1-10. (canceled)
11. A pharmaceutical composition comprising:
(i) a poorly water soluble drug having a drug solubility of 100 ml or more as a volume of solvent required for dissolving 1 g;
(ii) a gel-forming water-soluble polymer; and
(iii) a salt substance consisting of an alkali and a weak or strong acid and said salt substance having an endothermic standard enthalpy of solution (KJmol) or heat of solution (Kcalmol) wherein said salt substance is selected from the group consisting of sodium bicarbonate, potassium bicarbonate, potassium sulfate, potassium chloride, sodium chloride and potassium dihydrogenphosphate;
wherein said poorly water soluble drug is held in said gel forming water soluble polymer as a solid dispersion
wherein said drug, said gel-forming water-soluble polymer and said salt substance are added in amounts (wt.wt %) of 1 to 30%, 3 to 60%, and 3 to 50%, respectively based on the total amount of the preparation, and
without adding any organic acid.
12. The pharmaceutical composition according to claim 11, wherein said salt substance is present in an amount of 0.1 part by weight or more based on 1 part by weight of the gel-forming water soluble polymer.
13. The pharmaceutical composition according to claim 12, wherein said salt substance is present in an amount of from 0.1 to 6 parts by weight based on 1 part by weight of the gel-forming water-soluble polymer.
14. The pharmaceutical composition according to claim 11, which is in the form of a tablet, a granule, or a capsule.
15. The pharmaceutical composition according to claim 11, wherein the poorly water soluble drug is 4\u2032-(2-methyl-1,4,5,6-tetrahydroimidazo4,5-d1benzoazepin-6-yl)carbonyl-2 phenylbenzanilide or a salt thereof.
16. A pharmaceutical preparation according to claim 11, which comprises a medicament of 4\u2032-(2-methyl-1,4,5,6-tetrahydroimidazo4,5-d1benzoazepin-6-yl)carbonyl-2 phenylbenzanilide or a salt thereof and a pharmaceutical carrier, said preparation exhibiting a dissolution of 75% of said medicament within 15 minutes when a test is performed using 500 ml of a first fluid (pH 1.2) at 100 r.p.m. in accordance with a second method (paddle method) for dissolution as specified in Japanese Pharmacopeia, 13th Edition.
17. The pharmaceutical preparation according to claim 16, wherein the pharmaceutical carrier comprises a gel-forming water-soluble polymer, a surfactant and a salt substance comprising an alkali and a weak or strong acid, and said salt substance having an endothermic standard enthalpy of solution or heat of solution.
The claims below are in addition to those above.
All refrences to claim(s) which appear below refer to the numbering after this setence.
1. A process for producing light aromatic hydrocarbons and light alkanes from hydrocarbonaceous feedstock, comprising the following steps:
(a) introducing hydrogen and a hydrocarbonaceous feedstock having boiling point in range of 30-250\xb0 C. into at least one reaction zone;
(b) converting the hydrocarbonaceous feedstock to an effluent enriched in light aromatic hydrocarbons of benzene, toluene and xylene and light alkanes in the reaction zone in the presence of a catalyst, wherein of the hydrocarbonaceous feedstock the heavy aromatic hydrocarbons are subjected to hydrodealkylation andor transalkylation with light aromatic hydrocarbon, the light aromatic hydrocarbons are subjected to isomerization and the non-aromatic hydrocarbons are subjected to hydrocracking reaction, and the catalyst comprises metallic Pt andor Pd supported on a binder-free zeolite for producing light aromatic hydrocarbons and light alkanes from hydrocarbonaceous feedstock, wherein the amount of metallic Pt andor Pd is of 0.01-0.8 wt % on the basis of the total weight of the catalyst, and the binder-free zeolite is selected from the group consisting of mordenite, beta zeolite, Y zeolite, ZSM-5, ZSM-11 and composite or cocrystal zeolite thereof; and
(c) recovering the light aromatic hydrocarbons and the light alkanes respectively by passing the effluent through gas-liquid separation and distillation sequentially, and the separated heavy fraction is recycled to the reaction zone for further reaction.
2. The process according to claim 1, wherein in step (a) the hydrocarbonaceous feedstock is introduced into the reaction zone at a weight hour space velocity of 0.5-10 hr\u22121, and the molar ratio of hydrogen to the hydrocarbonaceous feedstock is of 0.5:1-10:1.
3. The process according to claim 1, wherein in step (b) the reaction temperature is of 250-600\xb0 C. and the reaction pressure is of 0.5-5.0 MPa.
4. The process according to claim 1, wherein the hydrocarbonaceous feedstock is selected from the group consisting of reformate, pyrolysis gasoline, naphtha and mixture thereof.
5. The process according to claim 1, wherein step (c) comprises passing the effluent through a gas-liquid separator to obtain first overhead stream comprising hydrogen, methane, ethane and LPG and first bottom stream comprising aromatic hydrocarbons as well as residual hydrogen and non-aromatic hydrocarbons, recovering LPG from the first overhead stream; and passing the first bottom stream through a distillation column to obtain second overhead stream comprising residual hydrogen and non-aromatic hydrocarbons and second bottom stream comprising aromatic hydrocarbons, further recovering LPG from the second overhead stream, and recovering aromatic hydrocarbons from the second bottom stream.
6. The process according to claim 2, wherein in step (b) the reaction temperature is 250-600\xb0 C., and the reaction pressure is 0.5-5.0 MPa.
7. The process according to claim 2, wherein the hydrocarbonaceous feedstock is selected from the group consisting of reformate, pyrolysis gasoline, naphtha and mixture thereof.
8. The process according to claim 2, wherein step (c) comprises passing the effluent through a gas-liquid separator to obtain first overhead stream comprising hydrogen, methane, ethane and LPG and first bottom stream comprising aromatic hydrocarbons as well as residual hydrogen and non-aromatic hydrocarbons, recovering LPG from the first overhead stream; and passing the first bottom stream through a distillation column to obtain second overhead stream comprising residual hydrogen and non-aromatic hydrocarbons and second bottom stream comprising aromatic hydrocarbons, further recovering LPG from the second overhead stream, and recovering aromatic hydrocarbons from the second bottom stream.
9. The process according to claim 1, wherein the binder-free zeolite is ZSM-5, mordenite, beta zeolite, ZSM-5USY composite zeolite, ZSM-5beta composite zeolite, or ZSM-5ZSM-11 cocrystal zeolite.
10. The process according to claim 1, wherein the catalyst further comprises a promoter selected from the group consisting of Cu, Zn, Sn, Pb, Fe and mixture thereof in amount of less than 1 wt %.
11. The process according to claim 10, wherein the promoter is Zn.
12. The process according to claim 1, wherein the binder-free zeolite has a molar ratio SiO2Al2O3 in the range of 10-200.
13. The process according to claim 9, wherein the catalyst further comprises a promoter selected from the group consisting of Cu, Zn, Sn, Pb, Fe and mixture thereof in amount of less than 1 wt %.
14. The process according to claim 13, wherein the promoter is Zn.
15. The process according to claim 14, wherein the binder-free zeolite has a molar ratio SiO2Al2O3 in the range of 10-200.
16. The process according to claim 2 wherein the hydrocarbonaceous feedstock is introduced into the reaction zone at a weight hour space velocity of 1-4 hr\u22121 and a molar ratio of hydrogen to the hydrocarbonaceous feedstock ranges from 2:1 to 8:1.
17. The process according to claim 3 wherein in step (b), the reaction temperature is 300-500\xb0 C. and the reaction pressure is 2.0-4.0 MPa.
18. The process according to claim 6 wherein in step (b) the reaction temperature is 300-500\xb0 C. and the reaction pressure is 2.0-4.0 MPa.
19. The process according to claim 10 wherein the catalyst further comprises a promoter selected from Cu, Zn, Sn, Pb, Fe and mixture thereof in an amount of less than 0.6 wt % on the basis of the total weight of the catalyst.
20. The process according to claim 12 wherein the binder-free zeolite has a molar ratio SiO2Al2O3 in the range of 20-100.
21. The process according to claim 13, wherein the catalyst further comprises a promoter selected from Cu, Zn, Sn, Pb, Fe and mixture thereof in a amount less than 0.6% on the basis of the total weight the catalyst.
22. The process according to claim 15 wherein the binder-free zeolite has a molar ratio SiO2Al2O3 in the range of 20-100.
23. The process according to claim 1 wherein the amount of metallic Pt andor Pd is of 0.01-0.5 wt % on the basis of the total weight of the catalyst.