1. A catalytic conversion process for increasing the cetane barrel of diesel, wherein the process comprises contacting the feedstock oil with a catalyst having a relatively homogeneous activity containing mainly the large pore zeolites in a catalytic conversion reactor, wherein the reaction temperature, residence time of oil vapors and weight ratio of the catalystfeedstock oil are sufficient to obtain a reaction product containing a diesel, and from about 12 to about 60% by weight of a fluid catalytic cracking gas oil relative to the weight of the feedstock oil; the reaction temperature ranges from about 420\xb0 C. to about 550\xb0 C.; the residence time of oil vapors ranges from about 0.1 to about 5 seconds; the weight ratio of the catalystfeedstock oil is about 1 to about 10.
2. The process according to claim 1, further comprising:
introducing all or a part of the fluid catalytic cracking gas oil into a conventional catalytic cracking reactor or a riser with variable diameters to further produce a product comprising diesel and gasoline, orand introducing the fluid catalytic cracking gas oil back to the initial catalytic conversion reactor or feeding it into another catalytic conversion reactor.
3. The process according to claim 1, wherein all or a part of the fluid catalytic cracking gas oil is introduced into a hydrocracking unit for the further production of diesel having high cetane number.
4. The process according to claim 1, wherein all or a part of the fluid catalytic cracking gas oil is introduced into the hydrotreating unit to produce a product comprising diesel and gasoline.
5. The process according to claim 3, wherein the hydrocracked tail oil is introduced into a conventional catalytic cracking reactor or a riser with variable diameters to further produce a product comprising diesel and gasoline.
6. The process according to claim 4, wherein all or a part of the hydrotreated fluid catalytic cracking gas oil is introduced into a conventional catalytic cracking reactor or a riser with variable diameters to further produce a product comprising diesel and gasoline, orand is introduced back to the catalytic conversion reactor.
7. The process according to claim 1, wherein the feedstock oil is selected from or comprises petroleum hydrocarbons andor other mineral oils, wherein petroleum hydrocarbons are selected from one or more of vacuum gas oil, atmospheric gas oil, coker gas oil, deasphalted oil, vacuum residue and atmospheric residue or combinations thereof; other mineral oils are selected from one or more of coal liquefied oil, oil sand oil and shale oil, or combinations thereof.
8. The process according to claim 1, wherein the catalyst comprises zeolites, inorganic oxides and clays respectively in an amount of from about 5 to about 35 wt %, preferably about 10 to about 30 wt % of the zeolites; from about 0.5 to about 50 wt % of the inorganic oxides; and from 0 to about 70 wt % of the clays, relative to the total weight of the catalyst on a dry basis, wherein the zeolite as the active component is selected from large pore zeolites which are selected from one or more of rare earth Y, rare earth H\u2014Y, ultra-stable Y obtained by various methods, and high-silica Y.
9. The process according to claim 1, wherein the particle size distribution of the catalyst is the particle size distribution of the conventional catalytic cracking catalyst or a coarse particle size distribution.
10. The process according to claim 9, wherein the catalyst having a coarse particle size distribution comprises less than about 10 vol. %, preferably less than about 5 vol. % of the particles having a particle size of less than 40 \u03bcm relative to the volume of all the particles; less than about 15 vol. %, preferably less than about 10 vol. % of the particles having a particle size of greater than 80 \u03bcm relative to the volume of all the particles, and the remaining being the particles having a particle size of from about 40 to about 80 \u03bcm.
11. The process according to claim 1, wherein the catalytic conversion reactor is one or more selected from the group consisting of a riser, a fluidized bed with an equal linear velocity, a fluidized bed with an equal diameter, an upstream conveyor line and a downstream conveyor line or combinations thereof, or combinations of two or more same reactors, wherein the combinations comprises combinations in series orand parallel; the riser is a conventional one with an equal diameter or one with various variable diameters.
12. The process according to claim 1, wherein the feedstock oil is fed into the catalytic conversion reactor at one position, or at more than one positions at the same or different heights.
13. The process according to claim 1, wherein the temperature of the catalytic conversion ranges from about 430\xb0 C. to about 500\xb0 C., preferably from about 430\xb0 C. to about 480\xb0 C.; the residence time of oil vapors ranges from about 0.5 to about 4 seconds, preferably from about 0.8 to about 3 seconds; the weight ratio of catalystfeedstock oil is from about 2 to about 8, preferably from about 3 to about 6; and the reaction pressure ranges from about 0.10 MPa to about 1.0 MPa, preferably from about 0.15 MPa to about 0.6 MPa.
14. The process according to claim 1, wherein the fluid catalytic cracking gas oil is a fraction having an initial boiling point of not less than 350\xb0 C. and a hydrogen content of not less than 11.5 wt %; preferably not less than 12.0 wt %.
15. The process according to claim 1, wherein the catalyst having a relatively homogeneous activity for the catalytic conversion has an initial activity of not higher than about 80, preferably not higher than about 75, more preferably not higher than about 70, a self-balancing time ranging from about 0.1 h to about 50 h, preferably from about 0.2 h to about 30 h, more preferably from about 0.5 h to about 10 h, and an equilibrium activity ranging from about 35 to about 60, preferably from about 40 to about 55.
16. The process according to claim 1, wherein the catalyst for catalytic conversion in the catalytic conversion reactor is obtainable by the following processing method:
(1) loading a fresh catalyst into a fluidized bed, preferably a dense phase fluidized bed, contacting with water vapor, ageing under a certain hydrothermal circumstance to obtain a catalyst having a relatively homogeneous activity; and
(2) loading the catalyst having a relatively homogeneous activity into the corresponding reaction unit; and
wherein the certain hydrothermal circumstance comprises: the ageing temperature ranges from about 400\xb0 C. to about 850\xb0 C., preferably from about 500\xb0 C. to about 750\xb0 C., more preferably from about 600\xb0 C. to about 700\xb0 C., the superficial linear velocity of the fluidized bed ranges from about 0.1 to about 0.6 ms, preferably from about 0.15 to about 0.5 ms, the ageing time ranges from about 1 h to about 720 h, preferably from about 5 h to about 360 h.
17. The process according to claim 1, wherein the catalyst for catalytic conversion in the catalytic conversion reactor is obtainable by the following processing method:
(1) loading a fresh catalyst into the fluidized bed, preferably a dense phase fluidized bed, contacting with an ageing medium containing water vapor, ageing under a certain hydrothermal circumstance to obtain a catalyst having a relatively homogeneous activity;
(2) loading the catalyst having a relatively homogeneous activity into the corresponding reaction unit; and
wherein the certain hydrothermal circumstance comprises: the ageing temperature ranges from about 400\xb0 C. to about 850\xb0 C., preferably from about 500\xb0 C. to about 750\xb0 C., more preferably from about 600\xb0 C. to about 700\xb0 C.; the superficial linear velocity of the fluidized bed ranging from about 0.1 to about 0.6 ms, preferably from about 0.15 to about 0.5 ms; the weight ratio of water vapor to the ageing medium ranging from about 0.20 to about 0.9, preferably from about 0.40 to about 0.60; and the ageing time ranging from about 1 to about 720 h, preferably from about 5 to about 360 h.
18. The process according to claim 1, wherein the catalyst for catalytic conversion in the catalytic conversion reactor is obtainable by the following processing method:
(1) loading a fresh catalyst into a fluidized bed, preferably a dense phase fluidized bed, feeding the hot regenerated catalyst in the regenerator into the fluidized bed, and conducting heat exchanging in the fluidized bed;
(2) contacting the heat exchanged fresh catalyst with water vapor or the ageing medium containing water vapor, ageing under a certain hydrothermal circumstance to obtain a catalyst having a relatively homogeneous activity; and
(3) loading the catalyst having a relatively homogeneous activity into the corresponding reaction unit,
wherein the certain hydrothermal circumstance comprises: the ageing temperature ranging from about 400\xb0 C. to about 850\xb0 C., preferably from about 500\xb0 C. to about 750\xb0 C., more preferably from about 600\xb0 C. to about 700\xb0 C.; the superficial linear velocity of the fluidized bed ranging from about 0.1 to about 0.6 ms, preferably from about 0.15 to about 0.5 ms; the ageing time ranging from about 1 to about 720 h, preferably from about 5 to about 360 h; and the weight ratio of water vapor to the ageing medium (if any) ranging from greater than about 0 to about 4, preferably ranging from about 0.5 to about 1.5.
19. The process according to claim 4, wherein the hydrotreating is conducted under the conditions of a hydrogen partial pressure of from about 3.0 to about 20.0 MPa, a reaction temperature of from about 300\xb0 C. to about 450\xb0 C., a volume hourly space velocity of about 0.1 to about 3 h\u22121, and a hydrogenoil ratio of from about 300 to about 2000 vv.
20. The process according to claim 4, wherein the hydrotreating catalyst comprises a support and molybdenum andor tungsten and nickel andor cobalt supported thereon; the support consists of alumina and a zeolite, with a weight ratio of the alumina to the zeolite ranging from about 90:10 to about 50:50; the alumina is compounded by small pore alumina and large pore alumina in a weight ratio ranging from about 75:25 to about 50:50, wherein the small pore alumina comprises about 95% or more by volume of pores with a diameter less than about 80 angstroms based on the total volume of the pores, and the large pore alumina comprises about 70% or more by volume of pores with a diameter of about 60 to about 600 angstroms based on the total volume of the pores.
21. The process according to claim 20, wherein the hydrotreating catalyst comprises, in terms of oxides and based on the total weight of the catalyst, molybdenum andor tungsten in an amount of about 10 to about 35 wt %; and nickel andor cobalt in an amount of about 1 to about 15 wt %.
22. The process according to claim 20, wherein the weight ratio of the alumina to the zeolite ranges from about 90:10 to about 60:40.
23. The process according to claim 20, wherein the zeolite is a Y-type zeolite.
24. The process according to claim 2, wherein the fluid catalytic cracking gas oil is subjected to cracking reaction in another conversion reactor, the oil vapors produced are subjected to hydrogen transfer reaction and isomerization reaction under certain reaction ambient, and a reaction product comprising low olefin gasoline is obtained through separation.
25. The process according to claim 24, wherein the reaction conditions of the cracking reaction comprise: a reaction temperature ranging from about 480\xb0 C. to about 600\xb0 C., preferably from about 485 to about 580\xb0 C.; a reaction time ranging from about 0.1 to about 3 seconds, preferably about 0.5 to about 2 seconds; a ratio by weight of the conversion catalyst to the fluid catalytic cracking gas oil ranging from about 0.5 to about 25:1, preferably about 1 to about 15:1; a ratio by weight of the prelifting medium to the fluid catalytic cracking gas oil ranging from about 0.01 to about 2:1, preferably about 0.05 to about 1:1.
26. The process according to claim 24, wherein the reaction conditions of the hydrogen transfer reaction and isomerization reaction comprise: a reaction temperature ranging from about 450\xb0 C. to about 550\xb0 C., preferably about 460\xb0 C. to about 530\xb0 C.; a weight hourly space velocity in the second reaction zone ranging from about 1 to about 50 hour\u22121, preferably about 1 to about 40 hour\u22121.
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. An undergarment comprising
a single unit of wearable fabric whereon three closure systems each having a male part and female counterpart are sewn to the inner surface thereof;
said unit is formed from two identical panels of continuous fabric sewn together thereafter forming a seam in the middle of said inner surface approximately 12\u2033 in length;
said unit contains a main body portion and identically long left and right extending leg segments;
said body portion is reinforced with 2\u2033 high waistband sewn at the top thereof;
said fabric is measured and cut so that when the undergarment is formed it fits the contour of the of the legs, waist, buttocks, and hips;
said closure systems are one short set and two identically longer sets;
whereby each said set contains a said male part and said female counterpart;
said body portion has a continuous right side and left side;
whereupon a said male part and said female counterpart are separated and sewn respectively to the said right side and said left side of the said body portion;
said left and right extending leg segments each have a right side and left side;
whereupon a said male part and said female counterpart are separated and sewn respectively to the said right side and said left side of the said left extending leg segment;
whereupon a said male part and said female counterpart are separated and sewn respectively to the said right side and said left side of the said right extending leg segment;
said undergarment envelops the hips, buttocks, waist, and lower abdomen after both said sides of said body portion are wrapped around the waist and thereafter the said closure system fastened perpendicularly to the navel;
wherein said left and right extending leg segments dangle around the respective legs;
said undergarment envelops the left leg after both said sides of the said left extending leg segment are wrapped around the leg and thereafter the said closure system fastened along the inner left leg;
said undergarment envelops the right leg after both said sides of the said right extending leg segment are wrapped around the leg and thereafter the said closure system fastened along the inner right leg;
said undergarment is naturally void of said fabric around the groin after all three closure systems have been fastened;
said undergarment has a said inside surface and an outside surface whereby the inside surface is in contact with flesh;
said male and female parts of said closure systems protrude just beyond said sides of said undergarment so to fasten the said closure systems from the said outside surface;
said backs of said male and female parts of said closure systems are covered by fabric on the said inside surface so to not contact the flesh.
2. An undergarment in which the said closure systems as defined in claim 1 are zippers
whereby the said male parts of said closure system contain a slider to connect the teeth of said male and female parts.
3. An undergarment in which the said closure systems as defined in claim 1 are pile-type fasteners
whereby said male parts of said closure systems are sewn on the said outside surface so to overlap with its female counterpart.
4. An undergarment in which the said closure systems as defined in claim 1 are snaps
whereby the said male parts of said closure systems protrude through said inside surface of said undergarment;
whereby the said female counterparts of said closure systems protrude through the said outside surface of said undergarment.