CN104628512A - System for preparing industrial refined naphthalene - Google Patents
System for preparing industrial refined naphthalene Download PDFInfo
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- CN104628512A CN104628512A CN201510091423.3A CN201510091423A CN104628512A CN 104628512 A CN104628512 A CN 104628512A CN 201510091423 A CN201510091423 A CN 201510091423A CN 104628512 A CN104628512 A CN 104628512A
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- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 title claims abstract description 138
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 54
- 239000007788 liquid Substances 0.000 claims abstract description 19
- 238000005406 washing Methods 0.000 claims abstract description 18
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 claims abstract description 12
- 238000004806 packaging method and process Methods 0.000 claims abstract description 11
- 238000003860 storage Methods 0.000 claims abstract description 7
- 238000002425 crystallisation Methods 0.000 claims description 107
- 230000008025 crystallization Effects 0.000 claims description 104
- 238000000034 method Methods 0.000 claims description 28
- 238000001816 cooling Methods 0.000 claims description 11
- 238000013022 venting Methods 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000003638 chemical reducing agent Substances 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 238000005303 weighing Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 13
- 239000002994 raw material Substances 0.000 abstract description 6
- 239000002912 waste gas Substances 0.000 abstract description 2
- 239000002351 wastewater Substances 0.000 abstract description 2
- 239000003921 oil Substances 0.000 abstract 2
- 125000005306 thianaphthenyl group Chemical group 0.000 abstract 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 abstract 1
- 230000018044 dehydration Effects 0.000 abstract 1
- 239000000295 fuel oil Substances 0.000 abstract 1
- 239000011265 semifinished product Substances 0.000 abstract 1
- 239000000463 material Substances 0.000 description 11
- 229910000975 Carbon steel Inorganic materials 0.000 description 6
- 239000010962 carbon steel Substances 0.000 description 6
- 238000010792 warming Methods 0.000 description 5
- 239000003513 alkali Substances 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 4
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 3
- 241000534944 Thia Species 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 3
- 150000002469 indenes Chemical class 0.000 description 3
- 238000005554 pickling Methods 0.000 description 3
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000010306 acid treatment Methods 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 206010067482 No adverse event Diseases 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- XTXZAZCDNWMPRK-UHFFFAOYSA-N naphthalene;phenol Chemical compound OC1=CC=CC=C1.C1=CC=CC2=CC=CC=C21 XTXZAZCDNWMPRK-UHFFFAOYSA-N 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 150000003222 pyridines Chemical class 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 125000002256 xylenyl group Chemical class C1(C(C=CC=C1)C)(C)* 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a system for preparing industrial refined naphthalene. The system comprises a liquid industrial naphthalene storage tank, an intermediate crystallizing tank, a primary crystallizing tank, a primary fraction slot, a secondary fraction slot, a semi-finished product slot, a high-grade crystallizing tank, a finished product slot, a finished naphthalene packaging device, a warm water slot, an exhaust washing tower, a phenol oil storage tank, and a dehydration tower. The waste gas, waste water and water residue cannot be produced in the production process, and the environment cannot be polluted; the product quality is stable, and the purity of the produced industrial naphthalene can achieve 99.4%; through the adoption of the system, a large amount of naphthalene oil thianaphthenyl can be obtained and used as a raw material for extracting thianaphthenyl or used as fuel oil.
Description
Technical field
The present invention relates to a kind of system prepared industrial refined naphthalene and produce, belong to chemical field.
Background technology
Regardless of which kind of cut, all containing acidic components, basic component, neutral component etc.The boiling point wherein had is close in the boiling point of naphthalene, and being easily mixed in NAPTHALENE FLAKES. (INDUSTRIAL GRADE） during rectifying affects quality product.For ensureing the quality of NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, all need to carry out alkali cleaning and cleanup acid treatment before rectifying.Be called through the cut of alkali cleaning and cleanup acid treatment and wash naphthalene and wash two mixed cuts or washed phenol naphthalene and wash tri-mixed fractions.These have washed the raw material that cut all can do NAPTHALENE FLAKES. (INDUSTRIAL GRADE） production.
But in actual production, if with only carrying out rectifying through low-priced mixed fraction of washing without pickling, pyridine bases in raw material proceeds in carbolic oil and rectifying Residual oil (washing oil) mostly, and only have about 0.1% in NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, substantially the quality of naphthalene is not affected, therefore the cut rectifying manufacture naphthalene after some coke-oven plant employing alkali cleaning, to cutting out carbolic oil, washing oil, then carries out pickling extraction heavy pridine bases class respectively.When industrial scale is less do not need extract pyridines product time, also can without sulfuric acid scrubbing.
Because current NAPTHALENE FLAKES. (INDUSTRIAL GRADE） major part is used for drawing phthalic anhydride, the process modification of producing along with phthalic anhydride, the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） containing a small amount of unsaturated compound, all has no adverse effects to phthalic anhydride quality product and catalyst catalyst performance.Therefore, present many coke-oven plants all use and only extract NAPTHALENE FLAKES. (INDUSTRIAL GRADE） through the feedstock fraction of alkali cleaning.
Refined naphthalene is thick naphthalene (NAPTHALENE FLAKES. (INDUSTRIAL GRADE）) the naphthalene product containing naphthalene more than 98.45% that purification is obtained further.Impurity in NAPTHALENE FLAKES. (INDUSTRIAL GRADE） mainly naphthalene boiling point close to naphthane, thia indenes, xylenol etc.In order to manufacture the higher refined naphthalene of purity, the naphthalene physical properties different from these impurity fusing points will be utilized to be separated, or utilize chemical process to change their chemical constitution, mainly contain melting-crystallization process, hydrogenation method, pickling distillation method, solvent crystallization, subliming method and formaldehyde method etc.
Summary of the invention
For prior art Problems existing, the invention provides a kind of system preparing industrial refined naphthalene, this system comprises liquid industrial naphthalene hold-up vessel, intermediate crystallization case, primary crystallization case, elementary cut groove, intermediate cut groove, work in-process groove, senior crystallization case, pan tank, finished product naphthalene packaging facilities, warm water tank, exhaust washing column, carbolic oil hold-up vessel, dehydration reaction tower.Wherein, the discharge port of liquid industrial naphthalene storage tank lower end connects the feeding mouth of dehydration reaction tower by pipeline, the discharge port of dehydration reaction tower connects the first feeding mouth of primary crystallization case by pipeline, first discharge port of primary crystallization case connects the first opening for feed of elementary cut groove by pipeline, second discharge port of primary crystallization case connects the first opening for feed of intermediate cut groove by pipeline, 3rd discharge port of primary crystallization case connects the first feeding mouth of work in-process groove by pipeline, the discharge port of middle rank cut groove connects the second feeding mouth of primary crystallization case by pipeline, first discharge port of middle rank crystallization case connects the second feeding mouth of elementary cut groove by pipeline, second discharge port of middle rank crystallization case connects the second feeding mouth of intermediate cut groove by pipeline, 3rd discharge port of middle rank crystallization case connects the feeding mouth of water reducer production equipment by pipeline, the discharge port of elementary cut groove connects the feeding mouth of intermediate crystallization case by pipeline, the carbolic oil discharge port of elementary cut groove connects the feeding mouth of carbolic oil hold-up vessel by pipeline, first discharge port of senior crystallization case connects the 3rd feeding mouth of intermediate cut groove by pipeline, second discharge port of senior crystallization case connects the second feeding mouth of work in-process groove by pipeline, 3rd discharge port of senior crystallization case connects the feeding mouth of pan tank by pipeline, the discharge port of work in-process groove connects the feeding mouth of senior crystallization case by pipeline, the discharge port of pan tank connects the feeding mouth of finished product naphthalene packaging facilities by pipeline, the water outlet of warm water tank connects the water inlet of intermediate crystallization case by pipeline, the water outlet of middle rank crystallization case connects the water inlet of senior crystallization case by pipeline, the water outlet of senior crystallization case connects the water inlet of liquid NAPTHALENE FLAKES. (INDUSTRIAL GRADE） hold-up vessel by pipeline, the water outlet of liquid industrial naphthalene hold-up vessel connects the water inlet of primary crystallization case by pipeline, the water outlet of primary crystallization case connects the water inlet of warm water tank by pipeline, the venting port of elementary cut groove connects the first inlet mouth of exhaust washing column by pipeline, the venting port of middle rank cut groove connects the second inlet mouth of exhaust washing column by pipeline, the venting port of work in-process groove connects the 3rd inlet mouth of exhaust washing column by pipeline, wherein, middle rank crystallization case adopts float valve case, 60 layers, float valve case layer, case footpath 800-1200mm, primary crystallization case adopts float valve case, 80 layers, float valve case layer, case footpath 1200-1600mm, arranges condensate cooler in intermediate crystallization case, primary crystallization case, and condensate cooler diameter is 1.2m, long is 3.376m, and cooling area is 122m
2naphthalene steam enters from condensate cooler jacking with the temperature of 138-140 DEG C, go out from condensate cooler underflow with the liquid of 80-90 DEG C again after heat exchange, water coolant enters at the bottom of condensate cooler, flow out with 40-50 DEG C of temperature from condensate cooler top, be provided with rotary drum crystallizer in intermediate crystallization case, primary crystallization case, rotary drum crystallizer diameter is 1.0m, long 1.0m, throughput 1-1.5t/h.
Naphthalene packaging facilities comprises scrapes naphthalene feeder, storage bin, automatic weighing parts, automatic bag feeding device, conveying belt, sealing machine, the trimmer of falling bag, weight tester, selection stacker crane, package speed=400 bag/time, capacity packing 8 tons/time.
Cooling or heating with the speed of 2.5 DEG C/h of primary crystallization case; Senior crystallization case is with the cooling of the speed of 6 DEG C/h or heating; Middle rank crystallization case is with the cooling of the speed of 0.5-2 DEG C/h or heating.
The invention has the advantages that:
1, refined naphthalene raw materials for production are single, do not need auxiliary material.Technical process and equipment and operate fairly simple, facility investment is few.
2, a large amount of naphtalene oil thia indenes can be obtained by this system, can as extracting the raw material of thia indenes or using as oil fuel.
3, only need the escort of pump, crystallisation by cooling, heating and melting during operation, process cost and energy consumption lower.
4, waste gas, waste water, waste residue is not produced in production process, environmentally safe.
5, raw material also can use fraction of naphthalene oil by NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, and quality product can be regulated with crystallisation cycle number of times, and handiness is larger.
6, constant product quality, NAPTHALENE FLAKES. (INDUSTRIAL GRADE） is produced per year can reach 50,000 tons, and its purity can reach 99.4%, and its ctystallizing point is not less than 78.3 DEG C, and non-volatile matter is not more than 0.03%, and ash content is not more than 0.01%.
7, for preventing naphthalene crystal from causing e-quipment and pipe to block, this device is provided with Warm water circulation system, with warm water as heat-eliminating medium.
Accompanying drawing explanation
Fig. 1 is the equipment schematic diagram preparing industrial refined naphthalene.
In figure: 1-liquid industrial naphthalene hold-up vessel, 2-primary crystallization case, 3-middle rank crystallization case, 4-elementary cut groove, 5-middle rank cut groove, 6-work in-process groove, the senior crystallization case of 7-, 8-pan tank, 9-water reducer production equipment, 10-naphthalene packaging facilities, 11-warm water tank, 12-are vented washing column, 13-carbolic oil hold-up vessel, 14 dehydration reaction towers.
Embodiment
The system that preparation industry refined naphthalene is as shown in Figure 1 produced, this system comprises liquid industrial naphthalene hold-up vessel, intermediate crystallization case, primary crystallization case, elementary cut groove, intermediate cut groove, work in-process groove, senior crystallization case, pan tank, finished product naphthalene packaging facilities, warm water tank, exhaust washing column, carbolic oil hold-up vessel, dehydration reaction tower etc.Wherein, the discharge port of liquid industrial naphthalene storage tank lower end connects the feeding mouth of dehydration reaction tower by pipeline, the discharge port of dehydration reaction tower connects the first feeding mouth of primary crystallization case by pipeline, first discharge port of primary crystallization case connects the first opening for feed of elementary cut groove by pipeline, second discharge port of primary crystallization case connects the first opening for feed of intermediate cut groove by pipeline, 3rd discharge port of primary crystallization case connects the first feeding mouth of work in-process groove by pipeline, the discharge port of middle rank cut groove connects the second feeding mouth of primary crystallization case by pipeline, first discharge port of middle rank crystallization case connects the second feeding mouth of elementary cut groove by pipeline, second discharge port of middle rank crystallization case connects the second feeding mouth of intermediate cut groove by pipeline, 3rd discharge port of middle rank crystallization case connects the feeding mouth of water reducer production equipment by pipeline, the discharge port of elementary cut groove connects the feeding mouth of intermediate crystallization case by pipeline, the carbolic oil discharge port of elementary cut groove connects the feeding mouth of carbolic oil hold-up vessel by pipeline, first discharge port of senior crystallization case connects the 3rd feeding mouth of intermediate cut groove by pipeline, second discharge port of senior crystallization case connects the second feeding mouth of work in-process groove by pipeline, 3rd discharge port of senior crystallization case connects the feeding mouth of pan tank by pipeline, the discharge port of work in-process groove connects the feeding mouth of senior crystallization case by pipeline, the discharge port of pan tank connects the feeding mouth of finished product naphthalene packaging facilities by pipeline, the water outlet of warm water tank connects the water inlet of intermediate crystallization case by pipeline, the water outlet of middle rank crystallization case connects the water inlet of senior crystallization case by pipeline, the water outlet of senior crystallization case connects the water inlet of liquid NAPTHALENE FLAKES. (INDUSTRIAL GRADE） hold-up vessel by pipeline, the water outlet of liquid industrial naphthalene hold-up vessel connects the water inlet of primary crystallization case by pipeline, the water outlet of primary crystallization case connects the water inlet of warm water tank by pipeline, the venting port of elementary cut groove connects the first inlet mouth of exhaust washing column by pipeline, the venting port of middle rank cut groove connects the second inlet mouth of exhaust washing column by pipeline, the venting port of work in-process groove connects the 3rd inlet mouth of exhaust washing column by pipeline, wherein, middle rank crystallization case adopts float valve case, 60 layers, float valve case layer, case footpath 800-1200mm, primary crystallization case adopts float valve case, 80 layers, float valve case layer, case footpath 1200-1600mm, arranges condensate cooler in intermediate crystallization case, primary crystallization case, and condensate cooler diameter is 1.2m, long is 3.376m, and cooling area is 122m
2naphthalene steam enters from condensate cooler jacking with the temperature of 138-140 DEG C, go out from condensate cooler underflow with the liquid of 80-90 DEG C again after heat exchange, water coolant enters at the bottom of condensate cooler, flow out with 40-50 DEG C of temperature from condensate cooler top, be provided with rotary drum crystallizer in intermediate crystallization case, primary crystallization case, rotary drum crystallizer diameter is 1.0m, long 1.0m, throughput 1-1.5t/h.
By store in NAPTHALENE FLAKES. (INDUSTRIAL GRADE） hold-up vessel higher than the liquid industrial naphthalene submerged pump suction primary crystallization case of 80 DEG C, under the cooling of cooler condenser, liquid industrial naphthalene is made to be reduced to 63 DEG C with the speed of 2.5 DEG C/h, release defective naphtalene oil to elementary cut groove, then intermediate crystallization case is warming up to 75 DEG C with the speed of 2.5 DEG C/h, release the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） of fusing again to intermediate cut groove, then primary crystallization case is continued to be warming up to remaining crystallization all to melt, the liquid product obtained is NAPTHALENE FLAKES. (INDUSTRIAL GRADE）, drains into work in-process groove; Work in-process groove intercrystalline point is 60 DEG C, temperature is that the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） of 85 DEG C enters senior crystallization case, when being cooled to about 48-49 DEG C with the speed of 6 DEG C/h, releasing ctystallizing point is that the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） of 50 DEG C is to pan tank, again senior crystallization case is warming up to 57-58 DEG C with the speed of 6 DEG C/h, release ctystallizing point be the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） of 60 DEG C in work in-process groove, be finally warming up to whole fusing, obtaining ctystallizing point is that the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） of 73 DEG C drains into intermediate cut groove.Elementary cut groove intercrystalline point is 50 DEG C, temperature is that the naphtalene oil of 80 DEG C loads intermediate crystallization case, with 0.5-2 DEG C/h speed be cooled to 28-32 DEG C time, releasing ctystallizing point is that the industrial naphtalene oil of 30-33 DEG C is to water reducer production equipment, then heat up, release the NAPTHALENE FLAKES. (INDUSTRIAL GRADE） extremely elementary cut groove that ctystallizing point is 40-45 DEG C, be finally warming up to whole fusing, obtaining ctystallizing point is that the naphtalene oil of 60 DEG C is to intermediate cut groove.Refined naphthalene in pan tank sends into naphthalene packaging facilities, together through automatic weighing, automatic bag feeding, conveying, sealing, the shaping of falling bag, weight detecting, selection stacker crane, is packaged into and sells finished product naphthalene.Package speed=400 bag/time, capacity packing 8 tons/time.
NAPTHALENE FLAKES. (INDUSTRIAL GRADE） hold-up vessel groove material is 20R OCr18Ni9; Middle rank crystallization box lumber matter is carbon steel, and specification is vertical; Primary crystallization box lumber matter is carbon steel, and specification is vertical; Elementary cut groove material is 20R OCr18Ni9; Middle rank cut groove material is 20R OCr18Ni; Work in-process groove material is Q235-A, and specification is horizontal; Senior crystallization box lumber matter is Q235-A, and specification is horizontal; Pan tank material is Q235-A, and specification is horizontal; Water reducer device material is carbon steel, and specification is vertical; Warm water tank material is Q235-A, and specification is horizontal; Exhaust washing column material is carbon steel, and specification is vertical; Carbolic oil hold-up vessel material is carbon steel, and specification is vertical; Dehydration reaction tower material is carbon steel, and specification is vertical.
Claims (3)
1. prepare a system for industrial refined naphthalene, it is characterized in that this system comprises liquid industrial naphthalene hold-up vessel, intermediate crystallization case, primary crystallization case, elementary cut groove, intermediate cut groove, work in-process groove, senior crystallization case, pan tank, finished product naphthalene packaging facilities, warm water tank, exhaust washing column, carbolic oil hold-up vessel, dehydration reaction tower etc., wherein, the discharge port of liquid industrial naphthalene storage tank lower end connects the feeding mouth of dehydration reaction tower by pipeline, the discharge port of dehydration reaction tower connects the first feeding mouth of primary crystallization case by pipeline, first discharge port of primary crystallization case connects the first opening for feed of elementary cut groove by pipeline, second discharge port of primary crystallization case connects the first opening for feed of intermediate cut groove by pipeline, 3rd discharge port of primary crystallization case connects the first feeding mouth of work in-process groove by pipeline, the discharge port of middle rank cut groove connects the second feeding mouth of primary crystallization case by pipeline, first discharge port of middle rank crystallization case connects the second feeding mouth of elementary cut groove by pipeline, second discharge port of middle rank crystallization case connects the second feeding mouth of intermediate cut groove by pipeline, 3rd discharge port of middle rank crystallization case connects the feeding mouth of water reducer production equipment by pipeline, the discharge port of elementary cut groove connects the feeding mouth of intermediate crystallization case by pipeline, the carbolic oil discharge port of elementary cut groove connects the feeding mouth of carbolic oil hold-up vessel by pipeline, first discharge port of senior crystallization case connects the 3rd feeding mouth of intermediate cut groove by pipeline, second discharge port of senior crystallization case connects the second feeding mouth of work in-process groove by pipeline, 3rd discharge port of senior crystallization case connects the feeding mouth of pan tank by pipeline, the discharge port of work in-process groove connects the feeding mouth of senior crystallization case by pipeline, the discharge port of pan tank connects the feeding mouth of finished product naphthalene packaging facilities by pipeline, the water outlet of warm water tank connects the water inlet of intermediate crystallization case by pipeline, the water outlet of middle rank crystallization case connects the water inlet of senior crystallization case by pipeline, the water outlet of senior crystallization case connects the water inlet of liquid NAPTHALENE FLAKES. (INDUSTRIAL GRADE） hold-up vessel by pipeline, the water outlet of liquid industrial naphthalene hold-up vessel connects the water inlet of primary crystallization case by pipeline, the water outlet of primary crystallization case connects the water inlet of warm water tank by pipeline, the venting port of elementary cut groove connects the first inlet mouth of exhaust washing column by pipeline, the venting port of middle rank cut groove connects the second inlet mouth of exhaust washing column by pipeline, the venting port of work in-process groove connects the 3rd inlet mouth of exhaust washing column by pipeline, wherein, middle rank crystallization case adopts float valve case, 60 layers, float valve case layer, case footpath 800-1200mm, primary crystallization case adopts float valve case, 80 layers, float valve case layer, case footpath 1200-1600mm, arranges condensate cooler in intermediate crystallization case, primary crystallization case, and condensate cooler diameter is 1.2m, long is 3.376m, and cooling area is 122m
2naphthalene steam enters from condensate cooler jacking with the temperature of 138-140 DEG C, go out from condensate cooler underflow with the liquid of 80-90 DEG C again after heat exchange, water coolant enters at the bottom of condensate cooler, flow out with 40-50 DEG C of temperature from condensate cooler top, be provided with rotary drum crystallizer in intermediate crystallization case, primary crystallization case, rotary drum crystallizer diameter is 1.0m, long 1.0m, throughput 1-1.5t/h.
2. system according to claim 1, it is characterized in that, naphthalene packaging facilities comprises scrapes naphthalene feeder, storage bin, automatic weighing parts, automatic bag feeding device, conveying belt, sealing machine, the trimmer of falling bag, weight tester, selection stacker crane, package speed=400 bag/time, capacity packing 8 tons/time.
3. use the system described in claim 1, it is characterized in that, cooling or heating with the speed of 2.5 DEG C/h of primary crystallization case; Senior crystallization case is with the cooling of the speed of 6 DEG C/h or heating; Middle rank crystallization case is with the cooling of the speed of 0.5-2 DEG C/h or heating.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113185379A (en) * | 2021-04-27 | 2021-07-30 | 河南鑫利安全技术服务有限责任公司 | Method for industrially preparing refined naphthalene and application |
| CN115417743A (en) * | 2022-08-25 | 2022-12-02 | 中建安装集团有限公司 | Fractional melting crystallization process for preparing refined naphthalene from industrial naphthalene |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101311150A (en) * | 2007-05-25 | 2008-11-26 | 宝山钢铁股份有限公司 | Process for producing high-purity naphthalin |
| CN201214027Y (en) * | 2008-03-21 | 2009-04-01 | 上海宝钢化工有限公司 | Crystallization box for refining naphthaline |
| CN101475435A (en) * | 2009-02-02 | 2009-07-08 | 济宁碳素工业总公司 | Method for preparing industrial naphthalin by single-furnace double-tower vacuum distillation |
| CN202700129U (en) * | 2012-07-23 | 2013-01-30 | 抚顺齐隆化工有限公司 | System for purifying naphthalin by crystalizing |
| CN104744205A (en) * | 2015-02-16 | 2015-07-01 | 陈国荣 | Industrial naphthalene refining system |
-
2015
- 2015-03-02 CN CN201510091423.3A patent/CN104628512B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101311150A (en) * | 2007-05-25 | 2008-11-26 | 宝山钢铁股份有限公司 | Process for producing high-purity naphthalin |
| CN201214027Y (en) * | 2008-03-21 | 2009-04-01 | 上海宝钢化工有限公司 | Crystallization box for refining naphthaline |
| CN101475435A (en) * | 2009-02-02 | 2009-07-08 | 济宁碳素工业总公司 | Method for preparing industrial naphthalin by single-furnace double-tower vacuum distillation |
| CN202700129U (en) * | 2012-07-23 | 2013-01-30 | 抚顺齐隆化工有限公司 | System for purifying naphthalin by crystalizing |
| CN104744205A (en) * | 2015-02-16 | 2015-07-01 | 陈国荣 | Industrial naphthalene refining system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113185379A (en) * | 2021-04-27 | 2021-07-30 | 河南鑫利安全技术服务有限责任公司 | Method for industrially preparing refined naphthalene and application |
| CN113185379B (en) * | 2021-04-27 | 2024-01-26 | 河南鑫利安全技术服务有限责任公司 | Industrial refined naphthalene preparing process and application |
| CN115417743A (en) * | 2022-08-25 | 2022-12-02 | 中建安装集团有限公司 | Fractional melting crystallization process for preparing refined naphthalene from industrial naphthalene |
| CN115417743B (en) * | 2022-08-25 | 2024-01-30 | 中建安装集团有限公司 | Fractional melting crystallization process for industrial naphthalene refined naphthalene |
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