CN1117959A - Etherification reaction process and equipment for light hydrocarbon and fatty alcohol - Google Patents
Etherification reaction process and equipment for light hydrocarbon and fatty alcohol Download PDFInfo
- Publication number
- CN1117959A CN1117959A CN94110775A CN94110775A CN1117959A CN 1117959 A CN1117959 A CN 1117959A CN 94110775 A CN94110775 A CN 94110775A CN 94110775 A CN94110775 A CN 94110775A CN 1117959 A CN1117959 A CN 1117959A
- Authority
- CN
- China
- Prior art keywords
- reaction
- ether
- zone
- methyl
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000006266 etherification reaction Methods 0.000 title claims abstract description 21
- 150000002191 fatty alcohols Chemical class 0.000 title claims abstract description 8
- 238000000034 method Methods 0.000 title claims abstract description 8
- 229930195733 hydrocarbon Natural products 0.000 title claims description 18
- 150000002430 hydrocarbons Chemical class 0.000 title claims description 18
- 239000004215 Carbon black (E152) Substances 0.000 title claims description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 41
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000004821 distillation Methods 0.000 claims abstract description 17
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 150000001993 dienes Chemical class 0.000 claims abstract description 8
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 36
- 239000000463 material Substances 0.000 claims description 32
- 239000012808 vapor phase Substances 0.000 claims description 17
- 239000003054 catalyst Substances 0.000 claims description 13
- 238000006555 catalytic reaction Methods 0.000 claims description 13
- 239000007791 liquid phase Substances 0.000 claims description 13
- 238000005194 fractionation Methods 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 10
- HVZJRWJGKQPSFL-UHFFFAOYSA-N tert-Amyl methyl ether Chemical compound CCC(C)(C)OC HVZJRWJGKQPSFL-UHFFFAOYSA-N 0.000 claims description 10
- 150000001336 alkenes Chemical group 0.000 claims description 9
- 238000000066 reactive distillation Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 7
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 7
- 239000002994 raw material Substances 0.000 claims description 7
- 238000009834 vaporization Methods 0.000 claims description 6
- 230000008016 vaporization Effects 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 5
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 claims description 4
- 125000000217 alkyl group Chemical group 0.000 claims description 4
- 239000012071 phase Substances 0.000 claims description 4
- 239000000376 reactant Substances 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 3
- 230000005540 biological transmission Effects 0.000 claims description 3
- BUWXUSLQPDDDSD-UHFFFAOYSA-N 2-methyl-2-(2-methylbutan-2-yloxy)butane Chemical compound CCC(C)(C)OC(C)(C)CC BUWXUSLQPDDDSD-UHFFFAOYSA-N 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- -1 ether compound Chemical class 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims 6
- 239000007789 gas Substances 0.000 claims 4
- 241000282326 Felis catus Species 0.000 claims 3
- 150000001298 alcohols Chemical class 0.000 claims 2
- 239000011229 interlayer Substances 0.000 claims 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 claims 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical group COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims 1
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical class CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims 1
- AQEFLFZSWDEAIP-UHFFFAOYSA-N di-tert-butyl ether Chemical compound CC(C)(C)OC(C)(C)C AQEFLFZSWDEAIP-UHFFFAOYSA-N 0.000 claims 1
- 150000002170 ethers Chemical class 0.000 claims 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 claims 1
- 239000007792 gaseous phase Substances 0.000 claims 1
- 239000008187 granular material Substances 0.000 claims 1
- 229920006395 saturated elastomer Polymers 0.000 claims 1
- 238000004508 fractional distillation Methods 0.000 abstract 1
- MHNNAWXXUZQSNM-UHFFFAOYSA-N 2-methylbut-1-ene Chemical compound CCC(C)=C MHNNAWXXUZQSNM-UHFFFAOYSA-N 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 230000009466 transformation Effects 0.000 description 6
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical compound CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 description 5
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 4
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 4
- JMMZCWZIJXAGKW-UHFFFAOYSA-N 2-methylpent-2-ene Chemical compound CCC=C(C)C JMMZCWZIJXAGKW-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- WWUVJRULCWHUSA-UHFFFAOYSA-N 2-methyl-1-pentene Chemical compound CCCC(C)=C WWUVJRULCWHUSA-UHFFFAOYSA-N 0.000 description 2
- RRHGJUQNOFWUDK-UHFFFAOYSA-N Isoprene Chemical compound CC(=C)C=C RRHGJUQNOFWUDK-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- ZSWFCLXCOIISFI-UHFFFAOYSA-N cyclopentadiene Chemical compound C1C=CC=C1 ZSWFCLXCOIISFI-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- PMJHHCWVYXUKFD-SNAWJCMRSA-N (E)-1,3-pentadiene Chemical compound C\C=C\C=C PMJHHCWVYXUKFD-SNAWJCMRSA-N 0.000 description 1
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- WYLQOLGJMFRRLX-UHFFFAOYSA-N 2-methoxy-2-methylpentane Chemical compound CCCC(C)(C)OC WYLQOLGJMFRRLX-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 239000003729 cation exchange resin Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000012451 post-reaction mixture Substances 0.000 description 1
- CGFYHILWFSGVJS-UHFFFAOYSA-N silicic acid;trioxotungsten Chemical compound O[Si](O)(O)O.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1.O=[W]1(=O)O[W](=O)(=O)O[W](=O)(=O)O1 CGFYHILWFSGVJS-UHFFFAOYSA-N 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A process and apparatus for preparing ether by reaction distillation features that the catalytic distillation equipment is used to perform selective hydrogenation to remove diolefin, the etherification reaction of tert-olefin and fatty alcohol and the separation of product, the reaction distillation tower is divided into three segments, the middle one contains two mixed-phase reaction regions and one catalytic distillation region, and two middle fractional distillation regions are arranged in said reaction regions.
Description
The present invention relates to a kind of new preparation method of alkyl oxide, especially a kind of catalytic distillation method and the equipment that in the etherification reaction that contains tertiary olefin class and ester fat alcohol, uses.
People are known under the effect of covering unsticking soil, silicotungstic acid, storng-acid cation exchange resin or molecular sieve catalyst, produce alkyl oxide by hydrocarbon polymer that contains tertiary olefin and Fatty Alcohol(C12-C14 and C12-C18) reaction.Traditional mode adopts fixed-bed reactor, reacts under liquid phase state, in order to take out reaction heat.Adopt the inner array tubular reactors or respond material outer circulation refrigerative cartridge reactor (USP.4.198.530) and expanded bed reactor (Fr.2455019.Fr.2440931) owing to react the restriction that is subjected to equilibrium conversion, in order to improve transformation efficiency, adopt reaction and--separate--reaction again--separation processes long flow path again, facility investment is big, the energy consumption height; Succeeding in developing of catalytic distillation technology.Make reaction and be separated in the same equipment and carry out simultaneously.Simplified technical process.Because resultant constantly shifts out reaction zone, destroyed the balance of reaction, also improved transformation efficiency, (USP4.439.3507).But catalyst loading structure more complicated in the tower; In order to guarantee the transformation efficiency of reactant, the height of catalytic distillation tower is invested also bigger also than higher.
The objective of the invention is to simplify the catalyst loading structure of reactive distillation column, reduce production costs, reduce energy consumption, reduce the tower height degree, reduce investment, improve the transformation efficiency of reactant.
For achieving the above object, design of the present invention is to adopt novel catalytic distillation method and equipment:
The feature of reactive distillation column of the present invention is to have comprised two mixed phase catalysis reaction districts and a reactive distillation zone in the conversion zone; In reaction zone, be provided with two middle fractionation zones.Reactant is selected diolefin in the hydrogenation and removing raw material at first catalytic reaction zone, and carries out the etherification reaction of tertiary olefin and Fatty Alcohol(C12-C14 and C12-C18); After in middle fractionation zone, removing the ether that in first etherification reaction zone, generates, enter in second catalytic reaction zone and proceed etherification reaction; After removing the ether of second catalytic reaction zone generation, material enters reactive distillation zone, carries out simultaneously at this etherification reaction and product separation, meets the requirements of transformation efficiency.
Now in conjunction with the accompanying drawings reactive distillation technology of the present invention is elaborated: we do as a whole narration the (also can make a tower) with tower A and B.Reactive distillation column is divided into three parts: top is conventional stripping stage [7] for conventional rectifying section [26] bottom, and the feature of middle part conversion zone comprises: the catalytic distillation zone IIc on catalytic reaction zone Ia (4), middle fractionation zone Ib (3), catalytic reaction zone IIa (15), middle fractionation zone IIb (21) and its top.Be respectively equipped with beds (4a.4b.4c and 15) and at least 1 liquid channel (5.16) among the catalytic reaction zone Ia.IIa.Article at least 1, vapor phase channel (6.17) is equipped with among the bed Ia and selects hydrogenation catalyst and catalyst for etherification, also can be that the catalyst for etherification of selecting hydrogenating function is arranged.In IIa (15) bed catalyst for etherification is housed.Among the middle fractionation zone Ib.IIb respectively is the plate or the filler of at least one routine; Be provided with at least two beds (22.23) among the catalytic distillation zone IIc, and establish at least one plate (25) and at least one vapor phase channel (24) between bed.
The hydrocarbon polymer that contains tertiary olefin mixes through pipeline (1) by a certain percentage with hydrogen, methyl alcohol, and preheater (2) enters reaction zone Ia top, and passes beds (4a.4b.4c), at first selects the diolefin in the hydrogenation and removing raw material, alkynes; Carry out etherification reaction then, emit reaction heat, when temperature was elevated to the bubble point of reaction mass under the working pressure, partial reaction material vaporization absorption reaction heat made temperature-stable; Reaction back mixture flow is to stripping stage [7]; After [7] vapor-phase material that rises and vapor-phase material mixing of reacting generation, disengaging zone Ib (3) in vapor phase channel (6) enters; Liquid phase material under separating flows to the top of stripping stage [7] through liquid channel (5).Vapor-phase material after the separation enters interchanger (13) through pipeline (12), after heat exchange liquefaction, enter catalytic reaction zone IIa (15) by pipeline (14), carry out etherification reaction, partial reaction material vaporization absorption reaction heat, the post reaction mixture materials flow is to the B tower bottom; Vapor-phase material is separation area II b (21) in vapor phase channel (17) flows to; Liquid phase material under separating flows to the B tower bottom through liquid channel (16); Flow out through pipeline (17a).A part is the heat exchange vaporization in interchanger (13), the bottom of separation area II b in pipeline (18) enters; Another part enters the top of disengaging zone Ib in the A tower through pipeline (19.20).Vapor-phase material after separating from IIb is through vapor phase channel (24) beds of having mercy on, and passes and carry out the caloic exchange on column plate (25), and vapor-phase material enters rectifying section (26); Liquid phase material under separating flows downward, and passes the beds (23) of IIc, carries out etherification reaction; Liquid phase material is gone up and vapor-phase material carries out the caloic transmission at separation tray (25).Liquid phase material after stripping stage (7) separates flows to the A tower bottom and flows out through pipeline (8), and a part is in reboiler (9) vaporization, at the bottom of pipeline (10) returns the A tower; Another part goes out device through pipeline (11), i.e. the ether compound product.Vapor-phase material after rectifying section (26) separates after pipeline (27) enters condenser (28) condensation, enters return tank (29), and one one is back to the B top of tower through pipeline (30); Another part enters downstream unit through pipeline (31).
Effect of the present invention has reached the purpose of invention, because the progress of equipment and technology adopts repeatedly Reaction Separation to destroy the balance of reaction, transformation efficiency is improved; Catalyzer in bulk makes filling structure simple, reduces running cost, and the tower total height decreases than existing catalysis-distillation equipment.The investment of catalysis-distillation equipment is saved.
By means of embodiment effect of the present invention is described below;
Embodiment 1.
Iso-butylene and methyl alcohol reaction that the present invention is used for mixed c 4 generate methyl tertiary butyl ether.Iso-butylene in the material carbon four is 36.5% (M/M), butadiene content is that 1.0% (M/M) is according to technology of the present invention, be respectively 0.7mPa (A tower) and 0.6mPa (B tower) at pressure, reflux ratio 1.0, alfin ratio 1.05 (mol/mol), temperature are 25--140 ℃, and conversion for isobutene is 99.%, content≤the 20PPM of divinyl, the purity of methyl tertiary butyl ether is 98%.
The tertiary olefin (2 monomethyl butene-1s and 2 monomethyl butene-2s) that the present invention is used for the catalyzed carbon 5 distillate generates tert amyl methyl ether(TAME) with the methyl alcohol reaction.2-methyl butene-1 is 7.59% in the material carbon 5 distillate, and 2-methyl butene-2 is 15.52%, and diolefin (isoprene, cyclopentadiene is along pentadiene) is 1.2%; According to technology of the present invention, at pressure is 0.4MPa (A tower) and 0.3MPa (B tower), alfin ratio is 1.05 (MOL/MOL), reflux ratio 1.0, temperature is 25--140 ℃, and 2-methyl butene-1 has 99% to be converted into tert amyl methyl ether(TAME), and 2-methyl butene-2 has 95% to be converted into tert amyl methyl ether(TAME), the content of diolefin is reduced to below the 100PPM, and the purity of tert amyl methyl ether(TAME) is 98%.
Embodiment 3.
The present invention is used for tertiary olefin (the 2-methyl butene-1 of catalyzed carbon 5 distillate and carbon six fractions, 2-methyl butene-2, a 2.3 neohexene-1,2-methylpentene-1,2-methylpentene-2, suitable-3-methylpentene-2 and anti--3-methylpentene-2) produce methyl alcohol tert-amyl ether and methyl alcohol uncle Buckie ether with the methyl alcohol reaction, 2-methyl butene-1 is 3.80% in the raw material, 2-methyl butene-2 is that 7.76%, 2.3-neohexene-1 is 0.26%, and 2-methylpentene-1 is 1.55%, 2-methylpentene-2 is 2.46%, suitable-3-methylpentene-2 is 2.38%, anti--3-methylpentene-2 is 2.18%, diolefin content is 1.52%; According to technology of the present invention, be respectively 0.2MPa (A tower) and 1.0mPa (B tower) at pressure, reflux ratio 1.0, alfin ratio is 1.05 (moP/moP), temperature is 25--140 ℃, 2-methyl butene-1 has 99.% to be converted into tert amyl methyl ether(TAME), and 2-methyl butene-2 has 94% to be converted into tert amyl methyl ether(TAME); 2-methylpentene-1,2-methylpentene-2, anti--3-methylpentene-2 and suitable-3-methylpentene-2 have 99% respectively, 77%, 65% and 38% is converted into methyl-tert Buckie ether, and diolefin content is reduced to 150PPM, and 60% tert amyl methyl ether(TAME) and 38% methyl-tert hexyl ether are arranged in the product.
Claims (5)
1. the preparation method of an alkyl oxide is mixed by a certain percentage by lighter hydrocarbons that contain tertiary olefin and Fatty Alcohol(C12-C14 and C12-C18), gives heat to certain temperature, carries out etherification reaction under catalyst action, and this etherification reaction and product separation carry out in catalytic distillation tower simultaneously, it is characterized in that:
A. adopt catalysis-distillation equipment of the present invention,
B. give heat and in catalytic reaction zone Ia, under catalyst action, select hydrogenation and removing diolefin and etherification reaction, flow to stripping stage under directly to the reaction raw materials of certain temperature,
C. the product and the unreacted raw material that in middle fractionation zone Ib, separate etherificate through the vapor-phase material at vapor phase channel upper reaches.
D. the unreacted material of behind Ib, separating through interchanger [13] with from the liquid phase material heat exchange of [17], enter catalytic reaction zone IIa after the liquefaction, proceed etherification reaction,
E. fractionation zone IIb product separation and unreacted material during reaction mass flows on the gas phase channel [17] of IIa,
F. enter catalytic distillation zone IIc on the tower tray of catalyst bed interlayer in the upper reaches through the unreacted material behind the IIb again through vapor phase channel [24], carry out the caloic transmission,
G. the unreacted gaseous phase materials from IIc flows out from cat head after distilling period [26] separates, and a part refluxes after condensation, and a part goes out device,
H. the liquid phase material from rectifying section [26] directly enters reactive distillation zone IIc, on the tower tray of catalyst bed interlayer, carry out the caloic transmission, and flow downward and pass beds and carry out etherification reaction simultaneously, liquid phase material through reactive distillation zone IIc separates in middle fractionation zone IIb, liquid phase material after the separation is through [17] pipeline, and a part is advanced vaporization in the heat exchanger [13].The bottom of fractionation zone IIb in pipeline [18] enters, another part is the top of fractionation zone Ib in pipe [19.20] enters, and the liquid phase material of separating through Ib enters the top of stripping stage through the liquid channel of Ia.
L. flow out through pipeline [8] through the isolating liquid phase material of stripping stage, one one at the bottom of turning back to tower after reboiler [9] vaporization, another part goes out device through [11] pipe, is product ether.
J. when granules of catalyst bigger, or voidage also can not establish vapor phase channel and liquid channel in the reaction bed when big, the gas-liquid phase materials can convection current passes bed.
2. by the described method of claim 1, it is characterized in that: described light hydrocarbon etherifying reaction is meant that lighter hydrocarbons and alcohols generate the reaction of ether under catalyst action.Lighter hydrocarbons are meant the alkene of C3 to C7, and alcohols is meant Fatty Alcohol(C12-C14 and C12-C18) such as methyl alcohol, propyl alcohol, butanols.The ether compound of looks correspondence thus is as methyl tertiary butyl ether, tert amyl methyl ether(TAME), ethyl uncle Ding Quan ether, methyl sec-butyl ether, methyl-tert ethyl ether etc.
Above-mentioned lighter hydrocarbons can be same carbon number hydro carbons.It also can be two or more hydrocarbon mixture, the ethers that generates can be the ether with carbon number, also can be the ether of different carbon numbers, carry out etherification reaction as mixed olefins and methyl alcohol with C4, C5, C6, can obtain methyl tertiary butyl ether simultaneously, the mixed ether of the basic ether of tert amyl methyl ether(TAME) and methyl-tert.
3. by the described method of claim 1, it is characterized in that: the temperature control of light hydrocarbon etherifying reaction is to be foundation to satisfy the etherification reaction requirement, reaction system difference, temperature of reaction is also different, and generally between 25--200 ℃, working pressure is that reactant ties up to the saturated vapor pressure under the temperature of reaction.
4. by the described method of claim 1, it is characterized in that the reaction of described lighter hydrocarbons ether, if raw material is the hydrocarbon (as the C5 hydrocarbon mixture) of single carbon number, used alcohol is methyl alcohol, can obtain purity like this at the bottom of the tower greater than 98% tert amyl methyl ether(TAME), cat head will obtain reaction residue C5 and a small amount of azeotropic is formed methyl alcohol.If raw material is the hydrocarbon (as the hydrocarbon mixture of C4 and C5) of two kinds of carbon numbers, used alcohol is methyl alcohol, can obtain the formaldehyde tertbutyl ether at the bottom of the tower like this, and the mixture that formaldehyde tert-amyl ether and residue C5 form, cat head must react the methyl alcohol that residue C4 and a small amount of azeotropic are formed,
5. produce the equipment of alkyl oxide by lighter hydrocarbons and Fatty Alcohol(C12-C14 and C12-C18) for one kind, adopt catalytic distillation tower to carry out catalyzed reaction and separate, tower divides three sections of upper, middle and lowers, and top is rectifying section, and the bottom is a stripping stage, and the middle part is a conversion zone, it is characterized in that:
A. Zhong Bu conversion zone comprises catalytic reaction zone Ia, and the middle fractionation zone Ib on top, and again top/or at the catalytic reaction zone IIa of another tower bottom and up middle fractionation zone IIb successively, catalytic distillation zone IIc,
B.Ia comprises two above catalytic bed [4a.4b.4c],
C.Ia is provided with/or do not establish (when catalyzer macrobead or space are big) at least 1 gas phase channel [6] and at least 1 liquid channel [5],
D. as gas, during liquid channel, a closure plate of shutting is arranged at the top of beds [4] and [15],
E.IIb is an at least one plate,
F.IIc is at least two beds, and at least one plate between bed is provided with at least one gas phase channel in the beds.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94110775A CN1044805C (en) | 1994-08-30 | 1994-08-30 | Etherification reaction technology and equipment for light hydrocarbon and aliphatic alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN94110775A CN1044805C (en) | 1994-08-30 | 1994-08-30 | Etherification reaction technology and equipment for light hydrocarbon and aliphatic alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1117959A true CN1117959A (en) | 1996-03-06 |
| CN1044805C CN1044805C (en) | 1999-08-25 |
Family
ID=5034705
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN94110775A Expired - Fee Related CN1044805C (en) | 1994-08-30 | 1994-08-30 | Etherification reaction technology and equipment for light hydrocarbon and aliphatic alcohol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1044805C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1085648C (en) * | 1997-05-07 | 2002-05-29 | 中国石化齐鲁石油化工公司 | Light hydrocarbon etherifying technology |
| CN109173310A (en) * | 2018-08-29 | 2019-01-11 | 张家港市科华化工装备制造有限公司 | Dimethoxym ethane rectifying column |
| CN109651063A (en) * | 2017-10-10 | 2019-04-19 | 中国石油化工股份有限公司 | The preparation method of iso-amylene |
| CN109651057A (en) * | 2017-10-10 | 2019-04-19 | 中国石油化工股份有限公司 | The method for preparing iso-amylene |
| CN114011341A (en) * | 2021-11-15 | 2022-02-08 | 丹东明珠特种树脂有限公司 | Catalytic distillation tower and high-purity MTBE preparation system for deeply removing isobutene |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS55323A (en) * | 1978-06-17 | 1980-01-05 | Fuji Sekiyu Kk | Preparation of methyl tertiary-butyl ether |
| US4418219A (en) * | 1981-03-02 | 1983-11-29 | National Distillers And Chemical Corporation | Preparation of methyl tertiary-butyl ether |
-
1994
- 1994-08-30 CN CN94110775A patent/CN1044805C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1085648C (en) * | 1997-05-07 | 2002-05-29 | 中国石化齐鲁石油化工公司 | Light hydrocarbon etherifying technology |
| CN109651063A (en) * | 2017-10-10 | 2019-04-19 | 中国石油化工股份有限公司 | The preparation method of iso-amylene |
| CN109651057A (en) * | 2017-10-10 | 2019-04-19 | 中国石油化工股份有限公司 | The method for preparing iso-amylene |
| CN109173310A (en) * | 2018-08-29 | 2019-01-11 | 张家港市科华化工装备制造有限公司 | Dimethoxym ethane rectifying column |
| CN114011341A (en) * | 2021-11-15 | 2022-02-08 | 丹东明珠特种树脂有限公司 | Catalytic distillation tower and high-purity MTBE preparation system for deeply removing isobutene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1044805C (en) | 1999-08-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7982086B2 (en) | Deisobutenizer | |
| MXPA06014686A (en) | Process for fine purification of 1-butenic streams . | |
| US5523061A (en) | Equipment for catalytic distillation | |
| CN102516036B (en) | Process method for preparing methyl tert-butyl ether by differential reaction rectification and equipment for same | |
| CN1020411C (en) | Mixed phase catalysis reaction distillation technology and equipment | |
| JPH10182507A (en) | Hydrogen isomerization reaction distillation, and production of high-purity isobutene by combination of distillation and skeleton isomeriziation | |
| CN1044805C (en) | Etherification reaction technology and equipment for light hydrocarbon and aliphatic alcohol | |
| CN108774100B (en) | Combined method for preparing methyl tert-butyl ether and isobutene from tert-butyl alcohol and methanol | |
| US6242662B1 (en) | Process for obtaining butene-1 | |
| CN1170609C (en) | Reactive distilling apparatus | |
| CN212199065U (en) | Separation device for coal-to-ethanol liquid-phase product | |
| WO2015097285A1 (en) | Process for the preparation of higher alcohols from lower alcohols by guerbet condensation | |
| CN101898930A (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| JPH10231256A (en) | Production of high-purity isobutene in combination of hydroisomerization and reactive distillation with skeleton isomerization | |
| CN102050690A (en) | Isoolefine production method | |
| CN112569620B (en) | Process system for preparing cyclopentyl methyl ether by using bulkhead reaction rectifying tower | |
| CN100513374C (en) | Method for preparing dimethyl ether by dehydration of methanol | |
| KR102627301B1 (en) | Use of separating wall technology to produce high purity methanol | |
| EP1513791A2 (en) | Process and apparatus for catalytic distillations | |
| KR100466035B1 (en) | Process for preparing tertiary alkyl ethers | |
| CN101260018B (en) | Method for synthesizing exo-tetrahydrocyclopentadiene | |
| CN1108844C (en) | Fractionating reaction column plate type catalytic distillating equipment | |
| CN210287179U (en) | Retrieve transformation MTBE apparatus for producing of three components of carbon | |
| US6262314B1 (en) | Process for preparation of ethers in a catalytic distillation column | |
| CN111423313B (en) | Process method and process device for preparing methyl tertiary butyl ether |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C53 | Correction of patent of invention or patent application | ||
| CB01 | Change of bibliographic data |
Address after: 100029 Beijing Chaoyang District Huixin East Street Jia 6 255436 Zibo City 124 Mailbox, Shandong Province Applicant after: China Petrochemical Corporation Applicant after: Sinopec qilu petrochemical company Applicant before: Sinopec qilu petrochemical company |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: APPLICANT; FROM: SINOPEC QILU PETRO-CHEMICAL CORP. TO: CHINA PETRO-CHEMICAL CORP.; SINOPECQILU PETRO-CHEMICAL CORP., HUIXINDONG STREET, CHAOYANG DISTRICT, BEIJING 100029; MAILBOX 124, ZIBO CITY, SHANDONG255436 |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: CHINA PETROCHEMICAL CORPORATION Free format text: FORMER OWNER: CHINA PETROCHEMICAL CORPORATION; SINOPEC QILU PETRO-CHEMICAL CORP. Effective date: 20071228 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| C56 | Change in the name or address of the patentee |
Owner name: CHINA PETROCHEMICAL CORPORATION; SINOPEC QILU PETR Free format text: FORMER NAME OR ADDRESS: CHINA PETRO-CHEMICAL CORP.; SINOPEC QILU PETRO-CHEMICAL CORP. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: No. 6 Huixin East Street Jia, Chaoyang District, Beijing: 100029 Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec qilu petrochemical company Address before: No. 6 Huixin East Street Jia, Chaoyang District, Beijing: 100029 Patentee before: China Petrochemical Corporation Patentee before: Sinopec qilu petrochemical company |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20071228 Address after: Zibo City, Shandong Province, Linzi District, China Petrochemical Qilu Branch, Ministry of Science and Technology zip code: 100029 Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Address before: No. 6 Huixin East Street Jia, Chaoyang District, Beijing: 100029 Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: Sinopec qilu petrochemical company |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 19990825 Termination date: 20130830 |