CN103539299B - Process for recycling wastewater containing low boiling-point organism such as formaldehyde and high-concentration inorganic salt - Google Patents
Process for recycling wastewater containing low boiling-point organism such as formaldehyde and high-concentration inorganic salt Download PDFInfo
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- CN103539299B CN103539299B CN201210236065.7A CN201210236065A CN103539299B CN 103539299 B CN103539299 B CN 103539299B CN 201210236065 A CN201210236065 A CN 201210236065A CN 103539299 B CN103539299 B CN 103539299B
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- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 title claims abstract description 101
- 229910017053 inorganic salt Inorganic materials 0.000 title claims abstract description 55
- 239000002351 wastewater Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000008569 process Effects 0.000 title claims abstract description 25
- 238000004064 recycling Methods 0.000 title abstract description 4
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000004821 distillation Methods 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 230000008020 evaporation Effects 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 15
- 150000003839 salts Chemical class 0.000 claims abstract description 11
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 6
- 239000011780 sodium chloride Substances 0.000 claims abstract description 3
- 230000006835 compression Effects 0.000 claims description 35
- 238000007906 compression Methods 0.000 claims description 35
- 239000006200 vaporizer Substances 0.000 claims description 35
- 238000007599 discharging Methods 0.000 claims description 30
- 239000007864 aqueous solution Substances 0.000 claims description 17
- 150000002894 organic compounds Chemical class 0.000 claims description 16
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical group O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 claims description 15
- 238000009835 boiling Methods 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 230000000694 effects Effects 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 13
- 239000000243 solution Substances 0.000 claims description 13
- 238000002425 crystallisation Methods 0.000 claims description 10
- 238000001465 metallisation Methods 0.000 claims description 8
- 238000006386 neutralization reaction Methods 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 230000008025 crystallization Effects 0.000 claims description 5
- 239000012535 impurity Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 5
- 239000012452 mother liquor Substances 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 5
- -1 inorganic acid radical ion Chemical class 0.000 claims description 3
- 239000000470 constituent Substances 0.000 claims description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 21
- 235000002639 sodium chloride Nutrition 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 5
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 abstract description 3
- 239000002918 waste heat Substances 0.000 abstract description 3
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 2
- 235000019270 ammonium chloride Nutrition 0.000 abstract description 2
- 230000008901 benefit Effects 0.000 abstract description 2
- 230000008878 coupling Effects 0.000 abstract description 2
- 238000010168 coupling process Methods 0.000 abstract description 2
- 238000005859 coupling reaction Methods 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 2
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 2
- 238000007670 refining Methods 0.000 abstract 2
- 239000007832 Na2SO4 Substances 0.000 abstract 1
- 239000012266 salt solution Substances 0.000 abstract 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 9
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000000460 chlorine Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 239000003905 agrochemical Substances 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000003317 industrial substance Substances 0.000 description 2
- 239000010985 leather Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000011017 operating method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 1
- SVOZWQVJNZEQFC-UHFFFAOYSA-M S(=O)(=O)([O-])[O-].Cl[NH3+].[Na+] Chemical compound S(=O)(=O)([O-])[O-].Cl[NH3+].[Na+] SVOZWQVJNZEQFC-UHFFFAOYSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229960001040 ammonium chloride Drugs 0.000 description 1
- 230000003444 anaesthetic effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 231100000315 carcinogenic Toxicity 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 210000003169 central nervous system Anatomy 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000013355 food flavoring agent Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- JUMYIBMBTDDLNG-OJERSXHUSA-N hydron;methyl (2r)-2-phenyl-2-[(2r)-piperidin-2-yl]acetate;chloride Chemical compound Cl.C([C@@H]1[C@H](C(=O)OC)C=2C=CC=CC=2)CCCN1 JUMYIBMBTDDLNG-OJERSXHUSA-N 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000003471 mutagenic agent Substances 0.000 description 1
- 231100000707 mutagenic chemical Toxicity 0.000 description 1
- 230000003505 mutagenic effect Effects 0.000 description 1
- 210000001328 optic nerve Anatomy 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 230000007170 pathology Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- 210000001525 retina Anatomy 0.000 description 1
- 229940099204 ritalin Drugs 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a process for recycling wastewater containing low-boiling-point organisms such as formaldehyde and high-concentration inorganic salt. The process mainly adopts equipment such as a refining tower and a multiple-effect evaporation system, and an inorganic salt solution with high concentration and organisms such as methanol and formaldehyde in the wastewater are obtained by processing the wastewater containing low-boiling-point organisms with the concentration of 0.01-10% or higher and inorganic salts such as NaCl, Na2SO4 or NH4Cl and the like with the concentration of 1-40% or higher by using the refining tower and the multiple-effect evaporation system. In the process, preheating of raw materials and heating in the middle process are realized by utilizing waste heat of tower top steam and tower bottom material liquid in the distillation process, so as to form a thermal coupling network, and therefore the energy consumption for treating wastewater per unit mass is greatly reduced as compared with that of the conventional processes. The process has the outstanding advantages of low energy consumption, high efficiency and the like.
Description
Technical field
The present invention relates to a kind of containing low-boiling-point organic compound and high density inorganic salt waste water resource metallization processes such as formaldehyde.
Background technology
Containing the waste water of the low-boiling-point organic compound such as formaldehyde and high density inorganic salt refer in the industries such as pharmacy, spices and essence, coating, leather, plastics, produce contain the organism of the boiling points such as formaldehyde, methyl alcohol, ethanol, methane, vinyl acetic monomer, ritalin lower than water, and contain the inorganic salt such as high strength ammonium-chloride, Repone K, sodium-chlor, ammonium sulfate, potassium sulfate, sodium sulfate simultaneously or contain high density Cl
-, or SO
4 =, or NO
3 -deng the waste water of inorganic acid radical ion.These low-boiling-point organic compounds and inorganic salt are all valuable resources, are worth recycling.If formaldehyde, methyl alcohol, ethanol are conventional chemical industry basic material and clean fuel liquids, it is widely used in the industry such as organic synthesis, medicine, agricultural chemicals, coating, dyestuff, the energy and national defence; Formaldehyde is a kind of important industrial chemicals, at the field of chemical synthesis such as chemical pharmaceuticals, especially has very important effect at agricultural chemicals and the synthetic field of intermediate thereof; Inorganic salt, as sodium-chlor, it,, at the industrial basic material that can be used for manufacturing hydrogen, caustic soda, chlorine etc., can be used as heat treatment agent in Iron And Steel Industry, also has important effect simultaneously in pharmaceutical industries.
Meanwhile, if the direct discharge of such trade effluent containing low-boiling-point organic compound and high density inorganic salt will cause great pollution to environment.As methyl alcohol, there is toxicity, excessive contact, can have anesthetic action to central nervous system, and optic nerve and retina are had to special selective action, causes pathology, also can cause generation penetrating property oxypathy.Formaldehyde, as a kind of high toxicity carcinogenic substance, is now defined as carcinogenic and teratogenecity material by the World Health Organization, is also one of potential strong mutagen.
If these organism and salt are reclaimed, both can save resource, be conducive to again environment protection.Therefore be necessary the recycling treatment process technology of development of new.
Summary of the invention
The object of this invention is to provide a kind of waste water resource metallization processes containing the low-boiling-point organic compounds such as formaldehyde and high density inorganic salt (acid ion), as shown in Figure 1.The present invention adopts multiple-effect evaporation and the integrated method of rectifying, organism in waste water and inorganic salt are reclaimed and realize its resource utilization, utilize the waste heat of tower bed material liquid and overhead vapours as the thermal source of raw material preheating and multiple-effect evaporator simultaneously, thereby realize the object of accompanied by substantial power saving.
Object of the present invention can realize by following technical solution:
Containing a waste water resource metallization processes for low-boiling-point organic compound and high density inorganic salt, it comprises the following steps:
Step 1. heat exchange: by NaCl or Na containing 0.01%-10% or greater concn low-boiling-point organic compound and 1%-40% or greater concn
2sO
4, or NH
4cl inorganic salt or by the Cl that contains 1%-40% or greater concn or SO
4 2-, or NO
3 -deng the waste water raw material of inorganic acid radical ion enter in waste water by pipeline 1 and storage tank one V-1 in carry out alkali neutralization after, by fluid delivery pump, P-1 carries, carry out three preheatings through interchanger A E-1, interchanger B E-2 and C E-3 respectively, the thermal source of interchanger A E-1 is the low-temperature wastewater in relay tank V-2; The heat source of interchanger B E-2 is the overhead vapours of the 3rd utmost point vaporizer T-5; The heat source of interchanger C E-3 is the overhead vapours of rectifying tower T-1.The heat source temperature of three grades of vaporizer E-1, E-2, E-3 raises gradually;
Step 2. light constituent separates with solution: enter atmospheric distillation tower T-1 through the waste water raw material of three grades of preheatings by pipeline 33 and separate, overhead vapours through interchanger C E-3 to raw material preheating after, part is refluxed by pipeline 55, rest materials is by pipeline 27 dischargings, this discharging consist of not the lower boiling organic aqueous solution containing formaldehyde and inorganic salt, this aqueous solution is sent to conventional rectification system again and carries out fine separation, obtains the high purity product of different components; Its separation method is routine techniques, does not repeat them here
.
Materials at bottom of tower is the aqueous solution containing inorganic salt and formaldehyde, part heats through reboiler E-4, part is carried out discharging by pipeline 66, the heat source of reboiler E-4 is the overhead vapours of compression rectification tower T-2, like this, the first step that has just realized this waste water separates, i.e. formaldehyde, inorganic salt mixing solutions and other organic separation;
Step 3. formaldehyde separates with salts solution: at the bottom of the tower of atmospheric distillation tower T-1, the feed liquid of discharging is by fluid delivery pump two P-2, enter into compression rectification tower T-2 through piping 77 and carry out compression rectification, the pressure of compression rectification tower T-2 is 2-10 atm, the pressure of optimizing is 3-6 atm, tower top is the steam containing formaldehyde 30%-37%, it is condensed after the reboiler of rectifying tower T-1 and the well heater of one-level vaporizer T-3, a phlegma part refluxes, a part reclaims from pipeline 12 dischargings, at the bottom of the tower of compression rectification tower T-2, be to contain concentration of formaldehyde lower than 0.05% inorganic salt waste water, the heat source of tower bottom reboiler is the raw steam of 0.8-1.0MPa, like this, the second step of just having realized this waste water separates, be inorganic salt and the separating of formaldehyde,
Step 4. water separates with salt: the feed liquid of discharging at the bottom of the tower of compression rectification tower T-2, entered the first evaporator T-3 of triple effect evaporation system (if desired more multiple-effect) through piping 14 by fluid delivery pump three P-3, second stage vaporizer T-4 and third evaporator T-5 evaporate, the heat source of first evaporator T-3 is the overhead vapours of compression rectification tower T-2, the heat source of second stage vaporizer T-4 is the overhead vapours of first evaporator T-3, the heat source of third evaporator T-5 is the overhead vapours of second stage vaporizer T-4, the steam (generally only for containing micro-content organism and water vapour) at first evaporator T-3 and vaporizer T-4 vaporizer top, the second stage is respectively in order to heat lower 1st effective evaporator, after being then condensed into liquid, enter storage tank V-2, three grades of vaporizer T-3, working pressure in T-4 and T-5 progressively reduces, storage tank V-2 is connected with vacuum system.And the steam at T-5 top is because temperature is lower, can only be used as the use of the first step preheating of waste water raw material;
After triple effect evaporation (if desired more multiple-effect), it at the bottom of the tower of third evaporator T-5, is the salt concentrated liquid that does not contain lower boiling organic impurity, it is conveyed to crystallisation by cooling and obtains inorganic salt product, mother liquor after crystallization can again be sent back in storage tank one V-1 and circulate, in storage tank two V-2, be only the phlegma containing micro-content organism and water vapor, this phlegma can be fed to the processing up to standard of the further degree of depth of biochemical treatment system.Like this, the 3rd step that has just realized this waste water separates, i.e. separating of water and inorganic salt.
Advantage of the present invention is:
Above-mentioned is operate continuously process containing low-boiling-point organic compound and high density inorganic salt waste water resource metallization processes, and described rectifying tower T-1 and T-2 are respectively atmospheric distillation tower and compression rectification tower, for separating of the aqueous solution of low-boiling-point organic compound, formaldehyde and inorganic salt.And T-3, T-4 and T-5 in triple effect evaporation system (if desired more multiple-effect) is three vaporizers that pressure reduces successively, it is intended to reclaim the inorganic salt in waste water, makes the hear rate of this process be down to minimum degree simultaneously.The thermal source of vaporizer T-3 is the steam at the compression rectification tower T-2 top high temperature formalin liquid-vapor mixture after the heat release of atmospheric distillation tower T-1 tower bottom reboiler, and the evaporation thermal source of T-4 and T-5 is respectively the steam at front 1st effective evaporator top.
In the low-boiling-point organic compounds such as above-mentioned formaldehyde and high density inorganic salt waste water resource metallization processes, except the heat source of the tower bottom reboiler of T-2 is made a living steam, remaining raw material preheating and heat source are all the steam at miscellaneous equipment top and the hot wastewater of bottom, at the bottom of utilizing tower and the waste heat of tower top feed liquid and reboiler and feed preheater form thermal coupling, thereby realize the object of accompanied by substantial power saving.
Above-mentioned is all important industrial chemicals containing the inorganic salt and the organism that reclaim in the low-boiling-point organic compounds such as formaldehyde and high density inorganic salt waste water resource metallization processes, unlike traditional technique, adopt direct biochemical treatment, make product but they are reclaimed respectively to resource utilization, realize resources circulation.
Brief description of the drawings
Fig. 1 is of the present invention containing low-boiling-point organic compound and high density inorganic salt waste water reclaiming process flow diagram.Wherein:
P-1, P-2, P-3, P-4, P-5, P-6, P-7 is fluid delivery pump one to seven, V-1 is in raw material waste water and storage tank one, V-2 is organic aqueous solution storage tank two, E-1, E-2, E-3 is interchanger A, B, C, E-4 is reboiler, T-1, T-2 is respectively normal pressure and compression rectification tower, T-3, T-4, T-5 is the one-level in multi-effect evaporation system, secondary, three grades of vaporizers, 1-27 is fluid-transporting tubing one to 27, 12 is concentrated formaldehyde outlet, 25 is strong brine discharge port, 26 is waste water discharge port after treatment, go again biochemical treatment, 27 is organic mixture discharge port, go conventional rectification system, 28 steam inlets of making a living.
Embodiment
Further illustrate by the following examples the present invention.
embodiment 1:
By in essence and flavoring agent industry, produce containing the low-boiling-point organic compound such as formaldehyde and the technical process of high density inorganic salt waste water reclaiming as shown in Figure 1.This system is mainly made up of distillation system and multi-effect evaporation system.Be provided with metering and control instruments and pipeline at each equipment room.Waste water containing 0.01% lower boiling organic mixture (comprising formaldehyde, methyl alcohol, monochloro methane etc.) and 10% inorganic salt is entered and in neutralization tank V-1, carried out alkali neutralization by pipeline 1, solution is become to neutrality, carry out three preheatings through interchanger E-1, E-2 and E-3 afterwards, the thermal source of interchanger A E-1 is the mixing solutions in tundish V-2, interchanger B E-2 thermal source is the steam at third evaporator T-5 top, and E-3 thermal source is the steam at atmospheric distillation tower T-1 top.Raw material through three preheatings enters atmospheric distillation tower T-1 by pipeline 33, atmospheric distillation tower T-1 overhead vapours through interchanger C E-3 to raw material preheating after, part is refluxed by pipeline 55, rest materials is by pipeline 27 dischargings, this discharging consist of not the lower boiling organic aqueous solution containing formaldehyde and inorganic salt, this aqueous solution enters into conventional rectification system and separates, and obtains their technical grade product separately.Materials at bottom of tower is the aqueous solution containing inorganic salt and formaldehyde, part is carried out discharging by pipeline 66, part heats through reboiler E-4, feed liquid enters into compression rectification tower T-2 by fluid delivery pump two P-2 through piping 77 and carries out compression rectification, the pressure of compression rectification tower T-2 is 2 atm, tower top discharging is the steam containing formaldehyde 30%, it is condensed after the reboiler of atmospheric distillation tower T-1 and the well heater of first evaporator T-3, a phlegma part refluxes, and a part reclaims from pipeline 12 dischargings.At the bottom of the tower of compression rectification tower T-2, be that to contain concentration of formaldehyde be 0.003% inorganic salt waste water, the heat source of tower bottom reboiler is the raw steam of 8 kilograms.
The feed liquid of discharging at the bottom of the tower of compression rectification tower T-2, entered the first evaporator T-3 of triple effect evaporation system (if desired more multiple-effect) through piping 14 by fluid delivery pump three P-3, second stage vaporizer T-4 and third evaporator T-5 evaporate, the heat source of first evaporator T-3 is the overhead vapours of compression rectification tower T-2, the heat source of second stage vaporizer T-4 is the overhead vapours of first evaporator T-3, the heat source of third evaporator T-5 is the overhead vapours of second stage vaporizer T-4, the steam (generally only for containing micro-content organism and water vapour) at first evaporator T-3 and vaporizer T-4 top, the second stage is respectively in order to heat lower 1st effective evaporator, after being then condensed into liquid, enter storage tank V-2, first evaporator T-3, working pressure in second stage vaporizer T-4 and third evaporator T-5 progressively reduces, T-1, T-2, the pressure of T-3 is respectively 0.57atm, 0.38atm, 0.23atm, storage tank V-2 is connected with vacuum system.
After triple effect evaporation system (if desired more multiple-effect), at the bottom of the tower of third evaporator T-5, be the salt concentrated liquid containing lower boiling organic impurity not, it can be conveyed to crystallisation by cooling system, obtain the crystalline product of inorganic salt.Mother liquor after crystallization can again be sent back in storage tank V-1 and circulate.It in storage tank V-2, is only the phlegma containing micro-content organism and water vapor.This phlegma enters into the further processing up to standard of biochemical treatment system.
The whole process formaldehyde rate of recovery is 98.9%, and the rate of recovery of inorganic salt is 99.7%, and energy consumption has reduced by 37% compared with traditional technology.
embodiment 2:
Operating method is as embodiment 1.
During the waste water containing 4.2% lower boiling organic mixture (comprising formaldehyde, methyl alcohol, ethanol, monochloro methane etc.) and 23% inorganic salt producing in pharmaceutical industry is entered by pipeline 1 with in storage tank V-1, carry out alkali neutralization, solution is become to neutrality, process interchanger A, B and C E-1, E-2 and E-3 carry out three preheatings afterwards, the thermal source of interchanger A E-1 is the mixing solutions in tundish V-2, interchanger B E-2 thermal source is the steam at the 3rd utmost point vaporizer T-5 top, and interchanger C E-3 thermal source is the steam at atmospheric distillation tower T-1 top.Raw material through three preheatings enters atmospheric distillation tower T-1 by pipeline 33, atmospheric distillation tower T-1 overhead vapours through interchanger C E-3 to raw material preheating after, part is refluxed by pipeline 55, rest materials is by pipeline 27 dischargings, this discharging consist of not the lower boiling organic aqueous solution containing formaldehyde and inorganic salt, this aqueous solution enters into conventional rectification system and separates, and obtains their technical grade product separately.Materials at bottom of tower is the aqueous solution containing inorganic salt and formaldehyde, part is carried out discharging by pipeline 66, part heats through reboiler E-4, feed liquid enters into compression rectification tower T-2 by fluid delivery pump two P-2 through piping 77 and carries out compression rectification, the pressure of compression rectification tower T-2 is 5 atm, tower top discharging is the steam containing formaldehyde 34.4%, it is condensed after the reboiler of atmospheric distillation tower T-1 and first evaporator T-3 heat exchange, a phlegma part refluxes, and a part reclaims from pipeline 12 dischargings.At the bottom of the tower of compression rectification tower T-2, be that to contain concentration of formaldehyde be 0.02% inorganic salt waste water, the heat source of tower bottom reboiler is the raw steam of 9 kilograms.
The feed liquid of discharging at the bottom of the tower of compression rectification tower T-2, entered the first evaporator T-3 of triple effect evaporation system through piping 14 by fluid delivery pump three P-3, second stage vaporizer T-4 and third evaporator T-5 evaporate, the heat source of first evaporator T-3 is the overhead vapours of compression rectification tower T-2, the heat source of second stage vaporizer T-4 is the overhead vapours of first evaporator T-3, the heat source of third evaporator T-5 is the overhead vapours of second stage vaporizer T-4, the steam (generally only for containing micro-content organism and water vapour) at first evaporator T-3 and vaporizer T-4 top, the second stage is respectively in order to heat lower 1st effective evaporator, after being then condensed into liquid, enter storage tank V-2, first evaporator T-3, working pressure in second stage vaporizer T-4 and third stage T-5 progressively reduces, T-1, T-2, the pressure of T-3 is respectively 0.66atm, 0.43atm, 0.31atm, storage tank V-2 is connected with vacuum system.
After triple effect evaporation system (if desired more multiple-effect), at the bottom of the tower of third evaporator T-5, be the salt concentrated liquid containing lower boiling organic impurity not, it can be conveyed to crystallisation by cooling system, obtain the crystalline product of inorganic salt.Mother liquor after crystallization can again be sent back in storage tank V-1 and circulate.It in storage tank V-2, is only the phlegma containing micro-content organism and water vapor.This phlegma enters into the further processing up to standard of biochemical treatment system.
The whole process formaldehyde rate of recovery is 98.2%, and the rate of recovery of inorganic salt is 98.9%, and energy consumption has reduced by 34% compared with traditional technology.
embodiment 3:
Operating method is as embodiment 1.
During the waste water containing 10% lower boiling organic mixture (comprising formaldehyde, methyl alcohol, monochloro methane etc.) and 40% inorganic salt producing in leather industry is entered by pipeline 1 with in storage tank V-1, carry out alkali neutralization, solution is become to neutrality, process interchanger A, B and C E-1, E-2 and E-3 carry out three preheatings afterwards, the thermal source of interchanger A E-1 is the mixing solutions in tundish V-2, interchanger B E-2 thermal source is the steam at third evaporator T-5 top, and interchanger C E-3 thermal source is the steam at atmospheric distillation tower T-1 top.Raw material through three preheatings enters atmospheric distillation tower T-1 by pipeline 33, atmospheric distillation tower T-1 overhead vapours through interchanger C E-3 to raw material preheating condensation after, part is refluxed by pipeline 55, rest materials is by pipeline 27 dischargings, this discharging consist of not the lower boiling organic aqueous solution containing formaldehyde and inorganic salt, this aqueous solution enters into conventional rectification system and separates, and obtains their technical grade product separately.Materials at bottom of tower is the aqueous solution containing inorganic salt and formaldehyde, part is carried out discharging by pipeline 66, part heats through the reboiler E-4 of atmospheric distillation tower, feed liquid enters into compression rectification tower T-2 by fluid delivery pump two P-2 through piping 7 and carries out compression rectification, the pressure of compression rectification tower T-2 is 10 atm, tower top discharging is the steam containing formaldehyde 37%, it is condensed after the reboiler of atmospheric distillation tower T-1 and the heat exchanger of first evaporator T-3, a phlegma part refluxes, and a part reclaims from pipeline 12 dischargings.At the bottom of the tower of compression rectification tower T-2, be that to contain concentration of formaldehyde be 0.01% inorganic salt waste water, the heat source of tower bottom reboiler is the raw steam of 10 kilograms.
The feed liquid of discharging at the bottom of the tower of compression rectification tower T-2, entered the first evaporator T-3 of triple effect evaporation system through piping 14 by fluid delivery pump three P-3, second stage vaporizer T-4 and third evaporator T-5 evaporate, the heat source of first evaporator T-3 is the overhead vapours of compression rectification tower T-2, the heat source of second stage vaporizer T-4 is the overhead vapours of first evaporator T-3, the heat source of third evaporator T-5 is the overhead vapours of second stage vaporizer T-4, the steam (generally only for containing micro-content organism and water vapour) at first evaporator T-3 and vaporizer T-4 top, the second stage is respectively in order to heat lower 1st effective evaporator, after being then condensed into liquid, enter storage tank V-2, first evaporator T-3, working pressure in second stage vaporizer T-4 and third evaporator T-5 progressively reduces, T-1, T-2, the pressure of T-3 is respectively 0.62atm, 0.41atm, 0.28atm, storage tank V-2 is connected with vacuum system.
After triple effect evaporation system (if desired more multiple-effect), at the bottom of the tower of third evaporator T-5, be the salt concentrated liquid containing lower boiling organic impurity not, it can be conveyed to crystallisation by cooling system, obtain the crystalline product of inorganic salt.Mother liquor after crystallization can again be sent back in storage tank V-1 and circulate.It in storage tank V-2, is only the phlegma containing micro-content organism and water vapor.This phlegma enters into the further processing up to standard of biochemical treatment system.
The whole process formaldehyde rate of recovery is 98.1%, and the rate of recovery of inorganic salt is 99.1%, and energy consumption has reduced by 32% compared with traditional technology.
Claims (1)
1. containing a waste water resource metallization processes for low-boiling-point organic compound and high density inorganic salt, it is characterized in that it comprises the following steps:
Step 1. heat exchange: by NaCl or Na containing 0.01%-10% or greater concn low-boiling-point organic compound and 1%-40% or greater concn
2sO
4, or NH
4cl inorganic salt or will contain the Cl of 1%-40% or greater concn
-, or SO
4 2-, or NO
3 -the waste water raw material of inorganic acid radical ion entered in waste water by pipeline (1) and storage tank one (V-1) in carry out alkali neutralization after, carried by fluid delivery pump (P-1), pass through respectively interchanger A (E-1), interchanger B (E-2) and C (E-3) and carry out three preheatings, the thermal source of interchanger A (E-1) is the low-temperature wastewater in relay tank (V-2); The heat source of interchanger B (E-2) is the overhead vapours of the 3rd utmost point vaporizer (T-5); The heat source of interchanger C (E-3) is the overhead vapours of rectifying tower (T-1).The heat source temperature of three grades of vaporizer E-1, E-2, E-3 raises gradually;
Step 2. light constituent separates with solution: enter atmospheric distillation tower (T-1) through the waste water raw material of three grades of preheatings by pipeline three (3) and separate, overhead vapours through interchanger C (E-3) to after raw material preheating, part is refluxed by pipeline five (5), rest materials is by pipeline 27 (27) dischargings, this discharging consist of not the lower boiling organic aqueous solution containing formaldehyde and inorganic salt, this aqueous solution is sent to conventional rectification system again and carries out fine separation, obtains the high purity product of different components; Its separation method is routine techniques, does not repeat them here;
Materials at bottom of tower is the aqueous solution containing inorganic salt and formaldehyde, part heats through reboiler (E-4), part is carried out discharging by pipeline six (6), the heat source of reboiler (E-4) is the overhead vapours of compression rectification tower (T-2), like this, the first step that has just realized this waste water separates, i.e. formaldehyde, inorganic salt mixing solutions and other organic separation;
Step 3. formaldehyde separates with salts solution: at the bottom of the tower of atmospheric distillation tower (T-1), the feed liquid of discharging is by fluid delivery pump two (P-2), enter into compression rectification tower (T-2) through piping seven (7) and carry out compression rectification, the pressure of compression rectification tower (T-2) is 2-10atm, tower top is the steam containing formaldehyde 30%-37%, it is condensed after the reboiler of rectifying tower (T-1) and the well heater of one-level vaporizer (T-3), a phlegma part refluxes, a part reclaims from pipeline ten two (12) dischargings, at the bottom of the tower of compression rectification tower (T-2), be to contain concentration of formaldehyde lower than 0.05% inorganic salt waste water, the heat source of tower bottom reboiler is the raw steam of 0.8-1.0MPa, like this, the second step of just having realized this waste water separates, be inorganic salt and the separating of formaldehyde,
Step 4. water separates with salt: the feed liquid of discharging at the bottom of the tower of compression rectification tower (T-2), entered the first evaporator (T-3) of triple effect evaporation system (if desired more multiple-effect) through piping ten four (14) by fluid delivery pump three (P-3), second stage vaporizer (T-4) and third evaporator (T-5) evaporate, the heat source of first evaporator (T-3) is the overhead vapours of compression rectification tower (T-2), the heat source of second stage vaporizer (T-4) is the overhead vapours of first evaporator (T-3), the heat source of third evaporator (T-5) is the overhead vapours of second stage vaporizer (T-4), the steam (generally only for containing micro-content organism and water vapour) at first evaporator (T-3) and second stage vaporizer (T-4) vaporizer top is respectively in order to heat lower 1st effective evaporator, after being then condensed into liquid, enter storage tank (V-2), three grades of vaporizer (T-3, T-4 and T-5) in working pressure progressively reduce, storage tank (V-2) is connected with vacuum system, and (T-5) steam at top because temperature is lower, can only be as the use of the first step preheating of waste water raw material,
After triple effect evaporation (if desired more multiple-effect), it at the bottom of the tower of third evaporator (T-5), is the salt concentrated liquid that does not contain lower boiling organic impurity, it is conveyed to crystallisation by cooling and obtains inorganic salt product, mother liquor after crystallization can be sent back to circulation in storage tank one (V-1) again, in storage tank two (V-2), be only the phlegma containing micro-content organism and water vapor, this phlegma can be fed to the processing up to standard of the further degree of depth of biochemical treatment system.
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|---|---|---|---|---|
| CN104909523B (en) * | 2015-07-01 | 2017-05-10 | 百川化工(如皋)有限公司 | Treatment system and treatment method for sewage containing high-concentration formaldehyde |
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| CN112174239A (en) * | 2019-07-01 | 2021-01-05 | 湖南万容科技股份有限公司 | Waste water evaporation treatment process |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB970855A (en) * | 1959-12-03 | 1964-09-23 | Burnett & Rolfe Ltd | Improvements relating to the recovery of formaldehyde |
| CN101306902A (en) * | 2008-07-08 | 2008-11-19 | 南京大学 | Harnessing and resource recovering process of low concentration industrial oxymethylene waste water |
| CN101597117A (en) * | 2009-06-23 | 2009-12-09 | 南京大学 | A kind of improvement of industrial oxymethylene waste water and recycling recovery process |
| CN101811965A (en) * | 2010-05-07 | 2010-08-25 | 南京大学 | Process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification |
| CN102126917A (en) * | 2010-12-15 | 2011-07-20 | 南京大学 | High purity recycling and energy integration technology for different concentrations of dichloromethane wastewater |
-
2012
- 2012-07-10 CN CN201210236065.7A patent/CN103539299B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB970855A (en) * | 1959-12-03 | 1964-09-23 | Burnett & Rolfe Ltd | Improvements relating to the recovery of formaldehyde |
| CN101306902A (en) * | 2008-07-08 | 2008-11-19 | 南京大学 | Harnessing and resource recovering process of low concentration industrial oxymethylene waste water |
| CN101597117A (en) * | 2009-06-23 | 2009-12-09 | 南京大学 | A kind of improvement of industrial oxymethylene waste water and recycling recovery process |
| CN101811965A (en) * | 2010-05-07 | 2010-08-25 | 南京大学 | Process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification |
| CN102126917A (en) * | 2010-12-15 | 2011-07-20 | 南京大学 | High purity recycling and energy integration technology for different concentrations of dichloromethane wastewater |
Non-Patent Citations (2)
| Title |
|---|
| 李文建等.综合利用精馏***余热蒸发处理"三高"废水工艺技术.《化工技术与开发》.2011,第40卷(第12期), * |
| 综合利用精馏***余热蒸发处理"三高"废水工艺技术;李文建等;《化工技术与开发》;20111231;第40卷(第12期);第45-49页 * |
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