CN101428799A - System for producing calcium carbide - Google Patents
System for producing calcium carbide Download PDFInfo
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- CN101428799A CN101428799A CNA2008102398056A CN200810239805A CN101428799A CN 101428799 A CN101428799 A CN 101428799A CN A2008102398056 A CNA2008102398056 A CN A2008102398056A CN 200810239805 A CN200810239805 A CN 200810239805A CN 101428799 A CN101428799 A CN 101428799A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
A calcium carbide production system belongs to the field of calcium carbide production. The calcium carbide production system includes a raw material preheating unit and a reaction unit; the raw material preheating unit includes a raw material mixing and feeding device, a preheating device, a gas compression device and a heat exchanger; the raw material mixing and feeding device includes a solid raw material mixer and a feeder; a raw material inlet, a gas inlet, a gas outlet and a solid material outlet are formed on the preheating device; the raw material mixing and feeding device is communicated with the preheating device; the reaction unit includes a feeding device, a reactor and a heat exchanger; a raw material nozzle, a gas outlet and a product outlet are arranged on the reactor; the solid material inlet of the feeding device is communicated with the preheating device; the solid material outlet of the feeding device is communicated with the raw material nozzle on the reactor; the reactor is communicated with the heat exchanger; and the heat exchanger is connected with the gas compression device of the preheating unit. The system realizes the coupling of the process of coal coking and lime calcining and the production of calcium carbide; the capacity usage ratio is high; the powdery material is adopted; the selection range of the raw material is wide; the production capacity is large; and the furnace type is simple.
Description
Technical field:
The present invention relates to a kind of system for producing calcium carbide, relate to a kind of system that produces calcium carbide by two-stage method by solid carbon raw material and calcic raw material specifically.
Background technology:
Carbide of calcium is commonly called as calcium carbide (CaC
2), the middle of last century is described as the mother of organic synthesis before.Be mainly used in series product such as producing chlorovinyl, vinyl acetate between to for plastic base and acrylic at present, come from carbide acetylene as PVC (polyvinyl chloride) production of China about 70%.In recent years, the surging calcium carbide industrial expansion that stimulated of oil price, China's calcium carbide output was by 4,250,000 tons of 1,177 ten thousand tons of being increased to 2006 in 2002.
Fixed bed-arc process is adopted in traditional calcium carbide production, and the high temperature that utilizes electric arc to produce is heated to block calcium oxide in the fixed bed (also claiming moving-bed or electric furnace) and block coke more than 2000 ℃, stops certain hour and generates the molten state calcium carbide.The mixture of calcium oxide and coke is added by the electric furnace upper end in the production process, and the CO that the two reaction generates discharges from upper of furnace body by the lumpy material slit, and fused product calcium carbide is discharged by furnace bottom, obtains finished product through cooling, fragmentation.
Arc process adopts high-grade electric energy heating, and energy consumption is very high.It is reported that the average current drain of 1 ton of calcium carbide of China's production reaches 3250kWh[Tang Wei, power-saving technology, 1999,17 (1): 38], wherein, about 60% are used for raw material heating and reaction, take away [Zheng Guohan by high temperature calcium carbide furnace gas (comprising CO) emptying about 40%, the calcium carbide progress in Production Technology, modern chemical industry, 1985:22-25].In addition, the electric furnace complex structure, be difficult to amplify, consumed electrode is big, cause dropping into and running cost very high.
It is reported that calcium carbide also can promptly provide heat by burnings such as coal, heavy oil or Sweet natural gases by the hot method preparation of oxygen, substitutes electrode heat supply [Zheng Guohan, calcium carbide progress in Production Technology, modern chemical industry, 1985:22-25].Japan (clear 61-178412) and Germany disclose the hot method of the complete burnt oxygen of shaft furnace, but because the multiplication of coke consumption amount, production cost also is higher than arc process.2005, China (CN1843907A) disclosed a kind of oxygen combustion injection technology with relatively inexpensive fuel auxiliary heat supplying such as coal, Sweet natural gas, heavy oil, by adding fluorite and bushel iron, produces calcium carbide and ferrosilicon simultaneously, and by-product gas CO is used to produce coal gas.But so far, oxygen Re Fashang does not apply [chemical industry Technological Economy, 1990,1:20].
Obviously, the hot method of traditional arc process and oxygen is produced calcium carbide and is all adopted fixed-bed reactor, can only use block raw material (3-20cm), to ensure the discharge of product C O gas, avoids air-flow freely not cause " collapsing bed ".Yet the reaction surface of block raw material is little, speed of reaction is slow, and the residence time in stove is long, throughput is little, and energy consumption of unit product is very high.In addition, the loss of block raw material in getting the raw materials ready is very big, and general about raw material more than 20% can not use [Wei Zemin, calcium carbide industrial energy saving Study on Technology, Chinese chlor-alkali, 1998,7:31] because grinding particle size is too small.The key reason of therefore, calcium carbide production " high investment, high energy consumption, high pollution " is that the mode, the by-product gas CO that adopt block raw material and electric arc heat supply rationally do not utilize.
Summary of the invention:
The present invention is intended to solve the problem of calcium carbide production " high investment, high energy consumption, high pollution ", and the contriver develops a kind of hot method system for producing calcium carbide of oxygen of powdery charging by a large amount of research and performing creative labour, and throughput is big, energy-saving and cost-reducing.
A kind of system for producing calcium carbide provided by the invention is characterized in that: comprise raw material preheating unit and reaction member;
The raw material preheating unit comprises raw material mixing and feeding device 1, primary heater unit 2, gas compressing apparatus 3 and interchanger I11; Raw material mixing and feeding device 1 comprises solid raw material mixer 12 and feeder 13, and the outlet of solid raw material mixer 12 is communicated with the import of feeder 13; Primary heater unit 2 is provided with feed(raw material)inlet 16, gas feed 17, pneumatic outlet I18 and solid materials outlet 19; The outlet of raw material mixing and feeding device 1 is communicated with the feed(raw material)inlet 16 of primary heater unit 2, and gas compressing apparatus 3 is communicated with primary heater unit 2 by gas feed 17; Interchanger I11 is communicated with primary heater unit 2 by pneumatic outlet I18;
Reaction member comprises feeding unit 4, reactor 5 and interchanger II9; Reactor 5 is provided with raw material spout 6, pneumatic outlet II7 and product relief outlet 8; The solid material inlet of feeding unit 4 is communicated with the solid materials outlet 19 of primary heater unit 2; The solid materials outlet of feeding unit 4 is communicated with the raw material spout 6 on the reactor 5, and raw material spout 6 is provided with the oxygen-containing gas inlet; Pneumatic outlet II7 on the reactor 5 is communicated with the gas inlet of interchanger II9, and heat exchange rear section gas enters the gas compressing apparatus 3 of preheating unit.
Further, feeder 13 is provided with the gas purging mouth, stops up feeder to prevent solid materials.
Further, described primary heater unit 2 comprises preheater 14, and the solid material inlet 16 and the gas inlet 17 of primary heater unit 2 are located on the preheater; Preheater is fluidized-bed reactor or air flow bed reactor.
Further, when described preheater 14 is the air flow bed reactor, primary heater unit 2 also comprises gas-solid separator 15, and the pneumatic outlet I18 of primary heater unit 2 and solid materials outlet 19 are located on the gas-solid separator 15.The gas that pneumatic outlet I18 comes out is by interchanger I11 emptying.
Gas-solid separator 15 is preferably cyclonic separator.
Further, the feeding unit 4 of reaction member is provided with the gas purging mouth, stops up feeding unit to prevent material.
Described feeder 13 and feeding unit 4 are screw feeder or U type pneumavalve material feeder.Because the temperature of charge of feeder 13 is low, preferred screw feeder.Since the temperature of charge height of feeding unit 4, preferred U type pneumavalve material feeder.
Further, also be provided with the oxygen-containing gas inlet on the raw material spout 6 of described reactor; Raw material spout 6 is single jet, to spout or multi-port.Preferably to spout, to increase the mixing of solid materials.
Further, the connecting pipe of described gas compressing apparatus 3 and interchanger II9 is provided with the auxiliary fuel inlet.
Further, be provided with storing unit between the feeding unit 4 of described primary heater unit 2 and reaction member.Described storing unit is storage tank, storage tank, storage pipe or lock hopper.
Description of drawings
Synoptic diagram of the present invention when the described preheater 14 of Fig. 1 is fluidized-bed reactor.
Synoptic diagram of the present invention when the described preheater 14 of Fig. 2 is the air flow bed reactor.
Embodiment
Mode one: as shown in Figure 1, after powdery carbon raw material and powdery calcic raw material mix, send into the fluidized-bed preheater in solid raw material mixer by screw feeder; Gas after oxygen-containing gas and the waste heat boiler heat exchange is delivered to the gas inlet of preheater bottom by gas compressing apparatus; Gas after part carbon raw material and the waste heat boiler heat exchange burns in preheater under the effect of oxygen-containing gas, and raw material is heated to 700-1000 ℃, and making the carbon raw material pyrolysis is coke powder, and the pyrolysis of calcic raw material is a calcium oxide powder.The high-temperature gas that produces is discharged after by the pipe bundle heat exchanger heat exchange, the high-temp solid mixture that forms is delivered to the raw material spout of reactor by U type pneumavalve material feeder, spray into reactor by the spout pipe core, oxygen-containing gas sprays into reactor by the spout outer shroud, part coke powder and oxygen-containing gas are heated to 1750-2000 ℃ with material and form calcium carbide in reactor mixed firing.Calcium carbide is discharged by the product relief outlet of reactor bottom; Gaseous product is discharged by the pneumatic outlet of reactor and is entered waste heat boiler, and heat exchange rear section gas sprays into preheater by gas compressing apparatus, as preheater fuel.
Mode two: as shown in Figure 2, after powdery carbon raw material and powdery calcic raw material mix, send into the air flow bed preheater in solid raw material mixer by screw feeder; Gas after oxygen-containing gas and the waste heat boiler heat exchange is delivered to the gas inlet of preheater bottom by gas compressing apparatus; Gas after part carbon raw material and the waste heat boiler heat exchange burns in preheater under the effect of oxygen-containing gas, and raw material is heated to 700-1000 ℃, and making the carbon raw material pyrolysis is coke powder, and the pyrolysis of calcic raw material is a calcium oxide powder.The high-temperature product that forms enters cyclonic separator, the gaseous product of separating is discharged after the pipe bundle heat exchanger cooling, the solid product of separating is delivered to the raw material spout of reactor by U type pneumavalve material feeder, spray into reactor by the spout pipe core, oxygen-containing gas sprays into reactor by the spout outer shroud, the mixed firing in reactor of part coke powder and oxygen-containing gas is heated to 1750-2000 ℃ with material and forms calcium carbide.Calcium carbide is discharged by the product relief outlet of reactor bottom; Gaseous product is discharged by the pneumatic outlet of reactor and is entered waste heat boiler, and heat exchange rear section gas sprays into preheater by gas compressing apparatus, as preheater fuel.
The invention solves the problem of calcium carbide production " high investment, high energy consumption, high pollution ", develop a kind of hot method system for producing calcium carbide of oxygen of powdery charging, its throughput is that more than 5 times of arc process, production cost reduce more than 20%.
Claims (10)
1. a system for producing calcium carbide is characterized in that: comprise raw material preheating unit and reaction member;
The raw material preheating unit comprises raw material mixing and feeding device (1), primary heater unit (2), gas compressing apparatus (3) and interchanger I (11); The unitary raw material mixing and feeding device of described raw material preheating (1) comprises solid raw material mixer (12) and feeder (13), and the outlet of solid raw material mixer (12) is communicated with the import of feeder (13); Primary heater unit (2) is provided with feed(raw material)inlet (16), gas feed (17), pneumatic outlet I (18) and solid materials outlet (19); The outlet of raw material mixing and feeding device (1) is communicated with the feed(raw material)inlet (16) of primary heater unit (2), and gas compressing apparatus (3) is communicated with primary heater unit (2) by gas feed (17); Interchanger I (11) is communicated with primary heater unit (2) by pneumatic outlet I (18);
Reaction member comprises feeding unit (4), reactor (5) and interchanger II (9); Reactor (5) is provided with raw material spout (6), pneumatic outlet II (7) and product relief outlet (8); The solid material inlet of feeding unit (4) is communicated with the solid materials outlet (19) of primary heater unit (2); The solid materials outlet of feeding unit (4) is communicated with the raw material spout (6) on the reactor (5); Pneumatic outlet II (7) on the reactor (5) is communicated with the gas inlet of interchanger II (9), and the pneumatic outlet of interchanger II (9) connects the gas compressing apparatus (3) of preheating unit.
2. system for producing calcium carbide according to claim 1 is characterized in that: feeder (13) is gone up or the feeding unit (4) of reaction member is provided with the gas purging mouth.
3. system for producing calcium carbide according to claim 1, it is characterized in that described primary heater unit (2) comprises preheater (14), the feed(raw material)inlet (16) and the gas feed (17) of primary heater unit (2) are located on the preheater, and preheater is fluidized-bed reactor or air flow bed reactor;
When described preheater (14) is the air flow bed reactor, primary heater unit (2) also comprises gas-solid separator (15), and the solid materials outlet (19) and the pneumatic outlet I (18) of primary heater unit (2) are located on the gas-solid separator (15).
4. system for producing calcium carbide according to claim 3 is characterized in that described gas-solid separator (15) is a cyclonic separator.
5. system for producing calcium carbide according to claim 1 is characterized in that: described feeder (13) and feeding unit (4) are screw feeder or U type pneumavalve material feeder.
6. system for producing calcium carbide according to claim 1 is characterized in that: described interchanger II (9) and interchanger I (11) are pipe bundle heat exchanger, plate-type heat exchanger or waste heat boiler.
7. system for producing calcium carbide according to claim 1 is characterized in that: the raw material spout (6) of described reactor is single jet, to spout or multi-port.
8. system for producing calcium carbide according to claim 1 is characterized in that also being provided with on the raw material spout (6) the oxygen-containing gas inlet.
9. system for producing calcium carbide according to claim 1 is characterized in that: the connecting pipe of described gas compressing apparatus (3) and interchanger II (9) is provided with the auxiliary fuel inlet.
10. system for producing calcium carbide according to claim 1 is characterized in that: be provided with storing unit between the feeding unit (4) of described primary heater unit (2) and reaction member.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102398056A CN101428799B (en) | 2008-12-12 | 2008-12-12 | System for producing calcium carbide |
| CA2730754A CA2730754C (en) | 2008-08-01 | 2009-07-15 | Method and system for producing calcium carbide |
| JP2011520306A JP5498494B2 (en) | 2008-08-01 | 2009-07-15 | Carbide manufacturing method and system |
| PCT/CN2009/072770 WO2010012193A1 (en) | 2008-08-01 | 2009-07-15 | Method and system for the production of calcium carbide |
| CN200980123693.0A CN102066248B (en) | 2008-08-01 | 2009-07-15 | Method and system for the production of calcium carbide |
| US13/017,207 US20110123428A1 (en) | 2008-08-01 | 2011-01-31 | Method and system for producing calcium carbide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102398056A CN101428799B (en) | 2008-12-12 | 2008-12-12 | System for producing calcium carbide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101428799A true CN101428799A (en) | 2009-05-13 |
| CN101428799B CN101428799B (en) | 2011-05-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008102398056A Expired - Fee Related CN101428799B (en) | 2008-08-01 | 2008-12-12 | System for producing calcium carbide |
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| Country | Link |
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| CN (1) | CN101428799B (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010012193A1 (en) * | 2008-08-01 | 2010-02-04 | 北京化工大学 | Method and system for the production of calcium carbide |
| CN102701205A (en) * | 2012-02-01 | 2012-10-03 | 新疆中泰化学（集团）股份有限公司 | Method for repairing and recycling calcium carbide pot |
| CN102850172A (en) * | 2012-09-13 | 2013-01-02 | 北京化工大学 | Coal chemical poly-generation process and system |
| CN102889944A (en) * | 2012-09-17 | 2013-01-23 | 许继集团有限公司 | Calcium carbide production furnace temperature monitoring method |
| CN103408014A (en) * | 2013-08-27 | 2013-11-27 | 北京化工大学 | System for producing calcium carbide by using biomass fuel |
| WO2015027644A1 (en) * | 2013-08-27 | 2015-03-05 | 北京化工大学 | Method and device for producing calcium carbide from biomass fuel |
| CN104645882A (en) * | 2015-02-12 | 2015-05-27 | 东至绿洲环保化工有限公司 | Organic silicon synthesis equipment |
| CN105293497A (en) * | 2015-11-16 | 2016-02-03 | 中冶南方工程技术有限公司 | Calcium carbide smelting process by oxygen heating method |
| CN105293495A (en) * | 2015-11-04 | 2016-02-03 | 中冶南方工程技术有限公司 | Flash smelting furnace for calcium carbide and system |
| CN106276901A (en) * | 2015-05-28 | 2017-01-04 | 中国科学院上海高等研究院 | A kind of oxygen full-boiled process produces carbide and the method and system of CO gas |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3044858A (en) * | 1957-12-16 | 1962-07-17 | Texaco Inc | Calcium carbide process |
-
2008
- 2008-12-12 CN CN2008102398056A patent/CN101428799B/en not_active Expired - Fee Related
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102066248A (en) * | 2008-08-01 | 2011-05-18 | 北京化工大学 | Method and system for the production of calcium carbide |
| WO2010012193A1 (en) * | 2008-08-01 | 2010-02-04 | 北京化工大学 | Method and system for the production of calcium carbide |
| CN102701205B (en) * | 2012-02-01 | 2014-06-25 | 新疆中泰化学（集团）股份有限公司 | Method for repairing and recycling calcium carbide pot |
| CN102701205A (en) * | 2012-02-01 | 2012-10-03 | 新疆中泰化学（集团）股份有限公司 | Method for repairing and recycling calcium carbide pot |
| CN102850172A (en) * | 2012-09-13 | 2013-01-02 | 北京化工大学 | Coal chemical poly-generation process and system |
| CN102850172B (en) * | 2012-09-13 | 2014-12-03 | 北京化工大学 | Coal chemical poly-generation process and system |
| CN102889944A (en) * | 2012-09-17 | 2013-01-23 | 许继集团有限公司 | Calcium carbide production furnace temperature monitoring method |
| CN103408014B (en) * | 2013-08-27 | 2014-12-03 | 北京化工大学 | System for producing calcium carbide by using biomass fuel |
| CN103408014A (en) * | 2013-08-27 | 2013-11-27 | 北京化工大学 | System for producing calcium carbide by using biomass fuel |
| WO2015027644A1 (en) * | 2013-08-27 | 2015-03-05 | 北京化工大学 | Method and device for producing calcium carbide from biomass fuel |
| CN104645882A (en) * | 2015-02-12 | 2015-05-27 | 东至绿洲环保化工有限公司 | Organic silicon synthesis equipment |
| CN106276901A (en) * | 2015-05-28 | 2017-01-04 | 中国科学院上海高等研究院 | A kind of oxygen full-boiled process produces carbide and the method and system of CO gas |
| CN106276901B (en) * | 2015-05-28 | 2020-07-24 | 中国科学院上海高等研究院 | Method and system for producing calcium carbide and CO gas by using oxygen thermal method |
| CN105293495A (en) * | 2015-11-04 | 2016-02-03 | 中冶南方工程技术有限公司 | Flash smelting furnace for calcium carbide and system |
| CN105293495B (en) * | 2015-11-04 | 2017-11-21 | 中冶南方工程技术有限公司 | Calcium carbide flash smelting furnace and system |
| CN105293497A (en) * | 2015-11-16 | 2016-02-03 | 中冶南方工程技术有限公司 | Calcium carbide smelting process by oxygen heating method |
| CN105293497B (en) * | 2015-11-16 | 2018-03-13 | 中冶南方工程技术有限公司 | A kind of hot method of oxygen smelts calcium carbide technique |
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