CN103923242B - Hydrolyzed polyacrylonitrile ammonium salt production system - Google Patents
Hydrolyzed polyacrylonitrile ammonium salt production system Download PDFInfo
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- CN103923242B CN103923242B CN201410161349.3A CN201410161349A CN103923242B CN 103923242 B CN103923242 B CN 103923242B CN 201410161349 A CN201410161349 A CN 201410161349A CN 103923242 B CN103923242 B CN 103923242B
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- 150000003863 ammonium salts Chemical class 0.000 title claims abstract description 40
- 229920002239 polyacrylonitrile Polymers 0.000 title claims abstract description 39
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 141
- 238000000746 purification Methods 0.000 claims abstract description 96
- 239000011344 liquid material Substances 0.000 claims abstract description 79
- 238000001035 drying Methods 0.000 claims abstract description 63
- 238000011084 recovery Methods 0.000 claims abstract description 53
- 239000002994 raw material Substances 0.000 claims abstract description 46
- 239000007789 gas Substances 0.000 claims abstract description 44
- 239000002912 waste gas Substances 0.000 claims abstract description 38
- 239000002918 waste heat Substances 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 105
- 239000007921 spray Substances 0.000 claims description 99
- 235000011149 sulphuric acid Nutrition 0.000 claims description 61
- 239000001117 sulphuric acid Substances 0.000 claims description 61
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 57
- 239000010881 fly ash Substances 0.000 claims description 52
- 239000007788 liquid Substances 0.000 claims description 39
- 238000001914 filtration Methods 0.000 claims description 29
- 238000012546 transfer Methods 0.000 claims description 29
- 239000000428 dust Substances 0.000 claims description 27
- 238000005406 washing Methods 0.000 claims description 27
- 238000004891 communication Methods 0.000 claims description 21
- 230000008676 import Effects 0.000 claims description 19
- 238000007791 dehumidification Methods 0.000 claims description 15
- 239000002699 waste material Substances 0.000 claims description 15
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 12
- 238000002485 combustion reaction Methods 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 11
- 238000013022 venting Methods 0.000 claims description 11
- 238000004140 cleaning Methods 0.000 claims description 10
- 239000012535 impurity Substances 0.000 claims description 10
- 238000011068 loading method Methods 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 239000001301 oxygen Substances 0.000 claims description 5
- 229910052760 oxygen Inorganic materials 0.000 claims description 5
- 239000008400 supply water Substances 0.000 claims description 5
- 238000010276 construction Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 238000004804 winding Methods 0.000 claims description 3
- 239000003245 coal Substances 0.000 abstract description 8
- 238000010438 heat treatment Methods 0.000 abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 42
- 229910021529 ammonia Inorganic materials 0.000 description 21
- 230000000694 effects Effects 0.000 description 21
- 239000000243 solution Substances 0.000 description 19
- 238000000034 method Methods 0.000 description 18
- 230000008569 process Effects 0.000 description 18
- 239000012716 precipitator Substances 0.000 description 9
- 230000007423 decrease Effects 0.000 description 8
- 238000005553 drilling Methods 0.000 description 7
- 208000005156 Dehydration Diseases 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 229920002972 Acrylic fiber Polymers 0.000 description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 3
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 3
- 235000011130 ammonium sulphate Nutrition 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000011049 filling Methods 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 239000000779 smoke Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 230000007115 recruitment Effects 0.000 description 2
- 230000002000 scavenging effect Effects 0.000 description 2
- 238000002791 soaking Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 229920006397 acrylic thermoplastic Polymers 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011026 diafiltration Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920003229 poly(methyl methacrylate) Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 235000019608 salt taste sensations Nutrition 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- ISXSCDLOGDJUNJ-UHFFFAOYSA-N tert-butyl prop-2-enoate Chemical compound CC(C)(C)OC(=O)C=C ISXSCDLOGDJUNJ-UHFFFAOYSA-N 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a hydrolyzed polyacrylonitrile ammonium salt production system which comprises a reaction kettle, a raw material feeding system and a heat-conducting oil furnace, wherein the oil outlet of the heat-conducting oil furnace is communicated with the oil inlet of the reaction kettle, and the oil inlet of the heat-conducting oil furnace is communicated with the oil outlet of the reaction kettle; the reaction kettle is connected with a material buffer tank through a discharge pipe and a liquid material output heat-insulating pipeline; the discharge port of the material buffer tank is connected with a material storage tank through a filter, the discharge port of the material storage tank is connected with a drying system, and the drying system is connected with the exhaust port of the heat-conducting oil furnace; the gas outlet of the material buffer tank is connected with a waste heat recovery system, the waste heat recovery system is connected with the raw material feeding system, the waste heat recovery system is also connected with a waste gas recovery and purification system, and the waste gas recovery and purification system is connected with the raw material feeding system. The hydrolyzed polyacrylonitrile ammonium salt production system disclosed by the invention can reduce the labor intensity of workers and shorten the feeding time, can be used for recovering the hot steam, save the production cost, improve the operating environment of the workers by utilizing waste gas, reduce the usage amount of air heating furnace coal by using the drying system and reduce the cost.
Description
Technical field
The invention belongs to hydrolyzed polyacrylonitrile ammonium salt production technical field, specifically relate to a kind of hydrolyzed polyacrylonitrile ammonium salt production system.
Background technology
In petroleum drilling operation, diafiltration will occur when drilling fluid flows through pervious course under stress, cause drilling fluid liquid phase to infiltrate stratum, this process is referred to as " dehydration ".If dehydration can not be well controlled, a large amount of dehydrations enters stratum and not only induces well unstability, and can produce infringement to hydrocarbon zone, and the effective ways addressed this problem at present add fluid loss agent exactly in drilling fluid.Fluid loss agent is water retaining again, and its function is the stability ensureing drilling mud performance, reduces the filter loss of drilling mud and the apparent viscosity of drilling fluid, and reduces harmful liquid leak-off to stratum, the Simultaneous Stabilization borehole wall, guarantee hole diameter rule.Fluid loss agent product category is more, and hydrolyzed polyacrylonitrile ammonium salt because cost is low, simple, the stable performance of processing, heat and salinity tolerance is effective is widely used in petroleum system probing.
The industrial water requirement of hydrolyzed polyacrylonitrile ammonium salt is large; it is hydrolyzed at high temperature under high pressure by acrylics filament and obtained product; and the main moiety of a large amount of waste and old clothings is acrylic fibers; with the acrylic fibers in waste and old clothing for raw material; prepare hydrolyzed polyacrylonitrile ammonium salt and can realize environment protection, also can be cost-saving.
Hydrolyzed polyacrylonitrile ammonium salt adopts hydrolyzed polyacrylonitrile ammonium salt production system to produce, in use mainly there is the defect of following several respects in current hydrolyzed polyacrylonitrile ammonium salt production system: (1) produces is all adopt the artificial second floor (because the charging opening of reactor is at second floor) the waste and old clothes sorted being transported to workshop, and then material manually joins in reactor by use, in reinforced process, need 4-6 people to operate simultaneously, some people is reinforced in reactor, one personal responsibility adds water in reactor, and (object added water is soaked by material, reaction after being convenient to heat up), some people waddy reaches in tank and the material be filled into is carried out tamping (because material ratio is more fluffy, every tank reactor charge weight limits, so very important person's ceaselessly tamping), the whole process need time is at 1-2 hour, and whole workshop condition is filthy.(2) most of enterprise by the hot gas that produces during reactor blowdown (because the material blowdown in reactor is in material buffer tank, so the hot gas produced during reactor blowdown is the hot gas in material buffer tank) direct or indirect be discharged in air, cause serious environmental pollution, often there is very unpleasant temperature in the Working environment of workman, affect the healthy of workman, and great waste is caused to the energy.(3) produce in hydrolyzed polyacrylonitrile ammonium salt process and can produce a large amount of ammonias, gas is directly discharged in air by most of factory, causes serious environmental pollution, and whole plant area the working environment of workers is poor simultaneously.(4) in drying process, the usage quantity of coal is comparatively large, wastes a large amount of coal resources, adds production cost; Manpower is adopted to carry out sizing screening to dried material, labor strength is comparatively large, and librarian use cost is higher, is entrained with a large amount of ammonium salt tastes in dry waste gas of discharging, these are not discharged in air through any process is directly outer, severe contamination Air quality.
Summary of the invention
The object of the invention is to overcome above-mentioned deficiency of the prior art, provide a kind of hydrolyzed polyacrylonitrile ammonium salt production system, greatly can reduce the labour intensity of workman after using raw material feeding system, curtail the feeding hours, operative's environment neat and tidy is orderly; After using residual neat recovering system, the hot steam produced during reactor blowdown is reclaimed again, add the index content of product, reduce the time that reactor heats up, decrease the usage quantity of heat-conducting oil furnace coal, save production cost; Accomplish that waste gas utilizes again after using waste gas recovery purification system, improved operative's environment; Greatly reduce the usage quantity of hotblast stove coal after using dehumidification system, reduce production cost, and decrease labor strength and recruitment cost.
For achieving the above object, the technical solution used in the present invention is: a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: comprise reactor, to the raw material feeding system of reactor material loading with provide the heat-conducting oil furnace of intensification thermal source for the reaction of reactor, the oil outlet of described heat-conducting oil furnace is communicated with the oil-in of reactor, the oil-in of described heat-conducting oil furnace is communicated with the oil outlet of reactor, described reactor exports utilidor by blowdown pipe and liquid material and is connected with material buffer tank, the discharge port of described material buffer tank is connected with material storing tank by strainer, the discharge port of described material storing tank is connected with for the dehumidification system to dry materials, described dehumidification system is connected with the venting port of heat-conducting oil furnace, the air outlet of described material buffer tank is connected with the residual neat recovering system for hot gas in recovered material surge tank, described residual neat recovering system is connected with raw material feeding system, described residual neat recovering system is also connected with the waste gas recovery purification system for reclaiming clean waste gas, described waste gas recovery purification system is connected with raw material feeding system.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: described raw material feeding system comprises the first transfer roller, second conveyor, one-level knife mill, 3rd transfer roller, secondary knife mill, first wind stopping device, 6th induced draft fan, pulsaire collector and the assorted tripping device of material, described first transfer roller is obliquely installed, described second conveyor is horizontally disposed with, the feed end of described second conveyor is positioned at below the discharge end of the first transfer roller, the discharge end of described second conveyor is positioned at above the chute import of one-level knife mill, the discharge port of described one-level knife mill is positioned at above the feed end of the 3rd transfer roller, described 3rd transfer roller is horizontally disposed with, the discharge end of described 3rd transfer roller is positioned at above the chute import of secondary knife mill, the discharge port of described secondary knife mill to be communicated with and by expect to mix tripping device by the impurity in the raw material after shredding through secondary knife mill and dust separation out by the mix opening for feed of tripping device of Material pipeline and described material, the mix discharge port of tripping device of described material is communicated with the opening for feed of the first wind stopping device, the discharge port of described first wind stopping device is connected with hopper, the bottom of described hopper is connected with hose connector, the end of described hose connector is communicated with the opening for feed of reactor, described hopper is provided with coupled logical supplying hot water water pipe and first outlet pipe, the link position of described supplying hot water water pipe and hopper is higher than the link position of first outlet pipe and hopper, the blast inlet of described 6th induced draft fan is communicated with by the mix air outlet of tripping device of first outlet pipe road and described material, the air outlet of described 6th induced draft fan is communicated with the inlet mouth of pulsaire collector by second exhaust pipe road.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: described material tripping device of mixing comprises casing, described opening for feed is arranged on the upper end of casing, described discharge port is arranged on the bottom of casing, described air outlet is arranged on the top of casing, described air outlet is positioned at the below of opening for feed, mesh roller is installed in described casing, the inwall of described casing is positioned at the rubber baffle being provided with below mesh roller and being close to mesh roller, one of described mesh roller is rectified air outlet, the other end of described mesh roller is installed with the first sprocket wheel, on described casing and near the first sprocket wheel place, drive-motor is installed, the output shaft of described drive-motor is installed with the second sprocket wheel, described first sprocket wheel and the second sprocket wheel are connected to form sprocket wheel chain gear by chain.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: air outlet, the top place of described material buffer tank is provided with multiple material inlet, one end that described material inlet exports utilidor with liquid material is communicated with, the other end that described liquid material exports utilidor is communicated with one end of blowdown pipe, and the other end of described blowdown pipe stretches in reactor; The bottom of described material buffer tank is provided with top discharge mouth, lower discharge port and slag-drip opening.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: described residual neat recovering system comprises waste heat recovery tank, 3rd spray pump and main jet shower pipe, the bottom of described waste heat recovery tank is provided with liquid level porthole and lower liquid level porthole, described waste heat recovery tank is communicated with by the air outlet of insulating pipe with material buffer tank top, described insulating pipe to stretch in waste heat recovery tank and is positioned at the bottom of waste heat recovery tank, the bottom of described waste heat recovery tank is provided with the first water outlet and the second water outlet, described second water outlet is through pipeline, pump is connected with supplying hot water water pipe with the heat supply water pipe leading to workshop, described first water outlet is connected by the import of the first pipeline with the 3rd spray pump, described 3rd spray pump outlet is connected with one end of main jet shower pipe, the other end of described main jet shower pipe is provided with the coupled logical shower in one end, the other end of described shower stretches in insulating pipe, stretch on the shower in insulating pipe and the 3rd spray header is installed.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: described strainer comprises cabinet, feed liquid collection box, filter gantry and the first drive-motor, the top of described cabinet is provided with chassis lid, described feed liquid collection box is arranged in cabinet, the bottom of described feed liquid collection box is provided with discharge nozzle integrated with it, described filter vat frame is arranged in feed liquid collection box, detachably filtering net is installed in described filtration gantry, the top of described filtration gantry is provided with filtering net bung, the top of described cabinet is provided through filtering net bung and stretches into the feed-pipe in filtering net, the bottom of described filtration gantry is fixed with axle, the end of described axle passes feed liquid collection box and is rotationally connected with feed liquid collection box, the bottom of described feed liquid collection box is fixed with axle sleeve, described axle is through axle sleeve, the end winding support of described axle has the second belt pulley, described first drive-motor is fixed on cabinet, the output shaft of described first drive-motor is installed with the first belt pulley, described first belt pulley is connected to form belt transport by belt and the second belt pulley, described feed-pipe is all communicated with lower discharge port with top discharge mouth by liquid material transport pipe, and described discharge nozzle is communicated with the opening for feed of material storing tank.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: described waste gas recovery purification system comprises first class purification tower, first spray pump, secondary purification tower, second spray pump and dilute sulfuric acid solution case, the inlet mouth of described first class purification tower is communicated with the air outlet of the first tracheae with waste heat recovery tank top by the 5th induced draft fan, the air outlet place of described 5th induced draft fan is connected with waste pipe, described waste pipe is communicated with first outlet pipe by the 4th induced draft fan, overhead gage for changing exhaust gas flow direction and lower baffle plate are installed in described first class purification tower, the outlet of described first class purification tower and the inlet communication of the first spray pump, described first spray pump outlet is connected with the first dilute sulphuric acid pipe, the end of described first dilute sulphuric acid pipe to be stretched in first class purification tower and is positioned at above lower baffle plate, described first dilute sulphuric acid pipe is also connected with end and stretches in first class purification tower and the second dilute sulphuric acid pipe be positioned at above overhead gage, stretch into the first dilute sulphuric acid pipe in first class purification tower and the second dilute sulphuric acid Guan Shangjun is provided with the first spray header, the top of described first class purification tower to be stretched in secondary purification tower and is communicated with secondary purification tower, in the top of described first class purification tower, baffle plate is installed, the top of described secondary purification tower is provided with venting port, described secondary purification tower is communicated with dilute sulfuric acid solution case by the 3rd dilute sulphuric acid pipe, described dilute sulfuric acid solution case is enclosed construction, the sidewall of described dilute sulfuric acid solution case is provided with dilute sulphuric acid import, the bottom of described dilute sulfuric acid solution case and the inlet communication of the second spray pump, described second spray pump outlet is connected with the 4th dilute sulphuric acid pipe, the end of described 4th dilute sulphuric acid pipe to be stretched in secondary purification tower and is positioned at above first class purification tower, stretch on the 4th dilute sulphuric acid pipe in secondary purification tower and the second spray header is installed.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: the bottom of described first class purification tower is provided with dilute sulphuric acid and adds entrance, the bottom sidewall of described first class purification tower is provided with dilute sulphuric acid and arranges mouth outward, the sidewall of described first class purification tower to be disposed with from the bottom to top under dilute sulfuric acid solution porthole, spray header porthole on porthole and spray header, under described spray header, porthole is positioned at the top of overhead gage, and on described spray header, porthole is positioned at the top of lower baffle plate; The bottom of described secondary purification tower is provided with relief outlet.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: described dehumidification system comprises the first fly-ash separator, vent gas tower, hotblast stove, second fly-ash separator, drying tower, 3rd fly-ash separator and washing, purifying tower, described first fly-ash separator is connected with heat-conducting oil furnace by the first induced draft fan, the air outlet of described heat-conducting oil furnace is communicated with the inlet mouth of the first induced draft fan, the air outlet of described first induced draft fan is communicated with the inlet mouth of the first fly-ash separator, the air outlet of described first fly-ash separator is by the second induced draft fan, first MOD, first temperature transmitter is communicated with the inlet mouth of vent gas tower with pipeline, the wind mixed chamber of described hotblast stove is by the second MOD and the pipeline communication between the first temperature transmitter and the first MOD, the air outlet of the bottom of combustion chamber of described hotblast stove is connected with gas blower, the bottom of described wind mixed chamber and be provided with the second temperature transmitter near combustion chamber place, the top of described wind mixed chamber and be provided with the 3rd temperature transmitter near air outlet place of wind mixed chamber, the bottom of described wind mixed chamber is provided with the 3rd MOD, described wind mixed chamber air outlet is connected with the inlet mouth of the second fly-ash separator by the 4th temperature transmitter, dust outlet bottom described second fly-ash separator is connected with the 3rd wind stopping device, the discharge port of described 3rd wind stopping device stretches in setting tank thereunder, the air outlet of described second fly-ash separator is connected with the inlet mouth of drying tower by the 5th temperature transmitter, the top of described drying tower is provided with centrifugal atomizer, the second pipe that the inlet mouth of described 3rd fly-ash separator is stretched in drying tower by one end is communicated with drying tower, described 3rd fly-ash separator is communicated with the bottom of washing, purifying tower by the 3rd induced draft fan, the bottom of described washing, purifying tower is also connected with the first cleaning circulation pump by water tank, described first cycles of washing pump outlet is connected with end and stretches into the first sluicing pipe in the middle part of washing, purifying tower, stretch on the first sluicing pipe in washing, purifying tower and the 4th spray header is installed, the top of described washing, purifying tower is provided with pure qi (oxygen) air outlet, described centrifugal atomizer is by liquid material transferpump, liquid material stirred pot, liquid material recycle pump, liquid material hold-up vessel is connected with centrifugal atomizer opening for feed with feeding pump, the import of described liquid material transferpump and the outlet of material storing tank, the inlet communication of described liquid material conveying pump outlet and liquid material stirred pot, the outlet of described liquid material stirred pot and the inlet communication of liquid material recycle pump, described liquid material circulation pump outlet is by the inlet communication of pipeline and first-hand movable valve and liquid material hold-up vessel, the described outlet of liquid material hold-up vessel is communicated with the opening for feed of centrifugal atomizer, described liquid material stirred pot is connected with auxiliary material charging machine by pipeline, the import of described liquid material stirred pot is by second-hand's movable valve and the pipeline communication between liquid material recycle pump and first-hand movable valve.
Above-mentioned a kind of hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: the quantity of described 3rd fly-ash separator is two, two the 3rd fly-ash separators are all communicated with drying tower by second pipe, dust outlet bottom described 3rd fly-ash separator is connected with the 4th wind stopping device, the discharge port of described 4th wind stopping device is connected with tremie pipe, is provided with reciprocating sieve below the end of described tremie pipe; The below of described drying tower is provided with worm conveyor, and the opening for feed of described worm conveyor is positioned at below the discharge port bottom drying tower, and the discharge port of described worm conveyor is positioned at the top of reciprocating sieve; The bottom of described drying tower is provided with motor, and the output shaft of described motor stretches in drying tower and end is provided with material toggling pawl.
The present invention compared with prior art has the following advantages:
1, raw material feeding system of the present invention adopts transfer roller to carry out material loading, greatly can reduce the labour intensity of workman, curtail the feeding hours (feed time completes within half an hour), can stream time long, saved recruitment cost, operative's environment neat and tidy is orderly; And because of raw material be laid on the conveying belt of transfer roller when material loading, therefore can reject impurity in raw material while material loading, the secondary quality inspection of raw material can be realized.
2, raw material feeding system of the present invention by means of by high-power induced draft fan to the pull of vacuum produced in pipeline, utilize the draught head of vacuum and environment space, make to form gas flow in transport pipe, drive useless acrylic fibres raw material to move, thus raw material is risen to the conveying of about 8 meters height location from ground; Because material loading carries out at enclosed space, so gas-tight phenomenon, the working environment of workers sanitation and hygiene, and reach atmospheric emission standard from pulsaire collector air outlet expellant gas.
3, the present invention can carry out spray water soak treatment to material when adding material, material is fully sprayed and soaks mixing, by being connected hose connector in the bottom of hopper with between reactor, material after soaking like this again fully mixes in decline process, therefore can ensure that material and water fully mix, fast reaction speed, improves reaction efficiency.In addition, the present invention can carry out spray water soak treatment when adding material, makes material have certain gravity, and material decline is stacked solid, therefore solves fluffy, the unreal problem needing manpower rod not stop tamping of waste and old clothes blanking in prior art.
4, after the present invention uses residual neat recovering system, the hot steam produced during reactor blowdown is reclaimed again, also absorbed by the ammonia carried secretly in hot gas, the hot gas after absorption becomes hot water simultaneously, hot water again for the production of in, containing ammonia in water, considerably increase the index content of product, supply water to reactor with hot water simultaneously, greatly reduce the time that reactor heats up, decrease the usage quantity of heat-conducting oil furnace coal, save production cost.
5, after the present invention uses waste gas recovery purification system, the Ammonia recovery that can will produce in production process, dilute sulphuric acid and ammonia is mainly used to react in scavenging tower, produce ammonium sulfate, then will reach certain density ammonium sulfate to discharge, again for the production of in (ammonium sulfate is indispensable addition material aborning), the utilization again of the waste gas accomplished thus, improves the operating environment of workman simultaneously.
6, after the present invention uses dehumidification system, first reduce from personnel cost a greater part of, adopt reciprocating sieve to carry out classification process to material in dehumidification system, greatly reduce the labour intensity of workman; By sending for reactor the hot blast in the heat-conducting oil furnace of thermal oil to be guided as drying tower provides in the hotblast stove of heat by pipeline, two kinds of hot blasts being mixed, greatly reduces the usage quantity of hotblast stove coal, thus reduce production cost.
Below by drawings and Examples, the present invention is described in further detail.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Fig. 2 is the A place enlarged view of Fig. 1.
Fig. 3 is the B place enlarged view of Fig. 1.
Fig. 4 is the structural representation of dehumidification system of the present invention.
Fig. 5 material of the present invention is mixed the annexation schematic diagram of tripping device and the first wind stopping device.
Fig. 6 is the structural representation of mesh roller of the present invention.
Fig. 7 is the structural representation of strainer of the present invention.
Description of reference numerals:
1-raw material feeding system; 1-1-the first transfer roller; 1-2-one-level knife mill;
1-3-the 3rd transfer roller; 1-4-secondary knife mill; 1-5-casing;
1-51-porthole; 1-52-air outlet; 1-61-opening for feed;
1-62-discharge port; 1-7-mesh roller; 1-71-the first sprocket wheel;
1-8-rubber baffle; 1-9-the first wind stopping device; 1-10-hopper;
1-101-supplying hot water water pipe; 1-102-first outlet pipe; 1-12-Material pipeline;
1-13-the 6th induced draft fan; 1-14-second exhaust pipe road; 1-15-first outlet pipe road;
1-16-pulsaire collector air outlet; 1-17-precipitator dust hopper;
1-18-the second wind stopping device; 1-19-precipitator dust discharge port; 1-20-second conveyor;
1-21-pulsaire collector; 1-22-hose connector; 1-23-drive-motor;
1-231-the second sprocket wheel; 1-24-chain; 2-waste gas recovery purification system;
2-1-the first tracheae; 2-2-the 5th induced draft fan; 2-3-first class purification tower;
2-4-the first spray header; 2-5-the second dilute sulphuric acid pipe; 2-6-the first spray pump;
2-7-the first dilute sulphuric acid pipe; 2-8-the second spray header; 2-9-the second spray pump;
2-10-dilute sulfuric acid solution case; 2-101-dilute sulphuric acid import; 2-11-the 3rd dilute sulphuric acid pipe;
2-12-the 4th dilute sulphuric acid pipe; 2-13-secondary purification tower; 2-131-relief outlet;
2-14-venting port; 2-151-overhead gage; 2-152-lower baffle plate;
2-153-baffle plate; 2-16-dilute sulphuric acid adds entrance; 2-17-dilute sulphuric acid arranges mouth outward;
2-18-dilute sulfuric acid solution porthole; 2-19-waste pipe; 2-201-cold water;
Porthole under 2-23-spray header; Porthole on 2-24-spray header; 3-residual neat recovering system;
3-2-pump; 3-3-waste heat recovery tank; 3-4-the 3rd spray header;
3-5-the first water outlet; 3-6-the second water outlet; A 3-7-shower;
3-8-the 4th induced draft fan; 3-91-upper liquid level porthole; 3-92-lower liquid level porthole;
3-10-the 3rd spray pump; 3-11-the first pipeline; 3-12-heat supply water pipe;
3-13-main jet shower pipe; 3-14-insulating pipe; 4-dehumidification system;
4-1-the first temperature transmitter; 4-2-the 3rd temperature transmitter; 4-3-the 4th temperature transmitter;
4-4-the 5th temperature transmitter; 4-5-the second temperature transmitter; 4-6-the second MOD;
4-7-the first MOD; 4-8-the 3rd MOD; 4-9-gas blower;
4-10-venting; 4-12-the first fly-ash separator; 4-13-vent gas tower;
4-141-wind mixed chamber; 4-142-combustion chamber; 4-15-the second fly-ash separator;
4-16-drying tower; 4-17-the 3rd fly-ash separator; 4-18-washing, purifying tower;
4-181-pure qi (oxygen) air outlet; 4-19-the first induced draft fan; 4-20-the second induced draft fan;
4-21-the 3rd wind stopping device; 4-22-tank; 4-23-centrifugal atomizer;
4-24-second pipe; 4-25-the 3rd induced draft fan; 4-26-water tank;
4-27-the first cleaning circulation pump; 4-28-the first sluicing pipe; 4-29-the 4th spray header;
4-30-the second sluicing pipe; 4-31-the second cleaning circulation pump; 4-32-the 3rd spray header;
4-33-the 3rd sluicing pipe; 4-34-the 4th wind stopping device; 4-35-tremie pipe;
4-36-reciprocating sieve; 4-37-worm conveyor; 4-38-motor;
4-39-material toggling pawl; 4-40-air intake passage; 4-41-air outlet;
4-42-the 5th spray header; 5-material storing tank; 6-strainer;
6-1-feed-pipe; 6-2-filtering net bung; 6-3-filtration gantry;
6-4-cabinet; 6-5-feed liquid collection box; 6-6-discharge nozzle;
6-7-axle sleeve; 6-8-the second belt pulley; 6-9-belt;
6-10-the first belt pulley; 6-11-the first drive-motor; 6-12-filtering net;
6-13-axle; 6-14-chassis lid; 6-15-the first vision slit;
6-16-the second vision slit; 7-blowdown pipe; 8-liquid material exports utilidor;
9-heat-conducting oil furnace; 10-reactor; 11-material buffer tank;
11-1-material inlet; 11-2-lower discharge port; 11-3-slag-drip opening;
12-liquid material transferpump; 13-liquid material stirred pot; 14-liquid material hold-up vessel;
15-liquid material recycle pump; 16-feeding pump; 17-first-hand movable valve;
18-second-hand movable valve; 19-liquid material transport pipe; 20-auxiliary material charging machine.
Embodiment
As shown in Figure 1, the present invention includes reactor 10, to the raw material feeding system 1 of reactor 10 material loading with provide the heat-conducting oil furnace 9 of intensification thermal source for the reaction of reactor 10, the oil outlet of described heat-conducting oil furnace 9 is communicated with the oil-in of reactor 10, the oil-in of described heat-conducting oil furnace 9 is communicated with the oil outlet of reactor 10, described reactor 10 exports utilidor 8 by blowdown pipe 7 and liquid material and is connected with material buffer tank 11, the discharge port of described material buffer tank 11 is connected with material storing tank 5 by strainer 6, the discharge port of described material storing tank 5 is connected with for the dehumidification system 4 to dry materials, described dehumidification system 4 is connected with the venting port of heat-conducting oil furnace 9, the air outlet of described material buffer tank 11 is connected with the residual neat recovering system 3 for hot gas in recovered material surge tank 11, described residual neat recovering system 3 is connected with raw material feeding system 1, described residual neat recovering system 3 is also connected with the waste gas recovery purification system 2 for reclaiming clean waste gas, described waste gas recovery purification system 2 is connected with raw material feeding system 1.
As depicted in figs. 1 and 2, described raw material feeding system 1 comprises the first transfer roller 1-1, second conveyor 1-20, one-level knife mill 1-2, 3rd transfer roller 1-3, secondary knife mill 1-4, first wind stopping device 1-9, 6th induced draft fan 1-13, pulsaire collector 1-21 and the assorted tripping device of material, described first transfer roller 1-1 is obliquely installed, described second conveyor 1-20 is horizontally disposed with, the feed end of described second conveyor 1-20 is positioned at below the discharge end of the first transfer roller 1-1, the discharge end of described second conveyor 1-20 is positioned at above the chute import of one-level knife mill 1-2, the discharge port of described one-level knife mill 1-2 is positioned at above the feed end of the 3rd transfer roller 1-3, described 3rd transfer roller 1-3 is horizontally disposed with, the discharge end of described 3rd transfer roller 1-3 is positioned at above the chute import of secondary knife mill 1-4, the discharge port of described secondary knife mill 1-4 to be communicated with and by expect to mix tripping device by the impurity in the raw material after shredding through secondary knife mill 1-4 and dust separation out by the mix opening for feed 1-61 of tripping device of Material pipeline 1-12 and described material, the mix discharge port 1-62 of tripping device of described material is communicated with the opening for feed of the first wind stopping device 1-9, the discharge port of described first wind stopping device 1-9 is connected with hopper 1-10, the bottom of described hopper 1-10 is connected with hose connector 1-22, the end of described hose connector 1-22 is communicated with the opening for feed of reactor 10, described hopper 1-10 is provided with coupled logical supplying hot water water pipe 1-101 and first outlet pipe 1-102, the link position of described supplying hot water water pipe 1-101 and hopper 1-10 is higher than the link position of first outlet pipe 1-102 and hopper 1-10, the blast inlet of described 6th induced draft fan 1-13 is communicated with by the mix air outlet 1-52 of tripping device of first outlet pipe road 1-15 and described material, the air outlet of described 6th induced draft fan 1-13 is communicated with the inlet mouth of pulsaire collector 1-21 by second exhaust pipe road 1-14.
As Fig. 1, Fig. 2, shown in Fig. 5 and Fig. 6, described material tripping device of mixing comprises casing 1-5, described opening for feed 1-61 is arranged on the upper end of casing 1-5, described discharge port 1-62 is arranged on the bottom of casing 1-5, described air outlet 1-52 is arranged on the top of casing 1-5, described air outlet 1-52 is positioned at the below of opening for feed 1-61, mesh roller 1-7 is installed in described casing 1-5, the inwall of described casing 1-5 is positioned at the rubber baffle 1-8 being provided with below mesh roller 1-7 and being close to mesh roller 1-7, one of described mesh roller 1-7 rectifies air outlet 1-52, the other end of described mesh roller 1-7 is installed with the first sprocket wheel 1-71, on described casing 1-5 and near the first sprocket wheel 1-71 place, drive-motor 1-23 is installed, the output shaft of described drive-motor 1-23 is installed with the second sprocket wheel 1-231, described first sprocket wheel 1-71 and the second sprocket wheel 1-231 is connected to form sprocket wheel chain gear by chain 1-24.Drive-motor 1-23 drives the second sprocket wheel 1-231 to rotate, the first sprocket wheel 1-71 is driven to rotate by chain 1-24 transmission, because the first sprocket wheel 1-71 is fixedly mounted on mesh roller 1-7, so mesh roller 1-7 rotates, under the effect of the 6th induced draft fan 1-13, by opening for feed 1-61 enter in casing 1-5 through secondary chopping raw material in impurity and dust be pumped, and raw material is adsorbed on mesh roller 1-7, the raw material be adsorbed in the process that mesh roller 1-7 rotates on mesh roller 1-7 is stopped by rubber baffle 1-8 and scrapes off, and enters bottom casing 1-5.
As shown in Figure 1, Figure 2 with shown in Fig. 5, in the present embodiment, the bottom of described casing 1-5 is provided with porthole 1-51, is convenient to the blanking situation of observing raw material.Precipitator dust hopper 1-17 bottom described pulsaire collector 1-21 and be provided with the second wind stopping device 1-18 between precipitator dust discharge port 1-19, the opening for feed of described second wind stopping device 1-18 is communicated with the bottom of precipitator dust hopper 1-17, and the discharge port of described second wind stopping device 1-18 is communicated with the top of precipitator dust discharge port 1-19; Second wind stopping device 1-18 is arranged so that pulsaire collector 1-21 is in non-stop-machine situation, can discharge the dust bottom pulsaire collector 1-21 by precipitator dust discharge port 1-19.The chute outlet of described secondary knife mill 1-4 is the discharge port of secondary knife mill 1-4, the chute outlet of described Material pipeline 1-12 and secondary knife mill 1-4; Such can make whole feeding system formed enclosed space, not only make material loading effective, and can space be saved.
The raw material feeding system 1 of the present embodiment in use, raw material delivers in one-level knife mill 1-2 by the first transfer roller 1-1 and second conveyor 1-20, one-level knife mill 1-2 is to after raw material chopping, delivered in secondary knife mill 1-4 by the 3rd transfer roller 1-3 and shred, entered in the discharge port below secondary knife mill 1-4 by the raw material after again shredding; Under the effect of the 6th induced draft fan 1-13, because the discharge port of secondary knife mill 1-4 is communicated with the opening for feed 1-61 of the assorted tripping device of material, so raw material sucks from the discharge port of secondary knife mill 1-4, be transported to opening for feed 1-61 place by Material pipeline 1-12, entered in casing 1-5 by opening for feed 1-61 raw material.Because of the effect of the 6th induced draft fan 1-13, the part material after secondary chopping is attracted on mesh roller 1-7, and the impurity in raw material and dust are extracted out by the first outlet pipe road 1-15 be communicated with air outlet 1-52 under the 6th induced draft fan 1-13 effect.The impurity be drawn out of and dust enter in pulsaire collector 1-21 through the 6th induced draft fan 1-13 by second exhaust pipe road 1-14, impurity and dust are after treatment, gas is discharged by pulsaire collector air outlet 1-16, impurity and dust enter in the second wind stopping device 1-18 by the precipitator dust hopper 1-17 bottom pulsaire collector 1-21, then discharge through precipitator dust discharge port 1-19.Mesh roller 1-7 is under the effect of drive-motor 1-23, by the second sprocket wheel 1-231, chain 1-24 and the first sprocket wheel 1-71 driven rotary, be adsorbed in the process that raw material on mesh roller 1-7 rotates at mesh roller 1-7, stopped by rubber baffle 1-8 casing 1-5 inwall being close to mesh roller 1-7 and scrape off, raw material enters bottom casing 1-5.Raw material continues to decline, and then enter in the first wind stopping device 1-9, in the first wind stopping device 1-9 rotary course, raw material is isolated to the below of the first wind stopping device 1-9, and raw material freely falling body enters in hopper 1-10, is declined by hopper 1-10.
Material falls under gravity, when falling to the water outlet of supplying hot water water pipe 1-101, hot water in supplying hot water water pipe 1-101 forms the water smoke of injection under the effect of water outlet areolation, material in declining is carried out fully spraying soaking mixing, soak mixed material to decline along hose connector 1-22, again fully mix in decline process, mixed material enters in reactor 10.When material and hot water do not enter reactor 10, water vapour in reactor 10 and ammonia are risen by hose connector 1-22 under the effect of the 4th induced draft fan 3-8, when rising to first outlet pipe 1-102 position, enter in first outlet pipe 1-102 after areolation by first outlet pipe 1-102 mouth of pipe place, the water vapour in reactor 10 and ammonia are admitted in first class purification tower 2-3 and purify.When material and hot water enter reactor 10, the water vapour that hot water in water vapour in same reactor 10, injection produces and part ammonia (now part ammonia absorbs by water) are under the effect of the 4th induced draft fan 3-8, enter in first outlet pipe 1-102 after water vapour and the areolation of part ammonia by first outlet pipe 1-102 mouth of pipe place, the water vapour in reactor 10 and ammonia are admitted in first class purification tower 2-3 and purify.
As shown in figures 1 and 3, air outlet, the top place of described material buffer tank 11 is provided with multiple material inlet 11-1, one end that described material inlet 11-1 and liquid material export utilidor 8 is communicated with, the other end that described liquid material exports utilidor 8 is communicated with one end of blowdown pipe 7, and the other end of described blowdown pipe 7 stretches in reactor 10; The bottom of described material buffer tank 11 is provided with top discharge mouth 11-1, lower discharge port 11-2 and slag-drip opening 11-3.In the present embodiment, material inlet 11-1 is arranged on air outlet, the top place near material buffer tank 11, the material (mainly hydrolyzed polyacrylonitrile ammonium salt) that can enter in material buffer tank 11 is like this more, material after buffering can be led to strainer 6 and filter by top discharge mouth 11-1 and lower discharge port 11-2, and linen-cotton class impurity in material buffer tank 11 can eject by slag-drip opening 11-3.
As shown in figures 1 and 3, described residual neat recovering system 3 comprises waste heat recovery tank 3-3, 3rd spray pump 3-10 and main jet shower pipe 3-13, the bottom of described waste heat recovery tank 3-3 is provided with liquid level porthole 3-91 and lower liquid level porthole 3-92, described waste heat recovery tank 3-3 is communicated with the air outlet at material buffer tank 11 top by insulating pipe 3-14, described insulating pipe 3-14 to stretch in waste heat recovery tank 3-3 and is positioned at the bottom of waste heat recovery tank 3-3, the bottom of described waste heat recovery tank 3-3 is provided with the first water outlet 3-5 and the second water outlet 3-6, described second water outlet 3-6 is through pipeline, pump 3-2 is connected with supplying hot water water pipe 1-101 with the heat supply water pipe 3-12 leading to workshop, described first water outlet 3-5 is connected with the import of the 3rd spray pump 3-10 by the first pipeline 3-11, the outlet of described 3rd spray pump 3-10 is connected with one end of main jet shower pipe 3-13, the other end of described main jet shower pipe 3-13 is provided with the coupled logical shower 3-7 in one end, the other end of described shower 3-7 stretches in insulating pipe 3-14, stretch on the shower 3-7 in insulating pipe 3-14 and the 3rd spray header 3-4 is installed.
As shown in figures 1 and 3, in the present embodiment, the quantity of described shower 3-7 is three, and three shower 3-7 from top to bottom set gradually, the quantity of described 3rd spray header 3-4 is multiple, and water can be made fully to be absorbed by the heat that the ammonia of High Temperature High Pressure and heat steam carry.
As shown in figures 1 and 3, in the present embodiment, be loaded with cold water 2-201 in described waste heat recovery tank 3-3, described insulating pipe 3-14 passes the inlet mouth of waste heat recovery tank 3-3 and lower end is stretched in cold water 2-201, waste gas can be made fully to contact with cold water 20-1 and carry out heat exchange.
The residual neat recovering system 3 of the present embodiment in use, in the material in material buffer tank 11 after pressure release, go out from the air outlet, top of material buffer tank 11, entered in waste heat recovery tank 3-3 by insulating pipe 3-14 by a large amount of heat steams and ammonia.When heat steam and ammonia are about to the inlet mouth entering waste heat recovery tank 3-3 top, start the 3rd spray pump 3-10,3rd spray pump 3-10 aspirates the cold water held in waste heat recovery tank 3-3, then the 3rd spray header 3-4 ejects a large amount of cold mist under the effect of the 3rd spray pump 3-10, and now the amount of heat that the ammonia in insulating pipe 3-14 and hot steam carry fully absorbs by water smoke.Insulating pipe 3-14 leads to the bottom of waste heat recovery tank 3-3 always, and part ammonia and heat steam are absorbed heat by the cold water in waste heat recovery tank 3-3, and a small amount of ammonia and heat steam lead to first class purification tower 2-3 by the first tracheae 2-1 and purify.In this process, observe the liquid level of water in waste heat recovery tank 3-3 by upper liquid level porthole 3-91 and lower liquid level porthole 3-92, make insulating pipe 3-14 stretch in water, such ammonia and heat steam can carry out sufficient heat exchange with water.
As shown in Figure 1 and Figure 7, described strainer 6 comprises cabinet 6-4, feed liquid collection box 6-5, filter gantry 6-3 and the first drive-motor 6-11, the top of described cabinet 6-4 is provided with chassis lid 6-14, described feed liquid collection box 6-5 is arranged in cabinet 6-4, the bottom of described feed liquid collection box 6-5 is provided with discharge nozzle 6-6 integrated with it, described filtration gantry 6-3 is arranged in feed liquid collection box 6-5, in described filtration gantry 6-3, filtering net 6-12 is detachably installed, the top of described filtration gantry 6-3 is provided with filtering net bung 6-2, the top of described cabinet 6-4 is provided through filtering net bung 6-2 and stretches into the feed-pipe 6-1 in filtering net 6-12, the bottom of described filtration gantry 6-3 is fixed with axle 6-13, the end of described axle 6-13 passes feed liquid collection box 6-5 and is rotationally connected with feed liquid collection box 6-5, the bottom of described feed liquid collection box 6-5 is fixed with axle sleeve 6-7, described axle 6-13 is through axle sleeve 6-7, the end winding support of described axle 6-13 has the second belt pulley 6-8, described first drive-motor 6-11 is fixed on cabinet 6-4, the output shaft of described first drive-motor 6-11 is installed with the first belt pulley 6-10, described first belt pulley 6-10 is connected to form belt transport by belt 6-9 and the second belt pulley 6-8, described feed-pipe 6-1 is all communicated with lower discharge port 11-2 with top discharge mouth 11-1 by liquid material transport pipe 19, and described discharge nozzle 6-6 is communicated with the opening for feed of material storing tank 5.In the present embodiment, the top of filtering net bung 6-2 is provided with the second vision slit 6-16, the top of chassis lid 6-14 is provided with the first vision slit 6-15, the second vision slit 6-16 and the first vision slit 6-15 be convenient to observe liquid material number and filtration in expect slag number and filter effect how.
The strainer 6 of the present embodiment in use, liquid material enters through feed-pipe 6-1, moving axis 6-13 is with to rotate by the first drive-motor 6-11, belt 6-9 and the second belt pulley 6-8, and then drive and filter gantry 6-3 and rotate together with filtering net 6-12 liquid material is filtered out, the liquid material filtered out is discharged through discharge nozzle 6-6.
As shown in figures 1 and 3, described waste gas recovery purification system 2 comprises first class purification tower 2-3, first spray pump 2-6, secondary purification tower 2-13, second spray pump 2-9 and dilute sulfuric acid solution case 2-10, the inlet mouth of described first class purification tower 2-3 is communicated with the air outlet at waste heat recovery tank 3-3 top with the first tracheae 2-1 by the 5th induced draft fan 2-2, the air outlet place of described 5th induced draft fan 2-2 is connected with waste pipe 2-19, described waste pipe 2-19 is communicated with first outlet pipe 1-102 by the 4th induced draft fan 3-8, overhead gage 2-151 for changing exhaust gas flow direction and lower baffle plate 2-152 is installed in described first class purification tower 2-3, the outlet of described first class purification tower 2-3 and the inlet communication of the first spray pump 2-6, the outlet of described first spray pump 2-6 is connected with the first dilute sulphuric acid pipe 2-7, the end of described first dilute sulphuric acid pipe 2-7 to be stretched in first class purification tower 2-3 and is positioned at above lower baffle plate 2-152, described first dilute sulphuric acid pipe 2-7 is also connected with end and stretches in first class purification tower 2-3 and the second dilute sulphuric acid pipe 2-5 be positioned at above overhead gage 2-151, stretch on the first dilute sulphuric acid pipe 2-7 in first class purification tower 2-3 and the second dilute sulphuric acid pipe 2-5 and the first spray header 2-4 is all installed, the top of described first class purification tower 2-3 to be stretched in secondary purification tower 2-13 and is communicated with secondary purification tower 2-13, in the top of described first class purification tower 2-3, baffle plate 2-153 is installed, the top of described secondary purification tower 2-13 is provided with venting port 2-14, described secondary purification tower 2-13 is communicated with dilute sulfuric acid solution case 2-10 by the 3rd dilute sulphuric acid pipe 2-11, described dilute sulfuric acid solution case 2-10 is enclosed construction, the sidewall of described dilute sulfuric acid solution case 2-10 is provided with dilute sulphuric acid import 2-101, the bottom of described dilute sulfuric acid solution case 2-10 and the inlet communication of the second spray pump 2-9, the outlet of described second spray pump 2-9 is connected with the 4th dilute sulphuric acid pipe 2-12, the end of described 4th dilute sulphuric acid pipe 2-12 to be stretched in secondary purification tower 2-13 and is positioned at above first class purification tower 2-3, stretch on the 4th dilute sulphuric acid pipe 2-12 in secondary purification tower 2-13 and the second spray header 2-8 is installed.
As shown in figures 1 and 3, the bottom of described first class purification tower 2-3 is provided with dilute sulphuric acid and adds entrance 2-16, the bottom sidewall of described first class purification tower 2-3 is provided with dilute sulphuric acid and arranges mouth 2-17 outward, the sidewall of described first class purification tower 2-3 to be disposed with from the bottom to top under dilute sulfuric acid solution porthole 2-18, spray header porthole 2-24 on porthole 2-23 and spray header, under described spray header, porthole 2-23 is positioned at the top of overhead gage 2-151, and on described spray header, porthole 2-24 is positioned at the top of lower baffle plate 2-152; Under spray header on porthole 2-23 and spray header porthole 2-24 for observing the response situation of the first spray header 2-4 and dilute sulphuric acid.The bottom of described secondary purification tower 2-13 is provided with relief outlet 2-131, is convenient to the dilute sulphuric acid in secondary purification tower 2-13 to discharge.
In the present embodiment, the quantity of described first spray header 2-4 and the second spray header 2-8 is multiple, is beneficial to waste gas and dilute sulphuric acid fully reacts, to improve waste-gas cleaning effect.Described overhead gage 2-151, lower baffle plate 2-152 and baffle plate 2-153 are shutter, by regulation shutter blade, waste gas not only can be made to change direction, also can make air-flow just to the first spray header 2-4, to improve decontamination effect improving.
The waste gas recovery purification system 2 of the present embodiment in use, waste gas in waste heat recovery tank 3-3 is under the effect of the 5th induced draft fan 2-2, first class purification tower 2-3 is entered by the first tracheae 2-1 be connected with the 5th induced draft fan 2-2, simultaneously, start the first spray pump 2-6, the exit of the dilute sulphuric acid of first class purification tower 2-3 inner bottom part from first class purification tower 2-3 is extracted out, run to the first spray header 2-4 place be positioned at above overhead gage 2-151, the dilute sulphuric acid mist that first spray header 2-4 produces, carries out reactive absorption with the exhaust flow risen; Remainder of exhaust gas after reactive absorption continues to rise, be positioned at the dilute sulphuric acid sprayed through the first spray header 2-4 above lower baffle plate 2-152 and carry out reactive absorption with being transported to, overhead gage 2-151 and lower baffle plate 2-152 is for changing the air flow line of waste gas, to make waste gas and the abundant reactive absorption of dilute sulphuric acid, a small amount of waste gas after first class purification tower 2-3 purifies continues to rise in first class purification tower 2-3 to enter secondary purification tower 2-13.When waste gas rises to the second spray header 2-8 place soon, start the second spray pump 2-9, dilute sulphuric acid in secondary purification tower 2-13 enters in dilute sulfuric acid solution case 2-10 by the 3rd dilute sulphuric acid pipe 2-11, dilute sulphuric acid is transported to the second spray header 2-8 place by the 4th dilute sulphuric acid pipe 2-12, baffle plate 2-153 is for changing the air flow line of waste gas, the atomization shape dilute sulphuric acid mist that second spray header 2-8 produces, fully absorbed by remaining waste gas, clean gas is discharged by venting port 2-14.In like manner, the waste gas entered from waste pipe 2-19 is also purified completely.
As shown in Figure 1 and Figure 4, described dehumidification system 4 comprises the first fly-ash separator 4-12, vent gas tower 4-13, hotblast stove, second fly-ash separator 4-15, drying tower 4-16, 3rd fly-ash separator 4-17 and washing, purifying tower 4-18, described first fly-ash separator 4-12 is connected with heat-conducting oil furnace 9 by the first induced draft fan 4-19, the air outlet of described heat-conducting oil furnace 9 is communicated with the inlet mouth of the first induced draft fan 4-19, the air outlet of described first induced draft fan 4-19 is communicated with the inlet mouth of the first fly-ash separator 4-12, the air outlet of described first fly-ash separator 4-12 is by the second induced draft fan 4-20, first MOD 4-7, first temperature transmitter 4-1 is communicated with the inlet mouth of pipeline with vent gas tower 4-13, the wind mixed chamber 4-141 of described hotblast stove is by the second MOD 4-6 and the pipeline communication between the first temperature transmitter 4-1 and the first MOD 4-7, air outlet bottom the combustion chamber 4-142 of described hotblast stove is connected with gas blower 4-9, the bottom of described wind mixed chamber 4-141 and be provided with the second temperature transmitter 4-5 near 4-142 place, combustion chamber, the top of described wind mixed chamber 4-141 and be provided with the 3rd temperature transmitter 4-2 near air outlet place of wind mixed chamber, the bottom of described wind mixed chamber 4-141 is provided with the 3rd MOD 4-8, described wind mixed chamber air outlet is connected with the inlet mouth of the second fly-ash separator 4-15 by the 4th temperature transmitter 4-3, dust outlet bottom described second fly-ash separator 4-15 is connected with the 3rd wind stopping device 4-21, the discharge port of described 3rd wind stopping device 4-21 stretches in setting tank 4-22 thereunder, the air outlet of described second fly-ash separator 4-15 is connected with the inlet mouth of drying tower 4-16 by the 5th temperature transmitter 4-4, the top of described drying tower 4-16 is provided with centrifugal atomizer 4-23, the second pipe 4-24 that the inlet mouth of described 3rd fly-ash separator 4-17 is stretched in drying tower 4-16 by one end is communicated with drying tower 4-16, described 3rd fly-ash separator 4-17 is communicated with the bottom of washing, purifying tower 4-18 by the 3rd induced draft fan 4-25, the bottom of described washing, purifying tower 4-18 is also connected with the first cleaning circulation pump 4-27 by water tank 4-26, the outlet of described first cleaning circulation pump 4-27 is connected with end and stretches into the first sluicing pipe 4-28 in the middle part of washing, purifying tower 4-18, stretch on the first sluicing pipe 4-28 in washing, purifying tower 4-18 and the 4th spray header 4-29 is installed, the top of described washing, purifying tower 4-18 is provided with pure qi (oxygen) air outlet 4-181, described centrifugal atomizer 4-23 is by liquid material transferpump 12, liquid material stirred pot 13, liquid material recycle pump 15, liquid material hold-up vessel 14 is connected with centrifugal atomizer 4-23 opening for feed with feeding pump 16, the import of described liquid material transferpump 12 and the outlet of material storing tank 5, the outlet of described liquid material transferpump 12 and the inlet communication of liquid material stirred pot 13, the outlet of described liquid material stirred pot 13 and the inlet communication of liquid material recycle pump 15, the outlet of described liquid material recycle pump 15 is by pipeline and first-hand movable valve 17 inlet communication with liquid material hold-up vessel 14, the outlet of described liquid material hold-up vessel 14 is communicated with the opening for feed of centrifugal atomizer 4-23, described liquid material stirred pot 13 is connected with auxiliary material charging machine 20 by pipeline, the import of described liquid material stirred pot 13 is by second-hand's movable valve 18 and the pipeline communication between liquid material recycle pump 15 and first-hand movable valve 17.
As shown in Figure 1 and Figure 4, the quantity of described 3rd fly-ash separator 4-17 is two, two the 3rd fly-ash separator 4-17 are all communicated with drying tower 4-16 by second pipe 4-24, dust outlet bottom described 3rd fly-ash separator 4-17 is connected with the 4th wind stopping device 4-34, the discharge port of described 4th wind stopping device 4-34 is connected with tremie pipe 4-35, is provided with reciprocating sieve 4-36 below the end of described tremie pipe 4-35; The below of described drying tower 4-16 is provided with worm conveyor 4-37, and the opening for feed of described worm conveyor 4-37 is positioned at below the discharge port bottom drying tower 4-16, and the discharge port of described worm conveyor 4-37 is positioned at the top of reciprocating sieve 4-36; The bottom of described drying tower 4-16 is provided with motor 4-38, and the output shaft of described motor 4-38 stretches in drying tower 4-16 and end is provided with material toggling pawl 4-39.Discharged by hydrolyzed polyacrylonitrile ammonium salt after drying in drying tower 4-16 by installing the material toggling pawl 4-39 that driven by motor 4-38 in the bottom of drying tower 4-16, discharge is convenient, and discharge is thorough.By installing worm conveyor 4-37 in the below of drying tower 4-16, reciprocating sieve 4-36 is installed below the discharge port of worm conveyor 4-37, directly outer draining into can to the problem of hydrolyzed polyacrylonitrile ammonium salt generation pollution on ground to not only solve hydrolyzed polyacrylonitrile ammonium salt in prior art, and the hydrolyzed polyacrylonitrile ammonium salt that the discharge port bottom drying tower 4-16 is discharged directly can fall into the opening for feed of reciprocating sieve 4-36, the hydrolyzed polyacrylonitrile ammonium salt of appropriate particle size can be sifted out by reciprocating sieve 4-36, directly packing sack can be placed in the bottom of reciprocating sieve 4-36, required personnel are less, working efficiency is high, improve the working environment of workers.
As shown in Figure 1 and Figure 4, in the present embodiment, described first sluicing pipe 4-28 is connected with one end and stretches into the second sluicing pipe 4-30 in washing, purifying tower 4-18, stretch into the second sluicing pipe 4-30 end in washing, purifying tower 4-18 and the 5th spray header 4-42 is installed; Described first sluicing pipe 4-28 is also communicated with the top of washing, purifying tower 4-18 with the 3rd sluicing pipe 4-33 by the second cleaning circulation pump 4-31, and described 3rd sluicing pipe 4-33 stretches into the top of washing, purifying tower 4-18 and end is provided with the 3rd spray header 4-32; By arranging the second cleaning circulation pump 4-31 and the 3rd spray header 4-32, the further washing and recycling to ammonia in gas gas can be realized.The quantity of described 4th spray header 4-29, the 5th spray header 4-42 and the 3rd spray header 4-32 is multiple, improves spraying effect.
As shown in Figure 1 and Figure 4, in the present embodiment, the top center of described drying tower 4-16 is provided with air intake passage 4-40 and air outlet 4-41, described air intake passage 4-40 is arranged on outside drying tower 4-16, described air outlet 4-41 is arranged in drying tower 4-16, the shape of described air outlet 4-41 is inverted trapezoidal shape, described air outlet 4-41 is the inlet mouth of drying tower 4-16, described air outlet 4-41 communicates with air intake passage 4-40, described centrifugal atomizer 4-23 is by the top of wire rope suspensioning at drying tower 4-16, described centrifugal atomizer 4-23 is positioned at the center of air outlet 4-41.First the hot gas of the second fly-ash separator 4-15 out after dedusting enter air intake passage 4-40, then air outlet 4-41 is entered, because air outlet 4-41 is inverted trapezoidal shape and centrifugal atomizer 4-23 is positioned at center, so hot blast can surround being formed through centrifugal atomizer 4-23 hydrolyzed polyacrylonitrile ammonium salt out, be beneficial to rapid drying.
As shown in Figure 1 and Figure 4, in the present embodiment, the top of described drying tower 4-16 is provided with venting 4-10, can discharge instantaneous pressure in drying tower 4-16, avoids in drying tower 4-16 on fire.Described first temperature transmitter 4-1, the second temperature transmitter 4-5, the 3rd temperature transmitter 4-2, the 4th temperature transmitter 4-3 and the 5th temperature transmitter 4-4 are TMT180F-J integrative temperature transmitter.Described centrifugal atomizer 4-23 is JGF electric high-speed centrifugal atomizer, and result of use is good.Described first fly-ash separator 4-12, the second fly-ash separator 4-15 and the 3rd fly-ash separator 4-17 are tornado dust collector, good dedusting effect.
The dehumidification system 4 of the present embodiment in use, suppose that the temperature of demand in drying tower 4-16 is 480 DEG C, the 3rd temperature transmitter 4-2 now on wind mixed chamber 4-141 is responding to the temperature at 4-141 air outlet place of wind mixed chamber, suppose that the temperature in the 4-142 of combustion chamber is 550 DEG C, now check the temperature of display on the 3rd temperature transmitter 4-2, the temperature of demand in the contrast temperature of wind mixed chamber 4-141 and drying tower 4-16, if temperature is too high in wind mixed chamber 4-141, Non-follow control second MOD 4-6, the amount temperature of the hot blast from heat-conducting oil furnace 9 out after the first fly-ash separator 4-12 dedusting (now suppose be 300 DEG C) out entering wind mixed chamber 4-141 hot blast from heat-conducting oil furnace 9 after the first fly-ash separator 4-12 dedusting is controlled by the second MOD 4-6.When the second MOD 4-6 is opened to upper limit position, check the temperature of display on the 4th temperature transmitter 4-3, when the temperature of display on the 4th temperature transmitter 4-3 does not also drop to the temperature of demand in drying tower 4-16, Non-follow control the 3rd MOD 4-8, controls by the 3rd MOD 4-8 the amount that extraneous cold air enters wind mixed chamber 4-141.When the 3rd MOD 4-8 is opened to upper limit position, check the temperature of display on the 5th temperature transmitter 4-4, when the temperature of temperature still higher than demand in drying tower 4-16 of display on the 5th temperature transmitter 4-4, the running speed controlling gas blower 4-9 enters air combustion-supporting in the 4-142 of combustion chamber to reduce, thus reduces the combustionvelocity in the 4-142 of combustion chamber.In the process, contrast the temperature that the second temperature transmitter 4-5 and the first temperature transmitter 4-1 shows, Non-follow control first MOD 4-7 is to control the hot gas amount of discharging through vent gas tower 4-13.On the contrary, if during temperature (temperature namely wind mixed chamber 4-141 in lower than the temperature of drying tower 4-16 in demand) of temperature lower than demand in drying tower 4-16 of display on the 3rd temperature transmitter 4-2, Non-follow control second MOD 4-6 all opens and Non-follow control the 3rd MOD 4-8 Close All, second temperature transmitter 4-5 display digit and the first temperature transmitter 4-1 display digit make temperature comparisons, Non-follow control first MOD 4-7 Close All, to meet the temperature requirements in drying tower 4-16.
Principle of work of the present invention is: raw material (waste and old clothing) is delivered in one-level knife mill 1-2 by the first transfer roller 1-1 and second conveyor 1-20, be delivered in secondary knife mill 1-4 through the 3rd transfer roller 1-3 again, after raw material is shredded, under the effect of the 6th induced draft fan 1-13, enter in the assorted tripping device of material by Material pipeline 1-12 from the opening for feed 1-61 of the assorted tripping device of material, the material entered in the assorted tripping device of material is declined by hopper 1-10 through the first wind stopping device 1-9 in casing 1-5, then enters in reactor 10.Now, dust gas in the assorted tripping device of material is under the effect of the 6th induced draft fan 1-13, enter in pulsaire collector 1-21 by air outlet 1-52, after dust gas is processed in pulsaire collector 1-21, discharge from pulsaire collector air outlet 1-16.At the same time, the deep fat after heating up is sent from the oil outlet of heat-conducting oil furnace by heat-conducting oil furnace 9, and thermal oil, after the zone of heating of reactor 10, prolongs oil pipeline and to enter in heat-conducting oil furnace heat temperature raising again from the oil-in of heat-conducting oil furnace.
Material in reactor 10 is after high temperature high pressure process, exporting utilidor 8 by liquid material enters in material buffer tank 11 from material inlet 11-1, then liquid material exports from the top discharge mouth 11-1 of material buffer tank 11 and lower discharge port 11-2, entering after strainer 6 filters through liquid material transport pipe 19 sends in material storing tank 5, export from the exit bottom material storing tank 5 again, enter in liquid material stirred pot 13 by Cemented filling, in liquid material stirred pot 13, add auxiliary material by auxiliary material charging machine 20, then carry out the process that stirs.
The liquid material handled well enters in liquid material hold-up vessel 14 by liquid material recycle pump 15 and pipeline, liquid material again through feeding pump 16 by Cemented filling in centrifugal atomizer 4-23.Now, the hot blast (hot blast is the hot gas of the generation that Combustion of Hot Air Furnace coal produces and the hot blast of heat-conducting oil furnace 9 intensification generation) meeting demand in drying tower 4-16 delivers in drying tower 4-16 by hot air duct at the downward hot gas duct of effect of the 3rd induced draft fan 4-25 by hotblast stove, liquid material after centrifugal atomizer 4-23 process declines at drying tower 4-16 inner drying, then enter in worm conveyor 4-37 by the discharge port of drying tower 4-16, dried material is exported by the effect of worm conveyor 4-37 and enters in reciprocating sieve 4-36, the finished product are formed after reciprocating sieve 4-36 process, product enters in packing bag from the discharge port bottom reciprocating sieve 4-36.At the same time, hot gas in drying tower 4-16 is drawn out of through second pipe 4-24 due to the effect of the 3rd induced draft fan 4-25, hot gas prolongs pipeline and enters in washing, purifying tower 4-18 after the 3rd fly-ash separator 4-17 process, and hot gas is discharged from the pure qi (oxygen) air outlet 4-181 at washing, purifying tower 4-18 top.
At the same time, the liquid material steam in material buffer tank 11 and ammonia enter in waste heat recovery tank 3-3 by insulating pipe 3-14, and hot gas leads in the cold water at material buffer tank 11 end by insulating pipe 3-14, and most hot steam and ammonia are absorbed by cold water.Simultaneously, 3rd spray pump 3-10 starts, the water of waste heat recovery tank 3-3 inner bottom part is transported to the 3rd spray header 3-4 place, the hot steam that waste heat recovery tank 3-3 inlet mouth place enters by the acid solution water smoke that the 3rd spray header 3-4 sprays and ammonia carry out spray absorber, and unabsorbed waste gas enters in first class purification tower 2-3 under the effect of the 5th induced draft fan 2-2.
Meanwhile, first spray pump 2-6 starts, liquid acid in first class purification tower 2-3 is transported to the first spray header 2-4 place in scavenging tower by the first dilute sulphuric acid pipe 2-7 and the second dilute sulphuric acid pipe 2-5, waste gas is in the process risen, the liquid acid be atomized absorbs fully, then remaining waste gas continues to rise to secondary purification tower 2-13 in first class purification tower 2-3, now the second spray pump 2-9 starts, liquid acid in secondary purification tower 2-13 is extracted in dilute sulfuric acid solution case 2-10, liquid acid by Cemented filling to the second spray header 2-8 place, the waste gas of remnants absorbs by atomized liquid acid that the second spray header 2-8 produces completely, purified gas is discharged from venting port 2-14.
The above; it is only preferred embodiment of the present invention; not the present invention is imposed any restrictions, every above embodiment is done according to the technology of the present invention essence any simple modification, change and equivalent structure transformation, all still belong in the protection domain of technical solution of the present invention.
Claims (8)
1. a hydrolyzed polyacrylonitrile ammonium salt production system, it is characterized in that: comprise reactor (10), raw material feeding system (1) to reactor (10) material loading and the reaction for reactor (10) provide the heat-conducting oil furnace (9) of intensification thermal source, the oil outlet of described heat-conducting oil furnace (9) is communicated with the oil-in of reactor (10), the oil-in of described heat-conducting oil furnace (9) is communicated with the oil outlet of reactor (10), described reactor (10) exports utilidor (8) by blowdown pipe (7) and liquid material and is connected with material buffer tank (11), the discharge port of described material buffer tank (11) is connected with material storing tank (5) by strainer (6), the discharge port of described material storing tank (5) is connected with for the dehumidification system (4) to dry materials, described dehumidification system (4) is connected with the venting port of heat-conducting oil furnace (9), the air outlet of described material buffer tank (11) is connected with the residual neat recovering system (3) for recovered material surge tank (11) interior hot gas, described residual neat recovering system (3) is connected with raw material feeding system (1), described residual neat recovering system (3) is also connected with the waste gas recovery purification system (2) for reclaiming clean waste gas, described waste gas recovery purification system (2) is connected with raw material feeding system (1),
Described raw material feeding system (1) comprises the first transfer roller (1-1), second conveyor (1-20), one-level knife mill (1-2), 3rd transfer roller (1-3), secondary knife mill (1-4), first wind stopping device (1-9), 6th induced draft fan (1-13), pulsaire collector (1-21) and the assorted tripping device of material, described first transfer roller (1-1) is obliquely installed, described second conveyor (1-20) is horizontally disposed with, the feed end of described second conveyor (1-20) is positioned at below the discharge end of the first transfer roller (1-1), the discharge end of described second conveyor (1-20) is positioned at above the chute import of one-level knife mill (1-2), the discharge port of described one-level knife mill (1-2) is positioned at above the feed end of the 3rd transfer roller (1-3), described 3rd transfer roller (1-3) is horizontally disposed with, the discharge end of described 3rd transfer roller (1-3) is positioned at above the chute import of secondary knife mill (1-4), the discharge port of described secondary knife mill (1-4) to be communicated with and by expect to mix tripping device by the impurity in the raw material after secondary knife mill (1-4) shreds and dust separation out by the mix opening for feed (1-61) of tripping device of Material pipeline (1-12) and described material, the mix discharge port (1-62) of tripping device of described material is communicated with the opening for feed of the first wind stopping device (1-9), the discharge port of described first wind stopping device (1-9) is connected with hopper (1-10), the bottom of described hopper (1-10) is connected with hose connector (1-22), the end of described hose connector (1-22) is communicated with the opening for feed of reactor (10), described hopper (1-10) is provided with coupled logical supplying hot water water pipe (1-101) and first outlet pipe (1-102), the link position of described supplying hot water water pipe (1-101) and hopper (1-10) is higher than the link position of first outlet pipe (1-102) with hopper (1-10), the blast inlet of described 6th induced draft fan (1-13) is communicated with by the mix air outlet (1-52) of tripping device of first outlet pipe road (1-15) and described material, the air outlet of described 6th induced draft fan (1-13) is communicated with the inlet mouth of pulsaire collector (1-21) by second exhaust pipe road (1-14),
Air outlet, the top place of described material buffer tank (11) is provided with multiple material inlet (11-1), one end that described material inlet (11-1) and liquid material export utilidor (8) is communicated with, the other end that described liquid material exports utilidor (8) is communicated with one end of blowdown pipe (7), and the other end of described blowdown pipe (7) stretches in reactor (10); The bottom of described material buffer tank (11) is provided with top discharge mouth (11-1), lower discharge port (11-2) and slag-drip opening (11-3).
2. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 1, it is characterized in that: described material tripping device of mixing comprises casing (1-5), described opening for feed (1-61) is arranged on the upper end of casing (1-5), described discharge port (1-62) is arranged on the bottom of casing (1-5), described air outlet (1-52) is arranged on the top of casing (1-5), described air outlet (1-52) is positioned at the below of opening for feed (1-61), mesh roller (1-7) is installed in described casing (1-5), on the inwall of described casing (1-5) and be positioned at mesh roller (1-7) below the rubber baffle (1-8) be close to mesh roller (1-7) is installed, one of described mesh roller (1-7) is rectified air outlet (1-52), the other end of described mesh roller (1-7) is installed with the first sprocket wheel (1-71), described casing (1-5) is upper and close first sprocket wheel (1-71) place is provided with drive-motor (1-23), the output shaft of described drive-motor (1-23) is installed with the second sprocket wheel (1-231), described first sprocket wheel (1-71) and the second sprocket wheel (1-231) are connected to form sprocket wheel chain gear by chain (1-24).
3. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 1, it is characterized in that: described residual neat recovering system (3) comprises waste heat recovery tank (3-3), 3rd spray pump (3-10) and main jet shower pipe (3-13), the bottom of described waste heat recovery tank (3-3) is provided with liquid level porthole (3-91) and lower liquid level porthole (3-92), described waste heat recovery tank (3-3) is communicated with by the air outlet of insulating pipe (3-14) with material buffer tank (11) top, described insulating pipe (3-14) to stretch in waste heat recovery tank (3-3) and is positioned at the bottom of waste heat recovery tank (3-3), the bottom of described waste heat recovery tank (3-3) is provided with the first water outlet (3-5) and the second water outlet (3-6), described second water outlet (3-6) is through pipeline, pump (3-2) is connected with supplying hot water water pipe (1-101) with the heat supply water pipe (3-12) leading to workshop, described first water outlet (3-5) is connected by the import of the first pipeline (3-11) with the 3rd spray pump (3-10), the outlet of described 3rd spray pump (3-10) is connected with one end of main jet shower pipe (3-13), the other end of described main jet shower pipe (3-13) is provided with the coupled logical shower (3-7) in one end, the other end of described shower (3-7) stretches in insulating pipe (3-14), stretch on the shower (3-7) in insulating pipe (3-14) and the 3rd spray header (3-4) is installed.
4. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 1, it is characterized in that: described strainer (6) comprises cabinet (6-4), feed liquid collection box (6-5), filter gantry (6-3) and the first drive-motor (6-11), the top of described cabinet (6-4) is provided with chassis lid (6-14), described feed liquid collection box (6-5) is arranged in cabinet (6-4), the bottom of described feed liquid collection box (6-5) is provided with discharge nozzle integrated with it (6-6), described filtration gantry (6-3) is arranged in feed liquid collection box (6-5), in described filtration gantry (6-3), filtering net (6-12) is detachably installed, the top of described filtration gantry (6-3) is provided with filtering net bung (6-2), the top of described cabinet (6-4) is provided through filtering net bung (6-2) and stretches into the feed-pipe (6-1) in filtering net (6-12), the bottom of described filtration gantry (6-3) is fixed with axle (6-13), the end of described axle (6-13) passes feed liquid collection box (6-5) and is rotationally connected with feed liquid collection box (6-5), the bottom of described feed liquid collection box (6-5) is fixed with axle sleeve (6-7), described axle (6-13) is through axle sleeve (6-7), the end winding support of described axle (6-13) has the second belt pulley (6-8), described first drive-motor (6-11) is fixed on cabinet (6-4), the output shaft of described first drive-motor (6-11) is installed with the first belt pulley (6-10), described first belt pulley (6-10) is connected to form belt transport by belt (6-9) and the second belt pulley (6-8), described feed-pipe (6-1) is all communicated with lower discharge port (11-2) with top discharge mouth (11-1) by liquid material transport pipe (19), and described discharge nozzle (6-6) is communicated with the opening for feed of material storing tank (5).
5. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 3, it is characterized in that: described waste gas recovery purification system (2) comprises first class purification tower (2-3), first spray pump (2-6), secondary purification tower (2-13), second spray pump (2-9) and dilute sulfuric acid solution case (2-10), the inlet mouth of described first class purification tower (2-3) is communicated with the air outlet of the first tracheae (2-1) with waste heat recovery tank (3-3) top by the 5th induced draft fan (2-2), the air outlet place of described 5th induced draft fan (2-2) is connected with waste pipe (2-19), described waste pipe (2-19) is communicated with first outlet pipe (1-102) by the 4th induced draft fan (3-8), overhead gage (2-151) for changing exhaust gas flow direction and lower baffle plate (2-152) are installed in described first class purification tower (2-3), the outlet of described first class purification tower (2-3) and the inlet communication of the first spray pump (2-6), the outlet of described first spray pump (2-6) is connected with the first dilute sulphuric acid pipe (2-7), the end of described first dilute sulphuric acid pipe (2-7) to be stretched in first class purification tower (2-3) and is positioned at lower baffle plate (2-152) top, described first dilute sulphuric acid pipe (2-7) is also connected with end and stretches in first class purification tower (2-3) and the second dilute sulphuric acid pipe (2-5) being positioned at overhead gage (2-151) top, stretch on the first dilute sulphuric acid pipe (2-7) in first class purification tower (2-3) and the second dilute sulphuric acid pipe (2-5) and the first spray header (2-4) is all installed, the top of described first class purification tower (2-3) to be stretched in secondary purification tower (2-13) and is communicated with secondary purification tower (2-13), in the top of described first class purification tower (2-3), baffle plate (2-153) is installed, the top of described secondary purification tower (2-13) is provided with venting port (2-14), described secondary purification tower (2-13) is communicated with dilute sulfuric acid solution case (2-10) by the 3rd dilute sulphuric acid pipe (2-11), described dilute sulfuric acid solution case (2-10) is enclosed construction, the sidewall of described dilute sulfuric acid solution case (2-10) is provided with dilute sulphuric acid import (2-101), the bottom of described dilute sulfuric acid solution case (2-10) and the inlet communication of the second spray pump (2-9), the outlet of described second spray pump (2-9) is connected with the 4th dilute sulphuric acid pipe (2-12), the end of described 4th dilute sulphuric acid pipe (2-12) to be stretched in secondary purification tower (2-13) and is positioned at first class purification tower (2-3) top, stretch on the 4th dilute sulphuric acid pipe (2-12) in secondary purification tower (2-13) and the second spray header (2-8) is installed.
6. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 5, it is characterized in that: the bottom of described first class purification tower (2-3) is provided with dilute sulphuric acid and adds entrance (2-16), the bottom sidewall of described first class purification tower (2-3) is provided with dilute sulphuric acid and arranges mouth (2-17) outward, the sidewall of described first class purification tower (2-3) is disposed with dilute sulfuric acid solution porthole (2-18) from the bottom to top, porthole (2-24) on porthole (2-23) and spray header under spray header, under described spray header, porthole (2-23) is positioned at the top of overhead gage (2-151), on described spray header, porthole (2-24) is positioned at the top of lower baffle plate (2-152), the bottom of described secondary purification tower (2-13) is provided with relief outlet (2-131).
7. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 1, it is characterized in that: described dehumidification system (4) comprises the first fly-ash separator (4-12), vent gas tower (4-13), hotblast stove, second fly-ash separator (4-15), drying tower (4-16), 3rd fly-ash separator (4-17) and washing, purifying tower (4-18), described first fly-ash separator (4-12) is connected with heat-conducting oil furnace (9) by the first induced draft fan (4-19), the air outlet of described heat-conducting oil furnace (9) is communicated with the inlet mouth of the first induced draft fan (4-19), the air outlet of described first induced draft fan (4-19) is communicated with the inlet mouth of the first fly-ash separator (4-12), the air outlet of described first fly-ash separator (4-12) is by the second induced draft fan (4-20), first MOD (4-7), first temperature transmitter (4-1) is communicated with the inlet mouth of pipeline with vent gas tower (4-13), the wind mixed chamber (4-141) of described hotblast stove is by the second MOD (4-6) and the pipeline communication that is positioned between the first temperature transmitter (4-1) and the first MOD (4-7), the air outlet of the bottom, combustion chamber (4-142) of described hotblast stove is connected with gas blower (4-9), the bottom of described wind mixed chamber (4-141) and be provided with the second temperature transmitter (4-5) near combustion chamber (4-142) place, the top of described wind mixed chamber (4-141) and be provided with the 3rd temperature transmitter (4-2) near air outlet place of wind mixed chamber, the bottom of described wind mixed chamber (4-141) is provided with the 3rd MOD (4-8), described wind mixed chamber air outlet is connected with the inlet mouth of the second fly-ash separator (4-15) by the 4th temperature transmitter (4-3), the dust outlet of described second fly-ash separator (4-15) bottom is connected with the 3rd wind stopping device (4-21), the discharge port of described 3rd wind stopping device (4-21) stretches in setting tank thereunder (4-22), the air outlet of described second fly-ash separator (4-15) is connected with the inlet mouth of drying tower (4-16) by the 5th temperature transmitter (4-4), the top of described drying tower (4-16) is provided with centrifugal atomizer (4-23), the second pipe (4-24) that the inlet mouth of described 3rd fly-ash separator (4-17) is stretched in drying tower (4-16) by one end is communicated with drying tower (4-16), described 3rd fly-ash separator (4-17) is communicated with the bottom of washing, purifying tower (4-18) by the 3rd induced draft fan (4-25), the bottom of described washing, purifying tower (4-18) is also connected with the first cleaning circulation pump (4-27) by water tank (4-26), the outlet of described first cleaning circulation pump (4-27) is connected with the first sluicing pipe (4-28) that washing, purifying tower (4-18) middle part is stretched in end, stretch on the first sluicing pipe (4-28) in washing, purifying tower (4-18) and the 4th spray header (4-29) is installed, the top of described washing, purifying tower (4-18) is provided with pure qi (oxygen) air outlet (4-181), described centrifugal atomizer (4-23) is by liquid material transferpump (12), liquid material stirred pot (13), liquid material recycle pump (15), liquid material hold-up vessel (14) is connected with centrifugal atomizer (4-23) opening for feed with feeding pump (16), the import of described liquid material transferpump (12) and the outlet of material storing tank (5), the outlet of described liquid material transferpump (12) and the inlet communication of liquid material stirred pot (13), the outlet of described liquid material stirred pot (13) and the inlet communication of liquid material recycle pump (15), the outlet of described liquid material recycle pump (15) is by pipeline and first-hand movable valve (17) inlet communication with liquid material hold-up vessel (14), the outlet of described liquid material hold-up vessel (14) is communicated with the opening for feed of centrifugal atomizer (4-23), described liquid material stirred pot (13) is connected with auxiliary material charging machine (20) by pipeline, the import of described liquid material stirred pot (13) is by second-hand's movable valve (18) and the pipeline communication that is positioned between liquid material recycle pump (15) and first-hand movable valve (17).
8. according to a kind of hydrolyzed polyacrylonitrile ammonium salt production system according to claim 7, it is characterized in that: the quantity of described 3rd fly-ash separator (4-17) is two, two the 3rd fly-ash separators (4-17) are all communicated with drying tower (4-16) by second pipe (4-24), the dust outlet of described 3rd fly-ash separator (4-17) bottom is connected with the 4th wind stopping device (4-34), the discharge port of described 4th wind stopping device (4-34) is connected with tremie pipe (4-35), is provided with reciprocating sieve (4-36) below the end of described tremie pipe (4-35); The below of described drying tower (4-16) is provided with worm conveyor (4-37), the opening for feed of described worm conveyor (4-37) is positioned at below the discharge port of drying tower (4-16) bottom, and the discharge port of described worm conveyor (4-37) is positioned at the top of reciprocating sieve (4-36); The bottom of described drying tower (4-16) is provided with motor (4-38), and the output shaft of described motor (4-38) stretches in drying tower (4-16) and end is provided with material toggling pawl (4-39).
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| CN110343289B (en) * | 2019-07-30 | 2022-04-12 | 石家庄华信泥浆助剂有限公司 | Heating treatment method and equipment in process of generating ammonium salt from environment-friendly waste acrylic fibers |
| CN111495046B (en) * | 2020-04-24 | 2021-10-19 | 安徽晋煤中能化工股份有限公司 | Online cleaning device of low pressure fuel gas filter |
| CN117535123B (en) * | 2023-10-31 | 2024-06-21 | 浙江中科沃尔德生物科技有限公司 | System for preparing natural gas by high-efficiency biomass medium-high temperature anaerobic fermentation and process for preparing natural gas by using same |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1470590A (en) * | 2003-06-20 | 2004-01-28 | 鞍钢附属企业公司化工厂 | Apparatus and process for producing efficient water reducing agent |
| CN1884912A (en) * | 2006-07-06 | 2006-12-27 | 上海金州环境工程有限公司 | Medical refuse incineration process and system equipment therefor |
| JP2011236337A (en) * | 2010-05-11 | 2011-11-24 | Mitsubishi Rayon Co Ltd | Thermal decomposition device and thermal decomposition method of resin |
| CN102660038A (en) * | 2012-04-26 | 2012-09-12 | 山东大学 | Method for preparing hydrolytic polyacrylonitrile filtrate reducer by organic diamine cross-linking agent |
| CN202658121U (en) * | 2012-07-18 | 2013-01-09 | 天津市静海县桂春工贸有限公司 | Waste acrylic fiber hydrolyzing kettle |
| CN102994055A (en) * | 2012-12-27 | 2013-03-27 | 河北华运鸿业化工有限公司 | Method for preparing filtrate reducer hydrolyzed polyacrylonitrile for drilling fluid |
| CN103224246A (en) * | 2013-05-09 | 2013-07-31 | 中化重庆涪陵化工有限公司 | Chemical gypsum-to-ammonium sulfate reaction slurry concentration, waste heat recovery and waste ammonia recovery method |
-
2014
- 2014-04-19 CN CN201410161349.3A patent/CN103923242B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1470590A (en) * | 2003-06-20 | 2004-01-28 | 鞍钢附属企业公司化工厂 | Apparatus and process for producing efficient water reducing agent |
| CN1884912A (en) * | 2006-07-06 | 2006-12-27 | 上海金州环境工程有限公司 | Medical refuse incineration process and system equipment therefor |
| JP2011236337A (en) * | 2010-05-11 | 2011-11-24 | Mitsubishi Rayon Co Ltd | Thermal decomposition device and thermal decomposition method of resin |
| CN102660038A (en) * | 2012-04-26 | 2012-09-12 | 山东大学 | Method for preparing hydrolytic polyacrylonitrile filtrate reducer by organic diamine cross-linking agent |
| CN202658121U (en) * | 2012-07-18 | 2013-01-09 | 天津市静海县桂春工贸有限公司 | Waste acrylic fiber hydrolyzing kettle |
| CN102994055A (en) * | 2012-12-27 | 2013-03-27 | 河北华运鸿业化工有限公司 | Method for preparing filtrate reducer hydrolyzed polyacrylonitrile for drilling fluid |
| CN103224246A (en) * | 2013-05-09 | 2013-07-31 | 中化重庆涪陵化工有限公司 | Chemical gypsum-to-ammonium sulfate reaction slurry concentration, waste heat recovery and waste ammonia recovery method |
Non-Patent Citations (3)
| Title |
|---|
| 刘延栋.腈纶废料的综合应用.《回收高分子材料的工艺与配方》.化学工业出版社,2002,第138-140页. * |
| 张淑英.水解聚丙烯腈-铵盐生产过程中的尾气回收与再利用.《工业设计》.2011,(第06期),第162页. * |
| 来胜利.水解聚丙烯腈铵盐.《常用精细化工产品研制与生产》.陕西科学技术出版社,2006,第462-464页. * |
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