CN210366982U - Absorption device for potassium sulfate byproduct hydrochloric acid by Mannheim method - Google Patents
Absorption device for potassium sulfate byproduct hydrochloric acid by Mannheim method Download PDFInfo
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- CN210366982U CN210366982U CN201920614176.4U CN201920614176U CN210366982U CN 210366982 U CN210366982 U CN 210366982U CN 201920614176 U CN201920614176 U CN 201920614176U CN 210366982 U CN210366982 U CN 210366982U
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Abstract
The utility model provides a potassium sulfate byproduct hydrochloric acid absorption device by a Mannheim method, wherein the input end of a carbon fine cooler is connected with a HCL outlet of a Mannheim furnace; the output end of the carbon cooler is connected with the input end of the crude acid intermediate tank; the output end of the crude acid intermediate tank is connected with the input end of the washing tower group; the output end of the washing tower group is connected with the input end of the falling film absorption tower group; the output end of the falling film absorption tower group is connected with the input end of the tail gas absorption tower group; the output end of the tail gas absorption tower group is connected with the input end of the tail gas neutralization tower group; the alkali liquor input end of the tail gas neutralization tower group is connected with an alkali liquor tank through an alkali liquor pump and a valve; and the output end of the tail gas neutralizing tower group is connected with a tail gas discharge chimney. The device is also additionally provided with hydrochloric acid decoloring and filtering and automatic water replenishing and acid discharging equipment. The quality of the hydrochloric acid in the process can reach the quality standard of first-class products in the industrial synthetic hydrochloric acid GB320-2006 standard. The tail gas emission meets the national emission requirements, and the operation is simpler and more practical.
Description
Technical Field
The utility model relates to a potassium sulphate preparation technical field especially relates to a manheim method potassium sulphate byproduct hydrochloric acid absorbing device.
Background
The Mannheim method realizes the preparation of potassium sulfate by a series of preparation equipment. The Mannheim method is widely used for preparing potassium sulfate at present, the technology of the Mannheim method is mature and reliable, and the production capacity of preparing the potassium sulfate can be adjusted according to actual requirements. In the process of preparing the sulfate product by the Mannheim method, potassium sulfate and byproduct HC1 can be simultaneously generated.
HC1 can be used as by-product for preparing dichloroethane, hydrochloric acid, chlorosulfonic acid, etc. However, the absorption effect of the HC1 is poor or the HC1 cannot be effectively recovered, so that the HC1 is wasted, the unrecovered HC1 is discharged, the environment is affected, and the recovery and reuse of the HC1 are also affected.
Disclosure of Invention
The utility model provides an effective recovery manheim method preparation sulphate in-process produces HC1 to manheim method potassium sulphate byproduct hydrochloric acid absorbing device of HC1 quality and absorption efficiency has been improved.
Therefore, the utility model discloses a: a carbon cooler, a crude acid intermediate tank, a washing tower group, a falling film absorption tower group, a tail gas neutralization tower and a lye tank;
the input end of the carbon cooler is connected with the gas input end of HC 1; the output end of the carbon cooler is connected with the input end of the crude acid intermediate tank; the output end of the crude acid intermediate tank is connected with the input end of the washing tower group;
the output end of the washing tower group is connected with the input end of the falling film absorption tower group; the output end of the falling film absorption tower group is connected with the input end of the tail gas absorption tower group; the output end of the tail gas absorption tower group is connected with the input end of a tail gas neutralization tower group HC 1; the alkali liquor input end of the tail gas neutralization tower group is connected with an alkali liquor tank through an alkali liquor pump and a valve; and the output end of the tail gas neutralizing tower group is connected with a tail gas discharge chimney.
It is further noted that the scrubber tower set comprises at least two scrubber towers; the washing towers are connected in series;
each washing tower is provided with a circulation input end and a circulation output end;
the circulation input end of the washing tower is connected with the circulation output end through a valve and a washing circulation pump.
Further, it should be noted that the method further includes: a high-level water tank, a circulating tank and a finished acid intermediate tank;
the falling film absorption tower group comprises: a first falling film absorption tower and a second falling film absorption tower;
the first falling film absorption tower and the second falling film absorption tower are connected in series;
the bottom output end of the first falling film absorption tower is connected with the top input end of the finished acid intermediate tank;
the bottom output end of the second falling film absorption tower is connected with the top input end of the circulating groove;
the circulating output end of the finished acid intermediate tank is connected with the circulating input end of the first falling film absorption tower through a valve and a hydrochloric acid circulating pump;
the circulating output end of the circulating groove is connected with the circulating input end of the second falling film absorption tower through the falling film absorption pump;
the high-level water tank is connected with the water input end of the tail gas absorption tower group through a valve and a water injection flowmeter;
the tail gas acid output end of the tail gas absorption tower group is connected with the tail gas acid input end of the circulating tank through a valve;
the tail gas acid output end of the circulating tank is connected with the tail gas acid input end of the finished product acid intermediate tank through a valve;
the tail gas acid output end of the finished product acid intermediate tank is communicated with the crude product acid intermediate tank through a valve and a washing tower group.
Further, it should be noted that the method further includes: a deironing and decolorizing resin tank group;
the circulating output end of the finished acid intermediate tank is also connected with the input end of the iron removal decolorizing resin tank group through a valve and a finished acid circulating pump;
the output end of the iron removal decolorizing resin tank group is connected with a finished acid storage tank;
the finished acid circulating pump is connected with the hydrochloric acid circulating pump in parallel;
the iron removal decolorizing resin tank group comprises at least one iron removal decolorizing resin tank;
the iron removal decoloration resin tanks are connected in series.
Further, the tail gas absorption tower group comprises an absorption fan and at least one tail gas absorption tower;
the tail gas absorption towers are connected in series; the absorption fan is connected in series between the tail gas absorption towers;
each tail gas absorption tower is provided with a circulation input end and a circulation output end;
the circulation input end of the tail gas absorption tower is connected with the circulation output end through a valve and a tail gas absorption circulating pump.
It is further noted that the tail gas neutralization tower is provided with a circulation input end and a circulation output end;
the circulating input end of the tail gas neutralizing tower is connected with the circulating output end through a valve and a tail gas neutralizing circulating pump.
It should be further noted that the bottom discharge end of the washing tower set, the bottom discharge end of the finished acid intermediate tank, the bottom discharge end of the tail gas absorption tower set, the bottom discharge end of the tail gas neutralization tower and the bottom discharge end of the lye tank are respectively connected with a washing bottom discharge pipeline through valves.
It should be further noted that a valve and a flowmeter are connected between the water input end of the tail gas absorption tower group and the high-level water tank.
According to the technical scheme, the utility model has the advantages of it is following:
the device comprises a carbon-refining cooler, a crude acid intermediate tank, a washing tower group, a falling film absorption tower group, a tail gas neutralization tower and a lye tank, and forms a Mannheim method potassium sulfate byproduct hydrochloric acid absorption device, the quality and the absorption efficiency of hydrochloric acid are improved, hydrochloric acid filtration is added in the device, automatic water replenishing and acid discharging equipment is adopted, the absorption effect of HC1 is improved, and HC1 can be recycled.
Drawings
In order to more clearly illustrate the technical solution of the present invention, the drawings used in the description will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art that other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic diagram of a hydrochloric acid absorption apparatus for potassium sulfate byproduct produced by Mannheim process.
Detailed Description
In order to make the objects, features and advantages of the present invention more obvious and understandable, the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments, and obviously, the embodiments described below are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the scope of protection of this patent.
The utility model provides a manheim method potassium sulphate byproduct hydrochloric acid absorbing device, as shown in figure 1, include: a carbon cooler 1, a crude acid intermediate tank 2, a washing tower group 3, a falling film absorption tower group 4, a tail gas absorption tower group 5, a tail gas neutralization tower 6 and a lye tank 7; the input end of the carbon cooler 1 is connected with the gas input end of HC 1; the output end of the carbon cooler 1 is connected with the input end of the crude acid intermediate tank 2; the output end of the crude acid intermediate tank 2 is connected with the input end of the washing tower group 3; the output end of the washing tower group 3 is connected with the input end of the falling film absorption tower group 4; the output end of the falling film absorption tower group 4 is connected with the input end of the tail gas absorption tower group 5; the output end of the tail gas absorption tower group 5 is connected with the input end of the tail gas neutralization tower group 6 HC 1; the alkali liquor input end of the tail gas neutralizing tower 6 group is connected with an alkali liquor tank 7 through an alkali liquor pump and a valve; the output end of the tail gas neutralization tower 6 group is connected with a tail gas discharge chimney.
The scrubber bank 3 comprises at least two scrubbers 11; the washing tower 11 is connected with the washing tower 11 in series; each washing tower 11 is provided with a circulation input end and a circulation output end; the circulation input end of the washing tower 11 is connected with the circulation output end through a valve and a washing circulation pump.
The device still includes: a high-level water tank 8, a circulating tank 13 and a finished acid intermediate tank 12; the falling film absorption tower group 4 includes: a first falling film absorption tower 21 and a second falling film absorption tower 22; the first falling film absorption tower 21 and the second falling film absorption tower 22 are connected in series; the bottom output end of the first falling film absorption tower 21 is connected with the top input end of the finished acid intermediate tank 12; the bottom output end of the second falling film absorption tower 22 is connected with the top input end of the circulating groove 13; the circulating output end of the finished acid intermediate tank 12 is connected with the circulating input end of the first falling film absorption tower 21 through a valve and a hydrochloric acid circulating pump; the circulation output end of the circulation tank 13 is connected with the circulation input end of the second falling film absorption tower 22 through a falling film absorption pump; the high-level water tank 8 is connected with the water input end of the tail gas absorption tower group 5 through a valve and a water injection flowmeter; the tail gas acid output end of the tail gas absorption tower group 5 is connected with the tail gas acid input end of the circulating tank 13 through a valve; the tail gas acid output end of the circulating tank 13 is connected with the tail gas acid input end of the finished product acid intermediate tank 12 through a valve; the tail gas acid output end of the finished product acid intermediate tank 12 is communicated with the crude product acid intermediate tank 2 through a valve and a washing tower group 3.
The device still includes: a deironing and decolorizing resin tank group; the circulating output end of the finished acid intermediate tank 12 is also connected with the input end of the iron removal decolorizing resin tank group through a valve and a finished acid circulating pump; the output end of the iron removal decolorizing resin tank group is connected with a finished acid storage tank; the finished acid circulating pump is connected with the hydrochloric acid circulating pump in parallel; the iron removal decolorizing resin tank group comprises at least one iron removal decolorizing resin tank 14; the iron removal decolorizing resin tanks 14 are connected in series.
The tail gas absorption tower group 5 comprises an absorption fan 15 and at least one tail gas absorption tower 16; the tail gas absorption towers 16 are connected in series; the absorption fan 15 is connected in series between the tail gas absorption towers 16; each tail gas absorption tower 16 is provided with a circulation input end and a circulation output end; the circulation input end of the tail gas absorption tower 16 is connected with the circulation output end through a valve and a tail gas absorption circulation pump.
The tail gas neutralizing tower 6 is provided with a circulating input end and a circulating output end; the circulation input end of the tail gas neutralization tower 6 is connected with the circulation output end through a valve and a tail gas neutralization circulation pump.
The bottom discharge end of the washing tower group 3, the bottom discharge end of the finished acid intermediate tank 12, the bottom discharge end of the tail gas absorption tower group 5, the bottom discharge end of the tail gas neutralization tower 6 and the bottom discharge end of the lye tank 7 are respectively connected with a washing bottom discharge pipeline through valves.
A valve and a flowmeter are connected between the water input end of the tail gas absorption tower group 5 and the high-level water tank 8.
The above devices are connected by pipelines, and valves, flow meters, driving pumps and the like can be arranged according to needs, and the specific arrangement mode is not limited here.
The hydrogen chloride gas generated in the production process of the potassium sulfate by the Mannheim method enters a hydrochloric acid absorption system from the gas outlet at the top of the furnace through the temperature reduction of a carbon fine cooler 1. The absorption system is made of polypropylene or glass fiber reinforced plastic, and the washing tower 11, the falling film absorber, the tail gas absorption tower 16 and the tail gas neutralizing tower 6 are connected in series for use, so that the quality and the absorption efficiency of hydrochloric acid are improved; a hydrochloric acid filtering device is added in the system; the water replenishing of the system adopts an automatic water replenishing and acid discharging system. The utility model discloses a hydrogen chloride absorptivity can reach 99.5%, and exhaust emission HCL ≦ 100mg/m, and the hydrochloric acid colour is colorless transparent, and concentration HCL > 31%, SO4< 0.01%.
The washing tower 11 can adopt phi 1200mm x 10000mm and is internally provided with an acid mist removing device. The falling film absorption tower 14 can be a square meter of 80, and the tail gas absorption tower 16 can be a tower with a diameter phi of 1200mm x 10000mm and an acid mist removing device inside. The tail gas neutralizing tower 6 can adopt phi 1200mm x 10000mm and is internally provided with an acid mist removing device. The iron removal decolorizing resin tank 14 realizes hydrochloric acid filtration. The quality of the hydrochloric acid in the process can reach the quality standard of first-class products in the industrial synthetic hydrochloric acid GB320-2006 standard. The tail gas emission meets the national emission requirements, and the operation is simpler and more practical.
The terms "first," "second," "third," "fourth," and the like in the description and in the claims, as well as in the drawings, if any, are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used is interchangeable under appropriate circumstances such that the embodiments of the invention described herein are capable of operation in sequences other than those illustrated or otherwise described herein. Furthermore, the terms "comprising" and "having," as well as any variations thereof, are intended to cover non-exclusive inclusions.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (8)
1. The utility model provides a manheim method potassium sulphate by-product hydrochloric acid absorption device which characterized in that includes: a carbon cooler, a crude acid intermediate tank, a washing tower group, a falling film absorption tower group, a tail gas neutralization tower and a lye tank;
the input end of the carbon cooler is connected with the gas input end of HC 1; the output end of the carbon cooler is connected with the input end of the crude acid intermediate tank; the output end of the crude acid intermediate tank is connected with the input end of the washing tower group;
the output end of the washing tower group is connected with the input end of the falling film absorption tower group; the output end of the falling film absorption tower group is connected with the input end of the tail gas absorption tower group; the output end of the tail gas absorption tower group is connected with the input end of a tail gas neutralization tower group HC 1; the alkali liquor input end of the tail gas neutralization tower group is connected with an alkali liquor tank through an alkali liquor pump and a valve; and the output end of the tail gas neutralizing tower group is connected with a tail gas discharge chimney.
2. The apparatus for absorbing hydrochloric acid as a byproduct from potassium sulfate produced by Mannheim process according to claim 1,
the washing tower group comprises at least two washing towers; the washing towers are connected in series;
each washing tower is provided with a circulation input end and a circulation output end;
the circulation input end of the washing tower is connected with the circulation output end through a valve and a washing circulation pump.
3. The apparatus for absorbing hydrochloric acid as a byproduct of potassium sulfate produced by the Mannheim process according to claim 1 or 2, further comprising: a high-level water tank, a circulating tank and a finished acid intermediate tank;
the falling film absorption tower group comprises: a first falling film absorption tower and a second falling film absorption tower;
the first falling film absorption tower and the second falling film absorption tower are connected in series;
the bottom output end of the first falling film absorption tower is connected with the top input end of the finished acid intermediate tank;
the bottom output end of the second falling film absorption tower is connected with the top input end of the circulating groove;
the circulating output end of the finished acid intermediate tank is connected with the circulating input end of the first falling film absorption tower through a valve and a hydrochloric acid circulating pump;
the circulating output end of the circulating groove is connected with the circulating input end of the second falling film absorption tower through the falling film absorption pump;
the high-level water tank is connected with the water input end of the tail gas absorption tower group through a valve and a water injection flowmeter;
the tail gas acid output end of the tail gas absorption tower group is connected with the tail gas acid input end of the circulating tank through a valve;
the tail gas acid output end of the circulating tank is connected with the tail gas acid input end of the finished product acid intermediate tank through a valve;
the tail gas acid output end of the finished product acid intermediate tank is communicated with the crude product acid intermediate tank through a valve and a washing tower group.
4. The apparatus for absorbing hydrochloric acid as a byproduct of potassium sulfate produced by the Mannheim process as claimed in claim 3, further comprising: a deironing and decolorizing resin tank group;
the circulating output end of the finished acid intermediate tank is also connected with the input end of the iron removal decolorizing resin tank group through a valve and a finished acid circulating pump;
the output end of the iron removal decolorizing resin tank group is connected with a finished acid storage tank;
the finished acid circulating pump is connected with the hydrochloric acid circulating pump in parallel;
the iron removal decolorizing resin tank group comprises at least one iron removal decolorizing resin tank;
the iron removal decoloration resin tanks are connected in series.
5. The apparatus for absorbing hydrochloric acid as a byproduct of potassium sulfate produced by Mannheim process according to claim 1 or 2,
the tail gas absorption tower group comprises an absorption fan and at least one tail gas absorption tower;
the tail gas absorption towers are connected in series; the absorption fan is connected in series between the tail gas absorption towers;
each tail gas absorption tower is provided with a circulation input end and a circulation output end;
the circulation input end of the tail gas absorption tower is connected with the circulation output end through a valve and a tail gas absorption circulating pump.
6. The apparatus for absorbing hydrochloric acid as a byproduct of potassium sulfate produced by Mannheim process according to claim 1 or 2,
the tail gas neutralizing tower is provided with a circulating input end and a circulating output end;
the circulating input end of the tail gas neutralizing tower is connected with the circulating output end through a valve and a tail gas neutralizing circulating pump.
7. The apparatus for absorbing hydrochloric acid as a byproduct of potassium sulfate produced by Mannheim process according to claim 3,
the bottom discharge end of the washing tower group, the bottom discharge end of the finished acid intermediate tank, the bottom discharge end of the tail gas absorption tower group, the bottom discharge end of the tail gas neutralization tower and the bottom discharge end of the lye tank are respectively connected with a washing bottom discharge pipeline through valves.
8. The apparatus for absorbing hydrochloric acid as a byproduct of potassium sulfate produced by Mannheim process according to claim 1 or 2,
and a valve and a flowmeter are connected between the water input end of the tail gas absorption tower group and the high-level water tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920614176.4U CN210366982U (en) | 2019-04-29 | 2019-04-29 | Absorption device for potassium sulfate byproduct hydrochloric acid by Mannheim method |
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| CN201920614176.4U CN210366982U (en) | 2019-04-29 | 2019-04-29 | Absorption device for potassium sulfate byproduct hydrochloric acid by Mannheim method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113213426A (en) * | 2021-03-03 | 2021-08-06 | 眉山友禾科技有限公司 | Preparation process of high-concentration hydrochloric acid |
| CN113620249A (en) * | 2021-08-04 | 2021-11-09 | 河北卓泰肥业有限公司 | Method and production system for producing reagent hydrochloric acid by using Mannheim furnace tail gas |
| CN114768478A (en) * | 2022-04-25 | 2022-07-22 | 南通星球石墨股份有限公司 | High-purity hydrochloric acid preparation system |
-
2019
- 2019-04-29 CN CN201920614176.4U patent/CN210366982U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113213426A (en) * | 2021-03-03 | 2021-08-06 | 眉山友禾科技有限公司 | Preparation process of high-concentration hydrochloric acid |
| CN113620249A (en) * | 2021-08-04 | 2021-11-09 | 河北卓泰肥业有限公司 | Method and production system for producing reagent hydrochloric acid by using Mannheim furnace tail gas |
| CN114768478A (en) * | 2022-04-25 | 2022-07-22 | 南通星球石墨股份有限公司 | High-purity hydrochloric acid preparation system |
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