CN103030117B - Recovering technology for waste acid - Google Patents
Recovering technology for waste acid Download PDFInfo
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- CN103030117B CN103030117B CN201210596495.XA CN201210596495A CN103030117B CN 103030117 B CN103030117 B CN 103030117B CN 201210596495 A CN201210596495 A CN 201210596495A CN 103030117 B CN103030117 B CN 103030117B
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- gas
- separator
- acid
- spent acid
- venturi tube
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- 239000002253 acid Substances 0.000 title claims abstract description 77
- 239000002699 waste material Substances 0.000 title claims abstract description 11
- 238000005516 engineering process Methods 0.000 title abstract description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000002485 combustion reaction Methods 0.000 claims abstract description 18
- 238000011084 recovery Methods 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 36
- 238000000034 method Methods 0.000 claims description 30
- 238000005406 washing Methods 0.000 claims description 23
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 230000008016 vaporization Effects 0.000 claims description 15
- 239000000567 combustion gas Substances 0.000 claims description 12
- 238000009834 vaporization Methods 0.000 claims description 12
- 238000000605 extraction Methods 0.000 claims description 11
- 239000007921 spray Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 7
- 239000003546 flue gas Substances 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000003595 mist Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 239000011324 bead Substances 0.000 claims description 3
- 230000007613 environmental effect Effects 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 229910000831 Steel Inorganic materials 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 239000010959 steel Substances 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000002309 gasification Methods 0.000 abstract description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 6
- 235000010215 titanium dioxide Nutrition 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention aims at providing a recovering technology for waste acid, which is short in flow, high in adaptability, little in power equipment, easy to control and energy-saving. The technology is characterized in that the whole technology consists of a combustion and gasification separation system, a product acid generation and separation system and a waste acid preheating system. The technology has the benefits: (1) the whole technological flow is short, the power equipment is little, and investment and the operation costs can be saved, (2) technological parameters are easy to adjust, requirements of a wider waste acid treating concentration range and a wider product concentration range are met, the technology is suitable for recovering waste sulfuric acid with middle/low concentration (10-90%), the concentration of a recovery product can be adjusted, and the appropriate concentration is 70-90%, and (3) the recovering technology is low in energy consumption, and has considerable economic benefits.
Description
Technical field
The invention belongs to spent acid solution process field.The present invention relates to a kind of spent acid recovery process.
Background technology
Sulfuric acid is industrial mother liquor, a lot of industries are used sulfuric acid, chemical engineering industry particularly, produce a large amount of spent acid, as gas mixture in calcium carbide process PVC production is dry, with acid and acetylene cleaning, use sour, produce the black Waste Sulfuric Acid of high density (concentration is 70%～95%), and for example in Producing Titanium Dioxide, produce the spent acid of a large amount of 20% left and right.These spent acid are difficult to recycle, and to ecological, environmental protective, cause very large pressure.
Patents about spent acid has:
CN102730650A discloses a kind of titanium white waste acid recovery process, further says that take fire coal or combustion gas is the energy, takes temperature control gasification absorption technique reclaim(ed) sulfuric acid; Whole technique is comprised of the operation of burning, vaporization cleaning section, absorption operation, waste heat recovery operation and vent gas treatment operation.The invention has the beneficial effects as follows: recovered acid is purer, concentration is adjustable, and economic concentration is 80～90%, can meet the object of Producing Titanium Dioxide reuse completely; In spent acid, vitriol is separated with solid formation, can further fully utilize; Recovery energy consumption is low, has considerable economic benefit.
This patent has solved the recovery problem of titanium white waste acid well, but this technique still exists complex process, and power-equipment is many, and processing parameter is adjusted long problem time of lag.
Summary of the invention
The object of the present invention is to provide that a kind of flow process is short, strong adaptability, power-equipment are few, be easy to control and the spent acid recovery process of save energy.
A spent acid recovery process, is comprised of vaporization separation circuit, absorption extraction operation and spent acid preheating procedure, comprising:
(1) vaporization separation circuit, is comprised of combustion unit 1, temperature control gas tank 2, the first Venturi tube 3 and cyclonic separator 4; Take combustion gas as the energy, combustion gas supercharging enters combustion unit 1, air enters combustion unit 1 and temperature control gas tank 2 after gas blower pressurization, enter the first Venturi tube 3, in the first Venturi tube 3 throats, suck the spent acid through preheating, rapidly after vaporization, enter cyclonic separator 4, in spent acid impurity separated in cyclonic separator 4 under, separated after flue gas send absorption extraction operation;
(2) absorption extraction operation, is comprised of the second Venturi tube 5, separator 6, and wherein separator 6 forms connected device by cylindrical shell and tower body; Vaporization separation circuit comes gas mixture to pass through the second Venturi tube 5, in the second Venturi tube 5 throats, spray into through cooling finished acid, mixed flue gas reduces heat is realized gas-liquid separation in separator 6, liquid phase is in separator 6 bottoms through coil heat exchanger heat exchange, and temperature maintains 150～180 ℃; Tower body is padding washing tower structure, and cycles of washing liquid is supplied with by the sour pump 11 of the first sour pump 10, second, and stuffing washing tower upper strata is water washing layer, uses, or require standby according to tail gas when going into operation; The direct discharge up to standard of stuffing washing tower outlet tail gas;
(3) spent acid preheating procedure, is comprised of spent acid interchanger 7, product storage tank 8, spent acid groove 9 and the first sour pump 11 of sour pump 10, second and the 3rd sour pump 12, by separator 6, comes sulfuric acid to send spent acid interchanger 7 heat exchange, and temperature drops to below 40 ℃, send product storage tank 8; Meanwhile, by spent acid groove 9, through the spent acid of the 3rd sour pump 12 pressurizations, through spent acid interchanger 7, separator 6 bottoms, through coil heat exchanger heat exchange, send the first Venturi tube 3 respectively.
The present invention be embodied in following some:
(1) whole technique is comprised of the separation circuit of vaporizing, absorption extraction operation and spent acid preheating procedure, and the separation circuit of wherein vaporizing is comprised of combustion unit 1, temperature control gas tank 2, the first Venturi tube 3 and cyclonic separator 4; Absorption extraction operation is comprised of the second Venturi tube 5, separator 6; Spent acid preheating procedure, is comprised of spent acid interchanger 7, product storage tank 8, spent acid groove 9 and the first sour pump 11 of sour pump 10, second and the 3rd sour pump 12; Flow process is short, and strong adaptability, power-equipment be few, be easy to control, thereby can reduce investment outlay and process cost.
(2) processing parameter is more easily adjusted, temperature control absorbs to reach and regulates the object that reclaims product concentration, regulative mode can be by regulating the spray acid amount of the second Venturi tube 5 and separator 6 spray acids or recycle acid amount to control, it is convenient to regulate, a set of equipment adapts to wider processing acid-spending strength and wider product concentration demand, be applicable to the recovery of middle lower concentration (10～49%) Waste Sulfuric Acid, reclaim product concentration adjustable, reclaiming product suitable concentration is 70～90%; With the second Venturi tube 5 spray acid cooling condensations, replace spray cooling, can reduce separator to the load of acid mist separation and reduce the thermosteresis that gas is taken steam out of.
(3) separator 6 adopts cylindrical shell and tower body to form connected device, equipment and materials adopts general Steel Lining tetrafluoro, in cylindrical shell, arrange and on horizontal baffle, horizontal baffle, tetrafluoro material bead is set and becomes rapid ball layer, under horizontal baffle, coil heat exchanger is set, tower body is padding washing tower structure, stuffing washing tower is divided into two-layer (sour absorption layer and water washing layer), tower top installs mesh mist eliminator additional, the direct discharge up to standard of stuffing washing tower outlet tail gas, or add vent gas treatment to reach stricter environmental protection standard; With disjunctor tower, replace series connection absorbing separator, can reduce the demand of power-driven pump.
(4) take combustion gas as the energy, combustion gas supercharging enters combustion unit 1, air enters combustion unit and temperature control gas tank after gas blower 13 pressurizations, combustion unit is take in supercharging pressurization, and the pressure drop of follow-up flow process pipe-line equipment is provided is index, in flow process, do not establish booster fan or induced draft fan, to reduce the power consumption of whole system; Air not preheating enters system, and shortened process, reduces investment to greatest extent; Venturi tube adopts venturi scrubber with internal injection structure, liner silica glass, inlet gas flow velocity: 18m/s, trunnion central gas speed: 60m/s; Cyclonic separator adopts Type B or E type cyclone separator arrangement, and material adopts general steel, or adds wear-resistant liner.
Accompanying drawing explanation
Accompanying drawing is process flow diagram of the present invention
In figure, combustion unit 1, temperature control gas tank 2, the first Venturi tubes 3, cyclonic separator 4, the second Venturi tubes 5, separator 6, spent acid interchanger 7, product storage tank 8, sour pump the 11, the 3rd sour pump 12 of the sour pump 10, second of spent acid groove 9, the first, blower fan 13; Air A, combustion gas B, discharge flue gas C, process water D, product acid E, spent acid F, acid sludge G.
Below in conjunction with accompanying drawing, production technique of the present invention is described further.
Embodiment
With reference to accompanying drawing, whole technique is comprised of the separation circuit of vaporizing, absorption extraction operation, spent acid preheating procedure.
(1) vaporization separation circuit, is comprised of combustion unit 1, temperature control gas tank 2, the first Venturi tube 3 and cyclonic separator 4.Take combustion gas as the energy, be pressurized to >=5KPa of combustion gas B enters combustion unit 1, air A enters combustion unit and temperature control gas tank 2 after gas blower 13 pressurizations (>=5KPa), enter the first Venturi tube 3, in the first Venturi tube 3 throats, suck the spent acid through preheating, enter cyclonic separator 4 rapidly after vaporization, cyclonic separator 4 service temperatures are controlled at approximately 380 ℃, under impurity in spent acid (acid sludge G) is separated in cyclonic separator 4, separated rear flue gas send absorption extraction operation.
(2) absorption extraction operation, is comprised of the second Venturi tube 5, separator 6, and wherein separator 6 forms connected device by cylindrical shell and tower body.Vaporization separation circuit comes gas mixture to pass through the second Venturi tube 5, in the second Venturi tube 5 throats, spray into through cooling finished acid E, mixed flue gas C reduces heat to 180～200 ℃, in separator 6, realize gas-liquid separation, liquid phase is in separator 6 bottoms through coil heat exchanger heat exchange, and temperature maintains approximately 150～180 ℃; Tower body is padding washing tower structure, and cycles of washing liquid is supplied with by the sour pump 11 of the first sour pump 10, second, and stuffing washing tower upper strata is water D scrubber layer, when going into operation, uses, and also can require according to tail gas standby; Up to standard can directly discharge of stuffing washing tower outlet tail gas C.
(3) spent acid preheating procedure, is comprised of spent acid interchanger 7, product storage tank 8, spent acid groove 9 and sour pump 10, sour pump 11 and sour pump 12, and wherein spent acid interchanger 7 sets up tetrafluoro heat exchanger separately and graphite heat exchanger is composed in series.By separator 6, carry out approximately 150 ℃ of sulfuric acid temperature, send spent acid interchanger 7 heat exchange, temperature drops to below 40 ℃, send product storage tank 8; Meanwhile, by spent acid groove 9 through the spent acid F of sour pump 12 pressurizations respectively through spent acid interchanger 7, separator 6 bottoms through coil heat exchanger heat exchange, temperature rises to approximately 180 ℃ and send the first Venturi tube 3.
The invention has the beneficial effects as follows: (1) whole technical process is short, and power-equipment is few, can reduce investment outlay and process cost; (2) processing parameter is more easily adjusted, and adapts to wider processing acid-spending strength and wider product concentration demand, is applicable to the recovery of middle lower concentration (10～49%) Waste Sulfuric Acid, reclaims product concentration adjustable, and product suitable concentration is 70～90%; (3) recovery energy consumption is low, has considerable economic benefit.
Claims (4)
1. a spent acid recovery process, is comprised of vaporization separation circuit, absorption extraction operation and spent acid preheating procedure, comprising:
A, vaporization separation circuit
By combustion unit (1), temperature control gas tank (2), the first Venturi tube (3) and cyclonic separator (4), formed; Take combustion gas as the energy, combustion gas supercharging enters combustion unit (1), air enters combustion unit (1) and temperature control gas tank (2) after gas blower pressurization, enter the first Venturi tube (3), in the first Venturi tube (3) throat, suck the spent acid through preheating, after vaporization, enter cyclonic separator (4) rapidly, in spent acid, impurity is separated in cyclonic separator (4) gets off, and separated rear flue gas send absorption extraction operation;
B, absorption extraction operation
By the second Venturi tube (5), separator (6), formed, wherein separator (6) forms connected device by cylindrical shell and tower body, equipment and materials adopts general Steel Lining tetrafluoro, in cylindrical shell, arrange and on horizontal baffle, horizontal baffle, tetrafluoro material bead is set and becomes rapid ball layer, under horizontal baffle, coil heat exchanger is set, tower body is padding washing tower structure; Vaporization separation circuit comes gas mixture to pass through the second Venturi tube (5), in the second Venturi tube (5), throat sprays into through cooling finished acid, mixed flue gas reduces heat, in separator (6), realize gas-liquid separation, liquid phase is in separator (6) bottom through coil heat exchanger heat exchange, and temperature maintains 150～180 ℃; Tower body is padding washing tower structure, and cycles of washing liquid is supplied with by the first sour pump (10), the second sour pump (11), and stuffing washing tower upper strata is water washing layer, uses, or require standby according to tail gas when going into operation; The direct discharge up to standard of stuffing washing tower outlet tail gas;
C, spent acid preheating procedure
By spent acid interchanger (7), product storage tank (8), spent acid groove (9) and the first sour pump (10), the second sour pump (11) and the 3rd sour pump (12), formed, by separator (6), come sulfuric acid to send spent acid interchanger (7) heat exchange, temperature drops to below 40 ℃, send product storage tank (8); Meanwhile, by spent acid groove (9), through the spent acid of the 3rd sour pump (12) pressurization, through spent acid interchanger (7), separator (6) bottom, through coil heat exchanger heat exchange, send the first Venturi tube (3) respectively.
2. spent acid recovery process according to claim 1, it is characterized in that: processing parameter is more easily adjusted, temperature control absorbs to reach and regulates the object that reclaims product concentration, regulative mode is by the spray acid amount or separator (6) spray acid or the control of recycle acid amount that regulate the second Venturi tube (5), it is convenient to regulate, a set of equipment adapts to wider processing acid-spending strength and wider product concentration demand, be applicable to the recovery of middle lower concentration Waste Sulfuric Acid, recovery product concentration is adjustable, and reclaiming product suitable concentration is 70～90%; With the second Venturi tube (5) spray acid cooling condensation, replace spray cooling, reduce separator to the load of acid mist separation and reduce the thermosteresis that gas is taken steam out of.
3. spent acid recovery process according to claim 1, it is characterized in that: separator (6) adopts cylindrical shell and tower body to form connected device, equipment and materials adopts general Steel Lining tetrafluoro, in cylindrical shell, arrange and on horizontal baffle, horizontal baffle, tetrafluoro material bead is set and becomes rapid ball layer, under horizontal baffle, coil heat exchanger is set, tower body is padding washing tower structure, stuffing washing tower is divided into sour absorption layer and water washing layer, tower top installs mesh mist eliminator additional, the direct discharge up to standard of stuffing washing tower outlet tail gas, or add vent gas treatment to reach stricter environmental protection standard; With disjunctor tower, replace series connection absorbing separator, reduce the demand of power-driven pump.
4. spent acid recovery process according to claim 1, it is characterized in that: take combustion gas as the energy, combustion gas supercharging enters combustion unit (1), air enters combustion unit (1) and temperature control gas tank (2) after gas blower (13) pressurization, supercharging is pressurised into combustion unit the pressure drop of follow-up flow process pipe-line equipment is provided, in flow process, do not establish booster fan or induced draft fan, to reduce the power consumption of whole system; Air not preheating enters system, and shortened process, reduces investment to greatest extent; Venturi tube adopts venturi scrubber with internal injection structure, liner silica glass, inlet gas flow velocity: 18m/s, trunnion central gas speed: 60m/s; Cyclonic separator adopts Type B or E type cyclone separator arrangement, and material adopts general steel, or adds wear-resistant liner.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210596495.XA CN103030117B (en) | 2012-12-28 | 2012-12-28 | Recovering technology for waste acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210596495.XA CN103030117B (en) | 2012-12-28 | 2012-12-28 | Recovering technology for waste acid |
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| Publication Number | Publication Date |
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| CN103030117A CN103030117A (en) | 2013-04-10 |
| CN103030117B true CN103030117B (en) | 2014-10-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201210596495.XA Active CN103030117B (en) | 2012-12-28 | 2012-12-28 | Recovering technology for waste acid |
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| Country | Link |
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| CN (1) | CN103030117B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104016311B (en) * | 2014-06-09 | 2016-03-02 | 淮南市明月环保科技有限责任公司 | A kind of dense spent acid produces sulfuric acid purification unstripped gas system |
| CN106829880B (en) * | 2016-12-08 | 2018-12-21 | 荆门市渝楚化工有限公司 | A kind of regeneration of sulfuric acid production line |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3713786A (en) * | 1971-12-06 | 1973-01-30 | New Jersey Zinc Co | Evaporative sulfuric acid recovery from sulfuric acids containing sulfates |
| CN102730650A (en) * | 2011-04-12 | 2012-10-17 | 安徽理工大学 | Recovery technology of titanium white waste acid |
| CN102745655A (en) * | 2011-04-22 | 2012-10-24 | 安徽理工大学 | Waste acid recovery technology for PVC factory |
| CN102826518A (en) * | 2011-06-15 | 2012-12-19 | 安徽理工大学 | Concentrated waste acid recovery technology |
-
2012
- 2012-12-28 CN CN201210596495.XA patent/CN103030117B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3713786A (en) * | 1971-12-06 | 1973-01-30 | New Jersey Zinc Co | Evaporative sulfuric acid recovery from sulfuric acids containing sulfates |
| CN102730650A (en) * | 2011-04-12 | 2012-10-17 | 安徽理工大学 | Recovery technology of titanium white waste acid |
| CN102745655A (en) * | 2011-04-22 | 2012-10-24 | 安徽理工大学 | Waste acid recovery technology for PVC factory |
| CN102826518A (en) * | 2011-06-15 | 2012-12-19 | 安徽理工大学 | Concentrated waste acid recovery technology |
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Inventor after: Ni Shujun Inventor before: Tao Jun Inventor before: Xu Jihong |
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Effective date of registration: 20171011 Address after: Baishuiyang town Huang Tanyang coastal village of Taizhou City, Zhejiang province 317032 City No. 155 Patentee after: Ni Shujun Address before: 232001 Anhui Province, Huainan city tianjia'an District Chaoyang Street Garden Village Bai Jiao yuan building 602 room 2 Patentee before: Huainan City's bright moon environmental protection science and technology limited Company |
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Effective date of registration: 20190603 Address after: 225400 No. 10 Xingang Road, Taixing Economic Development Zone, Taizhou City, Jiangsu Province Patentee after: Taixing Jinhui Chemical Industry Co., Ltd. Address before: 317032 155 Huang Tan Yang village, Baishui Yang, Taizhou, Zhejiang. Patentee before: Ni Shujun |