48 Prepared Examples are A1P04-11. The procedure is repeated, similar to example 29, except for the parameters listed in table. 3. The composition of each finished reaction mixture in molar ratios of oxides is as follows: 1.0 R::: 40. The twist product of each reaction contains in each case a phase characterized by x-ray diffraction with a Deb-a-Scherrer gram that is essentially the same as the x-ray of the undigested product from Example 29. The varieties are crystalline metallog phosphate, whose characteristic frame structure has a chemical composition, expressed as molar ratios of oxides:, 1.0 i 0.2 Example 34. Preparation of A1P04-12. The reaction mixture is prepared by combining 46.0 g of 85% HsP04 and 119.2 g of water, to which.4 Add 27.5 g of the same hydrated alumina as in Example 1 (pseudo-boehmite phase, 74.2 wt.% AliOj, 25.8 wt.% NdO), and mix the mixture until homogeneous. To this mixture is added 6.0 g of ethylene diamine (), and the mixture is stirred until a homogeneous state. The composition of the final reaction mixture in the form of oxide molar ratios follows Total: 0.5 CaHjN R.O. : 40. The reaction mixture is placed in a pressurized, stainless steel pressure vessel, lined inside with polytetrafluoroethylene, and heated in an oven at 200 s under autogenous pressure for 24 hours. temperature Chemical analysis, May. %: C 4.3; N 4.3; AljO 35.0; 49.5; ash loss 15.4, which corresponds to eight the composition of the product in the form of molar CO ratios of oxides: 0.52: : 1.00 A1.05: 1.02 P.0: 0.75. Example 35. Preparation of A1P04-I2. The reaction mixture is prepared by combining 76.8 g of 85% HjPG and 83.7 g of water, to which 45.8 g of hydrated alumina is added and stirred until homogeneous. 28.7 g of 2-imvdazolidone ((CH NHjiCO) dissolved in 75 g are added to this mixture. The mixture is stirred to a homogeneous state. The composition of the final reaction mixture is in the form of molar ratios of oxides five about 0 0 five 0 Rao five Next:: 50 NgO. The reaction mixture is placed in a pressure vessel made of stainless steel, lined from the inside with a neutral lining, and the bottom. heat in an oven at autogenous pressure for 169 hours. The solid reaction product is isolated by filtration, washed with water and dried in air at. Chemical analysis, wt.%: C 5.2; N 6.2; AliOj 33.2; 48.3; loss of ashing to 18.1, which corresponds to the composition of the product, expressed as molar ratios of oxides. as follows: 0.68 () CO: AljrOj: 1.04: 0.97. The above indicated product appears, characterized by a Deba-Scherrer x-ray diffraction pattern, substantially identical to the X-ray pattern of example 34. Example 36. Preparation. The reaction mixture is prepared by combining 57.7 g of 85% HjPO and 100 g of water, to which 34.4 g of hydrated alumina (74.2% by weight, 25.8% by weight of HgO) is added and stirred until homogeneous. 18.3 g of tertiary butylamine (tertiary BuNHj) and then 49.1 g of water are added to this mixture, and the mixture is stirred until a homogeneous state. The composition of the obtained reaction mixture in the form of molar ratios of 5 research institutes of oxides is expressed as follows: 1,0-tertiary BuNifj:: 40. The reaction mixture is placed in a pressure vessel A1.0 stainless steel, provided with an inert plastic lining, and heated in an oven at autogenous pressure for 96 hours. The solid reaction product is isolated by filtration, washed with water and dried in air at 110 ° C, Chemical analysis, wt.%: C 7,2; N 2,6; AljOs 34.3; PiO. 47.7; loss on ashing 17,5; which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.49 tertiary BuNHj: 1.00:: 1.00 P-jO: 0.91 H.jO. Example 37. Cooking. The reaction mixture is prepared by combining 46.1 g of 85% and 119.2 g of water, to which 27.5 g of the same hydrated alumina as in Example 24 is added and stirred until homogeneous. To this mixture was added 11.8 g of iso-propylamine (i-PrNH) and the mixture was stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios has the following form: 1.0 i-PrNlIi:: 40. The reaction mixture is placed in a sealed pressure vessel. stainless steel lined from the inside with an inert plastic material (polytetrafluoroethylene) and heated in an oven at 200 ° C under autogenous pressure for 24 hours. The solid reaction product is filtered by filtration, washed with water and dried in air at room temperature. Chemical analysis, wt.%: C 6.0; N 2.4; 34.8; , 6; ash loss 16.1; which corresponds to a product having the following composition in the form of molar ratios of oxides: 0.49 i-PrNHj: 1.00 AlgOj:: 1.00 PiOj-: 1.03 N.O. Example 38. Preparation of A1P04-16 ,. a) The reaction mixture was prepared by combining 57.7 g of 85% water and 69.6 g of water, to which 34.4 g of hydrated oxide was added with alumina 29.1 of water and the resulting mixture was stirred until homogeneous. The composition of the resulting reaction mixture in molar ratios of oxides is as follows: 1.0 N:::: 40 H2O. The reaction mixture is placed in a sealed pressure vessel; 10, made of stainless steel, lined from the inside with an inert plastic material, and heated in an oven at autogenous pressure for 48 hours. The solid reaction product is; 15ci are isolated by filtration, washed with water and dried in air with PO C. Chemical analysis, wt.%: C 7.7; N 1.33; 32.4; .Pj.05-43,4; ash loss 24.1; which corresponds to the composition of the product with the molar ratio of oxides: 0.28 CyH, jN: 1.00 0.96. : 2.45. B) Similarly, but the ratio x, 5 nuclidine reduced by 50% and the mixture is heated at 2pc for 24 h, get A1RSTS-16. A small amount is also present as an impurity. AP, c) The procedure and composition of the gel from of the example of ZVa is repeated, except that the reaction mixture is heated for 16 hours. Part of the solid parts; subjected to x-ray analysis. The specified product is defined as A1P04-16 on the X-ray diffraction pattern of Deb-Sherrer, essentially identical to the X-ray pattern of example 38a. 40 d) A portion of the crystalline solid obtained above is melted in air at a temperature of 200 to 1 hour and then for approximately 45 2 hours. The calcined product has a X-ray diffraction pattern of Debé Sherrer, almost identical to the X-ray diffraction pattern of example 38c. PRI me R 39. Cooking 50 A1P04-17. a) The reaction mixture was prepared by combining 56.7 g of 85% HzRO and 69.6 g of water, to which 34.4 g of hydrated alumina was added. nor (pseudoboehmite phase, 74.2 kk (pseudo-obemktna phase 74.2 wt.% , 25.8 wt.% HgO) and mixed with Al Oj, 35.8 wt.%, And stirring; until homogeneous. To this, until a homogeneous state. To this mixtures are added 27.8 g of quinuclide mixture 27.8 g of quinucleans () dissolved in 50.4 g of water. (), dissolved in 50.4 g of water, 1 then 29.1% water and the resulting mixture is stirred until homogeneous. The composition of the resulting reaction mixture in molar ratios of oxides is as follows: 1.0 N:::: 40 H2O. The reaction mixture is placed in a sealed pressure vessel; stainless steel lined from the inside with an inert plastic material, and heated in an oven at autogenous pressure for 48 hours. The solid reaction product is; The extracts are isolated by filtration, washed with water and dried in air with PO C. Chemical analysis, wt.%: C 7.7; N 1.33; 32.4; .Pj.05-43,4; ash loss 24.1; which corresponds to the composition of the product with the molar ratio of oxides: 0.28 CyH, jN: 1.00 0.96. : 2.45. B) Similarly, but the ratio x, of the nuclidine is reduced by 50% and the mixture is heated at 2pc for 24 hours, get A1RSTS-16. A small amount is also present as an impurity. c) The procedure and composition of the gel from of example, Zva is repeated, except that the reaction mixture is heated for 16 hours. Part of the solid particles; subjected to x-ray analysis. The specified product is defined as A1P04-16 on the X-ray diffraction pattern of Deb-Sherrer, essentially identical to the X-ray pattern of example 38a. . d) A portion of the crystalline solid obtained above is melted in air at a temperature of 200 to 1 hour and then for approximately 2 h. The calcined product has a X-ray diffraction pattern of Deb-Sherrer, almost identical to the X-ray pattern of example 38c. PRI me R 39. Cooking A1P04-17. a) The reaction mixture is prepared by combining 56.7 g of 85% HzRO and 69.6 g of water, to which 34.4 g of hydrated alumina is added. then 29.1 g of water and the mixture is stirred until homogeneous. The composition of the final reaction mixture in the form of molar ratios of oxides of oxides: 1.0 SuNC: A1-0,: P, 0j: 40. The reaction mixture is placed in a hermetic pressure vessel, made of stainless steel, lined inside with an inert plastic material (polytetrafluoroethylene), and heated in an oven at 200 ° C under autogenous pressure for 96 hours. The solid reaction product is filled with and washed by re-centrifuging with water and drying in air under PO. Chemical analysis, May.%: C 12.4 N 2.2; A120332.5; 45.9; loss on ashing to 21.4, which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.46: 1.00: 0.99 0.87. b) A portion of the solid crystalline product obtained after continuing dehydrogenation of the said reaction mixture to 168 hours shows a X-ray diffraction pattern of Deba-Sherrer, identical to the product from Example 39a. c) A portion of the product from Example 39b is calcined in air for approximately 2 hours. Example 40. Preparation of A1RO, -17. The reaction mixture is prepared by combining 115.3 g of 85% and 256 g of water to which 68.7 g of hydrated alumina (pseudo-boehmite phase, 74.2% by weight of AljOj 25.8% by weight) and mix until homogeneous. 43.6 g of neopentipamine () and then 44.1 g of water are added to this mixture, and the mixture is stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios is as follows: 1.0 C, j-HyjN:: AHgOz:: 40 H, 0. The reaction mixture is placed in a hermetic pressure vessel made of stainless steel, lined from the inside with an inert plastic material (polytetrafluoroethylene), and heated in an oven at 150 ° C under autogenous pressure for yu 15 20 25 thirty , - 35 40 e 0 168 h. The solid products of the reaction are isolated and washed by repeated centrifugation with water and dried in air at. Chemical analysis, wt.%: C 9.9; N 2.5; 32.6; 44.2; loss of ashing 21,8; which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.52 1.00 Ain,: 0.97Р, 0 ,. :: 1.28. Examples 41 and 42. Preparation. The procedure, similar to Example 39, is repeated, with the exception of the parameters: 4. The composition of each final reaction mixture in the form of oxide molar ratios is as follows: 1.0 R: AljOj:: 40, where R is from the table. 4. A part of the solid product from each reaction is subjected to an x-ray study and in each case a phase is observed characterized by the presence of a Debat-Scherrer diffraction X-ray diffraction pattern, almost similar to the X-ray diffraction pattern of the product from example 39a .; Example 43. Preparation of A1P04-I8. The reaction mixture is prepared by combining 46.1 g of 85% HjPO and 53.8 g of water, to which 27.5 g of the pseudo-boehmite phase (74.2 wt.% 25.8 wt.%) Are added, and stirred until homogeneous state. To this mixture is added a water solution prepared by combining 6.5 g of 37% HCl and 98.0 g of 40% tetraethylammonium hydroxide (GOTEA), and the mixture is stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios is as follows: 0.33 HC1:: 0.67 (TEA);, 0::: 40 H2O. The reaction mixture is placed in a pressurized, stainless steel pressure vessel, lined from the inside with an inert plastic material (polytetrafluoroethylene), and heated in an oven at autogenous pressure for 336 hours. The solid reaction product is filtered by filtration, washed with water and air dry at room temperature., Chemical analysis, wt.%: C 8.9; N 1.28; 33.5; Р 05-38,9; 13 terry on ashing 26.4; which corresponds to the following composition of the product in the form of oxide molar ratios: (T3A) jO: 1.0 AliOj: 0.83: 0.9 HiO. Example 44. Cooking. a) The reaction mixture is prepared by mixing 23.1 g of 85% and 34.6 g of water, to which 13.8 g of hydrated alumina is added and stirred to a homogeneous state. The reaction mixture is placed in a pressurized pressure vessel made of stainless steel, veneered from the inside with an inert plastic. To this mixture, 36.2 g of foam material is added, and heated in an oven. tetramethlammonium hydroxide tetrahydrate (GOTMA 5), dissolved in 50 g of water, and the mixture stirred until homogeneous. The composition of the final reaction mixture in the form of molar ratios of oxides is as follows: 0.5 (TMA) 20:: P, 0: 43. The reaction mixture is placed in a pressurized pressure vessel made of stainless steel, lined from the inside with polytetrafluoroethylene, and heated in an oven at 50 ° C under autogenous pressure for 71 hours. The solid reaction product is injected by re centrifuging and washing with water and dried; in air at room temperature. The chemical composition of the product ,, wt.%: C 6.0; N 1.76; 32.7; . iQf 44.9; loss on ashing is 22.8; which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.20 (TMA) О: 1.0 AlgOj:: 0.98 P.jOj-: 2.17. b) A portion of the solid crystalline product obtained using a similar procedure and characterized by a diffraction, x-ray pattern of Deb-Scherrer, essentially identical to the x-ray pattern of example 44a, is subjected to calcination in air at 100 s for 1 hour at 200 s for 1 h, at for 1 hour and finally for 1 hour, Example 45; Cooking .A1P04-20, The reaction mixture was prepared by combining 57.6 g of 85% and 90.5 g of water, to which 37.8 g of the same hydrated alumina as in Example 40 was added and mixed until homogeneous. 36.2 g of penta are added to the mixture. Cooking at 150 ° C under autogenous pressure for 72 hours. The solid product was removed by centrifuging and rinsing with water and dried at 10 ° C. Example 4b. A1PQ.-20. The reaction mixture is prepared by combining 92.1 g of 85% HzP04 and 25 220.9 g of water, to which 55.0 g of hydrated alumina (pseudo-boehmite phase 74.2 wt.% 25.8 wt.%) Are added and stirred until homogeneous. To this 30 mixtures were added 72.5 g of tetramethylammonium hydroxide pentahydrate (GOTMA 4.5) dissolved in 50 g, and the mixture was outweighed to a homogeneous state. To this mixture is added 25 13.0 g of NaA zeolite, the mixture is subjected to homogenization. With the exception of NaA zeolite, the composition of the final reaction mixture in the form of oxide molar ratios is as follows: 0.5 (TMA),: 40:: Pj, 0: 50-H- O, The reaction mixture is placed in a stainless steel pressure vessel, which has a plastic lining inside, and is heated in a furnace at 125 ° C under autogenous pressure for 53 hours. The solid reaction product is isolated by centrifugation and rinsed with water and dried air at. Example 47. Cooking, The reaction mixture was prepared by combining 57.7 g of 85% PzRO and 80.4 g of water, to which 55 34.4 g of hydrated alumina (55.2 wt.% AljO, pseudo-boehmite phase, 25.2 wt.%) Were added. %) and mix until homogeneous. .. To this mixture add 110.6 g of water. tetramethylammonium hydroxide hydroxide (GOTMA-5) and 2.0 g of sodium hydroxide dissolved in 50 g of water, and the mixture is stirred until a homogeneous state. The composition of the final reactive mixture in the form of oxide molar ratios is as follows: 0.1 NagO: : 0.4 (TMA) 20: 1.1::: 43 NgO. The reaction mixture is placed in a pressurized pressure vessel made of stainless steel, lined from the inside with an inert plastic material, and heated in an oven. 15 kim material, and heated in an oven Cooking at 150 ° C under autogenous pressure for 72 hours. The solid reaction product is extracted by centrifuging and rinsing with water and dried on air at 1-10 ° C. Example 4b. A1PQ.-20. The reaction mixture is prepared by combining 92.1 g of 85% HzP04 and 25 220.9 g of water, to which 55.0 g of hydrated alumina (pseudo-boehmite phase 74.2 wt.% 25.8 wt.%) Are added and stirred until homogeneous. To this 30 mixtures were added 72.5 g of tetramethylammonium hydroxide pentahydrate (GOTMACH 4.5), dissolved in 50 g, and the mixture was outweighed to a homogeneous state. To this mixture is added 25 13.0 g of NaA zeolite, the mixture is subjected to homogenization. With the exception of NaA zeolite, the composition of the final reaction mixture in the form of oxide molar ratios is as follows: 0.5 (TMA),: 40:: Pj, 0: 50-H- O, The reaction mixture is placed in a stainless steel pressure vessel, having a plastic lining inside, and heated 5 in an oven at 125 ° C under autogenous pressure for 53 hours. The solid reaction product is isolated by centrifugation and rinsed with water and dried in air at . Example 47. Cooking, The reaction mixture was prepared by combining 57.7 g of 85% PzRO and 80.4 g of water, to which 5 34.4 g of hydrated alumina was added (pseudo-boehmite phase 74.2 wt.% AljO, 25.8 wt. %) and mix until homogeneous. .. To this mixture add 110.6 g of water. 68.2 wt.% N, N-dimethyl-1,4-diazabicyclo (2.2.2) octane (DDO) dihydroxide, the mixture is stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios is as follows: 1.7 DCO: AljOa:: 40. The reaction mixture is placed in a pressurized pressure vessel, lined with stainless steel, and heated in an oven at 200 ° C under autogenous pressure for 72 hours. The solid reaction product is isolated by filtration,. rinse with water and air dry at 110 C. Chemical analysis, wt.%: C 9.6; N 2.9; 33.2; PzO 47.6; ashing loss 19.4; which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.31 DCO: 1.0 AljOj: 1.03:: 0.31 HjO. Example 48. Preparation of A1P04-25.a) The reaction mixture is prepared by combining 7.7 with 85% and 25.9 g of water, to which 4.6 g of pseudo-boehmite phase f74.2 wt.%, 25 , 8 wt.% H20) and stirred until homogeneous. 2.4 g of (CII) NH (pyrrolidine) are added to this mixture, and the mixture is stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios is as follows: 1.0 (CHg): NH::: 40 HjO. The reaction mixture is placed in a stainless steel pressure vessel, lined with polytetrafluoroethylene, and heated in an oven at 150 ° C under autogenous pressure for 150 h. The solid reaction product is isolated by filtration, rinsed with water and dried in air at 110 C. Chemical analysis, wt.%: C 10.2; N 3.2; 32,); P 05-47.1 loss on ash content 19.8; which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.67 (CHi) 4NH: 1.00 G: 1.05 RDO: 0.83 HgO. b) A procedure similar to Example 48a is repeated, except as indicated in Table. 5. A part of the solid product of each reaction is subjected to X-ray analysis, and in each case, one or a mixture is observed in the phase, characterized by a X-ray diffraction diffraction pattern. c) Cooking. Part of the A1RO + -21 crystalline product is calcined in air at a temperature of approximately 600 ° C for 2 hours. The calcined product had a Debra-Scherrer diffraction X-ray diffraction pattern different from the original A1P04-21 and is a new kind of microporous apyumophosphate (A1P04-25 ). Example 49. Cooking. The Pt-dry mixture was prepared by coeduction of 23.1 g of 85% and 77.6 g of water, to which 13.8 g of hydrated alumina (pseudo-boehmite phase, 74.2% by weight of AlgO, 25.8% % HjO) and stirred until homogeneous. 7.1 g (CH): III (pyrrolide) is added to this mixture, and the mixture is stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios is as follows: 1.0 (СН.,) NH .. 3; PjOf: 50. The reaction mixture is placed in a pressurized pressure vessel made of stainless steel, lined from the inside with an inert plastic material, and heated in an oven at autogenous pressure for 91 hours. The solid reaction product is filtered, washed with water and dried. in the air at. Chemical analysis, wt.%: C 9.9; N 31; A1gOz 32.8; P or 47.5; ash loss 19.3; which corresponds to the following composition of the product in the form of molar ratios: 0.64 (CHj,) JNH:: 1.00 Alg.0z: 1.04: 0.79. Example 50. Preparation of A1P04-31. The reaction mixture is prepared by dispersing 164.8 g of the pseudo-boehmite phase (74.2 wt.% AlzOg; 25.8 wt. HgO) into 715.2 g of water, to which 276.7 85% NdRO is added and stirred until homogeneous state nc To this mixture, 121.4 g of di- ((-propro PIP) amine () was added and the mixture was stirred until homogeneous. The composition of the final reaction mixture in the form of oxide molar ratios is as follows: 1.0::: AO HgO. The reaction mixture is placed in a stainless steel pressure vessel, lined inside with polytetrafluoroethylene, and heated in an oven at autogenous pressure for 46 hours. The solid reaction product is separated by re-centrifuging and washing with water and distilled air at room temperature. Chemical analysis, wt.%: C 4.7; N 0.85; 37.4; P20i-51.6; ash loss 10.3; which corresponds to the following composition of the product in the form of molar ratios of oxides: 0.18: 1.00: 0.99Pj, 0: 0.56 H2.0. Example 57 a) The adsorption properties of the A1P04-5 composition prepared in Example 3 are determined using a standard McBain-Bakr gravimetric adsorption apparatus. On a sample activated by, the data presented in tab. 6 .. The pore size of the product subjected to calcination exceeds 6 and below IDA, as can be seen from the adsorption of neopentane, a kinetic diameter of 6.2 A, and a negligible adsorption (. 9) 3, a kinetic diameter of 10 A. b) The adsorption properties of A1P04-5 obtained in Example 2 are determined using the standard gravimetric adsorption apparatus Mac-Bain-Bakr 4 The following data was obtained on a sample activated at 350 ° C (Table 7). The pore size of the product subjected to calcination exceeds 6.2 A, as can be seen from the adsorption of neopentane, with a kinetic diameter of 6.2 A. c) The adsorption properties obtained as in Example 2, were determined using a standard Mac-Bain-Bakr gravimetric adsorption apparatus. The following data was obtained on a sample activated at 350 ° C (Table 8). Example 52. The adsorption properties (obtained in Example 49) are determined using a mill. d 15 20 25 ZO 40 0 Mac-Bain-Bakr gravimetric adsorption apparatus. The following data was obtained on a sample activated with (table. 9). The pore size of the calcined product exceeds 2.65 Au less than 3.46 A, as can be seen from water adsorption, kinetic diameter A, and slight adsorption 0, kinetic diameter 3.46 A. Example 53. The adsorption properties of A1P04-25, obtained in Example 48, were determined using a standard Mac-Bane-Bakr gravimetric adsorption apparatus. The following data was obtained on a sample activated at 350 ° C (Table 10). The pore size of the calcined product is 3.4 and 4.3 A, as can be seen from the adsorption of oxygen, with a kinetic diameter of 3.46 A, and a slight adsorption of n-hexane, with a kinetic diameter of 4.3 1. Example 54. The adsorption properties of A1P04-20, prepared according to Example 44b, were determined using a standard gravimetric adsorption. Sac-Bayna-Bakr device. The following data was obtained on a sample activated at 350 ° C (Table I1). The pore size of the calcined product is approximately 3 A, as. can be seen from the adsorption of water, the kinetic diameter of 2.65 A, and low adsorption at low partial pressures 0, the kinetic diameter of 3.46 A. Example 55. The adsorption properties obtained in Example 39c are determined using a standard Mac-Bain-Bakr gravimetric adsorption apparatus. On the sample activated at 350 ° C, the following data (Table 12). The pore size of the product of 4.3 Au and 5.0 A subjected to p), which can be seen from the adsorption of n-hexane, a kinetic diameter of 4.3 A, and a low adsorption of isobutane, a kinetic diameter of 5.0 A. Example 56. The adsorption properties of A1P04-16, obtained in Example 38c, were determined using a standard Mac-Bain-Bakr gravimetric adsorption apparatus. The following data was obtained on a sample activated at 350 ° C (Table 13). The size under the subjected product is 2.65 A and exact adsorption of neopentane, kinetic diameter 6.2 A. Example 61, The adsorption properties of A1P04-18 obtained in Example 43 were determined using a standard Mac-Bain-Bakr standard-gravimetric adsorption apparatus. Next 191461371 20 .3.46 A, as can be seen from the adsorption with a kinetic diameter of 6.0 A and nigra KfOf with a kinetic diameter of 2.65 A, and a low adsorption of 0 at low partial pressures, a kinetic diameter of 3.46 A, Example 57, The adsorption properties obtained in Example 3b are determined using a standard gravimetric adsorption data obtained on a sample of the Mc Bain-Bakr apparatus activated at 350 ° C (Table 18). sample activated when, according to the size of the calcined pores The following data are given (Table 14). product is 4.3 1 and 5, .0 A, The pore size of the bent calcined as seen by the adsorption of n-butane and the product is V3.64 A, 3 A 15 slight adsorption of isobutane which is visible by the adsorbant, N, kinetic - with a low partial pressure, the IMI with a diameter of 3.64 A , and by negligible Alyumophosphate compositions were strongly hydrophilic. All varieties demonstrated Pre-Example 58, the Adsorption 20, the thorough water adsorption compared to the properties obtained by analogy with the usual hydrogen sulfide example 26, are determined using a standard gravimetric adsorption of n-hexane, kinetic diameter of 4.3 A. McBain-BAKLAMU adsorption apparatus (paraffins, olefins, and benzoic aromatic compounds, for example, benzene, xylenes, and cumene), Tarak. On a sample activated with 25 of them, the proposed apumenophos- the following data obtained as a group are useful. (tab. 15). as drying agents in such pro-size pores of calcined adsorption separation processes product exceeds 6.2 A, which is clear cleaning, as drying of natural gas, by neopentan adsorption by kinetic ZO, cracking gas drying. Water also has a diameter of 6.2 A, is substantially adsorbed compared to the so-called, constant gases, such as carbon dioxide, nitrogen, oxygen and hydrogen, Aluminophos-35, and therefore most suitable for drying hydrogen streams from gravimetric adsorption. -: „reforming and drying oxygen-. headquarters of the McBain-Bakr, The data presented in table. 16, obtained on a sample, activated Q properties provided in the invention - at J50 C. The pore size exceeds 6.2 A, which Example 59, the adsorption properties of A1P04-31, prepared analogously to example 50b, except that the product was calcined before, is determined using the standard-. Yes, nitrogen or air before liquefaction, In this regard, the adsorption The scientific research institutes of alkaline phosphates seem to be quite similar with the properties of alkanol or silica zeolites with a low content of silica, despite the fact that.-J oQ-L. G 45 that it demonstrates non-ion exchange The adsorption properties of the proposed A1P04-P compositions illustrate-- with the data given in Table 19, 19 “The adsorption properties of i- and 20 were determined on this calcined product using a standard gravimetric adsorption apparatus, McBain-Bakr, The following data by the adsorption of neopentane, Example 60, Part of a crystal. measure 29 is subjected to calcination in air from 200 to for at least 1 h, followed by heating at 500 C for 2 h. Static drying of moist air is carried out at room temperature, ,, To illustrate hydrophilic whether they were obtained on sample, the nature of the compositions in equestrian at 350 ° C (Table 17), in contact with an aqueous organic solution; the size of the calcined rum dehydrated samples of the compounds of the product above 6.0 A and less than 6.2 A, AlPO comparative as can be seen from the adsorption of cyclohexane, the adsorbent (each weighing 0.5 g), the continuous adsorption of neopentane, with a kinetic diameter of 6.2 A. Example 61, The adsorption properties of A1P04-18 obtained in Example 43 were determined using a standard Mac-Bain-Bakr standard-gravimetric adsorption apparatus. With a kinetic diameter of 6.0 A and nothing the following data were obtained on a sample activated at 350 ° C (Table 18) associated gases, such as carbon dioxide, nitrogen, oxygen and hydrogen, are alumophosphate1, therefore, are most suitable for drying hydrogen streams from “reforming” and for drying oxygen properties are provided for in the invention Yes, nitrogen or air before liquefaction, In this regard, the adsorption The adsorption properties of the proposed A1P04-P compositions are illustrated with data given in Table 19, and 20. Static drying of moist air is carried out at room temperature, ,, To illustrate hydrophilic 21146137 Place in 2 g of a solution of 4 vol.% HjO and 96 vol% of 2-butanone at ambient room temperature and subject to moderate stirring for 5 hours. After that, the remaining solution and adsorbent are examined for water content. The results are shown in Table. 20, These compositions demonstrate new signs of surface selectivity that make them useful as catalysts or catalyst carriers in a number of hydrocarbon conversion and oxidative combustion reactions. Example 62. Preparation of A1P04-5. The reaction mixture was prepared by sweeping 23.1 g of 85% water with 44.0 g of water, and 13.7 g of hydrated alumina (pseudoboment phase 74.2 wt.% AlgOj) was added to the mixture thus obtained. and; 25.8 wt.% HgO), and then thoroughly mixed until a uniform mixture is formed. Then, 21.8 g of an aqueous solution: 23% (by weight) tetrapropyl ammonium hydroxide (TPAOH), thus obtained, is added to the mixture, thus obtained, the mixture is thoroughly: stirred until a homogeneous mass is formed. As a result, the following composition of the final reaction mixture was obtained based on molar oxide ratios: 0.1 (TPA). About:: A1gOz:: 40. Thus obtained; The mixture is placed and hermetically sealed. They are sealed in a high-pressure stainless steel tank and heated for 24 hours at a corresponding gas pressure. The solid reaction product is recovered by filtration, rinsing with water and then drying in air at room temperature. As a result of x-ray analysis, it was found that the final prod kt reaction consists of Pilene amine and 12.1 g of acetic acid. The mixture thus formed is thoroughly triturated to form a homogeneous mass and sealed in a stainless steel reactor with a polytetrafluoroethylene liner. the following composition of the reaction mixture based on molar oxide from 10 bearings: 2.0 n-Рг NH: Al.O, i P, 0f. UNHC: 40. Placed in a sealed in the composition of the reactor is heated for 168 h before, and solid particles 15, the reaction product is recovered by centrifuging. Chemical analysis of part of the final reaction product (after washing with water and drying gives the following results, wt.% G 20 carbon 8.0; nitrogen 1.5; A1.0z 38.2; Pj-Oj- 45.9 and losses when burned at JOO C 21.6. This analysis corresponds to the following chemical composition of the product: 25 0.16::: 0.9N ,, Formula-30 and Bretati Method for the preparation of crystalline aluminophosphate, including the interaction Hydrated alumina with phosphoric acid at 100–300 ° C, followed by separation of the product and its sediment, is also different because, in order to impart the properties of molecular sieves, the interaction in a closed volume is in the presence of an organic reagent selected from the group containing tetrapropylamone 40 moni hydroxide, tetraethylammonium hydroxide, tripropylamine, triethylamine, piperidine, cyclohexylamine, 2-methylpyridine N, N-dimethylbenzylamine, K, K-diethyl ethanolamine, dicyclohexylamine, and 3-methylpyridine; in, choline, K, methylpiperazine, 1,4-diazabicyclo (2,2,2) octane, K-methyldiethanolamine, - N-methylzthanolamine, N-methylpiperidine, 3-methylpiperidine, N-methylcyclohexipamine, 3-methiopyridine, quinoline and A1P04-5 together with crystalline impurities, which include metavari-50 J-methylpyridine, quinoline, and zit, and AHRO -tridymite. N, N-dimethyl-1,4-diazabicyclo (2,2,2) Octane hydroxy hydroxide, tetramethylammonium hydroxide, tetrabutyl ammonium hydroxide, tetrapentylammonium hydroxide, 2 g of pseudoboehmite (wt.% jj oxide, di- (n-butckp) amine, neopentyl-AljtOj, and 24.9 wt.%) mix sine, di- (n-pentip) amine, isopropyl solution of 46.2 g of 85% E-PO amine, C-butylamine, etkellenediamine and and 46.2 g of water, and then K2-imidazolidone, alkylamine, in which the resulting mixture of 40.5 g of di-p-pro alkyl half of cb is kept from Example 63. Preparation of A1P04-39. 22 Pilene amine and 12.1 g of acetic acid. The mixture thus formed is triturated to a uniform mass and sealed in a polytetrafluoroethylene lined stainless steel reactor. The following composition of the reaction mixture is based on molar oxide ratios: 2.0 n-Pr NH: Al.O, i P, 0f:. UNHC: 40. Placed in a sealed in the composition of the reactor is heated for 168 h before, and solid particles 15, the reaction product is recovered by centrifuging. Chemical analysis of part of the final reaction product (after washing with water and drying) gives the following results, wt.% G 20 carbon 8.0; nitrogen 1.5; A1.0z 38.2; Pj-Oj- 45.9 and losses when burned at JOO C 21.6. This analysis corresponds to the following chemical composition of the product: 5 0.16::: 0.9N ,, 0 / Formula-30 and Bretati Method for the preparation of crystalline aluminophosphate, including Hydrated alumina with phosphoric acid at 100–300 ° C, followed by separation of the product sediment and its cake, is also different because, in order to impart the properties of molecular sieves, the interaction in a closed volume leads to - the presence of an organic reagent selected from the group containing tetrapropylamo mono hydroxide, tetraethylammonium hydroxyl acetate, tripropylamine, triethylamine, piperidine, cyclohexylamine, 2 methylpyridine N, N-dimethylbenzylamine, K, K-diethyp- ethanolamine, dicyclohexylamine, methylamine, methylamine, hydrochloride; n, choline, K, methylpiperazine, 1,4-diazabicyclo (2,2,2) octane, K-methyldiethanolamine, - N-methylzthanolamine, N-methylpiperidine, 3-methylpiperidine, N-methylcyclohexipamine, 3-methiopyridine, quinoline and J-methylpyridine, quinoline, and N, N-dimethyl-1,4-diazabicyclo (2.2.2) 23146137124 two to seven carbon atoms, and is at least 2, equal to ammonium quaternary ammonium salt (Crf Hj NiXOH), where X is a value, the amount of 0.2-2.0 mod on 1 mol of alumina. Table 1 A small amount of acetone is used to rinse the solid. I Taёlitsa 3 1,4-Dimethylpiperazine (C, H, N) З- (di-p-butylamino) propyl-amine (Crt) table 2 Table 4 Table 5 40 168 200 40 168 200 27 1461371 N, N, N, Y-tetramethyl-1,3-β-propanediamine () N, N, -dimethylethanolamine Continuation of table.5 40 168 200 Table 6 Table 7 29 1461371 30 Table 8 35 1461371 The sample Moisture percentage Initial Konechna l Zeolite 4A Zeolite 5A Silica gel A1P04-5 36 Table 17 Table 18 Table 19 Contact time, h 3 16 16 four 3.5 18 5.5 37 146137138 Continuation of table 19 Table 20
权利要求:
Claims (3) [1] Claim A method of obtaining crystalline aluminophosphate, including the interaction of hydrated alumina with phosphoric acid during subsequent separation of it and washing it, which is due to the fact that, owing to the product properties of molecular sieves, the interaction in a closed volume is carried out in the presence of an organic reagent selected from the group consisting of tetrapropylammonium hydroxide, tetraethylammonium hydroxide, tripropylamine, triethylamine, piperidine, cyclohexylamine, 2-methylpyridine Ν, Ν-dimethylbenzylamine, Ν, Ν-diethipetanol amine, dicyclohexyl amine, Ν, Ν dimethylethanolamine, choline, Ν, Ν ^ -dimethylpiperazine, 1,4-diazabicyclo (2,2,2) octane, N-methyldiethanoamine, · N-methylzanolamine, N-methylpiperidine, 3-methippiperidia, N -methylcyclohexipamine, 3-methylpyridine, quinoline and Ν, Ν '' -dimethyl-1,4-diae abicyclo (2,2,2) octane dihydroxide, tetramethylammonium hydroxide, tetrabutylammonium hydroxide, tetrapentylammonium hydroxide, di- (n-butip) amine , neopentylamine, di- (n-pentyl) amine, isopropipamine, t-butylamine, ethipendiamine and [2] 2-imidazolidone, an alkylamine in which the alkyl half contains from 100-300 ° C with a precipitate, the product is designed to give : 23 1461371 two to seven carbon atoms, and a polymer quaternary ammonium salt (С Hj t N x ) (0Н) 4 *, where x is the value, equal to at least 2, taken in an amount of 0.2-2.0 mod per 1 mol of aluminum oxide. Table 1 Example R Reaction time,h Temperature ° C 5 (C 4 H ^) 4 N0H (tetraethylammonium hydroxide) 24 200 6 (CH 4 CH x 0H) 3 (triethanolamine) 72 150 7 Piperidine 24 150 8 2-methylpyridia 168 150 9 Cyclohexylamine 168 150 10 N-N-Dimethylbenz Ylamine 168 150 1 Ϊ N, N-Diethyl tanolamine 24 ' 200 12 Dicyclohexylamine 24 150 thirteen N, N-Dime Tile Tanolamine 24 150 14 (sn 3 ) 3 tssn .sn 4 he OH * 52 150 fifteen Ν, Ν-Dimethylpiperazine * 24 200 16 1,4-Diazobicyclo (2.2.2) approx. 192 tan (DAVCO) ** *200 17 N-Methyldiethanolamine * 24 200 18 N-Methylethanolamine * 24 200 19 N-methylpiperidine 24 200 20 Z-methylpiperidine 168 150 21 N-Me filsiklo g ec silamin ’24 200 22 Z-methylpyridine 24 150 23 4-methylpyridia 168 150 ♦ The finished reaction mixture contains 50 N y 0, The finished reaction mixture contains 0.5 DABSO Table 2 Example Used organic matter (R) Leveling time, h Temperature in C 25 (nC f H „) 4 noh 24 ' 150 26 (nC <H g ) 2 NH 72 150 27 (n C £ H ^ NH * 24 150 * A small amount of acetone is used to rinse the solid product. , I Table 3 Example R Reaction time,h The reaction temperature, G thirty (iC 3 H ) £ NH 24 200 31 (C g H y ) (nC ^ H # ) NH 24 200 32 (n-CfHj) 4 NH 48 200 33 (p-C, H „) 2 NH 24 200 Table 4 Example R Time Temperaturereactions ra re-h tion, 0 C 41 Cyclohexylamine 168,200 42 piperidine 168,200 T a b l Ts 5 Organic Used Composition reactionary mixtures Cooking timeh Temperature, ° C substanceΛ1, θ5 | P 2 eleven11 about 1eleven1 and 1eleven1_______________________________1 Trimethylamine ((SP) 3 N) 1 1 1fifty 94 150 Pyrrolidine ((CH 3 ) <: NH) 1 1 1fifty 166 150 1,4-Dimethylpiperazine (C 6 H „N X ) i 1 140 168 200 40 168 200 3 ~ (di-p-butylamino) propylamine (C „Η 2ί Ν 2 ) Organic matter used Continuation of Table 5 The composition of the reaction mixture Cooking timeh Temperature * C G7eleven Al t 0 3 j L o, H 2 0 Ν, Ν, Ν Ν'-tetramethyl-1,3- -propanediamine (ϋ, Π ^ Ν ^) 1 1 1 40 168 200 „Ν, Ν, -Dimethylethanolamine '' (C + H, Z NO) • 1 1 1 40 336 200 , n-Propylamine (n-CjH ^ NHj) .1 1 1 ' fifty 334 200 Ν, Ν, Ν * ^ '- tetramethylethylenediamine (С ^ Н М Ν ζ ) 1 1 1 fifty 168 200 N-Methylethanolamine (C, H tf NO) 1 1 1 fifty 168 200 4 T a b 6 Adsorbate Kinetic diameter, A Pressure torr Temperature, * С Adsorption, wt.% ° 23.46 97 -183 12.6 3.46 750 -183 17.0 Neopentane 6.2 102 24 5.5 (C <F S ) 3 N (after 4 hours) Yu 0,073 • 24 1,2 n g o 2.65 4.6 24 4.6 to 2 o 2.65 18.5 23 * 26,4 T a b l Ts a 7 Adsorbate Kinetic. diameter, X Pressure torr Temperature ° C Adsorptionto me · % θί 3.46 99 -183 13.3 0 3.46 730 -183 18.3 Cyclohexane ‘6.0 54 24 9.5 Neopentane 6.2 102 24 4.8 H 2 0 2.65 4,5 24 3.9 n 2 about 2.65 21, 0 24 29.8 Table 8 Adsorbate Kinetic diameter, A Pressure torr Temperature, s Adsorption wt.% ° 23.46 105 -183 14.6 0 43.46 705 -183 21, 3 Neopentane 6.2 103 25 6.5 H 2 0 2.65 4.6 25 6.5 n 2 about 2.65 20.7 25 32.6 Table 9 Adsorbate Kinetic diameter, A Pressure torr Temperature ° C Adsorption mA s ·% o < 3.46 103 -183 1,0 3.46 761 -183 2,5 p-hexane ‘ 4.3 28 24 0.4 Neopentane 6.2 310 24 0.5 H 2 0 2.65 4.6 24 And, 1 N g O 2.65 20,0 24 21.4 Table 10 Adsorbate Kinetic diameter, A Pressure torr Temperature ° C Adsorption wt.% • about 23.46 103 -183 4.9 L 3.46 761 -183 5.9 p-hexane 4.3 28 25 0.3 Neopentane 6.2 310 25 0.4 n g o 2.65 .4.6 25 0.4 H 4 0 2.65 20,0 25 16.6 Table 11 Adsorbate Kinetic diameter, X Pressure torr Temperature ,’s Adsorption, wt.% ° 2 3.46 97 -183 2.7 ° χ 3.46 750 -183 11.5 n-hexane 4.3 45 24 1.7 Neopentane 6.2 303 24 1,5 Cyclohexane 6.0 eleven 24 1.3 n g o 2.65 4.6 24 22.6 H t 0 2.65 18.5 24 37.8• Table 12 Adsorbate Kinetic diameter, A Pressure torr Temperature, ΰ ο Adsorption, wt.% θι 3.46 102 -183 22.2 about/ 3.46 724 -183. 23.1 n-hexane • 4.3 45 23 7.7 Isobutane 5,0 101 22 0.2 Neopentane 6.2 308 23 0.3 H <02.65 4.6 22 24.9 n 2 about 2.65 18 22 27.8 Table 13 Adsorbate Kinetic diameter, A Pressure torr Temperature in C Absorption, Ms with L 3.46 101 -183 1,2 about 43.46 755 -183 11.6 n-butane 4.3 / 768 24 2.0 Neopentane 6.2 301 25 1.4 n 2 about 2.65 4.6 24 19.0 H 2 0 2.65 20 24 36.3 Table 14 Adsorbate Kinetic diameter, A Pressure torr Temperature, * s Adsorption, wt.% 3.46 102 -183 15,53 3.46 763 -183 21.56 n-hexane 4.3 45 26 0.25 Neopentane 6.2 499 24 0.37 H 2 0 2.65 4.6 24 21.46 H 2 0 2.65 21.0 24 28.66 N * 3.64 100 -196 11.28 3.64 747 -196 14,99 Table 15 Adsorbate Kinetic Pressure, Tempera- Adsorption, diameter, A torr tour, C wt.%. [3] 3.46 100 -183 8.9 3.46 755 -183 18.6 n-butane 4.3 768 24 5,0 Neopentane 6.2 501 24 4,5 (C <F 3 ) 3 N (post- le 4 h) 10.00,073 25 8.2 n g o 2.654.6 24 18.5 H 2 0 2.6520,0 24 3G, 9 . T a b faces 16 Adsorbate Kinetic diameter, I. Pressure torr Temperature ° C Adsorption, wt.% 0 23.4699 -183 8.1 3.4674 -183 And 5 Butane 4.3107 224 4.0 Cyclohexane 6.054 ' 24 5.3 Neopentane 6.2109 24 3,1 H 2 0 2.654.6 24 5.3 H 2 0 2.6514.0 24 13.9 Table 17 Adsorbate Kinetic diameter, A Pressure torr Temperature, “s Adsorption, wt.% Oi 3.46 101 -183 9.22 01 3.46 755 -183 10.7 n-butane 4.3 304 24 4.35 Isobutane 5,0 502 24 4.71 Neopentane 6.2 301 24 1, 22 Cyclohexane 6.0 thirty 24 5.30 H 1 2.65 4.6 24 11, 8 H 4 0 2.65 20,0 24 16,4 T a b l 1 l c a 18 ' Adsorbate Kinetic Pressure, Tempera- Adsorption, diameter, A torr round, ° C May. % 3.46 130 -183 23.0 ° 1 3.46 697 -183 27.9 n-butane 4.3 718 24 16,2 iso-butane 5,0 101 ' 24 0.1 n £ o 2.65. 4.6 24 30.3 n £ o 2.65 21, 0 24 36.9 Table 19 Sample Moisture percentage Contact timeh Initial | The ultimate Zeolite 4A 60 5 3 Zeolite 5A 54 18 16 Silica gel 56 18 16 ΑΙΡΟ ^ -5 55 29th 4 AIPO4-8 60 21 3,5 AIPO4-8 61 19 18 AIPO4-11 . 5729th 5.5 Continuation of Table 19 Moisture percentage Sample Contact time Initial I ultimate h A1P0 <-14 56 19 3.0 A1R0 4 -16 70 22 3.0 A1RO 4 -16 56 14 72 ‘ A1RO 4 -17 63 24 18.5 A1P0 4 -20 60 17 . 16 A1P0 4 ~ 28 56 7 17.5 A1P0 4 -25 56 26 18.5 A1P0 4 -9 51 29th 23 AIPO4-I8 56 19 24 A1P0 / -31 51 24 19 Table 20 Adsorbent The percentage of removal of water from the solution Download Percentage * A1P0 4 -5 55 23 AIPO4-8 74 45 A1P0 4 -11 21 23 A1RO 4 -14 80 45 A1RO 4 -16 80 45 A1P0 4 -17 77 41 A1RO 4 -2O 87 58 Zeolite NaY 80 37 Silica gel 28 - Silica gel ** -5 Percentage of maximum theoretical performance. * US patent No. 4061724.
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同族专利:
公开号 | 公开日 DE3164146D1|1984-07-19| DD202277A5|1983-09-07| JPH0157041B2|1989-12-04| NO154691B|1986-08-25| US4310440A|1982-01-12| NO812253L|1982-01-08| ES8504899A1|1985-04-16| AU546783B2|1985-09-19| ES503667A0|1982-11-01| ES8504900A1|1985-04-16| DK158207C|1990-09-24| DK158207B|1990-04-09| NO154691C|1986-12-03| ES8401922A1|1984-01-01| ES526141A0|1985-04-16| ES8300640A1|1982-11-01| AT7882T|1984-06-15| EP0043562B1|1984-06-13| CA1168220A|1984-05-29| DD220234A5|1985-03-27| JPS5777015A|1982-05-14| ES526142A0|1985-04-16| EP0043562A1|1982-01-13| ES513176A0|1984-01-01| AU7260881A|1982-01-14| DK299581A|1982-01-08|
引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题 US2282602A|1938-03-15|1942-05-12|Phillips Petroleum Co|Process for the conversion of hydrocarbons| US2330115A|1940-09-30|1943-09-21|Phillips Petroleum Co|Catalytic isomerization of 1-olefins to 2-olefins| US3227519A|1962-04-12|1966-01-04|Grace W R & Co|Metal phosphates and methods for producing same| US3386801A|1966-02-01|1968-06-04|Mobil Oil Corp|Alkalimetal and alkylammonium phosphatoaluminate complexes and the preparation of crystalline aluminosilicates| US3941871A|1973-11-02|1976-03-02|Mobil Oil Corporation|Crystalline silicates and method of preparing the same| DE2403707A1|1974-01-26|1975-08-14|Hoechst Ag|METHOD OF MANUFACTURING ALH LOW 3 LOW 2. 3H LOW 2 O| US3947482A|1974-03-20|1976-03-30|W. R. Grace & Co.|Method for producing open framework zeolites| NZ178543A|1974-09-23|1978-04-03|Mobil Oil Corp|Conversion catalyst, crystalline alumin osilicate zeolite containing phosphorus| US3969273A|1975-04-24|1976-07-13|W. R. Grace & Co.|Process for preparing phosphated alumina extrudates| US4061724A|1975-09-22|1977-12-06|Union Carbide Corporation|Crystalline silica| US4080311A|1976-08-31|1978-03-21|Gulf Research & Development Company|Thermally stable phosphate containing alumina precipitates and their method of preparation| US4066572A|1976-10-12|1978-01-03|Nalco Chemical Company|Phospha-alumina gel and method of preparation| US4132669A|1977-10-06|1979-01-02|Nalco Chemical Company|Process for preparing phosphorous-alumina catalysts using polycarboxylic acids as extrusion aids| DE3061264D1|1979-07-03|1983-01-13|Laporte Industries Ltd|Aluminophosphorous compound, process for producing same and its use|US4419271A|1979-10-15|1983-12-06|Union Oil Company Of California|Hydrocarbon conversion catalyst| US4683050A|1979-10-15|1987-07-28|Union Oil Company Of California|Mild hydrocracking with a catalyst containing an intermediate pore molecular sieve| US4829040A|1979-10-15|1989-05-09|Union Oil Company Of California|Catalyst containing an intermediate pore molecular sieve for mild hydrocracking| US4743355A|1979-10-15|1988-05-10|Union Oil Company Of California|Process for producing a high quality lube oil stock| US4743354A|1979-10-15|1988-05-10|Union Oil Company Of California|Process for producing a product hydrocarbon having a reduced content of normal paraffins| US4898660A|1980-07-07|1990-02-06|Union Carbide Corporation|Catalytic uses of crystalline metallophosphate compositions| US4877762A|1981-05-26|1989-10-31|Union Oil Company Of California|Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons| US4790927A|1981-05-26|1988-12-13|Union Oil Company Of California|Process for simultaneous hydrotreating and hydrodewaxing of hydrocarbons| US4440871A|1982-07-26|1984-04-03|Union Carbide Corporation|Crystalline silicoaluminophosphates| CA1220771A|1982-08-02|1987-04-21|Frank P. Gortsema|Modification of molecular sieves by treatment with asilicon tetrafluoride gas mixture| US4569833A|1982-08-02|1986-02-11|Union Carbide Corporation|Modification of aluminophosphate molecular sieves by treatment with a silicon tetrafluoride gas mixture| US4568654A|1982-11-03|1986-02-04|Mobil Oil Corporation|Zeolite ZSM-51 composition| US4840780A|1983-03-28|1989-06-20|Mobil Oil Corporation|ZSM-51, method of preparing same and catalytic conversion therewith| US4473663A|1983-03-31|1984-09-25|Union Carbide Corporation|Crystalline aluminophosphate compositions| US4605492A|1983-03-31|1986-08-12|Union Carbide Corporation|Separation and conversion processes with titanium-containing molecular sieves| US4551236A|1983-03-31|1985-11-05|Union Carbide Corporation|Conversion processes with titanium-containing molecular sieves| US4500651A|1983-03-31|1985-02-19|Union Carbide Corporation|Titanium-containing molecular sieves| US4992160A|1983-05-02|1991-02-12|Uop|Conversion of crude oil feeds by catalytic cracking| US4512875A|1983-05-02|1985-04-23|Union Carbide Corporation|Cracking of crude oils with carbon-hydrogen fragmentation compounds over non-zeolitic catalysts| US4803184A|1983-05-02|1989-02-07|Uop|Conversion of crude oil feeds| US4859314A|1983-05-02|1989-08-22|Uop|Catalytic cracking catalysts and cracking process using non-zeolitic molecular sieves| US4482776A|1983-06-27|1984-11-13|Exxon Research & Engineering Co.|Separation of ortho aromatic isomers by selective adsorption with an aluminophosphate| US4801364A|1983-07-15|1989-01-31|Uop|Separation and conversion processes using metal aluminophosphates| US4567029A|1983-07-15|1986-01-28|Union Carbide Corporation|Crystalline metal aluminophosphates| US4744885A|1983-07-15|1988-05-17|Union Carbide Corporation|Hydro-carbon conversion using ferroaluminophosphates| US4554143A|1983-07-15|1985-11-19|Union Carbide Corporation|Crystalline ferroaluminophosphates| US4845069A|1983-09-29|1989-07-04|The Dow Chemical Company|Porous amorphous metallo phosphates process for preparing porous amorphous metallo phosphates| US4528414A|1983-11-15|1985-07-09|Union Carbide Corporation|Olefin oligomerization| US4613721A|1983-11-15|1986-09-23|Union Carbide Corporation|Small olefin interconversions| US4612406A|1983-11-15|1986-09-16|Union Carbide Corporation|Olefin oligomerization| US4499315A|1983-11-15|1985-02-12|Union Carbide Corporation|Conversion of certain hydrocarbons using silicoaluminophosphate catalysts| US4527001A|1983-11-15|1985-07-02|Union Carbide Corporation|Small olefin interconversions| US4664897A|1983-12-19|1987-05-12|Mobil Oil Corporation|Crystalline silicophosphoaluminate MCM-4| NZ210465A|1983-12-19|1988-02-29|Mobil Oil Corp|Crystalline silicophosphoaluminate and its use as a catalyst| US4639358A|1983-12-19|1987-01-27|Mobil Oil Corporation|Crystalline silicophosphoaluminate MCM-1| US5147525A|1983-12-19|1992-09-15|Mobil Oil Corporation|Synthesis of crystalline metalloaluminophosphate composition| US4647442A|1983-12-19|1987-03-03|Mobil Oil Corporation|Crystalline silicophosphoaluminate from a two phase medium| US4673559A|1983-12-19|1987-06-16|Mobil Oil Corporation|Silicoaluminophosphate crystallization using hydrolysis| US4880611A|1983-12-19|1989-11-14|Mobil Oil Corp.|Crystalline composition| US5326464A|1983-12-19|1994-07-05|Mobil Oil Corp.|Crystalline composition| US4639357A|1983-12-19|1987-01-27|Mobil Oil Corporation|Crystalline silicophosphoaluminate MCM-5| US4632811A|1983-12-19|1986-12-30|Mobil Oil Corporation|Crystalline silicophosphoaluminate MCM-3| NZ210462A|1983-12-19|1988-06-30|Mobil Oil Corp|Crystalline oxides, their synthesis and use in the conversion of organic compounds| US4891197A|1983-12-19|1990-01-02|Mobil Oil Corporation|Silicophosphoaluminates and related crystalline oxides| US4654138A|1983-12-19|1987-03-31|Mobil Oil Corporation|Catalytic process for modifying organic compounds| NZ210464A|1983-12-19|1987-08-31|Mobil Oil Corp|Crystalline silicophosphoaluminates and their use as catalysts| GB8406768D0|1984-03-15|1984-04-18|Ici Plc|Crystalline metallophosphates| US4744970A|1984-04-13|1988-05-17|Union Carbide Corporation|Cobalt-aluminum-phosphorus-silicon-oxide molecular sieves| US4973460A|1984-04-13|1990-11-27|Uop|Lithium-aluminum-phosphorus-silicon-oxide molecular sieve compositions| CA1241627A|1984-04-13|1988-09-06|Edith M. Flanigen|Molecular sieve compositions| US4882038A|1984-04-13|1989-11-21|Uop|Process for the use of magnesium-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4917876A|1984-04-13|1990-04-17|Uop|Iron-titanium-aluminum-phosphorus-oxide molecular sieve compositions| CA1241943A|1984-04-13|1988-09-13|Brent M.T. Lok|Molecular sieve compositions| US4992250A|1984-04-13|1991-02-12|Uop|Germanium-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4686093A|1984-04-13|1987-08-11|Union Carbide Corporation|Molecular sieve compositions with aluminum, phosphorus and at least two other elements| US4894213A|1984-04-13|1990-01-16|Uop|Arsenic-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4741892A|1984-04-13|1988-05-03|Union Carbide Corporation|Quinary molecular sieve compositions| US4686092A|1984-04-13|1987-08-11|Union Carbide Corporation|Manganese-aluminum-phosphorus-silicon-oxide molecular sieves| US4793984A|1984-04-13|1988-12-27|Union Carbide Corporation|Molecular sieve compositions| US4737353A|1984-04-13|1988-04-12|Union Carbide Corporation|Beryllium-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4735806A|1984-04-13|1988-04-05|Union Carbide Corporation|Gallium-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4801309A|1984-04-13|1989-01-31|Uop|Titanium-aluminum-phosphorus-silicon-oxide molecular sieves| CA1241628A|1984-04-13|1988-09-06|Brent M.T. Lok|Molecular sieve compositions| US4789535A|1984-04-13|1988-12-06|Union Carbide Corporation|Lithium-aluminum-phosphorus-oxide molecular sieve compositions| US4956164A|1984-04-13|1990-09-11|Uop|Quinary molecular sieve compositions| US4851106A|1984-04-13|1989-07-25|Uop|Process for the use of chromium-aluminum-phosphorus-oxide molecular sieve compositions| US4952383A|1984-04-13|1990-08-28|Uop|Boron-aluminum-phosphorus-oxide molecular sieve compositions| US4952384A|1984-04-13|1990-08-28|Uop|Molecular sieve compositions| US4759919A|1984-04-13|1988-07-26|Union Carbide Corporation|Chromium-aluminum-phosphorus-oxide molecular sieve compositions| US4683217A|1984-04-13|1987-07-28|Union Carbide Corporation|Iron-aluminum-phosphorus-silicon-oxide molecular sieves| US4824554A|1984-04-13|1989-04-25|Uop|Processes for the use of cobalt-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4888167A|1984-04-13|1989-12-19|Uop|Germanium-aluminum-phosphorus-oxide molecular sieve compositions| US4973785A|1984-04-13|1990-11-27|Uop|Molecular sieve compositions| US4935216A|1984-04-13|1990-06-19|Uop|Zinc-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4684617A|1984-04-13|1987-08-04|Union Carbide Corporation|Titanium-aluminum-phosphorus-silicon-oxide molecular sieves| US4940570A|1984-04-13|1990-07-10|Uop|Beryllium-aluminum-phosphorus-oxide molecular sieve compositions| US4913888A|1984-04-13|1990-04-03|Uop|Arsenic-aluminum-phosphorus-oxide molecular sieve compositions| US4956165A|1984-04-13|1990-09-11|Uop|Molecular sieve compositions| US5032368A|1984-04-13|1991-07-16|Uop|Gallium-aluminum-phosphorus-oxide molecular sieve compositions| US4758419A|1984-04-13|1988-07-19|Union Carbide Corporation|Magnesium-aluminum-phosphorus-silicon-oxide molecular sieve compositions| US4869805A|1984-04-26|1989-09-26|Uop|Titanium-aluminum-silicon-oxide molecular sieve compositions| US4707345A|1984-04-26|1987-11-17|Union Carbide Corporation|Titanium-aluminum-silicon-oxide molecular sieve compositions and process for preparing the same| NZ211790A|1984-05-03|1988-06-30|Mobil Oil Corp|Increasing activity of aluminium phosphate catalyst| US4780444A|1984-05-03|1988-10-25|Mobil Oil Corporation|Activation of metallophophates| US4619818A|1984-05-30|1986-10-28|Mobil Oil Corporation|Crystalline antimonophosphoaluminate| NZ212070A|1984-05-30|1988-04-29|Mobil Oil Corp|Crystalline metallophosphoaluminate, prouction thereof, and use as a catalyst| US4684511A|1984-08-29|1987-08-04|Union Carbide Corporation|Process for the halogen modification of aluminophosphate molecular sieves and a product so produced| US4524234A|1984-10-19|1985-06-18|Union Carbide Corporation|Production of hydrocarbons with aluminophosphate molecular sieves| GB2167052B|1984-11-17|1988-09-07|Laporte Industries Ltd|Synthetic crystalline molecular sieve materials and a method for their preparation| USRE33009E|1984-11-30|1989-08-01|Mobil Oil Corporation|Method for preparing crystalline zirconium phosphates| US4695642A|1984-11-30|1987-09-22|Mobil Oil Corporation|Method for preparing crystalline zirconium phosphates| US4560542A|1984-12-06|1985-12-24|Exxon Research And Engineering Co.|Method for the preparation of zeolites using a low water low alkali metal content gel| US4913799A|1984-12-18|1990-04-03|Uop|Hydrocracking catalysts and processes employing non-zeolitic molecular sieves| US4913798A|1984-12-18|1990-04-03|Uop|Hydrocracking catalyts and processes employing silicoaluminophosphate molecular sieves| US4898722A|1984-12-19|1990-02-06|Mobil Oil Corp.|Synthesis of crystalline SAPO-37| US4590050A|1984-12-20|1986-05-20|Mobil Oil Corporation|Synthesis of crystalline aluminum phosphates with a urea templating agent| US4724066A|1985-01-22|1988-02-09|Mobil Oil Corporation|Composites of microporous aluminum phosphates and zeolites and conversions over these catalysts| EP0189243A3|1985-01-22|1987-05-13|Mobil Oil Corporation|A catalytic dewaxing process and a catalyst composition for use in the same| US4629717A|1985-06-11|1986-12-16|Uop Inc.|Phosphorus-modified alumina composite, method of manufacture and use thereof| US4867861A|1985-06-18|1989-09-19|Union Oil Company Of California|Process and catalyst for the dewaxing of shale oil| US5084159A|1985-06-18|1992-01-28|Union Oil Company Of California|Process and catalyst for the dewaxing of shale oil| US5292701A|1985-08-29|1994-03-08|W. R. Grace & Co.-Conn.|High pore volume and pore diameter aluminum phosphate and method of making the same| US4663139A|1985-12-16|1987-05-05|Union Carbide Corporation|Crystalline AlPO4 -39| US4861457A|1985-12-20|1989-08-29|Uop|Crystalline gallophosphate compositions| US4690808A|1985-12-20|1987-09-01|Union Carbide Corporation|Crystalline gallophosphate compositions| US4741820A|1986-03-27|1988-05-03|Union Carbide Corporation|Reforming/dehydrocyclization catalysts and processes| US4790982A|1986-04-07|1988-12-13|Katalistiks International, Inc.|Metal-containing spinel composition and process of using same| US4714783A|1986-05-12|1987-12-22|Uop Inc.|Separation of nitrobenzaldehyde isomers| US4760184A|1986-05-12|1988-07-26|Air Products And Chemicals, Inc.|Alkylation of aromatic amines in the presence of non-zeolitic molecular sieves| US4751340A|1986-06-16|1988-06-14|Union Carbide Corporation|Selective production of para-aromatics| US4740650A|1986-06-16|1988-04-26|Union Carbide Corporation|Xylene isomerization| US4704478A|1986-06-25|1987-11-03|Union Carbide Corporation|Process for the condensation of ketones| US4873325A|1986-06-25|1989-10-10|Uop|Process for the production of amides| US4777157A|1986-06-30|1988-10-11|Union Oil Company Of California|Hydrocracking catalyst| US4871445A|1986-06-30|1989-10-03|Union Oil Company Of California|Hydrocarbon conversion| DE3768164D1|1986-06-30|1991-04-04|Union Carbide Corp|CRYSTALLINE ALUMOPHOSPHATE OF THE MOLECULAR SCREEN TYPE AND METHOD FOR THE PRODUCTION THEREOF.| US4695368A|1986-07-31|1987-09-22|Union Oil Company Of California|Process for producing high octane gasoline| DE3640596A1|1986-11-27|1988-06-01|Basf Ag|METHOD FOR PRODUCING 3-PENTENIC ACID ESTERS FROM 2-PENTENIC ACID ESTERS| US4778666A|1986-12-04|1988-10-18|Mobil Oil Corporation|Crystallization method employing microwave radiation| US4743572A|1986-12-05|1988-05-10|Mobil Oil Corporation|Magnesia-alumina-aluminum phosphate catalyst and catalyst product thereof| US4734538A|1986-12-24|1988-03-29|Union Carbide Corporation|Process for the production of dienes| US4810361A|1987-05-18|1989-03-07|Mobil Oil Corporation|Resid hydrotreating process using lanthana-alumina-aluminum phosphate catalyst| US4814316A|1987-06-04|1989-03-21|Uop|Novel catalyst composition, and processes for making and using same| US4851204A|1987-06-04|1989-07-25|Uop|Crystalline aluminophosphate composition| US4826804A|1987-06-04|1989-05-02|Uop|Catalyst for oligomerization process| US4803185A|1987-06-04|1989-02-07|Uop|Octane boosting catalyst| US4861739A|1987-06-04|1989-08-29|Uop|Microporous crystalline composite compositions| DK303788A|1987-06-04|1988-12-05|Union Carbide Corp|PROCEDURE FOR THE PREPARATION OF A MICROCrystalline MATERIAL CONTAINING ALUMINOPHOSPHATE| US4938937A|1987-06-04|1990-07-03|Uop|Crystalline aluminophosphate composition| US4853197A|1987-06-04|1989-08-01|Uop|Crystalline metal aluminophosphates| US4765884A|1987-07-02|1988-08-23|Phillips Petroleum Company|Cracking catalyst and process| US4873211A|1987-07-02|1989-10-10|Phillips Petroleum Company|Cracking catalyst and process| US5374411A|1987-08-28|1994-12-20|The Dow Chemical Company|Crystalline aluminumphosphate compositions| AU612713B2|1987-08-28|1991-07-18|Dow Chemical Company, The|Crystalline aluminophosphate compositions| HU208511B|1987-08-28|1993-11-29|Dow Chemical Co|Process for producing christalline aluminium-phosphate compositions| US5189182A|1987-09-09|1993-02-23|Basf Aktiengesellschaft|Preparation of 5-methylbutyrolactone| US4861743A|1987-11-25|1989-08-29|Uop|Process for the production of molecular sieves| US4973709A|1987-12-18|1990-11-27|Union Carbide Chemicals And Plastics Company, Inc.|Process for the production of amines, hydroxyamines and aziridines| US5120860A|1987-12-18|1992-06-09|Union Carbide Chemicals & Plastics Technology Corporation|Process for the production of aziridines| US4849567A|1987-12-28|1989-07-18|Mobil Oil Corporation|Catalytic dehydrogenation of hydrocarbons over indium-containing crystalline microporous materials| US4922050A|1987-12-28|1990-05-01|Mobil Oil Corporation|Catalytic dehydrogenation of hydrocarbons over indium-containing crystalline microporous materials| US4929576A|1988-01-04|1990-05-29|Mobil Oil Corporation|Reactivating catalysts containing noble metals on molecular sieves containing oxides of aluminum and phosphorus| DE3804162A1|1988-02-11|1989-08-24|Basf Ag|METHOD FOR PRODUCING VINYL ETHERS| US4913796A|1988-03-10|1990-04-03|Mobil Oil Corp.|Novel crystalline silicoaluminophosphate| US4877593A|1988-03-10|1989-10-31|Mobil Oil Company|Synthesis of crystalline aluminophosphate composition| WO1989008608A1|1988-03-10|1989-09-21|Mobil Oil Corporation|Synthetic crystalline molecular sieve and its synthesis| US4913795A|1988-03-10|1990-04-03|Mobil Oil Corp.|Novel crystalline metalloaluminophosphate| US5147626A|1988-04-08|1992-09-15|Mobil Oil Corporation|Synthesis of crystalline aluminophosphate composition| US5141728A|1988-04-08|1992-08-25|Mobil Oil Corporation|Synthesis of crystalline aluminophosphate composition| US5147627A|1988-04-08|1992-09-15|Mobil Oil Corporation|Synthesis of crystalline silicoaluminophosphate composition| US5169614A|1988-04-08|1992-12-08|Mobil Oil Corporation|Synthesis of crystalline silicoaluminophosphate composition| US5141729A|1988-04-08|1992-08-25|Mobil Oil Corporation|Synthesis of crystalline metalloaluminophosphate composition| GB8813121D0|1988-06-03|1988-07-06|Shell Int Research|Novel crystalline aluminophosphates & related compounds| GB8814292D0|1988-06-16|1988-07-20|Shell Int Research|Process for conversion of hydrocarbonaceous feedstock| CN1021913C|1988-06-16|1993-08-25|国际壳牌研究有限公司|Process for conversion of phdrocarbonaceous feedstock| US4933068A|1988-12-06|1990-06-12|Uop|Hydrocarbon conversion process using crystalline microporous metal sulfide compositions| US5013337A|1988-12-06|1991-05-07|Uop|Process for separating a mixture of molecular species using crystalline microporous metal sulfide compositions| US4880761A|1988-12-06|1989-11-14|Uop|Crystalline microporous metal sulfide compositions| GB8902083D0|1989-01-31|1989-03-22|Shell Int Research|Novel crystalline aluminophosphates and related compounds| US5013535A|1989-04-20|1991-05-07|Uop|Stabilized aluminophosphate compositions and process for preparing same| GB8914469D0|1989-06-23|1989-08-09|Shell Int Research|Novel crystalline aluminophosphates and related compounds| US4960745A|1989-07-20|1990-10-02|Mobil Oil Corporation|Layered aluminum compounds containing phosphorus or arsenic and pendant organic groups| US5135642A|1989-09-07|1992-08-04|Uop|Hydrocarbon conversion processes using novel crystalline silicon enhanced aluminas| GB8920906D0|1989-09-15|1989-11-01|Shell Int Research|Novel crystalline aluminophosphates and related compounds| GB8924262D0|1989-10-27|1989-12-13|Shell Int Research|Novel crystalline aluminophosphates and related compounds| GB8926602D0|1989-11-24|1990-01-17|Shell Int Research|Novel crystalline aluminophosphates and related compounds| US5102643A|1990-01-25|1992-04-07|Mobil Oil Corp.|Composition of synthetic porous crystalline material, its synthesis| US5108725A|1990-01-25|1992-04-28|Mobil Oil Corp.|Synthesis of mesoporous crystalline material| US5198203A|1990-01-25|1993-03-30|Mobil Oil Corp.|Synthetic mesoporous crystalline material| US5196633A|1990-01-25|1993-03-23|Mobil Oil Corp.|Catalytic conversion| US5174888A|1990-01-25|1992-12-29|Mobil Oil Corp.|Catalytic conversion| US5300277A|1990-01-25|1994-04-05|Mobil Oil Corporation|Synthesis of mesoporous crystalline material| US5068485A|1990-03-16|1991-11-26|The United States Of America As Represented By The United States Department Of Energy|Activation of methane by transition metal-substituted aluminophosphate molecular sieves| US5168084A|1990-05-07|1992-12-01|Uop|Molecular sieve agglomerates with improved transport properties| GB9012429D0|1990-06-04|1990-07-25|Enichem Elastomers|Preparation of conjugated dienes| US5264644A|1990-06-04|1993-11-23|Enichem Elastomers Limited|Preparation of conjugated dienes| US5091073A|1990-07-13|1992-02-25|Mobil Oil Corp.|Crystalline molecular sieve compositions mcm-37| US5152972A|1990-08-31|1992-10-06|E. I. Du Pont De Nemours And Company|Process for producing molecular sieves and novel molecular sieve compositions| US5102582A|1990-09-17|1992-04-07|Uop|Process for separating fatty acids and triglycerides| US5126120A|1990-10-02|1992-06-30|Uop|Crystalline microporous zinc phosphate compositions| GB9023847D0|1990-11-02|1990-12-12|Shell Int Research|Novel crystalline aluminophosphates and related compounds| US5179219A|1990-11-19|1993-01-12|Uop|Process for separating fatty acids and triglycerides| US5167942A|1990-11-21|1992-12-01|Board Of Regents, The University Of Texas System|Methods for the preparation of molecular sieves, including zeolites, using metal chelate complexes| US5203888A|1990-11-23|1993-04-20|Uop|Pressure swing adsorption process with multiple desorption steps| US5057296A|1990-12-10|1991-10-15|Mobil Oil Corp.|Method for synthesizing mesoporous crystalline material| US5107052A|1990-12-31|1992-04-21|Uop|Extraction of dimethyl paraffins from isomerates| US5174976A|1990-12-31|1992-12-29|Mobil Oil Corporation|Method for calcining crystalline aluminophosphate compositions| US5128025A|1991-03-18|1992-07-07|Uop|Hydrocarbon conversion processes using a novel crystalline microporous metal oxysulfide composition| US5122357A|1991-03-18|1992-06-16|Uop|Crystalline microporous metal oxysulfide compositions| US5160493A|1991-04-29|1992-11-03|Uop|Silicon enhanced amorphous silica-alumina| US5259948A|1991-04-29|1993-11-09|Uop|Hydrocarbon conversion process using a novel silicon enhanced amorphous silica-alumina| CA2069648A1|1991-06-21|1992-12-22|Quang N. Le|Naphtha cracking| US5232580A|1991-06-21|1993-08-03|Mobil Oil Corporation|Catalytic process for hydrocarbon cracking using synthetic mesoporous crystalline material| US5480556A|1991-07-01|1996-01-02|Ulan; Judith G.|Trapping and sealing process| US5156828A|1991-07-18|1992-10-20|Mobil Oil Corporation|Method for manufacturing synthetic mesoporous crystalline material| US5143879A|1991-07-18|1992-09-01|Mobil Oil Corporation|Method to recover organic templates from freshly synthesized molecular sieves| US5185306A|1991-07-24|1993-02-09|Uop|Prevention of noble metal migration in bound zeolites during thermal oxidation| US5139989A|1991-08-28|1992-08-18|Uop|Amorphous silica/alumina/phosphate composition and uses thereof| US5230789A|1991-08-28|1993-07-27|Uop|Hydrocarbon conversion process using an amorphous silica/alumina/phosphate composition| DE4131447A1|1991-09-21|1993-03-25|Basf Ag|COLORED, CRYSTALLINE ALUMOPHOSPHATES AND / OR AEL-TYPE SILICOALUMOPHOSPHATES| US5294429A|1991-10-24|1994-03-15|Shell Oil Company|Crystalline aluminophosphates| US5191141A|1991-11-13|1993-03-02|Uop|Process for converting methanol to olefins using an improved metal aluminophosphate catalyst| US5126308A|1991-11-13|1992-06-30|Uop|Metal aluminophosphate catalyst for converting methanol to light olefins| DE4138272A1|1991-11-21|1993-07-01|Vaw Ver Aluminium Werke Ag|CATALYST MATERIAL, ITS USE AND A METHOD FOR HYDRODEHALOGENATING ORGANIC HALOGEN COMPOUNDS| US5438027A|1991-12-13|1995-08-01|Phillips Petroleum Company|Chromium compounds and uses thereof| US5449450A|1992-04-10|1995-09-12|Uop|Hydrocarbon conversion process using a crystalline microporous metallo-zinc phosphate composition| US5302362A|1992-04-10|1994-04-12|Uop|Crystalline microporous metallo-zinc phosphate compositions| US5296208A|1992-08-07|1994-03-22|Uop|Molecular sieve synthesis| US5338527A|1992-08-20|1994-08-16|Uop|Zirconium silicate composition, method of preparation and uses thereof| US5879655A|1992-11-02|1999-03-09|Chevron Research And Technology Company|Method of making microporous non-zeolitic molecular sieves| US5344553A|1993-02-22|1994-09-06|Mobil Oil Corporation|Upgrading of a hydrocarbon feedstock utilizing a graded, mesoporous catalyst system| US5594263A|1993-03-26|1997-01-14|Uop|Semiconductor device containing a semiconducting crystalline nanoporous material| US5346685A|1993-04-23|1994-09-13|Mobil Oil Corp.|Synthetic porous crystalline MCM-51, its synthesis and use| US5370851A|1993-05-27|1994-12-06|Uop|Crystalline silicoalumino phosphates: SAPO-36 and SAPO-56| US5437781A|1993-05-27|1995-08-01|Uop|Hydrocarbon conversion processes using crystalline silicoalumino phosphates: SAPO-36 and SAPO-56| NO300012B1|1993-08-17|1997-03-17|Polymers Holding As|Microporost crystalline silica aluminophosphate, process for the preparation thereof, and use thereof| US5503658A|1993-11-12|1996-04-02|Uop|Process for the removal of volatile organic compounds from a fluid stream| US5512082A|1993-11-12|1996-04-30|Uop|Process for the removal of volatile organic compounds from a fluid stream| US5501848A|1994-02-08|1996-03-26|Chevron U.S.A. Inc.|Method for preparing crystalline aluminophosphate materials using azapolycyclic templating agents| JP2615421B2|1994-03-11|1997-05-28|工業技術院長|Crystalline organic aluminum phosphate| US5453113A|1994-04-11|1995-09-26|Uop|Process for separation and recovery of methyl chloride from vent streams containing isobutane| US5514362A|1994-05-03|1996-05-07|Chevron U.S.A. Inc.|Preparation of non-zeolitic molecular sieves| US5489424A|1994-08-24|1996-02-06|Board Of Regents, The University Of Texas System|Synthesis of novel molecular sieves using a metal complex as a template| DE4431528A1|1994-09-03|1996-03-07|Basf Ag|Process for the preparation of n-butyraldehyde and / or n-butanol| US5583277A|1994-10-03|1996-12-10|Mobil Oil Corporation|Removal of large molecules from a fluid| US5518707A|1994-10-24|1996-05-21|Uop|Metallo germanates| US5667695A|1994-10-24|1997-09-16|Uop|Process for removing contaminant metal ions from liquid streams using metallo germanate molecular sieves| US5552132A|1994-10-28|1996-09-03|Chevron U.S.A. Inc.|Preparing a crystalline aluminophosphate composition| US5756789A|1995-06-08|1998-05-26|Texaco, Inc.|Synthesis of metal--containing aluminophosphates with layered structure| GB9514388D0|1995-07-13|1995-09-13|Tioxide Group Services Ltd|Titanium dioxide pigments| US5830427A|1995-08-21|1998-11-03|Uop Llc|Metallochalcogenide microporous compositions having metal-metal bonds| US5741751A|1995-11-07|1998-04-21|Chevron U.S.A. Inc.|Alumina source for non-zeolitic molecular sieves| AU7553996A|1995-11-07|1997-05-29|Chevron U.S.A. Inc.|Alumina source for non-zeolitic molecular sieves| US5648508A|1995-11-22|1997-07-15|Nalco Chemical Company|Crystalline metal-organic microporous materials| FR2742070B1|1995-12-08|1998-01-09|Inst Francais Du Petrole|PROCESS FOR THE CONTROLLED PRODUCTION OF SUPPORTED ZEOLITE MEMBRANES| US5939349A|1996-01-26|1999-08-17|Chevron U.S.A. Inc.|Method of preparing non-zeolitic molecular sieve catalyst| NO310106B1|1996-03-13|2001-05-21|Norsk Hydro As|Microporous, crystalline metallophosphate compounds, a process for the preparation and use thereof| US6040264A|1996-04-04|2000-03-21|Exxon Chemical Patents Inc.|Use of alkaline earth metal containing small pore non-zeolitic molecular sieve catalysts in oxygenate conversion| US5780003A|1996-08-23|1998-07-14|Uop Llc|Crystalline manganese phosphate compositions| US6060415A|1997-02-10|2000-05-09|National Science Council|Aligned molecular sieve crystals grown on anodic alumina membrane| US6051746A|1997-06-18|2000-04-18|Exxon Chemical Patents Inc.|Oxygenate conversions using modified small pore molecular sieve catalysts| RO114524B1|1997-10-02|1999-05-28|Sc Zecasin Sa|Process for producing olefins with low molecular mass by fluidized bed catalytic conversion of methanol| US5912393A|1997-12-09|1999-06-15|Uop Llc|Metallo aluminophosphate molecular sieve with novel crystal morphology and methanol to olefin process using the sieve| US5976491A|1998-10-09|1999-11-02|Exxon Research And Engineering Co.|Synthesis of and composition of ECR-40, large pore aluminophosphate| GB9822654D0|1998-10-17|1998-12-09|Procter & Gamble|Odour control methods and compositions| US5989518A|1998-12-29|1999-11-23|Uop Llc|Process for synthesizing and controlling the particle size and particle size distribution of a molecular sieve| US6656447B1|1998-12-29|2003-12-02|Uop Llc|Process for synthesizing and controlling the particle size and particle size distribution of a molecular sieve| US6503863B2|1999-06-07|2003-01-07|Exxonmobil Chemical Patents, Inc.|Heat treating a molecular sieve and catalyst| US6407269B2|1999-06-08|2002-06-18|Kao Corporation|Catalyst for transesterification| US6187981B1|1999-07-19|2001-02-13|Uop Llc|Process for producing arylalkanes and arylalkane sulfonates, compositions produced therefrom, and uses thereof| US6303841B1|1999-10-04|2001-10-16|Uop Llc|Process for producing ethylene| US6406521B1|1999-11-30|2002-06-18|Linda S. Cheng|Process for purifying propylene| US6293999B1|1999-11-30|2001-09-25|Uop Llc|Process for separating propylene from propane| US6296688B1|1999-11-30|2001-10-02|Uop Llc|Vacuum swing adsorption process for separating propylene from propane| US6797155B1|1999-12-21|2004-09-28|Exxonmobil Research & Engineering Co.|Catalytic cracking process using a modified mesoporous aluminophosphate material| US6773694B1|1999-12-22|2004-08-10|Uop Llc|Process for synthesizing molecular sieves| US6531639B1|2000-02-18|2003-03-11|Exxonmobil Chemical Patents, Inc.|Catalytic production of olefins at high methanol partial pressures| US6392109B1|2000-02-29|2002-05-21|Chevron U.S.A. Inc.|Synthesis of alkybenzenes and synlubes from Fischer-Tropsch products| US6437197B1|2000-04-27|2002-08-20|Shell Oil Company|Process for catalytic hydroxylation of aromatic hydrocarbons| US6548718B2|2000-04-27|2003-04-15|Shell Oil Company|Process for catalytic hydroxylation of, saturated or unsaturated, aliphatic compounds| US6379641B1|2000-05-01|2002-04-30|Uop Llc|Microporous rare earth silicates and method of producing same| US6613950B1|2000-06-06|2003-09-02|Exxonmobil Chemical Patents Inc.|Stripping hydrocarbon in an oxygenate conversion process| US6566569B1|2000-06-23|2003-05-20|Chevron U.S.A. Inc.|Conversion of refinery C5 paraffins into C4 and C6 paraffins| US6441261B1|2000-07-28|2002-08-27|Exxonmobil Chemical Patents Inc.|High pressure oxygenate conversion process via diluent co-feed| US6486219B1|2000-09-27|2002-11-26|Exxonmobil Chemical Patents, Inc.|Methanol, olefin, and hydrocarbon synthesis process| US6444712B1|2000-09-28|2002-09-03|Exxonmobil Chemical Patents, Inc.|Methanol, olefin, and hydrocarbon synthesis process| US6593506B1|2000-10-12|2003-07-15|Exxonmobil Chemical Patents Inc.|Olefin recovery in a polyolefin production process| US6495609B1|2000-11-03|2002-12-17|Exxonmobil Chemical Patents Inc.|Carbon dioxide recovery in an ethylene to ethylene oxide production process| DK1214974T3|2000-12-13|2008-09-29|Uop Llc|Metalloaluminium phosphate molecular sieve with cubic crystal morphology and methanol for olefin process using the sieve| US6580010B2|2001-01-03|2003-06-17|Exxonmobil Chemical Patents, Inc.|Olefin recovery in an olefin production process| US6596156B1|2001-01-05|2003-07-22|China Petroleum And Chemical Corporation|SAPO-11 molecular sieve, its synthetic method and a catalyst containing the molecular sieve| CN100523655C|2001-02-21|2009-08-05|三菱化学株式会社|Adsorption heat pump and use of adsorbent as adsorbent for adsorption heat pump| US6965026B2|2001-02-23|2005-11-15|University Of South Florida|Nanoscale faceted polyhedra| GB0106269D0|2001-03-14|2001-05-02|Auntiegravity Ltd|Improvements in noise cancellation| WO2002076612A1|2001-03-22|2002-10-03|Uop Llc|Metallo aluminophosphate molecular sieve with cubic crystal morphology and methanol to olefin process using the sieve| US6632415B2|2001-04-09|2003-10-14|Chevron U.S.A. Inc.|Methods for making molecular sieves| CA2445415C|2001-04-24|2011-08-30|Harold J. Vinegar|In situ recovery from a oil shale formation| ES2282488T3|2001-07-02|2007-10-16|Exxonmobil Chemical Patents Inc.|INHIBITION OF THE COKE FORMATION IN A CATALYST IN THE MANUFACTURE OF AN OLEFINA.| US7015175B2|2001-08-29|2006-03-21|Uop Llc|High-activity isomerization catalyst and process| US6979396B2|2001-08-29|2005-12-27|Uop Llc|Combination reforming and isomerization process| US7435329B1|2001-08-29|2008-10-14|Uop Llc|Combination reforming and isomerization process| US7022889B2|2001-08-29|2006-04-04|Uop Llc|Isomerization process using novel catalyst| US6699385B2|2001-10-17|2004-03-02|Chevron U.S.A. Inc.|Process for converting waxy feeds into low haze heavy base oil| WO2003036039A1|2001-10-24|2003-05-01|Shell Internationale Research Maatschappij B.V.|In situ production of a blending agent from a hydrocarbon containing formation| US6660682B2|2001-11-30|2003-12-09|Exxon Mobil Chemical Patents Inc.|Method of synthesizing molecular sieves| US20030130555A1|2001-11-30|2003-07-10|Minquan Cheng|Oxygenated hydrocarbon compositions and method for recovering the compositions| US7227048B2|2001-12-31|2007-06-05|Exxonmobil Chemical Patents Inc.|Converting oxygenates to olefins over a catalyst comprising acidic molecular sieve of controlled carbon atom to acid site ratio| US7319178B2|2002-02-28|2008-01-15|Exxonmobil Chemical Patents Inc.|Molecular sieve compositions, catalysts thereof, their making and use in conversion processes| US7208442B2|2002-02-28|2007-04-24|Exxonmobil Chemical Patents Inc.|Molecular sieve compositions, catalyst thereof, their making and use in conversion processes| US6995111B2|2002-02-28|2006-02-07|Exxonmobil Chemical Patents Inc.|Molecular sieve compositions, catalysts thereof, their making and use in conversion processes| US7307196B2|2002-02-28|2007-12-11|Exxonmobil Chemical Patents Inc.|Molecular sieve compositions, catalyst thereof, their making and use in conversion processes| US6730142B2|2002-03-19|2004-05-04|Exxonmobil Research And Engineering Company|Separation of propylene from hydrocarbon mixtures| US7271123B2|2002-03-20|2007-09-18|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion process| FR2837489B1|2002-03-20|2004-06-18|Inst Francais Du Petrole|IM-6 CRYSTALLIZED SOLID METALLOPHOSPHATE TYPE AND PROCESS FOR PREPARING THE SAME| US6872680B2|2002-03-20|2005-03-29|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| US6759360B2|2002-03-29|2004-07-06|Exxonmobil Chemical Patent Inc.|Interior surface modifications of molecular sieves with organometallic reagents and the use thereof for the conversion of oxygenates to olefins| US6680278B2|2002-06-12|2004-01-20|Exxonmobil Chemical Patents, Inc.|Synthesis of silicoaluminophosphates| US6793901B2|2002-06-12|2004-09-21|Exxonmobil Chemical Patents, Inc.|Synthesis of molecular sieves having the CHA framework type| US6620983B1|2002-06-12|2003-09-16|Exxonmobil Chemical Patents Inc.|Synthesis of aluminophosphates and silicoaluminophosphates| US6906232B2|2002-08-09|2005-06-14|Exxonmobil Chemical Patents Inc.|Molecular sieve compositions, catalysts thereof, their making and use in conversion processes| WO2004016574A1|2002-08-14|2004-02-26|Exxonmobil Chemical Patents Inc.|Process for preparing olefins from oxygenates| US7238846B2|2002-08-14|2007-07-03|Exxonmobil Chemical Patents Inc.|Conversion process| US7317133B2|2002-11-21|2008-01-08|Uop Llc|Process for enhanced olefin production| US7026267B2|2002-12-20|2006-04-11|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its production and use in conversion processes| US6767858B1|2003-02-20|2004-07-27|Exxonmobil Chemical Patents Inc.|Synthesis of alumino- and silicoalumino-phosphates of CHA framework type| FR2854171B1|2003-04-24|2005-06-17|Inst Francais Du Petrole|IM-8 METALLOPHOSPHATE CRYSTALLIZED SOLID AND PROCESS FOR PREPARING THE SAME| US7247287B2|2003-06-11|2007-07-24|Exxonmobil Chemical Patents Inc.|Synthesis of aluminophosphates and silicoaluminophosphates| US7148392B2|2003-06-17|2006-12-12|Exxonmobil Research And Engineering Company|Separation of 1-butene from C4 feed streams| ES2317043T3|2003-06-23|2009-04-16|Baxter International Inc.|CARTE PROTEINS FOR VACCINES.| US7255849B2|2003-06-24|2007-08-14|Exxonmobil Research And Engineering Company|EMM-3, new crystalline microporous material| US6927187B2|2003-07-11|2005-08-09|Exxonmobil Chemical Patents Inc.|Synthesis of silicoaluminophosphates| US6951830B2|2003-08-05|2005-10-04|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst compositions, their production and use in conversion processes| US6835363B1|2003-08-06|2004-12-28|Exxonmobil Chemical Patents Inc.|Synthesis of molecular sieves of CHA framework type| US6984765B2|2003-09-08|2006-01-10|Exxonmobil Chemical Patents Inc.|Separation of methanol, ethanol and/or dimethyl ether from hydrocarbon mixtures| US7122500B2|2003-09-22|2006-10-17|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| US7241713B2|2003-10-02|2007-07-10|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| AU2004285450B2|2003-10-20|2010-01-14|Gregory K. Frykman|Zeolite molecular sieves for the removal of toxins| US7153483B2|2003-10-22|2006-12-26|Chevron U.S.A. Inc.|Crystalline molecular sieve SSZ-51 composition of matter and synthesis thereof| US7241716B2|2003-11-10|2007-07-10|Exxonmobil Chemical Patents Inc.|Protecting catalytic sites of metalloaluminophosphate molecular sieves| US6894201B1|2003-12-19|2005-05-17|Uop Llc|Process and apparatus for the removal of nitrogen compounds from a fluid stream| US7205448B2|2003-12-19|2007-04-17|Uop Llc|Process for the removal of nitrogen compounds from a fluid stream| US7138006B2|2003-12-24|2006-11-21|Chevron U.S.A. Inc.|Mixed matrix membranes with low silica-to-alumina ratio molecular sieves and methods for making and using the membranes| US7166146B2|2003-12-24|2007-01-23|Chevron U.S.A. Inc.|Mixed matrix membranes with small pore molecular sieves and methods for making and using the membranes| US7253331B2|2004-05-12|2007-08-07|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| WO2005114203A2|2004-05-20|2005-12-01|The Regents Of The University Of California|Dominant b cell epitopes and methods of making and using thereof| US7456123B2|2004-06-08|2008-11-25|Exxonmobil Research And Engineering Company|FCC catalyst| US7504021B2|2004-06-08|2009-03-17|Exxonmobil Research And Engineering Company|FCC process using mesoporous catalyst| US8916208B2|2004-06-24|2014-12-23|California Institute Of Technology|Aluminophosphate-based materials for the treatment of wounds| US7663012B2|2004-06-25|2010-02-16|Uop Llc|Conversion of dimethylether to propylene using moving bed technology| US7371915B1|2004-06-25|2008-05-13|Uop Llc|Conversion of oxygenate to propylene using moving bed technology| US7199277B2|2004-07-01|2007-04-03|Exxonmobil Chemical Patents Inc.|Pretreating a catalyst containing molecular sieve and active metal oxide| CN100418880C|2004-07-19|2008-09-17|中国石油化工股份有限公司|Molecular sieve with AWO structure and its synthesizing process| US7186875B2|2004-07-30|2007-03-06|Exxon Mobil Chemical Patents Inc.|Conversion of oxygenates to olefins| US7166757B2|2004-07-30|2007-01-23|Exxonmobil Chemical Patents Inc.|Conversion of oxygenates to olefins| US7199278B2|2004-07-30|2007-04-03|Exxonmobil Chemical Patents Inc.|Conversion of oxygenates to olefins| US7582203B2|2004-08-10|2009-09-01|Shell Oil Company|Hydrocarbon cracking process for converting gas oil preferentially to middle distillate and lower olefins| AU2005274030B2|2004-08-10|2008-11-20|Shell Internationale Research Maatschappij B.V.|Method and apparatus for making a middle distillate product and lower olefins from a hydrocarbon feedstock| US20060040821A1|2004-08-18|2006-02-23|Pujado Peter R|Treatment of air to a catalyst regenerator to maintain catalyst activity| US7371916B1|2004-09-16|2008-05-13|Uop Llc|Conversion of an alcoholic oxygenate to propylene using moving bed technology and an etherification step| US7405337B2|2004-09-21|2008-07-29|Uop Llc|Conversion of oxygenate to propylene with selective hydrogen treatment of heavy olefin recycle stream| US7408092B2|2004-11-12|2008-08-05|Uop Llc|Selective conversion of oxygenate to propylene using moving bed technology and a hydrothermally stabilized dual-function catalyst| US7374660B2|2004-11-19|2008-05-20|Exxonmobil Chemical Patents Inc.|Process for selectively producing C3 olefins in a fluid catalytic cracking process with recycle of a C4 fraction to a secondary reaction zone separate from a dense bed stripping zone| US7465845B2|2004-12-22|2008-12-16|Exxonmobil Chemical Patents Inc.|Increasing ethylene and/or propylene production in an oxygenate to olefins reaction systems| US7414167B2|2005-01-14|2008-08-19|Uop Llc|Conversion of oxygenate to propylene using moving bed technology and a separate heavy olefin interconversion step| US7449611B2|2005-01-31|2008-11-11|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| WO2006083423A1|2005-01-31|2006-08-10|Exxonmobil Chemical Patents, Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| US7453020B2|2005-01-31|2008-11-18|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| US7456330B2|2005-01-31|2008-11-25|Exxonmobil Chemical Patents Inc.|Molecular sieve catalyst composition, its making and use in conversion processes| US7737316B2|2005-06-24|2010-06-15|Exxonmobil Chemical Patents Inc.|Method of flocculation and formulation of crystalline materials| US7550403B2|2005-06-30|2009-06-23|Uop Llc|Methods for recovering activity of molecular sieve catalysts| US8129576B2|2005-06-30|2012-03-06|Uop Llc|Protection of solid acid catalysts from damage by volatile species| US7442233B2|2005-07-06|2008-10-28|Basf Catalysts Llc|Integrated heavy hydrocarbon removal, amine treating and dehydration| US7112316B1|2005-08-08|2006-09-26|Uop Llc|Process for preparing molecular sieves via continuous addition of nutrients| WO2007021394A2|2005-08-18|2007-02-22|Exxonmobil Chemical Patents Inc.|Catalytic conversion of oxygenates to olefins| US8048402B2|2005-08-18|2011-11-01|Exxonmobil Chemical Patents Inc.|Synthesis of molecular sieves having the chabazite framework type and their use in the conversion of oxygenates to olefins| US7301064B1|2005-09-14|2007-11-27|Uop Llc|Ethylbenzene conversion and xylene isomerization processes and catalysts therefor| US7381677B1|2005-09-14|2008-06-03|Uop Llc|Ethylbenzene conversion and xylene isomerization processes and catalysts therefor| US7297830B2|2005-09-14|2007-11-20|Uop Llc|Process for isomerizing non-equilibrium xylene-containing feed streams| US7784510B2|2005-10-17|2010-08-31|Sumitomo Rubber Industries, Ltd.|Heavy duty tire having cap and base rubber layers, belt cushion rubber and sidewall rubber| CA2626965C|2005-10-24|2014-10-14|Shell Internationale Research Maatschappij B.V.|Methods of cracking a crude product to produce additional crude products| US20070142212A1|2005-11-22|2007-06-21|Pujado Peter R|Treatment of air to a catalyst regenerator to maintain catalyst activity| US7998893B2|2005-11-22|2011-08-16|Uop Llc|Treatment of air to a catalyst regenerator to maintain catalyst activity| US8562941B2|2005-12-20|2013-10-22|Exxonmobil Research And Engineering Company|Perturbed synthesis of materials| CA2631560C|2005-12-20|2014-08-12|Exxonmobil Research And Engineering Company|Itq-26, new crystalline microporous material| US7767871B2|2005-12-22|2010-08-03|Exxonmobil Chemical Patents Inc.|Method of recovering crystalline material and compositions therefrom| US8227367B2|2006-03-23|2012-07-24|Uop Llc|Removal of water and salts from a catalyst regenerator to maintain catalyst activity| EP2010754A4|2006-04-21|2016-02-24|Shell Int Research|Adjusting alloy compositions for selected properties in temperature limited heaters| JP5158305B2|2006-06-02|2013-03-06|東ソー株式会社|High-purity aluminophosphate zeolite, method for producing the same, and use thereof| CN100463695C|2006-07-06|2009-02-25|欧阳允武|Antesepsis processing method for printed matter and antibiotic printed matter processed thereby| CN100358805C|2006-07-26|2008-01-02|中国科学院上海硅酸盐研究所|Nitrogen-containing aluminium phosphate mesoporous molecular sieve and its prepn| US7744850B2|2006-08-03|2010-06-29|Uop Llc|UZM-22 aluminosilicate zeolite, method of preparation and processes using UZM-22| JP5055944B2|2006-10-18|2012-10-24|トヨタ自動車株式会社|Dehumidifying / humidifying device for vehicles| US7841401B2|2006-10-20|2010-11-30|Shell Oil Company|Gas injection to inhibit migration during an in situ heat treatment process| US7655824B2|2006-10-30|2010-02-02|Uop Llc|Processes for producing alkylbenzenes over solid acid catalyst at low benzene to olefin ratios and low heavies make| WO2008073237A2|2006-12-07|2008-06-19|Exxonmobil Research And Engineering Company|Itq-34, crystalline microporous material| CN101600782B|2007-02-06|2013-02-13|国际壳牌研究有限公司|Process for the preparation of alkylate and middle distillate| US7576247B2|2007-02-12|2009-08-18|Uop Llc|Processes for making detergent range alkylbenzenes| US7652182B2|2007-02-12|2010-01-26|Uop Llc|Energy integrated processes including alkylation and transalkylation for making detergent range alkylbenzenes| US7692055B2|2007-02-12|2010-04-06|Uop Llc|Transalkylation of dialkylbenzene| US7642389B2|2007-02-12|2010-01-05|Uop Llc|Energy integrated processes including alkylation and transalkylation for making detergent range alkylbenzenes| JP5266657B2|2007-03-30|2013-08-21|三菱樹脂株式会社|Dehumidifying / humidifying device for vehicles| EP2147083A1|2007-04-13|2010-01-27|Shell Internationale Research Maatschappij B.V.|Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock| US8381815B2|2007-04-20|2013-02-26|Shell Oil Company|Production from multiple zones of a tar sands formation| BRPI0810963A2|2007-04-30|2017-05-09|Shell Int Research|system and method| US8993468B2|2007-05-24|2015-03-31|Saudi Basic Industries Corporation|Catalyst for conversion of hydrocarbons, process of making and process of using thereof—Ge zeolites| US8969232B2|2007-05-24|2015-03-03|Saudi Basic Industries Corporation|Catalyst for conversion of hydrocarbons, process of making and process of using thereof—incorporation 2| US9221723B2|2007-05-24|2015-12-29|Saudi Basic Industries Corporation|Catalyst for conversion of hydrocarbons, process of making and process of using thereof—incorporation-1| US9233884B2|2007-05-24|2016-01-12|Saudi Basic Industries Corporation|Catalyst for conversion of hydrocarbons, process of making and process of using thereof—bimetallic deposition| KR101395454B1|2007-09-20|2014-05-15|삼성전자주식회사|Optical film having a graded index of refraction and fabricating method thereof| MX2010003577A|2007-10-01|2010-09-22|Lummus Technology Inc|Separating olefin streams.| US7589044B2|2007-10-02|2009-09-15|Chevron Phillips Chemical Company Lp|Methods of preparing a polymerization catalyst| DE112008002718T5|2007-10-10|2010-09-09|Shell Internationale Research Maatschappij B.V.|Systems and processes for producing a middle distillate product and lower olefins from a hydrocarbon feedstock| CA2700737A1|2007-10-19|2009-04-23|Shell Internationale Research Maatschappij B.V.|Three-phase heaters with common overburden sections for heating subsurface formations| US8431509B2|2007-10-30|2013-04-30|Cerahelix, Inc.|Structure for molecular separations| US8431508B2|2007-10-30|2013-04-30|Cerahelix, Inc.|Inorganic structure for molecular separations| US20090114089A1|2007-11-02|2009-05-07|Chunqing Liu|Microporous Aluminophosphate Molecular Sieve Membranes for Highly Selective Separations| WO2009070484A1|2007-11-29|2009-06-04|Shell Oil Company|Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock| EP2067528A1|2007-11-29|2009-06-10|Uop Llc|Process for preparing a layered molecular sieve composition| US7638456B2|2007-12-18|2009-12-29|Chevron Phillips Chemical Company Lp|Methods of preparing a polymerization catalyst| US20090163757A1|2007-12-20|2009-06-25|Gee Jeffery C|Linear olefin isomer isomerization using molecular sieve catalysts| CN101952392A|2007-12-21|2011-01-19|环球油品公司|Prepare aviation fuel from biological renewable raw materials| US8876922B2|2007-12-21|2014-11-04|Grace Gmbh & Co. Kg|Treatment of biofuels| EP2085360B1|2007-12-27|2014-05-07|Chevron U.S.A. Inc.|Crystalline silicoaluminophosphate| US7732537B2|2008-01-29|2010-06-08|Exxonmobil Chemical Patents Inc.|Methods addressing aging in flocculated molecular sieve catalysts for hydrocarbon conversion processes| US9169450B2|2008-02-12|2015-10-27|Chevron U.S.A. Inc.|Method of upgrading heavy hydrocarbon streams to jet and diesel products| US20100029998A1|2008-07-29|2010-02-04|Chevron U.S.A. Inc.|Synthesis of a Crystalline Silicoaluminophosphate| US8932454B2|2008-09-18|2015-01-13|Exxonmobile Research And Engineering Co.|Mesoporous Y hydrocracking catalyst and associated hydrocracking processes| US7922997B2|2008-09-30|2011-04-12|Uop Llc|UZM-35 aluminosilicate zeolite, method of preparation and processes using UZM-35| JP5692769B2|2008-11-25|2015-04-01|独立行政法人産業技術総合研究所|Method for synthesizing porous aluminophosphate crystal AlPO4-5| US8921627B2|2008-12-12|2014-12-30|Uop Llc|Production of diesel fuel from biorenewable feedstocks using non-flashing quench liquid| US8048403B2|2008-12-16|2011-11-01|Uop Llc|UZM-26 family of crystalline aluminosilicate compositions and method of preparing the compositions| US7915469B2|2008-12-16|2011-03-29|Uop Llc|Hydrocarbon conversion processes using UZM-26 and UZM-26X crystalline microporous zeolitic compositions| US7575737B1|2008-12-18|2009-08-18|Uop Llc|UZM-27 family of crystalline aluminosilicate compositions and a method of preparing the compositions| US7763764B2|2008-12-18|2010-07-27|Uop Llc|Hydrocarbon conversion processes using the UZM-27 family of crystalline aluminosilicate compositions| DK2440328T3|2009-06-12|2016-11-28|Albemarle Europe Sprl|SAPO molecular sieve and preparation and uses thereof| US7981273B2|2009-06-22|2011-07-19|Uop Llc|Process for catalytic cracking of hydrocarbons using UZM-35| US7982081B2|2009-06-29|2011-07-19|Uop Llc|Process for alkylation of aromatic hydrocarbons using UZM-35| FR2948299B1|2009-07-23|2011-07-01|Inst Francais Du Petrole|PROCESS FOR THE PREPARATION OF A LTA STRUCTURAL TYPE CRYSTALLIZED SOLID IN ION LIQUID MEDIUM| US8017824B2|2009-08-04|2011-09-13|Uop Llc|Hydrocarbon conversion processes using UZM-29 and UZM-29HS crystalline zeolitic compositions| US8268290B2|2009-08-04|2012-09-18|Uop Llc|UZM-29 family of crystalline zeolitic compositions and a method of preparing the compositions| FR2951162B1|2009-10-13|2012-01-06|Total Raffinage Marketing|PROCESS FOR PRODUCTION OF DISTILLATE BY CATALYTIC OLIGOMERIZATION OF OLEFINS IN THE PRESENCE OF METHANOL AND / OR DIMETHYL ETHER| KR101193973B1|2009-10-22|2012-10-24|현대엔지니어링 주식회사|Microspherical silicoaluminophosphate-34 catalyst with high performance & mechanical strength, Preparing method of the same and Preparing method of light olefins using that| US8409546B2|2009-11-24|2013-04-02|Basf Se|Process for the preparation of zeolites having B-CHA structure| BR112012012244A2|2009-11-24|2016-04-19|Basf Se|process for the preparation of zeolites having cha frame structure and a composition, zeolite material having cha frame, and use of a zeolite material| US8529868B2|2009-12-31|2013-09-10|Exxonmobil Research And Engineering Company|ITQ-40, new crystalline microporous material| US8715487B2|2010-03-11|2014-05-06|Exxonmobil Research And Engineering Company|Low small mesoporous peak cracking catalyst and method of using| US8158105B2|2010-03-31|2012-04-17|Uop Llc|UZM-37 aluminosilicate zeolite| US8158103B2|2010-03-31|2012-04-17|Uop Llc|UZM-37 aluminosilicate zeolite method of preparation| US7982084B1|2010-03-31|2011-07-19|Uop Llc|Processes using UZM-37 aluminosilicate zeolite| JP5786418B2|2010-04-22|2015-09-30|三菱樹脂株式会社|Adsorbent member and apparatus using the same| US8247631B2|2010-06-21|2012-08-21|Uop Llc|Process for catalytic cracking of hydrocarbons using UZM-35| US8053618B1|2010-06-21|2011-11-08|Uop Llc|UZM-35 zeolitic composition, method of preparation and processes| US8323747B2|2010-06-25|2012-12-04|Uop Llc|Zeolite containing wash coats for adsorber heat exchangers and temperature controlled adsorbers| US8158104B2|2010-07-01|2012-04-17|Uop Llc|UZM-7 aluminosilicate zeolite, method of preparation and processes using UZM-7| US8337593B2|2010-08-18|2012-12-25|Uop Llc|Process for purifying natural gas and regenerating one or more adsorbers| WO2012051004A1|2010-10-11|2012-04-19|Shell Oil Company|A process for catalytic cracking a fischer-tropsch derived feedstock with heat balanced operation of the catalytic cracking system| FR2966816B1|2010-10-28|2012-11-30|IFP Energies Nouvelles|IZM-4 CRYSTALLIZED SOLID AND PROCESS FOR PREPARING THE SAME| US8927799B2|2010-11-01|2015-01-06|Uop Llc|Propane dehydrogenation process utilizing fluidized catalyst system| US8350110B2|2010-11-02|2013-01-08|Uop Llc|Heavy alkylbenzene transalkylation operating cost reduction| US9359216B2|2010-11-23|2016-06-07|Reliance Industries Limited|Method for the preparation of MWW type zeolite| CN102485332B|2010-12-03|2013-10-16|中国石油天然气股份有限公司|Distillate oil hydrogenation deacidification catalyst containing molecular sieve, its preparation and application| CN102530987A|2010-12-29|2012-07-04|中国科学院大连化学物理研究所|Solvent thermal synthesis method of SAPOmolecular sieve and catalyst prepared by SAPO molecular sieve| US8900443B2|2011-04-07|2014-12-02|Uop Llc|Method for multi-staged hydroprocessing using quench liquid| US8518242B2|2011-05-26|2013-08-27|Uop Llc|Fibrous substrate-based hydroprocessing catalysts and associated methods| JP2015515429A|2011-12-22|2015-05-28|ユーオーピー エルエルシー|Layered conversion synthesis of zeolite.| WO2013096075A2|2011-12-22|2013-06-27|Uop Llc|Aromatic transformation using uzm-39 aluminosilicate zeolite| WO2013096069A2|2011-12-22|2013-06-27|Uop Llc|Uzm-39 aluminosilicate zeolite| US20130165717A1|2011-12-23|2013-06-27|Exxonmobil Research And Engineering Company|Process for increased production of fcc gasoline| US8906225B2|2012-06-29|2014-12-09|Uop Llc|Metallophosphate molecular sieves, methods of preparation and use| ES2627947T3|2012-06-29|2017-08-01|Uop Llc|Molecular metaphosphate sieves, method of preparation and use| US8871178B2|2012-06-29|2014-10-28|Uop Llc|Metallophosphate molecular sieves, methods of preparation and use| US8911614B2|2012-06-29|2014-12-16|Uop Llc|Metallophosphate molecular sieves, methods of preparation and use| CN102730713B|2012-06-29|2014-03-05|陕西师范大学|Ionothermal preparation method for rare earth-substituted ZON-structured aluminophosphate molecular sieve UiO-7| US8871177B2|2012-06-29|2014-10-28|Uop Llc|Metallophosphate molecular sieves, methods of preparation and use| CN102815720B|2012-07-24|2014-12-03|黑龙江大学|Synthetic method for SAPO-11 molecular sieve| IN2015DN02095A|2012-09-26|2015-08-14|Dalian Chemical Physics Inst| EP2902107B1|2012-09-26|2017-08-09|Dalian Institute Of Chemical Physics, Chinese Academy of Sciences|Sapo-34 molecular sieves and synthesis method thereof| US8569558B1|2012-11-30|2013-10-29|Uop Llc|Metallophosphate molecular sieves, method of preparation and use| US8936776B2|2012-11-30|2015-01-20|Uop Llc|Metallophosphate molecular sieves, method of preparation and use| US8569557B1|2012-11-30|2013-10-29|Uop Llc|Silicometallophosphate molecular sieves, method of preparation and use| ES2644610T3|2012-11-30|2017-11-29|Uop Llc|Molecular sieves of silicometaphosphates and use| US8911704B2|2012-11-30|2014-12-16|Uop Llc|Silicometallophosphate molecular sieves, method of preparation and use| ES2702178T3|2012-11-30|2019-02-27|Uop Llc|Molecular sieves of metal phosphate, method of preparation and use| US8609921B1|2012-12-12|2013-12-17|Uop Llc|Aromatic transalkylation using UZM-44 aluminosilicate zeolite| WO2014093440A1|2012-12-12|2014-06-19|Uop Llc|Conversion of methane to aromatic compounds using uzm-44 aluminosilicate zeolite| US8609910B1|2012-12-12|2013-12-17|Uop Llc|Catalytic pyrolysis using UZM-39 aluminosilicate zeolite| US8912378B2|2012-12-12|2014-12-16|Uop Llc|Dehydrocyclodimerization using UZM-39 aluminosilicate zeolite| US8609911B1|2012-12-12|2013-12-17|Uop Llc|Catalytic pyrolysis using UZM-44 aluminosilicate zeolite| US8609919B1|2012-12-12|2013-12-17|Uop Llc|Aromatic transformation using UZM-44 aluminosilicate zeolite| US8623321B1|2012-12-12|2014-01-07|Uop Llc|UZM-44 aluminosilicate zeolite| US8889939B2|2012-12-12|2014-11-18|Uop Llc|Dehydrocyclodimerization using UZM-44 aluminosilicate zeolite| US20140163281A1|2012-12-12|2014-06-12|Uop Llc|Conversion of methane to aromatic compounds using a catalytic composite| US8618343B1|2012-12-12|2013-12-31|Uop Llc|Aromatic transalkylation using UZM-39 aluminosilicate zeolite| WO2014100218A1|2012-12-21|2014-06-26|Exxonmobil Chemical Patents Inc.|Improved synthesis of succinimides and quaternary ammonium ions for use in making molecular sieves| PL2948244T3|2013-01-23|2020-08-10|Basf Corporation|Zsm-5 additive activity enhancement by improved zeolite and phosphorus interaction| US9376511B2|2013-03-13|2016-06-28|Chevron Phillips Chemical Company Lp|Polymerization catalysts and polymers| EP2980050B1|2013-03-29|2019-10-23|NGK Insulators, Ltd.|Aluminophosphate-metal oxide bonded body and production method for same| CN103303936A|2013-07-01|2013-09-18|中国海洋石油总公司|Method for synthesizing pure-phase SAPO-41 molecular sieve by use of crystallization mother liquid| CN103274430A|2013-07-01|2013-09-04|中国海洋石油总公司|Method for synthesizing pure phase SAPO-31 molecular sieve by recycling crystallization mother solution| BR112016000038B1|2013-07-04|2021-03-16|Total Research & Technology Feluy|catalyst compositions comprising small size molecular sieve crystals deposited in a porous material| US20150099913A1|2013-10-04|2015-04-09|Exxonmobil Research And Engineering Company|Methanol conversion process| RU2700590C2|2013-10-24|2019-09-18|В.Р.Грейс Энд Ко.-Конн.|Method for synthesis of silicoaluminophosphate-34 molecular sieves| CN105636693B|2013-11-22|2019-12-13|沙特基础工业公司|catalyst with improved activity/selectivity for light naphtha aromatization| WO2015094698A1|2013-12-20|2015-06-25|Exxonmobil Chemical Patents Inc.|Process for converting oxygenates to aromatic hydrocarbons| US9387469B2|2013-12-30|2016-07-12|Eastman Chemical Company|Carbonylation catalyst and process using same| US9416017B2|2014-07-03|2016-08-16|Chevron U.S.A. Inc.|Method for making molecular sieve SSZ-98| US10532350B2|2014-08-22|2020-01-14|W.R. Grace & Co.-Conn|Method for synthesizing silicoaluminophosphate-34 molecular sieves using monoisopropanolamine| JP6350160B2|2014-09-17|2018-07-04|東ソー株式会社|Method for producing zeolite| US9783463B2|2014-09-30|2017-10-10|Exxonmobil Chemical Patents Inc.|Conversion of acetylene and methanol to aromatics| US9751772B2|2014-12-04|2017-09-05|Uop Llc|Aluminophosphate molecular sieves using an organo-1-oxa-4-azoniumcyclohexane compound| US9815706B2|2014-12-04|2017-11-14|Uop Llc|Zeolites using an organo-1-oxa-4-azoniumcyclohexane compound| US9522896B2|2014-12-04|2016-12-20|Uop Llc|Organo-1-oxa-4-azonium cyclohexane compounds| US9901911B2|2014-12-18|2018-02-27|Uop Llc|Coherently grown composite aluminophosphate and silicoaluminophosphate molecular sieves| US10183285B2|2015-01-30|2019-01-22|Exxonmobil Research And Engineering Company|Process for preparing a molecular sieve| WO2016160081A1|2015-03-31|2016-10-06|Exxonmobil Chemical Patents Inc.|Oxygenated hydrocarbon conversion zoned method| EP3294842A1|2015-06-30|2018-03-21|ExxonMobil Research and Engineering Company|Fuel production from catalytic slurry oil| US9970869B2|2015-07-24|2018-05-15|Chevron Phillips Chemical Company Lp|Use of turbidimeter for measurement of solid catalyst system component in a reactor feed| WO2017023838A1|2015-08-06|2017-02-09|Uop Llc|Process for reconfiguring existing treating units in a refinery| WO2017105871A1|2015-12-17|2017-06-22|Exxonmobil Research And Engineering Company|Fluid catalytic cracking of tight oil resid| US10449527B2|2016-03-04|2019-10-22|Uop Llc|High charge density silicometallophosphate molecular sieves SAPO-79| US10449528B2|2016-03-04|2019-10-22|Uop Llc|High charge density silicometallophosphate molecular sieves| US10421063B2|2016-03-04|2019-09-24|Uop Llc|High charge density silicometallophosphate molecular sieves SAPO-69| US10449526B2|2016-05-25|2019-10-22|Uop Llc|High charge density metallophosphate molecular sieves| US10159965B2|2016-05-25|2018-12-25|Uop Llc|High charge density metallophosphate molecular sieves| US10370257B2|2016-05-25|2019-08-06|Uop Llc|High charge density metalloaluminophosphosilicate molecular sieves| CN108602052B|2016-05-25|2021-11-26|环球油品公司|High charge density metal phosphate molecular sieves| US10240099B2|2016-10-27|2019-03-26|Uop Llc|Processes for producing a fuel from a renewable feedstock| US10399007B2|2016-11-08|2019-09-03|Uop Llc|Temperature swing adsorption process and apparatus with closed loop regeneration| EP3555232A1|2016-12-19|2019-10-23|ExxonMobil Research and Engineering Company|Trim alkali metal desulfurization of refinery fractions| CA3059217A1|2017-04-07|2018-10-11|Exxonmobil Research And Engineering Company|Resid upgrading with reduced severity fcc processing| US10570021B2|2017-07-28|2020-02-25|Uop Llc|Crystalline metallophosphates, their method of preparation, and use| US10513440B2|2017-07-28|2019-12-24|Uop Llc|Crystalline metallophosphates, their method of preparation, and use| US10493424B2|2017-07-28|2019-12-03|Uop Llc|Crystalline metallophosphates, their method of preparation, and use| EP3676000A1|2017-08-31|2020-07-08|Umicore Ag & Co. Kg|Palladium/zeolite-based passive nitrogen oxide adsorber catalyst for purifying exhaust gas| US11161100B2|2017-08-31|2021-11-02|Umicore Ag & Co. Kg|Use of a palladium/platinum/zeolite-based catalyst as passive nitrogen oxide adsorber for purifying exhaust gas| EP3450015A1|2017-08-31|2019-03-06|Umicore Ag & Co. Kg|Palladium-zeolite-based passive nitrogen oxide adsorber catalyst for exhaust gas treatment| WO2019134958A1|2018-01-05|2019-07-11|Umicore Ag & Co. Kg|Passive nitrogen oxide adsorber| US10577547B2|2018-02-27|2020-03-03|Uop Llc|Process for producing fuels from a blended biorenewable feed| US10662069B2|2018-06-21|2020-05-26|Uop Llc|Crystalline metallophosphates, their method of preparation, and use| US10280089B1|2018-06-22|2019-05-07|Uop Llc|Crystalline metallophosphates, their method of preparation, and use| US10336622B1|2018-06-22|2019-07-02|Uop Llc|Crystalline metallophosphates, their method of preparation, and use| CN111099637A|2018-10-25|2020-05-05|中国石油化工股份有限公司|Silicon-phosphorus-aluminum molecular sieve and preparation method thereof| CN111099603A|2018-10-25|2020-05-05|中国石油化工股份有限公司|SCM-18 molecular sieve and preparation method thereof| US10703986B1|2019-01-30|2020-07-07|Exxonmobil Research And Engineering Company|Selective oxidation using encapsulated catalytic metal| US10899971B2|2019-02-13|2021-01-26|Exxonmobil Research And Engineering Company|Stabilization of zeolite beta for FCC processes| US10876050B2|2019-03-01|2020-12-29|Uop Llc|Process for producing diesel fuel from a biorenewable feed| WO2020197893A1|2019-03-28|2020-10-01|Exxonmobil Chemical Patents Inc.|Processes for converting benzene and/or toluene via methylation| WO2020197888A1|2019-03-28|2020-10-01|Exxonmobil Chemical Patents Inc.|Processes and systems for converting benzene and/or toluene via methylation| CN113574036A|2019-03-28|2021-10-29|埃克森美孚化学专利公司|Method for converting benzene and/or toluene via methylation| US10807083B1|2019-06-04|2020-10-20|Uop Llc|Metallophosphate molecular sieves and method of preparation and use| CN112079363A|2019-06-14|2020-12-15|中国石油化工股份有限公司|Silicon-phosphorus-aluminum molecular sieve with AFN structure and synthesis method and application thereof| US10737253B1|2019-09-11|2020-08-11|Uop Llc|Metallophosphate molecular sieves and method of preparation and use| EP3808431A1|2019-09-12|2021-04-21|Basf Se|Process and plant for deacidifying a fluid stream comprising sulfur compounds, including organic sulfur compounds| EP3824988A1|2019-11-20|2021-05-26|UMICORE AG & Co. KG|Catalyst for reducing nitrogen oxides| RU2750099C1|2020-04-03|2021-06-22|Федеральное государственное бюджетное научное учреждение Уфимский федеральный исследовательский центр Российской академии наук|Method for production of granular micro-meso-macroporous aluminophosphate molecular sieve alpo4-11 exhibiting high crystallinity| US20220048015A1|2020-08-12|2022-02-17|Chevron Phillips Chemical Company Lp|Catalyst Supports and Catalyst Systems and Methods|
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申请号 | 申请日 | 专利标题 US06/166,333|US4310440A|1980-07-07|1980-07-07|Crystalline metallophosphate compositions| 相关专利
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