CN85109383A - Sulfur trioxide absorption and technological process thereof - Google Patents
Sulfur trioxide absorption and technological process thereof Download PDFInfo
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- CN85109383A CN85109383A CN85109383A CN85109383A CN85109383A CN 85109383 A CN85109383 A CN 85109383A CN 85109383 A CN85109383 A CN 85109383A CN 85109383 A CN85109383 A CN 85109383A CN 85109383 A CN85109383 A CN 85109383A
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Abstract
Sulfur trioxide absorption with spray booth is used for the sulfuric acid absorption sulphur trioxide, the sulfuric acid absorption of being sprayed in the spray booth of most of sulphur trioxide in tower, and remaining sulphur trioxide in the filler uptake zone by sulfuric acid absorption.The outer spray booth of tower is available.This tower has improved heat transfer, and has reduced the tower internal corrosion.
Description
The present invention relates to produce the technological process of the vitriol oil and used equipment thereof with the sulfuric acid absorption sulphur trioxide.
With in the contact process of sulfur dioxide to produce sulfuric acid, resulting dry sulfur dioxide gas is by a series of catalyst layers in tradition, and all sulfurous gas all change into sulphur trioxide basically there.Then, sulphur trioxide is used sulfuric acid absorption in one or several absorption tower, just obtains the vitriol oil.
Generally, contain 5～13%(volume from the sulphur trioxide air-flow of catalyzed conversion layer) sulphur trioxide, before absorbing, this gas generally is cooled to 160～260 ℃.In being lined with the packed absorber of brick, generally be by sulphur trioxide being removed from air-flow with the sulfuric acid counter-current absorption.
Produce a large amount of heat owing to absorb sulphur trioxide, and need prevent from the air-flow of discharging, to contain unabsorbed sulphur trioxide,, just need a large amount of acid to flow through the absorption tower, therefore will avoid using caustic acid if the absorption tower is too hot.In addition, because the absorption of using acid flow is very big, be desirable so avoid the concentration range of acid wide.5～10% of the general just recycle acid in absorption tower filler and auxiliary pipeline system of the finished acid of discharging.Under the condition of using inexpensive material, the temperature of acid generally reaches 120 ℃.
Acid is downward, gas makes progress by the adverse current of tower packing, requirement is designed to that enough spaces can be arranged to tower, so that two kinds of fluids can interact and pass through mutually, and can avoid occurring usually said liquid flooding situation, promptly air-flow stops the situation that liquid is discharged from weighting material.When gas at first entered filler, this problem was the most serious, and this is because sulphur trioxide is present in the gas, thus this place's gas flow maximum, and the hottest (thereby density is minimum), cause gas volume maximum by the filler space.Simultaneously because acid absorbs most of sulphur trioxide in the gas in the lower, packing area, so the liquid flow rate that flows downward in this zone is also maximum.
The absorption tower of present design, requiring has sparger on the top of filler, makes the absorption acid that enters be distributed on the filler, and the surface of filler is all soaked, and absorbs sulphur trioxide to reach the biglyyest.
A critical defect on tradition absorption tower is, needs thick brick lining in tower, and is too hot with the liner of the shell that prevents tower and brick back.The gas (160～260 ℃) of heat generally is sent to the lower position of directly adjacent with brick lining tower, and disadvantageously, this position is only intermittently by moistening.Such brick lining has increased the expense of tower, and is difficult to install.
In addition, adopt acid to absorb and remove sulphur trioxide, generally must satisfy the requirement of two contradictions.Secondly, require to remove the whole sulphur trioxides in the gas one requires to surpass sulphur trioxide is all removed in the restriction of used vitriolic concentration and temperature from gas, and, the rate of removing reaches 99.9% or higher.
First requires usually at 15～20% places of inner-tower filling material bottom, promptly with go into the first part filler place that implication contacts and reach.This requirement has determined the diameter of tower, from but most important factor the expense of tower.80～85% remaining fillers make the sulphur trioxide absorption reach the high level that environmental management department requires, and for this part, do not need so big tower diameter or big sour flow like this.
Thereby there is another shortcoming in common absorption tower, and in those towers, with respect to other parts of tower and the flow of tower upper gas density, flow and acid, the top of tower is excessive.
In the modern sulfuric acid process for making that uses the biabsorption system, two absorption towers are arranged, wherein each all is subjected to the evil of above shortcoming.
The objective of the invention is for a kind of absorption tower and technological process thereof are provided, wherein the size of tower and all be reduced at the cycle rate of tower packing district acid and be lower than traditional scale.
Another object of the present invention be for reduce gas to tower at the bottom of the infringement of construction material, make and can use thin or make liner without brick.
So the present invention at first provides a kind of sulfur trioxide absorption, it comprises:
(a) shell;
(b) the sulfuric acid spray booth of the lower position in above-mentioned shell;
(c) in above-mentioned shell and above-mentioned spray booth above sulphur trioxide filler uptake zone;
(d) in above-mentioned spray booth, spray the vitriolic device;
(e) will contain hot sulphur trioxide air-flow and deliver to the device that above-mentioned spray booth goes, in spray booth, generate the sulphur trioxide air-flow that concentration has reduced;
(f) above-mentioned low dense sulphur trioxide air-flow is delivered to the device of above-mentioned filler uptake zone;
(g) sulfuric acid is delivered to the device of above-mentioned filler uptake zone;
(h) collect from the vitriolic device of above-mentioned spray booth and uptake zone;
(i) be collected in the device of the air-flow that above-mentioned filler uptake zone generates.
The present invention also provides aforesaid tower, comprises the side spray booth that tower is outer in addition, and this spray booth links to each other with above-mentioned sulfuric acid spray booth, and this is individual preferred plan.
In addition, the present invention also provides the technological process of producing the vitriol oil with the hot gas flow that contains sulphur trioxide, and this technological process comprises:
(a) said flow is delivered to sulfuric acid spray booth in the absorption tower;
(b) in above-mentioned spray booth, spray one time recycle sulfuric acid, make to be absorbed by above-mentioned recycle sulfuric acid, and generate vitriol oil and lower concentration sulphur trioxide air-flow from the sulphur trioxide major part in the said flow;
(c) above-mentioned low dense sulphur trioxide air-flow is delivered to the sulphur trioxide filler uptake zone above the spray booth in the above-mentioned absorption tower;
(d) secondary circulation sulfuric acid is delivered to above-mentioned sulphur trioxide uptake zone, made that staying the above-mentioned sulphur trioxide that hangs down in the dense sulphur trioxide air-flow all is absorbed substantially, and generate the secondary vitriol oil and the air-flow that is substantially free of sulphur trioxide;
(e) collect above-mentioned once with the secondary vitriol oil;
(f) collect the above-mentioned air-flow that is substantially free of sulphur trioxide.
Be sent to once can distinguishing directly from a common acid source of spray booth and filler uptake zone, perhaps come suitable different acid system in the comfortable scale operation vitriolic factory respectively with secondary circulation acid.For example, delivering to the recycle acid of packed absorber can be from drying tower, initial tower or the acid system of final tower or their any mixing.The acid of delivering to spray booth can be from above any filler uptake zone acid source or from other separate payment.Preferably supply with acid from a common circulation acid source for two kinds, and the volume of the volume ratio filler uptake zone acid of spray booth acid is big.
Thereby, in preferred plan, the invention provides the technological process of explanation as mentioned, a wherein said recycle sulfuric acid accounts for the major part of total recycle sulfuric acid, and described secondary circulation sulfuric acid accounts for the small portion of total recycle sulfuric acid.
According to the temperature of acid with the concentration requirement of concentrated acid is determined to deliver to the relative populations of the recycle acid of filler uptake zone and spray booth.Under normal operating condition, spray booth needs the flow of acid generally to surpass the desired flow in filler uptake zone., under the situation that relates to energy recovery or other consideration, corresponding discharge relation can change, so that opposite situation also exists.Such a case also has, and promptly when requiring from spray booth sour awfully hot, just should reduce to send into the recycle acid volume of spray booth.
Two kinds of concentrated acids can mix in tower and exist with the form of mixtures of acid, also can be used as the self filler uptake zone acid stream different with spray booth to emit from tower.In the previous case, two kinds of concentrated acids are mixed, and this causes one " jointly " in technological process of the present invention to carry sour system.On the other hand, system " separates " the directly mixing of concentrated acid that expression comes from filler uptake zone and spray booth with term.
Thereby as seen, the concentrated acid that generates in two different zones of tower or can arbitrarily mix perhaps can mix with any other the suitable recycle acid in the extensive sulfuric acid plant, perhaps goes up two kinds of mixing and all can allow.
In preferred plan, can pass through spray booth from the vitriol oil of packing area, thereby mix with the vitriol oil of spray booth.
In order to understand the present invention preferably, also optimum implementation of the present invention is described with reference to the accompanying drawings for example, wherein:
Fig. 1 illustrates the longitudinal sectional view of sulfur trioxide absorption among the present invention;
Fig. 2 illustrates the sectional view that places the sour sprinker in the tower (Fig. 1);
Fig. 3 illustrates the longitudinal sectional view of the tower (Fig. 1) that has side acid sprinker;
Fig. 4,5 and 6 has schematically represented the acid circulation system relevant with absorption tower of the present invention.
There is a carbon steel shell 11 on absorption tower shown in Fig. 1, and the shell upper top has waste gas outlet 12, at outer casing bottom hot gas inlet 13 and acid outlet 14 is arranged.
The liner of making at the useful acid resisting brick of shell 11 lower positions 15, and a ceramic support 16 are sulfuric acid spray booth 17 between the bottom of this support and shell.Placing in the chamber 17 is the sprinker 18 that disperses acid, and acid 19 is introduced from entering the mouth.
In shell 11, supporting 16 tops is the sulphur trioxide uptake zones 20 of filling with the saddle type ceramic packing, and gas and acid can both be passed filler, make can contact cmpletely between them.
The sour decollator 22 of 21 and cast irons of an acid inlet is arranged on the top of shell 11, is mist eliminator 23 above decollator, and it is made of the glass fibre that is contained in the stainless steel frame.
Fig. 2 illustrates sour sprinker 18, and it is made up of many parallel pipes, and many low pressure reduction nozzles 24 are arranged on the pipe.The another kind of arrangement mode of sprinker is with the nozzle arrangement radial in spray booth.
In another embodiment, can spray the acid that the vitriolic device can produce coflow, countercurrent flow or cross flow in distributing chamber 17, this is because there is not the reason of sulphur trioxide counterpressure on sulfuric acid.Sprinker generally should be checked with replaceable.
Fig. 3 illustrates a kind of better absorption tower among the present invention, and wherein the shell 11 of Fig. 1 connects a hot gas conduit 25 instead, and this conduit is formed from steel and makees lining with acid resisting brick 26.The lower end of conduit 25 is the outer side spray booth 27 of tower, and indoor have a side acid sprinker 28.
In another form of tower in Fig. 3, sprinker can place in the outer big conduit vertically downward of a tower, makes hot sulfur trioxide gas obtain handling before entering tower.
Fig. 4 illustrates the common sour circulation process that links to each other with the absorption tower, wherein from once the mixing in tower respectively with the secondary vitriol oil of spray booth and filler uptake zone, and is discharged to pump groove 29.Be recycled and by heat exchanger 30 coolings, respectively spray booth 17 delivered in most of acid from the acid of groove 29, filler uptake zone 20 is delivered in small portion acid.The installation of product line 31 as shown in FIG..
Fig. 5 illustrates another its sour circulation process, and wherein heat exchanger 30 places after the spray booth acid leading point, before the filler uptake zone inlet.Arrange like this to make the major part of global cycle acid can optionally reach higher temperature.
Fig. 6 illustrates the sour circulation process that filler uptake zone and sprinkling are distinguished, for the separately feed and the feasible vitriol oil that can produce comparatively high temps of acid circulation of spray booth, to reach higher energy recovery.
Be in operation, the tower among the present invention is equivalent to produce employed elementary absorption tower in 2000 short tons of sulfuric acid plant in general every day, and 200 ℃ sulfur trioxide gas is accepted on this absorption tower, and this gas is to be obtained through 93% conversion by 12% sulfur dioxide gas.
According to Fig. 1 and Fig. 4, the flow of total common recycle acid that enters tower is 4000 gallons of per minutes (made in U.S.A), and the temperature of acid is 80 ℃, and concentration is 98.5%.Most of (2500 gpm) delivers to spray booth, and small portion (1500 gpm) is delivered to the filler uptake zone.
In the embodiment illustrated, the diameter of place, filler uptake zone tower is 20 feet, and as long as fills 12 feet thick general 3 inches saddle packings.What form contrast therewith is for reaching the identical result who removes sulphur trioxide, in traditional tower design, to need 20 feet thick fillers.
Export 14 effusive acid from tower bottom, temperature is 120 ℃, and concentration is 99.2%.The sulphur trioxide specific absorption generally surpasses 99.99%.
In improved technological process,, be lower than through the spray booth inlet 19 sulfuric acid temperature that enter tower through the filler uptake zone inlet 21 recycle sulfuric acid temperature that enter tower according to Fig. 1 and Fig. 5.100 ℃ can only be cooled to through 19 the sulfuric acid of entering the mouth, and 80 ℃ can be cooled to by 21 the sulfuric acid of entering the mouth.In this case, now owing to conducting heat more than 100 ℃, so total heat 84% is useful, and in the technological process of first example, the acid of being sent to two places all is cooled to 80 ℃, and it is available having only 51% total heat like this.
Adopt the advantage of separately carrying out heat exchange to make in the design tangible handiness is arranged, this handiness does not have in traditional single tower design.
Thereby, can find out that the improvement with the sulfuric acid absorption sulphur trioxide provided by the present invention is, before entering filler, adopt acid to spray the sulphur trioxide that absorbs earlier in the gas to give, the such sprinkling generally space below filler is carried out, and also can carry out in the inlet gas pipe.The acid that is used to spray accounts for the major part of absorption system recycle acid, and the small portion of acid is used for washing the absorption tower filler.
Above-mentioned pre-absorption technical process has produced lot of advantages.
At first, with cold acid brick and the metal in the sprinkling district that at first enters of flushing gas continuously, the liner after can protection tile. And owing to can use thinner brick lining, the expense of can reducing investment outlay.
In another embodiment, when experiment of the present invention, in the sprinkling district of tower, use the corrosion resistant metal of nearest development, therefore can fully phase out acidproof brick.
Second advantage is, because littler by the gas flow of filler, the higher and fluid flow of gas density reduces, so can adopt the tower of small-scale. According to technical process of the present invention, the diameter of tower generally can be reduced to 25%.
The 3rd advantage is the flow that has reduced acid in the compartment system, so can use littler pipe and top of tower also can reduce size.
Another advantage is, along with the change that sulfur trioxide absorbs, can change the flow that sprays acid, and allow the sour flow of flushing filler not change. The tradition disperser flow can not turn down very soon, and if sprinkling system can be designed under reduced pressure operate or needs, can be designed to have the special nozzle that can close. In the absorption technique process that will carry out the energy recovery, this advantage is particularly useful.
Another advantage is that the heat exchange operation that links to each other with sprinkler is separated with the cooling of filler, and the former does not need acid is remained on low temperature, and to the latter, then needs good cooling.
Claims (6)
1, be used for being produced by the hot gas that contains sulphur trioxide the technological process of the vitriol oil, this technological process comprises:
(a) described gas is delivered to sulfuric acid spray booth in the absorption tower;
(b) in described spray booth, spray one time recycle sulfuric acid, the most of sulphur trioxide in the described gas is absorbed effectively, to generate a vitriol oil and to hang down dense sulfur trioxide gas by described recycle sulfuric acid;
(c) described low dense sulfur trioxide gas is delivered to the sulphur trioxide filler uptake zone above the spray booth in the described absorption tower;
(d) secondary circulation sulfuric acid is delivered to above-mentioned sulphur trioxide uptake zone, the sulphur trioxide that all are stayed in the described low dense sulfur trioxide gas all is absorbed basically, and generates the secondary vitriol oil and do not have the gas of sulphur trioxide substantially;
(e) collect above-mentioned once with the secondary vitriol oil;
(f) collect the above-mentioned gas that does not have sulphur trioxide substantially.
2, as the technological process that claim 1 proposed, a wherein above-mentioned recycle sulfuric acid accounts for the major part of common recycle sulfuric acid, and secondary circulation sulfuric acid accounts for the small portion of above-mentioned common recycle sulfuric acid.
3, as the technological process that claim 1 proposed, wherein above-mentioned is once mixed with the secondary vitriol oil.
4, any one technological process as being proposed in the claim 1,2 or 3, also further comprise: before the body of supplying gas arrives above-mentioned sulfuric acid chamber, with the described recycle sulfuric acid of a part and the described tower outside spray booth that links to each other with above-mentioned sulfuric acid chamber in, spray above-mentioned sulfur trioxide gas.
5, sulfur trioxide absorption comprises:
(a) shell;
(b) be positioned at the sulfuric acid spray booth of above-mentioned shell lower position;
(c) be positioned at the sulphur trioxide filler uptake zone of the spray booth top of above-mentioned shell;
(d) be used in above-mentioned spray booth, spray the vitriolic device;
(e) be used for the device that a hot gas that contains sulphur trioxide is delivered to described spray booth, low dense sulfur trioxide gas produces at spray booth;
(f) be used for above-mentioned low dense sulfur trioxide gas is delivered to the device of above-mentioned filler uptake zone;
(g) be used for sulfuric acid is delivered to the device of above-mentioned filler uptake zone;
(h) be used to collect sulfuric acid apparatus from above-mentioned spray booth and uptake zone;
(i) be used to the to collect device of the gas that produced from above-mentioned filler uptake zone.
6, as the tower that claim 5 proposed, also further comprise a side spray booth, this chamber is in the outside of above-mentioned tower, and is connected with above-mentioned sulfuric acid spray booth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN85109383A CN85109383B (en) | 1985-11-21 | 1985-12-27 | Absorption column and related process for so3 |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US80029485A | 1985-11-21 | 1985-11-21 | |
| CN85109383A CN85109383B (en) | 1985-11-21 | 1985-12-27 | Absorption column and related process for so3 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85109383A true CN85109383A (en) | 1987-09-16 |
| CN85109383B CN85109383B (en) | 1987-09-23 |
Family
ID=25742148
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85109383A Expired CN85109383B (en) | 1985-11-21 | 1985-12-27 | Absorption column and related process for so3 |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN85109383B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503865A (en) * | 2011-10-28 | 2012-06-20 | 南京佳和日化有限公司 | Method for recycling sulfur trioxide and efficiently producing sulfonic acid |
| CN102502529A (en) * | 2011-11-11 | 2012-06-20 | 王强斌 | Automatic control temperature-regulating acid-regulating water-regulating system in drying absorption contact sulfuric acid production |
-
1985
- 1985-12-27 CN CN85109383A patent/CN85109383B/en not_active Expired
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102503865A (en) * | 2011-10-28 | 2012-06-20 | 南京佳和日化有限公司 | Method for recycling sulfur trioxide and efficiently producing sulfonic acid |
| CN102502529A (en) * | 2011-11-11 | 2012-06-20 | 王强斌 | Automatic control temperature-regulating acid-regulating water-regulating system in drying absorption contact sulfuric acid production |
| CN102502529B (en) * | 2011-11-11 | 2013-06-05 | 王强斌 | Automatic control temperature-regulating acid-regulating water-regulating system in drying absorption contact sulfuric acid production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN85109383B (en) | 1987-09-23 |
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Correct: Li Luoying False: Wu Xiaonan Number: 42 Page: 54 Volume: 3 |
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Free format text: CORRECT FROM: WU XIAONAN TO: LI LUOYING |
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