CN207405109U - A kind of water-reducing agent production system - Google Patents
A kind of water-reducing agent production system Download PDFInfo
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- CN207405109U CN207405109U CN201721192274.0U CN201721192274U CN207405109U CN 207405109 U CN207405109 U CN 207405109U CN 201721192274 U CN201721192274 U CN 201721192274U CN 207405109 U CN207405109 U CN 207405109U
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- naphthalene
- water
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- pot
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 82
- 239000003638 chemical reducing agent Substances 0.000 title claims abstract description 30
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 311
- 238000006243 chemical reaction Methods 0.000 claims abstract description 74
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000007788 liquid Substances 0.000 claims abstract description 68
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 50
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 33
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000012546 transfer Methods 0.000 claims abstract description 20
- 235000011121 sodium hydroxide Nutrition 0.000 claims abstract description 17
- 238000001035 drying Methods 0.000 claims abstract description 14
- 230000003301 hydrolyzing effect Effects 0.000 claims abstract description 13
- 239000004566 building material Substances 0.000 claims abstract description 12
- 238000006482 condensation reaction Methods 0.000 claims abstract description 12
- 238000013329 compounding Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 55
- 230000000694 effects Effects 0.000 claims description 37
- PJKVFARRVXDXAD-UHFFFAOYSA-N 2-naphthaldehyde Chemical compound C1=CC=CC2=CC(C=O)=CC=C21 PJKVFARRVXDXAD-UHFFFAOYSA-N 0.000 claims description 27
- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- 239000012452 mother liquor Substances 0.000 claims description 16
- 238000012856 packing Methods 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 7
- 238000005516 engineering process Methods 0.000 abstract description 9
- 230000006872 improvement Effects 0.000 abstract description 6
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 238000009835 boiling Methods 0.000 description 36
- 239000000463 material Substances 0.000 description 36
- 238000002425 crystallisation Methods 0.000 description 35
- 238000000034 method Methods 0.000 description 35
- 238000001816 cooling Methods 0.000 description 28
- 239000007789 gas Substances 0.000 description 25
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 24
- 230000008025 crystallization Effects 0.000 description 23
- 239000000047 product Substances 0.000 description 23
- 230000007062 hydrolysis Effects 0.000 description 22
- 238000006460 hydrolysis reaction Methods 0.000 description 22
- 230000008569 process Effects 0.000 description 22
- 239000000243 solution Substances 0.000 description 21
- 238000010790 dilution Methods 0.000 description 16
- 239000012895 dilution Substances 0.000 description 16
- 238000004821 distillation Methods 0.000 description 16
- ZUQOBHTUMCEQBG-UHFFFAOYSA-N 4-amino-5-hydroxynaphthalene-1,7-disulfonic acid Chemical compound OS(=O)(=O)C1=CC(O)=C2C(N)=CC=C(S(O)(=O)=O)C2=C1 ZUQOBHTUMCEQBG-UHFFFAOYSA-N 0.000 description 14
- 239000003513 alkali Substances 0.000 description 13
- 239000011734 sodium Substances 0.000 description 13
- 229910052708 sodium Inorganic materials 0.000 description 13
- 238000002844 melting Methods 0.000 description 12
- 239000011265 semifinished product Substances 0.000 description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 11
- 230000008018 melting Effects 0.000 description 11
- 238000001914 filtration Methods 0.000 description 10
- 239000000843 powder Substances 0.000 description 10
- 238000012545 processing Methods 0.000 description 10
- 238000011084 recovery Methods 0.000 description 10
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 10
- 238000005406 washing Methods 0.000 description 10
- 230000004927 fusion Effects 0.000 description 9
- 150000002989 phenols Chemical class 0.000 description 9
- 239000007787 solid Substances 0.000 description 9
- 239000007921 spray Substances 0.000 description 9
- 238000003756 stirring Methods 0.000 description 9
- 238000005486 sulfidation Methods 0.000 description 9
- 239000013078 crystal Substances 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 8
- 238000003860 storage Methods 0.000 description 8
- 230000009615 deamination Effects 0.000 description 7
- 238000006481 deamination reaction Methods 0.000 description 7
- PSZYNBSKGUBXEH-UHFFFAOYSA-N naphthalene-1-sulfonic acid Chemical compound C1=CC=C2C(S(=O)(=O)O)=CC=CC2=C1 PSZYNBSKGUBXEH-UHFFFAOYSA-N 0.000 description 7
- 238000000967 suction filtration Methods 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- 229910021529 ammonia Inorganic materials 0.000 description 6
- IEXIPYCHASVPFD-UHFFFAOYSA-L disodium;7-hydroxynaphthalene-1,3-disulfonate Chemical compound [Na+].[Na+].C1=C(S([O-])(=O)=O)C=C(S([O-])(=O)=O)C2=CC(O)=CC=C21 IEXIPYCHASVPFD-UHFFFAOYSA-L 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- 239000000706 filtrate Substances 0.000 description 6
- KVBGVZZKJNLNJU-UHFFFAOYSA-N naphthalene-2-sulfonic acid Chemical compound C1=CC=CC2=CC(S(=O)(=O)O)=CC=C21 KVBGVZZKJNLNJU-UHFFFAOYSA-N 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- 238000006277 sulfonation reaction Methods 0.000 description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 5
- DGVVJWXRCWCCOD-UHFFFAOYSA-N naphthalene;hydrate Chemical compound O.C1=CC=CC2=CC=CC=C21 DGVVJWXRCWCCOD-UHFFFAOYSA-N 0.000 description 5
- 238000001556 precipitation Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- 235000010265 sodium sulphite Nutrition 0.000 description 5
- YWPOLRBWRRKLMW-UHFFFAOYSA-M sodium;naphthalene-2-sulfonate Chemical compound [Na+].C1=CC=CC2=CC(S(=O)(=O)[O-])=CC=C21 YWPOLRBWRRKLMW-UHFFFAOYSA-M 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 5
- 238000007664 blowing Methods 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000012065 filter cake Substances 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 230000020477 pH reduction Effects 0.000 description 4
- 229910052939 potassium sulfate Inorganic materials 0.000 description 4
- 235000011151 potassium sulphates Nutrition 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 238000010792 warming Methods 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 150000004782 1-naphthols Chemical class 0.000 description 3
- CMOLPZZVECHXKN-UHFFFAOYSA-N 7-aminonaphthalene-1,3-disulfonic acid Chemical compound C1=C(S(O)(=O)=O)C=C(S(O)(=O)=O)C2=CC(N)=CC=C21 CMOLPZZVECHXKN-UHFFFAOYSA-N 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 239000000908 ammonium hydroxide Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000002045 lasting effect Effects 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 150000004780 naphthols Chemical class 0.000 description 3
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000005201 scrubbing Methods 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- HIEHAIZHJZLEPQ-UHFFFAOYSA-M sodium;naphthalene-1-sulfonate Chemical compound [Na+].C1=CC=C2C(S(=O)(=O)[O-])=CC=CC2=C1 HIEHAIZHJZLEPQ-UHFFFAOYSA-M 0.000 description 3
- 238000003892 spreading Methods 0.000 description 3
- 230000007480 spreading Effects 0.000 description 3
- AOSFMYBATFLTAQ-UHFFFAOYSA-N 1-amino-3-(benzimidazol-1-yl)propan-2-ol Chemical compound C1=CC=C2N(CC(O)CN)C=NC2=C1 AOSFMYBATFLTAQ-UHFFFAOYSA-N 0.000 description 2
- 241001614291 Anoplistes Species 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 2
- -1 carbonyl ion Chemical class 0.000 description 2
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- OEYIOHPDSNJKLS-UHFFFAOYSA-N choline Chemical compound C[N+](C)(C)CCO OEYIOHPDSNJKLS-UHFFFAOYSA-N 0.000 description 2
- 229960001231 choline Drugs 0.000 description 2
- 230000003749 cleanliness Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 238000005554 pickling Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- 230000026676 system process Effects 0.000 description 2
- 235000020681 well water Nutrition 0.000 description 2
- 239000002349 well water Substances 0.000 description 2
- 238000004857 zone melting Methods 0.000 description 2
- DOBIZWYVJFIYOV-UHFFFAOYSA-N 7-hydroxynaphthalene-1,3-disulfonic acid Chemical compound C1=C(S(O)(=O)=O)C=C(S(O)(=O)=O)C2=CC(O)=CC=C21 DOBIZWYVJFIYOV-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 241000534944 Thia Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002535 acidifier Substances 0.000 description 1
- 229940111121 antirheumatic drug quinolines Drugs 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- ZETCGWYACBNPIH-UHFFFAOYSA-N azane;sulfurous acid Chemical compound N.OS(O)=O ZETCGWYACBNPIH-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000003467 diminishing effect Effects 0.000 description 1
- WBZKQQHYRPRKNJ-UHFFFAOYSA-L disulfite Chemical compound [O-]S(=O)S([O-])(=O)=O WBZKQQHYRPRKNJ-UHFFFAOYSA-L 0.000 description 1
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- RRDQTXGFURAKDI-UHFFFAOYSA-N formaldehyde;naphthalene-2-sulfonic acid Chemical compound O=C.C1=CC=CC2=CC(S(=O)(=O)O)=CC=C21 RRDQTXGFURAKDI-UHFFFAOYSA-N 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000000413 hydrolysate Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000000338 in vitro Methods 0.000 description 1
- 150000002469 indenes Chemical class 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- YZMHQCWXYHARLS-UHFFFAOYSA-N naphthalene-1,2-disulfonic acid Chemical compound C1=CC=CC2=C(S(O)(=O)=O)C(S(=O)(=O)O)=CC=C21 YZMHQCWXYHARLS-UHFFFAOYSA-N 0.000 description 1
- 150000002790 naphthalenes Chemical class 0.000 description 1
- 238000007500 overflow downdraw method Methods 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 150000003248 quinolines Chemical class 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003457 sulfones Chemical class 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model belongs to crude naphthalene finishing technology field,It is proposed a kind of water-reducing agent production system,Including the liquid naphthalene measuring tank being connected with building materials naphthalene transfer pipeline,Liquid naphthalene measuring tank is connected with the first sulfonating reaction kettle,First sulfonating reaction kettle is connected with the first sulfuric acid gauge tank,First hydrolytic reaction pot,First hydrolytic reaction pot is connected with the first condensation reaction kettle,First condensation reaction kettle is connected with the second sulfuric acid gauge tank,First formaldehyde measuring tank,First neutralization reaction kettle,First neutralization reaction kettle is connected with the first liquid caustic soda measuring tank,Liquid water-reducing agent transfer pipeline,First atomizer,Liquid water-reducing agent transfer pipeline is connected with the first compounding kettle,First atomizer is connected with the first drying tower,The utility model solves the water-reducing agent production in existing crude naphthalene finishing technology,The problem of having much room for improvement in production process in terms of resource utilization and environmental pollution.
Description
Technical field
The utility model belongs to crude naphthalene finishing technology field, the diminishing being related in a kind of crude naphthalene fine-processing production line
Agent production system.
Background technology
Naphthalene content in coal tar is about 8%~12%, in crude naphthalene in addition to containing naphthalene, also containing thia indenes, phenols,
Quinolines and other unsaturated compounds.To obtain refined naphthalene, it is necessary to which crude naphthalene is further refined.Traditional crude naphthalene essence
Technology method processed is pickling rectification method, and the process gradually to grow up has solvent method, catalytic hydrogenation method, zone-melting
Crystallisation and Steppecd crystallization.In the various technology sides that crude naphthalene refines, pickling rectification method is traditional old technique, special
Point is that product purity is not high, seriously corroded, and investment is big, waste water is difficult to handle.Due to these shortcomings, the traditional handicraft at present by
It eliminates；Solvent process shortcoming is that solvent for use has certain toxicity, and equipment is more numerous and more jumbled, and refining effect is bad.At present, it is external very
Less using this method, though domestic have this method production of the small station-service in several small towns, because of solvent price, solvent loss is big, product cost
Height is not also promoted；For catalytic hydrogenation method since technique is more complicated, capital construction and operating cost are higher, promote and apply more difficult.
And have the generation of by-product naphthane, limit the scope of this naphthalene products application；Zone melting method produces refined naphthalene production technology
Continuous flow procedure, product quality are stablized.But because its capital expenditure and operating cost are high, operating condition requirement is tighter, so
There are no be widely used at home.Water-reducing agent in existing crude naphthalene finishing technology produces, resource in production process
Have much room for improvement in terms of utilization rate and environmental pollution.
Utility model content
The utility model proposes a kind of water-reducing agent production systems, solve the above problem of the prior art.
What the technical solution of the utility model was realized in：
A kind of water-reducing agent production system, including
The liquid naphthalene measuring tank being connected with the building materials naphthalene transfer pipeline, the liquid naphthalene measuring tank and the first sulfonating reaction kettle connect
Connect, the first sulfonating reaction kettle is connected with the first sulfuric acid gauge tank, the first hydrolytic reaction pot, first hydrolytic reaction pot with
First condensation reaction kettle connects, and the first condensation reaction kettle is connected with the second sulfuric acid gauge tank, the first formaldehyde measuring tank, first
Neutralization reaction kettle, the first neutralization reaction kettle are connected with the first liquid caustic soda measuring tank, liquid water-reducing agent transfer pipeline, the first atomization
Device, the liquid water-reducing agent transfer pipeline are connected with the first compounding kettle, and first atomizer is connected with the first drying tower, described
First drying tower is connected with the first hot-blast stove, the first cyclone separator, the first spiral discharging device, first cyclone separator with
First water dust scrubber, first spiral discharging device connection, first spiral discharging device are connected with the first packing machine.
Further, first hydrolytic reaction pot is connected with the first metering sink, the first metering sink and the one or three
The condensation mouth of a river connection of evaporator is imitated, first triple effect evaporator conveys water lines with-naphthols mother liquor and is connected.
It the utility model use principle and has the beneficial effect that：
Above scheme improves resource utilization well, improve material balance while reduce caused by environment it is dirty
Dye.
Description of the drawings
The utility model is described in further detail with reference to the accompanying drawings and detailed description.
Fig. 1 is crude naphthalene fine-processing production line process schematic representation in the utility model；
Fig. 2 is water-reducing agent production system process schematic representation in the utility model；
Fig. 3 is a part of process schematic representation of beta naphthal production system in the utility model；
Fig. 4 is the another some processes schematic diagram of beta naphthal production system in the utility model；
Fig. 5 is beta naphthal production system another part process schematic representation in the utility model；
Fig. 6 is the another some processes schematic diagram of beta naphthal production system in the utility model；
Fig. 7 is K acid production system process schematic representations in the utility model；
In figure：1- crude naphthalene slots, 2- water-reducing agent production systems, 3-2- naphthols production systems, 4-K acid production systems, 5- are thin
Wall condenser, 6- sack cleaners, the crystallization casees of 7- first, 8- the first fraction slots, 9- the second fraction slots, the first semi-finished product tanks of 10-,
11- building materials naphthalene transfer pipelines, the first pan tanks of 12-, 13- continue feed inlet, 14- steam inlets, 15- waste gas spreading mouths, 16-
One slicer, the first packing machines of 17-, 18- semi-finished product crystallization case, 201- liquid naphthalene measuring tanks, 202- the first sulfonating reaction kettles, 203-
First sulfuric acid gauge tank, the first hydrolytic reaction pots of 204-, 205- the first condensation reaction kettles, the second sulfuric acid gauge tanks of 206-, 207-
First formaldehyde measuring tank, 208- the first neutralization reaction kettles, 209- the first liquid caustic soda measuring tanks, 210- liquid water-reducing agent transfer pipelines,
The first atomizers of 211-, 212- first compound kettle, the first drying towers of 213-, the first hot-blast stoves of 214-, the first cyclonic separations of 215-
Device, the first spiral discharging devices of 216-, the first water dust scrubbers of 217-, the first packing machines of 218-, 219- first measure sink, 220-
First triple effect evaporator, 221-2- naphthols mother liquor conveying water lines, 301- refined naphthalene melting tanks, 302- sulfidation pans, the first sulphur of 303-
Sour head tank, 304-, which is hydrolyzed, blows naphthalene pot, 305- the first sulfuric acid storage tanks, 306- the first water measuring tanks, 307- the second liquid caustic soda measuring tanks,
308- steam pipeworks, 309- the first naphthalene steam condensers, in 310- and pot, 311- the first naphthalene recovery towers, the first driers of 312-,
The first cooling tanks of 313-, the first suction filtration tanks of 314-, 315- alkal melting pans, 316- dilution pots, 317- first are acidified pot, and 318- first is boiled
Boiling pot, the second boiling pots of 319-, the 3rd boiling pots of 320-, the first dry pots of 321-, the first distillation stills of 322-, 323- first are centrifuged
Separator, 324- naphthalene water traps, the 3rd neutralization reaction kettles of 325-, the second triple effect evaporators of 326-, 327- cooling nutsch filters,
The first equipment of crystallisation by cooling of 328-, the first centrifugal devices of 329-, 330- alkali fusion devices, the second centrifugal devices of 331-, 332- second
Acidifying pot, 333- Asias sodium cooling slot, the first filter presses of 334-, 335- dnockout pumpss, the 3rd triple effect evaporators of 336-, 337- second are cold
But crystallization apparatus, the 3rd whizzers of 338-, 339- Asias sodium head tank, the new water inlets of 340-, 341- washing water outlets, 342- are done
Dry trap, 343- condensation liquid storage tanks, 344- distillation traps, the 3rd fraction slots of 345-, the second pan tanks of 346-, 347- the 4th
Fraction slot, 348- section head tanks, the second slicers of 349-, 350- second package machines, 401- sulfonating reaction kettles twice, 402- salt
Analyse kettle, 403- potassium sulfate solution measuring tanks, the second filter presses of 404-, the 4th neutralization reaction kettles of 405-, the 4th triple effect evaporations of 406-
Device, 407- waste water processing stations, the 3rd equipment of crystallisation by cooling of 408-, the 4th centrifugal devices of 409-, 410- aminating reaction kettles, 411- are sub-
Ammonium hydrogen sulfate entrance, 412- ammonia inlets, 413- the 3rd are acidified kettle, and kettle, the 3rd filter presses of 415-, 416- the is precipitated in 414- coolings
Five triple effect evaporators, the 4th sulphonation kettles of 417-, 418- dilution traps, the 4th filter presses of 419-, the 4th packing machines of 420-, 421- deaminations
Kettle.
Specific embodiment
The following is a combination of the drawings in the embodiments of the present utility model, and the technical scheme in the embodiment of the utility model is carried out
It clearly and completely describes, it is clear that the described embodiments are only a part of the embodiments of the utility model rather than whole
Embodiment.Based on the embodiment in the utility model, those of ordinary skill in the art are without creative efforts
All other embodiments obtained shall fall within the protection scope of the present invention.
As shown in Figure 2 the utility model proposes water-reducing agent production system, water-reducing agent production system 2 includes
The liquid naphthalene measuring tank 201 being connected with building materials naphthalene transfer pipeline 11, liquid naphthalene measuring tank 201 and the first sulfonating reaction kettle
202 connections, the first sulfonating reaction kettle 202 are connected with the first sulfuric acid gauge tank 203, the first hydrolytic reaction pot 204, and the first hydrolysis is anti-
Kettle 204 is answered to be connected with the first condensation reaction kettle 205, the first condensation reaction kettle 205 is connected with the second sulfuric acid gauge tank 206, first
Formaldehyde measuring tank 207, the first neutralization reaction kettle 208, the first neutralization reaction kettle 208 are connected with the first liquid caustic soda measuring tank 209, liquid
Water-reducing agent transfer pipeline 210, the first atomizer 211, liquid water-reducing agent transfer pipeline 210 are connected with the first compounding kettle 212, and first
Atomizer 211 is connected with the first drying tower 213, the first drying tower 213 and the first hot-blast stove 214, the first cyclone separator 215,
First spiral discharging device 216 connects, the first cyclone separator 215 and the first water dust scrubber 217,
First spiral discharging device 216 connects, and the first spiral discharging device 216 is connected with the first packing machine 218.
As further technical solution, the first hydrolytic reaction pot 204 is connected with the first metering sink 219, the first metering
Sink 219 is connected with the condensation mouth of a river of the first triple effect evaporator 220, and the first triple effect evaporator 220 conveys water with beta naphthal mother liquor
Pipeline 221, which connects, (by the water conservancy that production process in beta naphthal production line generates hydrolysis here, to be realized well
Water resource utilization).
In the utility model, for water-reducing agent production system 2 using building materials naphthalene as primary raw material, system passes through sulfonation, hydrolysis, contracting
The target product that processes are produced well such as close, neutralize, is dry, and the yield of the system production can improve to 86.5% with
On, building materials naphthalene is delivered to liquid naphthalene measuring tank 201 located underground by building materials naphthalene transfer pipeline 11, and when production is sent by submerged pump
Enter the first sulfonating reaction kettle 202, while according to naphthalene after 98% concentrated sulfuric acid is measured by the first sulfuric acid gauge tank 203：Sulfuric acid ≈
1:The ratio of 1.3 (molar ratios) is slowly added to after metering to the first sulfonating reaction kettle 202, while the first sulfonating reaction kettle 202
Chuck in be passed through steam, temperature of reaction kettle is made to rise to 160~165 DEG C of closed normal pressure sulfonation, by accurate temperature control and
Material is added than making the completion of sulfonating reaction in high yield, and the exhaust gas containing naphthalene, sulfuric acid discharged during simultaneous reactions passes through closed
Pipeline is sent to scrubbing tower purified treatment, and the noise that product pump generates also is isolated so that whole system can keep preferable
Production status.After sulfonating reaction, the by-product (α-naphthalenesulfonicacid) contained in reaction mixture is as far as possible by the first water
The hydrolysis of solution reaction kettle 204 removes, and the characteristic of hydrolysis is easier to using side reaction object and realizes purity and yield well
Raising, sulfonating reaction product by react carry steam press-in condensation kettle, carried out in the environment of 120 DEG C, due to a upper process
In temperature it is higher (165 DEG C), therefore realize the progress of hydrolysis well, 204 temperature of the first hydrolytic reaction pot is cold by cycling
But after water cooling, the condensed water being sent at the condensation mouth of a river of the first triple effect evaporator 220 is added in by the first metering sink 219, because
To mainly contain naphthalene sulfonic acids (sodium) in condensed water, be before hydrolysis in material i.e. existing for substance, therefore hydrolysis will not be produced
It is raw to influence, therefore this partial condensation water has been subjected to good utilization, the utilization rate for improving water improves production efficiency simultaneously,
In addition, sulfonating reaction occurs again in high temperature environments for part naphthalene and the sulfuric acid of hydrolysis generation, and based on can part naphthalene be converted
Product (beta-naphthalenesulfonic-acid) by the adjustment of hydrolysis, can cause the overall reaction yield of beta-naphthalenesulfonic-acid to reach more than 88%.It
Condensation reaction afterwards carries out in the first condensation reaction kettle 205, before reaction, is measured first in hydrolysate by the second sulfuric acid
Slot 206 adds a certain amount of 98% sulfuric acid, and acidity is increased to 30% or so, and condensation reaction is made to be easier to carry out, and reaction is more
Completely, the quality of product is finally improved, hydrolyzate is warming up to 120 DEG C with steam with the speed of 1 DEG C/min, while formaldehyde is through defeated
It send and is pumped to the first formaldehyde measuring tank 207, according to formaldehyde：Building materials naphthalene=1：Condensation kettle is added in after 7 ratio (mass ratio) metering
In, formaldehyde is converted into the stronger carbonyl ion of reactivity under the catalytic action of acid, and electrophilic contracting then occurs with beta-naphthalenesulfonic-acid again
Reaction is closed, ultimately generates beta-naphthalenesulfonic-acid formaldehyde condensation compound, a small amount of formaldehyde of pollutant and sulfuric acid mist which generates, by closed
Pipeline is sent to scrubbing tower so as to fulfill purification, while the equipment for generating noise is carried out sound insulation, can reach cleanliness without any pollution production
Purpose.Neutralization reaction is carried out in the first neutralization reaction kettle 208 afterwards, is added in right amount by the first liquid caustic soda measuring tank 209 thoroughly
NaOH solution neutralization reaction occurs therewith, naphthalene sulfonic acids is made to be converted into sodium salt, while the sulfuric acid of neutralization reaction, final neutralization production
7~9 or so, neutralization reaction is crossed by controlling amount of water for object pH controls, and material concentration is made to be maintained at 50%, while by material temperature
Degree is down to less than 80 DEG C so that the part naphthalene solidification generated in hydrolyzing process, after the completion of neutralization, part neutralizer subtracts by liquid
Aqua transfer pipeline 210 is delivered to the first compounding kettle 212, while is diluted with water to concentration 40% or so, obtains liquid concrete
Water-reducing agent, rest part neutralizer are pumped into head tank after filtering, send for producing solid water-reducing agent, filter consolidating for generation
State naphthalene send naphthalene slot to re-use.Solid water-reducing agent is sent into the first drying tower 213 and is dried afterwards, because finished product feed liquid moisture
Higher, 50% or so, therefore drying is essential, and feed liquid is sent into the first drying tower 213 by feed pump first, into tower it
The first atomizer 211 of preceding increase further improves efficiency, while the heat smoke blasted by the first hot-blast stove 214 is through hot-air distributor
Be sent into the first atomizer 211, atomization feed liquid hot wind effect under (350 DEG C) be dried, dried material have 90% from
First drying tower, 213 the first spiral discharging device of lower part 216 and Pneumatic conveyer send to the first packing machine 218 and carry out sacker
Sequence, remainder enter the first cyclone separator 215 with dry waste gas, and product is further recycled through the first cyclone separator 215,
Liquid is packed by the submitting of the first spiral discharging device 216, and dried moisture content of finished products is about 5%, so as to meet product quality
The requirement of middle solid content >=90%, the production process of entire water-reducing agent is scientific and reasonable, realizes the good utilization of resources, reaches
Good effect.
As shown in Fig. 1~Fig. 7, the utility model water-reducing agent production system 2 is specific in crude naphthalene fine-processing production line
Using crude naphthalene fine-processing production line includes crude naphthalene slot 1, and the lasting feed inlet being connected with pipeline is provided on crude naphthalene slot 1
It 13 and keeps the stable steam inlet 14 of internal temperature, waste gas spreading mouth 15 being provided on crude naphthalene slot 1 for being passed through steam, give up
Gas diffusion mouth 15 is connected successively with thin-walled condenser 5, sack cleaner 6, dust collection mouth and the lasting charging of sack cleaner 6
Mouth 13 connects,
Crude naphthalene slot 1 with first crystallization case 7 be connected, first crystallization case 7 be connected with the first fraction slot 8, the second fraction slot 9,
First semi-finished product tank 10, the first fraction slot 8 are connected with building materials naphthalene transfer pipeline 11, and the second fraction slot 9 connects with the first crystallization case 7
It connects, the first semi-finished product tank 10 is connected with semi-finished product crystallization case 18,18 and second fraction slot 9 of semi-finished product crystallization case, the first semi-finished product
Slot 10, the first pan tank 12 connect, and the first pan tank 12 is connected with 3 and first slicer 16 of beta naphthal production system, and first cuts
Piece machine 16 is connected with the first packing machine 17 and connects, and beta naphthal production system 3 is connected with K acid production system 4, building materials naphthalene transfer pipeline
11 are connected with water-reducing agent production system 2.
In the utility model, the refined naphthalene of production is melted crude naphthalene again using the physical characteristic of naphthalene using crude naphthalene as raw material
Cooling restructuring, re-melting fractionation, and repeat multistage fractionation and obtain product refined naphthalene, crude naphthalene is directly by carbon black company in pipeline
Conveying is continuously delivered to by lasting feed inlet 13 into crude naphthalene slot 1, therefore can continue uninterruptedly to produce, without a collection of
It carries out, is closed type in slot, is provided with heating coil, being passed through saturated vapor by the steam inlet 14 on crude naphthalene slot 1 protects
Temperature is held at 80 DEG C or more, holding crude naphthalene is liquid phase state, while the exhaust gas containing naphthalene of crude naphthalene slot 1 is drawn by waste gas spreading mouth 15
Go out, first pass through thin-walled condenser 5 and be condensed into naphthalene powder, purified treatment then is carried out to exhaust gas by sack cleaner 6, and pocket type removes
The dust collection mouth of dirt device 6 is connected with continuing feed inlet 13, and the naphthalene dirt of mobile phone is back to crude naphthalene slot 1 recycles,
Therefore it can realize that good material utilizes, and the pollution of environment has been also reduced to minimum, realize clean raw well
Production.Afterwards, crude naphthalene is pumped to the first crystallization case 7 (80 DEG C of ＞) by crude naphthalene slot 1 by submerged pump and carries out primary crystal fractionation,
Recirculated cooling water is passed through in the crystallization case tubulation of first crystallization case 7, liquid industrial naphthalene is cooled to 70 with the rate of temperature fall of 2 DEG C/h
DEG C, make its crystallization, be then passed through hot water again in the crystallization case tubulation of the first crystallization case 7, crystal is heated with the heating rate of 4 DEG C/h
Naphthalene, while the fractionation into the first fraction slot 8 (75~80 DEG C of fractions) by naphthalene liquid, when naphthalene liquid is warming up to 80 DEG C, naphthalene liquid is turned to
Second fraction slot 9 (80 DEG C of fractions of ＞) strains material, and final naphthalene liquid temperature degree is maintained at 81~82 DEG C, until first crystallization 7 lower floor's material of case
Crystalline temperature is 79 DEG C, and naphthalene liquid is gone to the first semi-finished product tank 10, and it is cold that Xun Huan is passed through in the crystallization case tubulation of the first semi-finished product tank 10
But semi-finished product naphthalene liquid is down to 72 DEG C by water with the rate of temperature fall of 2 DEG C/h, makes its crystallization, then is passed through hot water with the heating speed of 2 DEG C/h
Rate heats up crystal naphthalene, while strains material to the second fraction slot 9 (80 DEG C of fractions of ＞), until 80 DEG C of whens alter course, the first semi-finished product tank 10 is strained
Material, final naphthalene liquid temperature degree are maintained at 82 DEG C or so, take lowest level material assay, and crystalline temperature turns to naphthalene liquid when being 79.3 DEG C
After roller crystallisation by cooling, sheet is cut by the first slicer 16 for first pan tank, 12 blowing, then by the first packing machine 17 into
Row is packed as far as possible, while the fraction of the first fraction slot 8 is delivered to water-reducing agent production system 2 by building materials naphthalene transfer pipeline 11 and is subtracted
The production of aqua, the fraction of the first pan tank 12 send to beta naphthal production system 3 production for carrying out beta naphthal, beta naphthal production system
System 3 is also associated with the production of progress K acid after K acid production system 4, and good Matter Transfer is realized by this process, improves
The utilization rate of material, and pollution sources masters will be that naphthalene heats fusing in crystallization case, diversion channel, semi-finished product tank, pan tank a bit
The naphthalene dirt that the steam containing naphthalene and slicer and packing machine that process generates generate, the generations such as pump class, slicer, packing machine are made an uproar
Sound after the naphthalene steam generated in production process is collected by pipeline, is condensed into naphthalene dirt through thin-walled condenser, is then sent to pocket type and removes
Dirt device purified treatment so that purified treatment can also be carried out by condensing the solid naphthalene of recycling, therefore improve material utilization well, and
Reduce pollution, while production equipment of making an uproar is distributed on progress noise reduction isolation in workshop, it is whole so that production environment has obtained greatly
Improvement, realize good effect.
As further technical solution, beta naphthal production system 3 includes the refined naphthalene being connected with the first pan tank 12 fusing
Slot 301, refined naphthalene melting tank 301 are connected with sulfidation pan 302, and naphthalene pot 304 is blown in 302 and first sulfuric acid high position tank 303 of sulfidation pan, hydrolysis
Be all connected with, the first sulfuric acid high position tank 303 is connected with the first sulfuric acid storage tank 305, hydrolysis blow 304 and first water measuring tank 306 of naphthalene pot,
Second liquid caustic soda measuring tank 307, steam pipework 308, the first naphthalene steam condenser 309, neutralization pot 310 are all connected with, the first naphthalene steam
Condenser 309 is sequentially connected with the first naphthalene recovery tower 311, the first drier 312, the recycling naphthalene mouth and sulphur of the first drier 312
To change pot 302 to connect, the separation mouth of a river and the hydrolysis of the first naphthalene recovery tower 311 are blown naphthalene pot 304 and are connected,
It neutralizes 310 and first cooling tank 313 of pot, the first suction filtration tank 314, alkal melting pan 315, dilution pot 316, first and is acidified pot
317th, the first boiling pot 318, the second boiling pot 319, the 3rd boiling pot 320, the first dry pot 321, the first distillation still 322 be successively
Connection,
First suction filtration tank 314 is connected with the first whizzer 323, the first suction filtration tank 314 also with naphthalene water trap 324,
3rd neutralization reaction kettle 325, the second triple effect evaporator 326 are sequentially connected, the concentrated solution outlet of the second triple effect evaporator 326 with it is cold
But nutsch filter 327 connects, cooling nutsch filter 327 mother liquor outlet be connected with the first equipment of crystallisation by cooling 328, precipitate outlet and
First centrifugal device 329 connects, and the sodium naphthalene sulfonate outlet of the first centrifugal device 329 is connected with alkali fusion device 330, and the second triple effect steams
The condensate outlet of hair device 326 is connected with alkali fusion device 330, and alkali fusion device 330 is connected with dilution pot 316, the first crystallisation by cooling
The supernatant outlet of device 328 is connected with the second triple effect evaporator 326, crystallizes outlet is connected with the second centrifugal device 331, and second
The centrifugate outlet of centrifugal device 331 is connected with the second triple effect evaporator 326,
Dilution pot 316 is also connected by the second acidifying pot 332 with the first boiling pot 318, and the sulfur dioxide for neutralizing pot 310 goes out
Mouth is acidified pot 317 with the second acidifying pot 332, first successively and is connected,
As further technical solution, the outlet of the sodium sulfite solution of the first boiling pot 318 successively with sub- sodium cooling slot
333rd, the first filter press 334 connects, and the filtered solid outlet of the first filter press 334 is connected with dilution pot 316, the first filter press 334
Filtrate (liquid and dnockout pumps 335, the 3rd triple effect evaporator 336, the second equipment of crystallisation by cooling 337, the 3rd whizzer 338 according to
Secondary connection, the 3rd whizzer 338 are all connected with the 3rd triple effect evaporator 336, the second equipment of crystallisation by cooling 337, dnockout pumps
335 are also connected with sub- sodium head tank 339.
As further technical solution, new water inlet is both provided on the first boiling pot 318 and the 3rd boiling pot 320
340, washing water outlet 341, the washing water outlet of the second boiling pot 319 are both provided on the second boiling pot 319 and the 3rd boiling pot 320
341 are connected with dilution pot 316, and the washing water outlet 341 of the 3rd boiling pot 320 is connected with the second boiling pot 319.
As further technical solution, the steam outlet of the first dry pot 321 is connected with dry trap 342, is done
The condensation-water drain of dry trap 342 is connected with condensation liquid storage tank 343, and the first distillation still 322 is connected with distillation trap 344,
The condensation-water drain for distilling trap 344 is connected with condensation liquid storage tank 343, and condensation liquid storage tank 343 is connected with dilution pot 316.
As further technical solution, the first fraction outlets of the first distillation still 322, the second fraction outlets, the 3rd evaporate
Sub-export is connected respectively with the 3rd fraction slot 345, the second pan tank 346, the 4th fraction slot 347, the 3rd fraction slot the 345, the 4th
Fraction slot 347 is connected with the 3rd boiling pot 320, and the second pan tank 346 is connected with section head tank 348, head tank 348 of cutting into slices
It is sequentially connected with the second slicer 349, second package machine 350.
In the utility model, beta naphthal production system 3 uses naphthalene sulfonated alkali fusion method, is original with refined naphthalene, sulfuric acid, caustic soda etc.
Material, it is sulfonated, hydrolyze, blow naphthalene, neutralization, suction filtration, alkali fusion, be acidified, boil, press filtration, drying, distillation, the processes such as section, pass through
The improvement of system can be improved total yield of products to the production of more than 78.8%, 2- naphthalene powder with the essence in the first pan tank 12
Naphthalene is primary raw material, and through pipeline to refined naphthalene melting tank 301, using steam heating and thermal insulation, liquid naphthalene is sent by head tank to sulphur again
Change pot 302, it is heated using the steam jacket of sulfidation pan 302, liquid naphthalene temperature is made to rise to 120 DEG C, subsequent first sulfuric acid is high-order
98% concentrated sulfuric acid in slot 303 is according to naphthalene：Sulfuric acid=1:1.4 ratio (molar ratio) is slowly added dropwise to sulfidation pan 302, then
Stir and slowly heat up, 302 temperature of sulfidation pan is finally made to maintain 160~165 DEG C, naphthalene and sulfuric acid occur sulfonating reaction generate β-
Naphthalene sulfonic acids separately has the side reaction of part generation α-naphthalenesulfonicacid, while also has time side reaction β-dinaphthyl sulfone, naphthalenedisulfonic acid and its indexing
The generation of body, it is mainly exhaust gas containing naphthalene, the sulfuric acid mist escaped in refined naphthalene melting tank 301, sulfidation pan 302 which, which generates pollutant,
Exhaust gas, molten naphthalene exhaust gas is subjected to purified treatment using bag filter, sulphonation waste gas sent by closed conduit to scrubbing tower water
Good clear production can be reached by washing purified treatment.After sulfonating reaction, by hydrolysis except the larger α of deactivation-
Naphthalene sulfonic acids, has reached good production effect, eliminates influence of the production line to downstream process well, sulfonating reaction object is by pressing
Naphthalene pot 304 is blown in the press-in hydrolysis of contracting air, is opened agitating device and is blown naphthalene pot 304 to hydrolysis and adds water 306 by the first water measuring tank
Water is added in, and passes through steam pipework 308 and is passed through appropriate steam direct heating, 160 DEG C is maintained, α-naphthalenesulfonicacid is hydrolyzed to naphthalene,
By the improvement of hydrolysis, beta-naphthalenesulfonic-acid overall reaction yield can be improved to 90%, be restarted after hydrolysis
Agitating device, and a small amount of liquid caustic soda is added in by the second liquid caustic soda measuring tank 307, liquid caustic soda and part beta-naphthalenesulfonic-acid generation β-naphthalene sulphur can be made
Acid sodium-salt crystallizing seeds, while the sulfuric acid generation that liquid caustic soda can not also complete the sulfuric acid of reaction with sulfonating reaction and hydrolysis generates
It neutralizes, steam is then passed through by steam pipework 308 in material is hydrolyzed and carries out blowing naphthalene, that is, being passed through high-temperature steam generates hydrolysis
The distillation of free state naphthalene, and pass through closed conduit and send naphthalene steam to the first naphthalene steam condenser 309, then to the first naphthalene recovery tower
311, naphthalene exhaust gas is blown first after the secondary coil condensation of the first naphthalene steam condenser 309 into the first naphthalene recovery tower 311, with β
Spray liquid of the salt mother liquor as the first naphthalene of fountain recovery tower 311, while the naphthalene in tail gas is recycled, after blowing naphthalene, stop successively
Only steam supply, stirring and spray, when in hydrolyzer without overbottom pressure, 100 are warming up to 311 indirectly heat of the first naphthalene recovery tower
DEG C, the solid naphthalene of recycling is made all to melt, tower top is then turned on and puts naphthalene valve and bottom of towe into mother liquor valve, when 311 tower of the first naphthalene recovery tower
Interior liquid level rises to liquid naphthalene when putting naphthalene pipe height and all flow in the first drier 312, is closed after putting naphthalene into mother liquor valve, due to
Naphthalene is immiscible from β salt mother liquors and density is different, into the first drier 312 liquid naphthalene it is warm it is static after be layered, open
Bottom water valve releases β salt mother liquor, and so as to the separation for realizing naphthalene and β salt mother liquors being simple and efficient, naphthalene is back to as raw material
302 process of sulfidation pan utilizes, therefore improves the rate of recovery of naphthalene well, its rate of recovery is made to have reached 98%, naphthalene is blown in generation
Exhaust gas can realize good CR production using two-stage coil condensation combination naphthalene water trap spray cleaning, improve production
Cleanliness.Neutralization step is carried out afterwards, and naphthalene sulfonic acids is become sodium naphthalene sulfonate by main purpose, and extra sulfuric acid is neutralized, blowout
The hydrolysis material of free naphthalene blows naphthalene pot 304 from hydrolysis and is gone to through air compressor in neutralization pot 310, is passed through steam by mixed material
It directly heats to boiling, 18% preheated sodium sulfite solution is added in pot 310 (comes that whisper is subsequent to boil work to neutralizing
Sequence), it and keeps in micro-vacuum state in pot, and starting stirring makes material fully react, and is passed through steam to neutralize two generated
Sulfur oxide is taken out of, and sulfur dioxide is all sent after pipeline is collected to 317 and second acid of the first acidifying pot in follow-up acidizing process
Change pot 318 as acidulant and uses (neutralization reaction and acidification reaction be with open with stopping), when no longer generating foam in neutralization pot 310
When, that is, stop adding in sub- sodium, but still blast steam and all drive sulfur dioxide out of, it neutralizes material and goes to first through air compressor
Crystallisation by cooling is carried out in cooling tank 313, and opens stirring, is cooled to 35 DEG C indirectly by recirculated cooling water, sodiumβ-naphthalenesulfonate is opened
Begin to generate crystallization precipitation, then crystallized stock is gradually put into the first suction filtration tank 314 and is filtered with reciprocating pump, obtained
Wet beta-naphthalenesulfonic-acid sodium salt, then material is hung to alkal melting pan 315 with electric block, due to neutralization reaction in a heated condition into
Row, reaction solution is in alkalescence, and still blasts steam after reacting, so that the sulfur dioxide of reaction generation all escapes, therefore, is taken out
Filter process is arranged in vitro without sulfur dioxide gas, realizes harmless production well, sodiumβ-naphthalenesulfonate can be realized by this process
Reaction yield for 90%, and the major pollutants of the process are also handled well, are filtered mother liquor, are neutralized exhaust gas, take out
The exhaust gas to volatilize during filter is rationally handled, and suction filtration mother liquor is sent to naphthalene water trap 324 and is used as shower water, is jacked up more
After changing first through lye in the 3rd neutralization reaction kettles of 325- in and naphthalene sulfonic acids therein, be then sent to the second triple effect evaporator 326
Desalination is carried out, exhaust gas sulfur dioxide is neutralized and is all sent after pipeline to the first acidifying acidifying pot 318 of pot 317 and second as acidifying
Agent efficiently utilizes, and filters exhaust gas and blows naphthalene exhaust gas together through naphthalene water trap naphthalene water trap with condensed after gas gathering mask is collected
324 carry out spray cleaning processing, it is achieved that non-pollutant discharge production well, and realize efficiently production well.
Alkali fusion procedure afterwards is mainly to be reacted by the alkali of molten state with sodium naphthalene sulfonate, generates naphthalene powder sodium, solid caustic soda is added in choline pot
It is sent by metering after stove heat melts Huawei's liquid can be heated in alkal melting pan 315, alkal melting pan 315 is also risen using heating furnace
Temperature, then according to molar ratio 1:2 ratio slowly adds in sodiumβ-naphthalenesulfonate filter cake to alkal melting pan 315, and warming while stirring reaches
Stop heating to imposing a condition, sodiumβ-naphthalenesulfonate has reached 95% with sodium hydroxide reaction generation β-naphthalene powder sodium, reaction yield, alkali
Material is sent into dilution pot 316 by the molten outlet valve for opening alkal melting pan 315 after completion of the reaction, and dilution pot 316 first adds in before feeding
Alkali fusion material, is then slowly added to by the secondary boiled water of subsequent handling, and material closes inlet valve after shifting, and continuously adds
Secondary boiled water adjusts diluted material volume, and the pollutant of generation is choline exhaust gas and alkali fusion exhaust gas through cyclone dust removal and two level water
Outer row after spray-absorption purification, so as to fulfill good purification production.It is acidified afterwards, material is pressed into the after alkali fusion dilution
One acidifying pot 317, when temperature in the kettle is kept to be 260~270 DEG C, into kettle, negative pressure introduces sulfur dioxide gas (neutralization step production
Raw sulfur dioxide), wherein material guiding tube insertion feed liquid bottom, gas fairlead are located at kettle top, open stirring, steam bubble dress
It puts, carries out material acidifying, the two-stage that pot 332 is acidified by the first acidifying pot 317, second is acidified, and neutralizes the sulfur dioxide of generation
After appendix all send and to the second acidifying pot 332 it made fully to be acidified, through pipe after unabsorbed sulfur dioxide effusion liquid level
Road all send to the next first acidifying pot 317 and participates in acidification reaction, and the design of two-stage acidifying has obtained efficiency is acidified greatly
It improves, while reduces sulfur dioxide well and lose outer discharge capacity, the thick finished product of 2- naphthalene powder can be obtained after the completion of acidifying, generation
A small amount of sulfur dioxide that pollutant vacuumizes generation for acidification reaction can reach non-pollution discharge production after alkali cleaning absorbs.Acid
Containing thick naphthalene powder and sodium sulfite in compound material, using the difference of its solubility, by washing repeatedly, isolated purer crude phenols
After acidifying material enters the first boiling pot 318, clear water is added in by new water inlet 340 for naphthalene, and is passed through steam indirectly heat to boiling
It rises, is then shut off steam and is stood, bottom valve is opened by Asia after thick naphthalene powder and the good layering of sodium sulfite solution appearance
Metabisulfite solution after plate-type condenser by sending to sub- sodium cooling slot 333, by further cooling down a small amount of naphthols made in solution
334 press filtration of the first filter press is sent in crystallization after being precipitated, crystallisation by cooling uses obturator, and it is temporary that sub- sodium filtrate is sent into sub- sodium geosyncline
It deposits, press filtration filter cake is a small amount of crude phenols naphthalene, is sent to utilization in dilution pot 316, the compressed sky of upper strata crude phenols naphthalene of the first boiling pot 318
Air pressure enters to the second boiling pot 329, before the product crude phenols naphthalene of the first boiling pot 318 is received, first by the 3rd boiling pot 320
The ejected wash water that the second boiling pot 329 is depressed by washing water outlet thereon is heated to seething with excitement, then the crude phenols naphthalene that one is boiled injects,
And stood after stirring, after mixed material is fully layered, crude phenols naphthalene is pressed by the 3rd boiling pot 320, wash water by compressed air
As dilution kettle moisturizing, quantitative clear water is filled into it by the new water inlet 340 on the 3rd boiling pot 320 and is heated to boiling
It rises, adds in the crude phenols naphthalene boiled through the second boiling pot 329, stood again after opening stirring, after material layering, by crude phenols naphthalene press-in the
One dry pot 321 is pressed into the second boiling pot 329 by washing water outlet 341 thereon, therefore realizes production well
Water resource utilizes, and has reached good balance, and the exhaust gas that the volatilization of pressure-filtering process naphthalene powder generates is sent into spray cleaning after collection, is pressed
Filter generate sub- sodium filtrate send to sub- sodium head tank as neutralization step raw material utilization, partly send to the 3rd triple effect evaporator 336,
Second equipment of crystallisation by cooling 337, the 3rd whizzer 338 are utilized, and integrally realize good material balance.3rd boils
Moisture content, 1- naphthols, beta naphthal etc. in the thick naphthalene powder of 320 product of pot are boiled, the beta naphthal for not obtaining degree of purity is dehydrated and is separated
1- naphthols will boil product and be sent by the 3rd boiling pot 320 to the first dry pot 321 three times, be heated up and be dehydrated as heat source using steam,
Vacuum pump is opened to being vacuumized in the first dry pot 321 simultaneously, and the vapor that drying process generates enters in vacuum
Dry trap 342 is gathered in condensation liquid storage tank 343 after condensation, is recycled sending to the 3rd boiling pot 320, first is dry
Temperature rises to 110 DEG C or so in dry pot 321, and stopping is vacuumized and dried, and dried material is sent by compressed air to first and is steamed
Kettle 322 is evaporated, the first distillation still 322 is vacuumized using vacuum pump while thick naphthols is pressed into distillation still, charging finishes
The first distillation still 322 is heated afterwards, is heated stove heat initial stage, the heating draining of distilling material normal pressure, discharge moisture is through distillation
Trap 344 send to the 3rd boiling pot 320 using condensation liquid storage tank 343 and utilizes, when the jacket temperature of the first distillation still 322 reaches
To 220~250 DEG C, liquidus temperature at 185~205 DEG C, a fraction (predominantly moisture and a small amount of 1- naphthols, beta naphthal are steamed
Deng), into the 3rd fraction slot 345, continue to heat up, when jacket temperature reach 250~275 DEG C, liquid temperature reach 195~220 DEG C, gas
Temperature reach 190~220 DEG C, vacuum degree >=0.09MPa when, steam all two fractions (i.e. refined beta naphthal), be sent into the second finished product
Slot 346 is temporary, when in pot temperature of charge be raised to 330~360 DEG C, vapor phase temperature 300~330 DEG C, jacket temperature 380~
It 420 DEG C, steams three fractions (predominantly salinity, byproduct of reaction and a small amount of beta naphthal etc.) and sends out three fractions to the 4th fraction slot
347, finally with steam by distillation slag (predominantly resin, carbonizing matter etc.) discharge, distillation terminates, and a fraction and three fractions are sent to the
Three boiling pots 320 after boiling generate beta naphthal, impurity etc. and enter dilution pot 316 with wash water again, eventually enter into sub- sodium salt mother liquor,
The naphthols distillation vacuum system exhaust gas of generation, which is sent after secondary coil condenses to water spray system, to be purified, and plant area is sent in vacuum pump drainage
Waste water processing station processing, so as to fulfill hamlessizing technology.Finally, the beta naphthal for being temporarily stored into the second pan tank 346 is pumped through feed
To section head tank 348, section head tank 348 is kept the temperature by heat source of steam, and liquid beta naphthal is by blowing in head tank
To the second slicer 349, by adjusting rotary drum cooling water, control chip rate, cut into slices to beta naphthal, obtained sheet production
Product are packed through second package machine 350, finally realize efficient and rational production, have good actual production value.Slightly
Naphthalene powder boiling washing water contains about 18% sodium sulfite, by part boil water set for neutralization step, remaining boiling washing water
It is handled using evaporating and concentrating process, realizes good material balance and water resource utilizes.
As further technical solution, K acid production system 4 includes the sulfonation twice being connected with beta naphthal production system 3
Reaction kettle 401, twice sulfonating reaction kettle 401 be connected with kettle 402 of saltouing, kettle 402 of saltouing also connects with potassium sulfate solution measuring tank 403
It connecing, kettle 402 of saltouing is connected with the second filter press 404,
The mother liquor outlet of second filter press 404 is connected with the 4th neutralization reaction kettle 405, the 4th neutralization reaction kettle 405 and
Four triple effect evaporators 406 connect, and the condensate outlet of the 4th triple effect evaporator 406 is connected with waste water processing station 407, the 4th triple effect
The concentrated solution outlet of evaporator 406 is connected by the 3rd equipment of crystallisation by cooling 408 with the 4th centrifugal device 409, the 4th centrifugation dress
Put 409 centrifugate outlet be connected with the 4th triple effect evaporator 406,
The filtered solid outlet of second filter press 404 is connected with aminating reaction kettle 410, and sulfurous is provided on aminating reaction kettle 410
Sour hydrogen ammonium entrance 411 and ammonia inlet 412, aminating reaction kettle 410 are acidified kettle 413 with deamination kettle the 421, the 3rd successively and are connected, the
Three acidifying kettles 413 are sequentially connected with cooling precipitation kettle 414, the 3rd filter press 415, the filtered solid outlet of the 3rd filter press 415 and the
Five triple effect evaporators 416 connect, filtrate (liquid is connected with the 4th sulphonation kettle 417, the concentrate of the 5th triple effect evaporator 416 connection
The kettle 402 that exports and saltout connects,
4th sulphonation kettle 417 is connected by dilution trap 418 with the 4th filter press 419, the K acid outlet of the 4th filter press 419
It is connected with the 4th packing machine 420.
In the utility model, first by sour measuring tank by 98% concentrated sulfuric acid when producing K acid by K acid production system 4
It is fed through sulfonating reaction kettle 401 twice, and using steam as heat source indirectly heat sulfonating reaction kettle 401 twice, when temperature reaches 40
DEG C when, beta naphthal that beta naphthal production system 3 is produced is sent after metering to G salt sulfidation pans, is completed a sulfonating reaction, is controlled
Acidity and temperature just can realize good sulfonation, and 20% oleum is slowly added dropwise after acid measures into sulphur twice again afterwards
Change reaction kettle 401, so as to realize the process of secondary sulfonation well.Then a certain amount of potassium sulfate is added in configuration pot again,
And Amino-G Acid, K acid mother liquors after being concentrated by evaporation are added in thereto, it is made to be configured to the potassium sulfate solution that concentration is about 30%, so
After be passed to kettle 402 of saltouing, heated up and stirred with steam, then cooling and standings, so as to well realize G salt crystallization analysis
Go out, the crystal salt and mother liquor in kettle 402 of saltouing are put into the second filter press 404 and carry out good press filtration, and press filtration filtrate is taken out
It is handled to the 4th neutralization reaction kettle 405 and carries out certain recycling, so as to fulfill the good utilization of resources, obtained filter cake is G
Salt, and the reaction yield of G salt can be increased to 76%, at the same sulfonation, saltout, escaped in press filtration containing beta naphthal, sulfuric acid mist
Gas sampling after sent to secondary condenser and condense by closed conduit, the processing of spray column spray cleaning is then sent to, so as to very
The good discharge for reducing pollution.Afterwards, G salt, ammonium bisulfite and the concentration the second filter press 404 isolated are 20%
Ammonium hydroxide is pressed into aminating reaction kettle 410 by being passed through compressed air by ammonium bisulfite entrance 411, ammonia inlet 412 after metering, close
The aminating reaction kettle 410 closed can be very good temperature being promoted to 140 DEG C, and keep certain pressure, be opened after the completion of reaction
Feed liquid and the ammonia of releasing are pressed into deamination kettle 421 and carry out deamination by the valve of aminating reaction kettle 410 well, until pressure is put down
It weighs, the agitating device in deamination kettle 421 can be very good to ensure the efficient progress of reaction, while the ammonia that will escape out is recycled
Utilize, be passed through spray equipment it is achieved thereby that ammonium hydroxide it is spare, the reasonable utilization of resource is realized well, so that effect will be produced
Rate and product yield further improve, and the feed liquid in deamination kettle 421 is subsequently re-fed into the 3rd acidifying kettle 413 plus the 4th filter press
The K acid mother liquors and 100% sulfuric acid that 419 K acid outlet is produced are acidified, and Amino-G Acid, the dioxy of generation are obtained after reaction
Ammonium hydroxide made from changing the ammonia that sulphur is generated using the pressure of its own by pipeline with deamination kettle 421 is reacted, and is generated
Bisulfite ammonia can also continue on for 410 aminating reaction of aminating reaction kettle, so as to realize the efficient profit of resource well
With, therefore whole system design is very scientific and reasonable.After acidification reaction in 3rd acidifying kettle 413, by reaction mass
It send to cooling precipitation kettle 414 and carries out crystallization precipitation, it is closed structure that kettle 414, which is precipitated, in cooling, so as to improve precipitation effect, Zhi Houjie
Brilliant object send to the 3rd filter press 415 and carries out press filtration separation, and obtained filter cake is amino G crystal, and filtrate, which is sent to the 5th triple effect, steams
Hair device 416 is concentrated, and concentrate send to kettle 402 of saltouing and recycled, and condensed water is handled, therefore is improved well
Product yield and process rationality, improve production efficiency, and reduce the pollution that production is brought.Afterwards by 65% smoke
Sulfuric acid is pumped into sour measuring tank by acid, and the 4th sulphonation kettle 417 is added in after metering, agitating device stirring cooling is opened, when temperature reaches
During to 60 DEG C, G acid crystals are sent to the 4th sulphonation kettle 417, with steam indirectly heat, temperature are made to rise to 140 DEG C, keep certain
Reaction mass addition dilution trap 418 after completion of the reaction, is diluted with water adjustment acidity and is precipitated so as to improve crystal well by duration
Then reaction product is pumped into the 4th filter press 419 and carries out press filtration, obtains K acid crystals by effect, crush machine crush after by
It is finished product after 4th packing machine packaging, mother liquor equally send to the 5th triple effect evaporator 416 and concentrated, and concentrate is sent to saltouing
Kettle 402 is recycled, so as to improve production efficiency and resource utilization well.It is female that K acid production mother liquors include G salt
Liquid, Amino-G Acid mother liquor and K acid mother liquors have obtained good utilization, therefore global design is practical rationally, have actual production effect
The extraordinary advantage of fruit.
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Within the spirit and principle of utility model, any modifications, equivalent replacements and improvements are made should be included in the utility model
Protection domain within.
Claims (2)
1. a kind of water-reducing agent production system, which is characterized in that including the liquid naphthalene meter being connected with the building materials naphthalene transfer pipeline (11)
Measuring tank (201), the liquid naphthalene measuring tank (201) are connected with the first sulfonating reaction kettle (202), the first sulfonating reaction kettle
(202) be connected with the first sulfuric acid gauge tank (203), the first hydrolytic reaction pot (204), first hydrolytic reaction pot (204) with
First condensation reaction kettle (205) connects, and the first condensation reaction kettle (205) is connected with the second sulfuric acid gauge tank (206), first
Formaldehyde measuring tank (207), the first neutralization reaction kettle (208), the first neutralization reaction kettle (208) are connected with the metering of the first liquid caustic soda
Slot (209), liquid water-reducing agent transfer pipeline (210), the first atomizer (211), the liquid water-reducing agent transfer pipeline (210) with
First compounding kettle (212) connects, and first atomizer (211) is connected with the first drying tower (213), first drying tower
(213) it is connected with the first hot-blast stove (214), the first cyclone separator (215), the first spiral discharging device (216), first rotation
Wind separator (215) is connected with the first water dust scrubber (217), first spiral discharging device (216), and first spiral goes out
Glassware (216) is connected with the first packing machine (218).
A kind of 2. water-reducing agent production system according to claim 1, which is characterized in that first hydrolytic reaction pot
(204) the first metering sink (219), the condensation of the first metering sink (219) and the first triple effect evaporator (220) are connected with
The mouth of a river connects, and first triple effect evaporator (220) is connected with beta naphthal mother liquor conveying water lines (221).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721192274.0U CN207405109U (en) | 2017-09-18 | 2017-09-18 | A kind of water-reducing agent production system |
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| CN201721192274.0U CN207405109U (en) | 2017-09-18 | 2017-09-18 | A kind of water-reducing agent production system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108753333A (en) * | 2018-08-15 | 2018-11-06 | 山西新元太生物科技股份有限公司 | A kind of device that phenol slag recycling is generated to coal tar pitch |
| CN109651186A (en) * | 2019-01-02 | 2019-04-19 | 湖州欧利生物科技有限公司 | A kind of powdery sodium cocoyl glycinate process units and its technique |
-
2017
- 2017-09-18 CN CN201721192274.0U patent/CN207405109U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108753333A (en) * | 2018-08-15 | 2018-11-06 | 山西新元太生物科技股份有限公司 | A kind of device that phenol slag recycling is generated to coal tar pitch |
| CN109651186A (en) * | 2019-01-02 | 2019-04-19 | 湖州欧利生物科技有限公司 | A kind of powdery sodium cocoyl glycinate process units and its technique |
| CN109651186B (en) * | 2019-01-02 | 2023-12-12 | 湖州欧利生物科技有限公司 | Device and process for producing powdery sodium cocoyl glycinate |
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