CN104477853A - Pre-reforming and pre-absorption technology for production expansion of acid preparation from lead smelting gas - Google Patents
Pre-reforming and pre-absorption technology for production expansion of acid preparation from lead smelting gas Download PDFInfo
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- CN104477853A CN104477853A CN201410818971.7A CN201410818971A CN104477853A CN 104477853 A CN104477853 A CN 104477853A CN 201410818971 A CN201410818971 A CN 201410818971A CN 104477853 A CN104477853 A CN 104477853A
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- Prior art keywords
- gas
- inversion
- preabsorption
- pipe
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
Abstract
A pre-reforming and pre-absorption technology for production expansion of acid preparation from lead smelting gas comprises steps as follows: step one, a main air blower and a pre-reforming fan are started, part of gas A flows to a tenth pipe, and the other part of the gas A enters a pre-reforming heat exchanger; step two, the gas A is discharged from the pre-reforming heat exchanger and enters a heating electric furnace; step three, the gas A is discharged from the heating electric furnace and enters a pre-reformer to be converted into gas B; step four, the gas B enters the pre-reforming heat exchanger for heat exchange; step five, the gas B enters a pre-reforming S03 cooler, and an SO3 cooling fan is started to cool the gas B; step six, the gas B enters a pre-absorption tower to be converted into gas C; step seven, the gas C enters an eleventh pipe and is mixed with the gas A flowing from the tenth pipe to form gas D; step eighth, sulfuric acid is discharged from the pre-absorption tower and enters a pre-absorption circulating tank, part of the sulfuric acid is discharged from a branch pipe, and the other part enters the pre-absorption tower through another branch pipe. The pre-reforming and pre-absorption technology has the advantages as follows: with the application of the technology, flue gas with the SO2 concentration of 12.35% can be treated, the production expansion requirement of conventional equipment is met, and yearly increased yield of sulfuric acid is 30,000 tons.
Description
Technical field
The present invention relates to smelting lead pre-inversion preabsorption technique.
Background technology
Plumbous to smelt containing higher concentration in the flue gas produced
, direct discharge can cause severe contamination to environment, and common way these flue gases is sent into acid-producing apparatus extract sulfuric acid.Existing a set of acid-producing apparatus, can only process bottom convertor discharge quantity 35t/h and produce the flue gas produced, and along with bottom convertor production capacity expands, discharge quantity increases to 45t/h, and existing relieving haperacidity Zhu is standby cannot be processed with technique.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, and provide a kind of smelting lead relieving haperacidity to expand production pre-inversion preabsorption technique, the basis of existing acid-producing apparatus increases a set of pre-inversion preabsorption equipment and corresponding pre-inversion preabsorption technique, when spending few, solving production capacity and expanding and the standby problem that cannot process with technique of existing relieving haperacidity Zhu.
Technical scheme of the present invention is.
Smelting lead relieving haperacidity is expanded production pre-inversion preabsorption technique, and this technique comprises the steps:
Step one, starts main air blower and pre-inversion blower fan, and gas A is by shunting after main air blower, and a part 48% ~ 53% flows to pipe ten; Remaining gas A flows to pipe one, then by pre-inversion blower fan and pipe two, enter pre-inversion interchanger, have heat exchanging pipe in pre-inversion interchanger, gas A walks outside tubulation, carries out heat exchange, and temperature is upgraded to 370 ~ 400 DEG C.
In this step, in gas A
concentration be 10% ~ 14%,
concentration be 0% ~ 0.2%;
Step 2, gas A discharges from pre-inversion interchanger, enters temp .-elevating electric furnace, be heated to 400 ~ 420 DEG C, then close temp .-elevating electric furnace by pipe three.
Step 3, gas A discharges from temp .-elevating electric furnace, enters pre-converter by Guan Si, a part in gas A
be converted into
, be converted into gas B.
In gas B
concentration be 3.5% ~ 4.5%,
concentration be 8.5% ~ 9.5%.
Step 4, gas B discharges from pre-converter, and enter in pre-inversion heat exchanger tube by pipe five, carry out heat exchange, temperature reduces to 240 ~ 280 DEG C.
Step 5, gas B discharges from pre-inversion interchanger, enters pre-inversion by pipe six
in tubulation in water cooler, start simultaneously
cooling blower, cooling air enters pre-inversion by pipe seven
water cooler, cooling air is walked outside tubulation, lowers the temperature to gas B, makes its temperature reduce to 180 DEG C.
Step 6, gas B is from pre-inversion
water cooler is discharged, and enters preabsorption tower by pipe eight, and the effect of preabsorption tower absorbs in flue gas
, in preabsorption tower, acid sprays from top to bottom, and flue gas is walked from the bottom up, and acid is carried by the preabsorption recycle pump on preabsorption circulation groove to come, by absorbing in gas B in preabsorption tower
, gas B is converted into gas C.
In this step, in gas C
concentration be 4.0% ~ 4.6%,
concentration be 0% ~ 0.2%;
Step 7, the gas C in preabsorption tower discharges, and enters Guan Shiyi by pipe nine, flows through gas A and mixes, become gas D with pipe ten.
In this step, in gas D
concentration be 8.5% ~ 9.1%,
concentration be 0% ~ 0.2%;
Step 8, sulfuric acid is discharged from preabsorption tower, enters preabsorption circulation groove by pipeline, more successively through preabsorption recycle pump and preabsorption water cooler, a part 1% ~ 10% sulfuric acid is discharged by arm, and remaining sulfuric acid enters preabsorption tower by another root arm.
In step one, the sulfuric acid stream of 49% or 51% is to pipe 10; Remaining gas A flows to pipe 1, then by pre-inversion blower fan 13 and pipe 22, enter pre-inversion interchanger 14, have heat exchanging pipe in pre-inversion interchanger, gas A walks outside tubulation, carries out heat exchange, and temperature is upgraded to 380 or 390 DEG C, in gas A
concentration be 11% or 13%,
concentration be 0.05% or 0.1%.
In step 2, gas A enters temp .-elevating electric furnace 16, is heated to 405 or 415 DEG C.
In step 3, in gas B
concentration be 3.8% or 4.2%,
concentration be 8.9% or 9.3%.
In step 4, gas B enters in pre-inversion interchanger 14 tubulation, carries out heat exchange, and temperature reduces to 245 or 255 DEG C.
In step 6, in gas C
concentration be 4.1% or 4.5%,
concentration be 0.05% or 0.15%.
In step 7, in gas D
concentration be 8.8% or 9.05%,
concentration be 0.05% or 0.15%.
In step 8, the sulfuric acid of 5% or 8% is discharged by arm, and remaining sulfuric acid enters preabsorption tower 19 by another root arm.
Tool of the present invention has the following advantages: existing acid making system can only process the bottom convertor flue gas during smelting that so2 concentration is 9.1%, can not meet bottom convertor and to expand production requirement.By increase technique of the present invention on original acid making system basis after, can process
concentration is the bottom convertor flue gas during smelting of 12.35%, and can meet bottom convertor completely and produce requirement of expanding production, year increases sulphuric acid output about 30,000 tons.
Specifically, part of smoke is shunted and passes into newly-increased pre-inversion preabsorption acid-producing apparatus, by obtain after art breading of the present invention sulfuric acid and
the flue gas that content is lower, this part
the flue gas that content is lower with concentration be again 12.35% bottom convertor flue gas during smelting converge, thus to reduce in flue gas
content, to reach the requirement that existing acid-producing apparatus and technique can process completely.Newly-increased pre-inversion preabsorption acid-producing apparatus and technique, spend few, both expanded production capacity, and make use of existing installation again.
Below in conjunction with figure and embodiment, the present invention is further described.
Accompanying drawing explanation
Fig. 1 is each device annexation schematic diagram that technical process of the present invention and technique relate to.
Embodiment
Smelting lead relieving haperacidity is expanded production pre-inversion preabsorption technique, and this technique comprises the steps:
Step one, starts main air blower 12 and pre-inversion blower fan 13, and gas A is by shunting after main air blower 12, and a part 48% ~ 53% flows to pipe 10; Remaining gas A flows to pipe 1, then by pre-inversion blower fan 13 and pipe 22, enter pre-inversion interchanger 14, have heat exchanging pipe in pre-inversion interchanger, gas A walks outside tubulation, carries out heat exchange, and temperature is upgraded to 370 ~ 400 DEG C.
In this step, in gas A
concentration be 10% ~ 14%,
concentration be 0% ~ 0.2%;
Step 2, gas A discharges from pre-inversion interchanger 14, enters temp .-elevating electric furnace 16 by pipe 33, is heated to 400 ~ 420 DEG C, then closes temp .-elevating electric furnace.
Step 3, gas A discharges from temp .-elevating electric furnace 16, enters pre-converter 15 by pipe 44, a part in gas A
be converted into
, be converted into gas B.
In gas B
concentration be 3.5% ~ 4.5%,
concentration be 8.5% ~ 9.5%.
Step 4, gas B discharges from pre-converter 15, and entered in pre-inversion interchanger 14 tubulation by pipe 55, carry out heat exchange, temperature reduces to 240 ~ 280 DEG C.
Step 5, gas B discharges from pre-inversion interchanger 14, enters pre-inversion by pipe 66
in tubulation in water cooler 17, start simultaneously
cooling blower 18, cooling air enters pre-inversion by pipe 77
water cooler 17, cooling air is walked outside tubulation, lowers the temperature to gas B, makes its temperature reduce to 180 DEG C.
Step 6, gas B is from pre-inversion
water cooler 17 is discharged, and enters preabsorption tower 19 by pipe 88, and the effect of preabsorption tower 19 absorbs in flue gas
, in preabsorption tower, acid sprays from top to bottom, and flue gas is walked from the bottom up, and acid is carried by the preabsorption recycle pump 21 on preabsorption circulation groove 20 to come, by absorbing in gas B in preabsorption tower
, gas B is converted into gas C.
In this step, in gas C
concentration be 4.0% ~ 4.6%,
concentration be 0% ~ 0.2%;
Step 7, the gas C in preabsorption tower 19 discharges, and enters Guan Shiyi 11 by pipe 99, flows through gas A and mixes, become gas D with pipe 10.
In this step, in gas D
concentration be 8.5% ~ 9.1%,
concentration be 0% ~ 0.2%;
Step 8, sulfuric acid is discharged from preabsorption tower 19, enters preabsorption circulation groove 20 by pipeline, more successively through preabsorption recycle pump 21 and preabsorption water cooler 22, a part 1% ~ 10% sulfuric acid is discharged by arm, and remaining sulfuric acid enters preabsorption tower 19 by another root arm.
In step one, the sulfuric acid stream of 49% or 51% is to pipe 10; Remaining gas A flows to pipe 1, then by pre-inversion blower fan 13 and pipe 22, enter pre-inversion interchanger 14, have heat exchanging pipe in pre-inversion interchanger, gas A walks outside tubulation, carries out heat exchange, and temperature is upgraded to 380 or 390 DEG C, in gas A
concentration be 11% or 13%,
concentration be 0.05% or 0.1%.
In step 2, gas A enters temp .-elevating electric furnace 16, is heated to 405 or 415 DEG C.
In step 3, in gas B
concentration be 3.8% or 4.2%,
concentration be 8.9% or 9.3%.
In step 4, gas B enters in pre-inversion interchanger 14 tubulation, carries out heat exchange, and temperature reduces to 245 or 255 DEG C.
In step 6, in gas C
concentration be 4.1% or 4.5%,
concentration be 0.05% or 0.15%.
In step 7, in gas D
concentration be 8.8% or 9.05%,
concentration be 0.05% or 0.15%.
In step 8, the sulfuric acid of 5% or 8% is discharged by arm, and remaining sulfuric acid enters preabsorption tower 19 by another root arm.
As shown in Figure 1: smelting lead relieving haperacidity of the present invention is expanded production pre-inversion preabsorption technique, and the device related to comprises pipe 1, pipe 22, pipe 33, pipe 44, pipe 55, pipe 66, pipe 77, pipe 88, pipe 99, pipe 10, Guan Shiyi 11, main air blower 12, pre-inversion blower fan 13, pre-inversion interchanger 14, pre-converter 15, temp .-elevating electric furnace 16, pre-inversion
water cooler 17,
cooling blower 18, preabsorption tower 19, preabsorption circulation groove 20, preabsorption recycle pump 21 and preabsorption acid cooler 22.
The annexation of each pipeline and each device is as follows, main air blower 12 is connected with a point stream interface 101, pipe 1 one end is connected with the blast inlet of pre-inversion blower fan 13, the other end is connected on point stream interface 101, pipe 22 one end is connected with the air outlet of pre-inversion blower fan 13, the other end is connected with the inlet mouth 141 of pre-inversion interchanger 14, pipe 33 one end is connected with the venting port 142 of pre-inversion interchanger 14, the other end is connected with the inlet end of temp .-elevating electric furnace 16, pipe 44 one end is connected with the outlet side of temp .-elevating electric furnace 16, the other end is connected with the inlet mouth of pre-converter 15, pipe 55 one end is connected with the venting port of pre-converter 15, the other end is connected with the second inlet mouth 143 of pre-inversion interchanger 14, pipe 66 one end is connected with the second exhaust port 144 of pre-inversion interchanger 14, the other end and pre-inversion
the inlet mouth 171 of water cooler 17 connects, pipe 77 one end with
the air outlet of cooling blower 18 is communicated with, the other end and pre-inversion
the blast inlet 172 of water cooler 17 connects, pipe 88 one end and pre-inversion
the venting port 173 of water cooler 17 is communicated with, the other end is communicated with the inlet mouth 191 bottom preabsorption tower 19, pipe 99 one end is communicated with the venting port 192 of preabsorption tower 19 upper end, the other end is communicated with the interface 102 that confluxes, preabsorption recycle pump 21 is communicated with preabsorption circulation groove 20, and preabsorption acid cooler 22 is communicated with preabsorption recycle pump 21.Guan Shiyi 11 is communicated with the interface 102 that confluxes, and mixed gas D flows into existing acid-producing apparatus by Guan Shiyi 11.
Claims (8)
1. smelting lead relieving haperacidity is expanded production a pre-inversion preabsorption technique, and it is characterized in that, this technique comprises the steps:
Step one, starts main air blower (12) and pre-inversion blower fan (13), and gas A is shunted afterwards by main air blower (12), and a part (48% ~ 53%) flows to pipe ten (10); Remaining gas A
flow topipe one (1),
pass through againpre-inversion blower fan (13) and pipe two (2), enter pre-inversion interchanger (14), have heat exchanging pipe in pre-inversion interchanger, gas A walks outside tubulation, carries out heat exchange, and temperature is upgraded to 370 ~ 400 DEG C,
In this step, in gas A
concentration be 10% ~ 14%,
concentration be 0% ~ 0.2%;
Step 2, gas A discharges from pre-inversion interchanger (14), enters temp .-elevating electric furnace (16), be heated to 400 ~ 420 DEG C, then close temp .-elevating electric furnace by pipe three (3);
Step 3, gas A discharges from temp .-elevating electric furnace (16), enters pre-converter (15) by Guan Si (4), a part in gas A
be converted into
, be converted into gas B,
In gas B
concentration be 3.5% ~ 4.5%,
concentration be 8.5% ~ 9.5%;
Step 4, gas B discharges from pre-converter (15), and entered in pre-inversion interchanger (14) tubulation by pipe five (5), carry out heat exchange, temperature reduces to 240 ~ 280 DEG C;
Step 5, gas B discharges from pre-inversion interchanger (14), enters pre-inversion by pipe six (6)
in tubulation in water cooler (17), start simultaneously
cooling blower (18), cooling air enters pre-inversion by pipe seven (7)
water cooler (17), cooling air is walked outside tubulation, lowers the temperature to gas B, makes its temperature reduce to 180 DEG C;
Step 6, gas B is from pre-inversion
water cooler (17) is discharged, and enters preabsorption tower (19) by pipe eight (8), and the effect of preabsorption tower (19) absorbs in flue gas
, in preabsorption tower, acid sprays from top to bottom, and flue gas is walked from the bottom up, and acid is carried by the preabsorption recycle pump (21) on preabsorption circulation groove (20) to come, by absorbing in gas B in preabsorption tower
, gas B is converted into gas C,
In this step, in gas C
concentration be 4.0% ~ 4.6%,
concentration be 0% ~ 0.2%;
Step 7, the gas C in preabsorption tower (19) discharges, and enters Guan Shiyi (11) by pipe nine (9), flows through gas A and mixes, become gas D with pipe ten (10),
In this step, in gas D
concentration be 8.5% ~ 9.1%,
concentration be 0% ~ 0.2%;
Step 8, sulfuric acid is discharged from preabsorption tower (19), preabsorption circulation groove (20) is entered by pipeline, again successively through preabsorption recycle pump (21) and preabsorption water cooler (22), a part (1% ~ 10%) sulfuric acid is discharged by arm, and remaining sulfuric acid enters preabsorption tower (19) by another root arm.
2. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, and it is characterized in that: in step one, the sulfuric acid stream of 49% or 51% is to pipe ten (10); Remaining gas A
flow topipe one (1),
pass through againpre-inversion blower fan (13) and pipe two (2), enter pre-inversion interchanger (14), have heat exchanging pipe in pre-inversion interchanger, gas A walks outside tubulation, carries out heat exchange, and temperature is upgraded to 380 or 390 DEG C, in gas A
concentration be 11% or 13%,
concentration be 0.05% or 0.1%.
3. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, and it is characterized in that: in step 2, gas A enters temp .-elevating electric furnace (16), is heated to 405 or 415 DEG C.
4. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, it is characterized in that: in step 3, in gas B
concentration be 3.8% or 4.2%,
concentration be 8.9% or 9.3%.
5. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, and it is characterized in that: in step 4, gas B enters in pre-inversion interchanger (14) tubulation, carries out heat exchange, and temperature reduces to 245 or 255 DEG C.
6. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, it is characterized in that: in step 6, in gas C
concentration be 4.1% or 4.5%,
concentration be 0.05% or 0.15%.
7. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, it is characterized in that: in step 7, in gas D
concentration be 8.8% or 9.05%,
concentration be 0.05% or 0.15%.
8. smelting lead relieving haperacidity as claimed in claim 1 is expanded production pre-inversion preabsorption technique, and it is characterized in that: in step 8, the sulfuric acid of 5% or 8% is discharged by arm, and remaining sulfuric acid enters preabsorption tower (19) by another root arm.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410818971.7A CN104477853A (en) | 2014-12-25 | 2014-12-25 | Pre-reforming and pre-absorption technology for production expansion of acid preparation from lead smelting gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410818971.7A CN104477853A (en) | 2014-12-25 | 2014-12-25 | Pre-reforming and pre-absorption technology for production expansion of acid preparation from lead smelting gas |
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| CN104477853A true CN104477853A (en) | 2015-04-01 |
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|---|---|---|---|
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106672919A (en) * | 2017-01-18 | 2017-05-17 | 长沙有色冶金设计研究院有限公司 | Acid making process and device adopting SO2 pre-reforming |
| CN109095441A (en) * | 2017-06-20 | 2018-12-28 | 中国瑞林工程技术有限公司 | The method for preparing sulfuric acid |
| CN109592650A (en) * | 2017-09-30 | 2019-04-09 | 易门铜业有限公司 | A kind of high-concentration fume acid preparation method using pre-inversion pre-absorption |
| CN109761203A (en) * | 2019-03-04 | 2019-05-17 | 长沙有色冶金设计研究院有限公司 | A kind of high concentration SO2Convert acid-making process |
| CN113636527A (en) * | 2021-08-12 | 2021-11-12 | 楚雄滇中有色金属有限责任公司 | Method for turning on secondary absorption concentrated acid pump without stopping production |
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| CN102079511A (en) * | 2011-01-05 | 2011-06-01 | 金隆铜业有限公司 | Acid making system suitable for high-concentration sulfur dioxide-containing flue gas |
| CN102448875A (en) * | 2010-05-27 | 2012-05-09 | 赫多特普索化工设备公司 | Process and apparatus for sulphuric acid production |
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| US3855386A (en) * | 1971-11-23 | 1974-12-17 | Battelle Memorial Institute | Catalytic fused salt extraction process for removal of sulfur oxides from flue or other gases |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106672919A (en) * | 2017-01-18 | 2017-05-17 | 长沙有色冶金设计研究院有限公司 | Acid making process and device adopting SO2 pre-reforming |
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| CN109592650A (en) * | 2017-09-30 | 2019-04-09 | 易门铜业有限公司 | A kind of high-concentration fume acid preparation method using pre-inversion pre-absorption |
| CN109761203A (en) * | 2019-03-04 | 2019-05-17 | 长沙有色冶金设计研究院有限公司 | A kind of high concentration SO2Convert acid-making process |
| CN109761203B (en) * | 2019-03-04 | 2021-07-02 | 长沙有色冶金设计研究院有限公司 | High-concentration SO2Conversion acid-making process |
| CN113636527A (en) * | 2021-08-12 | 2021-11-12 | 楚雄滇中有色金属有限责任公司 | Method for turning on secondary absorption concentrated acid pump without stopping production |
| CN113636527B (en) * | 2021-08-12 | 2023-11-24 | 楚雄滇中有色金属有限责任公司 | Method for switching on and switching on secondary absorption concentrated acid pump without stopping production |
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