CN203389625U - Slurry bed reaction device - Google Patents
Slurry bed reaction device Download PDFInfo
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- CN203389625U CN203389625U CN201320492007.0U CN201320492007U CN203389625U CN 203389625 U CN203389625 U CN 203389625U CN 201320492007 U CN201320492007 U CN 201320492007U CN 203389625 U CN203389625 U CN 203389625U
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Abstract
The utility model provides a slurry bed reaction device. The slurry bed reaction device comprises a reaction barrel (1), a separator (2) and a filter (3), wherein a top opening of the reaction barrel (1) stretches into the separator (2); the outer wall of the reaction barrel (1) is connected with the bottom of the separator (2); the separator (2) is communicated with the filter (3) by a liquid-phase outlet (14); the filter (3) is communicated with the bottom of the reaction barrel (1) by a slurry liquid outlet (22); a gas outlet (13) is formed in the upper part of the separator (2); a gas inlet (12), a liquid-phase material inlet (11) and a discharge opening (15) are formed in the lower part of the reaction barrel (1). The slurry bed reaction device provided by the utility model integrates reaction, gas-liquid separation, liquid-solid separation, heat exchange and washing, is simple and practical in structure, convenient to operate, small in occupying area and easy to perform large-scale production, and is applicable to various gas-liquid-solid three-phase reaction systems and a relatively wide crystal grain diameter range; the continuous and stable operation is realized.
Description
Technical field
The utility model relates to a kind of slurry reactor device, for liquid-solid or gas-liquid-solid reaction field.
Background technology
Paste state bed reactor is a kind of consersion unit of conventional gas-liquid-solid three-phase contact.Liquid is continuous phase, and gas and solid are decentralized photo.Gas, as the power that mixes and promote, is suspended in catalyst in liquid phase and reacts.Owing to there is no mechanical agitation, thereby can be under high pressure without leaking operation.Paste state bed reactor all adopts finely grained catalyst conventionally, its granularity is generally between 10-150 micron, can effectively eliminate the impact of interior diffusion couple reaction, there is very high catalytic efficiency, paste state bed reactor is easily realized isothermal operation, is avoided occurring bed focus simultaneously, is beneficial to features such as improving reaction selectivity.
Although paste state bed reactor has lot of advantages, but the application in petrochemical process is not extensive, the topmost reason that restricts its application is in the separation problem that adopts product that finely grained catalyst brings and catalyst granules, slurries transportation problem, product, to carry micro-solid particle secretly and for addressing these problems a series of engineering problems that bring.Chinese scholars has proposed many improvement projects for this reason.
GB2403728A discloses a kind of method products of separated and catalyst that adopts the outer filtration of device, but this process route is longer.And, from paste state bed reactor, extract the conveying of suspension out and return to the conveying of paste state bed reactor, and the power that the catalyst slurry being filtered is carried is all provided by pump, not only energy consumption is higher, in process, very easily cause the breakage of catalyst granules, increased the difficulty of liquid-solid separation, to reactor, macrocyclic operation brings inconvenience.
CN102049222A has proposed a kind of paste state bed reactor that filter assemblies is set in tedge inside, but the dismounting of this filter is difficult, also increased the complexity of inside reactor structure, the maintenance of filter is changed the operating influence of slurry state bed very large, is difficult to maximize simultaneously.In addition, do not consider that slurries are degassed, bubbles in slurries, has increased slurries circulating line vapour lock, and gas is occupied filter medium surface simultaneously, and filter efficiency is low.
CN1233451C discloses a kind of paste state bed reactor that contains distribution of gas parts, heat exchanger components, liquid-solid separating component and foam removal parts, but structure of reactor is complicated, operate complicated, multiple inner member has not only taken the reaction compartment in reactor, make height for reactor higher, but also the control of impact slurry state bed inner fluid flow pattern.
CN101314120A discloses a kind of slurry bed circulatory flow reactor that comprises tedge and down-comer.Wherein, the decanting zone that tedge is expanded by reaction zone and caliber forms.Between decanting zone and reaction zone, having aperture is communicated with.Although this reactor adopts gas to replace pump transmitting power, peripheral hardware filter to be provided, to be provided with degas zone, because slurry state bed adopts micron order finely grained catalyst conventionally, so the diameter of decanting zone need to be very large.Therefore, this reactor is only applicable to the situation that catalyst granules is larger.And decanting zone catalyst particles concentration is higher, can cause over-reactive generation, further causes the adverse consequences such as coking, catalysqt deactivation.
From analyzing above, the conveying of the liquid phase of paste state bed reactor, liquid-solid separation, gas-liquid separation, reaction heat-obtaining are several key issues that must solve.
Utility model content
The technical problem that the utility model solves be to provide a kind of simple and practical, easy to operate, floor space is few, be easy to the slurry reactor device that maximizes.
The slurry reactor device that the utility model provides, comprise reaction tube 1, separator 2 and filter 3, separator 2 inside are stretched in the open top of described reaction tube 1, the outer wall of reaction tube 1 is connected with separator 2 bottoms, described separator 2 is communicated with filter 3 through liquid-phase outlet 14, and described filter 3 is communicated with the bottom of reaction tube 1 through slurries outlet 22; Described separator 2 tops are provided with gas vent 13, and described reaction tube 1 bottom is provided with gas access 12, liquid phase entrance 11 and discharge port 15.
The application process of the slurry reactor device that the utility model provides, raw material enters reaction tube 1 bottom by liquid phase entrance 11 and/or gas access 12, and the mixing of the slurries in reaction tube 1, contacts and react with catalyst, upwards flows simultaneously; Under gas push, reaction logistics flows into separator 2 from reaction tube 1 open top, carries out after gas-liquid separation, and slurries enter filter 3 from liquid-phase outlet 14, and gas is from gas vent 13 dischargers at separator 2 tops; After slurries filter in filter 3, clear liquid is drawn reaction unit as product by purified liquor outlet 19; The slurries that flowed out by slurries outlet 22 return in reaction tube 1 and continue to participate in reacting.
The slurry reactor device that the utility model provides and the beneficial effect of application process thereof are:
The slurry reactor device that the utility model provides arranges separator on reaction tube top, reaction logistics flow velocity in separator reduces, gas is fully separated with slurries, can avoid the vapour lock in feed-line, also avoid gas to enter filter and occupied filter core surface, guaranteed the operation of filter efficient stable.Separator bottom through liquid-phase outlet inflow filter, then loops back reaction tube bottom through the slurries outlet of filter containing the slurries of solid catalyst particle, and slurries rely on potential difference to flow, and have saved circulating consumption.Slurry reactor device integrated level of the present utility model is high, simple in structure, floor space is few, highly versatile and be easy to industrialization and amplify.The application process of the slurry reactor device that the utility model provides is applicable to multiple reaction system, stable operation.
Accompanying drawing explanation
The structural representation of the slurry reactor device that accompanying drawing 1 provides for the utility model;
The structural representation that accompanying drawing 2 is the slurry reactor device that adopts in embodiment.
Wherein:
1-reaction tube, 2-separator, 3-filter, 4-heat exchanger, 5-washing section, 6-compressor, 7,8-pipeline, 11-liquid phase entrance ，12-gas access, 13-gas vent, 14-liquid-phase outlet, 15-discharge port, 16-catalyst charging hole, 17-backwash liquid inlet, 18-cleaning solution entrance, 19-purified liquor outlet, 20-fluid level controller, 21-differential pressure controller, the outlet of 22-slurries.
The specific embodiment
Below describe the specific embodiment of the present utility model in detail, wherein, " top " of the container of mentioning in description refers to the position of the 0-30% of container from top to bottom, " bottom " of container refers to the position of the 50%-100% of container from top to bottom, and " bottom " of container refers to the position of the 90%-100% of container from top to bottom.
The slurry reactor device that the utility model provides, comprise reaction tube 1, separator 2 and filter 3, separator 2 inside are stretched in the open top of described reaction tube 1, the outer wall of reaction tube 1 is connected with separator 2 bottoms, described separator 2 is communicated with filter 3 through liquid-phase outlet 14, and described filter 3 is communicated with the bottom of reaction tube 1 through slurries outlet 22; Described separator 2 tops are provided with gas vent 13, and the bottom of described reaction tube 1 is provided with gas access 12, liquid phase entrance 11 and discharge port 15.
In the slurry reactor device that the utility model provides, described reaction tube 1 is 1:1.1～10 with the internal diameter of separator 2 ratio.
In the slurry reactor device that the utility model provides, the height that described reaction tube 1 open top is stretched in separator 2 is 10%～90% of separator 2 total heights, preferably 50%～80%.
In the slurry reactor device that the utility model provides, heat exchanger 4 is preferably set in described reaction tube 1.Can be under liquid phase import or on arrange, also single or multiple lift heat exchanger can be set as required.
In the slurry reactor device that the utility model provides, on described reaction tube 1, be also provided with catalyst charging hole 16.Described catalyst charging hole 16 is arranged on the sidewall of reaction tube, can be one or more being symmetrically distributed on sidewall circumference.
In the slurry reactor device that the utility model provides, described reaction tube bottom is provided with gas access 12, liquid phase entrance 11 and discharge port 15.Wherein, described liquid phase entrance 11He gas access is preferably placed at reaction tube lower sides, can be one or more being symmetrically distributed on sidewall circumference, liquid phase entrance 11 can be positioned at gas access 12 above or below.Described discharge port 15 is preferably placed at bottom or the bottom surface of reaction tube.
In the slurry reactor device that the utility model provides, described liquid-phase outlet 14 is preferably placed at the bottom of separator 2, is more preferably positioned at the bottommost of separator 2.
In the slurry reactor device that the utility model provides, preferably at the interior heat exchanger 4 that arranges of described separator 2.
In the slurry reactor device that the utility model provides, before described gas vent 13, be provided with washing section 5.Washing section 5 can be arranged on inside or the outside of described separator, with entrained solid catalyst granules in peace and quiet liquid removal gas.Described peace and quiet liquid refers to that reaction raw materials or product or other do not contain the liquid phase medium of solid particle.
In the slurry reactor device that the utility model provides, described separator 2 is provided with fluid level controller 20, by regulating the amount of leaching of purified liquor outlet 19, controls the interior liquid level equilibrium of separator 2.
In the slurry reactor device that the utility model provides, described filter preferably adopts multichannel to form, and every pipe filter is provided with independently pressure differential detection and automatic transfer valve, utilizes filter pressure reduction to realize the on-line automatic backwash in turn between multichannel filter.Multichannel filter is set and makes easy to operately, installation and repairing is easy, makes the operation steady in a long-term of slurry reactor device.Filter medium in filter can be to be made as the stainless steel of sintering or other as pottery, porous metals by any known filtering material.Filter medium aperture should meet and not allow catalyst granules to pass through, and comprises after abrasion of particles.Therefore, its size depends on average particle size and size distribution.Filter medium pore diameter range is 0.1～100 micron, preferably 0.1～50 micron, and more preferably 0.1～20 micron.Filter backwash liquid used can be liquid or gas, preferred liquid.Liquid can be reaction clear liquid after fresh feed liquid or filter, preferably reaction clear liquid after filter.
In the slurry reactor device that the utility model provides, described place, gas access preferably arranges gas distributor, and described liquid phase porch preferably arranges liquid distribution trough, is uniformly distributed and enters paste state bed reactor gas and liquid charging stock.
The application process of the above-mentioned slurry reactor device that the utility model provides, raw material enters slurry reactor device by liquid phase material entrance 11He gas access 12, and the mixing of the slurries in reaction tube 1, contacts and react with catalyst, upwards flows simultaneously; Under gas push, reacting slurry flows into separator 2 from reaction tube 1 open top, carries out after gas-liquid separation, and liquid phase enters filter 3 from liquid-phase outlet 14, and gas is from gas vent 13 dischargers at separator 2 tops; After liquid phase is filtered in filter 3, clear liquid is drawn reaction unit as product by purified liquor outlet 19; The reacting slurry being flowed out by slurries outlet 22 returns in reaction tube 1 and continues to participate in reacting.
The paste state bed reactor that the utility model provides, in application process, preferably arranges heat exchanger 4 in described reaction tube 1, takes out the waste heat in course of reaction as required by heat-obtaining media for heat exchange.
The paste state bed reactor that the utility model provides is in application process, and the superficial gas velocity of gas in reaction tube 1 is 0.01～1.0m/s, preferred 0.1～0.3m/s.
The paste state bed reactor that the utility model provides is in application process, and the solid catalyst particle diameter adopting in described reaction tube is 0.1～5000 micron, preferably 0.1～100 micron.
The slurry reactor device that the utility model provides arranged gas scrubbing section in preferred embodiment before gaseous phase outlet, can effectively prevent that solid catalyst particle from being taken out of by outer row's gas.Heat taking and exchanging device is preferably set in reaction tube, according to the size of reaction heat, can be used for taking out reaction heat, control reaction temperature, to guarantee reaction efficiency.Preferred embodiment middle liquid-phase outlet is positioned at separator bottommost, makes the whole inflow filters of slurries containing solid catalyst particle, at inside reactor, sedimentation does not occur, and avoids local catalyst granules excessive concentration to cause over-reactive situation.
Slurry reactor device and application process thereof that the utility model provides are described with reference to the accompanying drawings, but therefore the utility model is not subject to any restriction.
As shown in Figure 1, the slurry reactor device that the utility model provides, comprises separator 2 and the filter 3 on reaction tube 1, reaction tube 1 top, described reaction tube 1 with the internal diameter of separator 2 than being 1:1.1～10.Separator 2 inside are stretched in the open top of described reaction tube 1, and the height that separator 2 is stretched in reaction tube 1 open top accounts for 1/10～9/10 of separator 2 total heights.The outer wall of reaction tube 1 is connected with separator 2 bottoms, and described separator 2 is communicated with filter 3 through liquid-phase outlet 14, and described filter 3 is communicated with the bottom of reaction tube 1 through slurries outlet 22; Described separator 2 tops are provided with gas vent 13, and the bottom of described reaction tube 1 is provided with gas access 12, liquid phase material entrance 11 and discharge port 15.Reaction tube bottom arranges heat exchanger 4.
The method of the slurry reactor device that application the utility model provides, liquid charging stock enters in reaction tube 1 through gas access 12 and by gas distributor by liquid inlet 11, gas raw material, wherein liquid charging stock can be as required the liquid inlet on 12 tops enters 12 bottom, ，Ye Kecong gas access from gas access liquid inlet enter reaction tube 1.In the interior gas-liquid of reaction tube 1, contact with solid catalyst particle and react, reactant flows to upper flowing, through reaction tube, 1 open top enters in separator 2, in separator 2, logistics flow velocity reduces, gas-liquid is fully separated, through washing section, 5 washings remove after the solid catalyst particle carrying gas, from the gaseous phase outlet 13 at separator 2 tops, discharge, slurries containing solid catalyst particle export 14 by slurries, through pipeline 7, by potential difference, certainly flow in filter 3, reaction clear liquid through filter element filtering is discharged from purified liquor outlet 19, the slurries that are rich in solid catalyst particle rely on potential difference by bottom, to flow back to reaction tube 1 through pipeline 8 and recycle, by regulating the load of cleaner liquid, controlled the liquid level of separator 2, when filter pressure at both sides is excessive, can inject backwash liquid from backwash liquid inlet 17 filter 3 is carried out to online backwashing, backwash liquid can be used raw material liq, also can use the clear liquid after filter.
Further illustrate by the following examples the utility model, but therefore the utility model is not subject to any restriction.
Experimental provision as shown in Figure 2.Wherein, reaction tube is of a size of Φ 150 * 15000mm, and separator is of a size of Φ 400 * 1600mm, and the height that reaction tube stretches into separator is 1000mm.Separator top is provided with washing section Φ 150 * 500mm, and the BX500 filler of in-built high 300mm, is used two set filters, and in-built metal filtering core is set when each filter pressure reduction reaches 0.06MPa and carried out automatic backflushing, and backwash liquid is reaction clear liquid after filtering.
The preparation method of the catalyst that reaction adopts: will contain Co (NO
3)
3and Mg (NO
3)
2solution impregnation SiO
2microsphere supported, standing 24 hours, then 120 ℃ were dried, and within 6 hours, obtain in 400 ℃ of roastings the catalyst that particle size range is 1～100 μ m.Wherein, consisting of of catalyst, take total catalyst weight as benchmark, in oxide, and the CoO that contains 20.3 % by weight
3, the SiO of 76.1 % by weight
2mgO with 3.6 % by weight.
Raw material of synthetic gas (containing hydrogen and carbon monoxide) 12 enters reaction tube bottom from gas access, by bottom heat exchanger 4, regulates reaction temperatures.Reaction temperature is 220 ℃, and operating pressure is 3.0MPa.There is F-T synthetic reaction in raw material, generate a series of hydrocarbon compound under catalyst exists.Product is carried out gas-liquid separation in separator.Gas superficial velocity in reaction tube is 0.3m/s.Gas after washing section hydrocarbon product washing is after filtering by gas vent 13 dischargers, and the compressed gas access 12 that loops back.Hydrocarbon liquids containing catalyst granules enters filter, and catalyst is separated with product.After filtering, the slurries that are rich in catalyst granules are returned in reaction tube by bottom, and the reaction clear liquid after filtration is discharged and entered follow-up fractionating system through purified liquor outlet 19 under separator liquid level is controlled.In operation, according to reactivity, each intermittently take out proper catalyst, and the fresh catalyst of supplementary equivalent, maintain the reaction condition of stable operation after 700 hours and the results are shown in Table 1.
Adopt as shown in Figure 2 the experimental provision identical with embodiment 1, hydrogen and working solution enter reactor from liquid phase entrance 12He gas access 11 respectively, by bottom heat exchanger 4, regulate reaction temperature.Reaction temperature is 60 ℃, and used catalyst is the fine powder catalyst containing palladium, and its average diameter is 80 microns.Under catalyst action, the EAQ in working solution is generated the hydride containing ethyl anthracene quinhydrones by hydrogenation.Gas superficial velocity in reaction tube is 0.15m/s.Product is carried out gas-liquid separation in separator, gas hydride washing is after filtering by gas vent 13 dischargers, and the compressed hydrogen inlet that loops back, the hydride that contains catalyst enters filter, filter core in filter is separated with hydride by catalyst granules, the slurries that are rich in catalyst granules return to the bottom of reaction tube 1, and the hydride after filtration through purified liquor outlet 19 dischargers, enters follow-up oxidation-extraction system under separator liquid level is controlled.The reaction condition of stable operation after 1500 hours and the results are shown in Table 2.
The method for preparing catalyst that adopts is: boehmite, Ludox and deionized water are mixed to get to slurries.Wherein, sial mass ratio is SiO
2: Al
2o
3=1:4.By mixed serum spray drying device drying and moulding, after 600 ℃ of roasting 8h, make catalyst carrier.Catalyst carrier is distributed in the deionized water solution that contains palladium bichloride, at 25 ℃, fully floods, then under 120 ℃ of conditions, be dried 2h, then at 600 ℃ of roasting 5h, obtain oxidized catalyst.Under 150 ℃ of conditions with pure hydrogen by this oxidized catalyst reduction 4h, make required catalyst.Take total catalyst weight as benchmark, in metal, the Pd that this catalyst contains 1.2 % by weight.
Described working solution is the mixture of EAQ, tetrahydrochysene EAQ, trioctyl phosphate and heavy aromatics.The concentration of general anthraquinone is 130～140g/l, and the volume ratio of heavy aromatics and trioctyl phosphate is 75:25.Wherein, general anthraquinone refers to the summation of EAQ and tetrahydrochysene EAQ.
Described hydride is the mixture of EAQ, tetrahydrochysene EAQ, ethyl anthracene quinhydrones, tetrahydrochysene ethyl anthracene quinhydrones, trioctyl phosphate and heavy aromatics.The concentration of general anthraquinone is 130～140g/l, and the volume ratio of heavy aromatics and trioctyl phosphate is 75:25.Wherein, general anthraquinone refers to the summation of EAQ, tetrahydrochysene EAQ, ethyl anthracene quinhydrones and tetrahydrochysene ethyl anthracene quinhydrones, and ethyl anthracene quinhydrones and tetrahydrochysene ethyl anthracene quinhydrones account for 45 % by weight of general anthraquinone.
Experimental provision is identical with embodiment 1, and difference is the in-built ceramic membrane filter core of filter.The hydrogen peroxide of 27.5% concentration enters reactor from the liquid inlet 11 on top, and ammonia 12 enters reactor from gas access, and cyclohexanone and t-butanol solution enter reactor from the liquid inlet 11 of bottommost.Operating condition is: reaction temperature is that 83 ℃, reaction pressure are 0.32MPa.Former powder titanium-silicon molecular sieve TS-1 ，You builds in Hunan feldspathization joint-stock company and produces, and catalyst average grain diameter is 0.2 micron.Ammonia superficial velocity in reaction tube is 0.2m/s.Raw material issues ammonifying oximation reaction in the effect of catalyst, generates the t-butanol solution containing cyclohexanone oxime, separated through filter, and reaction clear liquid is delivered to aftercut system and processed.In operation, for keeping the activity stabilized of catalyst, from catalyst feeds 16, fill into continuously a certain amount of fresh catalyst, from discharge port 15, take out continuously the decaying catalyst of equivalent simultaneously, move the process conditions of 1000 hours and the results are shown in Table 3.
F-T synthetic reaction condition and result in table 1 embodiment 1
| Reaction temperature, ℃ | 220 |
| Reaction pressure, MPa | 3.0 |
| Fresh synthesis gas, H 2/CO | 2:1 |
| Fresh synthesis gas inlet amount, Nm 3/h | 178 |
| Gas superficial gas speed, m/s | 0.3 |
| CO conversion ratio, % | 94.5 |
| C1-C4 is selective, % | 14.1 |
| C5+ is selective, % | 85.9 |
Table 2 embodiment 2 synthesize hydrogen peroxide reaction condition and results
| Reaction temperature, ℃ | 60 |
| Reaction pressure, MPa | 0.3 |
| Working solution inlet amount, m 3/h | 1.2 |
| H2 inlet amount, Nm 3/h | 40 |
| Gas superficial gas speed, m/s | 0.15 |
| Hydrogen effect, gH
2O
2/ |
12 |
Table 3 embodiment 3 synthesizing cyclohexane 1 ketoxime reaction condition and results
| Reaction temperature, ℃ | 83-84 |
| Reaction pressure, MPa | 0.32 |
| Fed cyclohexanone amount, kg/h | 40 |
| Ammonia/ketone, mol ratio | 2.1 |
| The tert-butyl alcohol/ketone, mol ratio | 3.0 |
| H 2O 2/ ketone, mol ratio | 1.10 |
| Gas superficial gas speed, m/s | 0.2 |
| Cyclohexanone conversion ratio, % | 99.95 |
| Cyclohexanone oxime is selective, % | 99.8 |
Claims (10)
1. a slurry reactor device, it is characterized in that, comprise reaction tube (1), separator (2) and filter (3), separator (2) inside is stretched in the open top of described reaction tube (1), the outer wall of reaction tube (1) is connected with separator (2) bottom, described separator (2) is communicated with filter (3) through liquid-phase outlet (14), and described filter (3) is communicated with the bottom of reaction tube (1) through slurries outlets (22); Described separator (2) top is provided with gas vent (13), and the bottom of described reaction tube (1) is provided with gas access (12), liquid phase entrance (11) and discharge port (15).
2. according to the slurry reactor device of claim 1, it is characterized in that, described reaction tube (1) is 1:1.1～10 with the internal diameter ratio of separator (2).
3. according to the slurry reactor device of claim 1, it is characterized in that, the height that separator (2) is stretched in described reaction tube (1) open top is 10%～90% of separator (2) total height.
4. according to the slurry reactor device of claim 3, it is characterized in that, the height that separator (2) is stretched in described reaction tube (1) open top is 50%～80% of separator (2) total height.
5. according to the slurry reactor device of claim 1, it is characterized in that, heat exchanger (4) is set in described reaction tube (1).
6. according to any slurry reactor device in claim 1-5, it is characterized in that, on described reaction tube (1), be also provided with catalyst charging hole (16).
7. according to any slurry reactor device in claim 1-5, it is characterized in that, described liquid-phase outlet (14) is positioned at the bottom of separator (2).
8. according to any slurry reactor device in claim 1-5, it is characterized in that, heat exchanger (4) is set in described separator (2).
9. according to any slurry reactor device in claim 1-5, it is characterized in that, described gas vent (13) is provided with washing section (5) before.
10. according to any slurry reactor device in claim 1-5, it is characterized in that, described separator (2) is provided with fluid level controller (20), by regulating the amount of leaching of purified liquor outlet (19), controls the interior liquid level equilibrium of separator (2).
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|---|---|---|---|
| CN201320492007.0U CN203389625U (en) | 2013-08-13 | 2013-08-13 | Slurry bed reaction device |
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|---|---|---|---|
| CN201320492007.0U CN203389625U (en) | 2013-08-13 | 2013-08-13 | Slurry bed reaction device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104368283A (en) * | 2013-08-13 | 2015-02-25 | 中国石油化工股份有限公司 | Slurry bed reactor and applications thereof |
| CN116617911A (en) * | 2023-07-19 | 2023-08-22 | 山东广浦生物科技有限公司 | Method and device for synthesizing transesterification catalyst |
-
2013
- 2013-08-13 CN CN201320492007.0U patent/CN203389625U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104368283A (en) * | 2013-08-13 | 2015-02-25 | 中国石油化工股份有限公司 | Slurry bed reactor and applications thereof |
| CN116617911A (en) * | 2023-07-19 | 2023-08-22 | 山东广浦生物科技有限公司 | Method and device for synthesizing transesterification catalyst |
| CN116617911B (en) * | 2023-07-19 | 2023-09-12 | 山东广浦生物科技有限公司 | Method and device for synthesizing transesterification catalyst |
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