CN101862632B - Semi-circulation type gas-liquid multiphase flow contact method - Google Patents
Semi-circulation type gas-liquid multiphase flow contact method Download PDFInfo
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Abstract
The invention relates to a semi-circulation type gas-liquid multiphase flow contact method, in particular to a gas-liquid multiphase flow contact method which comprises a gas phase guide and disperse system, a semi-circulation line and a control system thereof as well as a phase contact and separate system. Through the method of the invention, a plurality of contact equipment and a plurality of separate equipment can have serial relation and also can have parallel relation at the same time. The method of the invention can be applied on the heterogeneous contact process of petroleum, chemical engineering, environmental protection and other fields with gas participation.
Description
Technical field
The present invention relates to a kind of semi-circulation type gas-liquid multiphase flow contact method, particularly a kind of gas-liquid polyphase flow contact method that uses gas phase introducing and decentralized system, half circulation line and control system thereof, joins and touch piece-rate system that comprises.The present invention can be used for GAS ABSORPTION, gas-liquid-liquid heterogeneous reaction, the liquid phase component stripping take gas as medium etc. the heterogeneous contact process in the fields such as the oil of gas participation, chemical industry, environmental protection.
Background technology
In the experiment such as Chemical Manufacture and environmental protection treatment and producing, often can run into the heterogeneous process that has gas to participate in, present realizing method mainly is the bubbling caldron process that adopts tubular type, tower or plural serial stage.But because the concrete difference of system and the difference of Aim of Process used, these methods tend to have certain limitation in actual applications.
At present representative gas-liquid contact process mainly contains chlorination reaction (such as the chlorination process take chlorine or hydrogen chloride as unstripped gas), hydrogenation reaction, oxidation reaction, unstripped gas purifying (such as unstripped gas desulfurization, carbon dioxide removal etc.), waste gas purification (such as discharging qi exhaustion chlorophenol, removal of mercaptans etc.), feed liquid air lift removing impurities (such as the hydrogen chloride in the nitrogen stripping feed liquid etc.) etc. in the commercial Application.For realizing Gas-Liquid Contacting and dispersion, need to overcome static pressure resistance and mobile transport resistance, this often requires the gas phase entrance to have higher pressure.In limited from the inlet to the outlet distance, the liquid phase average contact time is short, and the gas phase path is single and uncontrollable, in case gas phase flows out from outlet, the existence owing to Pressure Drop just is difficult to turn back to the original system that contacts.For improving mass transfer degree and the effect of gas-liquid two-phase, fully improve or reduce the concentration of object in gas phase, especially when gas phase is the toxic and harmfuls such as chlorine, hydrogen chloride, matter speed control situation reportedly adopts and reduces the gas admission velocity, increases gas liquid film or prolong the means such as average gas-liquid contact time.
In the gas-liquid polyphase flow contact process, the boundary area of gas-liquid contact, the gas average retention time in liquid phase is the index of two keys, and these two index comprehensives show as the size of what and device processes ability of process gas unit consumption, and then have influence on the quality and cost of final products, even can cause the infeasible of whole production technology.I Man Jiang etc. has designed a kind of device for gas liquid reaction (ZL200520004702.3), adopt the bubbling filled column to realize gas-liquid contact reaction, but in application process, gas is in the ample supply of filled column different parts and fully absorb and be difficult to satisfactory to both partiesly, and this will directly have influence on design and use control of equipment.Zhang Jingang etc. have designed a kind of gas-liquid/gas-liquid-solid reaction unit (ZL200820124219.2), utilize and stir the abundant contact that the negative pressure that forms realizes gas-liquid, the people such as Xiao Jin have designed a centrifugal gas-liquid reaction unit, utilize centrifugal blower to introduce gas in liquid, the two exists all that device structure is complicated, the gas soakage is little and is difficult to the problem such as control.In addition, how to realize gas ample supply and the utilization of multipoles reactors, these reports are not considered yet.
Make up one and have better applicability, controlled and efficient gas-liquid polyphase flow contact method, not only can improve the efficient of original production, can also further expand the gas-liquid polyphase flow process in the industrial applications scope in the fields such as chemical industry, environmental protection, even solve relevant industrialization bottleneck problem.
Summary of the invention
For overcoming the deficiencies in the prior art, the invention provides a kind of semi-circulation type gas-liquid multiphase flow contact method.The present invention can be used for GAS ABSORPTION, gas-liquid-liquid heterogeneous reaction, the liquid phase component stripping take gas as medium etc. the heterogeneous contact process in the fields such as the oil of gas participation, chemical industry, environmental protection.
Semi-circulation type gas-liquid multiphase flow contact method of the present invention comprises and uses gas phase to introduce and decentralized system that half circulation line and control system thereof are joined and touched piece-rate system.Described gas-liquid polyphase flow can be gas (or steam)-formed two phase flow of liquid, also can be the gas (or steam) that includes part solid content (such as catalyst)-formed multiphase flow of liquid-solid.
The used gas phase of the method for the invention is introduced and decentralized system, comprises that water rushes pump (jet pump) or gas compressor, and the parts such as supporting pipeline, valve.Gas is introduced function and can be utilized water to rush the forward pressure reduction that pump (jet pump) or gas compressor produce to realize.The gas that introducing obtains can rush the shearing force that pump produces by water to be disperseed in liquid phase; When gas pressure is larger, also can disperse in liquid phase with the bubbling form by aeration head.
Used half circulation line of the method for the invention and control system thereof are carried employed pipeline, valve except comprising fluid, also can comprise actual miscellaneous equipment space of playing the Fluid Transport effect.By pipeline setting and valve regulated, can allow many equipment rooms that contact both have series relationship, have simultaneously again relation in parallel, thereby can improve because of series relationship the degree of final two-phase mass exchange, also can avoid because of the parallel connection relation deficiency of fluid supply.The pipeline setting of simultaneously this half string half and relation also can realize the functions such as pressure balance between multiple devices.
The method of the invention is used joins that to touch piece-rate system can be the tankage system that simply has a constant volume and shape, also can be the device systems that has on this basis above-mentioned dispersion/separation function intensifying device.Touch in the piece-rate system joining, the degree of scatter that enters liquid-phase gas also can be by stirring, pump moving circulation, additional stops, the device such as guide shell is set strengthens, and the while also can prolong the average retention time of gas in liquid phase.When may having influence on when producing because mutually carrying secretly in the gas-liquid two-phase separation process, can the gas-liquid separation zone is set in the piece-rate system divide baffle plate (or annex etc.), add gas-liquid separator etc. and avoid joining to touching.
Touch in the separation equipment at different levels joining, liquid phase can be with same feed liquid through realizing multistage contacting with similar liquid phase half circulation line of gas phase and control system thereof, also can use different feed liquid respectively at different levels join to touching in the piece-rate system realize contacting with gas phase.Liquid phase material transmits between still, can adopt liquid level difference overflow type differential pressure transporting pattern to realize.In addition, each fluid temperature (F.T.) can be controlled by equipment chuck, coil pipe and pipeline heat exchanger.
The performing step of this method is:
1) gas enters from gas phase half circulation line entrance, first order gas phase introduce and the decentralized system effect under, gas phase is partly or entirely introduced, and then is dispersed and sends into the first order and join and touch piece-rate system;
2) touch piece-rate system joining, gas-liquid polyphase flow is kept certain boundary, realizes after the mass transfer of complete design, heat transfer and the reaction task separating, and gas phase comes back to gas phase half circulation line;
3) under gas phase half circulation line and control system effect thereof, gas phase can partly be returned the introducing of first order gas phase and decentralized system, partly be entered next stage gas phase drawing-in system, also can all return the introducing of first order gas phase and decentralized system or enter the next stage gas phase and introduce and decentralized system;
4) under gas phase half circulation line and control system effect thereof, gas phase introducings at different levels and decentralized system touch piece-rate system and all carry out similar operation with joining, finish respectively mass transfer, heat transfer and the reaction task of separately design, final gas phase is discharged through gas phase half circulation line and control system outlet thereof.
Should be noted that the technical foundation of the method for the invention is half circulation line and control system thereof.The statement of the process of front is to be gas phase at decentralized photo, and continuous phase is to carry out on the liquid phase basis.Semi-circulation type gas-liquid multiphase flow contact method of the present invention comprises that also decentralized photo is that liquid phase (such as spray, spraying) or two-phase are the continuous phase situation of (as rising film, falling liquid film).At this moment, on half circulation line and control system basis thereof, introduce mode by adjusting each phase fluid, the main equipment that contacts can be realized.
The invention has the beneficial effects as follows: 1) take the gas intake system as power, can introduce low-pressure gas to the feed liquid system, when introducing equipment is jet pump, also can realize simultaneously air feed, bubble crushing and stirring three functions; 2) under gas intake system and circulation line and control system effect thereof, absorption of gases can not join to touching in the separation equipment at separate unit and circulates, and wherein the coercibility component can be removed through condenser; 3) when liquid phase is same feed liquid, because the effect of reactive absorption and exhaust emissions, by half circulation line and control system thereof, the separate unit gas phase of touching circulation in the separation equipment of joining can be counter-current flow with the overflow liquid phase joining to touching between separation equipment again; 4) remove the gas of counter-current flow, each shortcoming part of touching the required gas of separation equipment internal reaction of joining can be provided with parallel form by half circulation line and control system thereof, this had both guaranteed the gas supply, had avoided again the excessive gas inhalation device high load capacity that causes of circulating flow rate and too much energy consumption; 5) by half circulation line and control system thereof, balance at different levels joining touch pressure in the separation equipment, for realization and the stable operation of flooding process provides guarantee.
Description of drawings
Below in conjunction with the drawings and specific embodiments the present invention is described in further detail.
Fig. 1 adopts water to rush pump (jet pump) provides power for gas phase FB(flow block).
Fig. 2 adopts gas compressor that the FB(flow block) of power is provided for gas phase.
Fig. 3 adopts spray to strengthen the FB(flow block) of gas-liquid contact.
Among the figure, 01, the total pipe unit entrance of gas phase, 02, unit circulating air entrance, 03, consersion unit gas phase entrance, 04, the gas phase dispersion mouth, 05, the consersion unit gaseous phase outlet, 06, unit circulating air outlet, 07, gas phase house steward's outlet, 08, unit liquid phase entrance, 09, unit circulation liquid-phase outlet, 10, gas phase recycle unit liquid phase entrance, 11, loop exit in the liquid phase, 12, the unit liquid-phase outlet, 13, consersion unit, 14, the liquid phase circulation pump, 15, the gas phase recycle unit, 1#, the gas-liquid contact system first module, 2#, the gas-liquid contact system second unit, 3#, gas-liquid contact system Unit the 3rd.
The specific embodiment
Take Fig. 1 as example:
Such as Fig. 1, the gas-liquid contact system first module that gas enters the semi-circulation type gas-liquid multiphase flow contact system from the total pipe unit entrance 01 of pipeline gas phase, can enter gas phase recycle unit 15 by consersion unit gas phase entrance 03 through unit circulating air entrance 02, pour consersion unit 13 with liquid from gas phase dispersion mouth 04, after this finishes gas-liquid contact, flow to unit circulating air outlet 06 from consersion unit gaseous phase outlet 05 and finish once circulation, and can export 07 follow-up unit or the link that flows to the semi-circulation type gas-liquid multiphase flow contact system through the gas phase house steward.Liquid enters consersion unit 13 from unit liquid phase entrance 08, under the driving of liquid phase circulation pump 14, can extract out from unit liquid phase entrance 09, enter gas phase recycle unit 15 at gas phase recycle unit liquid phase entrance 10, with gas loop exit 11 in the liquid phase, loop exit 11 overlaps with gas phase dispersion mouth 04 in this moment liquid phase, pour consersion unit 13 and finish 1 circulation, after this finishes gas-liquid contact, can flow out from unit liquid-phase outlet 12, enter follow-up unit or link.The gas phase recycle unit 15 here rushes pump for water.
In concrete the application, unit circulating air entrance 02 can directly communicate with consersion unit 13 to consersion unit gas phase entrance 03 pipeline, and can according to circumstances pipeline be simplified or adjust, as liquid phase circulation pump 14 being located at consersion unit 13 inside, unit circulating air entrance 02 direct and consersion unit 13; The position of unit circulating air entrance 02 and unit circulating air outlet 06 can be adjusted according to situation, such as place-exchange; Gas piping consersion unit gaseous phase outlet 05 can arrange heat exchanger to 06 section of unit circulating air outlet, with the control gas temperature, and condensable and separate the Partial Liquid Phase component of carrying secretly, isolated liquid phase can be returned consersion unit 13 or do its usefulness; Gas piping consersion unit gaseous phase outlet 05 also can arrange gas drying or purifier to 06 section of unit circulating air outlet, to keep the quality of gas, avoids the production problem brought thus, such as the etching apparatus pipeline, poisons catalyst etc.; Gas phase pipe-line cell circulating air entrance 02 exports 07 section to the gas phase house steward by-pass valve control can be set respectively to 06 section of unit circulating air outlet, unit circulating air outlet 06 to 06 section of unit circulating air outlet, unit circulating air entrance 02 to 03 section of consersion unit gas phase entrance, consersion unit gaseous phase outlet 05, thereby realize the control to system's internal pressure, gas flow and gas flow, when set valve is normal closing, can simplify or adjust it, as this pipeline section no longer is set; Liquid phase circulation pipe-line cell liquid phase entrance 09 can arrange heat exchanger to 10 sections of gas phase recycle unit liquid phase entrances, with control system temperature better; The inlet units liquid phase entrance 08 of feed liquid and unit liquid phase entrance 09 can be opened at the suitable position of consersion unit 13 or unit liquid phase entrance 09 to 10 sections pipelines of gas phase recycle unit liquid phase entrance, to satisfy the requirement of feeding and discharging according to situation; Can use separate liquid-phase system between each unit, also can connect the same feed liquid system that shares by pipeline; Consersion unit 13 can arrange the function intensified devices such as gas-liquid separator, guide shell, baffle plate, heat exchange coil, chuck, stirring, and according to needs relevant equipment opening and mouth is set.The semi-circulation type gas-liquid multiphase flow contact system can be made of multiple-unit, among Fig. 1 by two cell formations, each unit flow process can be identical or factually the border situation simplify respectively or adjust.
Take Fig. 2 as example:
The gas-liquid contact system first module that gas enters the semi-circulation type gas-liquid multiphase flow contact system from the total pipe unit entrance 01 of gas phase, can under the driving of gas phase recycle unit 15, flow to consersion unit gas phase entrance 03 by unit circulating air entrance 02, then pour consersion unit 13 from gas phase dispersion mouth 04, after this finishes gas-liquid contact, flow to unit circulating air outlet 06 from consersion unit gaseous phase outlet 05 and finish once circulation, and can export 07 follow-up unit or the link that flows to the semi-circulation type gas-liquid multiphase flow contact system through the gas phase house steward.Liquid enters consersion unit 13 from unit liquid phase entrance 08, after this finishes gas-liquid contact, can from 09 mouthful of outflow, enter follow-up unit or link.The gas phase recycle unit 15 here is compressor.
In concrete the application, unit circulating air entrance 02 can be adjusted to the position of unit circulating air outlet 06 according to situation, such as place-exchange; Gas piping consersion unit gaseous phase outlet 05 can arrange heat exchanger to 06 section of unit circulating air outlet, with the control gas temperature, and condensable and separate the Partial Liquid Phase component of carrying secretly, isolated liquid phase can be returned to join and touch separation equipment 1 or do its usefulness; Gas piping consersion unit gaseous phase outlet 05 also can arrange gas drying or purifier to 06 section of unit circulating air outlet, to keep the quality of gas, avoids the production problem (such as the etching apparatus pipeline, poisoning catalyst etc.) of bringing thus; Gas phase pipe-line cell circulating air entrance 02 exports 07 section to the gas phase house steward by-pass valve control can be set respectively to 06 section of unit circulating air outlet, unit circulating air outlet 06 to 06 section of unit circulating air outlet, unit circulating air entrance 02 to 03 section of consersion unit gas phase entrance, consersion unit gaseous phase outlet 05, thereby realize the control to system's internal pressure, gas flow and gas flow, when set valve is normal closing, can simplifies or adjust (as this pipeline section no longer is set) it; The consersion unit gas phase entrance 03 of gas and outlet 05 can be left suitable position at consersion unit 13 according to situation, to satisfy the requirement of intake and exhaust; The unit liquid phase entrance 08 of feed liquid and consersion unit gaseous phase outlet 05 can be opened suitable position at consersion unit 13 according to situation, to satisfy the requirement of feeding and discharging; Can use separate liquid-phase system between each unit, also can connect the same feed liquid system that shares by pipeline; Consersion unit 13 can arrange shower nozzle, gas-liquid separator, guide shell, baffle plate, heat exchange coil, chuck, stirring, filler, sieve plate, fall liquid level or rise the function intensified device such as liquid level, and according to needs arrange relevant equipment opening and mouthful; Consersion unit 13 also can be equipped with circulating pump, circulation line and shower nozzle, occurs with fountain equipment.The semi-circulation type gas-liquid multiphase flow contact system can be made of multiple-unit, as among Fig. 2 by two cell formations, each unit flow process can be identical or factually the border situation simplify respectively or adjust.
Below by 3 embodiment the present invention is described.
The toxic gas of chlorinated phenol is discharged in certain workshop, uses the semi-circulation type gas-liquid multiphase flow contact system with two processing units to process, and suction device is that water rushes pump, and absorption liquid is 5% sodium hydrate aqueous solution, and flow process can be with reference to the accompanying drawings 1.
Chlorophenol content is that the atmosphere gas of 500ppm enters the gas-liquid contact system first module for the treatment of system from the total pipe unit entrance 01 of pipeline gas phase, and flow is 300m
3/ h.Gas phase recycle unit 15 is for water rushes pump, and the inspiratory capacity that water rushes pump is 500m
3/ h, unstripped gas enters water through unit circulating air entrance 02 by consersion unit gas phase entrance 03 and rushes pump, pour tourie 1 with sodium hydroxide solution from gas phase dispersion mouth 04, gas flows to unit circulating air outlet 06 from consersion unit gaseous phase outlet 05 after gas-liquid separation in tank, export 06 portion gas at unit circulating air and flow to unit circulating air entrance 02, portion gas flows to the gas phase house steward and exports 07 and enter the second processing unit, and the content of chlorophenol is 10ppm in this moment gas.Repeat and the similar gas-liquid contact process of gas-liquid contact system first module at gas-liquid contact system the second processing unit, last gas exports 07 discharge the gas phase house steward of gas-liquid contact system second unit, and chlorophenol content is 0.1ppm in the Exhaust Gas.Liquid is counter-current flow with the general flow direction of series connection form and gas, advance from the tourie of gas-liquid contact system second unit, tourie to the gas-liquid contact system first module goes out, and the content of chlorophenol is about 30000ppm in the control efflux, and efflux goes to the workshop to reclaim chlorophenol.
Certain equipment is discharged the toxic gas that contains ammonia, use has the semi-circulation type gas-liquid multiphase flow contact system of two processing units and processes, the absorption liquid of gas-liquid contact system first module is water, the absorption liquid of gas-liquid contact system second unit is 5% dilute sulfuric acid, suction device is air blast, and gas-liquid polyphase flow contact flow process can be with reference to the accompanying drawings 2.
Ammonia level is that the atmosphere gas of 15% (v/v) enters the gas-liquid contact system first module for the treatment of system from the total pipe unit entrance 01 of pipeline gas phase, and flow is 200m
3/ h.Gas phase recycle unit 15 is air blast, and the air-blowing amount of air blast is 300m
3/ h, blast is the 3.5m water column, unstripped gas enters air blast through unit circulating air entrance 02, arrive the gas phase dispersion mouth 04 of tourie bottom from consersion unit gas phase entrance 03, be scattered in the tourie bottom through gas phase dispersion mouth 04 bubbling, gas flows to unit circulating air outlet 06 from consersion unit gaseous phase outlet 05 after gas-liquid separation in tank, export 06 portion gas at unit circulating air and flow to unit circulating air entrance 02, portion gas flows to the gas phase house steward and exports 07 and enter the gas-liquid contact system second unit, and this moment, the content of ammonia in gas gas was 2% (v/v).Repeat and the similar gas-liquid contact process of first module at the gas-liquid contact system second unit, the ammonia in gas gas content that exports discharge the gas phase house steward of gas-liquid contact system second unit is 0% (v/v).The feed liquid of gas-liquid contact system first module and gas-liquid contact system second unit is independently regulation and control separately, and ammonia concn is 20% in the control gas-liquid contact system first module feed liquid, and sulfuric acid concentration is 5% in the gas-liquid contact system second unit feed liquid.It is deionized water that gas-liquid contact system first module tourie stream adds absorption liquid, and efflux is 20% ammoniacal liquor; It is the concentrated sulfuric acid that gas-liquid contact system second unit tourie stream adds absorption liquid, regularly removes the solid ammonium sulfate of tourie bottom deposition, and the discharge section waste liquid, and it is 20 ℃ that circulating-pump outlet is established heat exchanger control feed temperature.
Certain equipment is discharged the toxic gas of containing hydrogen chloride, use has the semi-circulation type gas-liquid multiphase flow contact system of three processing units and processes, the absorption liquid of gas-liquid contact system first module and gas-liquid contact system second unit is water, the absorption liquid of gas-liquid contact system Unit the 3rd is 5% sodium hydrate aqueous solution, suction device is air blast, and gas-liquid polyphase flow contact flow process can be with reference to the accompanying drawings 3.
Hydrogen chloride content is that the atmosphere gas of 30% (v/v) enters the gas-liquid contact system first module for the treatment of system from the total pipe unit entrance 01 of pipeline gas phase, and flow is 100m
3/ h.Gas phase recycle unit 15 is air blast, and the air-blowing amount of air blast is 150m
3/ h, blast is the 3m water column, consersion unit 13 is spray absorber, unstripped gas enters air blast through unit circulating air entrance 02, entered by the consersion unit gas phase entrance 03 of being located at the spray absorber bottom, be scattered in the spray-absorption tower bottom through 0 gas phase dispersion mouth 4, gas flows to unit circulating air outlet 06 from consersion unit gaseous phase outlet 05 after gas-liquid separation in tank, export 06 portion gas at unit circulating air and flow to unit circulating air entrance 02, portion gas flows to the gas phase house steward and exports 07 and enter the gas-liquid contact system second unit, and the content of hydrogen chloride is 3% (v/v) in this moment gas.Repeat and the similar gas-liquid contact process of first module at the second and the 3rd processing unit, export the gas phase house steward of gas-liquid contact system second unit that hydrogen chloride content is 0.1% (v/v) in the gas of discharge, the gas phase house steward of gas-liquid contact system Unit the 3rd exports that hydrogen chloride content is 0 in 07 gas of discharging.The feed liquid series flow of gas-liquid contact system first module and gas-liquid contact system second unit, water enters the gas-liquid contact system second unit from the spray column jacking, beat to gas-liquid contact system first module spray cat head through the circulating pump branch road, the circulating pump branch road of this spray column is returned the workshop use with the by-product hydrochloric acid form at last.The diluted alkaline of gas-liquid contact system Unit the 3rd is independently regulated and control, and replenishes the industrial lye of 30%wt, regularly removes the solid sodium chloride of spray column bottom deposition, and the discharge section waste liquid, and it is 25 ℃ that circulating-pump outlet is established heat exchanger control feed temperature.Hydrogen cloride concentration is 30% in the control gas-liquid contact system first module feed liquid, and hydrogen cloride concentration is 10% in the gas-liquid contact system second unit feed liquid, and naoh concentration is 5% in gas-liquid contact system the 3rd unit feed liquid.
Claims (5)
1. semi-circulation type gas-liquid multiphase flow contact method, it comprises uses the gas phase drawing-in system, and half circulation line and control system thereof are joined and are touched piece-rate system, the steps include:
1) gas enters from gas phase half circulation line entrance, and under the effect of first order gas phase drawing-in system, gas phase is partly or entirely introduced, and then is dispersed and sends into the first order and join and touch piece-rate system;
2) touch piece-rate system joining, gas-liquid polyphase flow is kept certain boundary, realizes after the mass transfer of complete design, heat transfer and the reaction task separating, and gas phase comes back to gas phase half circulation line;
3) under gas phase half circulation line and control system effect thereof, gas phase can partly be returned first order gas phase drawing-in system, part enters next stage gas phase drawing-in system, perhaps all returns first order gas phase drawing-in system or enters next stage gas phase drawing-in system;
4) under gas phase half circulation line and control system effect thereof, gas phase drawing-in systems at different levels touch piece-rate system and all carry out similar operation with joining, finish respectively mass transfer, heat transfer and the reaction task of separately design, final gas phase is discharged through gas phase half circulation line and control system outlet thereof.
2. a kind of semi-circulation type gas-liquid multiphase flow contact method according to claim 1 is characterized in that, introduces functional utilization water in the described gas phase drawing-in system and rushes pump or gas compressor realization, and divergent function utilizes aeration head or fluid shearing to realize.
3. a kind of semi-circulation type gas-liquid multiphase flow contact method according to claim 1 is characterized in that, describedly joins that to touch piece-rate system be to have the device systems that device is divided in stirring, baffle plate, guide shell, gas-liquid separator or zone.
4. a kind of semi-circulation type gas-liquid multiphase flow contact method according to claim 1, it is characterized in that described gas-liquid polyphase flow is the formed two phase flow of gas or steam-liquid, include the formed multiphase flow of gas/vapor-liquid-solid of part solid content.
5. a kind of semi-circulation type gas-liquid multiphase flow contact method according to claim 1, it is characterized in that, touch in the piece-rate system in described joining at different levels, liquid phase uses same feed liquid to realize multistage contacting through and similar liquid phase half circulation line of gas phase and control system thereof, perhaps use different feed liquid respectively at different levels join to touching in the piece-rate system realize contacting with gas phase.
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|---|---|---|---|---|
| EP0249400A1 (en) * | 1986-06-07 | 1987-12-16 | Sankyo Kogyo Co., Ltd. | Gas-liquid contacting apparatus |
| US5602297A (en) * | 1995-02-08 | 1997-02-11 | Wang; Chi-Shang | Multistage double closed-loop process for waste decontamination |
| CN1386573A (en) * | 2002-03-13 | 2002-12-25 | 周喜荣 | Gas circulating chemical reactor with vertical baffling and its application method |
| CN1399619A (en) * | 1999-11-26 | 2003-02-26 | 英国石油勘探运作有限公司 | Process for converting synthesis gas into higher hydrocarbons |
| CN1962043A (en) * | 2006-10-27 | 2007-05-16 | 中国科学院广州能源研究所 | A gas hydrate high-speed preparation method and device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20020158009A1 (en) * | 2001-04-30 | 2002-10-31 | Khudenko Boris M. | Volatile acid transfer in biological-abiotic processes |
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Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0249400A1 (en) * | 1986-06-07 | 1987-12-16 | Sankyo Kogyo Co., Ltd. | Gas-liquid contacting apparatus |
| US5602297A (en) * | 1995-02-08 | 1997-02-11 | Wang; Chi-Shang | Multistage double closed-loop process for waste decontamination |
| CN1399619A (en) * | 1999-11-26 | 2003-02-26 | 英国石油勘探运作有限公司 | Process for converting synthesis gas into higher hydrocarbons |
| CN1386573A (en) * | 2002-03-13 | 2002-12-25 | 周喜荣 | Gas circulating chemical reactor with vertical baffling and its application method |
| CN1962043A (en) * | 2006-10-27 | 2007-05-16 | 中国科学院广州能源研究所 | A gas hydrate high-speed preparation method and device |
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