CN1283349C - Highly effective slurry phase bed reactor - Google Patents
Highly effective slurry phase bed reactor Download PDFInfo
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- CN1283349C CN1283349C CN 200410012366 CN200410012366A CN1283349C CN 1283349 C CN1283349 C CN 1283349C CN 200410012366 CN200410012366 CN 200410012366 CN 200410012366 A CN200410012366 A CN 200410012366A CN 1283349 C CN1283349 C CN 1283349C
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- inner sleeve
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- 239000002002 slurry Substances 0.000 title claims abstract description 45
- 238000010438 heat treatment Methods 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000005315 distribution function Methods 0.000 claims abstract 5
- 238000010992 reflux Methods 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 abstract description 53
- 238000006243 chemical reaction Methods 0.000 abstract description 26
- 239000002904 solvent Substances 0.000 abstract description 24
- 230000009467 reduction Effects 0.000 abstract description 7
- 239000007787 solid Substances 0.000 abstract description 5
- 238000002156 mixing Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 230000009257 reactivity Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 82
- 230000000694 effects Effects 0.000 description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008878 coupling Effects 0.000 description 3
- 238000010168 coupling process Methods 0.000 description 3
- 238000005859 coupling reaction Methods 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000009955 starching Methods 0.000 description 2
- 230000007306 turnover Effects 0.000 description 2
- 238000013019 agitation Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
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Abstract
本发明涉及一种高效浆态床反应器，属于化工机械领域。它主要由固液分离器，变径内套，反应器外套，带内构件的换热器，带喷嘴的升气管，具有加热和气体分布作用的内套筒，防堵喷嘴，喷嘴安装板，换热器，加热盘管出口，二次分布板，加热盘管等构成。本发明的有益效果是，反应器分布器不易堵塞，气液混合均匀，气固接触充分，反应效率高，催化剂和溶剂的携带量很小，不易出现偏流、沟流和死床，浆液流动速度快，反应器内浆液的粘度基本一致，反应热能够及时移出，尤其在催化剂还原升温阶段易实现反应器的平稳操作，另外，原料气在反应器内沿轴向的分布与催化剂浓度基本一致，使催化剂发挥最大的反应活性，反应器的空间得到充分利用。
The invention relates to a high-efficiency slurry bed reactor, which belongs to the field of chemical machinery. It mainly consists of a solid-liquid separator, a variable-diameter inner sleeve, a reactor jacket, a heat exchanger with internal components, a gas riser with nozzles, an inner sleeve with heating and gas distribution functions, anti-blocking nozzles, nozzle mounting plates, Heat exchanger, heating coil outlet, secondary distribution plate, heating coil, etc. The beneficial effects of the present invention are that the distributor of the reactor is not easily blocked, the gas-liquid mixing is uniform, the gas-solid contact is sufficient, the reaction efficiency is high, the carrying amount of the catalyst and the solvent is small, the bias flow, channel flow and dead bed are not easy to occur, and the slurry flow rate Fast, the viscosity of the slurry in the reactor is basically the same, and the heat of reaction can be removed in time, especially in the stage of catalyst reduction and temperature rise, it is easy to realize the stable operation of the reactor. In addition, the distribution of the feed gas in the reactor along the axial direction is basically the same as the concentration of the catalyst. The catalyst can maximize its reactivity, and the space of the reactor can be fully utilized.
Description
One, technical field
The present invention relates to a kind of paste state bed reactor that is suitable for producing chemicals such as dimethyl ether and methyl alcohol, belong to chemical machinery field.
Two, background technology
Paste state bed reactor is a kind of novel chemical reaction device, the power source that it utilizes unstripped gas to mix as reaction, with the atent solvent is carrier, the catalyst dispersion suspension is reacted in solvent, the consersion unit of this kind pattern is not owing to there is mechanical agitation, thereby can not have to leak under HTHP and move.Because adopt the carrier of atent solvent as dispersed catalyst, thermal capacitance is big, help reaction temperature steadily because the strong disturbance effect of gas in bed arranged, thereby reaction heat can in time shift out, and avoids occurring the bed focus, prolongs life of catalyst.Existing paste state bed reactor causes bias current, channel even the dead bed of reaction bed because the restriction of distributor is often stopped up.In addition, because bed structure is unreasonable, bed bottom solvent reduces with the operation of reactor, also easily causes the reactor bottom slurry viscosity excessive, forms bias current, channel and even dead bed.Also have, because project organization is unreasonable, a large amount of catalyst and solvent are carried to the outside of reactor by gas, influence the operation and the production of reactor greatly.
Because slurry attitude bed adopts gas to carry out the stirring and the mixing of material, so the quality of the distribution of gas is directly connected to the success or failure of bed.Before slurry attitude bed goes into operation, need to carry out the filling of catalyst,, often cause the obstruction of bottom distribution device in gas-fluid, influence the operation of bed because viscosity is bigger at low temperatures after catalyst and the solvent; When catalyst reduction owing to can not carry out indirect to bed, adding heat mainly is the heat that is carried by the high-temperature gas that the bed bottom constantly is blown into, make the solvent loss of reactor bottom cause the viscosity of slurry attitude to increase like this, the gas distribution elements of device bottom of also inducing reaction is easily stopped up, and, cause carrying in a large number of catalyst and solvent because the gas volume of turnover reactor changes not quite; When producing, also can make the viscosity of bed slurries change the obstruction that causes gas distribution elements, cause starching the bias current and even the channel of attitude bed bed owing to the bed operation is unstable, even dead bed.In addition, traditional slurry attitude bed can not be realized the interior circulation of an interior slurries, and concentration of slurry and viscosity profile are inhomogeneous in the bed, and gas holdup is low, and gas-liquid-solid contact is insufficient, thereby the efficient and the conversion ratio of reaction are lower.
The attitude bed is closely-related to be on the other hand with starching, because the design of tradition slurry attitude bed does not consider that unstripped gas is in the axial distribution of reactor, cause unstripped gas concentration to reduce gradually vertically, and catalyst concentration axially reduces little along reactor, catalyst does not just make full use of like this, therefore be necessary very much the distribution of concentration in reactor of unstripped gas adjusted, make it and the catalyst concentration coupling, give full play to the effect of catalyst.Because reactor is integrated design, the gas that arrives top routinely must be through the bottom of reactor, yet the gas through reactor bottom is wanted and catalyst reaction certainly, therefore the concentration of fresh feed gas also can reduce, like this can be lower with the unstripped gas concentration of catalyst reaction, therefore the utilization rate of reactor top catalyst is lower, for whole reactor, has reduced the utilization rate of the reaction efficiency and the reactor of reactor.
Three, summary of the invention
The object of the invention is to overcome that existing paste state bed reactor catalyst and solvent carry and be prone to bias current, channel and dead bed in a large number and the improper running that causes reactor.The invention provides a kind of paste state bed reactor, this reactor distributor is difficult for stopping up, the amount of carrying of catalyst and solvent is very little, be not prone to bias current, channel and dead bed, the viscosity basically identical of slurries in the reactor, reaction heat can in time shift out, especially in the quiet run of easy realization response device of catalyst reduction temperature rise period.
Be the utilization rate of raising catalyst in reactor and the space utilization efficient of reactor, the invention provides a kind of scheme that increases reactor middle and upper part unstripped gas concentration, make the concentration of unstripped gas axially relatively more even at reactor, with the comparison match that concerns of catalyst concn, the high efficiency utilization of realization response device and catalyst.
Efficient reactor with paddle bed of the present invention, it is characterized in that it being by solid-liquid separator 2, cover 3 in the reducing, reactor jacket 4, the heat exchanger 5 of band inner member, the riser 6 of band nozzle, inner sleeve 7 with heating and distribution of gas effect, anti-blocking nozzle 8, the nozzle installing plate 9 of head type structure and quadratic distribution plate 13 constitute, the inner member of the interior circulation that realizes slurries is set in this reactor, comprises cover 3 in the reducing, inner sleeve 7 with heating and distribution of gas effect, the nozzle installing plate 9 of head type structure, make gas along the axial equally distributed riser 6 of reactor, secondary air distribution grid 13 and the solid-liquid separator 2 of realizing the quadratic distribution of gas constitute.
Above-mentioned efficient reactor with paddle bed is characterized in that described anti-blocking nozzle 8 outlets have a ball body that prevents that slurries from flowing backwards, and its diameter is 1.1～1.3 times of nozzle trunnion.
Above-mentioned efficient reactor with paddle bed is characterized in that the nozzle installing plate 9 of its described head type structure is tangent with reactor wall, forms a smooth slurry reflux passage with reactor wall.
Above-mentioned efficient reactor with paddle bed is characterized in that its described inner sleeve 7 with heating and distribution of gas effect is to be formed by the coil pipe coiling, and the distance between the coil pipe changes to the coil pipe caliber from zero from bottom to top.
Above-mentioned efficient reactor with paddle bed, a tube diameter that it is characterized in that the heat exchanger 5 of cover 3 in its described reducing, band inner member and have an inner sleeve 7 of heating and distribution of gas effect changes to 0.8～1 times of reactor diameter from 0.4～0.6 times of reactor diameter respectively from the bottom to top along reactor.
Above-mentioned efficient reactor with paddle bed is characterized in that the inside that its described riser 6 is mounted in reactor directly links to each other with unstripped gas inlet 15, and the top has side opening, and its side opening aperture is consistent with the side opening aperture of anti-blocking nozzle 8.
Above-mentioned efficient reactor with paddle bed is characterized in that its described gas quadratic distribution plate 13 is positioned at the middle part of reactor.
The invention has the beneficial effects as follows, the reactor distributor is difficult for stopping up, gas-liquid mixed is even, the gas-solid full contact, the reaction efficiency height, the amount of carrying of catalyst and solvent is very little, be not prone to bias current, channel and dead bed, the slurries flowing velocity is fast, the viscosity basically identical of slurries in the reactor, reaction heat can in time shift out, especially in the quiet run of easy realization response device of catalyst reduction temperature rise period, in addition, unstripped gas vertically distribution and catalyst concn basically identical in reactor, making the maximum reactivity of catalyst performance, is fully used in the space of reactor.
Four, description of drawings
Fig. 1 is the internal structure profile diagram of efficient reactor with paddle bed, 1-product gas outlet, 2-solid-liquid separator, cover in the 3-reducing, 4-reactor jacket, the heat exchanger of 5-band inner member, the riser of 6-band nozzle, 7-has the inner sleeve of heating and distribution of gas effect, the anti-blocking nozzle of 8-, the nozzle installing plate of 9-head type structure, 10-heat exchanger entrance, 11-heat exchanger exit, the outlet of 12-heat(ing) coil, 13-quadratic distribution plate, 14-heat(ing) coil inlet, 15-unstripped gas inlet.
Five, the specific embodiment
Embodiment one:
Efficient reactor with paddle bed of the present invention, by solid-liquid separator 2, cover 3 in the reducing, reactor jacket 4, the heat exchanger 5 of band inner member, the riser 6 of band nozzle, inner sleeve 7 with heating and distribution of gas effect, anti-blocking nozzle 8, the nozzle installing plate 9 of head type structure and quadratic distribution plate 13 constitute, the inner member of the interior circulation that realizes slurries is set in this reactor, comprises cover 3 in the reducing, inner sleeve 7 with heating and distribution of gas effect, the nozzle installing plate 9 of head type structure, make gas along the axial equally distributed riser 6 of reactor, secondary air distribution grid 13 and the solid-liquid separator 2 of realizing the quadratic distribution of gas constitute.Anti-blocking nozzle 8 outlets have a ball body that prevents that slurries from flowing backwards, and its diameter is 1.1 times of nozzle trunnion.The nozzle installing plate 9 of head type structure is tangent with reactor wall, forms a smooth slurry reflux passage with reactor wall.Inner sleeve 7 with heating and distribution of gas effect is to be formed by the coil pipe coiling, and the distance between the coil pipe changes to the coil pipe caliber from zero from bottom to top.The heat exchanger 5 of cover 3, band inner member and a tube diameter with inner sleeve 7 of heating and distribution of gas effect change to 0.8 times of reactor diameter from 0.4 times of reactor diameter respectively from the bottom to top in the reducing.The inside that riser 6 is mounted in reactor directly links to each other with unstripped gas inlet 15, and top has side opening, and its side opening aperture is consistent with the side opening aperture of anti-blocking nozzle 8.Gas quadratic distribution plate 13 is positioned at the middle part of reactor.
After gas enters bed by anti-blocking nozzle 8, part gas reacts at the bottom and the catalyst of reactor, reacted gas distributes once more through the secondary air distribution grid 13 in the cover in being located in uphill process, bubble diameter diminishes, reaction contact area increases, become comparatively fierce through the gas post-reactor middle and lower part catalytic reaction that distributes once more, partial raw gas is by reaction consumes, because synthetic reaction is the reaction that a molecular number reduces, so the gas volume that rises reduces, the concentration that arrives the unstripped gas of reactor middle and upper part reduces.Because the induced effect of gas flow rate, slurries in the bed carry out violent mixing, when gas continues to rise, gas flow rate reduces, catalyst with contact the back with reactor jacket tube 4 after solvent is carried to top and flow downward along wall, Di Bu catalyst slurry has just obtained replenishing timely like this, and concentration of slurry and viscosity in the bed are consistent substantially.When gas flow rate is big, part catalyst and solvent are taken to the top of reactor by gas, arrive the interior cover 3 of reducing on top through heat exchanger 5 backs, same gas flow velocity behind reducing continues to reduce, catalyst and solvent flow downward along reactor wall once more, replenish lower catalytic agent and solvent, circulation in whole reactor inner catalyst and solvent just can be realized like this, concentration of slurry and viscosity just can be consistent substantially.When gas flow rate continues to increase, after still can not get separating behind the cover 3 in the reducing on part catalyst and solvent process reactor top, will enter the solid-liquid separator 2 on reactor top, through behind the solid-liquid separator 2, catalyst and solvent can flow back to reactor.Another part gas that is risen by reactor bottom passes through the middle part that riser 6 arrives reactors, because a series of apertures have been opened in the side, top of riser, gas is becoming tiny bubble after small holes, it is big that the gas holdup of the middle part fresh feed gas of feasible reaction becomes, replenished because reducing of bottom reactor feed gas concentration makes catalyst concn and unstripped gas concentration coupling.Because gas transverse and catalyst slurry carry out solid mass-transferring and reaction, the utilization rate of middle part catalyst and the utilization rate of space reactor have so just been improved simultaneously.
Embodiment two:
Efficient reactor with paddle bed of the present invention, anti-blocking nozzle 8 outlets have a ball body that prevents that slurries from flowing backwards, and its diameter is 1.2 times of nozzle trunnion.The nozzle installing plate 9 of head type structure is tangent with reactor wall, forms a smooth slurry reflux passage with reactor wall.Inner sleeve 7 with heating and distribution of gas effect is to be formed by the coil pipe coiling, and the distance between the coil pipe changes to the coil pipe caliber from zero from bottom to top.The heat exchanger 5 of cover 3, band inner member and a tube diameter with inner sleeve 7 of heating and distribution of gas effect change to 0.9 times of reactor diameter from 0.5 times of reactor diameter respectively from the bottom to top along reactor in the reducing.The inside that riser 6 is mounted in reactor directly links to each other with unstripped gas inlet 15, and top has side opening, and its side opening aperture is consistent with the side opening aperture of anti-blocking nozzle 8.Gas quadratic distribution plate 13 is positioned at the middle part of reactor.
When carrying out the reduction of catalyst, because the gas flow of turnover reactor differs less, the interior gas flow rate of reactor changes less, is easy to form carrying of catalyst and solvent.The bed heating is that the reducing gases that is blown into by the bottom provides in addition, and a large amount of high temperature reduction gas enter reactor bottom the bottom slurries are blown strongly, cause the bottom slurry viscosity excessive, form bias current and dead bed easily.This reactor is owing to overlap variable-diameter structure and top solid-liquid separator in having, gas flow rate has a distribution on bed is axial, avoid carrying of catalyst and solvent, make catalyst and solvent form interior circulation, keep the slurry viscosity unanimity in the reactor at inside reactor.Because the nozzle installing plate of reactor bottom adopts the head type structure, can not form the dead band when catalyst slurry flows to reactor bottom downwards in addition, catalyst slurry refluxes smooth, in time the solvent and the catalyst of post-reactor bottom.In addition, because the reactor bottom inner sleeve is to be formed by the coil pipe coiling, therefore also can feed high-temperature gas in the coil pipe bed is carried out indirect, avoid utilizing the raising gas flow to remedy carrying in a large number owing to not enough catalyst that causes of bed heating and solvent.Simultaneously, because the reducing gases that enters from reactor bottom is at first reacted with the catalyst of reactor bottom, make the density of hydrogen in the reducing gases reduce, therefore be necessary the top density of hydrogen is replenished, then can realize by the middle part that riser arrives reactor by another part gas that reactor bottom rises, because the upper side of riser has been opened a series of apertures, gas is becoming tiny bubble after small holes, it is big that the gas holdup of the fresh reducing gases in middle part of feasible reaction becomes, replenished because reducing of bottom reaction density of hydrogen makes catalyst concn and density of hydrogen coupling.Because gas transverse and catalyst slurry carry out solid mass-transferring and reaction, so just improved the utilization rate of middle part catalyst and the utilization rate of space reactor simultaneously, made catalyst reduction more all even fully, for reaction lays a good foundation.
Embodiment three:
Efficient reactor with paddle bed of the present invention, anti-blocking nozzle 8 outlets have a ball body that prevents that slurries from flowing backwards, and its diameter is 1.3 times of nozzle trunnion.The nozzle installing plate 9 of head type structure is tangent with reactor wall, forms a smooth slurry reflux passage with reactor wall.Inner sleeve 7 with heating and distribution of gas effect is to be formed by the coil pipe coiling, and the distance between the coil pipe changes to the coil pipe caliber from zero from bottom to top.The heat exchanger 5 of cover 3, band inner member and a tube diameter with inner sleeve 7 of heating and distribution of gas effect change to 1 times of reactor diameter from 0.6 times of reactor diameter respectively from the bottom to top along reactor in the reducing.The inside that riser 6 is mounted in reactor directly links to each other with unstripped gas inlet 15, and top has side opening, and its side opening aperture is consistent with the side opening aperture of anti-blocking nozzle 8.Gas quadratic distribution plate 13 is positioned at the middle part of reactor.
Claims (7)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410012366 CN1283349C (en) | 2004-06-25 | 2004-06-25 | Highly effective slurry phase bed reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410012366 CN1283349C (en) | 2004-06-25 | 2004-06-25 | Highly effective slurry phase bed reactor |
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|---|---|
| CN1593740A CN1593740A (en) | 2005-03-16 |
| CN1283349C true CN1283349C (en) | 2006-11-08 |
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| CN 200410012366 Expired - Fee Related CN1283349C (en) | 2004-06-25 | 2004-06-25 | Highly effective slurry phase bed reactor |
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Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102416307B (en) * | 2010-09-27 | 2015-09-23 | 中国石油化工股份有限公司 | A kind of internal-circulation type paste state bed reactor and application thereof |
| CN101979475B (en) * | 2010-10-26 | 2013-05-29 | 太原理工大学 | Process for synthesizing natural gas by performing methanation on coke oven gas |
| CN101979476B (en) * | 2010-10-26 | 2013-05-29 | 赛鼎工程有限公司 | A process for coal-to-synthesis gas to be methanated to synthesize natural gas |
| CN103962069B (en) * | 2013-01-31 | 2017-03-08 | 中国科学院上海高等研究院 | A kind of paste state bed reactor |
| CN103962067B (en) * | 2013-01-31 | 2017-02-08 | 中国科学院上海高等研究院 | Method for carrying out slurry bed reaction |
| CN104923132B (en) * | 2015-05-05 | 2017-11-28 | 中国石油大学(华东) | Circulating Slurry Reactor circulation flow reactor in a kind of gas-liquid charging |
| CN107175050A (en) * | 2017-03-27 | 2017-09-19 | 五邑大学 | A kind of efficient heterophase reactor |
| CN107126910A (en) * | 2017-03-27 | 2017-09-05 | 五邑大学 | A kind of novel pulpous bed reactor |
| CN107254327B (en) * | 2017-06-05 | 2021-12-17 | 中石化宁波工程有限公司 | Fischer-Tropsch synthetic oil process |
| CN109317058A (en) * | 2018-10-19 | 2019-02-12 | 江门市崖门新财富环保工业有限公司 | A kind of nozzle of novel pulpous bed gas reactor distributor |
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- 2004-06-25 CN CN 200410012366 patent/CN1283349C/en not_active Expired - Fee Related
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