CN1386573A - Gas circulating chemical reactor with vertical baffling and its application method - Google Patents
Gas circulating chemical reactor with vertical baffling and its application method Download PDFInfo
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- CN1386573A CN1386573A CN 02115601 CN02115601A CN1386573A CN 1386573 A CN1386573 A CN 1386573A CN 02115601 CN02115601 CN 02115601 CN 02115601 A CN02115601 A CN 02115601A CN 1386573 A CN1386573 A CN 1386573A
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- gas
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- pressure
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- 239000000126 substance Substances 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims description 20
- 239000007788 liquid Substances 0.000 claims abstract description 51
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- 239000000203 mixture Substances 0.000 claims abstract description 5
- 239000000945 filler Substances 0.000 claims description 35
- 239000003054 catalyst Substances 0.000 claims description 15
- 230000003647 oxidation Effects 0.000 claims description 15
- 238000007254 oxidation reaction Methods 0.000 claims description 15
- 239000000376 reactant Substances 0.000 claims description 11
- 239000007800 oxidant agent Substances 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 7
- 239000007787 solid Substances 0.000 claims description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 229910021536 Zeolite Inorganic materials 0.000 claims description 3
- 229910010293 ceramic material Inorganic materials 0.000 claims description 3
- 230000003009 desulfurizing effect Effects 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 229910052742 iron Inorganic materials 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- 239000004033 plastic Substances 0.000 claims description 3
- 229920003023 plastic Polymers 0.000 claims description 3
- 238000006722 reduction reaction Methods 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 239000010457 zeolite Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 33
- 239000012071 phase Substances 0.000 description 9
- 230000016507 interphase Effects 0.000 description 4
- 230000035484 reaction time Effects 0.000 description 3
- 238000003746 solid phase reaction Methods 0.000 description 3
- 239000000470 constituent Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 101100298222 Caenorhabditis elegans pot-1 gene Proteins 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 230000001869 rapid Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A chemical reactor with vertically baffling gas circulation has at least two reacting tanks serially connected via pipe from top of previous one to bottom of next one. Each reacting tank except the final one has a circulating pipe from top to bottom and a gas pump. The liquid or gas reaction substances are fed in the first reaction tank from its bottom for reaction. After reaction, the gas is separated from liquid and then returned back to own reaction tank via gas pump and circulating pipe and the gas-liquid mixture is fed into next reaction tank.
Description
Technical field
The present invention relates to a kind of chemical reaction equipment and application process thereof that is widely used in the Chemical Reaction Engineering, relate to a kind of gas circulating chemical reactor with vertical baffling and application process thereof specifically.
Background technology
Chemical reaction all relates to gas-liquid two-phase or gas-liquid-solid phase reaction process in many cases, and interphase mass transfer all is the restricted step of reaction speed in the ordinary course of things, so the hardening constituent transfer process is one of important means of quickening chemical reaction.The method of hardening constituent transfer process has usually, and increase phase border interfacial area (improving dispersed) improves the long-pending renewal speed of phase interphase (the repeatedly fragmentation of bubble), reduces the mass transfer film thickness, increases mass transfer power (alternate concentration difference), prolongs the interphase mass transfer time etc.On common stirring perfectly mixed reactor basis, people have developed interior circulation (gas lift, liquid liter) reactor, so that improve gas-liquid mass transfer speed; Packed bed gas-liquid-solid phase reaction device and fluid bed gas-liquid-solid phase reaction device " are selected from Chemical Engineering handbook the 6th volume " with the speed (inert filler) and the gas-liquid-solid three-phase mass transfer rate (active filler) that improve gas-liquid mass transfer.With the exception of this, people have also developed multiple new chemical consersion unit and technical process in recent years, and wherein representational have: string data chemical reactor, (modern chemical industry, 1998, the third phases) such as downstriker circulating fluid bed reactors.In a word, in relating to the chemical reaction process that gas phase is a reactant, for example, atmospheric air oxidation such as forced air oxidation, the wet type air oxidation, ozone oxidation, the pure oxygen oxidation, gas phase (gas) catalytic oxidation etc., gas phase just has great important to the transfer rate and the efficient of liquid phase, and the utilization rate of gaseous oxidizing agent depends on above-mentioned various factors, and utilization rate has also determined the economy and the availability of chemical reaction process simultaneously, therefore, reactor and reinforcement thereof have just determined the feasibility of a chemical reaction process sometimes.
Summary of the invention
Purpose of the present invention just is to provide a kind of can fully improve the gas-liquid two-phase turbulent extent in chemical reaction process, interphase interface is long-pending big, gas-liquid contact time is long, gas circulating chemical reactor with vertical baffling that the gaseous reactant utilization rate is high and application process thereof.
For achieving the above object, the present invention can take following technical proposals:
Chemical reactor of the present invention comprises at least and being made up of the two-stage reaction jar, the bottom of first order retort is provided with a three-way pipe import, its top is connected by the bottom of mozzle with the next stage retort, on the mozzle at each the retort top that is positioned at the first order and intergrade, be linked with a circulation pipe that has an air pump by three-way pipe, another mouth of pipe of this circulation pipe is connected with retort bottom at the corresponding levels; Offer gas outlet and liquid outlet at the top of final stage retort.
In described retort, be filled with inert filler, but also filling reactive filler certainly; For further improving reaction effect, on described retort outer wall, be wrapped with the heat medium layer.
The application process of chemical reactor of the present invention comprises
(a), carry out chemical reaction in the first order retort with entering after gas, of the three-way pipe mixing of liquid reactant through being arranged on described first order retort bottom; (b), in retort, carry out after the gas liquid reaction, gas is phase-splitting in gas-liquid separator, and gas turns back to retort at the corresponding levels bottom through described air pump, circulation pipe and carries out secondary response; (c), the part gas-liquid mixture after the process first order reaction enters into by mozzle and carries out chemical reaction in the next stage retort, first class reaction pot to the last successively, gas is discharged from the gas outlet at afterbody retort top, and liquid is discharged from this retort top liquid outlet.
The operating pressure of above-mentioned retort can be divided into high pressure (more than the 5MPa), middle pressure (5MPa--1MPa), low pressure (1MPa--0.01MPa) and minute-pressure (less than 0.01MPa); For generally adopting high pressure as the course of reaction of oxidant with the low air of oxidability, press in general the using of course of reaction for solid catalysis and liquid-phase catalysis air oxidation, for adopting general oxidant to carry out the time standby low pressure of oxidation, use minute-pressure when adopting the strong oxidizer oxidation, minute-pressure when reaction pressure is generally from the clean head of liquid of liquid phase, and other situation need utilize the pressure-regulating valve of afterbody to finish the control of pressure.
The filler that is arranged in the described retort can be divided into two classes according to reactive difference: inert filler and reactive filler, the former only strengthens mass transfer effect in order to improve the gas-liquid turbulent flow, the latter then is a catalysts, catalyst carrier or reactant, all kinds of chemical fillers that comprise stainless steel as the filler of inert carrier, all kinds of chemical fillers of ceramic material, all kinds of chemical fillers of plastic material, and other satisfy the filler of operating condition, as oxide-based catalyst of reactive filler common metal and carrier, activated carbon class catalyst and carrier, natural and artificial zeolite molecular sieve catalyst and carrier, and reduction reaction agent and desulfurizing agents such as solid reactants such as iron filings.
Knockout drum should be considered the size of gas liquid ratio, guarantee to divide and to compare thoroughly, reduce liquid entrainment as far as possible and enter in the air pump, and be to consider in 2-3 minute by gas residence time when selecting dischargeable capacity.
Outstanding innovative point of the present invention is to adopt endless form at the corresponding levels to improve gas effciency, also the gas of complete reaction and liquid also do not flow to the bottom that is transported to second level reactor down simultaneously, carry out partial chemical reaction, the particularly important is when carrying gas-liquid mixture downwards, because gas will be moved upward by buoyancy, and the liquid depended on pressure moves downward, the relative motion trend of this moment effectively raises gas-liquid turbulent flow and gas liquid reaction time, this reaction time can be according to the gas-liquid flow, gas liquid ratio is effectively controlled to reach different reaction time requirements with caliber, by reaction of high order process so, make gas effciency can reach more than 95%, gas-liquid mass transfer speed is also improved widely, also effectively reduces production cost simultaneously, has reduced the pollution of pernicious gas to environment.
Description of drawings
Fig. 1 is the structural representation of chemical reactor of the present invention.
The specific embodiment
As shown in the figure, chemical reactor of the present invention comprises at least and being made up of two-stage reaction jar 1, the bottom of first order retort 1 is provided with a three-way pipe import, its top is connected by the bottom of mozzle 2 with next stage retort 1, on the mozzle 2 at each retort 1 top that is positioned at the first order and intergrade, be linked with a circulation pipe 4 that has an air pump 3 by three-way pipe, another mouth of pipe of this circulation pipe 4 is connected with retort 1 bottom of the corresponding levels, offers gas outlet 5 and liquid outlet 6 at the top of final stage retort 1.In described retort 1, be filled with inert filler, but also filling reactive filler certainly; For further improving reaction effect, on described retort 1 outer wall, be wrapped with the heat medium layer.
Using method of the present invention comprises (a), carries out chemical reaction in the first order retort 1 with entering after gas, the three-way pipe mixing of liquid reactant through being arranged on described first order retort 1 bottom; (b), in retort 1, carry out after the gas liquid reaction, gas is phase-splitting in gas-liquid separator, and gas turns back to retort at the corresponding levels 1 bottom and carries out secondary response through described air pump 3, circulation pipe 4; (c), the gas-liquid mixture after the process first order reaction enters into by mozzle 2 and carries out chemical reaction in the next stage retort 1, first class reaction pot 1 to the last successively, gas is discharged from the gas outlet 5 at afterbody retort 1 top, and liquid is discharged from this retort 1 top liquid outlet 6.
The operating pressure of above-mentioned retort 1 can be divided into high pressure (more than the 5MPa), middle pressure (5MPa--1MPa), low pressure (1MPa--0.01MPa) and minute-pressure (less than 0.01MPa); For generally adopting high pressure as the course of reaction of oxidant with the low air of oxidability, press in general the using of course of reaction for solid catalysis and liquid-phase catalysis air oxidation, for adopting general oxidant to carry out the time standby low pressure of oxidation, use minute-pressure when adopting the strong oxidizer oxidation, minute-pressure when reaction pressure is generally from the clean head of liquid of liquid phase, and other situation need utilize the pressure-regulating valve of afterbody to finish the control of pressure.
The filler that is arranged in the described retort 1 can be divided into two classes according to reactive difference: inert filler and reactive filler, the former only strengthens mass transfer effect in order to improve gas-liquid rapids liquid, the latter then is a catalysts, catalyst carrier or reactant, filler as inert carrier comprises, all kinds of chemical fillers of stainless steel, all kinds of chemical fillers of ceramic material, all kinds of chemical fillers of plastics village matter, and other satisfy the filler of operating condition, as oxide-based catalyst of reactive filler common metal and carrier, activated carbon class catalyst and carrier, natural and artificial zeolite molecular sieve catalyst and carrier, and reduction reaction agent and desulfurizing agents such as solid reactants such as iron filings.
Knockout drum should be considered the size of gas liquid ratio, guarantee to divide and to compare thoroughly, reduce liquid entrainment as far as possible and enter in the air pump 3, and be to consider in 2-3 minute by gas residence time when selecting dischargeable capacity.
Claims (8)
1, a kind of gas circulating chemical reactor with vertical baffling, comprise at least and forming by two-stage reaction jar (1), it is characterized in that: be provided with a three-way pipe import in the bottom of first order retort (1), its top is connected by the bottom of mozzle (2) with next stage retort (1), go up by three-way pipe at the mozzle (2) at each retort (1) top that is positioned at the first order and intergrade and to be linked with a circulation pipe (4) that has air pump (3), another mouth of pipe of this circulation pipe (4) is connected with retort (1) bottom of the corresponding levels; Offer gas outlet (5) and liquid outlet (6) at the top of final stage retort (1).
2, gas circulating chemical reactor with vertical baffling according to claim 1 is characterized in that: be filled with inert filler in described retort (1).
3, gas circulating chemical reactor with vertical baffling according to claim 1 is characterized in that: be filled with reactive filler in described retort (1).
4, gas circulating chemical reactor with vertical baffling according to claim 1 is characterized in that: be wrapped with the heat medium layer on described retort (1) outer wall.
5, according to the using method of the described chemical reactor of claim 1, it is characterized in that: it comprises (a), carries out chemical reaction with entering in the first order retort (1) after gas, the three-way pipe mixing of liquid reactant through being arranged on described first order retort (1) bottom; (b), in retort (1), carry out gas liquid reaction after, gas is phase-splitting in gas-liquid separator, gas turns back to retort at the corresponding levels (1) bottom through described air pump (3), circulation pipe (4) and carries out secondary response; (c), the gas-liquid mixture after the process first order reaction enters in the next stage retort (2) by mozzle (2) and carries out chemical reaction, first class reaction pot (1) to the last successively, gas is discharged from the gas outlet (5) at afterbody retort (1) top, and liquid is discharged from this retort (1) top liquid outlet (6).
6, using method according to claim 5 is characterized in that: the operating pressure of described retort (1) can be divided into high pressure (more than the 5MPa), middle pressure (5MPa--1MPa), low pressure (1MPa--0.01MPa) and minute-pressure (less than 0.01MPa); For generally adopting high pressure as the course of reaction of oxidant with the low air of oxidability, press in general the using of course of reaction for solid catalysis and liquid-phase catalysis air oxidation, for adopting general oxidant to carry out the time standby low pressure of oxidation, use minute-pressure when adopting the strong oxidizer oxidation, minute-pressure when reaction pressure is generally from the clean head of liquid of liquid phase, and other situation need utilize the pressure-regulating valve of afterbody to finish the control of pressure.
7, using method according to the described chemical reactor of claim 5, it is characterized in that: the filler that is arranged in the described retort (1) can be divided into two classes according to reactive difference: inert filler and reactive filler, the former only strengthens mass transfer effect in order to improve the gas-liquid turbulent flow, the latter then is a catalysts, catalyst carrier or reactant, all kinds of chemical fillers that comprise stainless steel as the filler of inert carrier, all kinds of chemical fillers of ceramic material, all kinds of chemical fillers of plastic material, and other satisfy the filler of operating condition, as oxide-based catalyst of reactive filler common metal and carrier, activated carbon class catalyst and carrier, natural and artificial zeolite molecular sieve catalyst and carrier, and reduction reaction agent and desulfurizing agents such as solid reactants such as iron filings.
8, using method according to claim 1, it is characterized in that: described knockout drum should be considered the size of gas liquid ratio, guarantee dividing and to compare thoroughly, reduce liquid entrainment as far as possible and enter in the air pump (3), is to consider in 2-3 minute by gas residence time when selecting dischargeable capacity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02115601 CN1386573A (en) | 2002-03-13 | 2002-03-13 | Gas circulating chemical reactor with vertical baffling and its application method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02115601 CN1386573A (en) | 2002-03-13 | 2002-03-13 | Gas circulating chemical reactor with vertical baffling and its application method |
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| Publication Number | Publication Date |
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| CN1386573A true CN1386573A (en) | 2002-12-25 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02115601 Pending CN1386573A (en) | 2002-03-13 | 2002-03-13 | Gas circulating chemical reactor with vertical baffling and its application method |
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| Country | Link |
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| CN (1) | CN1386573A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101862632A (en) * | 2010-06-03 | 2010-10-20 | 常州大学 | A semi-circular gas-liquid multiphase flow contact method |
| CN109569008A (en) * | 2018-12-06 | 2019-04-05 | 南通市康桥油脂有限公司 | A kind of reinforcing condensation process for petroleum vapor recovery process |
-
2002
- 2002-03-13 CN CN 02115601 patent/CN1386573A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101862632A (en) * | 2010-06-03 | 2010-10-20 | 常州大学 | A semi-circular gas-liquid multiphase flow contact method |
| CN101862632B (en) * | 2010-06-03 | 2013-03-13 | 常州大学 | Semi-circulation type gas-liquid multiphase flow contact method |
| CN109569008A (en) * | 2018-12-06 | 2019-04-05 | 南通市康桥油脂有限公司 | A kind of reinforcing condensation process for petroleum vapor recovery process |
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