CN202823320U - Gas distributor, slurry bed reactor comprising same and crude methanol synthesis system - Google Patents
Gas distributor, slurry bed reactor comprising same and crude methanol synthesis system Download PDFInfo
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- CN202823320U CN202823320U CN2012205053497U CN201220505349U CN202823320U CN 202823320 U CN202823320 U CN 202823320U CN 2012205053497 U CN2012205053497 U CN 2012205053497U CN 201220505349 U CN201220505349 U CN 201220505349U CN 202823320 U CN202823320 U CN 202823320U
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Abstract
The utility model provides a gas distributor, a slurry bed reactor comprising the gas distributor and a crude methanol synthesis system. The gas distributor comprises a central gas duct, a gas distribution pipe group and a connecting pipe, wherein the gas distribution pipe group is arranged around the central gas duct with the central gas duct as the center and has a vent hole communicated with the outside; the connecting pipe is used for connecting the central gas duct and the gas distribution pipe group; the central gas duct comprises a gas inlet main pipe with one end communicated with the connecting pipe, and a plurality of rotational flow jet pipes for jetting out the circumferential revolving gas flow; and one end of each of the rotational flow jet pipes is communicated with the peripheral wall of the gas inlet main pipe, while the other end of each of the rotational flow jet pipes is a gas outlet. When the gas distributor provided by the utility model works, the gas enters the gas distribution pipe group via the central gas duct and is evenly distributed through the vent holes of the gas distribution pipe group; and with the rotational flow jet pipes arranged on the gas inlet main pipe of the central gas duct, part of the gas while passing through the gas inlet main pipe is jetted out through the rotational flow jet pipes and the gas flow rises under the pressure of the gas jetted out, therefore, the gas distribution effect is optimized.
Description
Technical field
The utility model relates to the synthetic field of methyl alcohol, in particular to a kind of gas distributor and comprise its paste state bed reactor, thick system for methanol synthesis.
Background technology
In methanol production process, usually because the reaction bed temperature in the synthesis reactor is uneven or reaction temperature is too high or cross reaction temperature spend low or reaction gas in methanol content too high, cause accessory substance too much, such as methane and wax etc.Wax can reduce the heat transfer effect of methanol-water cooler, the separating effect of reduction methanol separator on the one hand, carries methyl alcohol in the circulating air secretly thereby make, and then has reduced the conversion per pass of synthetic tower; Wax is bonded on pipeline and the column plate on the other hand, can reduce circulation area, even result in blockage; And behind downstream unit, in case temperature reduces, the wax in the thick methyl alcohol will condense, and has influence on the normal production of downstream unit.
For, ammonia synthesis and CO conversion this class gas-solid synthetic by the lower methylamine of pressurization, methyl ether, methyl alcohol exothermic catalytic reaction mutually, along with the carrying out of reaction, the reaction heat of constantly emitting improves reaction bed temperature.In order to reduce the efficient of accessory substance and raising reactor, need to shift out reaction heat so that reaction temperature is in a rational scope.
In industrial reactor, once widely a kind of of use was the multistage insulation reactor, reduce the reaction gas temperature with the unstripped gas Quench between two sections, this reactor has also reduced reactant concentration during because of the unstripped gas Quench when reducing the reaction gas temperature, affected combined coefficient.Another kind is the shell and tube reactor for the synthetic Lurgi company of methyl alcohol, lower perforated plate and many pipes between tube sheet in housing, having, catalyst is housed in the pipe, unstripped gas enters from the top air inlet and is distributed to each pipe, synthesizing methanol in the catalyst layer of installing in pipe, lateral inflow between pipe, the water boiling is continuously removed heat between pipe thereby the heat in the pipe makes, the steam that the water boiling produces is gone out by the side pipe, and reaction gas goes out tower by the bottom escape pipe.This tower has a narrow range of temperature, but the catalyst filling coefficient is little, and reaction efficiency is low.
At present, widely used is the methyl alcohol synthetic technology of DAVY company exploitation.As shown in Figure 1, Catalyst packing produces middle pressure steam at the shell-side of reactor in the pipe; Fresh reaction gas enters from the central tube 1 ' of reactor bottom, has dispensing orifice on the central tube 1 ' tube wall to guarantee being evenly distributed of gas; Gas is the beds by reactor from inside to outside radially; Then upwards flow in the bottom that the boiler water that comes from drum enters reactor by heat exchanger tube 2 ' and the reaction heat that the methyl alcohol synthetic reaction produces is taken away in the part vaporization; Reaction temperature is regulated by the pressure of steam in the control valve.
This technology can be with reaction temperature control within the specific limits, and the expansion of reactor production capacity can realize by lengthening reactor length, aspect the synthetic maximization of methyl alcohol its technical advantage is being arranged, is extensively being adopted by the synthetic producer of methyl alcohol gradually at present, but itself also have these some deficiencies:
1) enters because of the central tube of fresh reaction gas from reactor bottom, so at first radially entering into reactor middle and lower part beds from inside to outside by the dispensing orifice on the central tube 1 ' tube wall of reactor middle and lower part, the larger proportion reaction gas reacts, along central tube 1 ' more up, reaction gas is just thinner, namely the reactor lower part beds just has more reaction gases and participates in reaction for reactor upper catalyst bed layer, and the activity of reactor lower part catalyst will descend sooner with respect to the activity of reactor top catalyst like this;
When 2) having arrived the middle and later periods in catalyst service life, entering major part in the reaction gas of dispensing orifice on the reactor lower part central tube 1 ' tube wall radially enters into from inside to outside and does not have enough time to carry out chemical reaction toward contact behind the reactor lower part beds and just left beds, again because all large in reaction gas ratio middle and upper part that reactor lower part reacts, even the conversion ratio at the catalyst place that the activity of reaction gas on reactor top is higher also keeps higher level, but because the reaction tolerance less on reactor top, so that the conversion per pass of reaction gas reaction methanol will descend rapidly generally, so that methanol output also can descend thereupon; If the maintenance methanol output just needs to strengthen internal circulating load and the cycle-index of unreacted reaction gas, this has increased again energy consumption undoubtedly;
3) in the catalyst middle and later periods in service life, if adopt the method that significantly improves reaction bed temperature to improve the activity of catalyst, can make catalyst faster decline in service life on the one hand, can produce on the other hand more wax (especially when bed temperature is higher than more than 280 ℃), like this, often originally can use the time of the bed catalyst change of long or longer time greatly to shift to an earlier date; Because when catalyst changeout more, the catalyst of integral reactor all and contact with air, in case in air atmosphere, still activated catalyst also will damage and can't use because poisoning fast, therefore also keep the catalyst of greater activity also together to change with the catalyst that reactor lower part almost can't use on reactor top, caused economically waste.
4) methanol synthesis reactor is radial flow reactors, top in synthesis reactor, hot gas needs could flow out outside the tower behind the downward baffling, in tower the holdup time longer, cause the speed that shifts out reaction heat to shift out speed than the reaction heat of other positions of beds and want slow, so that local overheating usually appears in the reactor catalyst bed, especially when bed temperature is higher than 280 ℃, tend to produce a large amount of wax, so that catalyst activity is accelerated decay, indirectly cause the waste of catalyst simultaneously.
This shows, because reaction gas skewness in methanol synthesis reactor, cause that its and catalyst are inhomogeneous to be contacted and then cause that methanol yield is low, catalyst is wasted serious problem in the methanol synthesis reactor of the prior art.
The utility model content
The utility model aims to provide a kind of gas distributor and comprises its paste state bed reactor, thick system for methanol synthesis, to realize the purpose of even distributing gas.
To achieve these goals, according to an aspect of the present utility model, provide a kind of gas distributor, gas distributor comprises: central airway; The gas distribution tube group, centered by central airway, be arranged on central airway around, have the passage that communicates with the external world; Tube connector connects central airway and gas distribution tube group; Central airway comprises: the air inlet supervisor, and an end is communicated with tube connector; Be used for spraying a plurality of eddy flow jet pipes of circumferential gyration airflow, an end communicates with air inlet supervisor's perisporium, and the other end is gas vent.
Further, above-mentioned gas distributor pipe group comprises at least two annular gas distributor pipes that arrange with one heart, and passage is distributed on the tube wall of each annular gas distributor pipe, and the aperture arranges towards the below; Tube connector is along the radially setting of gas distribution tube group and be communicated with each annular gas distributor pipe; The air inlet supervisor's of central airway lower end is air inlet openings, and the upper end is communicated with tube connector; Each eddy flow jet pipe of central airway is circumferentially evenly arranged along the air inlet supervisor's, and the gas vent of each eddy flow jet pipe extends along the oblique below of the central axis that departs from the air inlet supervisor.
Further, above-mentioned eddy flow jet pipe comprises: horizontal component is connected on air inlet supervisor's the sidewall along radially extending of air inlet supervisor; Vertical component is communicated with and straight down extension with the end of horizontal component away from the air inlet supervisor; Sloping portion is communicated with the end of vertical component away from horizontal component, and is tilted to downward-extension, and the projection of sloping portion on horizontal plane extended along the direction perpendicular to horizontal component.
Further, above-mentioned passage comprises the hole of cutting sth. askew, the sidewall in the hole of cutting sth. askew along the gas distribution tube group radially from inside to outside all to counterclockwise or all to tilting to extend clockwise.
Further, above-mentioned passage also comprises the first straight hole, and the sidewall of the first straight hole vertically extends, and the first straight hole is intervally arranged at each annular gas distributor pipe with the hole of cutting sth. askew.
Further, the above-mentioned gas distributor also comprises the side wireway that even number is communicated with tube connector, and the side wireway is arranged on two tube connectors between the annular gas distributor pipe in twos symmetrically with respect to central airway, and with the equidirectional extension of central airway.
Further, above-mentioned tube connector comprises: the first tube connector, and along the internal diameter extension of outermost annular gas distributor pipe, the center of passing gas distribution tube is communicated with each annular gas distributor pipe, and central airway is communicated with the center of the first tube connector; The second tube connector, vertical with the first tube connector, and be arranged between outermost annular gas distributed pipeline and the most inboard annular gas distributed pipeline, each annular gas distributor pipe is communicated with, the side wireway is communicated with the second tube connector.
Further, above-mentioned the first tube connector is positioned at the caliber of the most inboard annular gas distributed pipeline greater than the caliber of the first tube connector remainder, and the caliber of the first tube connector is less than the caliber of the second tube connector.
Further, above-mentioned side wireway is two and is arranged on symmetrically near on the second tube connector of axis with respect to the axis of gas distribution tube group, the part that the side wireway is not set on the second tube connector has centered by central airway and along its second straight hole that is circumferentially arranged, the length direction along the first tube connector on the first tube connector evenly is placed with the 3rd straight hole.
Further, the cross section of above-mentioned each annular gas distributor pipe is annular, and is positioned at the most inboard annular gas distributed pipeline and is positioned at the internal diameter of outermost annular gas distributed pipeline greater than the internal diameter of the annular gas distributed pipeline in the middle of being positioned at.
According on the other hand of the present utility model, a kind of paste state bed reactor also is provided, comprise bathing pool setting up and down and gas cushion chamber, be provided with above-mentioned gas distributor in the bathing pool, the gas distribution tube group of gas distributor is fixed on the sidewall of bathing pool, and the central airway of gas distributor extends to the diapire of bathing pool.
Further, above-mentioned paste state bed reactor also comprises support member, and the first end of support member links to each other with the gas distribution tube group, and the second end links to each other with the sidewall of paste state bed reactor.
Further, the diapire of above-mentioned bathing pool is that the middle vertex of a cone is towards the conical bottom wall of below.
Further, the above-mentioned gas buffer is indoor to have the reaction gas inlet pipe, and the reaction gas inlet pipe runs through the sidewall of gas cushion chamber, and its gas outlet is towards the diapire of gas cushion chamber.
According to another aspect of the present utility model, a kind of thick system for methanol synthesis also is provided, thick system for methanol synthesis comprises: above-mentioned paste state bed reactor, reaction gas produces under catalyst action and generates gas in paste state bed reactor; The atent solvent recovery system, and have the letter shoot line of generation and atent solvent reflux pipeline between the paste state bed reactor; Thick methanol recovery system, be connected to process from the generation of atent solvent recovery system with the atent solvent recovery system and be so incensed that the thick methyl alcohol and the circulating air that separate, and have the pipeline that enters paste state bed reactor for part circulating air between thick methanol recovery system and the paste state bed reactor; Hydrogen recovery system, the hydrogen in the circulating air that reclaims thick methanol recovery system that is connected with thick methanol recovery system; The reactive gas cleaning system, the end formation admission line that is connected with fresh reactant source of the gas and hydrogen recovery system has the gas supply line that enters paste state bed reactor for the fresh reactant gas after purifying and hydrogen between the other end and the paste state bed reactor.
Further, above-mentioned thick system for methanol synthesis also comprises cyclone separator, is arranged on the generation letter shoot line between atent solvent recovery system and the paste state bed reactor, has: generate the gas import, be communicated with generation letter shoot line; Gas vent is communicated with generation letter shoot line; Solid outlet, and have the solids backflow pipeline between the paste state bed reactor.
Gas distributor of the present utility model is when work, gas is entered in the gas distribution tube group of this gas distributor by central airway, and spread by the passage on the gas distribution tube group, thereby realized gas equally distributed effect in being provided with the space of gas distributor downwards.And, be responsible for the eddy flow jet pipe that arranges in the air inlet of central airway and make gas part through the air inlet supervisor time pass through this eddy flow jet pipe ejection, utilize the air pressure of gas ejection that air-flow is risen, further optimized the effect of distribution of gas.
Description of drawings
The Figure of description that consists of the application's a part is used to provide further understanding of the present utility model, and illustrative examples of the present utility model and explanation thereof are used for explaining the utility model, do not consist of improper restriction of the present utility model.In the accompanying drawings:
Fig. 1 shows the structural representation of the methanol synthesis reactor of DAVY company in the prior art;
Fig. 2 there is shown paste state bed reactor and the slurry reactor the highest liquid level line when operation according to the cutaway view of gas distributor of the present utility model;
Fig. 3 shows the Q of gas distributor shown in Figure 2
1-Q
1To view;
Fig. 4 shows the Q of gas distributor shown in Figure 2
2-Q
2To view;
Fig. 5 shows the Q of gas distributor shown in Figure 2
4-Q
4To view; And
Fig. 6 shows the schematic diagram according to the thick system for methanol synthesis of a kind of preferred embodiment of the utility model.
The specific embodiment
Need to prove that in the situation of not conflicting, embodiment and the feature among the embodiment among the application can make up mutually.Describe below with reference to the accompanying drawings and in conjunction with the embodiments the utility model in detail.
Shown in Fig. 3 to 5, in a kind of typical embodiment of the utility model, a kind of gas distributor is provided, this gas distributor comprises central airway 280, gas distribution tube group 620 and tube connector 630, gas distribution tube group 620 centered by central airway 280, be arranged on central airway 280 around, have the passage 650 that communicates with the external world; Tube connector 630 connects central airway 280 and gas distribution tube group 620; Central airway 280 comprises: air inlet supervisor 281 and be used for spraying a plurality of eddy flow jet pipes 282 of circumferential gyration airflow, and an end of air inlet supervisor 281 is communicated with tube connector 630; One end of eddy flow jet pipe 282 communicates with air inlet supervisor 281 perisporium, and the other end is gas vent.
Gas distributor with said structure, gas is entered in the gas distribution tube group 620 of this gas distributor by central airway 280, and spread by passage 650, thereby realized gas equally distributed effect in being provided with the space of gas distributor downwards.In the time of in applying it to a certain equipment, all gas is from passage 650 diffusion ejection downwards, when gas is ejected in the equipment with gas distributor when stoping the assembly that air-flow further sinks when diffusion downwards, gas is decelerated to zero and oppositely rises or gas is subject to the barrier effect of assembly and rises, and gas this comes and goes and flow and the interaction in flow process makes gas obtain Uniform Dispersion at equipment; And, the eddy flow jet pipes 282 that arrange the air inlet of central airway 280 supervisor 281 make gas be responsible for 281 o'clock parts through air inlet by this eddy flow jet pipe 282 ejections, utilize the air pressure of gas ejection that air-flow is risen, further optimized the effect of distribution of gas.Eddy flow jet pipe 282 can be arranged on same cross section of the air inlet supervisor 281 and circumferentially arrange, and also can be circumferentially arranged on air inlet supervisor 281 with helical form.
In a kind of preferred embodiment of the utility model, above-mentioned gas distributor pipe group 620 comprises at least two annular gas distributor pipes 622,623 that arrange with one heart, 624, passage 650 is distributed in each annular gas distributor pipe 622,623, on 624 the tube wall, and the aperture arranges towards the below; Tube connector 630 radially arranges and is communicated with each annular gas distributor pipe 622,623,624 along gas distribution tube group 620; The air inlet supervisor's 281 of central airway 280 lower end is air inlet openings, and the upper end is blind end; Each eddy flow jet pipe 282 of central airway 280 is circumferentially evenly arranged along air inlet supervisor's 281, and the gas vent of each eddy flow jet pipe 282 extends along the oblique below of the central axis that departs from air inlet supervisor 281.
The gas that is entered by central airway 280 is distributed to each annular gas distributor pipe 622 by tube connector 630,623, in 624, and then by each annular gas distributor pipe 622, passage 650 on 623,624 is distributed to annular gas distributor pipe 622,623, around 624, realize distribution of gas each position on every side to gas distributor.
As shown in Figure 5, the eddy flow jet pipe 282 of the central airway 280 of above-mentioned gas distributor comprises horizontal component, vertical component and sloping portion, and horizontal component is connected on air inlet supervisor 281 the sidewall along radially extending of air inlet supervisor 281; Vertical component is communicated with and straight down extension with the end of horizontal component away from air inlet supervisor 281; Sloping portion is communicated with the end of vertical component away from horizontal component, and is tilted to downward-extension, and the projection of sloping portion on horizontal plane extended along the direction perpendicular to horizontal component.Eddy flow jet pipe 282 with said structure is simple in structure, is easy to installation, and has the effect with gas channeling eddy flow jet pipe 282 oblique belows.
In the structure of a kind of gas distributor that the utility model optimizes, as shown in Figure 4, passage 650 comprises the hole 652 of cutting sth. askew, the sidewall in the hole 652 of cutting sth. askew along gas distribution tube group 620 radially from inside to outside all to counterclockwise or all to tilting to extend clockwise.When gas passed through tangential hole 652, gas can spread and backflow to gas distribution tube group 620 unlapped zones, thereby has improved the distribution of gas at each position of whole equipment.
In order further to optimize the distribution of gas effect, as shown in Figure 4, optimizing breathing hole 650 also comprises the first straight hole 651, the sidewall of the first straight hole 651 vertically extends, the first straight hole 651 and the hole 652 of cutting sth. askew are intervally arranged on each annular gas distributor pipe 622,623,624.When gas passes through the first straight hole 651, spread and backflow in the zone that gas distribution tube group 620 covers along the direction parallel with the axis of gas distributor.The first straight hole 651 is intervally arranged on annular gas distributor pipe 622,623,624 with the hole 652 of cutting sth. askew, can be with annular gas distributor pipe 622,623,624 upper gas dispersion have further been improved the distribution of gas to the zone of failing to cover between its zone that can cover and pipe.
As shown in Figures 2 and 3, the another kind of gas distributor that the utility model optimizes also comprises the side wireway 380 that even number is communicated with tube connector 630, side wireway 380 is arranged on two annular gas distributor pipes 622 symmetrically with respect to central airway 280,623, on the tube connector 630 between 624, and with central airway 280 equidirectional extensions.Adopt central airway 280 and side wireway 380 simultaneously to the gas distributor air inlet, gas is entered in the gas distribution tube group 620 in more uniform mode, thereby thereby making each annular gas distributor pipe accept uniform intake method provide uniform distribution of gas mode.
As shown in Figure 3 and Figure 4, the tube connector 630 of above-mentioned gas distributor comprises the first tube connector 631 and the second tube connector 632, the first tube connector 631 extends along the internal diameter of outermost annular gas distributor pipe 623, pass gas distribution tube 622,623,624 center is with each annular gas distributor pipe 622,623,624 are communicated with, and central airway 280 is communicated with the center of the first tube connector 631; The second tube connector 632 is vertical with the first tube connector 631, and be arranged between outermost annular gas distributed pipeline 623 and the most inboard annular gas distributed pipeline 622, and with each annular gas distributor pipe 622,623,624 are communicated with, and side wireway 380 is communicated with the second tube connector 632.
Orthogonal the first tube connector 631 and the second tube connector 632 are set in gas distributor, so that the gas in the gas distribution tube group 620 is at each annular gas distributor pipe 622,623, flowing between 624 is more smooth and easy; And, at the first tube connector 631 central airway 280 that is communicated with it is set, at the second tube connector 632 connected side wireway 632 is set, the 620 while air feed from different guide pipelines to the gas distribution tube group, so that gas is distributed in each position of whole gas distribution tube group 620 sufficiently uniformly, for further providing good distribution of gas basis from passage 650 diffusions.
Because central airway 280 is arranged on the first tube connector 631, side wireway 380 is arranged on the second tube connector 632, enter gas distributor for the ease of gas, preferred the first tube connector 631 is positioned at the caliber of the most inboard annular gas distributed pipeline 622 greater than the caliber of the first tube connector 631 remainders, and the caliber of the first tube connector 631 is less than the caliber of the second tube connector 632.
From the better distribution consideration in gas distribution tube group 620 to gas distributor air feed and gas, the number of side wireway 380 is The more the better; But the utility model preferably adopts simple as far as possible structure, the gas distributor that alap cost forms has the distribution of gas effect that can optimize, therefore, the utility model preferential side wireway 380 is two and is arranged on symmetrically near on the second tube connector 632 of axis with respect to the axis of gas distribution tube group 620, the part that side wireway 380 is not set on the second tube connector 632 has centered by central airway 280 and along the length direction along the first tube connector 631 on its second straight hole 653, the first tube connectors 631 that are circumferentially arranged and evenly is placed with the 3rd straight hole 654.
As shown in Figure 3 and Figure 4, each annular gas distributor pipe 622,623,624 cross section is annular, and is positioned at the most inboard annular gas distributed pipeline 622 and is positioned at the internal diameter of outermost annular gas distributed pipeline 623 greater than the internal diameter of the annular gas distributed pipeline 624 in the middle of being positioned at.When the internal diameter of the most inboard annular gas distributor pipe 622 is larger, for being diffused rapidly in remaining annular gas distributor pipe, the gas that is entered by central airway 280 provides enough large passage; Simultaneously, because the caliber of outermost annular gas distributed pipeline 623 is maximum, the zone that it covers and to close on its region area all larger, for enough gas is provided to above-mentioned zone, the preferably expansion that outermost annular gas distributed pipeline 623 is suitable.
The utility model is considered from the practical application size of gas distributor, preferred the first straight hole 651 620 of gas distribution tube groups in the plane be projected as the circle that diameter is 5～80mm, the hole 652 of cutting sth. askew is 5～80mm parallelogram in 620 length of sides that are projected as in the plane of gas distribution tube group.
The annular gas distributor pipe 622 of above-mentioned gas distributor, 623,624 shape has multiple pattern, its shell is annular or oval ring or side's annular, the shape of its internal pipeline also can be annular or oval ring or side's annular, preferably each annular gas distributor pipe 622,623,624 cross section is annular, and the internal diameter of annular is 30～300mm.The internal diameter of the preferred annular gas distributed pipeline that from inside to outside distributes increases, thereby has overcome the drawback of gas at the easy skewness of gas distributor edge.
As shown in Figure 5, in the another kind of typical embodiment of the utility model, a kind of paste state bed reactor also is provided, comprise bathing pool setting up and down 100 and gas cushion chamber 200, be provided with above-mentioned gas distributor in the bathing pool 100, the gas distribution tube group 620 of gas distributor is fixed on the sidewall 102 of bathing pool 100, and the central airway 280 of gas distributor extends to the diapire 103 of bathing pool 100.When being provided with side wireway 380, side wireway 380 also will extend to the diapire 103 of bathing pool 100.
When adopting above-mentioned paste state bed reactor synthesizing methanol, reaction gas enters the gas buffer chamber 200 of paste state bed reactor bottom, then enters gas distributor by central airway 280 and side wireway 380, and gas is tentatively distributed; The eddy flow jet pipe 282 of central airway 280 will be by the partial reaction gas in the central airway 280 by 282 ejections of eddy flow jet pipe, the catalyst granules that is deposited on the paste state bed reactor bottom is expelled, can prevent to promote again catalyst granules to move at whole reactor bathing pool inward eddy because catalyst deposit causes unusual rising of paste state bed reactor bottom temp focus to occur.
In order to further specify better the achieved effect of paste state bed reactor of the present utility model, preferably the gas distribution tube group 620 with gas distributor has at least two annular gas distributor pipes 622 that arrange with one heart, 623,624 is example, reaction gas enters the bathing pool 100 of paste state bed reactor by the passage 580 of gas distributor, gas distributor from the first straight hole 651 reaction gas out around annular rises, reaction gas by the hole 652 of cutting sth. askew to two annular gas distributor pipes 622,623, between 624 or paste state bed reactor inwall place sprays outwardly and remedies at two annular gas distributor pipes 622,623, between 624 or the few drawback of reaction gas that rises on the position of the first straight hole 581 away from of paste state bed reactor inwall, reach and make reaction gas more equally distributed purpose in paste state bed reactor; The atent solvent that contains catalyst granules of bathing pool 100 just has larger contact area in equally distributed reaction gas and the paste state bed reactor, thereby the mobile the best that reaches reaction heat by atent solvent shifts out effect, be that these intensive first uniform straight holes 581 and the hole large strand of conglobation reaction gas of 582 order scripts of cutting sth. askew are divided into a lot of thin strand of uniform reaction gases in bathing pool 100, increase the contact area of reactor and atent solvent, improved the efficient of bathing pool 100 heat exchanges; While reaction under high pressure gas after compression tilts to spray through the hole 582 of cutting sth. askew, the atent solvent that contains catalyst granules that will promote bathing pool 100 motion of spinning, and the atent solvent that the contains catalyst granules driving a reaction cyclonic current conversely in the motion, promote the more even distribution of reaction gas, and because the lengthening in reaction gas path, so that the time of contact of catalyst granules and reaction gas is longer, also so that more atent solvent can conduct heat with reaction gas, thereby at the better heat transfer effect of bathing pool 100 interior acquisitions.This shows, in paste state bed reactor in reaction gas and the strong convection current of atent solvent, whole slurry reactor actuator temperature and distribution of gas are very even, so that reaction rate is faster, the conversion per pass of above-mentioned paste state bed reactor can improve about 15～70% than the conversion per pass of fixed bed reactors after tested.
When being installed in gas distributor of the present utility model in the paste state bed reactor, preferably in the following ways by gas distribution tube group 623 is fixed in the paste state bed reactor, that is: paste state bed reactor also comprises support member 680, the first end of support member 680 links to each other with gas distribution tube group 620, and the second end links to each other with the sidewall 102 of paste state bed reactor.Can realize gas distributor is stabilized in independent action and the synergy that can not affect again in the paste state bed reactor separately by support member 680.As shown in Figure 2, when the gas distribution tube group 620 of gas distributor had at least two annular gas distributor pipes that arrange with one heart at 622,623,624 o'clock, the first end of support member 680 links to each other with outermost annular gas distributed pipeline 623.
As shown in Figure 5, the utility model is in order further to improve reaction gas and the interaction that is deposited on the catalyst on bathing pool 100 diapires 103, effectively catalyst is expelled from diapire 103, the diapire 103 of preferred bathing pool 100 is that the middle vertex of a cone is towards the conical bottom wall of below.
In a kind of preferred embodiment of the utility model, has reaction gas inlet pipe 206 in the gas cushion chamber 200 of above-mentioned paste state bed reactor, reaction gas inlet pipe 206 runs through the sidewall 202 of gas cushion chamber 200, and its gas outlet is towards the diapire 203 of gas cushion chamber 200.
As shown in Figure 5, extraneous reaction under high pressure gas enters by reaction gas air inlet pipe 206 to move upward by pressure-acting behind the gas buffer chamber 2 of paste state bed reactor again and enters gas distributor by central airway 280 and side wireway 380, to finish follow-up distribution of gas effect, the utility model makes when the High Pressure that utilizes extraneous reaction under high pressure gas itself rises between the diapire of reaction under high pressure gas and gas buffer chamber 200 and forms impact, thereby further utilize the diapire of gas buffer chamber 200 that the recoil strength that reaction under high pressure gas produces is risen to central airway 280 and side wireway 380 more rapidly, and, the diapire of reaction under high pressure gas and gas buffer chamber 200 makes reaction gas diffuse to larger scope along shock point when impacting, thereby make reaction gas enter gas distributor with more uniform state by central airway 280 and side wireway 380, optimized the distribution effect of gas distributor to reactor.
As shown in Figure 6, in the another kind of typical embodiment of the utility model, a kind of thick system for methanol synthesis also is provided, thick system for methanol synthesis comprises above-mentioned paste state bed reactor 1, atent solvent recovery system, thick methanol recovery system, reactive gas cleaning system and hydrogen recovery system, and reaction gas produces under catalyst action in paste state bed reactor 1 and generates gas; Have the letter shoot line of generation and atent solvent reflux pipeline between atent solvent recovery system and the paste state bed reactor 1; Thick methanol recovery system and atent solvent recovery system are connected to process from the generation of atent solvent recovery system and are so incensed that the thick methyl alcohol and the circulating air that separate, and have the pipeline that confession part circulating air enters paste state bed reactor 1 between thick methanol recovery system and the paste state bed reactor 1; The hydrogen recovery system hydrogen in the circulating air that reclaims thick methanol recovery system that is connected with thick methanol recovery system; The reactive gas cleaning system one end formation admission line that is connected with fresh reactant source of the gas and hydrogen recovery system has the gas supply line that enters paste state bed reactor 1 for the fresh reactant gas after purifying and hydrogen between the other end and the paste state bed reactor 1.
Because the gas distributor of paste state bed reactor 1 of the present utility model evenly distributes reaction gas, simultaneously in paste state bed reactor 1 internal-response gas and the strong convection current of atent solvent, so that the reaction temperature of each position of whole paste state bed reactor 1 is more even, under same reaction condition, reaction rate accelerates, conversion per pass is higher.After the atent solvent system processes, after separating, atent solvent returns paste state bed reactor so that recycling from the generation gas of paste state bed reactor 1 from generate gas; The generation gas of isolating atent solvent enters the recovery that thick methanol recovery system is carried out thick methyl alcohol; In thick Production of methanol, for fear of catalyst poisoning, the reactor that enters paste state bed reactor 1 is carried out purified treatment remove the impurity that makes catalyst poisoning; And, the reaction of reaction gas in paste state bed reactor 1 is difficult to carry out fully, therefore the unreacted hydrogen of part enters thick methanol recovery system with generating gas, for the utilization rate that increases reaction gas and save cost, adopts hydrogen recovery system to reclaim hydrogen in the circulating air of thick methanol recovery system.
As shown in Figure 6, in a kind of preferred embodiment of the utility model, above-mentioned thick system for methanol synthesis atent solvent recovery system comprises atent solvent condenser 2 and dum boiler 3, atent solvent condenser 2 is arranged on the extension pipeline of the generation letter shoot line between paste state bed reactor 1 and the cyclone separator 10, and is connected with the gas vent of cyclone separator 10; Has pipeloop between dum boiler 3 and the atent solvent condenser 2.Adopt the atent solvent recovery system to be cooled to 100～140 ℃ through the generation gas that cyclone separator 10 was processed, the atent solvent of carrying secretly in the reaction gas is condensed and return slurry reactor gas device 1, realize the recycling of atent solvent, saved the synthetic cost of thick methyl alcohol; Adopt liquid and reaction gas from dum boiler 3 to carry out heat exchange in the process of reaction gas cooling, absorbing heat from the liquid of dum boiler 3 becomes steam and returns dum boiler 3 and cool off or reuse.
As shown in Figure 6, thick methanol recovery system in the above-mentioned preferred embodiment comprises air cooler 4, methanol separator 5, the first compressor 6, condenser 7 and thick methanol recovery device, and atent solvent condenser 2, air cooler 4, methanol separator 5 are communicated be used to reclaiming thick methyl alcohol successively with thick methanol recovery device; Methanol separator 5, the first compressor 6, condenser 7 are communicated be used to reclaiming thick methyl alcohol successively with thick methanol recovery device; The gas vent of methanol separator 5 is connected with hydrogen recovery system; The reactive gas cleaning system of thick methanol recovery system comprises that the second compressor 8 and reactive gas cleaning groove 9, the second compressors 8 are connected with hydrogen recovery system and fresh reactant source of the gas by gas feed; Reactive gas cleaning groove 9 one ends are connected with the gas vent of the second compressor 8, and the other end is connected with paste state bed reactor 1.
Enter air cooler 4 after the atent solvent condensation of generation gas in atent solvent condenser 2 that paste state bed reactor produces and be cooled to 60～70 ℃, entering methanol separator 5 further is cooled to about 45 ℃ again, in methanol separator 5, obtain the circulating air of thick methyl alcohol lime set and gas phase, thick methyl alcohol lime set enters thick methanol recovery device and is further processed and reclaims or directly reclaim, the thick circulating air of gas phase is about 7.1MPa at the pressure in methanol separator 5 exits, then be forced into about 8MPa by the first compressor 6,66 ℃, thick circulating air after the pressurization enters in the housing of condenser 7, temperature is reduced to 45 ℃ after carrying out heat exchange with cooling-air in the heat exchanger tube of condenser 7 and recirculated water, after being condensed, thick methyl alcohol in the thick circulating air enters thick methanol recovery system, remaining gaseous material carries out heat exchange through heat exchanger and drum steam from the heat of dum boiler, the condensate liquid that produces after the heat exchange is recyclable, and the circulating air that obtains is delivered in the paste state bed reactor 1 by the reactive gas cleaning system.The second compressor 8 will contract from the fresh reactant gas of fresh reactant gas source with from the hydrogen-pressure of hydrogen recovery system and be delivered to reactive gas cleaning groove 9, be filled with cleaning catalyst in the reactor purification tank 9 and remove the microcomponent of catalyst for methanol by toxic action, the fresh reactant gas after the purification and hydrogen are transported to paste state bed reactor 1 and react.
As shown in Figure 6, above-mentioned thick system for methanol synthesis also comprises cyclone separator 10, be arranged on the generation letter shoot line between atent solvent recovery system and the paste state bed reactor 1, have the import of the gas of generation, gas vent and solid outlet, generate the gas import and be communicated with generation letter shoot line; Gas vent is communicated with generation letter shoot line; Has the solids backflow pipeline between solid outlet and the paste state bed reactor 1.Gas enters atent solvent condenser 2 and follow-up device results in blockage to device and pipeline with generating to have avoided short grained catalyst.
The above is preferred embodiment of the present utility model only, is not limited to the utility model, and for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any modification of doing, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
Claims (16)
1. gas distributor, described gas distributor comprises:
Central airway (280);
Gas distribution tube group (620), centered by described central airway (280), be arranged on described central airway (280) around, have the passage (650) that communicates with the external world;
Tube connector (630) connects described central airway (280) and gas distribution tube group (620);
It is characterized in that described central airway (280) comprising:
Air inlet supervisor (281), an end is communicated with described tube connector (630);
Be used for spraying a plurality of eddy flow jet pipes (282) of circumferential gyration airflow, an end communicates with the perisporium that (281) are responsible in described air inlet, and the other end is gas vent.
2. gas distributor according to claim 1 is characterized in that,
Described gas distribution tube group (620) comprises at least two annular gas distributor pipes (622,623,624) that arrange with one heart, described passage (650) is distributed in each described annular gas distributor pipe (622,623,624) on the tube wall, and the aperture arranges towards the below;
Described tube connector (630) is along the radially setting of described gas distribution tube group (620) and be communicated with each described annular gas distributor pipe (622,623,624);
The air inlet supervisor's (281) of described central airway (280) lower end is air inlet openings, and the upper end is communicated with described tube connector (630);
The described eddy flow jet pipe of each of described central airway (280) (282) is responsible for circumferentially evenly arranging of (281) along described air inlet, and the gas vent of each described eddy flow jet pipe (282) extends along the oblique below of the central axis that departs from described air inlet supervisor (281).
3. gas distributor according to claim 2 is characterized in that, described eddy flow jet pipe (282) comprising:
Horizontal component is along described air inlet supervisor's (281) radially extension and be connected on described air inlet supervisor's (281) the sidewall;
Vertical component, an end of being responsible for (281) away from described air inlet with described horizontal component is communicated with and straight down extension;
Sloping portion is communicated with the end of described vertical component away from described horizontal component, and is tilted to downward-extension, and the projection of described sloping portion on horizontal plane extended along the direction perpendicular to described horizontal component.
4. gas distributor according to claim 2, it is characterized in that, described passage (650) comprises the hole of cutting sth. askew (652), and the sidewall in the described hole of cutting sth. askew (652) is radially from inside to outside all to counterclockwise or all tilting to extend to clockwise direction.
5. gas distributor according to claim 4, it is characterized in that, described passage (650) also comprises the first straight hole (651), the sidewall of described the first straight hole (651) vertically extends, described the first straight hole (651) and the described hole of cutting sth. askew (652) are at each described annular gas distributor pipe (622,623,624) be intervally arranged on.
6. gas distributor according to claim 2, it is characterized in that, described gas distributor also comprises the side wireway (380) that even number is communicated with described tube connector (630), described side wireway (380) is arranged on two described annular gas distributor pipes (622 in twos symmetrically with respect to described central airway (280), 623,624) on the described tube connector (630) between, and with the equidirectional extension of described central airway (280).
7. gas distributor according to claim 6 is characterized in that, described tube connector (630) comprising:
The first tube connector (631), internal diameter along outermost annular gas distributor pipe (623) extends, pass described gas distribution tube (622,623,624) center is with each described annular gas distributor pipe (622,623,624) be communicated with, described central airway (280) is communicated with the center of described the first tube connector (631);
The second tube connector (632), vertical with described the first tube connector (631), and be arranged between outermost annular gas distributed pipeline (623) and the most inboard annular gas distributed pipeline (622), with each described annular gas distributor pipe (622,623,624) be communicated with, described side wireway (380) is communicated with described the second tube connector (632).
8. gas distributor according to claim 7, it is characterized in that, described the first tube connector (631) is positioned at the caliber of the most inboard described annular gas distributed pipeline (622) greater than the caliber of described the first tube connector (631) remainder, and the caliber of described the first tube connector (631) is less than the caliber of described the second tube connector (632).
9. gas distributor according to claim 8, it is characterized in that, described side wireway (380) is two and is arranged on symmetrically near on second tube connector (632) of described axis with respect to the axis of described gas distribution tube group (620), the part that described side wireway (380) is not set on described the second tube connector (632) has centered by described central airway (280) and along its second straight hole (653) that is circumferentially arranged, the upper length direction along described the first tube connector (631) of described the first tube connector (631) evenly is placed with the 3rd straight hole (654).
10. each described gas distributor in 8 according to claim 2, it is characterized in that, each described annular gas distributor pipe (622,623,624) cross section is annular, and is positioned at the most inboard described annular gas distributed pipeline (622) and is positioned at the internal diameter of outermost described annular gas distributed pipeline (623) greater than the internal diameter of the described annular gas distributed pipeline (624) in the middle of being positioned at.
11. paste state bed reactor, it is characterized in that, comprise bathing pool setting up and down (100) and gas cushion chamber (200), be provided with each described gas distributor in the claim 1 to 10 in the described bathing pool (100), the gas distribution tube group (620) of described gas distributor is fixed on the sidewall (102) of described bathing pool (100), and the central airway of described gas distributor (280) extends to the diapire (103) of described bathing pool (100).
12. paste state bed reactor according to claim 11, it is characterized in that, described paste state bed reactor also comprises support member (680), the first end of described support member (680) links to each other with described gas distribution tube group (620), and the second end links to each other with the sidewall (102) of described paste state bed reactor.
13. paste state bed reactor according to claim 11 is characterized in that, the diapire (103) of described bathing pool (100) is that the middle vertex of a cone is towards the conical bottom wall of below.
14. each described paste state bed reactor in 13 according to claim 11, it is characterized in that, has reaction gas inlet pipe (206) in the described gas cushion chamber (200), described reaction gas inlet pipe (206) runs through the sidewall (202) of described gas cushion chamber (200), and its gas outlet is towards the diapire (203) of described gas cushion chamber (200).
15. a thick system for methanol synthesis is characterized in that, described thick system for methanol synthesis comprises:
Each described paste state bed reactor (1) in the claim 11 to 14, reaction gas produces under catalyst action and generates gas in described paste state bed reactor (1);
The atent solvent recovery system, and have the letter shoot line of generation and atent solvent reflux pipeline between the described paste state bed reactor (1);
Thick methanol recovery system, be connected to process from the generation of described atent solvent recovery system with described atent solvent recovery system and be so incensed that the thick methyl alcohol and the circulating air that separate, and have the pipeline that the described circulating air of confession part enters described paste state bed reactor (1) between described thick methanol recovery system and the described paste state bed reactor (1);
Hydrogen recovery system, the hydrogen in the circulating air that reclaims described thick methanol recovery system that is connected with described thick methanol recovery system;
The reactive gas cleaning system, the one end formation admission line that is connected with fresh reactant source of the gas and described hydrogen recovery system has the gas supply line that enters described paste state bed reactor (1) for the fresh reactant gas after purifying and hydrogen between the other end and the described paste state bed reactor (1).
16. thick system for methanol synthesis according to claim 15, it is characterized in that, described thick system for methanol synthesis also comprises cyclone separator (10), is arranged on the generation letter shoot line between described atent solvent recovery system and the described paste state bed reactor (1), has:
Generate the gas import, be communicated with described generation letter shoot line;
Gas vent is communicated with described generation letter shoot line;
Solid outlet, and have the solids backflow pipeline between the described paste state bed reactor (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205053497U CN202823320U (en) | 2012-09-28 | 2012-09-28 | Gas distributor, slurry bed reactor comprising same and crude methanol synthesis system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012205053497U CN202823320U (en) | 2012-09-28 | 2012-09-28 | Gas distributor, slurry bed reactor comprising same and crude methanol synthesis system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202823320U true CN202823320U (en) | 2013-03-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012205053497U Withdrawn - After Issue CN202823320U (en) | 2012-09-28 | 2012-09-28 | Gas distributor, slurry bed reactor comprising same and crude methanol synthesis system |
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| CN (1) | CN202823320U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102872769A (en) * | 2012-09-28 | 2013-01-16 | 神华集团有限责任公司 | Gas distributor and slurry bed reactor and crude carbinol synthetic system both comprising same |
| CN104226208A (en) * | 2013-06-06 | 2014-12-24 | 神华集团有限责任公司 | Gas distributor for multiphase flow reactor and multiphase flow reactor |
| CN108905904A (en) * | 2018-09-05 | 2018-11-30 | 上海兖矿能源科技研发有限公司 | A kind of gas distributor for Fischer-Tropsch synthesis device |
| CN109107498A (en) * | 2017-06-26 | 2019-01-01 | 神华集团有限责任公司 | gas distributor and reactor |
-
2012
- 2012-09-28 CN CN2012205053497U patent/CN202823320U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102872769A (en) * | 2012-09-28 | 2013-01-16 | 神华集团有限责任公司 | Gas distributor and slurry bed reactor and crude carbinol synthetic system both comprising same |
| CN102872769B (en) * | 2012-09-28 | 2015-04-22 | 神华集团有限责任公司 | Gas distributor and slurry bed reactor and crude carbinol synthetic system both comprising same |
| CN104226208A (en) * | 2013-06-06 | 2014-12-24 | 神华集团有限责任公司 | Gas distributor for multiphase flow reactor and multiphase flow reactor |
| CN104226208B (en) * | 2013-06-06 | 2016-07-06 | 神华集团有限责任公司 | A kind of gas distributor for multiphase flow reactor and multiphase flow reactor |
| CN109107498A (en) * | 2017-06-26 | 2019-01-01 | 神华集团有限责任公司 | gas distributor and reactor |
| CN108905904A (en) * | 2018-09-05 | 2018-11-30 | 上海兖矿能源科技研发有限公司 | A kind of gas distributor for Fischer-Tropsch synthesis device |
| CN108905904B (en) * | 2018-09-05 | 2024-05-28 | 上海兖矿能源科技研发有限公司 | Gas distribution method for Fischer-Tropsch synthesis reactor |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20130327 Effective date of abandoning: 20150422 |