CN102730638A - Fluidized bed transformation reactor and fluidized bed transformation system with same - Google Patents
Fluidized bed transformation reactor and fluidized bed transformation system with same Download PDFInfo
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- CN102730638A CN102730638A CN2012102544148A CN201210254414A CN102730638A CN 102730638 A CN102730638 A CN 102730638A CN 2012102544148 A CN2012102544148 A CN 2012102544148A CN 201210254414 A CN201210254414 A CN 201210254414A CN 102730638 A CN102730638 A CN 102730638A
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Abstract
The invention provides a fluidized bed transformation reactor and a fluidized bed transformation system with the same. The fluidized bed transformation reactor comprises a tank body, a first heat exchanger (5) and a catalyst separation device, wherein the tank body is provided with an inner cavity, the bottom of the tank body is provided with a gas inlet (6), and the top of the tank body is provided with a gas outlet (7); the first heat exchanger (5) is arranged in the tank body; the catalyst separation device comprises a filter (2) and a filter back flushing device, wherein the filter (2) is arranged in the tank body and positioned above the first heat exchanger (5), and the filter (2) comprises a plurality of groups of filter elements; and the filter back flushing device is provided with a plurality of filter back flushing ports (1), each filter back flushing port (1) corresponds to each filter element in a plurality of groups of filter elements, and the filter back flushing ports (1) are positioned above the filter elements. The fluidized bed transformation reactor can be used for catalyst separation, and is simple in structure.
Description
Technical field
The present invention relates to technical field of coal chemical industry, in particular to a kind of fluidized-bed shift-converter and have its fluidized-bed transformation system.
Background technology
Carbon monoxide and water vapour carry out transformationreation under the effect of catalyzer, generate hydrogen and carbonic acid gas, are the important preprocessing process of Coal Chemical Industry synthetic gas.The transformed depth that in shift conversion step, can control synthetic gas is regulated the ratio of hydrogen and carbon monoxide in the synthetic gas, and conversion product gas can be used for synthesizing methanol, synthetic ammonia after through the desulfurization in downstream, decarbonization process, Fischer-Tropsch is synthetic and technological process such as DCL/Direct coal liquefaction.
The synthetic gas converter technique that generally adopts in the world at present is axially-located bed synthetic gas conversion process.Because the synthetic gas conversion is thermopositive reaction; The hot(test)-spot temperature of the temperature out of reaction bed transformationreation just; For the work-ing life that guarantees that catalyzer uses and prolongs catalyzer under suitable temperature; The heat that needs in time transformationreation to be generated is removed, and this is difficult relatively for fixed-bed reactor.
In addition; For present large-scale Coal Chemical Industry, uniserial synthetic gas conversion load is very big, and the content of carbon monoxide is also higher relatively in the synthetic gas simultaneously; Therefore need two sections or more conversion equipment; Each conversion equipment is bulky high-tension apparatus, has increased the complicacy of conversion process flow process on the one hand, has also increased synthetic gas interconversion rate control degree of difficulty simultaneously.
Sum up present fixed bed conversion process and mainly contain following shortcoming: 1) transformationreation is a strong exothermal reaction; If the CO concentration in the general synthetic gas surpasses 15%; Reach higher CO interconversion rate; The fixed-bed reactor of two sections or multistage then need be set, and unit equipment is more, and process system is very complicated; 2) the heat exchange weak effect of beds; Catalyzer is when heating reduction or sulfuration; No matter using the cobalt molybdenum is low change catalyzer; Also be to use the Fe-Cr series hts catalyst, a large amount of heats that produce in the reaction process are difficult for shifting out from bed soon, so misoperation causes the reactor bed overtemperature easily; 3) fixed-bed reactor can only be selected the bigger granules of catalyst of particle diameter for use in order to control inlet outlet pressure differential, and therefore the existence of inside and outside diffusional effect has reduced transformationreation speed, and this just needs bigger loaded catalyst, thereby has increased running cost; 4) in fixed-bed reactor, beds will produce thermograde, thereby have reaction focus (general this reaction focus is positioned at the outlet of reactor drum), and the catalyzer easy ageing inactivation at the focus place is that low change catalyzer is prone to the reversal of cure inactivation for the cobalt molybdenum.
Technical barriers such as conventional axial fixed bed shift-converter bed pressure drag is big in order to solve, heat exchange weak effect, technical process complicacy; On the basis of axial restraint bed bioreactor, developed the diameter of axle again in succession to fixed bed shift-converter and radial fixed-bed shift-converter; These two kinds of reactor drums are because synthetic gas is radial flow in reactor drum; Improved transformationreation efficient to a certain extent; Reduced the usage quantity of transformation catalyst bed inlet outlet pressure differential and catalyzer, the effect of heat exchange simultaneously makes moderate progress, but in actual moving process, the phenomenon of synthetic gas short circuit often occurs; And these two kinds of reactor types fundamentally do not solve problems such as fixed bed conversion process flow process is complicated, reaction moves the heat difficulty and the reaction focus is wayward; And the diameter of axle of domestic present employing still needs from external introduction to fixed-bed reactor core inner member, and cost is higher, and manufacturing and maintenance intervals are longer.
Fluidized-bed reactor, heat and mass transfer performance is good, it is convenient to move heat, and temperature of reaction is easy to control; Can realize isothermal run; Catalyst grain size is little, and mass-and heat-transfer efficient is high, and the gas-solid contact area is big; Allow the synthetic gas conversion to have higher CO per pass conversion, dwindled the volume of shift-converter greatly.Simultaneously, the loading and unloading of catalyzer are more convenient in the fluidized-bed reactor.After adopting fluidized-bed reactor, reactor drum inner conversion catalyzer is fluidized state, and temperature can reach more uniformly and distribute.Heat production coil pipe is set in fluidized-bed reactor, can easily reaction heat be in time removed, thereby prevent that the variety of issue that overheating problem and catalyzer overtemperature are brought from appearring in catalyst area, built-in interchanger can produce steam simultaneously.Therefore the conversion of adopting fluidized-bed reactor to carry out synthetic gas can improve conversion efficiency significantly, solves the unmanageable problem of reaction focus in the conversion process, and simultaneously, the conversion process flow process will be reduced greatly.
Application number is that the Chinese invention patent of 99112426.X discloses a kind of conversion process that adopts fluidized-bed reactor, and behind the synthetic gas process fluidized-bed shift-converter, conversion product gas separates the back with the conversion solid particle catalyst and gets into lower procedure.In this invention the separation method of transformation catalyst and product gas is not described.
Application number is that the Chinese invention patent of 200810173645.X discloses a kind of process for transforming fluidized bed of synthetic gas; In this technology; The conversion product gas that comes out from fluidized-bed separates transformation catalyst through cyclonic separator, and the catalyzer of separating gets in the fluidized-bed reactor again.This technology has guaranteed the content of the catalyzer in the reactor drum owing to adopt external placed type transformation catalyst separation method, but said structure makes the shift-converter structure relative complex that becomes, and possibly exist catalyst distribution uneven and to problems such as pipeline erosions simultaneously.
Summary of the invention
The present invention aims to provide a kind of fluidized-bed transformation system that can carry out catalyst separating and fluidized-bed shift-converter simple in structure and have it.
To achieve these goals, according to an aspect of the present invention, a kind of fluidized-bed shift-converter is provided, has comprised: tank body, have inner chamber, the bottom of tank body is provided with gas feed, and the top is provided with pneumatic outlet; First interchanger is arranged in the tank body, and the fluidized-bed shift-converter also comprises: catalyst separation device, and catalyst separation device comprises: strainer, be arranged in the tank body and be positioned at the top of first interchanger, strainer comprises many group filter cores; The strainer back-blowing device has a plurality of strainer back blow ports, and each strainer back blow port is provided with each filter core of organizing in the filter cores correspondingly, and the strainer back blow port is positioned at the top of filter core.
Further, be in open mode more, be in closing condition more corresponding to the strainer back blow ports of organizing the filter core of all the other groups in the filter cores corresponding to the strainer back blow ports of organizing one or more groups filter core in the filter cores.
Further, the strainer back-blowing device also comprises and is used to control a plurality of valves of opening or closing of each strainer back blow port and the unit that all is electrically connected with each valve.
Further, every group of filter core comprises many filter cores, is disposed with gas distributor and grid distributor between the gas feed and first interchanger.
Further; Tank body comprises by following from the last first tank body section, the second tank body section and the 3rd tank body section that connects successively; The diameter of the first tank body section is less than the diameter of the 3rd tank body section; The diameter of the second tank body section is by become big from last down gradually, and first interchanger is positioned at the first tank body section, and catalyst separation device is positioned at the second tank body section.
According to a further aspect in the invention; A kind of fluidized-bed transformation system is provided; Comprise pretreater and the fluidized-bed shift-converter that is connected with pretreater; The fluidized-bed shift-converter is each a fluidized-bed shift-converter in the claim 1 to 5; The pneumatic outlet of fluidized-bed shift-converter is connected with product gas escape pipe, is connected with the blowback pipeline that is used for providing purge gas to the strainer back-blowing device of fluidized-bed shift-converter on the product gas escape pipe, and the blowback pipeline is connected with the strainer back-blowing device.
Further, the blowback pipeline is provided with compressor.
Further; The gas inlet of pretreater is connected with the synthetic gas inlet pipe; First interchanger of fluidized-bed shift-converter comprises water coolant overcurrent pipeline, and the fluidized-bed transformation system also comprises second interchanger and the 3rd interchanger, and second interchanger is positioned at the upper reaches of the 3rd interchanger; Second interchanger is used for synthetic gas inlet pipe and the heat exchange of product gas escape pipe, and the 3rd interchanger is used for the heat exchange of water coolant overcurrent pipeline and product gas escape pipe.
Further, the blowback pipeline is connected the downstream of second interchanger.
Further, the outlet of water coolant overcurrent pipeline is divided into two branch roads, and a branch road in two branch roads is connected with the gas feed of fluidized-bed shift-converter.
Use technical scheme of the present invention; In the tank body of fluidized-bed shift-converter, be provided with catalyst separation device; This catalyst separation device disposes strainer and strainer back-blowing device; The filter core of strainer is used for the filtration of catalyzer, can carry out the separation of catalyzer effectively, and the filter back-blowing device is used for carrying out blowback to filter core.Like this, fluidized-bed shift-converter of the present invention can carry out the separation of catalyzer through catalyst separation device, simultaneously, has omitted that catalyzer separates required equipment in the prior art outside shift-converter, makes that the structure of fluidized-bed shift-converter is simpler.
Description of drawings
The Figure of description that constitutes the application's a part is used to provide further understanding of the present invention, and illustrative examples of the present invention and explanation thereof are used to explain the present invention, do not constitute improper qualification of the present invention.In the accompanying drawings:
Fig. 1 shows the structural representation according to the embodiment of fluidized-bed shift-converter of the present invention; And
Fig. 2 shows the structural representation according to the embodiment of fluidized-bed transformation system of the present invention.
Embodiment
Need to prove that under the situation of not conflicting, embodiment and the characteristic among the embodiment among the application can make up each other.Below with reference to accompanying drawing and combine embodiment to specify the present invention.
As shown in Figure 1, the fluidized-bed shift-converter of present embodiment comprises: tank body, first interchanger 5 and the catalyst separation device.Tank body has inner chamber, and the bottom of tank body is provided with gas feed 6, and the top is provided with pneumatic outlet 7; First interchanger 5 is arranged in the tank body; Catalyst separation device comprises: strainer 2 and strainer back-blowing device; Strainer 2 is arranged in the tank body and is positioned at the top of first interchanger 5, and strainer 2 comprises many group filter cores, preferably; Strainer 2 comprises at least two group filter cores, and every group of filter core comprises many filter cores; The strainer back-blowing device has a plurality of strainer back blow ports 1, and each strainer back blow port 1 is provided with each filter core of organizing in the filter cores correspondingly, and strainer back blow port 1 is positioned at the top of filter core; Other group filter cores when wherein, organizing one or more groups filter core in the filter core more and be in the blowback state that cooperates with the strainer back-blowing device in many group filter cores are in the filtration state that does not cooperate with the strainer back-blowing device.
In the present embodiment; In the tank body of fluidized-bed shift-converter, be provided with catalyst separation device; This catalyst separation device disposes strainer 2 and strainer back-blowing device; The filter core of strainer 2 is used for the filtration of catalyzer, can carry out the separation of catalyzer effectively, and the filter back-blowing device is used for carrying out blowback to filter core.Like this; The fluidized-bed shift-converter of present embodiment can carry out the separation of catalyzer through catalyst separation device; Simultaneously, omitted that catalyzer separates required equipment in the prior art outside shift-converter, made that the structure of fluidized-bed shift-converter is simpler.
In the present embodiment; In order to guarantee the continuous operation of fluidized-bed shift-converter; It still is that the blowback state can be set in advance that filter core is in the filtration state, but preferably can guarantee, is in open mode so that the filter core of this group or many groups is in the blowback state corresponding to the strainer back blow ports 1 of organizing one or more groups filter core in the filter cores more; Be in closing condition corresponding to the strainer back blow ports 1 of organizing the filter core of all the other groups in the filter cores, so that the filter core of all the other groups is in the filtration state more.That is, filtration and blowback can be carried out simultaneously.Need to prove that at the initial stage of fluidized-bed shift-converter operation, also all filter core all is in the filtration state.
The strainer back-blowing device also comprises and is used to control a plurality of valves of opening or closing of each strainer back blow port 1 and the unit that is electrically connected with each valve.The switch of valve controlled filter device back blow port 1, thereby the blowback of the filter core of controlled filter device 2, simultaneously, through the opening and closing of each valve of unit control.This unit is preferably PLC (programmable logic controller, automation controller able to programme) or DCS (distributed control system, dispersing control system).When one group of filter core wherein is in the blowback state; The valve open of the strainer back blow port 1 that this filter core is corresponding, the blowback air of being come by compressor carries out blowback to the reorganization filter core, and preferably blowback finishes in 2-5 minute; Valve-off then, this group filter core gets into the filtration state again; Then next group filter core gets into the blowback state, goes round and begins again.
Certainly, the replacement scheme as those skilled in the art can know also can be provided with the valve of quantity less than strainer back blow port 1 quantity, removes to control a set filter back blow port 1 (this set filter back blow port 1 corresponding one group of filter core) by a valve.At this moment, only need valve is arranged on the main road, each strainer back blow port 1 that a plurality of branch roads of connection are connected respectively in the set filter back blow port 1 on main road again gets final product.
Preferably, the strainer purge gas adopts the conversion product gas through pressurization.Particularly; As shown in Figure 2; Pneumatic outlet 7 at the fluidized-bed shift-converter is connected with product gas escape pipe 71; Be connected with the blowback pipeline 72 that is used for providing purge gas to the strainer back-blowing device of fluidized-bed shift-converter on the product gas escape pipe 71, blowback pipeline 72 is connected with the strainer back-blowing device.
In the present embodiment, be disposed with gas distributor 4 and grid distributor 3 between the gas feed 6 and first interchanger 5.Wherein grid distributor 3 preferably adopts orifice plate, silk screen or bubble-cap forms.
In the present embodiment; Tank body comprises by following from the last first tank body section, the second tank body section and the 3rd tank body section that connects successively; The diameter of the first tank body section is less than the diameter of the 3rd tank body section; The diameter of the second tank body section is by become big from last down gradually, and first interchanger 5 is positioned at the first tank body section, and catalyst separation device is positioned at the second tank body section.First interchanger 5 is removed the heat that transformationreation generates, the temperature of control fluidized-bed shift-converter bed.Can reduce the entrainment velocity of catalyzer after above-mentioned reducing design makes gas get into the 3rd tank body section, thereby be convenient to the separation of catalyzer.
Preferably, preferably to adopt precision be the sintered metal filtration filter core of 5um to the filter core of the strainer 2 of present embodiment.Preferably, present embodiment can be handled the synthetic gas that CO content is 5-65%.Service temperature 180-300 ℃ of being suitable for of present embodiment, pressure 1-10MPa.The median size of the transformation catalyst of present embodiment is 10-200um, and it is transformation catalyst that catalyzer adopts the wide temperature cobalt of anti-sulphur molybdenum, and the loadings of catalyzer is the 10-30% of empty bed volume.The gas empty bed speed of operation is controlled at 0.2-0.8m/s, guarantees the fluid effect of beds.
The present invention also provides a kind of fluidized-bed transformation system; As shown in Figure 2; Embodiment according to fluidized-bed transformation system of the present invention comprises pretreater 11 and the fluidized-bed shift-converter that is connected with pretreater 11; The fluidized-bed shift-converter is above-mentioned fluidized-bed shift-converter; The pneumatic outlet 7 of fluidized-bed shift-converter is connected with product gas escape pipe 71, is connected with the blowback pipeline 72 that is used for providing purge gas to the strainer back-blowing device of fluidized-bed shift-converter on the product gas escape pipe 71, and blowback pipeline 72 is connected with the strainer back-blowing device.The fluidized-bed transformation system of present embodiment can carry out catalyst separating and simple in structure.Preferably, the blowback pipeline is provided with compressor 13.
In the present embodiment; The gas inlet of pretreater is connected with synthetic gas inlet pipe 14; First interchanger 5 of fluidized-bed shift-converter comprises water coolant overcurrent pipeline 16, and the fluidized-bed transformation system comprises that also second interchanger 12 and the 3rd interchanger 18, the second interchanger 12 are positioned at the upper reaches of the 3rd interchanger 18; Second interchanger 12 is used for synthetic gas inlet pipe 14 and 71 heat exchange of product gas escape pipe, and the 3rd interchanger 18 is used for the heat exchange of water coolant overcurrent pipeline 16 and product gas escape pipe 71.Preferably, blowback pipeline 72 is connected the downstream of second interchanger 12.
Preferably, the outlet of water coolant overcurrent pipeline 16 is divided into two branch roads, and a branch road 17 in two branch roads is connected with the gas inlet 6 of fluidized-bed shift-converter.Water in the branch road 17 and/or water vapour can be used to adjust the water to steam ratio of the synthetic gas that gets into the fluidized-bed shift-converter.
The conversion process process of the fluidized-bed transformation system of present embodiment is following:
From (temperature 150-300 ℃ of the synthetic gas of upstream units; Pressure 1-10MPa), after 18 heat exchange of the 3rd interchanger, gets into pretreater 11, further remove hazardous and noxious substances with conversion product gas (flowing out) from the pneumatic outlet 7 of fluidized-bed shift-converter; After the gas that comes out and steam (flowing out from branch road 17) mix; Controlled temperature is 180-300 ℃ (being higher than 25 ℃ of synthetic gas dew-point temperatures), through the bottom of gas feed 6 entering fluidized-bed shift-converters, behind gas distributor 4 and grid distributor 3; Entering is equipped with in the fluidized-bed that the cobalt molybdenum is a transformation catalyst (between the grid distributor 3 and first interchanger 5); Transformationreation takes place in carbon monoxide and water vapour in the fluidized-bed of transformation catalyst is housed, generate carbonic acid gas and hydrogen, and reaction institute liberated heat is removed by first interchanger 5.In first interchanger 5, adopt mesohigh saturation water, by-product mesohigh moist steam.The gas that generates through transformationreation obtains clean conversion product gas after built-in filter 2 is filtered granules of catalyst; Part conversion product gas gets into 1 pair of strainer 2 of strainer back blow port after compressor 13 compressions filter core carries out blowback, gets into postorder workshop section then.The pressure of controlled filter device purge gas and strainer place pressure reduction are no more than 0.5MPa, are preferably 0.3-0.5Mpa.This pressure reduction control has guaranteed the blowback effect can not cause damage to filter core simultaneously.Through the measurement that reactor batch temperature, conversion product gas are formed, control the synthetic gas load that gets into fluidized-bed reactor, operating parameterss such as the proportioning of steam and synthetic gas and synthetic gas feeding temperature.
From above description, can find out that the above embodiments of the present invention have realized following technique effect:.
1, the catalyzer in the fluidized-bed shift-converter is fluidized state, and the mixed effect of catalyzer and reactant gases is better, and the catalyst bed layer resistance can not increase with the prolongation of running time.
2, the heat exchange effect of first interchanger and the better effects if of regulating and controlling temperature in the fluidized-bed shift-converter can significantly reduce the probability of beds generation overheating problem, prevent sintering of catalyst and reversal of cure inactivation.
3, the fluidized-bed shift-converter can be selected catalyst particle for use; Increased total geometrical surface of per volume of catalyst; The shift activity of per volume of catalyst is significantly improved, and the utilization ratio of per volume of catalyst improves greatly, and catalyst consumption can significantly reduce.
4, the fluidized-bed shift-converter can be formed and arts demand adjustment catalyst for water-gas shift reaction amount according to virgin gas, thereby reaches the requirement of control change reaction depth; The loading and unloading of transformation catalyst simultaneously are convenient easily.
5, the fluidized-bed shift-converter is located at transformationreation and catalyst separation device in its tank body; Omitted that catalyzer separates required equipment in original fluidized-bed conversion process outside shift-converter; Guaranteed under the different operating condition; Catalyst in reactor content has been simplified the conversion process flow process simultaneously.
The above is merely the preferred embodiments of the present invention, is not limited to the present invention, and for a person skilled in the art, the present invention can have various changes and variation.All within spirit of the present invention and principle, any modification of being done, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. fluidized-bed shift-converter comprises:
Tank body has inner chamber, and the bottom of said tank body is provided with gas feed (6), and the top is provided with pneumatic outlet (7);
First interchanger (5) is arranged in the said tank body,
It is characterized in that said fluidized-bed shift-converter also comprises: catalyst separation device, said catalyst separation device comprises:
Strainer (2) is arranged in the said tank body and is positioned at the top of said first interchanger (5), and said strainer (2) comprises many group filter cores;
The strainer back-blowing device has a plurality of strainer back blow ports (1), and each said strainer back blow port (1) is provided with said each filter core of organizing in the filter cores correspondingly, and said strainer back blow port (1) is positioned at the top of said filter core.
2. fluidized-bed shift-converter according to claim 1; It is characterized in that; Strainer back blow port (1) corresponding to one or more groups filter core in said many group filter cores is in open mode, is in closing condition corresponding to the said strainer back blow ports (1) of organizing the filter core of all the other groups in the filter cores more.
3. fluidized-bed shift-converter according to claim 2; It is characterized in that said strainer back-blowing device also comprises and is used to control a plurality of valves of opening or closing of each said strainer back blow port (1) and the unit that all is electrically connected with each said valve.
4. fluidized-bed shift-converter according to claim 1 is characterized in that, every group of filter core comprises many filter cores, is disposed with gas distributor (4) and grid distributor (3) between said gas feed (6) and first interchanger (5).
5. fluidized-bed shift-converter according to claim 1; It is characterized in that; Said tank body comprises that by down from the last first tank body section, the second tank body section and the 3rd tank body section that connects successively, the diameter of the said first tank body section is less than the diameter of said the 3rd tank body section, and the diameter of the said second tank body section is by becoming big gradually from last down; Said first interchanger (5) is positioned at the said first tank body section, and said catalyst separation device is positioned at the said second tank body section.
6. fluidized-bed transformation system; Comprise pretreater (11) and the fluidized-bed shift-converter that is connected with said pretreater (11); It is characterized in that; Said fluidized-bed shift-converter is each described fluidized-bed shift-converter in the claim 1 to 5; The pneumatic outlet of said fluidized-bed shift-converter (7) is connected with product gas escape pipe (71), is connected with the blowback pipeline (72) that is used for providing purge gas to the strainer back-blowing device of said fluidized-bed shift-converter on the said product gas escape pipe (71), and said blowback pipeline (72) is connected with said strainer back-blowing device.
7. fluidized-bed transformation system according to claim 6 is characterized in that, said blowback pipeline is provided with compressor (13).
8. fluidized-bed transformation system according to claim 6; It is characterized in that; The gas inlet of said pretreater is connected with synthetic gas inlet pipe (14); First interchanger (5) of said fluidized-bed shift-converter comprises water coolant overcurrent pipeline (16), and said fluidized-bed transformation system also comprises second interchanger (12) and the 3rd interchanger (18), and said second interchanger (12) is positioned at the upper reaches of said the 3rd interchanger (18); Said second interchanger (12) is used for said synthetic gas inlet pipe (14) and said product gas escape pipe (71) heat exchange, and said the 3rd interchanger (18) is used for the heat exchange of said water coolant overcurrent pipeline (16) and said product gas escape pipe (71).
9. fluidized-bed transformation system according to claim 8 is characterized in that, said blowback pipeline (72) is connected the downstream of said second interchanger (12).
10. fluidized-bed transformation system according to claim 8; It is characterized in that; The outlet of said water coolant overcurrent pipeline (16) is divided into two branch roads, and the branch road (17) in said two branch roads is connected with the gas feed (6) of said fluidized-bed shift-converter.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105214575A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | New and effective detection reaction device |
| CN110397914A (en) * | 2019-07-31 | 2019-11-01 | 张家港市昇泰能源有限公司 | A kind of air preheater for furfural dregs fluidized bed |
| CN111715030A (en) * | 2020-07-17 | 2020-09-29 | 广州金鹏环保工程有限公司 | Fluidized bed waste gas zero discharge system |
| JP7527236B2 (en) | 2021-03-30 | 2024-08-02 | 大阪瓦斯株式会社 | Reformation treatment equipment |
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| CN201632251U (en) * | 2010-04-02 | 2010-11-17 | 中国石油化工集团公司 | Fluid bed reactor with automatic back flush filter |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105214575A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | New and effective detection reaction device |
| CN110397914A (en) * | 2019-07-31 | 2019-11-01 | 张家港市昇泰能源有限公司 | A kind of air preheater for furfural dregs fluidized bed |
| CN111715030A (en) * | 2020-07-17 | 2020-09-29 | 广州金鹏环保工程有限公司 | Fluidized bed waste gas zero discharge system |
| JP7527236B2 (en) | 2021-03-30 | 2024-08-02 | 大阪瓦斯株式会社 | Reformation treatment equipment |
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Application publication date: 20121017 |