CN201907973U - Reactor for oxygen thermal production of calcium carbide and synthesis gas - Google Patents
Reactor for oxygen thermal production of calcium carbide and synthesis gas Download PDFInfo
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- CN201907973U CN201907973U CN2010206515687U CN201020651568U CN201907973U CN 201907973 U CN201907973 U CN 201907973U CN 2010206515687 U CN2010206515687 U CN 2010206515687U CN 201020651568 U CN201020651568 U CN 201020651568U CN 201907973 U CN201907973 U CN 201907973U
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Abstract
The utility model discloses a reactor for the oxygen thermal production of calcium carbide and synthesis gas, which solves the problems in calcium carbide preparation of the conventional reactor such as large consumption of raw materials and fuel, plenty of equipment, high investment, complicated process, as well as difficult industrialized use of byproduct CO (carbon oxide) due to the small amount. The reactor comprises a gas-solid separator, wherein a closed type reaction furnace is arranged below the gas-solid separator and comprises an upper preheating chamber, a middle gasification chamber and a lower reaction chamber. Through the reactor, a large amount of CO gas can be produced during the calcium carbide synthesis, so as to be used as an industrial feed gas; all the reactions and heat exchanges are completed in the reactor, so that a preheater or other pretreatment devices are no more needed; and the reactor has the advantages of simple equipment, compact structure, small investment and convenience in mounting and maintenance.
Description
Technical field
The utility model relates to a kind of equipment for preparing calcium carbide and synthetic gas, and the hot method of oxygen is produced the reactor of calcium carbide and synthetic gas specifically.
Background technology
Calcium carbide is basic Organic Chemicals, and the acetylene gas that is made by it can replace petroleum product to produce thousands of kinds of organic productss such as acetic acid, polyvinyl chloride, vinyl acetate between to for plastic, polyvinyl alcohol, ethynyl ether, Shawinigan black.Therefore it has wide purposes, can predict, and market will rise steadily to the demand of calcium carbide.
Two kinds of the hot method of production method aerobic of calcium carbide and electric heating process, at present industrial general employing electric heating process is produced calcium carbide, be that coke (C) and calcium oxide (CaO) are in furnace of calcium carbide, adopt fixed bed to rely on high arc temperature (＞2000 ℃) fusing reaction and generation calcium carbide, the characteristics that electric heating process prepares calcium carbide are to adopt block raw material charging and utilize the electrical energy production calcium carbide, it exists that speed of reaction is slow, long reaction time, temperature of reaction height, current consumption is big, and calcium carbide yields poorly, the problem of dust and treating tail gas difficulty.Have the shortcoming of " high investment, high pollution, high energy consumption " just because of traditional calcium carbide production technology, do not meet the requirement of energy-saving and emission-reduction and Sustainable development, so National Development and Reform Committee repeatedly sends the documents and limits its development.
The hot method of oxygen is that part carbon is burnt, the heat of high temperature that produces makes residue carbon and the calcium generation calcium carbide that reacts, this method since have the reaction times short, temperature of reaction is low, pollute little advantage is much accounted of gradually, a kind of calcium carbide production method is disclosed as number of patent application 200810117540.2, powdered carbon raw material and calcic raw material mixing rear section burning direct heating mixture are produced calcium carbide, and the CO that utilizes calcium carbide to produce carries out preheating to raw material.Its principal feature is 1) utilize the heat of high temperature of oxygen and carbon burning generation to replace conventional arc high temperature to make C and CaO reaction generate calcium carbide, its temperature of reaction requires lower (getting final product more than 1700 ℃), and heat cost is also low than electric heating; 2) adopt powder raw material to substitute block raw material, reach and improve energy utilization rate, quickening speed of reaction, the temperature of reaction that reduces, improve the purpose of throughput, 3) raw material is carried out preheating, the CO and the auxiliary fuel combustion heat supplying of pre-thermal recovery calcium carbide by-product, to reduce the consumption of carbon content in the subsequent reactions, improve calcium carbide purity.This inventive method is further specializing this technical scheme on hot oxygen law theory basis.And for example 200810239805.6 disclose a kind of system for producing calcium carbide, comprised preheating unit and reaction member, preheating unit comprises hybrid feed mechanism, primary heater unit, gas compressing apparatus and interchanger; Reaction member comprises feeding unit, reactor and interchanger.For meeting the requirements of high temperature more than 1700 ℃, the oxygen of consumption, carbon amount are still more in reactor; Setting by each device of this production system it seems, utilizes the hot method of oxygen to produce that its equipment that relates to of calcium carbide is many, investment is big, technology is comparatively complicated, CO by-product measures less.Because the CO of by-product amount is few, therefore is not suitable for and uses as the chemical plant installations unstripped gas; As and if the technology thinking of CO feedback and oxygen combustion preheating material has reached the purpose of product recycle apparently, the actual problem that has increased processing step, improved running cost that but exists.
Summary of the invention
The utility model purpose is in order to solve the problems of the technologies described above, provide the hot method of a kind of oxygen to produce the reactor of calcium carbide and synthetic gas, this reactor can carry out preheating of fuel, calcium carbide reaction and gas solid separation simultaneously, floor space is little, relate to equipment few, invest with move into low, produce calcium carbide and synthesis gas reaction efficient height, calcium carbide purity height, the amount of the synthetic gas of generation is existing more than seven times of electrode preparation calcium carbide route, and the rate of consumption of raw material and fuel (oxygen) is low simultaneously.
Technical solutions of the utility model comprise gas-solid separator, the gas-solid separator below is provided with closed Reaktionsofen, described closed Reaktionsofen is made of the preheating chamber on top, the vaporizer at middle part, the reaction chamber of bottom, described preheating chamber top be provided with first opening for feed and arrange symmetrically and evenly through at least two air outlets that pipeline is connected with the gas-solid separator inlet mouth; The preheating chamber sidewall evenly is provided with a plurality of second opening for feeds, and is symmetrical arranged at least two ashes and returns import, and described ash returns import and is connected with the ash output hole of gas-solid separator through pipeline; Also be provided with the coal burner in the described vaporizer, igniter burner goes into operation; Described reaction chamber is provided with the oxygen burning and chews, and the bottom also is provided with discharge port.
Described preheating chamber is by top ball arcuate segment, and middle part straight section and bottom reducer constitute.
The reducing angle of described bottom reducer is 5-30 °.
The downward expansion angle of first opening for feed at described preheating chamber top is 5-8 °.
The downward inclination angle of second opening for feed of described preheating chamber sidewall is 10-30 °, and tangential angle is 3-10 °.
It is 3-8 ° that the oxygen burning of described reaction chamber is chewed tangential angle, and the inclination angle is 10-30 ° downwards.
The method of the hot method vaporizing system of the utility model oxygen power backup stone and synthetic gas will be sent into the preheating chamber preheating by opening for feed through coal-grinding and exsiccant carbon raw material and calcic raw material, simultaneously carbon in the part carbon raw material and the interior CO of preheating chamber
2Thermo-negative reaction takes place generate CO, CO enters and discharges after gas-solid separator is isolated the ashes of carbon containing and calcium oxide, isolated ashes is sent preheating chamber back to, descend together with remaining carbon raw material, calcic raw material and after the further preheating of vaporizer, to enter reaction chamber bottom, the heat of high temperature of carbon and pure oxygen burning makes carbon and the reaction of the calcium oxide in the calcic raw material in the residue carbon raw material generate calcium carbide and CO in reaction chamber, calcium carbide is through discharge hole for discharge, CO rises to preheating chamber to the raw material contact heat-exchanging, discharges after gas-solid separator is isolated the ashes of carbon containing and calcium oxide then.In described carbon raw material and the calcic raw material
C: CaWeight ratio be
2.2～3: 1, described calcic raw material and carbon raw material divide two portions to enter preheating chamber, gross weight 12
～14 enter from top jet, remaining part is circle of contact eddy flow from the preheating chamber sidewall and enters downwards.
Described calcic raw material is a lime carbonate, and lime carbonate is decomposed into calcium oxide and CO under the high temperature after entering preheating chamber
2, calcium oxide and carbon raw material descend together and enter the reaction chamber bottom through vaporizer.
Forced feed is adopted in described charging, and pressure-controlling is at 0.5～4.0MPa.
The high temperature of described reaction chamber is burnt by the oxygen that is positioned at reaction chamber to be chewed the pure oxygen that sprays into and keeps with the part carbon raw material burning of reaction chamber, or is burnt by oxygen and to chew the coal dust and the pure oxygen mixture burns that spray into simultaneously and keep burning generation CO
2Enter preheating chamber.
Burn tangential angle 3-8 ° and inclination angle 10-30 ° that chews downwards by control oxygen, control jet velocity 200～300m/s makes the air-flow of ejection form downtilt angles to impact the indoor calcium carbide pond of stirring reaction, quickens the calcium carbide reaction.
The high temperature of described vaporizer is chewed the coal dust and the oxygen-containing gas mixture burns that spray into simultaneously by the coal burning and is kept, and burning generates CO
2Enter preheating chamber; Heat that the CO that the high temperature of described preheating chamber is generated by the calcium carbide reaction is entrained and the hyperthermia radiation in vaporizer and the reaction chamber are kept.
Preheating zone, gasification zone and the reaction zone of the utility model reactor by in closed Reaktionsofen, dividing, and the gas-solid separator that is connected with closed Reaktionsofen is incorporated into preheating of fuel, calcium carbide production and gas-solid separating step in the equipment and carries out, and designs very ingenious.
Find in the experiment, single from the preheating chamber its top feed, reduce the preheating chamber room temperature though can generate CO, but because pulverized coal particle thin (most of pulverized coal particle is less than 20 μ m), particulate matter is turned round and round at the top under the effect of upstream, may exist raw material to be difficult to enter the problem that reaction chamber participates in reaction; Therefore be that 10-30 ° and tangential angle are 3-10 ° and make raw material be circle of contact eddy flow along sidewall to enter reaction chamber downwards by designing the downward inclination angle of second opening for feed, the downward mode of circle of contact eddy flow can increase the residence time of raw material in preheating chamber, makes it obtain abundant preheating.On the other hand, consider in the CO gas that rises the reaction back and contain slag, easily in the wall slagging scorification, because temperature is low, slag mobile bad, the wall caking causes coming off or the barrier gas passage of bulk slag above vaporizer easily, gas velocity is increased, the wearing and tearing wall, therefore the carrier gas temperature of controlling second throat-fed of preheating chamber sidewall is 200-220 ℃, the temperature of slag is being dropped rapidly to above the vaporizer below 900 ℃, forms solid particulate and continue to rise to gas-solid separator with CO.
The setting of dome head bottom straight section and reducer is in order to guarantee CO
2Fully contact at contraction mouth with raw material, make CO
2Fully react generation CO with C, take raw material out of reaction chamber in a large number for fear of air-flow simultaneously, the angle of reducer preferably is controlled at 5-30 °.
The downward flare angle of respective outer side edges opening for feed that reducer forms convergent fully is preheated to more than 500 ℃ material in preheating chamber.Special design increases vaporizer, utilizes the coal of vaporizer to burn to chew the oxygen-containing gas that sprays into and the mixture burns of coal can make the high temperature of vaporizer generation more than 1000 ℃.
The oxygen of reaction chamber burn chew can be provided with in the same way a plurality of, by control to its tangential angle and downward inclination angle, can make the gas of chewing ejection at a high speed by burning to generation stirring action in calcium carbide pond in the reaction chamber, make the calcium carbide reaction more abundant, reduce the reaction times, improve reaction efficiency and calcium carbide purity.
Described gas solid reactor preferably adopts cyclonic separator.Can carry out suitable high temperature resistant, erosion resistant according to the requirement of operating mode in the calcium carbide reactor handles.
Hot oxygen is reflected in the above-mentioned reactor and carries out, and raw material adopts the mixture of carbon raw material and calcic raw material, and described carbon raw material can be coal dust or blue carbon, and described calcic raw material can be calcium oxide or lime carbonate.When the calcic raw material adopts lime carbonate, can in preheating chamber, resolve into calcium oxide and CO under the high temperature
2, calcium oxide can be used as the raw material of calcium carbide reaction, CO
2Then can generate CO, improve the output of synthetic gas with coal dust generation thermo-negative reaction.In the utility model, carbon raw material is consumed at three places: 1) in preheating chamber and CO
2Reaction generates CO and is partially consumed; Be partially consumed when 2) in vaporizer, supplying with the vaporizer heat with oxygen-containing gas burning; 3) at high temperature carrying out the calcium carbide reaction with calcium oxide in reaction chamber is partially consumed; 4) in reaction chamber, be partially consumed with pure oxygen burning supply response chamber heat.Therefore the amount of carbon raw material and calcic raw material should take into full account above-mentioned reason, and the content of carbon is excessive in a large number, and the weight ratio that is C: Ca is 2.2～3: 1.
CO in the reactor
2Be generated at three places: 1) lime carbonate (when being lime carbonate as if the calcic raw material) decomposition at high temperature obtains CO in preheating chamber
22) pure oxygen and carbon burning generate CO in the reaction chamber
23) burning of oxygen-containing gas and carbon raw material generates CO in the vaporizer
2The contriver makes full use of the CO of a large amount of generations
2, it contacting with coal dust in preheating chamber generate CO, calcium carbide reaction itself also can generate CO in addition, and the CO gas volumes that two kinds of reactions generate can reach existing more than 7 times of technology, and energy utilization rate height, the unstripped gas that is particularly suitable as chemical industry use.Because the CO gas that generates in the Reaktionsofen all contains ashes (being dust-laden CO gas), therefore must after pipeline gathers, send into and just can discharge after the dedusting in the gas-solid separator for follow-up use, ashes after the separation can return in the Reaktionsofen and be recycled, and all reaction product of whole technology all can rationally be utilized or recycling.
In vaporizer, chew the oxygen-containing gas of ejection and the mixture burns generation CO of carbon raw material by the coal burning
2, and make vaporizer form high temperature more than 1000 ℃, because vaporizer is between preheating chamber and reaction chamber, this high-temperature area becomes an insulation belt, has four effects: produce stove heat together with reaction chamber and high-temperature gas provides heat for preheating chamber 1.; 2. increase the residence time before material enters reaction chamber, material is heated in vaporizer more than 1000 ℃; 3. this insulation belt can be kept apart preheating chamber and reaction chamber, reduces the thermal exposure of reaction chamber to preheating chamber, avoids carbon and the too much problem of oxygen depletion for keeping reaction chamber high temperature to cause, helps the formation of reaction chamber high-temperature zone and stable.4. the part slag of gasification reaction formation flows into reaction chamber at this downwards along wall, and further heating up in reaction chamber generates calcium carbide.
It is 3-8 ° that control oxygen burning is chewed tangential angle, the inclination angle is 10-30 ° downwards, jet velocity is more than 200m/s, when guaranteeing reaction the calcium carbide pond there is certain stirring, and provide a large amount of heats to keep reaction chamber temperature more than 1700 ℃ with carbon burning, make carbon and the reaction of the calcium oxide in the calcic raw material in the carbon raw material generate calcium carbide.Described oxygen-containing gas can be pure oxygen, oxygen level oxygen enrichment or the normal air greater than volume percent 30%.
The utility model reactor gathers multi-function in integral whole, and the high-temperature gas that rises in prepared using reaction chamber, vaporizer incendiary hyperthermia radiation and calcium carbide reaction back (comprises that CO and burning that the calcium carbide reaction generates produce CO
2) contact heat-exchanging in preheating chamber by fully preheating, need not other consume fuel, need not independent preliminary heating device, simultaneously coal dust and CO in the preheating chamber
2Thermo-negative reaction, and carry out contact heat-exchanging between high-temperature gas that rises and the raw material, raw material is preheated, dust-laden CO gas is lowered the temperature when entering gas-solid separator simultaneously, so also need not to be provided with in addition devices such as interchanger, all reactions and heat exchange are all carried out in reactor, need not to dispose in addition preheater or other pretreatment unit, and equipment is simple, compact construction, investment are little, be convenient to installation and maintenance.
The calcium carbide reaction generates the calcium carbide discharging, and by product is CO, carbon raw material and CO in the CO of this part by-product and the preheating chamber
2The CO that thermo-negative reaction produces is (the CO that generates in the stove together
2Can all generate CO) with the carbon reaction, send into through pipeline that (CO of all generations all contains ashes in the Reaktionsofen after the dedusting in the gas-solid separator, therefore be dust-laden CO gas, must dedusting) discharge for follow-up use, and isolated ashes returns in the Reaktionsofen and is recycled.Whole technology is in the enclosed reaction vessel, and all reaction product all are used appropriately, and does not efflux substantially, do not pollute environment is any, and its speed of reaction height, time weak point, the every index of the calcium carbide of generation meets the demands, and the manufacture gas scale of construction is very big and purity is high.
Description of drawings
Fig. 1 is the utility model structural representation.
Fig. 2 is the A-A synoptic diagram of Fig. 1.
Fig. 3 is the B-B synoptic diagram of Fig. 1.
Fig. 4 is the local structure synoptic diagram of second opening for feed.
Wherein, 1-cyclonic separator, the closed Reaktionsofen of 2-, 3-preheating chamber, 3.1-ball arcuate segment, 3.2-straight section, 3.3-reducer, 4-vaporizer, 5-reaction chamber, 6-first opening for feed, 7-air outlet, 8-inlet mouth, 9-ash return import, 10-pipeline, 11-ash output hole, 12-pipeline, 13-go into operation order that baked wheaten cake is chewed, 14-oxygen burn chew, 15-discharge port, 16-coal burn chew, 17-venting port, 18-second opening for feed.
Embodiment
Below in conjunction with accompanying drawing the utility model reactor is further explained explanation:
Reactor comprises the closed Reaktionsofen 2 that is positioned at cyclonic separator 1 below, described closed Reaktionsofen 2 is made of the preheating chamber 3 on top, the vaporizer 4 at middle part and the reaction chamber 5 of bottom, described preheating chamber 3 is by top ball arcuate segment 3.1, middle part straight section 3.2 and bottom reducer 3.3 constitute, the reducing angle of reducer is 5-30 °, preheating chamber 3 tops are provided with first opening for feed 6, the downward expansion angle of described opening for feed 6 is 5-8 °, preheating chamber 3 sidewalls evenly are provided with a plurality of second opening for feeds 18, its tangential angle is 3-10 °, and downward inclination angle is 10-30 °.Described preheating chamber 3 tops also symmetric offset spread have respectively through two air outlets 7 that pipeline 12 is connected with two inlet mouths 8 of cyclonic separator 1, and described inlet mouth 8 is the tangential admission mouth, can make dust-laden CO gas tangentially enter cyclonic separator 1, improve separation efficiency.Described preheating chamber 3 bottoms are provided with two ashes symmetrically and evenly and return import 9, described ash returns import 9 and is connected with the ash output hole 11 of cyclonic separator 1 through pipeline 10, can make ashes by carbon containing of separating among the CO and calcium oxide return import 9 by ash and return recycle in the closed Reaktionsofen 2, described whirlwind divides device 1 top to be provided with the venting port 17 that is used to discharge CO; Described vaporizer 4 establish go into operation order baked wheaten cake chew 13 and 4 coals arranging symmetrically and evenly burn and chew 16, described reaction chamber 5 is provided with 4 oxygen burnings of arranging symmetrically and evenly and chews 14, its tangential angle is 3-8 °, the inclination angle is 10-30 ° downwards, when pure oxygen is sprayed into, because the control of its high spraying speed degree and angle can produce stirring action to the calcium carbide reaction tank in the reaction chamber 5.Reaction chamber 5 bottoms also are provided with discharge port 15.Because the calcium carbide reactor is a high-temperature reactor, therefore its inner each several part should perform high temperature resistant and the every processing of abrasive according to corresponding working temperature, form by carbon steel sheet and fire-resistant high chromium mould material as closed Reaktionsofen 2 tops, material, the self-baking brick of making charcoal can be smash by the cryosphere charcoal in the bottom, light carbon brick, alumina firebrick, Lowweight Refractory Castable are formed, sidewall adopts the cryosphere charcoal to smash material, the self-baking brick of making charcoal, light carbon brick and spiral membrane wall are formed, cyclonic separator 1 central tube adopts round tube type heat-resistant antifriction steel plate to make internal surface spraying abrasion-proof mould material.The utility model is not limited to above-mentioned high temperature resistant and abrasive treatment process, and other processing of satisfying the utility model worst hot case all can be adopted.
Processing method:
The raw material weight ratio: coal dust: lime carbonate is 2.2: 1, and particle diameter is 0.15mm.
With above-mentioned raw materials weight 1/3rd drop in the closed Reaktionsofen 2 by first opening for feed 6 by the screw press feeding machine, two of its excess-three branch is dropped in the closed Reaktionsofen 2 by second opening for feed 18 by the pressurization feeding machine, the control input speed is that 7m/s, pressure are 1.0MPa, and lime carbonate is decomposed into calcium oxide and CO under the high temperature (more than 600 ℃) in preheating chamber 3
2, simultaneously the part coal dust also with preheating chamber 3 in CO
2Thermo-negative reaction takes place generate CO, remainder coal dust and calcium oxide in preheating chamber 3 with high temperature CO and CO from vaporizer 4 and reaction chamber 5
2Carry out descending together behind the contact heat-exchanging and enter vaporizer 4 (be preheated by the heat exchange raw material, CO is lowered the temperature); The coal of vaporizer 4 burns to be chewed 16 coal dusts that spray into and oxygen-rich mixture (speed of spraying into is 85m/s, and oxygen coal weight ratio is 0.5: 1) burning and vaporizer 4 temperature is reached more than 1000 ℃ continue preheating material; Remainder coal dust and calcium oxide behind vaporizer 4 continue to drop to reaction chamber 5, the part of remainder coal dust is chewed 14 pure oxygens that spray into (speed of spraying into is 60m/s) burning and produces high temperature more than 1700 ℃ with being burnt by oxygen in reaction chamber 5, the pure oxygen that tangential tilt sprays into also can produce mixing effect to the calcium carbide reaction tank, the remainder coal dust of remaining part then at high temperature reacts with calcium oxide and generates calcium carbide and CO, calcium carbide is by discharge hole for discharge, and calcium carbide reacts the CO of generation and the CO of oxygen and coal dust firing generation
2Rise to preheating chamber 3 together, CO
2Generate CO with the part coal dust reaction in the raw material, all CO all the air outlet 7 by closed Reaktionsofen 2 in pipeline 12 enters cyclonic separator 1, make and contain the ashes separation in the CO gas, CO behind the separation ashes is discharged by venting port 17 and enters lower procedure, and isolated ashes mixes decline by the remainder coal dust and the calcium oxide of ash output hole 11 after pipeline 10, ash return import 9 to enter preheating chamber 3 and preheating of cyclonic separator 1 bottom.0.2444 ton of calcium carbide that per 1 ton of feed coal can generate, its purity is 60wt%, synthetic tolerance is 950 liters/kg.(M 5wt% is pressed in the technical analysis of coal, V 25wt%, and C 55wt%, A 15wt% calculates).
Claims (6)
1. the hot method of an oxygen is produced the reactor of calcium carbide and synthetic gas, comprise gas-solid separator, it is characterized in that, the below of gas-solid separator is provided with closed Reaktionsofen, described closed Reaktionsofen is made of the preheating chamber on top, the vaporizer at middle part, the reaction chamber of bottom, described preheating chamber top be provided with first opening for feed and symmetric offset spread through at least two air outlets that pipeline is connected with the gas-solid separator inlet mouth; The preheating chamber sidewall evenly is provided with a plurality of second opening for feeds, and is symmetrical arranged at least two ashes and returns import, and described ash returns import and is connected with the ash output hole of gas-solid separator through pipeline; Also be provided with the coal burner in the described vaporizer, igniter burner goes into operation; Described reaction chamber is provided with the oxygen burning and chews, and the bottom also is provided with discharge port.
2. reactor as claimed in claim 1 or 2 is characterized in that, described preheating chamber is by top ball arcuate segment, and middle part straight section and bottom reducer constitute.
3. reactor as claimed in claim 2 is characterized in that, the reducing angle of described bottom reducer is 5-30 °.
4. reactor as claimed in claim 1 or 2 is characterized in that, the downward expansion angle of first opening for feed at described preheating chamber top is 5-8 °.
5. reactor as claimed in claim 1 or 2 is characterized in that, the downward inclination angle of second opening for feed of described preheating chamber sidewall is 10-30 °, and tangential angle is 3-10 °.
6. reactor as claimed in claim 1 or 2 is characterized in that, it is 3-8 ° that the oxygen burning of described reaction chamber is chewed tangential angle, and the inclination angle is 10-30 ° downwards.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153085A (en) * | 2010-12-03 | 2011-08-17 | 中国五环工程有限公司 | Method for preparing calcium carbide and synthesis gas through thermal oxidation reaction and calcium carbide reactor |
| CN107606949A (en) * | 2017-09-27 | 2018-01-19 | 河南科达东大国际工程有限公司 | A kind of gas suspension calcination of aluminium hydroxide stove low-temperature bake device |
| CN118684229A (en) * | 2024-08-22 | 2024-09-24 | 中国科学技术大学 | Growth device and growth method for silicon carbide porous material without inert atmosphere protection |
-
2010
- 2010-12-03 CN CN2010206515687U patent/CN201907973U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102153085A (en) * | 2010-12-03 | 2011-08-17 | 中国五环工程有限公司 | Method for preparing calcium carbide and synthesis gas through thermal oxidation reaction and calcium carbide reactor |
| CN102153085B (en) * | 2010-12-03 | 2013-10-16 | 中国五环工程有限公司 | Method for preparing calcium carbide and synthesis gas through thermal oxidation reaction and calcium carbide reactor |
| CN107606949A (en) * | 2017-09-27 | 2018-01-19 | 河南科达东大国际工程有限公司 | A kind of gas suspension calcination of aluminium hydroxide stove low-temperature bake device |
| CN118684229A (en) * | 2024-08-22 | 2024-09-24 | 中国科学技术大学 | Growth device and growth method for silicon carbide porous material without inert atmosphere protection |
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Granted publication date: 20110727 |
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