CN210159455U - Material taking unit based on calcium circulation desulfurization system of cement clinker production line - Google Patents
Material taking unit based on calcium circulation desulfurization system of cement clinker production line Download PDFInfo
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- CN210159455U CN210159455U CN201920858646.1U CN201920858646U CN210159455U CN 210159455 U CN210159455 U CN 210159455U CN 201920858646 U CN201920858646 U CN 201920858646U CN 210159455 U CN210159455 U CN 210159455U
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Abstract
The utility model discloses a material taking unit based on a cement clinker production line calcium circulation desulfurization system, which belongs to the technical field of flue gas desulfurization, wherein the material taking unit is arranged between a decomposition unit for decomposing raw materials into active hot raw materials and a desulfurizer preparation unit for preparing the active hot raw materials into a desulfurizer, and the active hot raw materials extracted from the decomposition unit are sent into the desulfurizer preparation unit; one end of the material taking unit is connected with a cyclone discharge pipe of a last-stage kiln tail preheater of the decomposing unit or an outlet air pipe of the decomposing furnace, and the other end of the material taking unit is connected with a material inlet of a cooling unit of the desulfurizer preparation unit. The utility model discloses get the material volume of getting of material unit and can freely control according to the demand, it is easy and simple to handle, calorific loss is little, and is little to the influence of system's energy consumption.
Description
Technical Field
The utility model relates to a flue gas desulfurization technical field especially relates to get material unit based on cement clinker production line calcium circulation desulfurization system.
Background
The cement raw materials mainly comprise calcium raw materials, silicon-aluminum raw materials, iron raw materials and the like, wherein the calcium raw materials are mainly used and generally account for about 80 percent. In the production process of cement clinker, when the raw material contains more low-valence sulfur such as organic sulfur or sulfide, the low-valence sulfur is released to generate SO by high-temperature oxidation in the preheater2Gas, resulting in SO in the flue gas2The concentration exceeds the standard, and the environmental-friendly emission index can be reached only by carrying out desulfurization treatment.
The existing cement kiln flue gas desulfurization methods mainly comprise dry desulfurization, wet desulfurization and the like, and the desulfurizing agent is mainly purchased from the outside. The desulfurizer adopted by dry desulfurization is calcium hydroxide or sodium bicarbonate and the like, and is fed to the positions of an air duct of a preheater at the tail of a kiln and the like, and the desulfurizer reacts with sulfur dioxide in flue gas to perform desulfurization, but the desulfurization efficiency is often lower, and the method is not suitable for cement production lines with high sulfur dioxide background concentration.
The cement kiln flue gas can also adopt a wet desulphurization process, wherein the most common wet desulphurization method is a lime/gypsum method, namely limestone is adopted as a desulfurizer, the limestone is mixed with water to prepare slurry, the slurry is sprayed into a desulphurization tower, and the lime slurry absorbs sulfur dioxide in the flue gas to react to generate gypsum. Wet desulfurization has the problems of white smoke, gypsum rain, chimney corrosion and the like, and has large water consumption, the wastewater needs to be treated, and the whole treatment cost is higher.
Compared with wet desulphurization, the semi-dry flue gas desulphurization technology has the advantages of clean smoke trace, no white smoke, no gypsum rain, low water consumption and no wasteWater treatment, little corrosion to the chimney and the like, and is the development direction of the flue gas desulfurization technology at home and abroad. The existing semi-dry desulfurization technology needs an external desulfurizer (quicklime or hydrated lime), the cost of the desulfurizer is high, the desulfurized slag is difficult to dispose, and the technology has no engineering application in the cement industry. The technical principle of the semi-dry desulfurization method is as follows: SO in flue gas2And the desulfurizing agent and water in the circulating fluidized bed desulfurizing tower are subjected to ionic chemical reaction to generate desulfurization products such as calcium sulfite and the like. The desulfurizer is highly enriched under the external circulation system of the dust collector to realize SO in the flue gas2The removal is efficient.
The main reaction formula is as follows:
CaO+H2O→Ca(OH)2
Ca(OH)2+SO2→CaSO3·1/2H2O+1/2H2O
in conclusion, the existing dry desulfurization, wet desulfurization and semi-dry desulfurization all need to purchase an external quick lime or slaked lime desulfurizer, self-sufficiency of a desulfurization machine cannot be realized, and the main component of the raw material calcined by the decomposing furnace is calcium oxide, so that the raw material has high activity, and the active raw material can be used for preparing the active desulfurizer to replace the external quick lime or slaked lime desulfurizer, so that the aims of saving resources and reducing the production cost are fulfilled. However, before the active raw materials are used for preparing the active desulfurizer, the active raw materials need to be taken out, so that the material taking unit based on the calcium cycle desulfurization system of the cement clinker production line is provided, and the method has important significance for popularization and application of the high-efficiency and low-cost desulfurization technology of the cement kiln flue gas.
Disclosure of Invention
An object of the utility model is to provide a get material unit based on cement clinker production line calcium cycle desulfurization system, the volume of getting of this material unit of getting can be according to demand free control, and is easy and simple to handle, and calorific loss is little, and is little to the influence of system's energy consumption.
The utility model discloses a realize like this, a get material unit based on cement clinker production line calcium circulation desulfurization system, get material unit setting be used for with the raw material decompose make active hot raw material decompose with be used for with the active hot raw material make desulfurizer preparation unit between, and will follow the active hot raw material of extraction in the decomposition unit and send into desulfurizer preparation unit; one end of the material taking unit is connected with a cyclone discharge pipe of a last-stage kiln tail preheater of the decomposing unit or an outlet air pipe of the decomposing furnace, and the other end of the material taking unit is connected with a material inlet of a cooling unit of the desulfurizer preparation unit.
In the above technical scheme, preferably, the material taking unit comprises a material dividing pipe, a high-temperature gate valve I and a high-temperature rotary discharger, the high-temperature gate valve I and the high-temperature rotary discharger are arranged on the material dividing pipe, one end of the material dividing pipe is connected with a cyclone discharge pipe of the last-stage kiln tail preheater, and the other end of the material dividing pipe is connected with a cooling unit material inlet of the desulfurizer preparation unit.
In the above technical solution, preferably, the material taking unit includes a material taking cyclone, a high temperature gate valve ii is arranged on an inlet pipeline of the material taking cyclone, and a high temperature gate valve iii is arranged on an outlet air pipe of the material taking cyclone; the inlet pipeline of the material taking cyclone is connected with an outlet air pipe of the decomposing furnace, the outlet air pipe of the material taking cyclone is connected with an outlet air pipe of a last-stage or penultimate-stage kiln tail preheater, and the discharging pipe of the material taking cyclone is connected with a material inlet of a cooling unit of the desulfurizer preparation unit.
The utility model has the advantages of it is following and beneficial effect:
by adopting the technical scheme, the material taking amount can be freely controlled according to requirements when the material taking unit takes materials, the operation is simple, the heat loss of the system is small when the materials are taken, and the influence on the energy consumption of the system is small; the high-activity desulfurizer is prepared by taking materials through the material taking unit, so that self-sufficiency of the desulfurizer can be realized, and the production of a normal production line is not influenced; the utility model relates to a rationally, manufacturing cost and running cost are low, convenient operation.
Drawings
Fig. 1 is a flow chart of the material taking from the cyclone tube feeding pipe of the final-stage kiln tail preheater according to the first embodiment of the present invention;
FIG. 2 is a first flow chart for taking materials from an outlet air duct of a decomposing furnace according to a second embodiment of the present invention;
fig. 3 is a second flow chart of material taking from an outlet air duct of a decomposing furnace according to a second embodiment of the present invention.
In the figure: 101-a decomposing furnace; 102-cyclone of last stage kiln tail preheater; 103-a cyclone of a penultimate kiln tail preheater; 104-cyclone of last but one stage kiln tail preheater;
201-first stage cyclone cylinder; 202-second stage cyclone; 203-a fan; 204-an exhaust gas treatment system; 205-a distributing valve; 206-aggregate bin; 207-gate valve; 208-a screw feeder with a meter;
30-a digestion unit;
401-material separating pipe; 402-high temperature gate valve one; 403-high temperature rotary discharger; 404-a take off cyclone; 405-a high-temperature gate valve II; 406-high temperature gate valve three;
50-a rotary kiln;
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention will be further described in detail with reference to the following embodiments and accompanying drawings. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "connected" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
Referring to fig. 1, an embodiment of the present invention provides a material taking unit of a calcium cycle desulfurization system for a cement clinker production line, wherein the material taking unit is disposed between a decomposition unit for decomposing raw materials into active hot raw materials and a desulfurizer preparation unit for preparing the active hot raw materials into a desulfurizer, and feeds the active hot raw materials extracted from the decomposition unit into the desulfurizer preparation unit; one end of the material taking unit is connected with a discharge pipe of a cyclone 102 of a last-stage kiln tail preheater of the decomposing unit, and the other end of the material taking unit is connected with a material inlet of a cooling unit of the desulfurizer preparation unit.
After the raw meal is calcined in the decomposing furnace 101, calcium carbonate in the raw meal is decomposed at high temperature into calcium oxide, and the high-temperature calcined raw meal is referred to as active raw meal. The active raw materials enter the cyclone 102 of the last-stage kiln tail preheater along with the flue gas, gas-solid separation is carried out through the cyclone 102 of the last-stage kiln tail preheater, most of the active raw materials are collected, and a small part of the active raw materials exit the cyclone 102 of the last-stage kiln tail preheater along with the flue gas and enter the last-stage kiln tail preheater. A portion of the active raw meal collected by the cyclone 102 of the final kiln tail preheater is passed through the take off unit to a cooling unit for cooling and another portion is returned to the rotary kiln 50. Active raw materials subjected to gas-solid separation by the cyclone 102 of the last-stage kiln tail preheater are easier to collect, and the material taking unit is convenient to take materials.
The material taking unit comprises a material distributing pipe 401, a high-temperature gate valve I402 and a high-temperature rotary discharger 403, wherein the high-temperature gate valve I402 and the high-temperature rotary discharger 403 are arranged on the material distributing pipe, one end of the material distributing pipe 401 is connected with a material discharging pipe of a cyclone cylinder 102 of a last-stage kiln tail preheater, and the other end of the material distributing pipe is connected with a material inlet of a cooling unit of the desulfurizer preparation. When the material needs to be taken, the high-temperature gate valve I402 is opened, and the amount of the high-temperature active raw material taken out from the discharge pipe of the cyclone 102 of the last-stage kiln tail preheater can be regulated and controlled by controlling the rotating speed of the high-temperature rotary discharger 403. The material taking amount can be freely controlled according to the requirement, and the operation is simple and convenient.
Example 2
Referring to fig. 2 and 3, an embodiment of the present invention provides a material taking unit of a calcium cycle desulfurization system based on a cement clinker production line, wherein the material taking unit is disposed between a decomposition unit for decomposing raw materials into active hot raw materials and a desulfurizer preparation unit for preparing the active hot raw materials into a desulfurizer, and the active hot raw materials extracted from the decomposition unit are sent to the desulfurizer preparation unit; one end of the material taking unit is connected with an outlet air pipe of a decomposing furnace 101 of the decomposing unit, and the other end of the material taking unit is connected with a material inlet of a cooling unit of the desulfurizer preparation unit.
After the raw meal is calcined in the decomposing furnace 101, calcium carbonate in the raw meal is decomposed at high temperature into calcium oxide, and the high-temperature calcined raw meal is referred to as active raw meal. The active raw material out of the decomposing furnace enters the cyclone 102 of the last-stage kiln tail preheater along with most of the flue gas, and the rest enters the cooling unit for cooling through the material taking unit.
The material taking unit comprises a material taking cyclone barrel 404, a high-temperature gate valve II 405 is arranged on an inlet pipeline of the material taking cyclone barrel 404, and a high-temperature gate valve III 406 is arranged on an outlet air pipe of the material taking cyclone barrel 404; an inlet pipeline of the material taking cyclone cylinder 404 is connected with an outlet air pipe of the decomposing furnace 101, an outlet air pipe of the material taking cyclone cylinder 404 is connected with an outlet air pipe of a last-stage or penultimate kiln tail preheater, and a discharging pipe of the material taking cyclone cylinder 404 is connected with a cooling unit feeding port of a desulfurizer preparation unit.
When material is required to be taken, the material amount entering the material taking cyclone barrel 404 is adjusted through the opening degrees of the high-temperature gate valve II 405 and the high-temperature gate valve III 406. The material taking amount can be freely controlled according to the requirement, and the operation is simple and convenient. Under the separating action of the material taking cyclone cylinder 404, the air out of the material taking cyclone cylinder 404 enters the inlet air pipe of the penultimate kiln tail preheater cyclone cylinder 103 or the penultimate kiln tail preheater cyclone cylinder 104, the high-temperature air returns to the heat exchange pipeline of the kiln tail preheater, most heat is recovered, the influence on the energy consumption of the system is small, and the material out of the material taking cyclone cylinder 404 enters the cooling unit. FIG. 2 shows the entry of air out of the extraction cyclone 404 into the penultimate kiln tail preheater cyclone 103, and FIG. 3 shows the entry of air out of the extraction cyclone 404 into the penultimate kiln tail preheater cyclone 104.
It should be noted that the decomposing unit of the present invention includes a multi-stage kiln tail preheater and a decomposing furnace 101, wherein the kiln tail preheater is a three-to seven-stage kiln tail preheater, preferably a five-stage preheater; the desulfurizer preparation unit utilizes partial hot raw materials decomposed by the decomposition unit to prepare desulfurizer through cooling and digestion, and comprises a cooling unit connected with a discharge port of the decomposition unit and a digestion unit 30 connected with a discharge port of the cooling unit; the raw materials are decomposed at high temperature by a decomposition unit to obtain active raw materials, the collected active raw materials are cooled by a cooling unit to be cooled to be within 150 ℃ from 800-950 ℃, and the cooled active raw materials are digested by a digestion unit 30 to be prepared into a desulfurizer to absorb sulfur dioxide generated in the production process of cement kiln clinker.
The cooling unit comprises a first-stage cyclone 201 and a second-stage cyclone 202, an outlet air pipe of the first-stage cyclone is connected with an inlet of the second-stage cyclone 202, a blanking pipe of the second-stage cyclone 202 is connected with the inlet of the first-stage cyclone 201, cooling air is introduced into the inlet of the first-stage cyclone 201, and an outlet air pipe of the second-stage cyclone 202 is connected with an exhaust gas treatment system 204 through a fan 203. The high-temperature active raw material taken out firstly enters an outlet air pipe of the first-stage cyclone 201 (namely, the other end of the material separating pipe 401 or a blanking pipe of the material taking cyclone 404 is connected with the outlet air pipe of the first-stage cyclone 201), and then enters the second-stage cyclone 202, under the separation action of the second-stage cyclone 202, most of the active raw material is collected, and the second-stage cyclone 202 preferably adopts a cyclone with the separation efficiency of more than 90%. The temperature of the active raw material collected from the second-stage cyclone 202 is 300-600 ℃, the active raw material is mixed with cooling air and enters the first-stage cyclone 201, the first-stage cyclone preferably adopts a cyclone with the separation efficiency of more than 80%, and the temperature of the active raw material separated by the first-stage cyclone 201 is reduced to below 150 ℃. Under the induced air of the fan 203, the cooling air firstly passes through the first-stage cyclone 201 from bottom to top and then passes through the second-stage cyclone 202, the dust-containing air which is discharged from the second-stage cyclone 202 enters the cement kiln flue gas and waste gas treatment system 204 after passing through the fan 203, and the waste gas treatment system 204 adopts the existing waste gas treatment device, such as a bag-type dust collector. The high-temperature active raw material can be cooled to below 150 ℃ after being subjected to two-stage suspension cooling, the feasibility of a scheme for directly taking the high-temperature active raw material is realized, and the cooling efficiency is high.
Referring to embodiment 1, referring to fig. 1, the feeding pipe of the second stage cyclone 202 is further connected to a material distribution pipe located at the upper part of the high temperature gate valve 402, and the feeding pipe of the second stage cyclone 202 is provided with a material distribution valve 205 at a branch. The temperature of the active raw materials collected from the second-stage cyclone 202 is 300-600 ℃, the active raw materials are divided into two parts through the material dividing valve 205, one part of the active raw materials is mixed with the high-temperature active raw materials with the temperature of 800-950 ℃ in the material taking pipe 401, the temperature of the high-temperature active raw materials is reduced, the temperature of the mixed materials entering the rotary discharger 403 is lower than 700 ℃, and therefore the requirement on high-temperature resistant materials of the rotary discharger 403 is reduced. Mixing a part of the active raw material from the second stage cyclone 202 with the high temperature active raw material just taken out can reduce the temperature of the mixed material to be more than 700 ℃, thereby protecting the high temperature material rotary discharger.
The feed opening of the first-stage cyclone 201 is connected with a material collecting bin 206, the discharge opening of the material collecting bin 206 is provided with a gate valve 207 and a screw feeder 208 with a meter, and the outlet of the screw feeder 208 with the meter is connected with the digestion unit 30. The cooled active raw materials are firstly fed into a material collecting bin 206 before digestion and synergism, and are fed into the digestion unit 30 after being measured by a screw feeder 208 with a meter, and the storage period of the material collecting bin 206 is less than 24 hours so as to avoid raw material hardening. The feeding speed and the feeding amount are controlled by the spiral feeder with the meter, and the operation is convenient.
The digestion mode of the digestion unit 30 is dry digestion. In practice, the digestion unit 30 may be implemented as an existing dry digester. By spraying water into the digestion unit 30, the calcium oxide in the material reacts with water to generate active calcium hydroxide, and the material exiting the digestion unit 30 is an active desulfurizer. The independent dry digester is adopted, so that the digestibility of calcium oxide can reach over 90 percent, and the activity of the prepared desulfurizer is higher.
The exhaust port of the digestion unit 30 is connected with a cement kiln flue gas and waste gas treatment system 204 through an air pipe of the cooling unit. In specific implementation, the exhaust port of the digestion unit 30 may be connected to the outlet air duct of the first stage cyclone 201 of the cooling unit through an exhaust duct, or may be connected to the outlet air duct of the second stage cyclone 202 of the cooling unit, and further connected to the flue gas and exhaust gas treatment system 204 of the cement kiln. The dusty water vapor out of the digestion unit 30 enters the two-stage suspension cooling unit through the exhaust pipeline and finally enters the waste gas treatment system 204, the waste gas treatment system 204 is used for purifying the dusty water vapor, the atmospheric pollution is avoided, a dusty water vapor purification treatment device does not need to be arranged independently, and the investment and the operation cost are saved.
Claims (3)
1. The material taking unit is arranged between a decomposition unit for decomposing raw materials into active hot raw materials and a desulfurizer preparation unit for preparing the active hot raw materials into a desulfurizer, and the active hot raw materials extracted from the decomposition unit are sent to the desulfurizer preparation unit; one end of the material taking unit is connected with a discharge pipe of a cyclone (102) of a last-stage kiln tail preheater of the decomposing unit or an outlet air pipe of the decomposing furnace (101), and the other end of the material taking unit is connected with a material inlet of a cooling unit of the desulfurizer preparation unit.
2. The material taking unit based on the calcium cycle desulfurization system of the cement clinker production line as recited in claim 1, wherein the material taking unit comprises a material dividing pipe (401), a high temperature gate valve I (402) and a high temperature rotary discharger (403), the material dividing pipe (401) is connected with a material discharging pipe of a cyclone (102) of a last stage kiln tail preheater at one end, and is connected with a material feeding port of a cooling unit of a desulfurizer preparation unit at the other end.
3. The taking unit of the calcium cycle desulfurization system of the cement clinker production line as recited in claim 1, wherein the taking unit comprises a taking cyclone (404), a high temperature gate valve II (405) is arranged on an inlet pipeline of the taking cyclone (404), and a high temperature gate valve III (406) is arranged on an outlet air pipe of the taking cyclone (404); an inlet pipeline of the material taking cyclone (404) is connected with an outlet air pipe of the decomposing furnace (101), an outlet air pipe of the material taking cyclone (404) is connected with an outlet air pipe of a last-stage or penultimate kiln tail preheater, and a discharging pipe of the material taking cyclone (404) is connected with a cooling unit feeding port of a desulfurizer preparation unit.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115121109A (en) * | 2022-07-20 | 2022-09-30 | 天津水泥工业设计研究院有限公司 | Low NO X System and process for denitration of flue gas and auxiliary desulfurization treatment of escaping ammonia |
| CN115121109B (en) * | 2022-07-20 | 2024-04-30 | 天津水泥工业设计研究院有限公司 | Low NOXSystem and process for flue gas denitration and auxiliary desulfurization treatment of escaped ammonia |
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2019
- 2019-06-06 CN CN201920858646.1U patent/CN210159455U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115121109A (en) * | 2022-07-20 | 2022-09-30 | 天津水泥工业设计研究院有限公司 | Low NO X System and process for denitration of flue gas and auxiliary desulfurization treatment of escaping ammonia |
| CN115121109B (en) * | 2022-07-20 | 2024-04-30 | 天津水泥工业设计研究院有限公司 | Low NOXSystem and process for flue gas denitration and auxiliary desulfurization treatment of escaped ammonia |
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