CN1157244C - Catalytic reaction distillation equipment - Google Patents
Catalytic reaction distillation equipment Download PDFInfo
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- CN1157244C CN1157244C CNB001239066A CN00123906A CN1157244C CN 1157244 C CN1157244 C CN 1157244C CN B001239066 A CNB001239066 A CN B001239066A CN 00123906 A CN00123906 A CN 00123906A CN 1157244 C CN1157244 C CN 1157244C
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- 238000004821 distillation Methods 0.000 title claims abstract description 59
- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 86
- 239000003054 catalyst Substances 0.000 claims abstract description 85
- 239000000463 material Substances 0.000 claims abstract description 55
- 238000011049 filling Methods 0.000 claims abstract description 39
- 239000007791 liquid phase Substances 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims description 27
- 230000000694 effects Effects 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 10
- 150000001336 alkenes Chemical group 0.000 claims description 4
- 239000011229 interlayer Substances 0.000 claims description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 2
- 239000002253 acid Substances 0.000 claims description 2
- 150000001345 alkine derivatives Chemical class 0.000 claims description 2
- 150000001993 dienes Chemical class 0.000 claims description 2
- 230000032050 esterification Effects 0.000 claims description 2
- 238000005886 esterification reaction Methods 0.000 claims description 2
- 150000002191 fatty alcohols Chemical class 0.000 claims description 2
- 238000006703 hydration reaction Methods 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- 238000005984 hydrogenation reaction Methods 0.000 claims description 2
- 238000007127 saponification reaction Methods 0.000 claims description 2
- 238000006266 etherification reaction Methods 0.000 claims 1
- 238000007789 sealing Methods 0.000 claims 1
- 238000003746 solid phase reaction Methods 0.000 claims 1
- 238000005192 partition Methods 0.000 abstract 4
- 230000002093 peripheral effect Effects 0.000 abstract 1
- 230000003197 catalytic effect Effects 0.000 description 42
- 239000000047 product Substances 0.000 description 28
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 26
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 18
- 239000012808 vapor phase Substances 0.000 description 12
- 230000005540 biological transmission Effects 0.000 description 10
- 238000000034 method Methods 0.000 description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 241000282326 Felis catus Species 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 9
- 239000000376 reactant Substances 0.000 description 9
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- 239000000945 filler Substances 0.000 description 6
- 238000009834 vaporization Methods 0.000 description 6
- 230000008016 vaporization Effects 0.000 description 6
- BKOOMYPCSUNDGP-UHFFFAOYSA-N 2-methylbut-2-ene Chemical group CC=C(C)C BKOOMYPCSUNDGP-UHFFFAOYSA-N 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000000066 reactive distillation Methods 0.000 description 4
- 239000010410 layer Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- 101000809257 Homo sapiens Ubiquitin carboxyl-terminal hydrolase 4 Proteins 0.000 description 1
- 102100038463 Ubiquitin carboxyl-terminal hydrolase 4 Human genes 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- IXSZQYVWNJNRAL-UHFFFAOYSA-N etoxazole Chemical compound CCOC1=CC(C(C)(C)C)=CC=C1C1N=C(C=2C(=CC=CC=2F)F)OC1 IXSZQYVWNJNRAL-UHFFFAOYSA-N 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000011491 glass wool Substances 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- HVZJRWJGKQPSFL-UHFFFAOYSA-N tert-Amyl methyl ether Chemical compound CCC(C)(C)OC HVZJRWJGKQPSFL-UHFFFAOYSA-N 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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Abstract
The present invention relates to catalytic reaction distillation equipment which comprises a rectifying section, a reaction section and a stripping section, wherein the reaction section is composed of an overlapped catalyst bed and a separating tower tray, the catalyst bed is composed of a down spout, a catalyst filling zone and a gas-liquid phase channel, and the catalyst filling zone is composed of upper gratings ((7, 7a or 7b), lower support plates ((9, 9a or 9b), peripheral partition boards (5, 5a or 5b) and guard boards (8, 8a or 8b). The down spout is formed between the partition boards or between the partition boards and a tower body, the gas-liquid phase channel is formed between the guard boards or between the guard boards and the tower body, at least one part of the partition boards and the guard boards is provided with holes or gaps, and thus, liquid phase reacting materials flows through the catalyst bed in the radial direction and carries out catalytic reaction under the action of a catalyst to increase reacting efficiency.
Description
The present invention relates to a kind of catalytic reaction distillation equipment, particularly be suitable for the catalytic reaction distillation equipment of the liquid-solid catalytic reaction that under the reaction mass bubble point temperature, carries out.
The chemical process of traditional catalysis of solid catalyst, carry out catalytic reaction under the effect of liquid phase reacting material solid catalyst in reactor, reacted material enters upstream device, carrying out product separates, for example: product enters in the rectifying column, and overhead product or tower bottom product are as final products or as further refining raw material.Like this, not only technological process is long, equipment investment is big, operating cost is high, and usually because the restriction of chemical balance or successive reaction etc. have limited the conversion ratio of product and the yield of target product.
In order to overcome the deficiency of traditional chemical process, produced reactor and separator have been combined in the reactive distillation technology that carries out simultaneously in the equipment.Carry out simultaneously because reaction is separated in the equipment with product, the product of production constantly shifts out reaction zone, destroys the balance of reaction, improves the conversion ratio of reactant; And reaction is to carry out under the bubble point temperature of reactant, and reaction heat is absorbed by reaction mass vaporization, not only controlled reaction temperature, and reaction heat is used for the separation of product.Reactive distillation technology has shortened process, reduces equipment investment, reduces the advantage of operating cost.Initial reactive distillation technology only is used for the homogeneous reaction still-process, has succeeded in developing heterogeneous reaction distillation technique one catalytic distillation technology subsequently again, makes the scope of application of reactive distillation technology wider.But the key of catalytic distillation technology is the filling structure of catalyst in the catalytic distillation tower, not only makes in the tower and passes conversion zone to last mobile vapor-phase material and the liquid phase material convection current that flows downward, and can satisfy the requirement that reaction separates with product.
Bibliographical information multiple catalyst filling structure, as USP3,434, the 534th, catalyst is contained in the downspout of conversion zone plate USP4,471,154 structures that disclose are that catalyst is contained in the sack of definite shape, place then on the tower tray of conversion zone; USP4, the catalyst packing methods of 215,011 inventions, be catalyst packing in the special sack of glass wool cloth, and be rolled into bundle, be contained in the middle part conversion zone of tower then.
The purpose of this invention is to provide a kind of catalytic reaction distillation equipment, liquid phase material radially passes beds, and carries out catalytic reaction under the effect of catalyst.
Catalytic distillation tower of the present invention comprises rectifying section, conversion zone and stripping section, and conversion zone is made up of separation tray between the beds of overlapping setting and bed, is provided with passage in the beds, can make in the tower vapour, liquid phase material convection current pass beds.On the tower tray between the reacting section catalyst bed, carry out heat, matter transmission to last mobile vapor-phase material in liquid phase material that flows downward in the tower and the tower, liquid phase material radial flow after heat, the matter transmission is crossed beds, and carries out catalytic reaction under the effect of catalyst.And vapor-phase material passes between the bed that beds flows to its top on the tower tray through passage.The product that so hockets separates and catalytic reaction, till meeting the requirements of conversion ratio.Because product constantly shifts out reaction zone, destroy the balance of reaction, improved the conversion ratio of reactant; Simultaneously, be reflected under the reaction mass bubble point and carry out, reaction heat is absorbed by the reaction mass vaporization, and reaction heat is used for product and separates, and has saved energy consumption.
Accompanying drawing 1～accompanying drawing 3 is catalytic reaction distillation equipment schematic diagram of the present invention
Below in conjunction with accompanying drawing 1, catalytic reaction distillation equipment of the present invention is elaborated.
Catalytic reaction distillation equipment (1) is divided into three parts: the rectifying section on top, the stripping section of bottom and middle part anti-Should section. The rectifying section on top is provided with a separation tray (2) at least, or is equivalent at least the separation of a separation tray One section filler of ability. The stripping section of bottom is provided with a separation tray (11) at least, or is equivalent at least a branch One section filler from the separating power of tower tray. The feature of middle part conversion zone comprises: at least two catalyst that overlap At least one separation tray (3) between bed (6,16) and bed. Beds dividing plate (5) and tower body consist of Arcuate region is the downspout (4) of the separation tray (3) on this bed top, beds (16) (or conversion zone Other beds) in block grid (7) structure by gripper shoe (9), baffle plate (8) and the catalyst of dividing plate (5), catalyst Become catalyst filling zone, catalyst both can be directly in bulk in catalyst filling zone, also can be rolled into certain shape and do Become member to put into filling area. Be provided with passage (10) in the beds so that vapour, liquid phase material convection current in the tower around Cross beds. Dividing plate (5) be a perforated panel or Web materials (but take the upper surface of catalyst filling zone as the boundary, The top of dividing plate does not have perforate or slit, the bottom perforate or to have the slit also can be Web materials), percent opening or slit Rate is generally 5%～80% (in the area of whole dividing plate) so that from the liquid phase material of tower tray (3) through downspout (4) radial flow, is opened for the contact condition of regulator solution stream with catalyst to the catalyst filling zone of bed (16) The percent opening of the upper and lower of bore region can be different. Catalyst gripper shoe (9) is a flat board, and main purpose is Support the liquid phase material of the catalyst of filling area and the filling area of flowing through. Baffle plate (8) is a perforated panel, and the size in hole is fair Permitted liquid and flow through, and do not allow catalyst to spill; The percent opening of baffle plate or gap rate are generally 5%～80% (area), Perhaps bigger with pore design set up the catalyst block in the inboard of baffle plate (8), and block allows liquid to flow through, And do not allow catalyst to spill. Block grid (7) and be a perforated panel or be woven wire, with limiting catalyst at filling area In, also can remove catalyst when needing and block grid.
The material that contains reactant enters on the tower tray of conversion zone adjacent catalyst bed interlayer through pipeline (20).The liquid phase material that comes from rectifying section flows in the beds (6) that conversion zone goes up most through downspout, and Radial Flow is passed beds, and carries out catalytic reaction under the effect of catalyst.Reacted liquid phase material flows on the separation tray (3) of its underpart, and on tower tray (3), carry out heat, matter transmission with vapor-phase material, liquid phase material after heat, matter are transmitted flows in the beds (16) through downspout (4), radial flow is crossed beds (16), and reacts under the effect of catalyst; Reacted material flows on the separation tray of its underpart through passage (10).The passage of vapor-phase material through being located at beds (6) after heat, the matter transmission passes beds, and flows to the separation tray on this beds top.So hocket reaction, separating process are till meeting the requirements of conversion ratio.The vapor-phase material that enters rectifying section after separating from cat head after pipeline (12), condenser (13) condensation, a part is back to cat head through pipeline (14), another part goes out device as light-end products through pipeline (15).The liquid phase material that flow to stripping section is emitted through pipeline (21) at the bottom of tower after separating, and wherein the vapour phase of a part after reboiler (22) vaporization is at the bottom of pipeline (23) returns tower, and another part goes out device as heavy product through pipeline (24).
Below in conjunction with accompanying drawing 2, catalytic reaction distillation equipment of the present invention is elaborated.
Catalytic reaction distillation equipment (1) is divided into three parts: the conversion zone at the rectifying section on top, the stripping section of bottom and middle part.The rectifying section on top is provided with a separation tray (2) at least, or is equivalent to one section filler of the separating power of a separation tray at least.The stripping section of bottom is provided with a separation tray (11) at least, or is equivalent to one section filler of the separating power of a separation tray at least.The feature of middle part conversion zone comprises: at least one separation tray (3) between beds of at least two overlapping settings (6,16) and bed.Beds (6) comprising: at least two catalyst filling zone (6a, 6b), at least one downspout (4), at least two passages (10a, 10b) and catalyst gripper shoe (9) and block grid (7a, 7b).Dividing plate (5a), baffle plate (8a), block grid (7a) and gripper shoe (9) and constitute catalyst filling zone (6a), and dividing plate (5b), baffle plate (8b), block grid (7b) and gripper shoe (9) and constitute catalyst filling zone (6b), also can remove catalyst when needing and block grid.Baffle plate (8a) and the arc of tower body formation are passage (10a), and baffle plate (8b) and the arc of tower body formation are passage (10b), so that beds is walked around in vapour, liquid phase material convection current in the tower.Dividing plate (5a, 5b) be a perforated panel or Web materials below the upper surface of catalyst filling zone, (8a 8b) is a perforated panel or Web materials to baffle plate, the size of perforate allows liquid to flow through and does not allow catalyst to spill, and can make liquid phase material flow through beds equably.The percent opening of dividing plate, baffle plate or gap rate are generally 5%～80% (area).If perforate is bigger, can set up the catalyst block in the inboard of catalyst filling zone, so that guarantee that catalyst does not spill.Catalyst gripper shoe (9) is a flat board, and main purpose is to support the liquid phase material of the catalyst of filling area and the filling area of flowing through.
The material that contains reactant enters on the tower tray of conversion zone adjacent catalyst bed interlayer through pipeline (20).The liquid phase material that comes from rectifying section through downspout (4) flow to the beds that conversion zone goes up most (6a, 6b) in, Radial Flow is passed beds, and carries out catalytic reaction under the effect of catalyst.Reacted liquid phase material flows on the separation tray (3) of its underpart, and on tower tray (3), carry out heat, matter transmission with vapor-phase material, liquid phase material after heat, the matter transmission flows to beds (16a through downspout, 16b), radial flow is crossed beds, and reacts under the effect of catalyst; (10a 10b) passes beds to the passage of vapor-phase material through being located at beds after heat, the matter transmission, and flows to the separation tray on this beds top.So hocket reaction, separating process are till meeting the requirements of conversion ratio.The vapor-phase material that enters rectifying section after separating from cat head after pipeline (12), condenser (13) condensation, a part is back to cat head through pipeline (14), another part goes out device as light-end products through pipeline (15).The liquid phase material that flow to stripping section is emitted through pipeline (21) at the bottom of tower after separating, and wherein the vapour phase of a part after reboiler (22) vaporization is at the bottom of pipeline (23) returns tower, and another part goes out device as heavy product through pipeline (24).
Below in conjunction with accompanying drawing 3, catalytic reaction distillation equipment of the present invention is elaborated.
Catalytic reaction distillation equipment (1) is divided into three parts: the conversion zone at the rectifying section on top, the stripping section of bottom and middle part.The rectifying section on top is provided with a separation tray (2) at least, or is equivalent to one section filler of the separating power of a separation tray at least.The stripping section of bottom is provided with a separation tray (11) at least, or is equivalent to one section filler of the separating power of a separation tray at least.The feature of middle part conversion zone comprises: at least one separation tray (3) between beds of at least two overlapping settings (6,16) and bed.Beds (6) comprising: at least two catalyst filling zone (6a, 6b), at least two downspouts (4a, 4b), at least one passage (10) and at least two catalyst gripper shoes (9a, 9b) and block grid (7a, 7b).Dividing plate (5a), baffle plate (8a) and gripper shoe (9a) and block grid (7a) and constitute catalyst filling zone (6a), and dividing plate (5b), baffle plate (8b) and gripper shoe (9b) and block grid (7b) and constitute catalyst filling zone (6b) also can be removed catalyst and block grid when needing.Dividing plate (5a) and the arc of tower body formation are downspout (4a), and dividing plate (5b) and the arc of tower body formation are downspout (4b), so that beds is walked around in vapour, liquid phase material convection current in the tower.Dividing plate (5a, 5b) be a perforated panel or Web materials below the upper surface of catalyst filling zone, (8a 8b) is a perforated panel or Web materials to baffle plate, the size of perforate allows liquid to flow through and does not allow catalyst to spill, and can make liquid phase material flow through beds equably.The percent opening of dividing plate, baffle plate or gap rate are generally 5%～80% (area).If perforate is bigger, can set up the catalyst block in the inboard of catalyst filling zone, so that guarantee that catalyst does not spill.(9a 9b) is a flat board to the catalyst gripper shoe, and main purpose is to support the liquid phase material of the catalyst of filling area and the filling area of flowing through.
The material that contains reactant enters on the tower tray of conversion zone adjacent catalyst bed interlayer through pipeline (20).The liquid phase material that comes from rectifying section through downspout (4a, 4b) flow to the beds that conversion zone goes up most (6a, 6b) in, Radial Flow is passed beds, and carries out catalytic reaction under the effect of catalyst.Reacted liquid phase material flows on the separation tray (3) of its underpart, and on tower tray (3), carry out heat, matter transmission with vapor-phase material, liquid phase material after heat, the matter transmission flows to beds (16a through downspout, 16b), radial flow is crossed beds, and reacts under the effect of catalyst; The passage (10) of vapor-phase material through being located at beds after heat, the matter transmission passes beds, and flows to the separation tray on this beds top.So hocket reaction, separating process are till meeting the requirements of conversion ratio.The vapor-phase material that enters rectifying section after separating from cat head after pipeline (12), condenser (13) condensation, a part is back to cat head through pipeline (14), another part goes out device as light-end products through pipeline (15).The liquid phase material that flow to stripping section is emitted through pipeline (21) at the bottom of tower after separating, and wherein the vapour phase of a part after reboiler (22) vaporization is at the bottom of pipeline (23) returns tower, and another part goes out device as heavy product through pipeline (24).
Reaction mass reacts simultaneously with product in catalytic distillation tower and separates, especially for balanced reaction, because product is constantly shifted out reaction zone, destroy molecular balance, reaction is proceeded to fully, in order to make reaction reach requirement, the catalyst bed number of plies of the conversion zone of catalytic distillation tower is many, loaded catalyst is big.But the catalytic distillation technology key is the filling pattern of catalyst, and how simple the catalyst filling structure of the catalytic distillation technology of no matter developing is, more than baroque with general fixed bed reactors.Therefore, in order to reduce the loaded catalyst of catalytic distillation tower, establish a pre-reactor before catalytic distillation tower, this pre-reactor can adopt tubulation fixed bed reactors, adiabatic outer circulation reactor, expanded bed reactor or mixed phase bed bioreactor.Reaction mass reaches certain conversion ratio in pre-reactor after, enter and further react in the catalytic distillation tower and separate, make till total conversion value of meeting the requirements of of reactant.
In conjunction with Fig. 4, the technological process that pre-reactor is connected with catalytic distillation is described.
Comprise pre-reactor (33) and catalytic distillation tower (1) in pre-reactor and the technological process that catalytic distillation tower of the present invention is connected, pre-reactor (33) can adopt the mixed phase reactor, and catalytic distillation tower (1) is the filling structure of catalytic distillation tower of the present invention.Two kinds of reaction masses (31,32) mix, and after being preheating to the temperature of energy initiation reaction, enter in the pre-reactor, react under the catalyst action in pre-reactor, reaction heat raises the temperature of reactant feed gradually, when temperature is elevated to the bubble point temperature of reaction mass under the operating pressure, reaction heat is absorbed by the partial material vaporization, and makes reaction temperature stable.When reactant reaches certain conversion ratio, flow out pre-reactor, enter in the catalytic distillation tower through pipeline (20).Entering reaction mass in the catalytic distillation tower further reacts with product and separates, unreacted lightweight logistics after rectifying section separates from cat head after pipeline (12), condenser (13) condensation, a part is back to cat head through pipeline (14), and another part goes out device as light-end products through pipeline (15).The heavy product that generates separates the back through stripping section emits through pipeline (21) at the bottom of tower, and wherein a part is vaporized after at the bottom of pipeline (23) returned tower, another part went out device as heavy product through pipeline (24) through reboiler (22).
Catalysis-distillation equipment of the present invention is suitable for C
4～C
8Tertiary olefin and C
1～C
4The synthetic corresponding ether product of fatty alcohol reaction, also be suitable for C
2～C
8The hydro carbons fraction is selected esterification, saponification, olefin hydration reaction and other similar reactions of hydrogenation and removing diolefin and alkynes, alcohol and acid.
Catalysis-distillation equipment of the present invention, owing to can make the liquid phase stream Radial Flow pass through beds, reduced flow resistance, can increase the loading height of catalyst in the catalyst filling zone, and can be by regulating the percent opening of downspout, increase the amount of liquid that flows through in the per unit height catalyst filling zone, increased reaction efficiency.
The present invention will be further described below by embodiment:
When the catalytic distillation tower shown in the accompanying drawing 1 of the present invention was used for the isobutene of mixed c 4 and methyl alcohol reaction and produces methyl tertiary butyl ether(MTBE) (MTBE), conversion for isobutene reached 99.6%, and unreacted carbon four can be used for producing the raw material of 1-butylene or other chemical products.
Operating condition and result:
Isobutene content in the carbon four, % (m/m), 21%
The mol ratio of methyl alcohol and isobutene, 1.1: 1.0
The catalytic distillation tower tower top pressure, MPa, 0.8
The catalytic distillation tower tower bottom pressure, MPa, 0.86
The catalytic distillation tower tower top temperature, ℃, 62
Catalytic distillation Tata still temperature, ℃, 139
Air speed, h
-1, 1.8
Catalytic distillation tower conversion zone bed number, layer, 18
Isobutene in the discharging of catalytic distillation column overhead in the unreacted carbon four, % (m/m), 0.1%
MTBE product purity % (m/m) at the bottom of the catalytic distillation Tata, 98.4%
Conversion for isobutene, % (m/m), 99.6%
When being used for the catalytic distillation tower shown in the accompanying drawing 2 of the present invention with mixing carbon five uncle's amylenes and methyl alcohol reaction synthesizing methyl tert-amyl ether (TAME), the conversion ratio of uncle's amylene reaches 95%.
Operating condition and result:
Uncle's amylene content in the carbon five, % (m/m), 27%
The mol ratio of methyl alcohol and uncle's amylene, 1.2: 1.0
The catalytic distillation tower tower top pressure, MPa, 0.4
The catalytic distillation tower tower bottom pressure, MPa, 0.46
The catalytic distillation tower tower top temperature, ℃, 68
Catalytic distillation Tata still temperature, ℃, 137
Air speed, h
-1, 2.2
Catalytic distillation tower conversion zone bed number, layer, 12
Uncle's amylene in the discharging of catalytic distillation column overhead in the unreacted carbon five, % (m/m), 1.8%
TAME product purity % (m/m) at the bottom of the catalytic distillation Tata, 98.2%
The conversion ratio of uncle's amylene, % (m/m), 95.04%
The equipment that pre-reactor shown in the accompanying drawing 4 of the present invention is connected with catalytic distillation tower is used for the isobutene of mixed c 4 and methyl alcohol reaction when producing methyl tertiary butyl ether(MTBE) (MTBE), conversion for isobutene reaches 99.8%, and unreacted carbon four can be used for producing the raw material of 1-butylene or other chemical products.
Operating condition and result:
Isobutene content in the carbon four, % (m/m), 21%
The mol ratio of methyl alcohol and isobutene, 1.1: 1.0
The operating pressure of pre-reactor, MPa, 0.9
The outlet temperature of pre-reactor, ℃, 69.3
Conversion for isobutene in the pre-reactor, % (m/m), 92.4%
The catalytic distillation tower tower top pressure, MPa, 0.8
The catalytic distillation tower tower bottom pressure, MPa, 0.86
The catalytic distillation tower tower top temperature, ℃, 62
Catalytic distillation Tata still temperature, ℃, 139
Air speed, h
-1, 3.4
Catalytic distillation tower conversion zone bed number, layer, 8
Isobutene in the catalytic distillation tower cat head effluent unreacted carbon four, % (m/m), 0.08%
MTBE product purity % (m/m) at the bottom of the catalytic distillation Tata, 98.6%
Conversion for isobutene, % (m/m), 99.8%
Claims (13)
1, a kind of catalytic reaction distillation equipment, comprise rectifying section, conversion zone and stripping section, conversion zone is made up of overlapping beds and separation tray, it is characterized in that beds is by downspout, catalyst filling zone and vapour-liquid passage are mutually formed, catalyst filling zone is by the gripper shoe (9 of bottom, 9a or 9b), and the dividing plate (5 of periphery, 5a or 5b) and baffle plate (8,8a or 8b) constitute, constitute downspout between its median septum and the dividing plate or between dividing plate and the tower body, constitute vapour-liquid passage mutually between baffle plate and the baffle plate or between baffle plate and the tower body, to have a part of zone on dividing plate and the baffle plate at least be perforate or have the slit, make the liquid phase reacting material radial flow cross beds, and under the effect of catalyst, carry out catalytic reaction.
2, according to the described equipment of claim 1, wherein the upper surface of catalyst filling zone blocks grid (7,7a or 7b).
3, according to claim 1 or 2 described equipment, the zone of its median septum below the catalyst filling zone upper surface be perforate or have the slit, and dividing plate also can be a Web materials, and the percent opening of dividing plate or gap rate count 5%～80% with the dividing plate area.
4, according to claim 1 or 2 described equipment, wherein the baffle plate of beds is that percent opening or gap rate are counted 5%～80% plate or Web materials with area.
5, according to claim 1 or 2 described equipment, wherein the gripper shoe of beds is not open the plate in virtually any size hole, and and tower body sealing.
6, according to claim 1 or 2 described equipment, wherein catalyst directly is seated in the described catalyst filling zone.
7,, a catalyst filling zone, downspout and vapour-liquid passage is mutually arranged in the beds wherein according to claim 1 or 2 described equipment.
8,, at least two catalyst filling zone, downspout and at least two vapour-liquids passage is mutually arranged in the beds wherein according to claim 1 or 2 described equipment.
9,, at least two catalyst filling zone, at least two downspouts and vapour-liquid passage is mutually arranged in the beds wherein according to claim 1 or 2 described equipment.
10, according to claim 1 or 2 described equipment, wherein the catalyst bed number of plies of conversion zone is 2～20.
11, according to claim 1 or 2 described equipment, wherein two adjacent catalyst bed interlayers are established a separation tray at least in the conversion zone.
12,, it is characterized in that the use of connecting with the fixed bed pre-reactor of described equipment according to claim 1 or 2 described equipment.
13. the purposes of the described equipment of claim 1 comprises C
4～C
8Tertiary olefin and C
1～C
4The etherification reaction of fatty alcohol, C
2～C
8The hydro carbons fraction is selected esterification, olefin hydration reaction, saponification and other similar vapour solid phase reactions of hydrogenation and removing diolefin and alkynes, alcohol and acid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001239066A CN1157244C (en) | 2000-09-22 | 2000-09-22 | Catalytic reaction distillation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001239066A CN1157244C (en) | 2000-09-22 | 2000-09-22 | Catalytic reaction distillation equipment |
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| Publication Number | Publication Date |
|---|---|
| CN1345617A CN1345617A (en) | 2002-04-24 |
| CN1157244C true CN1157244C (en) | 2004-07-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB001239066A Expired - Lifetime CN1157244C (en) | 2000-09-22 | 2000-09-22 | Catalytic reaction distillation equipment |
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| Country | Link |
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| CN (1) | CN1157244C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100584420C (en) * | 2008-10-20 | 2010-01-27 | 中国科学院大连化学物理研究所 | Catalytic distillation tower reaction segment structrue |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102462971B (en) * | 2010-11-11 | 2014-08-20 | 中国石油化工股份有限公司 | Mobile catalytic distillation equipment and its application |
| CN102485305B (en) * | 2010-12-03 | 2013-11-06 | 中国石油天然气股份有限公司 | Catalyst filling structure for tertiary butanol catalytic rectification dehydration and technology adopting the catalyst filling structure |
| CN102824752A (en) * | 2011-06-16 | 2012-12-19 | 徐志刚 | Catalytic distillation tower |
| CN103421532B (en) * | 2012-05-15 | 2015-07-29 | 中国石油化工股份有限公司 | A kind of solid acid alkylating reaction method |
| CN107652157A (en) * | 2017-08-11 | 2018-02-02 | 中国天辰工程有限公司 | A kind of method of butadiene in methanol removal olefin process using reactive distillation |
| CN112174809B (en) * | 2019-07-05 | 2022-10-21 | 中国石油化工股份有限公司 | Continuous preparation device of homogeneous organic molybdenum compound |
| CN114432971B (en) * | 2020-10-21 | 2023-04-07 | 中国石油化工股份有限公司 | Catalytic reactor and distillation tower using same |
| CN114452900B (en) * | 2020-10-21 | 2023-02-03 | 中国石油化工股份有限公司 | Catalytic reaction unit and reactive distillation tower |
| CN114452901B (en) * | 2020-10-21 | 2023-03-07 | 中国石油化工股份有限公司 | Catalytic reaction unit and reactive distillation column |
| CN115678595B (en) * | 2021-07-30 | 2024-03-12 | 中国石油化工股份有限公司 | Deep desulfurization method and system for gasoline |
-
2000
- 2000-09-22 CN CNB001239066A patent/CN1157244C/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100584420C (en) * | 2008-10-20 | 2010-01-27 | 中国科学院大连化学物理研究所 | Catalytic distillation tower reaction segment structrue |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1345617A (en) | 2002-04-24 |
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