CN85109394A - Preparation vitriolic method and apparatus - Google Patents
Preparation vitriolic method and apparatus Download PDFInfo
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- CN85109394A CN85109394A CN85109394A CN85109394A CN85109394A CN 85109394 A CN85109394 A CN 85109394A CN 85109394 A CN85109394 A CN 85109394A CN 85109394 A CN85109394 A CN 85109394A CN 85109394 A CN85109394 A CN 85109394A
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- acid
- tower
- drying tower
- intermediate absorber
- basin
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Abstract
In biabsorption manufactured vitriolic system, employing be single acid circulation system and single stage coolers.Mix in a public basin by dry air tower and the final effusive acid in absorption tower, and enter discrete basin by the effusive acid of intermediate absorber.The acid shunting of public basin enters in intermediate absorber and final absorption tower and the product line.The effusive acid of discrete basin is shunted after cooling off and is entered drying tower and intermediate absorber.Recycle unit only need cool off the position of a comparatively high temps, and can simplify the control of acidity and liquid level.Half that have only the recycle acid amount needs cooling, and the temperature in the drying tower is subjected to the influence of seasonal variation to be reduced to bottom line.
Description
What the present invention narrated is to prepare sulfuric acid with the biabsorption method by sulphur.
It is raw material with sulphur that the biabsorption legal system is equipped with sulfuric acid.This method divided for three steps carried out, and wherein main process gas flow contacts and discharge big calorimetric with sulfuric acid, these heats in the acid must be distributed.In traditional production method, the production system of implementing each operation is to be made up of packed tower (wherein process gas flow contacts by filler and with a large amount of recycle acid stream from bottom to up, and this recycle acid stream plays a part mass transfer and heat transfer), storage acid jar (special-purpose acid stream recycle pump is housed), water cooler (eliminating the heat that produces), acid delivering tube line, water dilution pipeline and metrical instrument (regulating acidity and inventory).
The first step in the operation of three steps is the dry feed air, contacts dry-off moisture at this extraneous air with acid.The thermal load of air (i.e. heat of Shi Fanging and heat to be removed) is lower than the heat that is discharged in other operations, is about 10% of total heat duties in the operation of three steps.As following will point out, institute's round-robin acid in drying tower, its H
2SO
4Typical content be 93-96%, its normal temperature range is 40-70 ℃.
The operation of second step is exactly to remove the SO in the process gas after the middle transformation stage
3In this step is that hot sulfuric acid (70-110 ℃) with 98% contacts with gas, can remove about 90% the SO that is generated in this process
3The thermal load of this step operation is about 70% of total heat duties usually.This step is commonly referred to the intermediate absorption operation.Since the needs of heat release and mass transfer, the acid circulation that this step has relatively high expectations.
The operation of the 3rd step is the SO that removes in last or final conversion process outflow process gas
3Be that process gas is contacted with recycle acid stream for the third time, to remove the SO that is not eliminated that this process is generated herein
3The thermal load that the thermal load in this step is produced less than the intermediate absorption operation usually is at most 20% of the total heat release amount of acid system.
State on the implementation in three sub-systems of three operations, all need to carry out acidity adjustment and Material control.Carry out that acidity adjustment is normally carried with the intersection of acid between system and (or) method of dilute with water finishes, and inventory is normally controlled by the liquid level of regulating each system.The internal circulating load of acid is compared with the H that will absorb in each system
2O or SO
3Amount is much bigger, and its concrete internal circulating load then will determine according to following requirement, promptly can fill in the tower filler and can be in suitable limit with temperature-stable, and the latter is according to selected for avoiding too corroding.
United States Patent (USP) No. 3536446 (Maurer etc.) has been described traditional gas washing in SA production factory, wherein said three towers all are equipped with recycle pump, water cooler, pump and basin separately, and the acidity of each system then flows intersection, thin up and accesses product with the liquid between the storage bucket regulates.This method needs independent water cooler, fluid level control device, basin, analysis meter and pumping appliance, and therefore, in actual production, this method might be the most expensive, and the producing apparatus of acid also is complicated.
Now developed a kind of through improved not too complicated sour preparation system, be called " list " system, wherein the recycle system relevant with drying and intermediate absorption operation is integrated, the acid that is total in basin and the purt bucket is extracted in drying tower and the intermediate absorber through several suitable water coolers.This moment, institute's round-robin acid in dehumidification system must be 98%, and this is to absorb desired acidity in the operation, and rarer acid normally produces in independent sour dilution system.Yet three separate payments are still and need and since dehumidification system now diluted system replace, so still need to regulate three liquid levels.
Above-mentioned two kinds of production methods require complicated line of pipes, liquid level control and analysis meter so that regulate sour inventory and controlling acidity.Also need various acid coolers (being heat exchanger) to handle a large amount of circulation acid solution stream.All these results just make that the cost of equipment is very expensive, wherein also have many hidden danger, and control is also comparatively complicated.
Canadian Patent further is improved to single-stage circulation and single-stage again to this No. 1181568 and cools off, and wherein acid solution directly flows into final absorption tower by drying tower through pumping installation, so just can reduce independently finally to absorb the recycle system.Though this system has the refrigerating unit of a single acid circulation system and single-stage again, it requires to have two basins that fluid level control device and pumping installation are housed separately.In addition, its shortcoming is that also it requires diverse pumping installation, and these two pumps promptly install.Need keep in repair with independent spare unit.Its a large amount of acid solution of also needing to connect pipeline, valve, the fluid level control device of two basins and the refrigerating unit of flowing through to be giving huge intermediate absorber perfusion acid solution in addition, and the acid solution of the drying tower and the drying tower of flowing through.
Therefore, one of purpose of the present invention is exactly to provide simpler sour preparation system for biabsorption equipment.
Another object of the present invention just provides a system, and in this system, but remove in the sour place that is in relatively hot on the heat slave unit of sour preparation system, reduces the cost of thermal conversion equipment to greatest extent, and makes relevant energy retrieve to do his usefulness easily.
On the one hand, the invention provides that a kind of this equipment comprises drying tower by sulphur system vitriolic equipment, intermediate absorber and final absorption tower, each tower all has an acid inlet and acid outlet; Wherein this equipment also comprises the device that several feed in raw material for public basin, promptly is added to the device of public basin by the acid that outlet drew off on above-mentioned drying tower and final absorption tower; Be added to the feeding device of discrete basin by the acid that outlet drew off of above-mentioned intermediate absorber; The acid of being come out by public basin is added to the feeding device of above-mentioned intermediate absorber and final absorption tower inlet; Heat exchanger; The acid of being come out by above-mentioned discrete basin then enters the pumping installation of above-mentioned drying tower and intermediate absorber inlet through described heat exchanger.
On the other hand, the present invention proposes to be equipped with sulfuric acid with the biabsorption legal system, and in the method, process gas flow drying tower is removed H wherein
2O then is used for the sulphur that burns, and therefrom generates SO
2, subsequent portion SO
2Be converted into SO
3, process gas flow is therefrom removed above-mentioned SO through intermediate absorber again
3, and nearly all SO that stays in this process gas flow
2, further be converted into SO subsequently
3Process gas flow enters final absorption tower and further removes SO
3Above-mentioned process gas flow contacts with sulfuric acid liquid stream in drying tower and two absorption towers again.Its improvement comprises:
A) the acid solution stream that is come out in above-mentioned drying tower and final absorption tower merges becomes mix acid liquor stream.;
B), wherein a part of acid is flow to into above-mentioned intermediate absorber and final absorption tower with the mix acid liquor diverting flow;
The acid solution stream cooling of c) above-mentioned intermediate absorber being come out becomes cold acid solution stream;
D), wherein a part of acid is flow to into described drying tower and intermediate absorber with above-mentioned cold acid solution diverting flow.
Reach with reference to the accompanying drawings (preparation vitriolic equipment block scheme) by following described typical embodiments of the present invention and can find out objects and advantages of the present invention further.
Equipment shown in the accompanying drawing comprises three towers, and promptly drying tower 10, intermediate absorber 11 and final absorption tower 12.Each tower bottom all has a gas inlet A, and a pneumatic outlet B is arranged at the top.Each cat head all has an acid inlet P, and an acid outlet Q is arranged at the bottom of the tower.Each tower is all filled filler, thereby process gas or air and acid solution are oozed out by filler and reached fully and fine and close contacting.
The process gas recycle system of this equipment turns round routinely.Air is through 13 access arrangements that enter the mouth, and 10A enters through entering the mouth and by drying tower 10, be dry air at the air that exports 10B.Sulphur is met the dry air burning and is generated sulfurous gas in burner (not drawing).Process gas (being the mixture of air and sulfurous gas this moment) enters catalytic converter (not drawing), and most here Sulphur Dioxide is a sulphur trioxide.Contain SO
3With unconverted SO
2Process gas enter intermediate absorber 11 through inlet 11A, 11B discharges by outlet, this moment most SO
3Be converted into acid.The gas that is come out by intermediate absorber enters second catalytic converter (not drawing), nearly all SO here
3All be converted into SO
3The gas that comes out from second convertor enters final absorption tower 12, in this tower with the SO of final residual
2Absorb with recycle acid.At last, gas enters atmosphere through chimney 14.
The acid that acid is exported 10Q, 11Q and 12Q discharge enters mixed storage tank 15, and this jar is passed to mutually by underflow by part plate washer 18(and keeps acid position balance between jar) it is divided into public basin 16 and discrete basin 17.Be transported to public basin 16 by drying tower 10 and final absorption tower 12 effusive acid, the acid of being come out by intermediate absorber 11 is transported to discrete basin 17.
The acid of being discharged by intermediate absorber 11 contains dissolved SO
2, therefore, divide the acid of Storage Tank 17 also to contain SO
2Like this, the acid that enters drying tower and inter-chamber tower equally also contains SO
2In drying tower, this quilt (SO
2) acid of polluting contacts with atmosphere.In this tower, not only airborne wet steam is easy to enter in the acid, and dissolved SO
2Also enter at an easy rate in the exsiccant airflow.Therefore, the air of outlet 10B is actually complete drying, and the acid of outlet 10Q does not virtually completely contain SO
2So in fact the acid of public basin 16 do not contain SO
2, the acid that enters final absorption tower 12 by inlet 12P does not contain SO yet
2So, finally do not contain SO in the expellant gas of absorption tower
2
Device of the present invention can also improve the design efficiency of heat exchanger.Reaction in each tower all produces heat, and therefore its temperature of acid of coming out in the tower is all than the height that enters, yet the heat that is produced in each tower has nothing in common with each other.In three total heat that tower produced, drying tower 10 accounts for 10%, and intermediate absorber 11 accounts for 70%, and final absorption tower 12 is 20%.Meanwhile, it is such in these towers the contact between gas, the acid being required, and the sour general proportions of these three towers of promptly flowing through is 1: 2: 1.The direct result of these two groups of data is: its temperature of acid of the drying tower 10 of flowing through only changes slightly, and its temperature of acid on the final absorption tower 12 of flowing through has bigger rising, and the temperature of the acid of the inter-chamber tower 11 of flowing through raises bigger.Institute's target temperature all is the typical equilibrium temperature that produces owing to these thermopositive reaction on the accompanying drawing.
As giving material, the acid of intermediate absorber outlet 11Q is the hottest, reaches 110 ℃.This acid that discrete basin 17 receives is by being pumped to heat exchanger 21, a little higher than 100 ℃ of its temperature.In order to prevent that Yin Wendu is too high and cause heavy corrosion, enter before the intermediate absorber 11, the temperature of acid must be chilled to about 70 ℃.This temperature also suits for the acid that enters drying tower 10.Because what produced in the drying tower is hot less, in the acid that exports 10Q only a little more than 75 ℃.Under this temperature, enter public basin 16 and must not cool off again before.By the acid of coming out in final absorption tower, its temperature is not higher than 90 ℃.
Therefore, the present invention only needs a heat exchanger 2.1.And it is set at the hotter part of acid.Like this, not only replaced three heat exchangers needing in the conventional apparatus with a single-stage heat exchanger, and this single-stage heat exchanger is arranged on the hotter part of acid, this can help removing heat, and can reduce the cost of heat-transfer system.
According to the equipment that the present invention disposed benefit is improved greatly, wherein have only the recycle acid of half to need cooling.No. 1181568 disclosed methods of this and Canadian Patent are just opposite, in this patent, the cycling stream of drying tower and the intermediate absorber of flowing through is walked the torrid zone in the technology acid, in any actual design, the total amount of mixed flow is equivalent to be circulated in the most of acid amount (being typically 3/4ths) in each tower of device.Therefore required cooling apparatus is very big, so involve great expense.In these two kinds of methods, though the heat that will remove is constant, the sour temperature of heat exchanger outlet is identical, and according to method of the present invention, the inlet temperature difference is bigger, and this just greatly reduces the scale and the cost of cooling apparatus.
In addition, the pump that equipment useful capacity of the present invention is identical is handled various acid streams respectively, and this just makes pumping appliance realize stdn.Like this, investment and maintenance cost are obviously saved.
In addition, equipment operation of the present invention is comparatively steady, so the temperature in the drying tower is subjected to the minimum that influences of seasonal variation.
In above-mentioned determined optimum embodiment, public basin 16 and discrete basin 17 are connected by the balance pipeline that is arranged under the dividing plate 18, its advantage only need to be acid solution position of control just passable, it is opposite that this and Canadian Patent are reported for No. 1181568, and it need control two acid solution positions.
In a general embodiment, two basins can make two independent basins that separate separately.
According to the institute's installed device that requires of the present invention, can not only reduce investment cost, improve heat exchanger effectiveness, but also can reduce the metrical instrument that is used for operating device.Owing to can regard what " series connection " joined as between each tower in the acid circulation system, therefore, all can pass through public basin 16 at a certain stage all acid.So only need a sleeving temperature to measure and control instruments, a cover acidity analysis and a control instruments.For ease of getting sour sample, these instrument preferably are installed on the public basin 16, because the acid in this place can reflect the variation (can reflect the characterization factor that acid changes) of sulphur content in the burner at first, any operation that needs to add water, as long as 11Q injects liquid stream, preferably be added within the tower 11.
Because the acid that enters final absorption tower from basin 16 intensification heating by drying tower or final absorption tower, so another benefit of present device is exactly, and final absorption tower can reach optimal working temp with the very fast heating of cold acid.This not only helps putting forward highly acid quality, and might reduce when starting sulphur trioxide to atmospheric pollution.Otherwise, when final absorption tower was moved at low temperatures, the problem of topsoil just might appear.
Errata
CPCH 856860
Claims (5)
1, makes vitriolic equipment with sulphur and comprise drying tower, middle tower and the final absorption tower of inhaling; Each tower all has an acid inlet and acid outlet; It is characterized in that acid that this equipment comprises that the outlet by above-mentioned drying tower and final absorption tower draws off is transported to the device of public basin;
The acid that is drawn off by the outlet of described intermediate absorber is transported to the device of discrete basin;
The acid of discrete basin is added to the device of intermediate absorber and final absorption tower inlet;
A heat exchanger;
The acid of discrete basin then is extracted into the device of described drying tower and intermediate absorber inlet by pump through above-mentioned heat exchanger.
2, as the desired equipment of claim 1, the acid that wherein is added to drying tower and intermediate absorber inlet nearly all is to cool off in above-mentioned heat exchanger;
3, as claim 1 or 2 desired equipment, wherein said public basin is harmonious also with dividing Storage Tank, and is provided with the equilibrator of underflow;
4, be equipped with in the vitriolic process in the biabsorption legal system, process gas flow is wherein therefrom removed H by drying tower
2O is used for the sulphur that burns then, generates SO
2, part SO
2Be converted into SO
3, process gas flow enters intermediate absorber again, therefrom removes SO
3, with remaining SO in this process gas flow
2Almost all be converted into SO again
3, process gas flow enters final absorption tower again, removes SO further
3, above-mentioned process gas flow contacts with sulfuric acid liquid stream in drying tower and two absorption towers, and its improvement comprises:
A) with the effusive acid stream of above-mentioned drying tower and final absorption tower merging becoming mixing acid stream;
B), make wherein a part of acid enter intermediate absorber and final absorption tower with above-mentioned mixing acid diverting flow;
The acid stream cooling of c) intermediate absorber being come out forms cold acid stream;
D), wherein a part of acid is flow to into above-mentioned drying tower and intermediate absorber with above-mentioned cold sour diverting flow.
5, according to the method for claim 4, wherein the acid of being come out by drying tower is before entering public basin, substantially without cooling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85109394A CN85109394B (en) | 1982-01-21 | 1985-12-27 | Method and apparatus for making sulphuric acid |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000394588A CA1181568A (en) | 1982-01-21 | 1982-01-21 | Method and apparatus for making sulphuric acid |
| CN85109394A CN85109394B (en) | 1982-01-21 | 1985-12-27 | Method and apparatus for making sulphuric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85109394A true CN85109394A (en) | 1987-07-08 |
| CN85109394B CN85109394B (en) | 1987-11-11 |
Family
ID=25669537
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85109394A Expired CN85109394B (en) | 1982-01-21 | 1985-12-27 | Method and apparatus for making sulphuric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN85109394B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1076215C (en) * | 1999-08-13 | 2001-12-19 | 丁华 | Complementary heat-exchanging process of two conversions of sulfuric acid apparatus |
| CN115350569A (en) * | 2022-08-31 | 2022-11-18 | 江西洪安化工有限公司 | Air purification system |
-
1985
- 1985-12-27 CN CN85109394A patent/CN85109394B/en not_active Expired
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1076215C (en) * | 1999-08-13 | 2001-12-19 | 丁华 | Complementary heat-exchanging process of two conversions of sulfuric acid apparatus |
| CN115350569A (en) * | 2022-08-31 | 2022-11-18 | 江西洪安化工有限公司 | Air purification system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN85109394B (en) | 1987-11-11 |
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