CN212832865U - Clean production system for co-production of chlorinated paraffin and polyaluminum chloride - Google Patents
Clean production system for co-production of chlorinated paraffin and polyaluminum chloride Download PDFInfo
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- CN212832865U CN212832865U CN202021771621.7U CN202021771621U CN212832865U CN 212832865 U CN212832865 U CN 212832865U CN 202021771621 U CN202021771621 U CN 202021771621U CN 212832865 U CN212832865 U CN 212832865U
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- 239000012188 paraffin wax Substances 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 31
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 title claims abstract description 28
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 89
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 84
- 238000003860 storage Methods 0.000 claims abstract description 43
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 27
- 239000010881 fly ash Substances 0.000 claims abstract description 19
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000000460 chlorine Substances 0.000 claims abstract description 13
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 13
- 239000003513 alkali Substances 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 56
- 238000010521 absorption reaction Methods 0.000 claims description 53
- 238000006243 chemical reaction Methods 0.000 claims description 52
- 239000011552 falling film Substances 0.000 claims description 51
- 238000005406 washing Methods 0.000 claims description 36
- 239000002002 slurry Substances 0.000 claims description 27
- 238000006116 polymerization reaction Methods 0.000 claims description 26
- 238000007670 refining Methods 0.000 claims description 26
- 239000000047 product Substances 0.000 claims description 22
- 239000000498 cooling water Substances 0.000 claims description 13
- 239000005708 Sodium hypochlorite Substances 0.000 claims description 9
- XFWJKVMFIVXPKK-UHFFFAOYSA-N calcium;oxido(oxo)alumane Chemical compound [Ca+2].[O-][Al]=O.[O-][Al]=O XFWJKVMFIVXPKK-UHFFFAOYSA-N 0.000 claims description 9
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 8
- 239000006228 supernatant Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 50
- 229910000041 hydrogen chloride Inorganic materials 0.000 abstract description 22
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 abstract description 22
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract 1
- 238000010438 heat treatment Methods 0.000 description 8
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 6
- 229910001570 bauxite Inorganic materials 0.000 description 4
- 238000004090 dissolution Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000012629 purifying agent Substances 0.000 description 3
- 238000001035 drying Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 231100000481 chemical toxicant Toxicity 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000010292 electrical insulation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
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Abstract
The utility model discloses a clean production system of chlorinated paraffin coproduction polyaluminium chloride, it includes chlorine storage tank, chlorination reation kettle, refined reation kettle, paraffin storage tank, steam source, water source, hydrochloric acid jar and deacidification cauldron. The utility model has the advantages that the connection structure is simple and easy to realize; the aim of producing hydrochloric acid products by using the tail gas containing hydrogen chloride is fulfilled, so that the hydrogen chloride gas in the tail gas generates value, and economic benefits are brought to enterprises; hydrochloric acid products are not needed to be purchased, so that the production cost is reduced; the resource recycling of the fly ash is realized, and the production cost is saved; the environment is not polluted, and zero emission is realized; and the use amount of alkali liquor is reduced, resources are saved, energy is saved, the environment is protected, and the production cost is reduced.
Description
The technical field is as follows:
the utility model relates to a production system, in particular to clean production system of chlorinated paraffin coproduction polyaluminium chloride.
Background art:
chlorinated paraffin is a chlorinated derivative of C10-C24 paraffin, is commonly known as chlorinated paraffin, and has the characteristics of low volatility, fire resistance, flame retardance, good electrical insulation performance, chemical corrosion resistance, low price and the like, so the chlorinated paraffin is widely applied to the production of products such as cable materials, floor plates, hoses, artificial leather, rubber and the like and additives such as coating, lubricating oil and the like. At present, the chlorinated paraffin is produced by a thermal chlorination multi-kettle series production process, a large amount of heat is generated due to paraffin chlorination which is an exothermic reaction in the reaction process, a large amount of byproduct hydrogen chloride tail gas is also generated in the process of producing the chlorinated paraffin, and hydrogen chloride gas is dissolved in water to form byproduct hydrochloric acid in a water absorption mode at present; the tail gas after the separation of the hydrogen chloride gas also contains chlorine waste gas, which causes environmental pollution and resource waste.
Polyaluminium chloride is a water-soluble inorganic polymeric flocculant between aluminum chloride and aluminum hydroxide, has the advantages of strong adaptability, wide application and the like, and is widely applied to the aspects of water supply purification, wastewater treatment, papermaking sizing, casting forming and the like; at present, the process for producing polyaluminium chloride in China is to carry out dissolution reaction on bauxite and hydrochloric acid, and then carry out polymerization reaction on the obtained aluminum chloride solution and calcium aluminate to prepare the polyaluminium chloride. However, because the existing bauxite resources in China are deficient, the country is gradually restricting the exploitation of the bauxite resources, and the market price of the existing bauxite is higher, so that the cost for producing the water purifying agent is higher, the economic performance of the product is poor, and the industrialization is not facilitated; and hydrochloric acid also needs to be purchased, increasing the production cost.
At present, fly ash is used as bulk industrial solid waste in China, and contains a large amount of Al2O3The main method for treating the fly ash at present is to pile the fly ash, and a large amount of fly ash can generate flying dust and pollute the atmosphere without being treated; if discharged into a water system, the river can be silted, and toxic chemicals in the river can cause harm to human bodies and organisms.
The utility model has the following contents:
an object of the utility model is to provide a clean production system of chlorinated paraffin coproduction polyaluminium chloride who has realized hydrogen chloride and retrieved, and has protected the environment.
The utility model discloses by following technical scheme implement: the patent aims at providing a clean production system for co-producing chlorinated paraffin and polyaluminium chloride, which comprises a chlorine storage tank, a chlorination reaction kettle, a refining reaction kettle, a paraffin storage tank, a steam source, a water source, a hydrochloric acid tank and a deacidification kettle; the gas outlet of the chlorine storage tank is respectively communicated with the gas inlets of the chlorination reaction kettle and the refining reaction kettle; a discharge hole of the paraffin storage tank is communicated with a feed inlet of the chlorination reaction kettle; the steam source is communicated with an air inlet of a jacket of the chlorination reaction kettle; the water outlet of the circulating cooling water system is communicated with the water inlet of the jacket, and the water outlet of the jacket is communicated with the water inlet of the circulating cooling water system; the discharge hole of the chlorination reaction kettle is communicated with the feed hole of the refining reaction kettle; the water source is communicated with a water inlet of the refining reaction kettle; the supernatant outlet of the refining reaction kettle is communicated with the liquid inlet of the hydrochloric acid tank; a discharge port at the bottom of the refining reaction kettle is communicated with a feed port of the deacidification kettle; the steam source is communicated with the air inlet of the deacidification kettle.
Further, the system also comprises a fly ash bin, a batching pool, an acid-soluble reaction kettle, a cache pool, a vertical filter press, a polymerization pool, a calcium aluminate powder bin, a plate-and-frame filter press and a polyaluminium chloride solution storage tank; the liquid outlet of the hydrochloric acid tank and the water source are respectively communicated with the liquid inlet of the batching pool; the discharge hole of the fly ash bin is communicated with the feed inlet of the batching pool; the slurry outlet of the batching pool is communicated with the slurry inlet of the acid-soluble reaction kettle; the gas outlet of the steam source is communicated with the gas inlet of the jacket of the acid-soluble reaction kettle; the slurry outlet of the acid-soluble reaction kettle is communicated with the slurry inlet of the cache pool; the slurry outlet of the buffer pool is communicated with the slurry inlet of the vertical filter press; the liquid outlet of the vertical filter press is communicated with the liquid inlet of the polymerization tank; the gas outlet of the steam source is communicated with the gas inlet of the polymerization tank; the discharge hole of the calcium aluminate powder bin is communicated with the feed inlet of the polymerization tank; the slurry outlet of the polymerization tank is communicated with the slurry inlet of the plate-and-frame filter press; and the liquid outlet of the plate-and-frame filter press is communicated with the liquid inlet of the polyaluminium chloride solution storage tank.
Further, the drying device also comprises a drum dryer and a finished product bin; the liquid outlet of the plate-and-frame filter press is communicated with the liquid inlet of the drum-type dryer; and the discharge hole of the drum dryer is communicated with the feed inlet of the finished product bin.
Further, the device also comprises a first-stage falling film absorption tower, a second-stage falling film absorption tower, a third-stage falling film absorption tower, a first-stage water washing tower, a second-stage alkaline washing tower, a third-stage alkaline washing tower and a chimney which are sequentially communicated through a gas conveying pipe; the gas outlet of the deacidification kettle and the gas outlet of the chlorination reaction kettle are both communicated with the gas inlet of the primary falling film absorption tower; gas collecting hoods are respectively arranged above the cache tank and the polymerization tank; the gas collecting hood and the gas outlet of the drum dryer are respectively communicated with the gas inlet of the induced draft fan; the air outlet of the induced draft fan is communicated with the air inlet of the three-stage falling film absorption tower; the water outlet end of the cooling water pipeline is communicated with the water inlet of the third-stage falling film absorption tower, the liquid outlet of the third-stage falling film absorption tower is communicated with the liquid inlet of the second-stage falling film absorption tower, and the liquid outlet of the second-stage falling film absorption tower is communicated with the liquid inlet of the first-stage falling film absorption tower; the liquid outlet of the primary falling film absorption tower is communicated with the liquid inlet of the hydrochloric acid tank; the water source is communicated with the water inlet of the primary water washing tower, and the water outlet of the primary water washing tower is communicated with the water inlet of the water storage tank; the water outlet of the water storage tank is respectively communicated with the water inlets of the refining reaction kettle and the batching pool; a liquid outlet of the alkali liquor storage tank is respectively communicated with liquid inlets of the second-stage alkaline washing tower and the third-stage alkaline washing tower; liquid outlets of the second-stage alkaline washing tower and the third-stage alkaline washing tower are communicated with a liquid inlet of the sodium hypochlorite storage tank.
The utility model has the advantages that: 1. the utility model has simple connection structure and easy realization; the tail gas containing hydrogen chloride in the system is fully contacted with water through the first-stage falling film absorption tower, the second-stage falling film absorption tower and the third-stage falling film absorption tower, so that the hydrogen chloride is dissolved in the water, the aim of producing hydrochloric acid products by using the tail gas containing the hydrogen chloride is fulfilled, the hydrogen chloride gas in the tail gas generates value, and economic benefit is brought to enterprises; 2. the hydrochloric acid product is directly used as a raw material for producing the polyaluminium chloride water purifying agent, so that the hydrochloric acid product is not required to be purchased, and the production cost is reduced; 3. the polyaluminium chloride is prepared by adopting the fly ash as a raw material, so that the resource reutilization of the fly ash is realized, and the production cost is saved; meanwhile, the pollution of water resources, air and land caused by stacking of the fly ash is avoided, and the environment is protected; 4. the chlorine in the tail gas reacts with sodium hydroxide to generate sodium hypochlorite through the treatment of a secondary alkaline tower and a tertiary alkaline tower, and the sodium hypochlorite can be directly sold as a product, so that economic benefits are further brought to enterprises; 5. the tail gas discharged after being treated by the system of the utility model reaches the qualified standard, does not pollute the environment, and realizes zero discharge; and the use amount of alkali liquor is reduced, resources are saved, energy is saved, the environment is protected, and the production cost is reduced.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic view of the overall structure of the present invention.
The specific implementation mode is as follows:
as shown in fig. 1, a clean production system for co-production of chlorinated paraffin and polyaluminium chloride comprises a chlorine storage tank 1, a chlorination reaction kettle 2, a refining reaction kettle 3, a paraffin storage tank 4, a steam source 5, a water source 6, a hydrochloric acid tank 7, a deacidification kettle 8, a fly ash bin 9, a dosing tank 10, an acid dissolution reaction kettle 11, a buffer tank 12, a vertical filter press 13, a polymerization tank 14, a calcium aluminate powder bin 15, a plate-and-frame filter press 16, a polyaluminium chloride solution storage tank 17, a drum dryer 18 and a finished product bin 19; the gas outlet of the chlorine storage tank 1 is respectively communicated with the gas inlets of the chlorination reaction kettle 2 and the refining reaction kettle 3; a discharge hole of the paraffin storage tank 4 is communicated with a feed inlet of the chlorination reaction kettle 2; the steam source 5 is communicated with an air inlet of a jacket of the chlorination reaction kettle 2; the water outlet of the circulating cooling water system 33 is communicated with the water inlet of the jacket, and the water outlet of the jacket is communicated with the water inlet of the circulating cooling water system 33; the discharge hole of the chlorination reaction kettle 2 is communicated with the feed hole of the refining reaction kettle 3; the water source 6 is communicated with the water inlet of the refining reaction kettle 3; a supernatant outlet of the refining reaction kettle 3 is communicated with a liquid inlet of the hydrochloric acid tank 7; a discharge port at the bottom of the refining reaction kettle 3 is communicated with a feed port of the deacidification kettle 8; the steam source 5 is communicated with the air inlet of the deacidification kettle 8.
A liquid outlet of the hydrochloric acid tank 7 and a water source 6 are respectively communicated with a liquid inlet of the dosing tank 10; a discharge hole of the fly ash bin 9 is communicated with a feed inlet of the dosing pool 10; the slurry outlet of the batching tank 10 is communicated with the slurry inlet of the acid-soluble reaction kettle 11; the air outlet of the steam source 5 is communicated with the air inlet of the jacket of the acid dissolution reaction kettle 11; the slurry outlet of the acid-soluble reaction kettle 11 is communicated with the slurry inlet of the buffer pool 12; the slurry outlet of the buffer pool 12 is communicated with the slurry inlet of the vertical filter press 13; the liquid outlet of the vertical filter press 13 is communicated with the liquid inlet of the polymerization tank 14; the air outlet of the steam source 5 is communicated with the air inlet of the polymerization tank 14; the discharge hole of the calcium aluminate powder bin 15 is communicated with the feed inlet of the polymerization tank 14; the slurry outlet of the polymerization tank 14 is communicated with the slurry inlet of the plate-and-frame filter press 16; the liquid outlet of the plate-and-frame filter press 16 is respectively communicated with the liquid inlet of a polyaluminium chloride solution storage tank 17 and the liquid inlet of a drum dryer 18; the discharge hole of the drum dryer 18 is communicated with the feed inlet of the finished product bin 19.
The system also comprises a primary falling film absorption tower 20, a secondary falling film absorption tower 21, a tertiary falling film absorption tower 22, a primary water washing tower 23, a secondary alkaline washing tower 24, a tertiary alkaline washing tower 25 and a chimney 26 which are sequentially communicated through a gas pipe; the gas outlet of the deacidification kettle 8 and the gas outlet of the chlorination reaction kettle 2 are both communicated with the gas inlet of the primary falling film absorption tower 20; gas collecting hoods 27 are respectively arranged above the buffer tank 12 and the polymerization tank 14; the air outlets of the air collecting hood 27 and the roller dryer 18 are respectively communicated with the air inlet of an induced draft fan 28; an air outlet of the induced draft fan 28 is communicated with an air inlet of the three-stage falling film absorption tower 22; the water outlet end of the cooling water pipeline 29 is communicated with the water inlet of the third-stage falling film absorption tower 22, the liquid outlet of the third-stage falling film absorption tower 22 is communicated with the liquid inlet of the second-stage falling film absorption tower 21, and the liquid outlet of the second-stage falling film absorption tower 21 is communicated with the liquid inlet of the first-stage falling film absorption tower 20; the liquid outlet of the first-stage falling film absorption tower 20 is communicated with the liquid inlet of the hydrochloric acid tank 7; the water source 6 is communicated with the water inlet of the first-stage washing tower 23, and the water outlet of the first-stage washing tower 23 is communicated with the water inlet of the water storage tank 30; the water outlet of the water storage tank 30 is respectively communicated with the water inlets of the refining reaction kettle 3 and the batching tank 10; a liquid outlet of the alkali liquor storage tank 31 is respectively communicated with liquid inlets of the second-stage alkaline washing tower 24 and the third-stage alkaline washing tower 25; the liquid outlets of the second-stage alkaline washing tower 24 and the third-stage alkaline washing tower 25 are both communicated with the liquid inlet of a sodium hypochlorite storage tank 32.
The working process is as follows: chlorine and paraffin are introduced into a chlorination reaction kettle 2; introducing steam into a jacket of the chlorination reaction kettle 2 for heating, stopping heating after heating to about 85 ℃, starting an exothermic reaction on the materials, introducing circulating cooling water into the jacket of the chlorination reaction kettle 2 for cooling at the moment, and controlling the reaction temperature in the chlorination reaction kettle 2 to be below 140 ℃; after a certain time of reaction, generating 42# chlorinated paraffin and a byproduct hydrogen chloride gas; sending the 42# chlorinated paraffin to a refining reaction kettle 3, introducing chlorine and water into the refining reaction kettle 3 at the same time, continuously reacting to obtain 70# chlorinated paraffin, standing the refined reaction kettle 3 for a certain time after the reaction is finished, and sending the supernatant, namely the hydrochloric acid solution, to a hydrochloric acid tank 7 for storage; the lower 70# chlorinated paraffin precipitate is sent to a deacidification kettle 8, steam is introduced into the deacidification kettle 8 for heating, and hydrochloric acid in the 70# chlorinated paraffin is evaporated into hydrogen chloride gas to be discharged from the hydrogen chloride gas; to obtain a No. 70 chlorinated paraffin product.
Hydrochloric acid solution, fly ash and water produced during the production of chlorinated paraffin are mixed in a proportioning pool 10, and a hydrochloric acid product is directly used as a raw material for producing the polyaluminium chloride water purifying agent, so that the hydrochloric acid product is not required to be purchased, and the production cost is reduced; then sending the mixed materials into an acid-soluble reaction kettle 11, introducing steam into a jacket of the acid-soluble reaction kettle 11 for heating, stopping heating after heating to about 100 ℃, carrying out a reaction on the materials to generate aluminum chloride, sending the slurry into a buffer tank 12 for natural cooling after the reaction, sending the slurry into a vertical filter press 13 for filter pressing after cooling to about 70 ℃, sending the filtrate into a polymerization tank 14 for mixing with added calcium aluminate powder, introducing steam into the polymerization tank 14 for heating to enable the steam to reach the polymerization reaction temperature, stopping introducing steam, carrying out a polymerization reaction in the polymerization tank 14, and generating polyaluminum chloride; the reacted slurry is subjected to pressure filtration by a plate-and-frame filter press 16, and the filtrate can be taken as a product and sent to a polyaluminium chloride solution storage tank 17 for storage, and also can be sent to a drum dryer 18 for drying to obtain a solid polyaluminium chloride product which is stored in a finished product bin 19; the polyaluminium chloride is prepared by adopting the fly ash as a raw material, so that the resource reutilization of the fly ash is realized, and the production cost is saved; meanwhile, the pollution of water resource, air and land caused by stacking of the fly ash is avoided, and the environment is protected.
Tail gas containing hydrogen chloride and chlorine gas from the chlorination reaction kettle 2 and the deacidification kettle 8 is purified by a primary falling film absorption tower 20, a secondary falling film absorption tower 21, a tertiary falling film absorption tower 22, a primary water washing tower 23, a secondary alkaline washing tower 24 and a tertiary alkaline washing tower 25 in sequence, and finally purified tail gas is discharged from a chimney 26; tail gas from the buffer tank 12, the polymerization tank 14 and the drum dryer 18 is conveyed to the third-stage falling film absorption tower 22 through the induced draft fan 28 to be mixed with tail gas from the second-stage falling film absorption tower 21; cooling water sequentially enters a third-stage falling film absorption tower 22, a second-stage falling film absorption tower 21 and a first-stage falling film absorption tower 20 to sequentially absorb hydrogen chloride in tail gas and convert the hydrogen chloride into hydrochloric acid, the amount of the hydrogen chloride absorbed in the third-stage falling film absorption tower 22 is small and the hydrogen chloride is changed into dilute hydrochloric acid, the absorption amount of the hydrogen chloride in the second-stage falling film absorption tower 21 is increased, so that the concentration of the hydrochloric acid is increased, finally, a large amount of hydrogen chloride is absorbed in the first-stage falling film absorption tower 20 and is changed into a concentrated hydrochloric acid product which is recycled to a hydrochloric acid tank 7 to be stored, the aim of producing the hydrochloric acid product by using the tail gas containing the hydrogen chloride is fulfilled, the hydrogen chloride gas in the tail gas generates value; the tail gas from the third-level falling film absorption tower 22 is sprayed and cleaned by spray water in a first-level water washing tower 23, the cleaned wastewater is sent to a water storage tank 30, and finally the waste water is used as reaction water of a refining reaction kettle 3 and batching water in a batching tank 10 and is respectively sent to the refining reaction kettle 3 and the batching tank 10, the cleaned tail gas is sequentially sent to a second-level alkaline washing tower 24 and a third-level alkaline washing tower 25, chlorine in the tail gas reacts with sodium hydroxide to generate sodium hypochlorite, the sodium hypochlorite solution is stored in a sodium hypochlorite storage tank 32 and is sold as a product, and further economic benefits are brought to enterprises; the tail gas discharged after being treated by the system of the utility model reaches the qualified standard, does not pollute the environment, and realizes zero discharge; the usage amount of alkali liquor is reduced, resources are saved, energy is saved, the environment is protected, and the production cost is reduced; the utility model discloses connection structure is simple, easily realizes.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. A clean production system for co-producing chlorinated paraffin and polyaluminium chloride is characterized by comprising a chlorine storage tank, a chlorination reaction kettle, a refining reaction kettle, a paraffin storage tank, a steam source, a water source, a hydrochloric acid tank and a deacidification kettle;
the gas outlet of the chlorine storage tank is respectively communicated with the gas inlets of the chlorination reaction kettle and the refining reaction kettle;
a discharge hole of the paraffin storage tank is communicated with a feed inlet of the chlorination reaction kettle; the steam source is communicated with an air inlet of a jacket of the chlorination reaction kettle; the water outlet of the circulating cooling water system is communicated with the water inlet of the jacket, and the water outlet of the jacket is communicated with the water inlet of the circulating cooling water system;
the discharge hole of the chlorination reaction kettle is communicated with the feed hole of the refining reaction kettle; the water source is communicated with a water inlet of the refining reaction kettle; the supernatant outlet of the refining reaction kettle is communicated with the liquid inlet of the hydrochloric acid tank;
a discharge port at the bottom of the refining reaction kettle is communicated with a feed port of the deacidification kettle; the steam source is communicated with the air inlet of the deacidification kettle.
2. The clean production system for co-production of chlorinated paraffin and polyaluminum chloride according to claim 1, further comprising a fly ash bin, a dosing tank, an acid-soluble reaction kettle, a buffer tank, a vertical filter press, a polymerization tank, a calcium aluminate powder bin, a plate-and-frame filter press and a polyaluminum chloride solution storage tank;
the liquid outlet of the hydrochloric acid tank and the water source are respectively communicated with the liquid inlet of the batching pool; the discharge hole of the fly ash bin is communicated with the feed inlet of the batching pool;
the slurry outlet of the batching pool is communicated with the slurry inlet of the acid-soluble reaction kettle; the gas outlet of the steam source is communicated with the gas inlet of the jacket of the acid-soluble reaction kettle;
the slurry outlet of the acid-soluble reaction kettle is communicated with the slurry inlet of the cache pool; the slurry outlet of the buffer pool is communicated with the slurry inlet of the vertical filter press;
the liquid outlet of the vertical filter press is communicated with the liquid inlet of the polymerization tank; the gas outlet of the steam source is communicated with the gas inlet of the polymerization tank; the discharge hole of the calcium aluminate powder bin is communicated with the feed inlet of the polymerization tank;
the slurry outlet of the polymerization tank is communicated with the slurry inlet of the plate-and-frame filter press; and the liquid outlet of the plate-and-frame filter press is communicated with the liquid inlet of the polyaluminium chloride solution storage tank.
3. The clean production system for the co-production of chlorinated paraffin and polyaluminum chloride as claimed in claim 2, further comprising a drum dryer and a finished product bin;
the liquid outlet of the plate-and-frame filter press is communicated with the liquid inlet of the drum-type dryer; and the discharge hole of the drum dryer is communicated with the feed inlet of the finished product bin.
4. The clean production system for co-production of chlorinated paraffin and polyaluminium chloride as claimed in claim 3, further comprising a primary falling film absorption tower, a secondary falling film absorption tower, a tertiary falling film absorption tower, a primary water washing tower, a secondary alkaline washing tower, a tertiary alkaline washing tower and a chimney which are sequentially communicated through a gas pipe;
the gas outlet of the deacidification kettle and the gas outlet of the chlorination reaction kettle are both communicated with the gas inlet of the primary falling film absorption tower;
gas collecting hoods are respectively arranged above the cache tank and the polymerization tank; the gas collecting hood and the gas outlet of the drum dryer are respectively communicated with the gas inlet of the induced draft fan; the air outlet of the induced draft fan is communicated with the air inlet of the three-stage falling film absorption tower;
the water outlet end of the cooling water pipeline is communicated with the water inlet of the third-stage falling film absorption tower, the liquid outlet of the third-stage falling film absorption tower is communicated with the liquid inlet of the second-stage falling film absorption tower, and the liquid outlet of the second-stage falling film absorption tower is communicated with the liquid inlet of the first-stage falling film absorption tower; the liquid outlet of the primary falling film absorption tower is communicated with the liquid inlet of the hydrochloric acid tank;
the water source is communicated with the water inlet of the primary water washing tower, and the water outlet of the primary water washing tower is communicated with the water inlet of the water storage tank; the water outlet of the water storage tank is respectively communicated with the water inlets of the refining reaction kettle and the batching pool;
a liquid outlet of the alkali liquor storage tank is respectively communicated with liquid inlets of the second-stage alkaline washing tower and the third-stage alkaline washing tower; liquid outlets of the second-stage alkaline washing tower and the third-stage alkaline washing tower are communicated with a liquid inlet of a sodium hypochlorite storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021771621.7U CN212832865U (en) | 2020-08-21 | 2020-08-21 | Clean production system for co-production of chlorinated paraffin and polyaluminum chloride |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115261070A (en) * | 2022-08-03 | 2022-11-01 | 常熟理工学院 | Method for synergistically preparing chlorinated paraffin and polyaluminum chloride flocculating agent |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115261070A (en) * | 2022-08-03 | 2022-11-01 | 常熟理工学院 | Method for synergistically preparing chlorinated paraffin and polyaluminum chloride flocculating agent |
| CN115261070B (en) * | 2022-08-03 | 2023-07-07 | 常熟理工学院 | Method for preparing chlorinated paraffin and polyaluminum chloride flocculant in synergistic manner |
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