CN103523762B - Yellow phosphorus production method and equipment - Google Patents
Yellow phosphorus production method and equipment Download PDFInfo
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- CN103523762B CN103523762B CN201310454643.9A CN201310454643A CN103523762B CN 103523762 B CN103523762 B CN 103523762B CN 201310454643 A CN201310454643 A CN 201310454643A CN 103523762 B CN103523762 B CN 103523762B
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Abstract
The invention discloses a yellow phosphorus production method and equipment which do not produce mud phosphorus and can reduce the dust content in tail gas. The method comprises the technology links as follows: 1, electric furnace smelting; 2, furnace gas purification, furnace gas discharged from an electric furnace is guided into a furnace gas dust collecting system through an exhaust pipeline, the furnace gas dust collecting system comprises at least a filter used for filtering the furnace gas, the filter is provided with a sintering inorganic porous material filter element capable of meeting following work conditions, and the operation performed according to the filter comprises the steps as follows: 1), the operation executed during driving: inert preheating gas is injected into the filter, and the sintering inorganic porous material filter element in the filter is heated to 187.5 DEG C or above; 2), the operation executed during normal operation: to-be-filtered furnace gas with the temperature maintained to be 187.5-280 DEG C is input into the filter, and the dust content in the filtered clean furnace gas is below 10-20 mg/m <3>; and 3), the operation executed during reverse blowing and 4) the operation executed during parking; and 3, phosphorus collecting and refining.
Description
Technical field
The application relates to production method and the equipment of yellow phosphorus.
Background technology
The electric furnace process phosphorus production technique of industrial applications is divided into the production technique and use multi-electrode phosphorus electric furnace production technique that use large-scale self baking electrode phosphor furnace.Though these two kinds of techniques are in the electric furnace type of furnace and scale, feed stock for blast furnace processing requirements, the aspects such as furnace gas dust suppression there are differences, but main flow is substantially identical, namely be all by by Rock Phosphate (72Min BPL), the compound that silica and coke are made in proportion sends into electric furnace, compound generation reduction reaction in electric furnace generates furnace gas, furnace gas is from the effusion of reaction melting zone, after the furnace gas filtering layer that stove internal upper part is formed by the compound of continuous supplementation, the impurity carried in a part of compound is discharged from electric furnace, again through dedusting, condensation is washed, refining spearation obtains yellow phosphorus product, tail gas is then recycled or is discharged.
Wherein, in the production technique using large-scale self baking electrode phosphor furnace, furnace transformer capacity is generally 50000-90000KVA, and output, generally more than 30000 tons/year, adopts self-baking electric furnace; Feed stock for blast furnace is required very strict (as feeding density charcoal moisture, granularity etc.), usually adopts sintering process, pelletizing method after carrying out pre-treatment, just can enter stove, can not directly use lump ore to enter stove, and the furnace gas temperature produced is generally higher than 350 DEG C; The furnace gas of discharging from electric furnace enters electrostatic precipitator (i.e. dry method dust), and (dustiness is generally at 50mg/m for the furnace gas after udst separation
3left and right) enter condensate recovery system after obtain thick phosphorus, then thick phosphorus is imported in thick phosphorus refining system and refines, obtain yellow phosphorus product.
Use in the production technique of multi-electrode phosphorus electric furnace, all little than large-scale self baking electrode phosphor furnace technique many of furnace transformer capacity and output, be generally below 28000KVA, output is generally 7000-10000 ton/year, adopt molded graphite electrode, arrangement form is generally three-phase 6 or three-phase 7 diameter 500mm or diameter 600mm Graphite Electrodes; Feed stock for blast furnace does not need sintered material or pelletizing feed, and adopt and dry pre-treatment, lump ore enters stove, the general 100-170 DEG C of furnace gas temperature; The furnace gas of discharging from electric furnace directly enters condensate recovery system (i.e. wet dedusting), and condensed yellow phosphorus enters in receiving tank and is thick phosphorus, is then imported in thick phosphorus refining system by thick phosphorus and refines, obtain yellow phosphorus product and a large amount of mud phosphorus.
Though the production technique of above-mentioned use large-scale self baking electrode phosphor furnace can produce less mud phosphorus and waste water, but electrostatic precipitator auxiliary facility construction cost is huge, run and maintenance cost is high, personnel's technical requirements is high, and insufficient to the dust purification process in furnace gas, can not the desirable emission problem solving PM2.5 in tail gas.And use the production technique of multi-electrode phosphorus electric furnace to have a large amount of difficult mud phosphorus be separated to produce, and dustiness in tail gas is higher.
Summary of the invention
Technical problems to be solved in this application have: the first, provide a kind of phosphorus production method and apparatus, use multi-electrode phosphorus electric furnace, substantially do not produce mud phosphorus and can reduce tail gas dustiness by the method and equipment.The second, a kind of yellow phosphorus preparation method and equipment are provided, use large-scale self baking electrode phosphor furnace, substantially do not produce mud phosphorus by the method and equipment and tail gas dustiness can be reduced, save system operation cost again simultaneously.
First, the phosphorus production method (calling method one in the following text) of the application, the process procedure comprised has:
One, electrosmelting
The compound be made in proportion by Rock Phosphate (72Min BPL), silica and coke is sent into electric furnace, compound generation reduction reaction in electric furnace generates furnace gas, furnace gas is from the effusion of reaction melting zone, and after the furnace gas filtering layer that stove internal upper part is formed by the compound of continuous supplementation, the impurity carried in a part of compound is discharged from electric furnace; Described electric furnace is multi-electrode phosphorus electric furnace;
Two, flue gas cleaning
By smoke discharging pipe, the furnace gas of discharging from electric furnace is imported dust-collecting system of flue, this dust-collecting system of flue at least comprises the strainer filtered for described furnace gas, this strainer has the sintering inorganic porous material filter core that can meet following working conditions, and the operation that should perform for this strainer comprises:
The operation performed when 1. driving: inject inertia preheating gas in strainer, thus the sintering inorganic porous material filter core in strainer is preheated to more than 187.5 DEG C;
The operation performed when 2. normally running: input temp remains the furnace gas to be filtered of 187.5-280 DEG C in strainer, and the dustiness of clean furnace gas after filtering is 10-20mg/m
3below;
3. the operation performed during blowback: start the inertia purge gas that back-blowing device to implantation temperature in strainer is more than 187.5 DEG C, the pressure-controlling of inertia purge gas is 0.2-1.0MPa;
The operation performed when 4. stopping: implantation temperature is the inertia substitution gas of more than 187.5 DEG C in strainer, makes sintering inorganic porous material filter core not occur to stick with paste fouling membrane under the protection of inertia substitution gas;
Three, receive phosphorus to refine
The clean furnace gas of being discharged by strainer imports condensate recovery system, and condensed yellow phosphorus enters in receiving tank and is thick phosphorus, is then imported in thick phosphorus refining system by thick phosphorus and refines, obtain yellow phosphorus product; Tail gas recycle utilizes or discharge;
In aforesaid method, by installing heat-exchanger rig on described smoke discharging pipe or/and the furnace gas filtering layer thickness of adjustment described in electric furnace or/and adjust electrode power thus the furnace gas temperature to be filtered passing into strainer is remained 187.5-280 DEG C under the prerequisite of strictly carrying out compound process.
In method one, when the furnace gas temperature to be filtered passing into strainer is lower than 187.5 DEG C, will the phosphorus vapor condensation in furnace gas be caused, and cause strainer normally to work; When the furnace gas temperature to be filtered passing into strainer is higher than 280 DEG C, then can reduce the yield of yellow phosphorus.The furnace gas temperature to be filtered passing into strainer is preferably 187.5-220 DEG C, and at this moment the yield of yellow phosphorus is higher.
The furnace gas temperature to be filtered passing into strainer is remained the technique means of 187.5-280 DEG C (being preferably 187.5-220 DEG C), one is utilize the temperature of heat-exchanger rig to furnace gas to control, two is the furnace gas filtering layer thickness of adjustment described in electric furnace, and three is adjust electrode power under the prerequisite of strictly carrying out compound process.These three kinds of means can be combined, and also can be used alone.Wherein, because usual the produced furnace gas temperature of multi-electrode phosphorus electric furnace is lower, the furnace gas temperature to be filtered passing into strainer be made to remain 187.5-280 DEG C by heat-exchanger rig, should be heated furnace gas by heat-exchanger rig.
The Main Function of furnace gas filtering layer reduces the dust carried secretly in furnace gas.In the past, in order to reduce the output of mud phosphorus, often require that furnace gas filtering layer is thicker.Owing to using multi-electrode phosphorus electric furnace, usually its furnace gas temperature produced itself is lower, at this moment, the furnace gas temperature to be filtered passing into strainer to be made to remain 187.5-280 DEG C by adjustment furnace gas filtering layer thickness, should take to reduce furnace gas filtering layer thickness, the calorific loss of furnace gas by furnace gas filtering layer can be reduced like this, thus the furnace gas temperature to be filtered passing into strainer is improved.
When using multi-electrode phosphorus electric furnace, in the past to the processing requirements of feed stock for blast furnace not high (as feeding density charcoal moisture, granularity etc.), if use too high electrode power, probably cause side reaction to increase, reduce output phosphor.Therefore, as the furnace gas temperature to be filtered passing into strainer made to remain 187.5-280 DEG C by adjustment electrode power, its prerequisite is that reply raw material strictly processes, stove is reentered after pre-treatment being carried out to raw material as adopted sintering process, pelletizing method, in this case, just electrode power can be improved by increase voltage, electric current.
In a word, means are above utilized the furnace gas temperature to be filtered passing into strainer can be remained 187.5-280 DEG C (being preferably 187.5-220 DEG C).In addition, for above-mentioned strainer, apply it in phosphorus furnace gas filtration environment and also need to overcome strainer driving, blowback and parking period, phosphorus vapor condensation is caused to cause filter core to stick with paste fouling membrane due to sintering inorganic porous material cartridge surface temperature shock, the technical difficulty of duct blocking.For this reason, the means of the inertia preheating gas of above-mentioned injection certain temperature, inertia purge gas and inertia substitution gas are taked.
Adopt the significant advantage of the strainer with the sintering inorganic porous material filter core precision that is also to gather dust high.In aforesaid method to the accuracy requirement of gathering dust of strainer be filter after clean furnace gas dustiness at 10-20mg/m
3below.For reaching this requirement, the sintering inorganic porous material filter core of respective aperture can be selected.Test finds, filters in environment, when the clean furnace gas dustiness after metre filter is at 20mg/m at phosphorus furnace gas
3time following, inertia purge gas pressure-controlling should can be ensured the work of sintering inorganic porous material filter core long-time stable at 0.2-1.0MPa.
The phosphorus production equipment of implementation method one, comprise electric furnace, dust-collecting system of flue, condensate recovery system and thick phosphorus refining system, electric furnace is connected with dust-collecting system of flue by smoke discharging pipe, described electric furnace is multi-electrode phosphorus electric furnace, described dust-collecting system of flue at least comprises the strainer for filtering furnace gas, this strainer has the sintering inorganic porous material filter core that can meet following working conditions, and the operation that should perform for this strainer comprises:
The operation performed when 1. driving: inject inertia preheating gas in strainer, thus the sintering inorganic porous material filter core in strainer is preheated to more than 187.5 DEG C;
The operation performed when 2. normally running: input temp remains the furnace gas to be filtered of 187.5-280 DEG C in strainer, and the dustiness of clean furnace gas after filtering is 10-20mg/m
3below;
3. the operation performed during blowback: start the inertia purge gas that back-blowing device to implantation temperature in strainer is more than 187.5 DEG C, the pressure-controlling of inertia purge gas is 0.2-1.0MPa;
The operation performed when 4. stopping: implantation temperature is the inertia substitution gas of more than 187.5 DEG C in strainer, makes sintering inorganic porous material filter core not occur to stick with paste pollution under the protection of inertia substitution gas;
Wherein, by installing heat-exchanger rig on described smoke discharging pipe or/and adjustment electric furnace in described furnace gas filtering layer thickness or/and adjust electrode power thus the furnace gas temperature to be filtered passing into strainer is remained 187.5-280 DEG C under the prerequisite of strictly carrying out the process of electrosmelting compound.
Secondly, the yellow phosphorus preparation method (calling method two in the following text) of the application, the process procedure comprised has:
One, electrosmelting
The compound be made in proportion by Rock Phosphate (72Min BPL), silica and coke is sent into electric furnace, compound generation reduction reaction in electric furnace generates furnace gas, furnace gas is from the effusion of reaction melting zone, and after the furnace gas filtering layer that stove internal upper part is formed by the compound of continuous supplementation, the impurity carried in a part of compound is discharged from electric furnace; Described electric furnace is large-scale self baking electrode phosphor furnace;
Two, flue gas cleaning
By smoke discharging pipe, the furnace gas of discharging from electric furnace is imported dust-collecting system of flue, this dust-collecting system of flue at least comprises the strainer filtered for described furnace gas, this strainer has the sintering inorganic porous material filter core that can meet following working conditions, and the operation that should perform for this strainer comprises:
The operation performed when 1. driving: inject inertia preheating gas in strainer, thus the sintering inorganic porous material filter core in strainer is preheated to more than 187.5 DEG C;
The operation performed when 2. normally running: input temp remains the furnace gas to be filtered of 420-590 DEG C in strainer, and the dustiness of clean furnace gas after filtering is 10-20mg/m
3below;
3. the operation performed during blowback: start the inertia purge gas that back-blowing device to implantation temperature in strainer is more than 187.5 DEG C, the pressure-controlling of inertia purge gas is 0.2-1.0MPa;
The operation performed when 4. stopping: implantation temperature is the inertia substitution gas of more than 187.5 DEG C in strainer, makes sintering inorganic porous material filter core not occur to stick with paste fouling membrane under the protection of inertia substitution gas;
Three, receive phosphorus to refine
The clean furnace gas of being discharged by strainer imports condensate recovery system, and condensed yellow phosphorus enters in receiving tank and is thick phosphorus, is then imported in thick phosphorus refining system by thick phosphorus and refines, obtain yellow phosphorus product; Tail gas recycle utilizes or discharge;
In aforesaid method, by installing heat-exchanger rig on described smoke discharging pipe or/and the furnace gas filtering layer thickness of adjustment described in electric furnace or/and adjust electrode power thus the furnace gas temperature to be filtered passing into strainer is remained 420-590 DEG C under the prerequisite of strictly carrying out compound process.
In method two, the furnace gas temperature to be filtered passing into strainer is 420-590 DEG C, far above 187.5 DEG C of the phosphorus vapor condensation that will cause in furnace gas, therefore, can ensure the normal work of strainer completely.Meanwhile, when filtration temperature is 420-590 DEG C, find that the yield of yellow phosphorus is higher.On this basis, the furnace gas temperature to be filtered passing into strainer is preferably 420-530 DEG C, and at this moment the yield of yellow phosphorus is higher.
The furnace gas temperature to be filtered passing into strainer is remained the technique means of 420-590 DEG C (being preferably 420-530 DEG C), one is utilize the temperature of heat-exchanger rig to furnace gas to control, two is the furnace gas filtering layer thickness of adjustment described in electric furnace, and three is adjustment electrode powers.These three kinds of means can be combined, and also can be used alone.
Because usual the produced furnace gas temperature of large-scale self baking electrode phosphor furnace is originally just higher, therefore, generally speaking, by heat-exchanger rig, furnace gas is suitably heated, slightly reduce furnace gas filtering layer thickness or slightly increase voltage, electric current improves electrode power and just the furnace gas temperature to be filtered passing into strainer can be remained 420-590 DEG C.
In addition, for above-mentioned strainer, apply it in phosphorus furnace gas filtration environment and also need to overcome strainer driving, blowback and parking period, phosphorus vapor condensation is caused to cause filter core to stick with paste fouling membrane due to sintering inorganic porous material cartridge surface temperature shock, the technical difficulty of duct blocking.For this reason, the means of the inertia preheating gas of above-mentioned injection certain temperature, inertia purge gas and inertia substitution gas are taked.
Usually, the temperature of inertia preheating gas, inertia purge gas and inertia substitution gas is controlled be 187.5 DEG C and just can stick with paste fouling membrane by filter core, but, preferably the temperature of inertia preheating gas, inertia purge gas and inertia substitution gas can be controlled for basically identical with the furnace gas temperature to be filtered passing into strainer (420-590 DEG C), filter core temperature can be stablized like this, improve the work-ing life of filter core.
Adopt the significant advantage of the strainer with the sintering inorganic porous material filter core precision that is also to gather dust high.In aforesaid method to the accuracy requirement of gathering dust of strainer be filter after clean furnace gas dustiness at 10-20mg/m
3below.For reaching this requirement, the sintering inorganic porous material filter core of respective aperture can be selected.Test finds, filters in environment, when the clean furnace gas dustiness after metre filter is at 20mg/m at phosphorus furnace gas
3time following, inertia purge gas pressure-controlling should can be ensured the work of sintering inorganic porous material filter core long-time stable at 0.2-1.0MPa.
The yellow phosphorus Preparation equipment of implementation method two, comprise electric furnace, dust-collecting system of flue, condensate recovery system and thick phosphorus refining system, electric furnace is connected with dust-collecting system of flue by smoke discharging pipe, described electric furnace is large-scale self baking electrode phosphor furnace, described dust-collecting system of flue at least comprises the strainer for filtering furnace gas, this strainer has the sintering inorganic porous material filter core that can meet following working conditions, and the operation that should perform for this strainer comprises:
The operation performed when 1. driving: inject inertia preheating gas in strainer, thus the sintering inorganic porous material filter core in strainer is preheated to more than 187.5 DEG C;
The operation performed when 2. normally running: input temp remains the furnace gas to be filtered of 420-590 DEG C in strainer, and the dustiness of clean furnace gas after filtering is 10-20mg/m
3below;
3. the operation performed during blowback: start the inertia purge gas that back-blowing device to implantation temperature in strainer is more than 187.5 DEG C, the pressure-controlling of inertia purge gas is 0.2-1.0MPa;
The operation performed when 4. stopping: implantation temperature is the inertia substitution gas of more than 187.5 DEG C in strainer, makes sintering inorganic porous material filter core not occur to stick with paste pollution under the protection of inertia substitution gas;
Wherein, by installing heat-exchanger rig on described smoke discharging pipe or/and adjustment electric furnace in described furnace gas filtering layer thickness or/and adjust electrode power thus the furnace gas temperature to be filtered passing into strainer is remained 420-590 DEG C under the prerequisite of strictly carrying out the process of electrosmelting compound.
Method one described above, method two, the strainer of sintering inorganic porous material filter core is used to carry out dry gas cleaning purification to the furnace gas that electric furnace is discharged because they all have employed, the filtering accuracy of sintering inorganic porous material filter core is high, thermal shock resistance is good, can be used by online pulse cleaning, therefore, aforesaid method can reduce mud phosphorus generation and tail gas dustiness, and running cost is lower simultaneously.
In the equipment of method one, method two, the dust removal installation of dust-collecting system of flue is preferably made up of described strainer and the mechanical dust-precipitator between strainer and electric furnace; The furnace gas of discharging from electric furnace is first entered mechanical dust-precipitator by smoke discharging pipe and carries out primary dust removing purification, and then enters in strainer and carry out two-stage dust removal purification.The gather dust amount of strainer within the unit time can be alleviated like this, and can interval time of corresponding raising strainer blowback.
In addition, in the equipment of method one, method two, also following improvement is carried out to the smoke discharging pipe be connected between electric furnace and dust-collecting system of flue, that is: this smoke discharging pipe has interconnective gas ascent stage and gas downcomer, the entrance of gas ascent stage is connected with electric furnace, and the outlet of gas downcomer is connected with dust-collecting system of flue; Described heat-exchanger rig is arranged on the pipeline section place, end of gas ascent stage, and the initiating terminal of gas downcomer is connected to the side of this gas ascent stage end pipeline section.
Because smoke discharging pipe has interconnective gas ascent stage and gas downcomer, and heat-exchanger rig is arranged on the pipeline section place, end of gas ascent stage, the initiating terminal of gas downcomer is connected to the side of this gas ascent stage end pipeline section, therefore, operationally, treat that first the furnace gas of dedusting flows in the gas ascent stage on lower, arrive pipeline section place, end and the abundant heat exchange of heat-exchanger rig, then break-in enters the initiating terminal of gas downcomer, dust granules in air-flow clashes into tube wall under inertia, thus with air flow settlement.Visible, above-mentioned innovative approach can improving heat exchanging efficiency, and is beneficial to and gathers dust.
In order to better impel dust settling, the main part of described gas downcomer is the straight tube be obliquely installed horizontal by angle 10-40 °.On this basis, the main part of gas downcomer is preferably the straight tube be obliquely installed horizontal by angle 15-25 °.Gas ascent stage and gas downcomer can connect into " people " font, and at this moment, air-flow is lower at the flow velocity at gas ascent stage end pipeline section place, and heat exchange is more abundant.In addition, the gas ascent stage is preferably arranged, so that gas upwards flows in vertical haply.
Below in conjunction with the drawings and specific embodiments, the application is described further.The aspect that the application adds and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by the practice of the application.
Embodiment
Yellow phosphorus technical process as shown in Figure 1, electric furnace 1 is provided with heat-exchanger rig 6 by smoke discharging pipe 2(smoke discharging pipe 2) be connected with dust-collecting system of flue 3, the dust removal installation of dust-collecting system of flue 3 is made up of strainer 301 and the mechanical dust-precipitator 302 between strainer 301 and electric furnace 1, the furnace gas that electric furnace 1 is discharged first is entered in mechanical dust-precipitator 302 by smoke discharging pipe 2 and carries out primary dust removing purification, and then enters in strainer 301 and carry out two-stage dust removal purification, the clean furnace gas that strainer 301 is discharged imports condensate recovery system 4, condensate recovery system 4 comprises spray column 401 and receiving tank 402, spray condensed yellow phosphorus through spray column 401 to enter in receiving tank 402 and be thick phosphorus, thick phosphorus enters in thick phosphorus refining system 5 again and refines, thick phosphorus refining system 5 comprises refining kettle 501, thick phosphorus uses steam heating in refining kettle 501, stir, after clarification, pure phosphorus is deposited in the bottom of a pan, tail gas gases such as () CO that spray column 401 is discharged is divided into two-way through total water seal, as fuel after one tunnel is through and purifies further, one tunnel is in not used time emptying, in addition, strainer 301 is also connected with one for providing the air feeder 303 of inertia preheating gas, inertia purge gas and inertia substitution gas needed for it to strainer 301, the first output tube 305 and the second output tube 306 is connected respectively after this air feeder 303 heater via 304, the output terminal of the first output tube 305 connects the back-blowing device of strainer 301, the output terminal of the second output tube 306 is connected on the furnace gas intake ducting to be filtered of strainer 301, and the first output tube 305 and the second output tube 306 are respectively arranged with valve.
As shown in Figure 2, described smoke discharging pipe 2 has interconnective gas ascent stage 201 and gas downcomer 202, this gas ascent stage 201 and gas downcomer 202 connect into " people " font, and the gas ascent stage 201 is haply in vertically arranging, the entrance of gas ascent stage 201 is connected with electric furnace 1, and the outlet of gas downcomer 202 is connected with the mechanical dust-precipitator 302 of dust-collecting system of flue 3; Described heat-exchanger rig 6 is arranged on the pipeline section place, end of gas ascent stage 201, and the initiating terminal of gas downcomer 202 is connected to the side of this gas ascent stage 201 end pipeline section.Heat-exchanger rig 6 adopts electrically heated, steam heating or the heating of thermal conductance oil, and heating unit (or heating tube) is located immediately in the end pipeline section of gas ascent stage 201, thus directly contacts with the air-flow passed through.The main part of gas downcomer 202 is be about 16 ° of straight tubes be obliquely installed horizontal by angle.Machinery dust-precipitator 302 comprises a tank body for dust settling, and the top of this tank body is provided with the delivery port of gas after dust settling, and place on the lower side, tank body top is provided with lower diffusion shell 302a, and the input aperture of lower diffusion shell 302a is connected with the delivery port of described smoke discharging pipe 2.Certainly, mechanical dust-precipitator 302 also can adopt gravitational precipitator, tornado dust collector etc.Said structure smoke discharging pipe 2 and mechanical dust-precipitator 302, when the system is operating, treat that first the furnace gas of dedusting flows in the gas ascent stage 201 on lower, arrive pipeline section place, end fully to contact with heat-exchanger rig 6, then break-in enters the initiating terminal of gas downcomer 202, dust granules in air-flow clashes into tube wall under inertia, thus with air flow settlement on the ramp way of gas downcomer 202, and move in the input aperture of diffusion shell 302a down, after dust-laden gas enters lower diffusion shell 302a, spread to tank base by lower diffusion shell 302a, make the abundant sedimentation of dust, the furnace gas that dustiness is less then discharges from the delivery port at the top of tank body to strainer 301.
As shown in Figure 3, by orifice plate arrangement, several sintering inorganic porous material filter core 301a is installed in strainer 301, the top of each group sintering inorganic porous material filter core 301a is provided with a Venturi meter 301b for blowback, the blowback rare gas element entering each Venturi meter 301b is controlled by a pulse valve 301c respectively, and each pulse valve 301c is namely by the first output tube 305 in gas bag (not shown) interface chart 1.In addition, the inlet air distribution device of furnace gas to be filtered is installed in the strainer 301 of Fig. 3, what this inlet air distribution device comprised that lower inlet duct 701 is connected with this lower inlet duct 701 respectively with Duo Gen leads riser 702, the upper end of leading riser 702 is provided with venting port 703, and the height of described venting port 703 is arranged in strainer 301 and sinters more than the upper height of inorganic porous material filter core 301a.Wherein, be promote uniform air distribution, lower inlet duct 701 comprises horizontally disposed ring pipe, and on this ring pipe, interval is furnished with and leads riser 702 described at least three.The furnace gas to be filtered entering strainer 301 can be divided into multichannel (facilitating being uniformly distributed of furnace gas to be filtered) Bing Shige road gas under the outside of sintering inorganic porous material filter core 301a is thrown with direction from top to bottom by above-mentioned inlet air distribution device, like this, make dust settling direction consistent with the flow direction of gas to be filtered, promote to be divided into sedimentation, effectively prevent airborne dust.
Be specifically described by the yellow phosphorus technical process of embodiment to the application below.Embodiment is divided into two groups, and first group of embodiment relates to the method two using method one, second group of embodiment of multi-electrode phosphorus electric furnace to use large-scale self baking electrode phosphor furnace.For the ease of comparing, in each group embodiment, each embodiment all uses same set of equipment, and their raw material also all branches away from ore deposit grade, proportioning, the identical same batch of material for the treatment of process (adopting prior art process).In order to accurately compare the yellow phosphorus yield that in each group embodiment, each embodiment obtains, design arranges refining kettle 501(each an embodiment corresponding refining kettle 501 consistent with embodiment quantity in thick phosphorus refining system 5), the outlet of condensate recovery system 4 can switch between these refining kettles 501; When an embodiment raw material complete reaction and receive after phosphorus terminates, when adding raw material (i.e. the raw material of another embodiment) of next batch, switch to corresponding refining kettle 501, like this, by calculating the yellow phosphorus amount that each refining kettle 501 obtains, the yellow phosphorus yield that these are implemented just can be obtained.
First group of enforcement
Embodiment 1
Employing transformer capacity is the multi-electrode phosphorus electric furnace of 15000KVA.50 tons of compounds are added electric furnace 1 continuously react, simultaneously, start air feeder 303, well heater 304, high temperature inert preheating gas is by the second output tube 306, strainer 301 is entered from the furnace gas intake ducting to be filtered of strainer 301, thus the sintering inorganic porous material filter core (adopting FeAl intermetallic compound porous material filter core) in strainer 301 is preheated to 187.5 DEG C, then close the valve on the second output tube 306.After this, by smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 200 DEG C.The every 600s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 187.5 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.6MPa.The dustiness of the clean furnace gas after filtration is 5mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 98.5%, far above the yield concentration of current 72-87%.
Embodiment 2
After embodiment 1 terminates, its equipment is directly adopted to proceed embodiment 2.Second batch 50 tons of compounds are added electric furnace 1 continuously react, meanwhile, switch to another refining kettle 501.By smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 250 DEG C.The every 600s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 187.5 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.6MPa.The dustiness of the clean furnace gas after filtration is 5mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 97%.
Embodiment 3
After embodiment 2 terminates, its equipment is directly adopted to proceed embodiment 3.3rd batch of 50 tons of compounds are added electric furnace 1 continuously react, meanwhile, switch to another refining kettle 501.By smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 300 DEG C.The every 600s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 187.5 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.6MPa.The dustiness of the clean furnace gas after filtration is 5mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 89%.
After embodiment 3 terminates; still be the inertia substitution gas of 187.5 DEG C by air feeder 303, well heater 304 and the second output tube 306 to implantation temperature in strainer 301, make sintering inorganic porous material filter core not occur to stick with paste fouling membrane under the protection of inertia substitution gas.
Second group of enforcement (adopting another set of equipment)
Embodiment 4
Employing transformer capacity is the large-scale self baking electrode phosphor furnace of 74750KVA.100 tons of compounds are added electric furnace 1 continuously react, simultaneously, start air feeder 303, well heater 304, high temperature inert preheating gas is by the second output tube 306, strainer 301 is entered from the furnace gas intake ducting to be filtered of strainer 301, thus the sintering inorganic porous material filter core (adopting FeAl intermetallic compound porous material filter core) in strainer 301 is preheated to 400 DEG C, then close the valve on the second output tube 306.After this, by smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 390 DEG C.The every 400s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 400 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.8MPa.The dustiness of the clean furnace gas after filtration is 6mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 97.5%.
Embodiment 5
After embodiment 4 terminates, its equipment is directly adopted to proceed embodiment 5.Second batch 100 tons of compounds are added electric furnace 1 continuously react, meanwhile, switch to another refining kettle 501.By smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 430 DEG C.The every 400s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 400 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.8MPa.The dustiness of the clean furnace gas after filtration is 6mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 98%.
Embodiment 6
After embodiment 5 terminates, its equipment is directly adopted to proceed embodiment 6.3rd batch of 100 tons of compounds are added electric furnace 1 continuously react, meanwhile, switch to another refining kettle 501.By smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 500 DEG C.The every 400s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 400 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.8MPa.The dustiness of the clean furnace gas after filtration is 6mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 98.5%.
Embodiment 7
After embodiment 6 terminates, its equipment is directly adopted to proceed embodiment 7.4th batch of 100 tons of compounds are added electric furnace 1 continuously react, meanwhile, switch to another refining kettle 501.By smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 550 DEG C.The every 400s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 400 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.8MPa.The dustiness of the clean furnace gas after filtration is 6mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 98%.
Embodiment 8
After embodiment 7 terminates, its equipment is directly adopted to proceed embodiment 8.5th batch of 100 tons of compounds are added electric furnace 1 continuously react, meanwhile, switch to another refining kettle 501.By smoke discharging pipe 2, the furnace gas of discharging from electric furnace 1 is imported dust-collecting system of flue 3, therebetween, heated by heat-exchanger rig 6 pairs of furnace gases.Carry out primary dust removing purification from first being entered mechanical dust-precipitator 302 by smoke discharging pipe 2 by the furnace gas after heating of discharging of electric furnace 1, and then enter in strainer 301 and carry out two-stage dust removal purification.The furnace gas intake ducting to be filtered of strainer 301 detects furnace gas temperature to be filtered and remains on about 620 DEG C.The every 400s of strainer 301 starts once online blowback, during blowback, the inertia purge gas that air feeder 303 exports is heated to 400 DEG C through well heater 304, and then by acting on sintering inorganic porous material filter core after 301c, Venturi meter 301b, the pressure of inertia purge gas is 0.8MPa.The dustiness of the clean furnace gas after filtration is 6mg/m
3left and right, after condensate recovery system 4, thick phosphorus enters in corresponding refining kettle 501, obtains yellow phosphorus product, does not almost produce mud phosphorus simultaneously, and dustiness in tail gas is extremely low.Calculating yellow phosphorus yield is 90%.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the application's method one, two.
Fig. 2 is the concrete structure schematic diagram of dynamo-electric stove in Fig. 1-mechanical dust-precipitator part.
Fig. 3 is the concrete structure schematic diagram of Fig. 1 middle filtrator part.
Claims (10)
1. phosphorus production method, the process procedure comprised has:
One, electrosmelting
The compound be made in proportion by Rock Phosphate (72Min BPL), silica and coke is sent into electric furnace (1), compound generation reduction reaction in electric furnace (1) generates furnace gas, furnace gas is from the effusion of reaction melting zone, and the impurity carried after the furnace gas filtering layer that stove internal upper part is formed by the compound of continuous supplementation in a part of compound is discharged from electric furnace (1); Described electric furnace (1) is multi-electrode phosphorus electric furnace;
Two, flue gas cleaning
The furnace gas will discharged from electric furnace (1) by smoke discharging pipe (2) imports dust-collecting system of flue (3), this dust-collecting system of flue (3) at least comprises the strainer (301) filtered for described furnace gas, this strainer (301) has the sintering inorganic porous material filter core meeting following working conditions, and the operation that should perform for this strainer (301) comprises:
The operation performed when 1. driving: inject inertia preheating gas in strainer (301), thus the sintering inorganic porous material filter core in strainer (301) is preheated to more than 187.5 DEG C;
The operation performed when 2. normally running: the furnace gas to be filtered remaining 187.5-280 DEG C to input temp in strainer (301), and the dustiness of clean furnace gas after filtering is 10-20mg/m
3below;
3. the operation performed during blowback: start the inertia purge gas that back-blowing device to implantation temperature in strainer (301) is more than 187.5 DEG C, the pressure-controlling of inertia purge gas is 0.2-1.0MPa;
The operation performed when 4. stopping: implantation temperature is the inertia substitution gas of more than 187.5 DEG C in strainer (301), makes sintering inorganic porous material filter core not occur to stick with paste fouling membrane under the protection of inertia substitution gas;
Three, receive phosphorus to refine
The clean furnace gas of being discharged by strainer (301) imports condensate recovery system (4), and condensed yellow phosphorus enters in receiving tank and is thick phosphorus, is then imported by thick phosphorus in thick phosphorus refining system (5) and refines, obtain yellow phosphorus product; Tail gas recycle utilizes or discharge;
In aforesaid method, by installing heat-exchanger rig (6) on described smoke discharging pipe (2) or/and the furnace gas filtering layer thickness described in adjustment electric furnace (1) or/and adjust electrode power thus the furnace gas temperature to be filtered passing into strainer (301) is remained 187.5-280 DEG C under the prerequisite of strictly carrying out compound process.
2. phosphorus production method as claimed in claim 1, is characterized in that: the dust removal installation of dust-collecting system of flue (3) is made up of described strainer (301) and the mechanical dust-precipitator (302) be positioned between strainer (301) and electric furnace (1); The furnace gas of discharging from electric furnace (1) is first entered mechanical dust-precipitator (302) by smoke discharging pipe (2) and carries out primary dust removing purification, and then enters in strainer (301) and carry out two-stage dust removal purification.
3. implement the claims the phosphorus production equipment of 1 method, comprise electric furnace (1), dust-collecting system of flue (3), condensate recovery system (4) and thick phosphorus refining system (5), electric furnace (1) is connected with dust-collecting system of flue (3) by smoke discharging pipe (2), described electric furnace (1) is multi-electrode phosphorus electric furnace, it is characterized in that: described dust-collecting system of flue (3) at least comprises the strainer (301) for filtering furnace gas, this strainer (301) has the sintering inorganic porous material filter core meeting following working conditions, the operation that should perform for this strainer (301) comprises:
The operation performed when 1. driving: inject inertia preheating gas in strainer (301), thus the sintering inorganic porous material filter core in strainer (301) is preheated to more than 187.5 DEG C;
The operation performed when 2. normally running: the furnace gas to be filtered remaining 187.5-280 DEG C to input temp in strainer (301), and the dustiness of clean furnace gas after filtering is 10-20mg/m
3below;
3. the operation performed during blowback: start the inertia purge gas that back-blowing device to implantation temperature in strainer (301) is more than 187.5 DEG C, the pressure-controlling of inertia purge gas is 0.2-1.0MPa;
The operation performed when 4. stopping: implantation temperature is the inertia substitution gas of more than 187.5 DEG C in strainer (301), makes sintering inorganic porous material filter core not occur to stick with paste fouling membrane under the protection of inertia substitution gas;
Wherein, by installing heat-exchanger rig (6) on described smoke discharging pipe (2) or/and the described furnace gas filtering layer thickness in adjustment electric furnace (1) or/and adjust electrode power thus the furnace gas temperature to be filtered passing into strainer (301) remained 187.5-280 DEG C under the prerequisite of strictly carrying out the process of electrosmelting compound.
4. phosphorus production equipment as claimed in claim 3, is characterized in that: the dust removal installation of dust-collecting system of flue (3) is made up of described strainer (301) and the mechanical dust-precipitator (302) be positioned between strainer (301) and electric furnace (1); The furnace gas of discharging from electric furnace (1) is first entered mechanical dust-precipitator (302) by smoke discharging pipe (2) and carries out primary dust removing purification, and then enters in strainer (301) and carry out two-stage dust removal purification.
5. phosphorus production equipment as claimed in claim 4, it is characterized in that: described mechanical dust-precipitator (302) comprises a tank body for dust settling, the top of this tank body is provided with the delivery port of gas after dust settling, place on the lower side, tank body top is provided with lower diffusion shell (302a), and the input aperture of lower diffusion shell (302a) is connected with the delivery port of described smoke discharging pipe (2).
6. phosphorus production equipment as claimed in claim 3, it is characterized in that: described smoke discharging pipe (2) has interconnective gas ascent stage (201) and gas downcomer (202), the entrance of gas ascent stage (201) is connected with electric furnace (1), and the outlet of gas downcomer (202) is connected with dust-collecting system of flue (3); Described heat-exchanger rig (6) is arranged on the pipeline section place, end of gas ascent stage (201), and the initiating terminal of gas downcomer (202) is connected to the side of this gas ascent stage (201) end pipeline section.
7. phosphorus production equipment as claimed in claim 6, is characterized in that: the main part of described gas downcomer (202) is the straight tube be obliquely installed horizontal by angle 10-40 °.
8. phosphorus production equipment as claimed in claim 3, it is characterized in that: the inlet air distribution device being provided with furnace gas to be filtered in described strainer (301), this inlet air distribution device comprise lower inlet duct (701) with many be connected with this lower inlet duct (701) respectively lead riser (702), the upper end of leading riser (702) is provided with venting port (703), and the height of described venting port (703) is arranged in more than the upper height of strainer (301) sintering inorganic porous material filter core (301a).
9. phosphorus production equipment as claimed in claim 8, is characterized in that: described lower inlet duct (701) comprises horizontally disposed ring pipe, and on this ring pipe, interval is furnished with and leads riser (702) described at least three.
10. as the phosphorus production equipment in claim 3 to 9 as described in any one claim, it is characterized in that: described inertia preheating gas, inertia purge gas and inertia substitution gas all come from same air feeder (303); The first output tube (305) and the second output tube (306) is connected respectively after this air feeder (303) heater via (304), the output terminal of the first output tube (305) connects back-blowing device, the output terminal of the second output tube (306) is connected on the furnace gas intake ducting to be filtered of strainer (301), and the first output tube (305) and the second output tube (306) are respectively arranged with valve.
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| CN104760941B (en) * | 2015-03-18 | 2017-09-15 | 贵州开磷集团股份有限公司 | A kind of preparation method of yellow phosphorus |
| CN105004192B (en) * | 2015-07-28 | 2017-06-13 | 成都易态科技有限公司 | Gas filter system and a kind of yellow phosphorus furnace gas filter method |
| CN110872128A (en) * | 2018-08-31 | 2020-03-10 | 贵州芭田生态工程有限公司 | Control phosphorite preparation system of component balance among phosphorite |
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