Evaporation device for multiple volatile substances
IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
H05B-003/02
F24F-006/08
출원번호
US-0918898
(2001-07-31)
우선권정보
EP-0107795 (2001-04-05)
발명자
/ 주소
Vieira, Pedro Queiroz
대리인 / 주소
McNair Law Firm, P.A.
인용정보
피인용 횟수 :
33인용 특허 :
5
초록▼
An evaporation device is disclosed for evaporating volatile substances such as insecticides and aromatics of a type having a housing containing a heating block with a heating element, a container for a volatile substance to be evaporated, a wick having a wick end protruding out of the container into
An evaporation device is disclosed for evaporating volatile substances such as insecticides and aromatics of a type having a housing containing a heating block with a heating element, a container for a volatile substance to be evaporated, a wick having a wick end protruding out of the container into a wick opening in the heating block, a switching device for the activation and deactivation of the heating device, and an adjusting device for the adjustment of the degree of evaporation. Preferably, two heating elements with different heating capacity are carried by the heating block. The heating elements are operatively connected to the switching device to adjust the heat output of the heating device and the degree of evaporation of the volatile substance.
대표청구항▼
An evaporation device is disclosed for evaporating volatile substances such as insecticides and aromatics of a type having a housing containing a heating block with a heating element, a container for a volatile substance to be evaporated, a wick having a wick end protruding out of the container into
An evaporation device is disclosed for evaporating volatile substances such as insecticides and aromatics of a type having a housing containing a heating block with a heating element, a container for a volatile substance to be evaporated, a wick having a wick end protruding out of the container into a wick opening in the heating block, a switching device for the activation and deactivation of the heating device, and an adjusting device for the adjustment of the degree of evaporation. Preferably, two heating elements with different heating capacity are carried by the heating block. The heating elements are operatively connected to the switching device to adjust the heat output of the heating device and the degree of evaporation of the volatile substance. two or more metals in oxidation state IV, has an SiO2/M2molar ratio of from greater than 100:1 to 40,000:1, and the reaction temperature is from 250 to 500° C. 2. A process as claimed in claim 1, wherein the reaction is carried out continuously. 3. A process as claimed in claim 1, wherein the reaction is carried out in the gas phase. 4. A process as claimed in claim 1, wherein the reaction is carried out in the presence of a solvent or diluent. 5. A process as claimed in claim 1, wherein the reaction is carried out in the presence of water or ammonia. 6. A process as claimed in claim 1, wherein the reaction is carried out in the presence of from 2 to 1200% by weight of water, based on EDA employed. 7. A process as claimed in claim 1, wherein the reaction is carried out in the presence of from 14 to 300% by weight of water, based on EDA employed. 8. A process as claimed in claim 1, wherein EDA and from 1 to 1000% by weight of piperazine (PIP), based on EDA, are reacted. 9. A process as claimed in claim 1, wherein EDA and from 7 to 250% by weight of piperazine (PIP), based on EDA, are reacted. 10. A process as claimed in claim 1, wherein EDA, from 8 to 250% by weight of PIP and from 23 to 300% by weight of water, in each case based on EDA, are reacted. 11. A process as claimed in claim 1, wherein PIP arising after the reaction is separated off and fed back into the reaction with EDA. 12. A process as claimed in claim 1, wherein the consumption of PIP in the overall balance is from 0 to 30 kg per 100 kg of TEDA. 13. A process as claimed in claim 1, wherein the reaction temperature is from 310 to 390° C. 14. A process as claimed in claim 1, wherein the absolute pressure is from 0.1 to 10 bar. 15. A process as claimed in claim 1, wherein the WHSV (weight hourly space velocity), based on the amines employed in the reaction, is from 0.05 to 6h-1. 16. A process as claimed in claim 1, wherein the zeolite catalyst, for M=Al, has an SiO2/M2O3molar ratio of from greater than 1400 to 40,000:1. 17. A process as claimed in claim 1, wherein the zeolite catalyst, for M=metal in oxidation state III or M=two or more metals in oxidation state III, has an SiO2/M2O3molar ratio of from greater than 100:1 to 5,000:1. 18. A process as claimed in claim 1, wherein the zeolite catalyst, for M=metal in oxidation state IV or M=two or more metals in oxidation state IV, has an SiO2/MO2molar ratio of from greater than 10:1 to 5,000:1. 19. A process as claimed in claim 1, wherein the zeolite catalyst is a pentasil zeolite. 20. A process as claimed in claim 1, wherein the metal M in oxidation state III is selected from the group consisting of Al, B, Fe, Co, Ni, V, Mo, Mn, As, Sb, Bi, La, Ga, In, Y, Sc and Cr, and mixtures thereof. 21. A process as claimed in claim 1, wherein the metal M in oxidation state IV is selected from the group consisting of Ti, Zr, Ge, Hf and Sn, and mixtures thereof. 22. A process as claimed in claim 1, wherein the zeolite catalyst is of the MFI or MEL structural type or mixed structures thereof (MEL/MFI or MFI/MEL). 23. A process as claimed in claim 1, wherein the zeolite catalyst exists or is employed at least partly in the H+and/or NH4+form under the reaction conditions if Al and/or other metals M are in oxidation state III in the zeolite. 24. A process as claimed in claim 1, wherein the zeolite catalyst is treated with a protic acid before use in the process. 25. A process as claimed in claim 1, wherein the zeolite catalyst has been doped with one or more transition metal selected from sub-groups I to VIII of the Periodic Table of the Elements. 26. A process as claimed in claim 1, wherein the zeolite catalyst comprises silicon dioxide as binder. 27. A process as claimed in claim 1, wherein a zeolite catalyst which has been treated or regenerated in a gas atmosphere in the pres
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