A vacuum cleaner having a reduced velocity chamber with a high velocity air inlet, an electric motor, a rotary blade driven by the motor to create a vacuum in the chamber, an outlet for exhausting air from the chamber, which air flows in a selected path from the air inlet, through the chamber and ou
A vacuum cleaner having a reduced velocity chamber with a high velocity air inlet, an electric motor, a rotary blade driven by the motor to create a vacuum in the chamber, an outlet for exhausting air from the chamber, which air flows in a selected path from the air inlet, through the chamber and out the air exhaust outlet and a disposable porous sheet filter layer in the chamber for removing large solid particles from the air.
대표청구항▼
A vacuum cleaner having a reduced velocity chamber with a high velocity air inlet, an electric motor, a rotary blade driven by the motor to create a vacuum in the chamber, an outlet for exhausting air from the chamber, which air flows in a selected path from the air inlet, through the chamber and ou
A vacuum cleaner having a reduced velocity chamber with a high velocity air inlet, an electric motor, a rotary blade driven by the motor to create a vacuum in the chamber, an outlet for exhausting air from the chamber, which air flows in a selected path from the air inlet, through the chamber and out the air exhaust outlet and a disposable porous sheet filter layer in the chamber for removing large solid particles from the air. 70° C. 3. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein the mixing proportion between the two brines varies between 6:1 and 1:6. 4. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein the mixing of the brines is done in a crystallizer, with a dwell time of the brine mixture of between 0.1 and 4 hours and at a temperature of between 0 and 100° C. 5. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein the first filtration and washing on the filter of step (f) is carried out with water or a solution of filtrate from the second filtration and washing of step (h), at a temperature of between 0 and 100° C. and with a volume ratio of from 0 to 100% relative to the volume of the monohydrated lithium sulfate crystals. 6. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein the monohydrated lithium sulfate crystals from the first filtration and washing of step (f) is re-pulped with water or a solution from the second filtration and washing of step (h), at a temperature of between 10 and 80° C., for a mean dwell time of between 2 and 60 minutes and a percentage of solid of 5-80% by weight. 7. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein during the second filtration and washing of step (h) the re-pulped crystals of monohydrated lithium sulfate are filtered and washed with water at a temperature of between 0 and 100° C. and at a volume ratio of 20-100% relative to the volume of the crystals. 8. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein drying is done with air or hot gas at between 120 and 500° C. 9. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein crystallization is carried out continuously in two crystallization stages, in the first of which stages carnallite is preferably crystallized at a temperature of between 0 and 60° C., with a mean dwell time of between 5 and 60 minutes, whereby the pulp from the first crystallizer is sent to a solid-liquid separation device in order to separate the crystallized solid and wherein the resulting brine is sent to a second crystallizer wherein the crystallization of the monohydrated lithium sulfate is accomplished at a temperature of between 0 and 60° C., with a mean dwell time of between 10 and 120 minutes, whereby the fines from the overflow from the second crystallizer are recovered in a sedimenter and whereby the discharge from said sedimenter and that from the second crystallizer containing the monohydrated lithium sulfate crystals are subject to filtration and washing, re-pulping and filtration and final washing, followed by drying thereof. 10. A process for producing monohydrated lithium sulfate from brines from natural salt deposits in accordance with claim 1, wherein crystallization is carried out continuously in two stages, in the first of which stages the brine which is high in magnesium and close to saturation with carnallite is sent to a first crystallizer where it is cooled to a temperature of between 0 and 30° C. in order to crystallize out carnallite, which is removed from the crystallizer, whereby the overflow from the crystallizer is sent to a heat exchanger in order to reheat the resulting brine to a temperature of between 10 and 80° C., whereby said brine is mixed with the brine that is saturated or nearly saturated with lithium sulfate and bischofite and is sent to a second crystallizer in order to crystalize out the monohydrated lithium sulfate, whereby the overflow from the second crystallizer sediments out in a sedimenter and the discharge from the sedimenter and from the second crystallizer containing the monohydrated lithium sulfate crystals is subject to filtration and washing, followed by re-pulping and filtration and final washing of the monohydrated lithium sulfate crystals, followed by the drying of said crystals, whereby the overflow from the sedimenter is sent for solar evaporation and concentrated brine from the evaporation is recycled to the process in order to increase the overall recovery of lithium from the brines. 11. The method in accordance with claim 4, wherein the dwell time is between 0.5 and 1 hr. 12. The method in accordance with claim 4, wherein the temperature is between 30 and 70° C. 13. The method in accordance with claim 5, wherein the temperature of the first stage of filtration and washing is between 0 and 50° C. 14. The method according to claim 5, wherein the volume ratio is between 20 and 50% by volume. 15. The method in accordance with claim 6, wherein the temperature is between 30 and 50° C. 16. The method in accordance with claim 6, wherein the mean dwell time is between 5 and 25 minutes. 17. The method in accordance with claim 6, wherein the percentage of solid is 50 to 70% by weight. 18. The method in accordance with claim 7, wherein the temperature is between 20 and 50° C. 19. The method in accordance with claim 7, wherein the volume ratio is 30 to 50% by volume. 20. The method in accordance with claim 8, wherein the drying is done at between 250 and 400° C. 21. The method in accordance with claim 9, wherein the carnallite is crystallized at a temperature between 5 and 30° C. 22. The method in accordance with claim 9, wherein the mean dwell time of the carnallite crystallization is between 10 and 30 minutes. 23. The method in accordance with claim 9, wherein the separation device is a filter. 24. The method in accordance with claim 9, wherein the monohydrated lithium sulfate is crystallized at a temperature between 5 and 30° C. 25. The method according to claim 9, wherein the mean dwell time of the crystallization of the monohydrated lithium sulfate is between 20 and 60 minutes. 26. The method in accordance with claim 10, wherein the brine in the first stage of crystallization is cooled in the first crystallizer to a temperature between 5 and 15° C. 27. The method in accordance with claim 10, wherein the temperature of reheating is between 20 and 40° C. n approximately 50/50 blend of N,N-dimethylcaprylamide and N,N-dimethylcapramide, and mixtures thereof; and heating the solution while in contact with the flame resistant fabric blend to a temperature below 82° C. 45. The method of claim 44, wherein the inherently flame resistant fibers are essentially composed of a material selected from the group consisting of aromatic polyamide, polyamide imide, polyimide, and mixtures thereof. 46. The method of claim 44, wherein the inherently flame resistant fibers are meta-aramid fibers. 47. The method of claim 44, wherein the cellulosic fibers are essentially composed of rayon, acetate, triacetate, lyocell, or mixtures thereof. 48. The method of claim 44, wherein the cellulosic fibers are rayon fibers. 49. The method of claim 44, wherein the dye-assistant is selected from the group consisting of N-cyclohexylpyrrolidone, benzyl alcohol, N,N-dibutylformamide, and mixtures thereof. 50. The method of claim 44, wherein the dye-assistant is one of N-cyclohexylpyrrolidone, benzyl alcohol, and N,N-dibutylformamide. 51. A method for dyeing a flame resistant fabric blend, comprising: contacting a flame resistant fabric blend comprising para-aramid fibers and cellulosic fibers that contain a flame retardant compound with a dyebath including at least one dye and a dye-assistant selected from the group consisting of N-cyclohexylpyrrolidone, benzyl alcohol, N,N-dibutylformamide, N,N-diethylbenzamide, hexadecyltrimethyl ammonium salt, N,N-dimethylbenzamide, N,N-diethyl-m-toluamide, N-octylpyrrolidone, aryl ether, an approximately 50/50 blend of N,N-dimethylcaprylamide and N,N-dimethylcapramide, and mixtures thereof; and heating the dyebath while in contact with the flame resistant fabric blend to a temperature that does not exceed 100° C. to fix the dye within the inherently flame resistant fibers. 52. The method of claim 51, wherein the cellulosic fibers are essentially composed of rayon, acetate, triacetate, lyocell, or mixtures thereof. 53. The method of claim 51, wherein the cellulosic fibers are rayon fibers. 54. The method of claim 51, wherein the dye-assistant is selected from the group consisting of N-cyclohexylpyrrolidone, benzyl alcohol, N,N-dibutylformamide, and mixtures thereof. 55. The method of claim 51, wherein the dye-assistant is N-cyclohexylpyrrolidone. 56. The method of claim 51, wherein the dye-assistant is benzyl alcohol. 57. The method of
연구과제 타임라인
LOADING...
LOADING...
LOADING...
LOADING...
LOADING...
이 특허에 인용된 특허 (73)
Nolen ; Jr. Edward F. (Memphis TN), Adjustable air filter.
Pick William (Highway 15 ; R.R. #1 Carleton Place ; Ontario CAX K7C 3P1), Charging element having odor and gas absorbing properties for an electrostatic air filter.
Cambo William H. (Rollinsford NH) Whitely Elliott F. (Acton ME) Bond Leroy E. (Rochester NH), Composite having improved transverse structural integrity and flexibility for use in high temperature environments.
Sundet Douglas C. (St. Paul MN) Fox Albert H. (St. Paul MN), Filtration media comprising non-charged meltblown fibers and electrically charged staple fibers.
※ AI-Helper는 부적절한 답변을 할 수 있습니다.