CN203700229U - Device for preparing refined anthracene and refined carbazole with anthracene oil as raw material - Google Patents
Device for preparing refined anthracene and refined carbazole with anthracene oil as raw material Download PDFInfo
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- CN203700229U CN203700229U CN201420039260.5U CN201420039260U CN203700229U CN 203700229 U CN203700229 U CN 203700229U CN 201420039260 U CN201420039260 U CN 201420039260U CN 203700229 U CN203700229 U CN 203700229U
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Abstract
The utility model belongs to the technical field of coal tar deep processing techniques in metallurgical coking industry, and particularly relates to a device for preparing refined anthracene and refined carbazole with anthracene oil as a raw material. The device is characterized by comprising a cooling concentration system, a rich anthracene oil prefractionation system, an anthracene phenanthrene crude fraction rectification system, a carbazole crude fraction rectification system, an anthracene phenanthrene narrow fraction washing and drying system, a carbazole narrow fraction washing and drying system and a solvent recovery system.According to the device, a light fraction, an anthracene phenanthrene crude fraction, a carbazole crude fraction and a heavy fraction are separated from a rich anthracene oil prefractionation device, the anthracene phenanthrene crude fraction and the carbazole crude fraction are refined in corresponding rectification devices to form an anthracene phenanthrene narrow fraction and a carbazole narrow fraction, and the anthracene phenanthrene narrow fraction and the carbazole narrow fraction are washed, separated and subjected to solid dryness in respective washing and drying devices to form a refined anthracene product and a refined carbazole product.The device is efficient, energy-saving, low in loss and environment-friendly.
Description
Technical field
The utility model belongs to metallurgical coking industry coal tar deep processing Technology field, especially relates to a kind of device take carbolineum as waste anthracene, smart carbazole.
Background technology
At present, the accurately machined main products of carbolineum is anthracene and smart carbazole, and physical separation method mainly contains solvent extration, solvent extraction-distillation method, distillation method, solvent extraction-distillation method-subliming method, crystallization-washing-distillation method etc.
Solvent extration is to utilize anthracene, phenanthrene and the carbazole different solubility in solvent, by operations such as heated scrub, crystallisation by cooling, centrifugings, easily dissolved component is dissolved in solvent, and Their Insoluble Components crystallizes out, and then each component is separated.This method due to use multi-solvents to crystallisate carry out several wash, cause a large amount of anthracenes and carbazole by dissolution with solvents after along with mother liquor runs off, cause product yield low; Because the structural shape of equipment makes the stopping property of equipment poor, and the very easy volatilization of solvent, in operating process, have a large amount of solvents and be dispersed in air, cause environmental pollution heavier, solvent loss amount is large; Meanwhile, also there is the shortcomings such as device processes ability is little, labour intensity is large.
Solvent extraction-distillation method is first carbolineum to be mixed with the circulating solvent that washing tower comes, and carry out entering washing tower after multistage crystallisation by cooling, at the bottom of tower, going out crystallisate, tower top flows out circulating solvent, circulating solvent is delivered to mixing tank and is mixed with carbolineum, and at the bottom of tower, isolated crystallisate repeats previous step after melting.Through repeatedly crystallization, washing, thawing, then mixture to be sent in flashing tower and carried out flash distillation, isolated cut is rectifying meticulously again, ties sheet packing after extraction finished product cut.The carbolineum of this method need to be through cooling, crystallization, crystallisate washing, crystallisate thaw process repeatedly, and its washing, crystallisation process and solvent extration are similar, by the same token, has that solvent-oil ratio is large, product yield is low and the problem such as environmental pollution; Meanwhile, owing to repeatedly heating up in operating process and lowering the temperature, cause the energy and power consumption to increase considerably.
The most representative distillation method is the reduced pressure distillation technique of French BEFS company, by the flash distillation processing to carbolineum and crude anthracene mixture, isolate rich carbolineum, rich carbolineum by with solvent after enter in crystallizer, isolate luxuriant and rich with fragrance oil by crystallisation by cooling, rich carbolineum after de-phenanthrene is sent in rectifying tower and is carried out rectifying separation, by side line extraction anthracene and smart carbazole cut.Aborning, because the content of anthracene in carbolineum and carbazole is very low, in the time of flash distillation, need to allocate crude anthracene into the anthracene in raising carbolineum and the content of carbazole, to reach the object that increases anthracene and carbazole content in the narrow fraction that flashes off, but the load that this has further increased equipment, causes the energy and power consumption in flash distillation and rectifying; Because the content of anthracene in cut and carbazole is not high, cause the content of product anthracene and smart carbazole not high; The energy and the power consumption purity of smart carbazole excessive and that produce is lower, is the major technique bottleneck of this method.
In " fuel and chemical industry " magazine 3 monthly magazines in 1999, " from crude anthracene, extracting the research of anthracene and smart carbazole " proposed the operational path of a kind of solvent extraction-component distillation-distillation, first this method is used light benzene solvent to wash 2 times crude anthracene, crude anthracene is purified and obtained half anthracene, then half anthracene is mixed and carries out azeotropic distillation with glycol ether, obtain containing the anthracene of anthracene 93.7% and the residue containing carbazole 66.5%.Re-use sublimation apparatus to carry out carbazole distillation operation containing the residue of carbazole, obtain the thick carbazole containing carbazole 88.4%, the carbazole content in residue is still up to 54.8%.Finally, use hot water repeatedly to wash anthracene, use hot water, dimethylbenzene to wash carbazole and recrystallization is produced the smart carbazole of content 90.7%.The technological process of this method is long and loaded down with trivial details, and required equipment is too much, from its data, can find out, because the factor such as washing repeatedly, the yield of product and purity are all undesirable; In still-process, need to use nonvariant boiling reagent, solvent loss amount is large; On washing plant adopts, also identical with common technique, inevitably there is environmental pollution and solvent loss problem.
Chinese invention patent application prospectus CN 103232318 A, disclose a kind of take a carbolineum as raw material production anthracene, the method of essence carbazole and luxuriant and rich with fragrance product, adopt crystallization-washing-distillation method, its operational path is for to proceed to stirring water cooler by a carbolineum, the slurries of cooling formation crystallization, the centrifugal rear isolated solid materials of slurries mixes in whizzer with solvent oil, then send into crystallization case Crystallization Separation, first the oil product that is rich in anthracene and carbazole that crystallization is gone out enters upgrading tower, the mixed fraction of extraction enters anthracene tower again, isolate anthracene cut, cut at the bottom of tower enters carbazole tower, isolate smart carbazole cut, cut send flaker granulation.This method adopts and uses hot solvent in whizzer and mixing of materials, and solvent loss is larger, and material and solvent insufficient, cause removing of impurity unclean; Washing process is placed on before rectification process, because the inventory of needs washing is many, makes the usage quantity of solvent large, and solvent loss increases, and in solvent Distillation recovery process, has also increased treatment capacity, and the energy and power consumption are increased; Simultaneously, owing to causing anthracene in crystallisate and the loss of carbazole in washing process, make originally further to reduce with regard to the content of the not high anthracene of content and carbazole in crystallisate, thereby increase the difficulty that distillation is processed, make the content of anthracene and carbazole in anthracene and smart carbazole cut reach higher, the stage number of the rectifying tower needing increases, and tower height increases, and equipment investment, the energy and power consumption are increased; Before distillation, wash, have a large amount of dissolvent residuals in crystallisate, make follow-up still-process need inventory to be processed to increase, inevitably increased the energy and power consumption.
Summary of the invention
The purpose of this utility model is to provide a kind of energy-efficient, low-loss, the eco-friendly device take carbolineum as waste anthracene, smart carbazole.
The purpose of this utility model realizes by following technical proposals:
Device take carbolineum as waste anthracene, smart carbazole of the present utility model, it is characterized in that comprising cooling concentration system, rich carbolineum fore-running system, the luxuriant and rich with fragrance thick cut distillation system of anthracene, the thick cut distillation system of carbazole, the luxuriant and rich with fragrance narrow fraction washing of anthracene, dehumidification system, the washing of carbazole narrow fraction, dehumidification system and solvent recovering system
Described cooling concentration system comprises thermal oil expansion slot, heat conduction oil groove, the Heat-transfer Oil Pump that heat conduction oil groove is connected therewith, Heat-transfer Oil Pump is connected therewith respectively hotline heater and thermal oil water cooler, stationary crystallization separator, stationary crystallization separator inlet is connected therewith carbolineum groove and carbolineum pump, the rich carbolineum groove being connected with described stationary crystallization separator outlet and rich carbolineum pump, the de-brilliant carbolineum groove being connected with told stationary crystallization separator and de-brilliant carbolineum pump, the vacuum pump and the vapor pipe that are connected with de-brilliant carbolineum groove
Described rich carbolineum fore-running system comprises the interchanger I being connected with described rich carbolineum pump, the primary tower being connected with interchanger I, be located at the primary tower water cooler of this primary tower tower top, be located at circulation extraction pump at the bottom of the primary tower tower at the bottom of this primary tower tower, the luxuriant and rich with fragrance thick cut side line extraction pump of anthracene, the thick cut side line of carbazole extraction pump and primary tower reboiler, at the bottom of described primary tower tower, recycle pump is connected with described interchanger I, described primary tower tower top side line extraction mouth is connected with described de-brilliant carbolineum groove, described primary tower tower top is connected with vacuum pump
The luxuriant and rich with fragrance thick cut distillation system of described anthracene comprises the anthracene tower being connected with the luxuriant and rich with fragrance thick cut side line extraction pump of described anthracene, be located at the anthracene tower cooler device of this anthracene column overhead, be located at circulation extraction pump at the bottom of the anthracene tower tower at the bottom of described anthracene tower tower, the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump, the interchanger II that the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump is connected therewith, anthracene tower tower bottom reboiler, at the bottom of described anthracene tower tower, circulation extraction pump is connected with described interchanger I, described anthracene column overhead side line extraction mouth is connected with described de-brilliant carbolineum groove, described anthracene column overhead is connected with vacuum pump
The thick cut distillation system of described carbazole comprises the carbazole tower being connected with the thick cut side line of described carbazole extraction pump, be located at the carbazole tower cooler device of this carbazole column overhead, be located at circulation extraction pump at the bottom of the carbazole tower tower at the bottom of described carbazole tower tower, carbazole narrow fraction side line extraction pump, the interchanger III that carbazole narrow fraction side line extraction pump is connected therewith, carbazole tower tower bottom reboiler, at the bottom of described carbazole tower tower, circulation extraction pump is connected with described interchanger I, described carbazole column overhead side line extraction mouth is connected with described de-brilliant carbolineum groove, described carbazole column overhead is connected with vacuum pump,
The luxuriant and rich with fragrance narrow fraction washing of described anthracene, dehumidification system comprise the luxuriant and rich with fragrance narrow fraction washing kettle of the anthracene being connected with described interchanger II, with the anthracene whizzer that the luxuriant and rich with fragrance narrow fraction washing kettle of anthracene is connected, the anthracene drying machine and the mother liquor tank that are connected with anthracene whizzer,
The described washing of carbazole narrow fraction, dehumidification system comprise the carbazole narrow fraction washing kettle being connected with described interchanger III, the smart carbazole whizzer being connected with carbazole narrow fraction washing kettle, and the smart carbazole drying machine and the mother liquor tank that are connected with smart carbazole whizzer,
Described solvent recovering system comprises solvent recovery tower, be located at the solvent tower water cooler of this solvent recuperation column overhead, be located at extraction pump at the bottom of the solvent recovery tower tower at the bottom of described solvent recovery tower tower, tower bottom reboiler, the interchanger IV being connected with solvent tower top side line extraction mouth, the solvent trough and the solvent pump that are connected with interchanger IV, the mother liquor tank and the mother liquor pump that are connected with described solvent recovery tower with interchanger III by interchanger II, at the bottom of described solvent recovery tower tower, extraction pump is connected with described interchanger I, described solvent recuperation column overhead is connected with described vacuum pump.
Described stationary crystallization separator comprises housing, be located at the overflow port of this case top, be located at the crystallization apparatus in described housing, the V-arrangement that the is arranged on lower housing portion groove that connects material, be arranged on the connect material material import and export of trench bottom of V-arrangement, described crystallization apparatus is made up of with the bottom crystallization apparatus that is arranged on bottom in housing the top crystallization apparatus that is arranged on housing internal upper part
Described crystallization apparatus is made up of with the bottom crystallization apparatus that is arranged on bottom in housing the top crystallization apparatus that is arranged on housing internal upper part,
Described top crystallization apparatus comprises the upper warp-wise pipe group that is horizontally set on housing internal upper part, go up therewith the upper broadwise pipe group that warp-wise pipe group horizontal stacking vertical interlaced arranges, go up therewith the cold and hot medium inlet house steward of upper warp-wise of the cold and hot medium inlet connection of broadwise pipe group, the cold and hot media outlet house steward of upper warp-wise who is connected with the cold and hot media outlet of described upper broadwise pipe group, the cold and hot medium inlet house steward of upper broadwise who is connected with the cold and hot medium inlet of described upper warp-wise pipe group, the cold and hot media outlet house steward of upper broadwise who is connected with the cold and hot media outlet of described upper warp-wise pipe group, the cold and hot medium inlet house steward of described upper broadwise is connected with the cold and hot medium input tube of cold and hot medium system respectively with the cold and hot medium inlet house steward of upper warp-wise, the cold and hot media outlet house steward of described upper warp-wise is connected with the cold and hot medium back flow pipe of cold and hot medium system respectively with the cold and hot media outlet house steward of upper broadwise,
Described bottom crystallization apparatus comprise horizontally disposed in housing the lower warp-wise pipe group of bottom, the lower broadwise pipe group of descending therewith warp-wise pipe group horizontal stacking vertical interlaced to arrange, the cold and hot medium inlet house steward of lower warp-wise who descends therewith the cold and hot medium inlet of broadwise pipe group to connect, the cold and hot media outlet house steward of lower warp-wise who is connected with the cold and hot media outlet of described lower broadwise pipe group, the cold and hot medium inlet house steward of lower broadwise who is connected with the cold and hot medium inlet of described lower warp-wise pipe group, the cold and hot media outlet house steward of lower broadwise who is connected with the cold and hot media outlet of described lower warp-wise pipe group, the cold and hot medium inlet house steward of described lower warp-wise is connected with the cold and hot medium input tube of cold and hot medium system with the cold and hot medium inlet house steward of lower broadwise, the cold and hot media outlet house steward of described lower warp-wise is connected with the cold and hot medium back flow pipe of cold and hot medium system with the cold and hot media outlet house steward of lower broadwise,
On the connect material top of groove of described V-arrangement, below lower crystallization apparatus, be provided with one group of filtration unit, be provided with material import and export in the described V-arrangement groove middle and lower part that connects material, be provided with warp-wise U-shaped pipe group and broadwise U-shaped pipe group at the described V-arrangement groove internal upper part that connects material, the cold and hot medium inlet of described warp-wise U-shaped pipe group and broadwise U-shaped pipe group is connected with the cold and hot medium inflow pipe of cold and hot medium system respectively, the cold and hot media outlet of described warp-wise U-shaped pipe group and broadwise U-shaped pipe group is connected with the cold and hot medium back flow pipe of cold and hot medium system respectively
Described filtration unit comprises that one group of top and bottom are arranged with the sleeve of rectangular aperture I, be located in this sleeve and top and bottom are arranged with the rotating cylinder of the rectangular aperture II that physical dimension is identical with rectangular aperture I, top in the rectangular aperture I of described sleeve is provided with ceramic membrane, the termination of described rotating cylinder be arranged on the connect material angle stroke performer of groove outside of V-arrangement and be connected.
The U-shaped pipe of described warp-wise U-shaped pipe group and described sleeve be staggered be arrangeding in parallel in same level, and the U-shaped pipe of described broadwise U-shaped pipe group is positioned at below described sleeve, and V-arrangement connects material above groove, and arrange with described sleeve horizontal vertical.
The quantity of the upper warp-wise pipe of described upper warp-wise pipe group and the lower warp-wise pipe of lower warp-wise pipe group is respectively 9～39.
The quantity of the upper broadwise pipe of described upper broadwise pipe group and the lower broadwise pipe of lower broadwise pipe group is respectively 6～32.
The quantity of the quantity of the U-shaped pipe of described warp-wise U-shaped pipe group and the U-shaped pipe of broadwise U-shaped pipe group is 3～15.
Described crystallization apparatus is 2～6 layers.
Advantage of the present utility model:
First carbolineum to be carried out to crystallization concentrated owing to adopting for the utility model, in the process of crystallization, adopt stationary crystallization separator, crystallization, separation once complete, replace traditional first stirred crystallization technique of centrifugation again, whole process is carried out in airtight space, there is no waste discharge, well solve problem of environmental pollution, simultaneously, owing to having adopted carbolineum chilling technique, in the cut that in crystallisate, the more traditional crystallization of the content of anthracene and carbazole or distillation method are obtained, the content of anthracene and carbazole is much higher, and the rate of recovery of anthracene, carbazole is high; The processing power of crystal separator is large, than adopting traditional crystallizer to reduce the quantity of required equipment, has reduced power consumption, has significantly reduced energy consumption compared with distilation method, has reduced the discharge of non-condensable gas, reduces environmental hazard; In the time of distillation, owing to there is no the solvent of the front wash residual of distillation, reduce material treatment capacity than traditional distillation method, save the energy; Fore-running extraction anthracene and carbazole narrow fraction, in cut, the content of anthracene and carbazole further improves, more respectively the narrow fraction after fore-running is carried out to rectifying, and in the smart carbazole cut of acquisition, carbazole content reaches the requirement of GB first grade; Finally, anthracene cut is washed with imurity-removal phenanthrene, because the inventory of needs washing is little, the solvent of use is few, and solvent loss is few, needs the mother liquor amount of regeneration recovery solvent few, and power and energy consumption are few.Efficient, energy-conservation, low-loss, environmental friendliness are really accomplished.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Fig. 2 is structural representation of the present utility model.
Fig. 3 is the vertical view of Fig. 2.
Fig. 4 is the A-A sectional view of Fig. 2 of the present utility model.
Fig. 5 is the schematic diagram of filtration unit of the present utility model.
Fig. 6 is the signal of the utility model filtration unit rotating cylinder.
The schematic diagram of Fig. 7 the utility model filtration unit sleeve.
Embodiment
Further illustrate embodiment of the present utility model below in conjunction with accompanying drawing.
As shown in Figure 1, device take carbolineum as waste anthracene, smart carbazole of the present utility model, it is characterized in that comprising carbolineum cooling concentration system, rich carbolineum fore-running system, the luxuriant and rich with fragrance thick cut distillation system of anthracene, the thick cut distillation system of carbazole, the luxuriant and rich with fragrance narrow fraction washing of anthracene, dehumidification system, the washing of carbazole narrow fraction, dehumidification system and solvent recovering system
Described carbolineum cooling concentration system comprises thermal oil expansion slot 1, heat conduction oil groove 5, the Heat-transfer Oil Pump 6 that heat conduction oil groove 5 is connected therewith, Heat-transfer Oil Pump 6 is connected therewith respectively hotline heater 3 and thermal oil water cooler 4, stationary crystallization separator 2, the carbolineum groove 7 that stationary crystallization separator 2 material import and exports are connected therewith, the carbolineum pump 8 being connected with carbolineum groove 7, the rich carbolineum groove 9 being connected with described stationary crystallization separator 2 material import and exports, the rich carbolineum pump 10 being connected with rich carbolineum groove 9, the de-brilliant carbolineum groove 17 being connected with described stationary crystallization separator 2 material import and exports and de-brilliant carbolineum pump 18, the vacuum pump 12 and the exhaust tank 11 that are connected with de-brilliant carbolineum groove 17,
Described rich carbolineum fore-running system comprises the interchanger I 14 being connected with described rich carbolineum pump 10, the primary tower 15 being connected with interchanger I 14, be located at the primary tower water cooler 13 of these primary tower 15 tower tops, be located at circulation extraction pump 19 at the bottom of the primary tower tower at the bottom of these primary tower 13 towers, the luxuriant and rich with fragrance thick cut side line extraction pump 21 of anthracene, the thick cut side line of carbazole extraction pump 20 and primary tower reboiler 16, at the bottom of described primary tower tower, circulation extraction pump 19 is connected with described interchanger I 14, described primary tower 15 tower top side line extraction mouths are connected with described de-brilliant carbolineum groove 17, described primary tower 15 tower tops are connected with vacuum pump 12,
The luxuriant and rich with fragrance thick cut distillation system of described anthracene comprises the anthracene tower 23 being connected with the luxuriant and rich with fragrance thick cut side line extraction pump 21 of described anthracene, be located at the anthracene tower cooler device 24 of these anthracene tower 23 tower tops, be located at circulation extraction pump 25 at the bottom of the anthracene tower tower at the bottom of described anthracene tower 23 towers, the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump 26, the interchanger II 27 that the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump 26 is connected therewith, anthracene tower tower bottom reboiler 22, at the bottom of described anthracene tower tower, circulation extraction pump 25 is connected with described interchanger I 14, described anthracene tower 23 tower top side line extraction mouths are connected with described de-brilliant carbolineum groove 17, described anthracene tower 23 tower tops are connected with vacuum pump 12,
The thick cut distillation system of described carbazole comprises the carbazole tower 29 being connected with the thick cut side line of described carbazole extraction pump 20, be located at the carbazole tower cooler device 28 of these carbazole tower 29 tower tops, be located at circulation extraction pump 31 at the bottom of the carbazole tower tower at the bottom of described carbazole tower 29 towers, carbazole narrow fraction side line extraction pump 32, carbazole heats up in a steamer the interchanger III 33 that narrow point of side line extraction pump 32 is connected therewith, carbazole tower tower bottom reboiler 30, at the bottom of described carbazole tower tower, circulation extraction pump 31 is connected with described interchanger I 14, described carbazole tower 29 tower top side line extraction mouths are connected with described de-brilliant carbolineum groove 17, described carbazole tower 29 tower tops are connected with vacuum pump 12,
The luxuriant and rich with fragrance narrow fraction washing of described anthracene, dehumidification system comprise the luxuriant and rich with fragrance narrow fraction washing kettle 34 of the anthracene being connected with described interchanger II 27, the anthracene whizzer 35 being connected with the luxuriant and rich with fragrance narrow fraction washing kettle 34 of anthracene, the anthracene drying machine 36 being connected with anthracene whizzer 35 and mother liquor tank 37
The described washing of carbazole narrow fraction, dehumidification system comprise the carbazole narrow fraction washing kettle 39 being connected with described interchanger III 33, the smart carbazole whizzer 40 being connected with carbazole narrow fraction washing kettle 39, the smart carbazole drying machine 41 and the mother liquor tank 37 that are connected with smart carbazole whizzer 40
Described solvent recovering system comprises solvent recovery tower 44, be located at the solvent tower water cooler 45 of described solvent recovery tower 44 tower tops, be located at extraction pump 42 at the bottom of the solvent recovery tower tower at the bottom of described solvent recovery tower 44 towers, tower bottom reboiler 43, the solvent tower top aftercooler 46 being connected with solvent tower top side line extraction mouth, the solvent trough 47 and the solvent pump 48 that are connected with solvent tower top aftercooler 46, the mother liquor tank 37 and the mother liquor pump 38 that are connected with described solvent recovery tower 44 with interchanger III 33 by interchanger II 27, at the bottom of described solvent recovery tower tower, extraction pump 42 is connected with described interchanger I 14, described solvent recovery tower 44 tower tops are connected with described vacuum pump 12.
As shown in Figure 2 to 7, stationary crystallization separator described in the utility model, comprises housing 2-5, is located at the overflow port 2-1 at this housing 2-5 top, is located at the crystallization apparatus in described housing 2-5, and the V-arrangement that the is arranged on housing 2-5 bottom groove 2-7 that connects material, is characterized in that:
Described crystallization apparatus is made up of with the bottom crystallization apparatus that is arranged on bottom in housing 2-5 the top crystallization apparatus that is arranged on housing 2-5 internal upper part,
Described top crystallization apparatus comprises the upper warp-wise pipe group 2-17 that is horizontally set on housing internal upper part, go up therewith the upper broadwise pipe group 2-16 that warp-wise pipe group 2-17 horizontal stacking vertical interlaced arranges, the cold and hot medium inlet of the upper warp-wise house steward 2-14 being connected with the cold and hot medium 2-16 entrance of described upper broadwise pipe group, the cold and hot media outlet house steward of the upper warp-wise 2-3 being connected with the cold and hot media outlet of described upper broadwise pipe group 2-16, the cold and hot medium inlet of the upper broadwise house steward 2-15 being connected with the cold and hot medium inlet of described upper warp-wise pipe group 2-17, the cold and hot media outlet house steward of the upper broadwise 2-2 being connected with the cold and hot media outlet of described upper warp-wise pipe group 2-17, the described cold and hot medium inlet of upper broadwise house steward 2-15 is connected with the cold and hot medium input tube of cold and hot medium system respectively with the cold and hot medium inlet of upper warp-wise house steward 2-14, the described cold and hot media outlet house steward of upper warp-wise 2-3 is connected with the cold and hot medium back flow pipe of cold and hot medium system respectively with the cold and hot media outlet house steward of upper broadwise 2-2.
Bottom described in the utility model crystallization apparatus comprise horizontally disposed in housing the lower warp-wise pipe group 2-10 of bottom, the lower broadwise pipe group 2-13 that descends therewith warp-wise pipe group 2-10 horizontal stacking vertical interlaced to arrange, the cold and hot medium inlet of the lower warp-wise house steward 2-11 that descends therewith the cold and hot medium inlet of broadwise pipe group 2-13 to connect, the cold and hot media outlet house steward of the lower warp-wise 2-18 being connected with the cold and hot media outlet of described lower broadwise pipe group 2-13, the cold and hot medium inlet of the lower broadwise house steward 2-12 being connected with the cold and hot medium inlet of described lower warp-wise pipe group 2-10, the cold and hot media outlet house steward of the lower broadwise 2-4 being connected with the cold and hot media outlet of described lower warp-wise pipe group 2-10, the described cold and hot medium inlet of lower warp-wise house steward 2-11 is connected with the hotline heater 3 of heat-conducting oil system and the thermal oil outlet pipe of thermal oil water cooler 4 with lower broadwise cold and hot medium inlet house steward 2-12, described lower warp-wise outlet header 2-18 and lower broadwise outlet header 2-4 are connected with the thermal oil entrance of the heat conduction oil groove 5 of heat-conducting oil system respectively.
The setting of upper and lower two crystallization apparatus, has improved cooling (heating) effect of material effectively, has improved working efficiency.
The utility model is on the connect material top of groove 2-7 of described V-arrangement, below lower crystallization apparatus, be provided with one group of filtration unit 2-6, be provided with material import and export 2-8 in the described V-arrangement groove 2-7 middle and lower part that connects material, be provided with warp-wise U-shaped pipe group 2-9-I and broadwise U-shaped pipe group 2-9 II at the described V-arrangement groove 2-7 internal upper part that connects material, the cold and hot medium inlet of described warp-wise U-shaped pipe group 2-9-I and broadwise U-shaped pipe group 2-9-II is connected with the hotline heater 3 of heat-conducting oil system and the thermal oil outlet pipe of thermal oil water cooler 4 respectively, the cold and hot media outlet of described warp-wise U-shaped pipe group 2-9-I and broadwise U-shaped pipe group 2-9-II is connected with the thermal oil entrance of the heat conduction oil groove 5 of heat-conducting oil system respectively.
As shown in Fig. 5, Fig. 6 and Fig. 7, filtration unit 2-6 described in the utility model comprises that one group of top and bottom are arranged with the sleeve 2-6-2 of rectangular aperture I 2-6-1, be located in this sleeve 2-6-2 and top and bottom are arranged with the rotating cylinder 2-6-3 of the rectangular aperture II 2-6-4 that physical dimension is identical with rectangular aperture I 2-6-1, top at the rectangular aperture I 2-6-1 of described sleeve 2-6-2 is provided with ceramic membrane 2-6-5, the termination 2-6-6 of described rotating cylinder 2-6-3 be arranged on the connect material angle stroke performer of groove 2-7 outside of V-arrangement and be connected.The setting of filtration unit 2-6, has guaranteed that crystallisate separates with the smooth of mother liquor, and well having solved other crystallizers will contain the solidliquid mixture of crystallisate, puts into the danger that causes pipeline obstruction when another separating device carries out solid-liquid separation.
The U-shaped pipe of warp-wise U-shaped pipe group 2-9-I described in the utility model and described sleeve be staggered be arrangeding in parallel at grade, and the U-shaped pipe of described broadwise U-shaped pipe group 2-9-II is positioned at below described sleeve, and arrange with described sleeve horizontal vertical.The quantity of the U-shaped pipe of described warp-wise U-shaped pipe group 2-9-I and the U-shaped pipe of broadwise U-shaped pipe group 2-9-II is respectively 3～15.
The quantity of the preferred upper warp-wise pipe quantity of upper warp-wise pipe group 2-17 described in the utility model and the lower warp-wise pipe of lower warp-wise pipe group 2-10 is respectively 9～39.
The preferred quantity of upper broadwise pipe of upper broadwise pipe group 2-16 described in the utility model and the quantity of the lower broadwise pipe of lower broadwise pipe group 2-13 are respectively 6～32.
Crystallization apparatus described in the utility model, can arrange 2～6 layers according to the treatment capacity of material.
The principle of work of stationary crystallization separator is:
In the time carrying out crystallization operation, start angle stroke performer (market can have been bought), driven rotary cylinder 2-6-3 rotates, and makes rectangular aperture II 2-6-4 become coincidence status with rectangular aperture I 2-6-1, and passage is opened, carbolineum is entered in stationary crystallization separator by material import and export 2-7, after charging finishes, start angle stroke performer, driven rotary cylinder 2-6-3 rotates, make rectangular aperture II 2-6-4 become plumbness, pathway closure with rectangular aperture I 2-6-1, open the inlet valve of thermal oil water cooler 4, close the inlet valve of hotline heater 3, start Heat-transfer Oil Pump 6, thermal oil in heat conduction oil groove 5 is delivered in thermal oil water cooler 4, the cold thermal oil that self-conductance hot oil cooler 4 thermal oils export is out by cold, thermal conductance deep fat input tube is first by lower broadwise entrance house steward 2-12, lower warp-wise entrance house steward 2-11, upper broadwise entrance house steward 2-15 and upper warp-wise entrance house steward 2-14, U-shaped pipe group entrance 2-9-1 and 2-9-2 etc. are cold, thermal medium flows into pipe and enters, enter respectively again in warp-wise pipe group 2-17 in each warp-wise pipe, in each broadwise pipe in upper broadwise pipe group 2-16, in each broadwise pipe in each warp-wise pipe in lower warp-wise pipe group 2-10 and in lower broadwise pipe group 2-13, again respectively by upper warp-wise outlet header 2-3, upper broadwise outlet header 2-2, lower broadwise outlet header 2-4 and lower warp-wise outlet header 2-18, U-shaped pipe group outlet 2-9-3 and 2-9-4 etc. are cold, thermal medium flows out pipe outflow and enters heat conduction oil groove 5, carbolineum is carried out to crystallisation by cooling, after crystallisation process finishes, start angle stroke performer, driven rotary cylinder 2-7-3 rotates, rectangular aperture II 2-7-4 is overlapped with rectangular aperture I 2-7-1, crystallisate in stationary crystallization separator is separated with mother liquor, mother liquor flows out from material import and export 2-8 after entering the mother liquor collector 2-19 bottom stationary crystallization separator, after separation completes, open the inlet valve of hotline heater 3, close the inlet valve of thermal oil water cooler 4, the thermal oil in heat conduction oil groove 5 is delivered to thermal oil and add but in device 3, the thermal conductance deep fat that exports out from hotline heater 3 thermal oils is by cold, thermal conductance deep fat input tube is first by lower broadwise entrance house steward 2-12, lower warp-wise entrance house steward 2-11, upper broadwise entrance house steward 2-15 and upper warp-wise entrance house steward 2-14, U-shaped pipe group entrance 2-9-1 and 2-9-2 etc. are cold, thermal medium flows into pipe and enters, then enters respectively in warp-wise pipe group 2-17 in each warp-wise pipe, in each broadwise pipe in upper broadwise pipe group 2-16, in each broadwise pipe in each warp-wise pipe in lower warp-wise pipe group 2-10 and in lower broadwise pipe group 2-13, more respectively by upper warp-wise outlet header 2-3, upper broadwise outlet header 2-2, lower broadwise outlet header 2-4 and lower warp-wise outlet header 2-18, U-shaped pipe group outlet 2-9-3 and 2-9-4 etc. are cold, thermal medium flows out pipe and flows out, and crystallisate is carried out to temperature raising thawing, and the crystallisate after thawing is flowed out and entered heat conduction oil groove 5 by material import and export 2-8.
Device take carbolineum as waste anthracene, smart carbazole of the present utility model, use stationary crystallization separator 2 to carry out separating of crystallization and crystallisate and mother liquor to carbolineum, then crystallisate, after melting, enters primary tower 15 predistillations and separates, the luxuriant and rich with fragrance thick cut of extraction anthracene and the thick cut of carbazole; The luxuriant and rich with fragrance thick cut of anthracene is sent into anthracene tower 23, and after 23 rectifying of anthracene tower, the luxuriant and rich with fragrance narrow fraction of the anthracene of extraction and solvent be mixing, washing in the luxuriant and rich with fragrance narrow fraction washing kettle of anthracene, wash rear crystallisation by cooling, use anthracene whizzer 35 to carry out solid-liquid separation, produce anthracene, its anthracene content is more than 97%; The thick cut of carbazole is sent into carbazole tower 29, after 29 rectifying of carbazole tower, extraction content is that 93%～95% carbazole narrow fraction and solvent are at carbazole narrow fraction washing kettle 39 interior mixing, washings, wash rear crystallisation by cooling, use smart carbazole whizzer 40 to carry out solid-liquid separation, produce smart carbazole, its carbazole content is 97～99%.
Concrete steps are as follows:
Start angle stroke performer (market can have been bought), driven rotary cylinder 2-7-3 rotates, make rectangular aperture II 2-7-4 become coincidence status with rectangular aperture I 2-7-1, passage is opened, and carbolineum is entered in stationary crystallization separator by material import and export 2-8, after charging finishes, start angle stroke performer, driven rotary cylinder 2-7-3 rotates, and makes rectangular aperture II 2-7-4 become plumbness, pathway closure with rectangular aperture I 2-7-1, open the inlet valve of thermal oil water cooler 4, close the inlet valve of hotline heater 3, start Heat-transfer Oil Pump 6, thermal oil in heat conduction oil groove 5 is delivered in thermal oil water cooler 4, the cold thermal oil that self-conductance hot oil cooler 4 thermal oils export is out by cold, thermal conductance deep fat input tube is first by lower broadwise entrance house steward 2-12, lower warp-wise entrance house steward 2-11, upper broadwise entrance house steward 2-15 and upper warp-wise entrance house steward 2-14, U-shaped pipe group entrance 2-9-1 and 2-9-2 etc. are cold, thermal medium flows into pipe and enters, enter respectively again in warp-wise pipe group 2-17 in each warp-wise pipe, in each broadwise pipe in upper broadwise pipe group 2-16, in each broadwise pipe in each warp-wise pipe in lower warp-wise pipe group 2-10 and in lower broadwise pipe group 2-13, again respectively by upper warp-wise outlet header 2-3, upper broadwise outlet header 2-2, lower broadwise outlet header 2-4 and lower warp-wise outlet header 2-18, U-shaped pipe group outlet 2-9-3 and 2-9-4 etc. are cold, thermal medium flows out pipe outflow and enters heat conduction oil groove 5, carbolineum is cooled to 20 ℃, keep this Tc 6 hours, crystallisation process finishes, start angle stroke performer, driven rotary cylinder 2-7-3 rotates, rectangular aperture II 2-7-4 is overlapped with rectangular aperture I 2-7-1, start vacuum pump 12, crystallisate in stationary crystallization separator and mother liquor are carried out to suction filtration, separate, mother liquor flows out from material import and export 2-8 after entering the mother liquor collector 2-19 bottom stationary crystallization separator, after separation completes, close the vacuum pipe valve being connected with stationary crystallization separator 2, open the inlet valve of hotline heater 3, close the inlet valve of thermal oil water cooler 4, thermal oil in heat conduction oil groove 5 is delivered in hotline heater 3, the thermal conductance deep fat that exports out from hotline heater 3 thermal oils is by cold, thermal conductance deep fat input tube is first by lower broadwise entrance house steward 2-12, lower warp-wise entrance house steward 2-11, upper broadwise entrance house steward 2-15 and upper warp-wise entrance house steward 2-14, U-shaped pipe group entrance 2-9-1 and 2-9-2 etc. are cold, thermal medium flows into pipe and enters, enter respectively again in warp-wise pipe group 2-17 in each warp-wise pipe, in each broadwise pipe in upper broadwise pipe group 2-16, in each broadwise pipe in each warp-wise pipe in lower warp-wise pipe group 2-10 and in lower broadwise pipe group 2-13, again respectively by upper warp-wise outlet header 2-3, upper broadwise outlet header 2-2, lower broadwise outlet header 2-4 and lower warp-wise outlet header 2-18, U-shaped pipe group outlet 2-9-3 and 2-9-4 etc. are cold, thermal medium flows out pipe outflow and enters heat conduction oil groove 5, rich carbolineum in stationary crystallization separator 2 is heated and is warmed up to 80 ℃, rich carbolineum in stationary crystallization separator 2 is melted, rich carbolineum after thawing enters into rich carbolineum groove 9 and stores, rich carbolineum from rich carbolineum groove 9 is sent through rich carbolineum pump 10, by after interchanger I 14 and last running heat exchange to 250 from extraction at the bottom of primary tower 15, anthracene tower 23, carbazole tower 29,44 4 tower towers of solvent recovery tower ℃, enters and in primary tower 15, carries out rectifying, tower top pressure maintenance-the 85KPa of primary tower 15, trim the top of column mode is internal reflux, tower top side line extraction lighting end enters de-brilliant carbolineum groove 17, tower top side line is at the luxuriant and rich with fragrance thick cut of 240～265 ℃ of extraction anthracenes, the luxuriant and rich with fragrance thick cut of the anthracene of extraction is sent into and in anthracene tower 23, is carried out rectifying through the luxuriant and rich with fragrance thick cut side line extraction pump 21 of anthracene, primary tower 15 bottom side lines are at 265～290 ℃ of thick cuts of extraction carbazole, the thick cut of carbazole of extraction is sent into and in carbazole tower 29, is carried out rectifying through the thick cut side line of carbazole extraction pump 20, at the bottom of primary tower 15 towers, the last running of extraction is after circulation extraction pump 19 at the bottom of primary tower 15 towers is sent into interchanger I 14 and lowered the temperature from the rich carbolineum heat exchange of rich carbolineum groove 9, enter in de-brilliant carbolineum groove 17, anthracene tower 23 tower top pressure maintenance-85KPa, reflux type is internal reflux, after the luxuriant and rich with fragrance thick cut rectifying of anthracene in tower, overhead extraction lighting end enters de-brilliant carbolineum groove 17, tower middle part side line is at the luxuriant and rich with fragrance narrow fraction of 240～265 ℃ of extraction anthracenes, the luxuriant and rich with fragrance narrow fraction of anthracene of extraction is after the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump 26 is sent into interchanger II 27 and lowered the temperature from the mother liquor heat exchange in mother liquor tank 37, enter into the luxuriant and rich with fragrance narrow fraction washing kettle 34 of anthracene, at the bottom of tower, the last running of extraction is after circulation extraction pump 25 at the bottom of anthracene tower 23 towers is sent into interchanger I 14 and lowered the temperature from the rich carbolineum heat exchange of rich carbolineum groove 9, enter in de-brilliant carbolineum groove 17, carbazole tower 29 tower top pressure maintenance-85KPa, reflux type is internal reflux, after the thick cut rectifying of carbazole in tower, tower top side line extraction lighting end enters de-brilliant carbolineum groove 17, tower middle part side line is at 265～290 ℃ of extraction carbazole narrow fractions, send into interchanger III 33 through carbazole narrow fraction side line extraction pump 32, after lowering the temperature with the mother liquor heat exchange from interchanger II 27, enter into carbazole narrow fraction washing kettle 39, at the bottom of tower, the last running of extraction is after circulation extraction pump 31 at the bottom of carbazole tower 29 towers is sent into interchanger I 14 and lowered the temperature from the rich carbolineum heat exchange of rich carbolineum groove 9, enter in de-brilliant carbolineum groove 17, the luxuriant and rich with fragrance narrow fraction of anthracene in the luxuriant and rich with fragrance narrow fraction washing kettle 34 of anthracene with the solvent from solvent trough 47 in anthracene phenanthrene narrow fraction 34 interior mixing of washing kettle, the proportioning of the luxuriant and rich with fragrance narrow fraction of solvent and anthracene is 1～2:1, pass into water coolant through fully stirring in the luxuriant and rich with fragrance narrow fraction washing kettle of backward anthracene 34 chucks, carry out crystallisation by cooling operation, after crystallization is qualified, solidliquid mixture is put into 35 centrifugations of anthracene whizzer, the isolated mother liquor of anthracene whizzer 35 enters in mother liquor tank 37, and the isolated solids of anthracene whizzer 35 is sent into dry rear packing in anthracene drying machine 36, carbazole narrow fraction in carbazole narrow fraction washing kettle 39 with the solvent from solvent trough 47 in 34 interior mixing of carbazole narrow fraction washing kettle, the proportioning of solvent and carbazole narrow fraction is 1～2:1, through fully stirring in backward carbazole narrow fraction washing kettle 39 chucks and pass into water coolant, carry out crystallisation by cooling operation, after crystallization is qualified, solidliquid mixture is put into smart carbazole whizzer 40 centrifugations, essence carbazole whizzer 40 isolated mother liquors enter in mother liquor tank 37, and the isolated solids of smart carbazole whizzer 40 is sent into dry rear packing in smart carbazole drying machine 41, mother liquor from mother liquor tank 37 is sent through mother liquor pump 38, be warmed up to after 150 ℃ with the last running heat exchange of extraction at the bottom of anthracene tower 23 and carbazole tower 29 towers by interchanger II 27 and interchanger III 33, enter in solvent recovery tower 44 and distill, reflux type is internal reflux, the solvent of overhead extraction enters the interior recycling of solvent trough 47 through solvent tower top water cooler 45 and solvent tower top aftercooler 46 after cooling, and at the bottom of solvent tower 44 towers, the last running of extraction enters into de-brilliant carbolineum groove 17 after extraction pump 42 at the bottom of solvent tower 44 towers is sent into interchanger I 14 and rich carbolineum heat exchange cooling.
First carbolineum to be carried out to crystallization concentrated owing to adopting for the utility model, in the process of crystallization, adopt stationary crystallization separator, Crystallization Separation once completes, replace traditional first stirred crystallization technique of centrifugation again, whole process is carried out in airtight space, there is no waste discharge, well solve problem of environmental pollution, simultaneously, owing to having adopted carbolineum chilling technique, in the cut that in crystallisate, the more traditional crystallization of the content of anthracene and carbazole or distillation method are obtained, the content of anthracene and carbazole is much higher, and the rate of recovery of anthracene, carbazole is high; The processing power of crystal separator is large, than adopting traditional crystallizer to reduce the quantity of required equipment, has reduced power consumption, has significantly reduced energy consumption compared with distilation method, has reduced the discharge of non-condensable gas, reduces environmental hazard; In the time of distillation, owing to there is no the solvent of the front wash residual of distillation, reduce material treatment capacity than traditional distillation method, save the energy; Fore-running extraction anthracene and carbazole narrow fraction, in cut, the content of anthracene and carbazole further improves, more respectively the narrow fraction after fore-running is carried out to rectifying, and in the smart carbazole cut of acquisition, carbazole content reaches the requirement of GB first grade; Finally, anthracene cut is washed with imurity-removal phenanthrene, because the inventory of needs washing is little, the solvent of use is few, and solvent loss is few, needs the mother liquor amount of regeneration recovery solvent few, and power and energy consumption are few.Efficient, energy-conservation, low-loss, environmental friendliness are really accomplished.
Claims (7)
1. the device take carbolineum as waste anthracene, smart carbazole, it is characterized in that comprising cooling concentration system, rich carbolineum fore-running system, the luxuriant and rich with fragrance thick cut distillation system of anthracene, the thick cut distillation system of carbazole, the luxuriant and rich with fragrance narrow fraction washing of anthracene, dehumidification system, the washing of carbazole narrow fraction, dehumidification system and solvent recovering system
Described cooling concentration system comprises thermal oil expansion slot, heat conduction oil groove, the Heat-transfer Oil Pump that heat conduction oil groove is connected therewith, Heat-transfer Oil Pump is connected therewith respectively hotline heater and thermal oil water cooler, stationary crystallization separator, stationary crystallization separator inlet is connected therewith carbolineum groove and carbolineum pump, the rich carbolineum groove being connected with described stationary crystallization separator outlet and rich carbolineum pump, the de-brilliant carbolineum groove being connected with described stationary crystallization separator and de-brilliant carbolineum pump, the vacuum pump and the vapor pipe that are connected with de-brilliant carbolineum groove
Described rich carbolineum fore-running system comprises the interchanger I being connected with described rich carbolineum pump, the primary tower being connected with interchanger I, be located at the primary tower water cooler of this primary tower tower top, be located at circulation extraction pump at the bottom of the primary tower tower at the bottom of this primary tower tower, the luxuriant and rich with fragrance thick cut side line extraction pump of anthracene, the thick cut side line of carbazole extraction pump and primary tower reboiler, at the bottom of described primary tower tower, recycle pump is connected with described interchanger I, described primary tower tower top side line extraction mouth is connected with described de-brilliant carbolineum groove, described primary tower tower top is connected with vacuum pump
The luxuriant and rich with fragrance thick cut distillation system of described anthracene comprises the anthracene tower being connected with the luxuriant and rich with fragrance thick cut side line extraction pump of described anthracene, be located at the anthracene tower cooler device of this anthracene column overhead, be located at circulation extraction pump at the bottom of the anthracene tower tower at the bottom of described anthracene tower tower, the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump, the interchanger II that the luxuriant and rich with fragrance narrow fraction side line of anthracene extraction pump is connected therewith, anthracene tower tower bottom reboiler, at the bottom of described anthracene tower tower, circulation extraction pump is connected with described interchanger I, described anthracene column overhead side line extraction mouth is connected with described de-brilliant carbolineum groove, described anthracene column overhead is connected with vacuum pump
The thick cut distillation system of described carbazole comprises the carbazole tower being connected with the thick cut side line of described carbazole extraction pump, be located at the carbazole tower cooler device of this carbazole column overhead, be located at circulation extraction pump at the bottom of the carbazole tower tower at the bottom of described carbazole tower tower, carbazole narrow fraction side line extraction pump, the interchanger III that carbazole narrow fraction side line extraction pump is connected therewith, carbazole tower tower bottom reboiler, at the bottom of described carbazole tower tower, circulation extraction pump is connected with described interchanger I, described carbazole column overhead side line extraction mouth is connected with described de-brilliant carbolineum groove, described carbazole column overhead is connected with vacuum pump,
The luxuriant and rich with fragrance narrow fraction washing of described anthracene, dehumidification system comprise the luxuriant and rich with fragrance narrow fraction washing kettle of the anthracene being connected with described interchanger II, with the anthracene whizzer that the luxuriant and rich with fragrance narrow fraction washing kettle of anthracene is connected, the anthracene drying machine and the mother liquor tank that are connected with anthracene whizzer,
The described washing of carbazole narrow fraction, dehumidification system comprise the carbazole narrow fraction washing kettle being connected with described interchanger III, the smart carbazole whizzer being connected with carbazole narrow fraction washing kettle, and the smart carbazole drying machine and the mother liquor tank that are connected with smart carbazole whizzer,
Described solvent recovering system comprises solvent recovery tower, be located at the solvent tower water cooler of this solvent recuperation column overhead, be located at extraction pump at the bottom of the solvent recovery tower tower at the bottom of described solvent recovery tower tower, tower bottom reboiler, the interchanger IV being connected with solvent tower top side line extraction mouth, the solvent trough and the solvent pump that are connected with interchanger IV, the mother liquor tank and the mother liquor pump that are connected with described solvent recovery tower with interchanger III by interchanger II, at the bottom of described solvent recovery tower tower, extraction pump is connected with described interchanger I, described solvent recuperation column overhead is connected with described vacuum pump.
2. the device take carbolineum as waste anthracene, smart carbazole according to claim 1, it is characterized in that described stationary crystallization separator comprises housing, be located at the overflow port of this case top, be located at the crystallization apparatus in described housing, the V-arrangement that the is arranged on lower housing portion groove that connects material, be arranged on the connect material material import and export of trench bottom of V-arrangement, described crystallization apparatus is made up of the bottom crystallization apparatus that is arranged on the top crystallization apparatus of housing internal upper part and is arranged on bottom in housing
Described crystallization apparatus is made up of with the bottom crystallization apparatus that is arranged on bottom in housing the top crystallization apparatus that is arranged on housing internal upper part,
Described top crystallization apparatus comprises the upper warp-wise pipe group that is horizontally set on housing internal upper part, go up therewith the upper broadwise pipe group that warp-wise pipe group horizontal stacking vertical interlaced arranges, go up therewith the cold and hot medium inlet house steward of upper warp-wise of the cold and hot medium inlet connection of broadwise pipe group, the cold and hot media outlet house steward of upper warp-wise who is connected with the cold and hot media outlet of described upper broadwise pipe group, the cold and hot medium inlet house steward of upper broadwise who is connected with the cold and hot medium inlet of described upper warp-wise pipe group, the cold and hot media outlet house steward of upper broadwise who is connected with the cold and hot media outlet of described upper warp-wise pipe group, the cold and hot medium inlet house steward of described upper broadwise is connected with the cold and hot medium input tube of cold and hot medium system respectively with the cold and hot medium inlet house steward of upper warp-wise, the cold and hot media outlet house steward of described upper warp-wise is connected with the cold and hot medium back flow pipe of cold and hot medium system respectively with the cold and hot media outlet house steward of upper broadwise,
Described bottom crystallization apparatus comprise horizontally disposed in housing the lower warp-wise pipe group of bottom, the lower broadwise pipe group of descending therewith warp-wise pipe group horizontal stacking vertical interlaced to arrange, the cold and hot medium inlet house steward of lower warp-wise who descends therewith the cold and hot medium inlet of broadwise pipe group to connect, the cold and hot media outlet house steward of lower warp-wise who is connected with the cold and hot media outlet of described lower broadwise pipe group, the cold and hot medium inlet house steward of lower broadwise who is connected with the cold and hot medium inlet of described lower warp-wise pipe group, the cold and hot media outlet house steward of lower broadwise who is connected with the cold and hot media outlet of described lower warp-wise pipe group, the cold and hot medium inlet house steward of described lower warp-wise is connected with the cold and hot medium input tube of cold and hot medium system with the cold and hot medium inlet house steward of lower broadwise, the cold and hot media outlet house steward of described lower warp-wise is connected with the cold and hot medium back flow pipe of cold and hot medium system with the cold and hot media outlet house steward of lower broadwise,
On the connect material top of groove of described V-arrangement, below lower crystallization apparatus, be provided with one group of filtration unit, be provided with material import and export in the described V-arrangement groove middle and lower part that connects material, be provided with warp-wise U-shaped pipe group and broadwise U-shaped pipe group at the described V-arrangement groove internal upper part that connects material, the cold and hot medium inlet of described warp-wise U-shaped pipe group and broadwise U-shaped pipe group is connected with the cold and hot medium inflow pipe of cold and hot medium system respectively, the cold and hot media outlet of described warp-wise U-shaped pipe group and broadwise U-shaped pipe group is connected with the cold and hot medium back flow pipe of cold and hot medium system respectively
Described filtration unit comprises that one group of top and bottom are arranged with the sleeve of rectangular aperture I, be located in this sleeve and top and bottom are arranged with the rotating cylinder of the rectangular aperture II that physical dimension is identical with rectangular aperture I, top in the rectangular aperture I of described sleeve is provided with ceramic membrane, the termination of described rotating cylinder be arranged on the connect material angle stroke performer of groove outside of V-arrangement and be connected.
3. the device take carbolineum as waste anthracene, smart carbazole according to claim 2, it is characterized in that the U-shaped pipe of described warp-wise U-shaped pipe group and described sleeve staggered be arrangeding in parallel in same level, the U-shaped pipe of described broadwise U-shaped pipe group is positioned at below described sleeve, V-arrangement connects material above groove, and arranges with described sleeve horizontal vertical.
4. the device take carbolineum as waste anthracene, smart carbazole according to claim 2, is characterized in that the described upper warp-wise pipe of upper warp-wise pipe group and the quantity of the lower warp-wise pipe of lower warp-wise pipe group are respectively 9～39.
5. the device take carbolineum as waste anthracene, smart carbazole according to claim 2, is characterized in that the described upper broadwise pipe of upper broadwise pipe group and the quantity of the lower broadwise pipe of lower broadwise pipe group are respectively 6～32.
6. according to the device take carbolineum as waste anthracene, smart carbazole described in claim 2 or 3, it is characterized in that the described quantity of U-shaped pipe of warp-wise U-shaped pipe group and the quantity of the U-shaped pipe of broadwise U-shaped pipe group are 3～15.
7. the device take carbolineum as waste anthracene, smart carbazole according to claim 2, is characterized in that described crystallization apparatus is 2～6 layers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420039260.5U CN203700229U (en) | 2014-01-22 | 2014-01-22 | Device for preparing refined anthracene and refined carbazole with anthracene oil as raw material |
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| CN201420039260.5U CN203700229U (en) | 2014-01-22 | 2014-01-22 | Device for preparing refined anthracene and refined carbazole with anthracene oil as raw material |
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| CN201420039260.5U Withdrawn - After Issue CN203700229U (en) | 2014-01-22 | 2014-01-22 | Device for preparing refined anthracene and refined carbazole with anthracene oil as raw material |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103739439A (en) * | 2014-01-22 | 2014-04-23 | 鞍山兴德工程技术有限公司 | Device for preparing refined anthracene and refined carbazole by taking anthracene oil as raw material |
| CN115161071A (en) * | 2022-06-09 | 2022-10-11 | 上海交通大学 | Method for purifying and removing crystal anthracene oil by ceramic membrane filtration and catalytic coupling |
-
2014
- 2014-01-22 CN CN201420039260.5U patent/CN203700229U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103739439A (en) * | 2014-01-22 | 2014-04-23 | 鞍山兴德工程技术有限公司 | Device for preparing refined anthracene and refined carbazole by taking anthracene oil as raw material |
| CN115161071A (en) * | 2022-06-09 | 2022-10-11 | 上海交通大学 | Method for purifying and removing crystal anthracene oil by ceramic membrane filtration and catalytic coupling |
| CN115161071B (en) * | 2022-06-09 | 2024-04-16 | 上海交通大学 | Method for purifying decrystallized anthracene oil by ceramic membrane filtration and catalytic coupling |
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