CN203247104U - Anhydrous sodium sulphate production system - Google Patents
Anhydrous sodium sulphate production system Download PDFInfo
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- CN203247104U CN203247104U CN 201320251377 CN201320251377U CN203247104U CN 203247104 U CN203247104 U CN 203247104U CN 201320251377 CN201320251377 CN 201320251377 CN 201320251377 U CN201320251377 U CN 201320251377U CN 203247104 U CN203247104 U CN 203247104U
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Abstract
The utility model discloses an anhydrous sodium sulphate production system which solves the problems of higher preparation cost and low anhydrous sodium sulphate production quality of the conventional anhydrous sodium sulphate. The anhydrous sodium sulphate production system comprises a multi-stage reduction tower, a neutralization reaction kettle, a flocculation settling tank, a crystallizing tank and a vapor compressor, wherein evaporation and crystallization are operated in one unit, chromium salt denitration liquid is thrown into an evaporative crystallization system by a buffer tank after reduction, neutralization reaction, flocculation settling and multi-stage pressure filtration, a crystal product is thrown into a centrifugal machine through a crystal slurry pump after discharging, and then is sent into a fluidized bed drier by a spiral conveying belt after centrifugation, and dried end products are packaged after entering a storage bin. Free control to anhydrous sodium sulphate particles can be effectively achieved, and the technical problems of high preparation cost, short evaporimeter operation period, bad heat exchange effect and the like can be solved.
Description
Technical field
The utility model relates to chemical field, specifically a kind of Sodium sulfate anhydrous.min(99) production system.
Background technology
And China's Sodium sulfate anhydrous.min(99) is originated mainly by natural mirabilite ore and salt industry by product, and main flow technique has multiple-effect evaporation to add secondary steam nitre technique at present, multiple-effect evaporation adds backward feed technique, the methods such as seasoning dehydration.The multiple-effect evaporation method is used more extensively, and multiple-effect evaporator can utilize the part secondary steam, can save the part live steam, but still can consume a large amount of live steams, and equipment investment is large, and production cost is higher.
Crystallization mostly is the intermittent cooling crystallization process, and production intensity is low, is Na
2SO
410H
2The follow-up drying cost of O strengthens, and the impurity inclusion phenomenon is more serious, and crystallizer has high input.My company's utility model cruelly spilt the weak point of this technique by production practice with the evaporated crystallization device of mechanical vapour compressor; the easy fouling of vaporizer causes degradation of heat exchange performance; thereby cause the compressor temperature rise to become large; and then vaporization temperature uprises; cause to replenish live steam; thereby long-play causes the compressor warning to be shut down stops production whole equipment; the design of reason crystallizer not rationally causes mixing in the purified liquor outlet a large amount of thin brilliant on the one hand in addition; thereby aggravated the scale velocity of interchanger; the 3rd; crystal concentration control is unstable in the crystallization discharging; cause whizzer energy consumption height and separation efficiency to descend, thereby even isolate slurry and affect normally carrying out of next drying process.
Large multiple enterprises is produced Sodium sulfate anhydrous.min(99) and is rested on the GB6009-2003 standard, is difficult to satisfy contemporary Fine Chemical to the requirement of Sodium sulfate anhydrous.min(99) quality, and the Sodium sulfate anhydrous.min(99) market value is about 500 yuan/t, and it is significant that the production control cost improves added value.
The utility model content
The purpose of this utility model provides a kind of Sodium sulfate anhydrous.min(99) production system, to solve the existing higher problem of Sodium sulfate anhydrous.min(99) production cost.
The technical solution of the utility model is: a kind of Sodium sulfate anhydrous.min(99) production system, comprise the multilevel reduction tower, the neutralization reaction still, the flocculation sediment groove, crystallizer, vapour compressor, described multilevel reduction tower links to each other with the neutralization reaction still, described neutralization reaction still links to each other with the flocculation sediment groove, described flocculation sediment groove links to each other with the buffering separation system, described buffering separation system is connected with hot pressing filter group, described buffering separation system also links to each other with described crystallizer, the purified liquor outlet at described crystallizer top is by the first material pipe connecting plate type vaporizer, the material outlet end of described plate-type evaporator is connected with the gas-liquid separation flash tank by the second material pipe, the top of described plate-type evaporator links to each other with the vapour outlet end of described vapour compressor by intake ducting, the bottom of described plate-type evaporator is connected with plate-type condenser by condensing water conduit, the bottom of described plate-type condenser is connected with vacuum pump, the vapour outlet end of described gas-liquid separation flash tank links to each other with the steam-in end of described vapour compressor by steam-pipe, and the bottom of described gas-liquid separation flash tank links to each other with the recycle feed pipe of described crystallizer by fluid pipeline; The discharge port of described crystallizer links to each other with the thickener import by the crystallizer discharge pipe, the lower end outlet of described thickener connects the opening for feed of whizzer by thickening fluid pipeline, the upper end outlet of described thickener links to each other with the mother liquor return line at described whizzer top by the clear liquid pipeline, and described mother liquor return line links to each other with the import of crystallizer mother liquor.
Further improve as the utility model, the bottom of described multilevel reduction tower is connected with the sulfurous gas producer.
Further improve as the utility model, it also comprises ion and particle on-line measuring device, described neutralization reaction still comprises the first neutralization reaction still and the second neutralization reaction still that links to each other successively, described flocculation sediment groove comprises the first flocculation sediment groove and the second flocculation sediment groove that links to each other successively, described buffering separation system comprises the first surge tank, the second surge tank, the 3rd surge tank, the 4th surge tank, described the first surge tank respectively with described the second flocculation sediment groove, described the 3rd surge tank and described hot pressing filter group link to each other, described the second surge tank, the 3rd surge tank links to each other successively with the 4th surge tank and all links to each other with described hot pressing filter group, and described the second surge tank also links to each other with described crystallizer by feed pipe with the 4th surge tank; Described ion links to each other with the first neutralization reaction still, the second neutralization reaction still, the first flocculation sediment groove, the second flocculation sediment groove, the second surge tank, the 4th surge tank respectively with the particle on-line measuring device.
Further improve as the utility model, described crystallizer comprises upper cover and lower cover, be provided with guide shell in the described crystallizer, described guide shell comprises the guide shell direct tube section) and the curved cylinder of guide shell, connect by the reducing head between the curved cylinder of described guide shell direct tube section and guide shell, described reducing head links to each other with described recycle feed pipe by bridge piece; The diameter of described guide shell direct tube section is greater than the diameter of the curved cylinder of described guide shell, and the top of described guide shell is provided with traverse baffle, and described guide shell and traverse baffle are fixed on the crystallizer cylindrical shell of described crystallizer by fixing arm; Described traverse baffle is 0.5-1.5 rice apart from the distance at crystallizer top.
Further improve as the utility model, described guide shell direct tube section is axially arranged with 1-5 rejection footpath magma suction port near the traverse baffle place, at least 1 of every rejection footpath magma suction port, the bottom of described guide shell is provided with eluriates pipe, the bottom of described crystallizer cylindrical shell is provided with blow-off pipe, and the sidewall of described crystallizer cylindrical shell is provided with visor.
Further improve as the utility model, described plate-type evaporator is provided with the on-line cleaning device, described on-line cleaning device comprises hot water pump and coupled hot water circulation groove, the exit end of described hot water pump is leaded up to the scavenging solution pipeline and is linked to each other with described plate-type evaporator, another road of the exit end of described hot water pump links to each other with described the first material pipe by the first waterpipe, described hot water circulation groove also links to each other with described the second material pipe, condensing water conduit, and described the first material pipe is provided with recycle pump.
Further improve as the utility model, it also comprises dcs, described dcs respectively with described ion and particle on-line measuring device, described on-line cleaning device, described sulfurous gas producer, described the second surge tank, described the 3rd surge tank, described the 4th surge tank, described feed pipe, described crystallizer discharge pipe, described fluid pipeline, described the first material pipe, described the second material pipe, described condensing water conduit, described plate-type condenser, described vapour compressor, the intake ducting of described plate-type evaporator, described steam-pipe links to each other.
The utility model adopts advanced secondary steam mechanically compress reutilization technology, to evaporate and crystallization is placed on a unit and operates, by the chromic salts denitration liquid is passed through reduction, neutralization reaction, flocculation sediment, multistage press filtration, squeezes into evaporation and crystallization system by surge tank, squeeze into whizzer by the magma pump after the crystal product discharging, send into fluid bed dryer by spiral conveyor after centrifugal, dried finished product is packed after entering feed bin.This method takes full advantage of the secondary steam that vacuum flashing produces, and heats up as the thermal source of plate-type evaporator after mechanically compress, does not consume extra live steam, and production cost is low.
In addition, reduction, in and Working Procedure Controlling strict, detrimental impurity is removed thoroughly, the utility model adopts the multiple tracks quality product to detect online operation, detects Cr after flocculation sediment and the hot pressing filter
6+With Ca, Mg ion content, then return corresponding operation and again process as defective.Whole material and energy-optimised utilization, hot pressing filter filter residue return stoving oven, centrifuge mother liquor return crystallizer recrystallization, crystallizer secondary steam by mechanically compress after Returning evaporimeter serve as thermal source.The utility model can productive capacity be higher than the Sodium sulfate anhydrous.min(99) product of premium grads, can be used for particular requirement industry or outlet.Filtration fraction can divide pressurization sheet frame heat filtering and two steps of Depth Filtration, and insolubles content is reduced to below 0.005%, and calcium ions and magnesium ions content adds the hydrated barta of equivalent below 0.01% in the neutralizer, use chloride ion content to be down to 0.01%.
The utility model can in time be processed chromic salts by product saltcake waste liquid in the system, save refuse and pile up the factory building land used, reducing the saltcake efflorescence pollutes surrounding enviroment, remove the harmful chromium element that contains in the denitration liquid and enter the water pollution environment with rainwater, enterprise has obtained solution to problems such as waste water, waste sludge discharge pollution abatement costs.Simultaneously, the technique that employing is produced the top grade Sodium sulfate anhydrous.min(99) by the chromic salts denitration liquid has played the effect of turning waste into wealth, reduce the Enterprise Integrated cost, lay a good foundation for Sustainable Development of Enterprises, reduced solid waste, discharge of wastewater handling, avoid simultaneously efflorescence pollution and pollution of chromium.
The utility model adopts the many evacuator bodies of single-action to add the secondary steam utilization process, reduce production cost and greatly reduced occupation area of equipment simultaneously, 30,000 tons of annual treatment capacity meters can the saving heat energy consuming cost 1,600,000 yuan, save 1,000,000 yuan of facility investments, by regularly starting washing unit plate-type evaporator is carried out cleaning and descaling, assurance heat exchange efficiency, save energy realize producing continuously fully, and whole cleaning during shutdowns moved several months continuously to not stopping from three days to make the driving cycle.Be applicable to by mirabilite ore or inorganic salt co-production Sodium sulfate anhydrous.min(99), also can be used for producing the chemical substance that other evaporative crystallization method is produced product.
Description of drawings
Fig. 1 is a kind of structural representation of Sodium sulfate anhydrous.min(99) production system;
Fig. 2 is the structural representation of crystallizer in a kind of Sodium sulfate anhydrous.min(99) production system;
Fig. 3 is crystallizer inner fluid simulation streamline synoptic diagram in a kind of Sodium sulfate anhydrous.min(99) production system.
The Reference numeral implication is as follows:
Crystallizer (1), plate-type evaporator (2), hot water circulation groove 3, gas-liquid separation flash tank (4), vapour compressor (5), plate-type condenser (6), vacuum pump (7), whizzer (8), hot water pump (9), recycle pump (10), thickener (11), sulfurous gas producer (12), the first neutralization reaction still (13), the second neutralization reaction still (14), the first flocculation sediment groove (15), the second flocculation sediment groove (16), the first surge tank (17), hot pressing filter group (18), the second surge tank (19), the 3rd surge tank (20), the 4th surge tank (21), fluid bed dryer (22), feed bin (23), automatic packaging system (24), exhaust gas processing device (25), multilevel reduction tower (26), ion and particle on-line measuring device (27), dcs (28), feed pipe (201), the first material pipe (202), the second material pipe (203), steam-pipe (204), intake ducting (205), fluid pipeline (206), crystallizer discharge pipe (207), mother liquor return line (208), scavenging solution pipeline (209), the first waterpipe (212), condensing water conduit (213), clear liquid pipeline (214), thickening fluid pipeline (215), guide shell (101), traverse baffle (102), purified liquor outlet (103), upper cover (104), magma suction port (105), crystallizer housing (106), fixed tube (107), bridge piece (108), recycle feed pipe (109), crystallizer discharge port (110), eluriate pipe (111), blow-off pipe (112), visor (113), lower cover (114), mother liquor import (115), guide shell direct tube section (116), the curved cylinder of guide shell (117), reducing head (118).
Embodiment
A kind of Sodium sulfate anhydrous.min(99) production system, comprise multilevel reduction tower 26, neutralization reaction still, flocculation sediment groove, crystallizer 1, vapour compressor 5, multilevel reduction tower 26 links to each other with the neutralization reaction still, the bottom of multilevel reduction tower 26 is connected with sulfurous gas producer 12, and multilevel reduction tower 26 also is connected with exhaust gas processing device 25.The neutralization reaction still links to each other with the flocculation sediment groove, the flocculation sediment groove links to each other with the buffering separation system, the buffering separation system is connected with hot pressing filter group 18, the buffering separation system also links to each other with crystallizer 1, the purified liquor outlet 103 at crystallizer 1 top is by the first material pipe 202 connecting plate type vaporizers 2, the material outlet end of plate-type evaporator 2 is connected with gas-liquid separation flash tank 4 by the second material pipe 203, the top of plate-type evaporator 2 links to each other with the vapour outlet end of vapour compressor 5 by intake ducting 205, the bottom of plate-type evaporator 2 is connected with plate-type condenser 6 by condensing water conduit 213, the bottom of plate-type condenser 6 is connected with vacuum pump 7, the vapour outlet end of gas-liquid separation flash tank 4 links to each other with the steam-in end of vapour compressor 5 by steam-pipe 204, and the bottom of gas-liquid separation flash tank 4 links to each other with the recycle feed pipe 109 of crystallizer 1 by fluid pipeline 206; The discharge port 110 of crystallizer 1 links to each other with thickener 11 tangential entries by crystallizer discharge pipe 207, the lower end outlet of thickener 11 connects the opening for feed of whizzer 8 by thickening fluid pipeline 215, the upper end outlet of thickener 11 links to each other with the mother liquor return line 208 at whizzer 8 tops by clear liquid pipeline 214, and mother liquor return line 208 links to each other with crystallizer 1 mother liquor import 115.
In the present embodiment, neutralization reaction still and flocculation sediment groove all use two, can play and replace and the switching effect, make to produce uninterruptedly; The neutralization reaction still comprises the first neutralization reaction still 13 and the second neutralization reaction still 14 that links to each other successively, the flocculation sediment groove comprises the first flocculation sediment groove 15 and the second flocculation sediment groove 16 that links to each other successively, the buffering separation system comprises the first surge tank 17, the second surge tank 19, the 3rd surge tank 20, the 4th surge tank 21, the first surge tank 17 respectively with the second flocculation sediment groove 16, the 3rd surge tank 20 and hot pressing filter group 18 link to each other, the second surge tank 19, the 3rd surge tank 20 links to each other successively with the 4th surge tank 21 and all links to each other with hot pressing filter group 18, and the second surge tank 19 also links to each other with crystallizer 1 by feed pipe 201 with the 4th surge tank 21; Ion links to each other with the first neutralization reaction still 13, the second neutralization reaction still 14, the first flocculation sediment groove 15, the second flocculation sediment groove 16, the second surge tank 19, the 4th surge tank 21 respectively with particle on-line measuring device 27.
Crystallizer 1 comprises upper cover 104 and lower cover 114, be provided with guide shell 101 in the crystallizer 1, guide shell 101 comprises guide shell direct tube section 116 and the curved cylinder 117 of guide shell, connect by reducing head 118 between the curved cylinder 117 of guide shell direct tube section 116 and guide shell, reducing head 118 links to each other with recycle feed pipe 109 by bridge piece 108; The diameter of guide shell direct tube section 116 is greater than the diameter of the curved cylinder of guide shell 117, and the top of guide shell 101 is provided with traverse baffle 102, and guide shell 101 and traverse baffle 102 are fixed on the crystallizer cylindrical shell 106 of crystallizer 1 by fixing arm 107; Traverse baffle 102 is 0.5-1.5 rice apart from the distance at crystallizer 1 top.
Guide shell direct tube section 116 is axially arranged with 1-5 rejection footpath magma suction port 105 near traverse baffle 102 places, 105 at least 1 of every rejection footpath magma suction ports, the bottom of guide shell 101 is provided with eluriates pipe 111, the bottom of crystallizer cylindrical shell 106 is provided with blow-off pipe 112, and the sidewall of crystallizer cylindrical shell 106 is provided with visor 113.
Plate-type evaporator 2 is provided with the on-line cleaning device, the on-line cleaning device comprises hot water pump 9 and coupled hot water circulation groove 3, the exit end of hot water pump 9 is leaded up to scavenging solution pipeline 209 and is linked to each other with plate-type evaporator 2, another road of the exit end of hot water pump 9 links to each other with the first material pipe 202 by the first waterpipe 212, hot water circulation groove 3 also links to each other with the second material pipe 203, condensing water conduit 213, and the first material pipe 202 is provided with recycle pump 10.
Because Sodium sulfate anhydrous.min(99) solubility curve under operational condition is on a declining curve, plate-type evaporator will produce the crystal dirt after 2 operation for some time between plate affect heat-transfer effect, can judge according to dcs 28 monitor datas this moment and open the on-line cleaning device that links to each other with plate-type evaporator, circulating hot water derives from the plate-type evaporator water of condensation, solution enters internal system consumption through scavenging solution pipeline 209 after cleaning, do not need the additional hot water supply, secondary pollution can be do not produced, best heat exchange state can be returned to about hot water circulation 2h.
A kind of Sodium sulfate anhydrous.min(99) production system, it also comprises dcs 28, and dcs 28 links to each other with particle on-line measuring device 27, on-line cleaning device, sulfurous gas producer 12, the second surge tank 19, the 3rd surge tank 20, the 4th surge tank 21, feed pipe 201, crystallizer discharge pipe 207, fluid pipeline 206, the first material pipe 202, the second material pipe 203, condensing water conduit 213, plate-type condenser 6, vapour compressor 5, the intake ducting 205 of plate-type evaporator 2, steam-pipe 204 with ion respectively.Dcs 28 is switched input and output material at any time, removes situation to reach the Real Time Monitoring detrimental impurity, and underproof material is also returned last process by pump.
Sodium sulfate anhydrous.min(99) is produced, and comprises the operations such as reduction, neutralization, flocculation sediment, Multi-stage heat press filtration, evaporative crystallization, drying and finished product packing, and concrete steps are as follows:
The chromic salts denitration liquid is passed into multilevel reduction tower in parallel 26 reduction, liquid after will reducing by product pump is squeezed into the neutralization reaction still, liquid is squeezed into flocculation sediment groove flocculation sediment by product pump after the neutralization reaction, by product pump precipitated liquid is squeezed into hot pressing filter group 18 afterwards, after the press filtration, by ion and particle on-line measuring device 27 check impurity ion content, underproof filter cake returns neutralization reaction still or flocculation sediment groove, the first surge tank 17 is for the liquid that receives and store from the first flocculation sediment groove 15 or the second flocculation sediment groove 16, switch at any time input and output material by dcs 28, remove situation to reach the Real Time Monitoring detrimental impurity, underproof material is also returned last process by pump.Filtrate after the second surge tank 19 and the 4th surge tank 21 are used for receiving and filter with store heat, carry out continuously to guarantee the evaporative crystallization operation, the 3rd surge tank 20 is used for accepting and storing underproof filtrate in the filtration procedure, then by pump underproof filtrate is returned the first surge tank 17 or is directly squeezed into hot pressing filter group 18.Qualified filtrate is flowed out by the second surge tank 19 and the 4th surge tank 21, enter crystallizer 1 through feed pipe 201, after being full of, crystallizer 1 interior material enters plate-type evaporator 2 by purified liquor outlet 103 by the first material pipe 202, material after plate-type evaporator 2 interior acceptance are heated up by vapour compressor 5 superchargings secondary steam and heat up, material after the intensification enters gas-liquid separation flash tank 4 from the second material pipe 203 and carries out vacuum flashing, and gas is entered by steam-pipe 204 and enters plate-type evaporator 2 by intake ducting 205 after vapour compressor 5 superchargings heat up and recycle; Liquid after the separation enters crystallizer 1 by fluid pipeline 206, minute two-way is in the crystallization of tank internal recycle after entering crystallizer 1, one the tunnel through bridge piece 108, move upward along guide shell straight tube 116 and to promote the crystal growth, arrive behind the top and to be stopped by traverse baffle 102 and to move downward the sedimentation crystal, another route elutriation pipe 111 moves downward the backward upper motion that rebounded at the bottom of the tank crystal is carried out classification, the crystal that meets dimensional requirement enters thickener 11 by crystallizer discharge port 110 through crystallizer discharge pipe 207 and increases magma concentration, magma enters the whizzer 8 centrifugal products that get through thickening fluid pipeline 215 behind the enrichment, supernatant liquor in the thickener enters crystallizer 1 through clear liquid pipeline 214 and continues circulation, centrifuge mother liquor returns crystallizer 1 by mother liquor return line 208 and continues circulation, undesirable crystal is sucked in crystallizing bed internal recycling growth by the magma suction port 105 on the guide shell direct tube section 116, and clear liquor enters plate-type evaporator 2 cyclical operations by crystallizer 1 top; Centrifugal rear solid is delivered to fluid bed dryer 22 by screw transmission strap, and dry rear product is packaged into finished product by automatic packaging system 24 after feed bin 23 of short duration storages.
Present method also comprises carries out the on-line cleaning operation to plate-type evaporator 2, and on-line cleaning operation and ion and particle on-line measuring device 27 are by dcs 28 controls.
The plate-type evaporator water of condensation enters condenser 7 with incondensable gas by the pipeline that links to each other with condenser 7, and vacuum pump 7 provides the operation vacuum for whole system; Be equipped with valve, pressure transmitter and temperature sensor on each pipeline, realize automatically control by dcs 28.
Claims (7)
1. Sodium sulfate anhydrous.min(99) production system, comprise the multilevel reduction tower, the neutralization reaction still, the flocculation sediment groove, crystallizer, vapour compressor, it is characterized in that: described multilevel reduction tower (26) links to each other with the neutralization reaction still, described neutralization reaction still links to each other with the flocculation sediment groove, described flocculation sediment groove links to each other with the buffering separation system, described buffering separation system is connected with hot pressing filter group (18), described buffering separation system also links to each other with described crystallizer (1), the purified liquor outlet (103) at described crystallizer (1) top is by the first material pipe (202) connecting plate type vaporizer (2), the material outlet end of described plate-type evaporator (2) is connected with gas-liquid separation flash tank (4) by the second material pipe (203), the top of described plate-type evaporator (2) links to each other with the vapour outlet end of described vapour compressor (5) by intake ducting (205), the bottom of described plate-type evaporator (2) is connected with plate-type condenser (6) by condensing water conduit (213), the bottom of described plate-type condenser (6) is connected with vacuum pump (7), the vapour outlet end of described gas-liquid separation flash tank (4) links to each other with the steam-in end of described vapour compressor (5) by steam-pipe (204), and the bottom of described gas-liquid separation flash tank (4) links to each other with the recycle feed pipe (109) of described crystallizer (1) by fluid pipeline (206); The discharge port (110) of described crystallizer (1) links to each other with thickener (11) import by crystallizer discharge pipe (207), the lower end outlet of described thickener (11) connects the opening for feed of whizzer (8) by thickening fluid pipeline (215), the upper end outlet of described thickener (11) links to each other with the mother liquor return line (208) at described whizzer (8) top by clear liquid pipeline (214), and described mother liquor return line (208) links to each other with crystallizer (1) mother liquor import (115).
2. Sodium sulfate anhydrous.min(99) production system according to claim 1, it is characterized in that: the bottom of described multilevel reduction tower (26) is connected with sulfurous gas producer (12).
3. Sodium sulfate anhydrous.min(99) production system according to claim 1 and 2, it is characterized in that: it also comprises ion and particle on-line measuring device (27), described neutralization reaction still comprises the first neutralization reaction still (13) and the second neutralization reaction still (14) that links to each other successively, described flocculation sediment groove comprises the first flocculation sediment groove (15) and the second flocculation sediment groove (16) that links to each other successively, described buffering separation system comprises the first surge tank (17), the second surge tank (19), the 3rd surge tank (20), the 4th surge tank (21), described the first surge tank (17) respectively with described the second flocculation sediment groove (16), described the 3rd surge tank (20) and described hot pressing filter group (18) link to each other, described the second surge tank (19), the 3rd surge tank (20) links to each other successively with the 4th surge tank (21) and all links to each other with described hot pressing filter group (18), and described the second surge tank (19) also links to each other with described crystallizer (1) by feed pipe (201) with the 4th surge tank (21); Described ion links to each other with the first neutralization reaction still (13), the second neutralization reaction still (14), the first flocculation sediment groove (15), the second flocculation sediment groove (16), the second surge tank (19), the 4th surge tank (21) respectively with particle on-line measuring device (27).
4. Sodium sulfate anhydrous.min(99) production system according to claim 3, it is characterized in that: described crystallizer (1) comprises upper cover (104) and lower cover (114), be provided with guide shell (101) in the described crystallizer (1), described guide shell (101) comprises guide shell direct tube section (116) and the curved cylinder of guide shell (117), connect by reducing head (118) between the curved cylinder of described guide shell direct tube section (116) and guide shell (117), described reducing head (118) links to each other with described recycle feed pipe (109) by bridge piece (108); The diameter of described guide shell direct tube section (116) is greater than the diameter of the curved cylinder of described guide shell (117), the top of described guide shell (101) is provided with traverse baffle (102), and described guide shell (101) and traverse baffle (102) are fixed on the crystallizer cylindrical shell (106) of described crystallizer (1) by fixing arm (107); Described traverse baffle (102) is 0.5-1.5 rice apart from the distance at crystallizer (1) top.
5. Sodium sulfate anhydrous.min(99) production system according to claim 4, it is characterized in that: described guide shell direct tube section (116) locates to be axially arranged with 1-5 rejection footpath magma suction port (105) near traverse baffle (102), (105) at least 1 of every rejection footpath magma suction ports, the bottom of described guide shell (101) is provided with eluriates pipe (111), the bottom of described crystallizer cylindrical shell (106) is provided with blow-off pipe (112), and the sidewall of described crystallizer cylindrical shell (106) is provided with visor (113).
6. Sodium sulfate anhydrous.min(99) production system according to claim 5, it is characterized in that: described plate-type evaporator (2) is provided with the on-line cleaning device, described on-line cleaning device comprises hot water pump (9) and coupled hot water circulation groove (3), the exit end of described hot water pump (9) is leaded up to scavenging solution pipeline (209) and is linked to each other with described plate-type evaporator (2), another road of exit end of described hot water pump (9) links to each other with described the first material pipe (202) by the first waterpipe (212), described hot water circulation groove (3) also with described the second material pipe (203), condensing water conduit (213) links to each other, and described the first material pipe (202) is provided with recycle pump (10).
7. Sodium sulfate anhydrous.min(99) production system according to claim 6, it is characterized in that: it also comprises dcs (28), described dcs (28) respectively with described ion and particle on-line measuring device (27), described on-line cleaning device, described sulfurous gas producer (12), described the second surge tank (19), described the 3rd surge tank (20), described the 4th surge tank (21), described feed pipe (201), described crystallizer discharge pipe (207), described fluid pipeline (206), described the first material pipe (202), described the second material pipe (203), described condensing water conduit (213), described plate-type condenser (6), described vapour compressor (5), the intake ducting (205) of described plate-type evaporator (2), described steam-pipe (204) links to each other.
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| CN 201320251377 CN203247104U (en) | 2013-05-10 | 2013-05-10 | Anhydrous sodium sulphate production system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103241749A (en) * | 2013-05-10 | 2013-08-14 | 甘肃蓝科石化高新装备股份有限公司 | Anhydrous sodium sulfate production system and production method |
| CN103539164A (en) * | 2013-11-01 | 2014-01-29 | 四川省银河化学股份有限公司 | Method for refining sodium sulfate powder from chromium-containing mirabilite |
-
2013
- 2013-05-10 CN CN 201320251377 patent/CN203247104U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103241749A (en) * | 2013-05-10 | 2013-08-14 | 甘肃蓝科石化高新装备股份有限公司 | Anhydrous sodium sulfate production system and production method |
| CN103539164A (en) * | 2013-11-01 | 2014-01-29 | 四川省银河化学股份有限公司 | Method for refining sodium sulfate powder from chromium-containing mirabilite |
| CN103539164B (en) * | 2013-11-01 | 2016-05-25 | 四川省银河化学股份有限公司 | A kind of by the method containing the refining glauber salt of chromium saltcake |
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