CN201454503U - Axial flow fixed bed gas-solid catalytic reactor - Google Patents
Axial flow fixed bed gas-solid catalytic reactor Download PDFInfo
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- CN201454503U CN201454503U CN2009200744482U CN200920074448U CN201454503U CN 201454503 U CN201454503 U CN 201454503U CN 2009200744482 U CN2009200744482 U CN 2009200744482U CN 200920074448 U CN200920074448 U CN 200920074448U CN 201454503 U CN201454503 U CN 201454503U
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- 239000007787 solid Substances 0.000 title abstract 3
- 239000011949 solid catalyst Substances 0.000 claims description 35
- 239000000945 filler Substances 0.000 claims description 20
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Abstract
The utility model relates to an axial flow fixed bed gas-solid catalytic reactor aiming at solving the problems that because reactant gas flow distributes unevenly and backflows after passing through a gas pre-distributor on the inlet of a fixed bed reactor, the gas flow in the catalyst bed layer of the reactor distributes unevenly, the catalyst can not be utilized evenly and completely, and moreover, the pressure drop loss of the reactor is larger in the prior art. In the utility model, the axial flow fixed bed reactor provided with a two-stage holed-baffle type inlet gas pre-distributor is adopted, the inlet gas pre-distributor comprises a distributor barrel (13), a multi-hole upper baffle (15) and a multi-hole lower baffle (17); the multi-hole upper baffle (15) and the multi-hole lower baffle (17) are homocentric oval baffles or sphere baffles in up and down cascading; the distributor cylinder (13) and the upper baffle as well as the upper baffle and lower baffle are both connected through vertical tiepieces and both form sidewise annular gaps, thereby better solving the problems. The utility model can be used for gas-solid catalytic reaction.
Description
Technical field
The utility model relates to a kind of axial flow fixed bed gas-solid catalyst reactor, particularly about a kind of axial flow fixed bed gas-solid catalyst reactor that can be used for the producing ethylene glycol from hydrogenation of oxalic ester catalytic reaction.
Background technology
As everyone knows, the industrial chemistry DESIGN OF REACTOR comprises the chemical reaction of its inside generation and the understanding of mobile two aspects of fluid.The former is a Chemical Problem, and the latter then belongs to engineering problem.These two aspect close ties influence each other.It is the smooth assurance of chemical reaction that good fluid flows.
Gu axial flow fixed bed gas-solid catalyst reactor is one of common industrial gas/catalytic reactor pattern.It is made up of sections such as inlet gas pre-distributor, homogenizing space, fixed bed (comprising beds and inert filler layer) and exit gas collection sections vertically usually.Characteristics such as have the flowing near piston flow of bed inner fluid, simple in structure, easy to operate, investment cost is low, and catalyst mechanical wear is little in the bed.
One of important symbol of axial flow fixed bed gas-solid catalyst reactor performance quality is that can the catalyst at each position in the beds obtain even utilization.A poorly designed axial flow fixed bed gas-solid catalyst reactor, can be because the air-flow skewness, make and occur dead band and short circuit in the beds, cause a part of catalyst excess load and too early inactivation, another part catalyst but works hardly, thereby cause entire reaction course deterioration in the reactor, reactor performance descends.
For many years, Gu the hydrodynamics behavior of commercial fixed bed gas/catalytic reactor is subjected to researchers' attention always.In early days, because plant layout is less, reactor diameter is little, and the uniform fluid distribution problem is outstanding, and the concentrating on of people involves the estimation that the fixed bed pressure of Fan Selection and power consumption falls.In recent years, along with the development of petro chemical industry and the expansion of scale, factory's single line production capacity maximizes day by day, shows outstanding the airflow uniform distribution problem day of the axial flow fixed bed gas-solid catalyst reactor of major diameter, and comes into one's own.Both at home and abroad the researcher studies the uniform effect of the inlet gas pre-distributor of axial flow fixed bed gas-solid catalyst reactor and inert filler layer etc.The inlet gas pre-distributor of various types is proposed.U.S. Howard F.Rase shows " chemical reactor design " (Chinese translation, Chemical Industry Press, December nineteen eighty-two) first volume (principle and method) the 190th page table 7-2 has been enumerated some inlet gas pre-distributor patterns, such as plate shaped single-stage baffle plate, multistage baffle plate (comprising dish-ring type, concentric circles bevel-type etc.), radial diffuser (comprising flat plate diffuser, vane diffuser and taper shutter etc.), screen cloth, porous plate, bar shaped sharp edge sieve plate and inert filler layer etc.These reactor on-board components that are used for improving the inlet air flow distribution situation are effective under specified conditions separately, played the effect that the inlet gas a fluid stream is come along the reactor radial dispersion, the high velocity jet air flow stream that has overcome the inflow reactor charging aperture is directly impacted beds, make beds central authorities form the disadvantage of pits (hole), radially the cross section forms the axial velocity profile of different uniformity coefficients in reactor.In the reactor on-board components, the most important thing is the inlet gas pre-distributor.As in the reactor of minor diameter, at the port of export of reactor inlet pipe a single-stage baffle plate gas pre-distributor is set and just can satisfies the equally distributed requirement of gas in the beds, but for the major diameter reactor, the gas pre-distributor that its Reactor inlet place is provided with requires than higher, single-stage baffle plate gas pre-distributor is difficult to satisfy the equally distributed requirement of air-flow in the beds, also must eliminate air-flow uneven distribution in the bed, cause the reactor pressure decrease loss bigger by thicker top inert filler layer.
Patent CN2675241 discloses a kind of conical single-stage baffle plate gas pre-distributor that is applied to axial flow fixed bed gas-solid catalyst reactor, with respect to the single-stage baffle plate gas pre-distributor described in " chemical reactor design " book, though improved the equally distributed degree of air-flow in the beds to a certain extent, but still there is certain backflow phenomenon at conical single-stage baffle plate periphery and bottom, still need thicker top inert filler layer to eliminate the interior air-flow uneven distribution of bed, the reactor pressure decrease loss is bigger.
Patent CN2075277 discloses a kind of combined type flow velocity uniform device, the same with the multistage baffle plate gas pre-distributor described in " chemical reactor design " book, when being applied to axial flow fixed bed gas-solid catalyst reactor, though it is relatively even that the air-flow in the beds distributes, but all exist the complex structure of gas pre-distributor, the shortcoming that the reactor pressure decrease loss is big.
Though the inlet gas pre-distributor of every kind of pattern generally all once had the people that it was carried out special testing research, this class research is carried out at inlet gas pre-distributor member itself mostly, and the testing research that carries out in conjunction with whole reactor then seldom.Even in conjunction with the research that a certain specific reactor carries out, because of the condition difference, the rule that it is summed up also is difficult to be applied to other reactor.
Shown in Figure 1 is typical axial flow fixed bed gas-solid catalyst reactor, and its inside comprises sections such as charging aperture, gas pre-distributor, homogenizing space, top, top inert filler layer, beds, bottom inert filler layer, supporting screening plate, homogenizing space, bottom and discharging opening from top to bottom.These section close ties, influence each other, and all center on a common target---under the situation of low-energy-consumption, realization response thing air-flow is uniformly distributed on each cross section of beds, makes whole catalyst can both obtain to utilize evenly and fully.But in actual mechanical process, often have the reactant flow skewness, catalyst can not evenly and fully be utilized, and the big problem of droop loss.
Summary of the invention
Technical problem to be solved in the utility model is the reactant flow skewness behind the gas pre-distributor of fixed bed reactors import department that exists in the conventional art, exist and reflux, cause air-flow skewness in the reactor catalyst bed, catalyst can not evenly and fully be utilized, and the bigger problem of reactor pressure decrease loss, a kind of new axial flow fixed bed gas-solid catalyst reactor is provided.This reactor has its gas pre-distributor and disperses air-flow effective, simple and reliable for structure, and air-flow is evenly distributed in the beds, the catalyst utilization height, and reactor pressure decrease is lost characteristics such as little.
For solving the problems of the technologies described above, the technical solution adopted in the utility model is as follows: a kind of axial flow fixed bed gas-solid catalyst reactor, reactor shell comprises upper cover, cylindrical shell, low head, comprise charging aperture, gas pre-distributor, homogenizing space, top, top inert filler layer, beds, bottom inert filler layer, supporting screening plate, homogenizing space, bottom and discharging opening in the reactor shell from top to bottom, wherein gas pre-distributor is inserted in the charging aperture, and part stretches into the homogenizing space; The structure of inlet gas pre-distributor is as follows: top is the cylindrical drum (13) that stretches into the homogenizing space, the bottom is an area more than or equal to the porous overhead gage (15) of cylindrical drum upright projection area and the area porous lower baffle plate (17) less than porous overhead gage area, porous overhead gage (15) and the concentric oval or spherical baffle plate of porous lower baffle plate (17) for being connected in series up and down, its baffle plate periphery angle is 10 °＜α＜90 °, be connected by the vertical lacing wire (14) that is distributed in the cylindrical drum inboard between cylindrical drum (13) and porous overhead gage (15), and form the side direction annular space, porous overhead gage (15) center has macropore, all the other are covered with aperture, be connected by the vertical lacing wire (16) that is welded on the baffle plate between porous overhead gage (15) and porous lower baffle plate (17), and form the side direction annular space, the porous lower baffle plate is covered with aperture on (17), and the percent opening of porous overhead gage is greater than the percent opening of porous lower baffle plate.
In the technique scheme, gas pre-distributor comprises distributor cylindrical shell and two perforated baffles, be connected in series up and down between described perforated baffle, be connected by equally distributed 4～8 lacing wires between distributor cylindrical shell and the porous overhead gage, connect by equally distributed 4～8 lacing wires between perforated baffle. when the reactor upper cover is sphere, the perforated baffle of described gas pre-distributor is spherical, the area of the spherical porous baffle plate on top is greater than the area of the spherical porous baffle plate in adjacent bottom. when the reactor upper cover is ellipse, the perforated baffle of described gas pre-distributor is oval, the area of the oval perforated baffle on top is greater than the area of the oval perforated baffle in adjacent bottom. and gas pre-distributor is made up of distributor cylindrical shell and two spherical porous baffle plates, have macropore in the middle of the porous overhead gage, the diameter d in this hole is 1: 2～4: 5 with the ratio of distributor cylindrical shell D, all the other are covered with aperture, and percent opening is 30～60%; The porous lower baffle plate has aperture, and percent opening is littler than porous overhead gage, and percent opening is 25～50%; The side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage and the ratio of the side direction annular space height H 2 between the upper and lower baffle plate of porous are 1: 1～2: 1. gas pre-distributor is made up of distributor cylindrical shell and two oval perforated baffles, have macropore in the middle of the porous overhead gage, the diameter d in this hole is 1: 2～4: 5 with the ratio of distributor cylindrical shell D, all the other are covered with aperture, and percent opening is 30～60%; The porous lower baffle plate has aperture, and percent opening is littler than porous overhead gage, and percent opening is 25～50%; The side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage and the ratio of the side direction annular space height H 2 between the upper and lower baffle plate of porous are 1: 1～2: 1. the aperture on the perforated baffle of gas pre-distributor can be circle, ellipse or square, circular. and the perforated baffle of gas pre-distributor periphery angle is 20 °＜α＜80 °.
In the axial flow fixed bed gas-solid catalyst reactor of the present utility model, inlet gas pre-distributor, homogenizing space, top, top inert filler layer, bottom inert filler layer and homogenizing space, bottom etc. all are the technical measures of taking in order to realize air-flow evenly to distribute this main target in beds.If the inlet gas pre-distributor is not set, when gas entered reactor from inlet pipeline with the jet state, the flow area sudden enlargement caused reactor radial section overdraught distributed pole inhomogeneous.High-speed jet continues to impact the fixed bed surface, will form pit (hole) on the fixed bed surface, and air-flow distributes in the severe exacerbation beds.By gas pre-distributor is set, inlet air flow is carried out water conservancy diversion, force air-flow to change direction, radially be distributed on the whole radial section of reactor rapidly, be diffused into requisite space height on the whole radial section thereby shorten the import jet greatly, improve the reactor volume utilization rate.Between the inlet gas pre-distributor is with fixed bed, reserve one section space, be that state must experience a mitigation homogenization process because the elementary instability that the inlet gas pre-distributor causes flows, by means of the turbulent flow Momentum Transfer, could form more stable fluidised form and distribution more uniformly.Therefore, this section space is referred to as the homogenizing space.Just the fixed bed that comprises beds and inert filler layer of dress should not stretch in the reactor upper cover on it.Because after reactor puts into operation, continue by in the fixed bed process at air-flow, sedimentation will take place in bed, and just vertical direction sedimentation.If just the fixed bed of dress stretches in the upper cover, after the bed sedimentation, its upper surface is high, low on every side in the middle of will being, causes thickness of bed layer inhomogeneous, is unfavorable for airflow uniform distribution so.Therefore, the homogenizing spatial altitude should be greater than reactor upper cover height.The certain thickness inert filler layer of bedding (adopting inert ceramic balls usually) is that the assurance air-flow is realized equally distributed important measures in beds on beds.The top porcelain ball layer of reactor is made of large, medium and small three layers of porcelain ball, and three's role has nothing in common with each other.By calculating as can be known, under identical superficial gas velocity and identical bed thickness, it is quite big that their pressure drop differs.The resistance of little porcelain ball layer is very big, and it plays the effect that disperses air-flow, but single little porcelain ball weight is light, is dispelled by air-flow easily; The weight of single big porcelain ball is big, and it is layered on the superiors, can resist gas shock, keeps bed surface smooth; The volume of middle porcelain ball is layered on the centre to it between little porcelain ball and big porcelain ball, play a transition role.But when gas evenly distributed requirement in satisfying reactor bed, the thickness of three layers of porcelain ball was difficult for too thick, otherwise the droop loss of meeting augmenting response device.The bottom porcelain ball layer of place mat also plays the effect that increases resistance under the beds except playing supporting role, and can prevent that air-flow is concentrated to the central outlets pipe too early, and cause beds lower stream of airflow skewness.In other words, its effect is to make gas concentrate caused air-flow skewness to occur in the inert ceramic balls layer to the central outlets pipe, rather than the beds bottom, thereby avoids occurring in the beds dead band, improves catalyst utilization.Equally, reserving one section space at supporting screening plate to reactor outlet, also is in order to relax air-flow when central discharging opening is concentrated, because flow area dwindles caused reactor radial section overdraught skewness suddenly.
In the axial flow fixed bed gas-solid catalyst reactor of the present utility model, owing to adopt by distributor cylindrical shell (13), the gas pre-distributor that porous overhead gage (15) and porous lower baffle plate (17) are formed, make overwhelming majority reaction logistics at the lateral rings clearance diameter by gas pre-distributor when flowing, the partial reaction logistics is by the hole axial flow on the gas pre-distributor baffle plate, thereby eliminated around the baffle plate of gas pre-distributor, bottom and the vortex phenomenon and the energy loss that occur near reactor upper cover wall zone, reduced the height of homogenizing space, top and inert filler layer, reactant gas physical efficiency is distributed in the beds of reactor more equably, thereby reach the purpose that improves catalyst utilization and reduce reactor pressure decrease. confirm through test, the ratio of big bore dia and distributor barrel diameter by appropriate design porous overhead gage, the height of two side direction annular spaces, on, the percent opening of following perforated baffle, parameters such as baffle plate periphery angle, just can guarantee that gas pre-distributor has better gas distribution effect, guarantee that air-flow evenly distributes in the reactor, the same cross section of its beds uniformity maximum deviation has obtained better technical effect less than 5.0%.
Description of drawings
Fig. 1 is typical axial flow fixed bed gas-solid catalyst reactor schematic diagram.
Fig. 2 is the axial flow fixed bed gas-solid catalyst reactor schematic diagram of the major diameter of polar distribution of field poor distribution.
Fig. 3 is conical single-stage Flapper type inlet gas pre-distributor structure chart.
Fig. 4 is the utility model two-stage perforated baffle type inlet gas pre-distributor structure chart.
Among Fig. 1,1 is charging aperture, and 2 is upper cover, and 3 is the inlet gas pre-distributor, and 4 is homogenizing space, top, 5 is top inert filler layer, and 6 is reactor shell, and 7 is beds, and 8 is bottom inert filler layer, 9 is supporting screening plate, and 10 is homogenizing space, bottom, and 11 is low head, and 12 is discharging opening.
Among Fig. 2,2.1 represent the main streamline of gas, and 2.2 is the beds top, 2.3 be because the souring of inlet gas jet, at the pit (hole) that the beds center of top forms, 2.4 refer to by air-flow position seldom, and 2.5 is " dead band " that does not almost have air communication to cross.
Among Fig. 3,3.1 is the distributor cylindrical shell of conical single-stage Flapper type inlet gas pre-distributor, 3.2 vertical lacing wires for suspention single-stage baffle plate, and 3.3 is conical single-stage baffle plate.D is an inlet gas pre-distributor cylinder internal diameter, D
InBe reactor feed mouth internal diameter, H is an inlet gas pre-distributor side direction annular space height, and α is the coning angle of conical single-stage baffle plate.
Among Fig. 4,1 is charging aperture, 13 is the distributor cylindrical shell, 14 be the distributor cylindrical shell with the porous overhead gage between vertical lacing wire, its quantity is 4～8, be welded on inlet gas pre-distributor cylindrical shell inboard by even distribution mode, 15 is the porous overhead gage, 16 be the porous overhead gage with the porous lower baffle plate between vertical lacing wire, its quantity is 4～8, is welded on the baffle plate by even distribution mode, 17 is the porous lower baffle plate, d is the big bore dia at porous overhead gage center, and D is an inlet gas pre-distributor cylinder internal diameter, D
InBe reactor feed mouth internal diameter,
Be the hole diameter of porous overhead gage,
Be the hole diameter of porous lower baffle plate, H1 is the side direction annular space height between distributor cylindrical shell and the porous overhead gage, and the side direction annular space height between H2 porous overhead gage and the porous lower baffle plate, α are baffle plate periphery angle.
Fig. 1 Raw workflow is: the reaction logistics is introduced by the charging aperture of reactor, after the gas pre-distributor at Reactor inlet place evenly distributes, enter in the homogenizing space, top of reactor, the inert filler layer enters in the beds through top, with the catalyst haptoreaction in the beds, the reaction effluent that generates enters the reactor lower part space through bottom inert filler layer and supporting screening plate, is drawn by the reactor discharging opening at last.
Below by embodiment the utility model is further elaborated.
The specific embodiment
[embodiment 1]
Axial flow fixed bed gas-solid catalyst reactor internal diameter is 2 meters, the charging aperture inside diameter D
InIt is 350 millimeters, adopt two-stage perforated baffle type inlet gas pre-distributor as shown in Figure 4, upper and lower perforated baffle is spherical porous baffle plate, be connected by 4 equally distributed lacing wires between distributor cylindrical shell and the porous overhead gage, connect by 4 equally distributed lacing wires between porous overhead gage and the porous lower baffle plate.Distributor cylinder internal diameter D is 300 millimeters, and the macropore diameter d of porous overhead gage is 150 millimeters, the circular aperture diameter
Be 5 millimeters, percent opening is 30%, the circular aperture diameter of porous lower baffle plate
Be 5 millimeters, percent opening is 25%, and the side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage is 130 millimeters, and the side direction annular space height H 2 between the upper and lower baffle plate of porous is 65 millimeters, and perforated baffle periphery angle α is 20 °.This inside reactor top homogenizing spatial altitude is 0.7 meter, and the Cu-series catalyst thickness of bed layer is 5.6 meters, and upper and lower porcelain ball layer thickness is 200 millimeters, wherein
Two kinds of porcelain balls respectively account for 1/2, bottom homogenizing spatial altitude is 0.3 meter.Under above structural parameters, design by the axial flow fixed bed reactor of the utility model producing ethylene glycol from hydrogenation of oxalic ester, can obtain comparatively ideal gas flow effect.Press the axial flow fixed bed reactor of the utility model method design, be used 200 millimeters high top inertia packed layer, the same cross section of its beds uniformity maximum deviation is less than 2.3%, and the utilization rate of catalyst is 99.6%.
[embodiment 2]
Axial flow fixed bed gas-solid catalyst reactor internal diameter is 4 meters, the charging aperture inside diameter D
InIt is 700 millimeters, adopt two-stage perforated baffle type inlet gas pre-distributor as shown in Figure 4, upper and lower perforated baffle is spherical porous baffle plate, be connected by 8 equally distributed lacing wires between distributor cylindrical shell and the porous overhead gage, connect by 8 equally distributed lacing wires between porous overhead gage and the porous lower baffle plate.Distributor cylinder internal diameter D is 660 millimeters, and the macropore diameter d of porous overhead gage is 500 millimeters, the circular aperture diameter
Be 8 millimeters, percent opening is 60%, the circular aperture diameter of porous lower baffle plate
Be 8 millimeters, percent opening is 50%, and the side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage is 240 millimeters, and the side direction annular space height H 2 between the upper and lower baffle plate of porous is 200 millimeters, and perforated baffle periphery angle α is 60 °.This inside reactor top homogenizing spatial altitude is 2 meters, and the Cu-series catalyst thickness of bed layer is 8.0 meters, and upper and lower porcelain ball layer thickness is 300 millimeters, wherein
Three kinds of porcelain balls respectively account for 1/3, bottom homogenizing spatial altitude is 0.8 meter.Under above structural parameters, design by the axial flow fixed bed reactor of the utility model producing ethylene glycol from hydrogenation of oxalic ester, can obtain comparatively ideal gas flow effect.Press the axial flow fixed bed reactor of the utility model method design, be used 300 millimeters high top inertia packed layer, the same cross section of its beds uniformity maximum deviation is less than 3.3%, and the utilization rate of catalyst is 99.2%.
[embodiment 3]
Axial flow fixed bed gas-solid catalyst reactor internal diameter is 3.4 meters, the charging aperture inside diameter D
InIt is 600 millimeters, adopt two-stage perforated baffle type inlet gas pre-distributor as shown in Figure 4, upper and lower perforated baffle is spherical porous baffle plate, be connected by 6 equally distributed lacing wires between distributor cylindrical shell and the porous overhead gage, connect by 6 equally distributed lacing wires between porous overhead gage and the porous lower baffle plate.Distributor cylinder internal diameter D is 540 millimeters, and the macropore diameter d of porous overhead gage is 360 millimeters, the circular aperture diameter
Be 6 millimeters, percent opening is 40%, the circular aperture diameter of porous lower baffle plate
Be 8 millimeters, percent opening is 35%, and the side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage is 180 millimeters, and the side direction annular space height H 2 between the upper and lower baffle plate of porous is 180 millimeters, and perforated baffle periphery angle α is 40 °.This inside reactor top homogenizing spatial altitude is 1.8 meters, and the Cu-series catalyst thickness of bed layer is 6.5 meters, and upper and lower porcelain ball layer thickness is 300 millimeters, wherein
Three kinds of porcelain balls respectively account for 1/3, bottom homogenizing spatial altitude is 0.7 meter.Under above structural parameters, design by the axial flow fixed bed reactor of the utility model producing ethylene glycol from hydrogenation of oxalic ester, can obtain comparatively ideal gas flow effect.Press the axial flow fixed bed reactor of the utility model method design, be used 300 millimeters high top inertia packed layer, the same cross section of its beds uniformity maximum deviation is less than 2.8%, and the utilization rate of catalyst is 99.3%.
[embodiment 4]
Axial flow fixed bed gas-solid catalyst reactor internal diameter is 4 meters, the charging aperture inside diameter D
InIt is 700 millimeters, adopt two-stage perforated baffle type inlet gas pre-distributor as shown in Figure 4, upper and lower perforated baffle is oval perforated baffle, be connected by 8 equally distributed lacing wires between distributor cylindrical shell and the porous overhead gage, connect by 8 equally distributed lacing wires between porous overhead gage and the porous lower baffle plate.Distributor cylinder internal diameter D is 660 millimeters, and the macropore diameter d of porous overhead gage is 450 millimeters, the circular aperture diameter
Be 8 millimeters, percent opening is 52%, the circular aperture diameter of porous lower baffle plate
Be 8 millimeters, percent opening is 40%, and the side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage is 240 millimeters, and the side direction annular space height H 2 between the upper and lower baffle plate of porous is 160 millimeters, and perforated baffle periphery angle α is 80 °.This inside reactor top homogenizing spatial altitude is 2 meters, and the Cu-series catalyst thickness of bed layer is 8.0 meters, and upper and lower porcelain ball layer thickness is 300 millimeters, wherein
Three kinds of porcelain balls respectively account for 1/3, bottom homogenizing spatial altitude is 0.8 meter.Under above structural parameters, design by the axial flow fixed bed reactor of the utility model producing ethylene glycol from hydrogenation of oxalic ester, can obtain comparatively ideal gas flow effect.Press the axial flow fixed bed reactor of the utility model method design, be used 300 millimeters high top inertia packed layer, the same cross section of its beds uniformity maximum deviation is less than 3.6%, and the utilization rate of catalyst is 99.0%
[embodiment 5]
Axial flow fixed bed gas-solid catalyst reactor internal diameter is 3.4 meters, the charging aperture inside diameter D
InIt is 600 millimeters, adopt two-stage perforated baffle type inlet gas pre-distributor as shown in Figure 4, upper and lower perforated baffle is oval perforated baffle, be connected by 6 equally distributed lacing wires between distributor cylindrical shell and the porous overhead gage, connect by 6 equally distributed lacing wires between porous overhead gage and the porous lower baffle plate.Distributor cylinder internal diameter D is 540 millimeters, and the macropore diameter d of porous overhead gage is 360 millimeters, the circular aperture diameter
Be 6 millimeters, percent opening is 40%, the circular aperture diameter of porous lower baffle plate
Be 6 millimeters, percent opening is 35%, and the side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage is 200 millimeters, and the side direction annular space height H 2 between the upper and lower baffle plate of porous is 180 millimeters, and perforated baffle periphery angle α is 45 °.This inside reactor top homogenizing spatial altitude is 1.8 meters, and the Cu-series catalyst thickness of bed layer is 6.5 meters, and upper and lower porcelain ball layer thickness is 300 millimeters, wherein
Three kinds of porcelain balls respectively account for 1/3, bottom homogenizing spatial altitude is 0.7 meter.Under above structural parameters, design by the axial flow fixed bed reactor of the utility model producing ethylene glycol from hydrogenation of oxalic ester, can obtain comparatively ideal gas flow effect.Press the axial flow fixed bed reactor of the utility model method design, be used 300 millimeters high top inertia packed layer, the same cross section of its beds uniformity maximum deviation is less than 3.2%, and the utilization rate of catalyst is 99.2%
[embodiment 6]
Axial flow fixed bed gas-solid catalyst reactor internal diameter is 2 meters, the charging aperture inside diameter D
InIt is 350 millimeters, adopt two-stage perforated baffle type inlet gas pre-distributor as shown in Figure 4, upper and lower perforated baffle is oval perforated baffle, be connected by 4 equally distributed lacing wires between distributor cylindrical shell and the porous overhead gage, connect by 4 equally distributed lacing wires between porous overhead gage and the porous lower baffle plate.Distributor cylinder internal diameter D is 300 millimeters, and the macropore diameter d of porous overhead gage is 150 millimeters, the circular aperture diameter
Be 5 millimeters, percent opening is 30%, the circular aperture diameter of porous lower baffle plate
Be 5 millimeters, percent opening is 25%, and the side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage is 130 millimeters, and the side direction annular space height H 2 between the upper and lower baffle plate of porous is 75 millimeters, and perforated baffle periphery angle α is 30 °.This inside reactor top homogenizing spatial altitude is 0.7 meter, and the Cu-series catalyst thickness of bed layer is 5.6 meters, and upper and lower porcelain ball layer thickness is 200 millimeters, wherein
Two kinds of porcelain balls respectively account for 1/2, bottom homogenizing spatial altitude is 0.3 meter.Under above structural parameters, design by the axial flow fixed bed reactor of the utility model producing ethylene glycol from hydrogenation of oxalic ester, can obtain comparatively ideal gas flow effect.Press the axial flow fixed bed reactor of the utility model method design, be used 200 millimeters high top inertia packed layer, the same cross section of its beds uniformity maximum deviation is less than 2.5%, and the utilization rate of catalyst is 99.5%.
[comparative example 1]
The condition of the axial flow fixed bed gas-solid catalyst reactor of certain producing ethylene glycol from hydrogenation of oxalic ester is identical with embodiment 1 with structural parameters, and unique difference is that it adopts single-stage Flapper type inlet gas pre-distributor.Reactor need be used at least 450 millimeters high top inertia packed layers, and the same cross section of its beds uniformity maximum deviation is less than 5.6%, and catalyst utilization is 96.5%.The reactor pressure decrease loss of embodiment 1 is littler by 20.5% than this comparative example.
[comparative example 2]
The spherical baffle plate of the two-stage perforate of the inlet gas pre-distributor of the axial flow fixed bed gas-solid catalyst reactor of the producing ethylene glycol from hydrogenation of oxalic ester of embodiment 2 makes plate shaped single-stage baffle plate into, and other structural parameters are all constant.Under all identical with embodiment 2 condition of all conditions, reactor need be used at least 450 millimeters high top inertia packed layers, and the same cross section of its beds uniformity maximum deviation is less than 7.2%, and catalyst utilization is 90.9%.The reactor pressure decrease loss of embodiment 2 is littler by 11.8% than this comparative example.
[comparative example 3]
The spherical baffle plate of the two-stage perforate of the inlet gas pre-distributor of the axial flow fixed bed gas-solid catalyst reactor of the producing ethylene glycol from hydrogenation of oxalic ester of embodiment 3 makes plate shaped single-stage baffle plate into, and other structural parameters are all constant.Under all identical with embodiment 3 condition of all conditions, reactor need be used at least 450 millimeters high top inertia packed layers, and the same cross section of its beds uniformity maximum deviation is less than 6.4%, and catalyst utilization is 92.8%.The reactor pressure decrease loss of embodiment 3 is littler by 10.6% than this comparative example.
[comparative example 4]
The oval baffle plate of the two-stage perforate of the inlet gas pre-distributor of the axial flow fixed bed gas-solid catalyst reactor of the producing ethylene glycol from hydrogenation of oxalic ester of embodiment 4 makes plate shaped single-stage baffle plate into, and other structural parameters are all constant.Under all identical with embodiment 4 condition of all conditions, reactor need be used at least 450 millimeters high top inertia packed layers, and the same cross section of its beds uniformity maximum deviation is less than 7.0%, and catalyst utilization is 91.2%.The reactor pressure decrease loss of embodiment 2 is littler by 11.5% than this comparative example.
Claims (8)
1. axial flow fixed bed gas-solid catalyst reactor, reactor shell comprises upper cover, cylindrical shell, low head, comprise charging aperture, gas pre-distributor, homogenizing space, top, top inert filler layer, beds, bottom inert filler layer, supporting screening plate, homogenizing space, bottom and discharging opening in the reactor shell from top to bottom, wherein gas pre-distributor is inserted in the charging aperture, and part stretches into the homogenizing space; The structure of inlet gas pre-distributor is as follows: top is the cylindrical drum (13) that stretches into the homogenizing space, the bottom is an area more than or equal to the porous overhead gage (15) of cylindrical drum upright projection area and the area porous lower baffle plate (17) less than porous overhead gage area, porous overhead gage (15) and the concentric oval or spherical baffle plate of porous lower baffle plate (17) for being connected in series up and down, its baffle plate periphery angle is 10 °＜α＜90 °, be connected by the vertical lacing wire (14) that is distributed in the cylindrical drum inboard between cylindrical drum (13) and porous overhead gage (15), and form the side direction annular space, porous overhead gage (15) center has macropore, all the other are covered with aperture, be connected by the vertical lacing wire (16) that is welded on the baffle plate between porous overhead gage (15) and porous lower baffle plate (17), and form the side direction annular space, the porous lower baffle plate is covered with aperture on (17), and the percent opening of porous overhead gage is greater than the percent opening of porous lower baffle plate.
2. axial flow fixed bed gas-solid catalyst reactor according to claim 1, it is characterized in that described gas pre-distributor comprises distributor cylindrical shell and two perforated baffles, be connected in series up and down between described perforated baffle, be connected by equally distributed 4～8 lacing wires between distributor cylindrical shell and the porous overhead gage, connect by equally distributed 4～8 lacing wires between perforated baffle.
3. axial flow fixed bed gas-solid catalyst reactor according to claim 1, it is characterized in that when the reactor upper cover is sphere, the perforated baffle of described gas pre-distributor is spherical, and the area of the spherical porous baffle plate on top is greater than the area of the spherical porous baffle plate in adjacent bottom.
4. axial flow fixed bed gas-solid catalyst reactor according to claim 1, it is characterized in that when the reactor upper cover is ellipse, the perforated baffle of described gas pre-distributor is oval, and the area of the oval perforated baffle on top is greater than the area of the oval perforated baffle in adjacent bottom.
5. axial flow fixed bed gas-solid catalyst reactor according to claim 1, it is characterized in that gas pre-distributor is made up of distributor cylindrical shell and two spherical porous baffle plates, have macropore in the middle of the porous overhead gage, the diameter d in this hole is 1: 2～4: 5 with the ratio of distributor cylindrical shell D, all the other are covered with aperture, and percent opening is 30～60%; The porous lower baffle plate has aperture, and percent opening is littler than porous overhead gage, and percent opening is 25～50%; The side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage and the ratio of the side direction annular space height H 2 between the upper and lower baffle plate of porous are 1: 1～2: 1.
6. axial flow fixed bed gas-solid catalyst reactor according to claim 1, it is characterized in that gas pre-distributor is made up of distributor cylindrical shell and two oval perforated baffles, have macropore in the middle of the porous overhead gage, the diameter d in this hole is 1: 2～4: 5 with the ratio of distributor cylindrical shell D, all the other are covered with aperture, and percent opening is 30～60%; The porous lower baffle plate has aperture, and percent opening is littler than porous overhead gage, and percent opening is 25～50%; The side direction annular space height H 1 between distributor cylindrical shell and the porous overhead gage and the ratio of the side direction annular space height H 2 between the upper and lower baffle plate of porous are 1: 1～2: 1.
7. axial flow fixed bed gas-solid catalyst reactor according to claim 1 is characterized in that the aperture on the perforated baffle of gas pre-distributor is circular, ellipse or square.
8. axial flow fixed bed gas-solid catalyst reactor according to claim 1, the perforated baffle periphery angle that it is characterized in that gas pre-distributor are 20 °＜α＜80 °.
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| CN2009200744482U CN201454503U (en) | 2009-08-31 | 2009-08-31 | Axial flow fixed bed gas-solid catalytic reactor |
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| CN2009200744482U CN201454503U (en) | 2009-08-31 | 2009-08-31 | Axial flow fixed bed gas-solid catalytic reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489222A (en) * | 2011-12-05 | 2012-06-13 | 新地能源工程技术有限公司 | Reaction device for synthesizing methane, and method for synthesizing methane |
| CN103585932A (en) * | 2013-10-30 | 2014-02-19 | 浙江大学 | Bionic fixed bed reactor with distributed feeding and discharging network channels |
| CN106966065A (en) * | 2017-05-29 | 2017-07-21 | 福州维金斯农业科技有限公司 | A kind of lichee controlled atmosphere is multiplexed antistaling box |
| WO2024159584A1 (en) * | 2023-02-01 | 2024-08-08 | 北京石油化工学院 | Gas distributor and gas-solid reactor containing same |
-
2009
- 2009-08-31 CN CN2009200744482U patent/CN201454503U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102489222A (en) * | 2011-12-05 | 2012-06-13 | 新地能源工程技术有限公司 | Reaction device for synthesizing methane, and method for synthesizing methane |
| CN103585932A (en) * | 2013-10-30 | 2014-02-19 | 浙江大学 | Bionic fixed bed reactor with distributed feeding and discharging network channels |
| CN103585932B (en) * | 2013-10-30 | 2016-01-13 | 浙江大学 | A kind of bionical reactor of fixed bed with distributed charging and discharging network channel |
| CN106966065A (en) * | 2017-05-29 | 2017-07-21 | 福州维金斯农业科技有限公司 | A kind of lichee controlled atmosphere is multiplexed antistaling box |
| WO2024159584A1 (en) * | 2023-02-01 | 2024-08-08 | 北京石油化工学院 | Gas distributor and gas-solid reactor containing same |
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