WO2018192267A1 - 一种全回收co2的石灰窑装置 - Google Patents

一种全回收co2的石灰窑装置 Download PDF

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Publication number
WO2018192267A1
WO2018192267A1 PCT/CN2018/000062 CN2018000062W WO2018192267A1 WO 2018192267 A1 WO2018192267 A1 WO 2018192267A1 CN 2018000062 W CN2018000062 W CN 2018000062W WO 2018192267 A1 WO2018192267 A1 WO 2018192267A1
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WIPO (PCT)
Prior art keywords
kiln
air
section
kiln body
lime
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PCT/CN2018/000062
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English (en)
French (fr)
Inventor
王长春
张紫毫
汪小龙
敖文青
姜曦
贾冰
Original Assignee
王长春
梁晶晶
张紫毫
汪小龙
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Application filed by 王长春, 梁晶晶, 张紫毫, 汪小龙 filed Critical 王长春
Priority to UAA201911190A priority Critical patent/UA124401C2/uk
Publication of WO2018192267A1 publication Critical patent/WO2018192267A1/zh
Priority to US16/595,514 priority patent/US20200048146A1/en

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B1/00—Shaft or like vertical or substantially vertical furnaces
    • F27B1/10—Details, accessories or equipment specially adapted for furnaces of these types
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B2/00—Lime, magnesia or dolomite
    • C04B2/10—Preheating, burning calcining or cooling
    • C04B2/12—Preheating, burning calcining or cooling in shaft or vertical furnaces
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1418—Recovery of products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B1/00—Shaft or like vertical or substantially vertical furnaces
    • F27B1/02—Shaft or like vertical or substantially vertical furnaces with two or more shafts or chambers, e.g. multi-storey
    • F27B1/04—Combinations or arrangements of shafts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B19/00—Combinations of different kinds of furnaces that are not all covered by any single one of main groups F27B1/00 - F27B17/00
    • F27B19/04—Combinations of different kinds of furnaces that are not all covered by any single one of main groups F27B1/00 - F27B17/00 arranged for associated working
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills

Definitions

  • the present invention relates to a lime kiln using a gas as a fuel and a process for producing lime using the lime kiln.
  • Lime, calcium oxide (CaO), is widely used in the steel industry, calcium carbide industry, alumina industry, refractory industry, etc. It is also one of the necessary raw materials for these large-scale industrial fields. For example, in the metallurgical industry, each ton is produced. The steel needs 70 kg of lime.
  • the main raw material for making lime is limestone.
  • the main component of limestone is calcium carbonate (CaCO 3 ).
  • the basic principle of burning lime is to decompose calcium carbonate in limestone into calcium oxide and carbon dioxide by means of high temperature.
  • the lime preparation process is mainly divided into preheating, calcination, cooling and unloading.
  • the process based on the existing lime preparation technology is: charging limestone and solid fuel into the lime kiln, or feeding the gaseous fuel into the kiln through the pipeline and the burner while the limestone is loaded into the lime kiln; the limestone is preheated Decomposition starts at 800 ° C ⁇ 850 ° C, and calcination is completed at 1200 ° C; the produced lime is cooled and discharged out of the kiln to complete the production of the quicklime product.
  • the existing lime production process more than 1 ton of CO 2 emissions are produced for every ton of lime produced.
  • CO 2 plays an important role in various sectors of the national economy such as food, sanitation, petrochemical, nuclear industry, and fire protection, it is also widely used in the metallurgical industry.
  • fuel is burning.
  • the volume concentration of CO 2 in the flue gas is about 10-15%, and the cost of recovering CO 2 is very high.
  • the company generally discharges the flue gas containing a large amount of CO 2 directly into the atmosphere, causing environmental pollution.
  • the existing lime kiln is divided into fuels: mixed kiln (mainly burning solid fuel, including coke, coke powder, coal, etc.) and gas kiln (that is, mainly burning gas fuel, such as blast furnace gas, coke oven gas , converter gas, calcium carbide tail gas, generator gas, natural gas, etc.), of which gas kiln is more widely used; according to kiln shape: there are shaft kiln, rotary kiln, sleeve kiln, parallel flow regenerative double kiln shaft kiln ( The Maerz kiln, also known as the Myers kiln), the Fukas kiln (Italy), etc., which are widely used are the annular sleeve shaft kiln and the Maerz kiln: according to the operation mode: there is a negative pressure operation kiln ( Such as annular sleeve shaft kiln) and positive pressure operation kiln (such as co
  • the existing lime kiln technology especially the characteristics of various gas kiln, all need to be equipped with a burner system.
  • the burner system of the gas kiln generally consists of a plurality of rows and groups of burners, and is equipped with a gas fuel pipeline and Combustion air ducts, nozzles, etc.
  • annular sleeve shaft kiln and a parallel-flow regenerative kiln (Mertz kiln).
  • the annular sleeve shaft kiln system includes: 1-furnace body, 1a-cooling air, 2-feed system, 3-1-upper sleeve, 3-2-heat exchanger, 3-3 Inner sleeve, 4-exhaust gas exhaust system, 4a-all exhaust gas, 5-burner, 5a-gas + burner air, 6-discharge system; furnace body 1 has: 1-1-pre-tropical, 1- 2-calcined belt, 1-3-cooling belt.
  • the limestone is heated to its calcination temperature.
  • the heat of the pre-tropical zone 1-1 comes from the waste flue gas of the calcination zone 1-2, and a part of the waste flue gas generated by the calcination zone 1-2 enters the pre-tropical zone 1-1, and then enters from the upper part of the pre-tropical zone 1-1.
  • Exhaust system 4 another part of the exhaust gas (with excess heat) enters the heat exchanger 3-2 through the upper inner sleeve 3-1 for heating the combustion air, and the heated combustion air is sent to the burner 5 through the pipeline for replacement The exhausted heat is then discharged through the exhaust system 4.
  • the calcination process is carried out in the calcination zone 1-2, the gas and the combustion air are mixed and combusted in the burner 5, and the limestone is calcined in the calcination zone 1-2, and a part of the waste flue gas 4a after calcination is upward in the pre-tropical zone 1-1
  • the mineral material is preheated, and the finished lime product enters the cooling zone 1-3 at the bottom of the calcining zone 1-2.
  • the hot lime exchanges heat with the cold air 1a sucked in at the bottom of the kiln, and after the temperature is lowered, the kiln body is discharged through the discharge system 6.
  • the cooling air 1a enters the kiln from the lower portion of the cooling belt 1-3, and is mixed with a part of the waste flue gas of the burner 5 in the lower inner sleeve 3-3 to become high-temperature waste air, and is discharged from the upper portion of the lower inner sleeve 3-3 into the burner. 5 participate in the burning.
  • the main technical advantages of the sleeve kiln include: high thermal efficiency, large size range of raw materials into the kiln, small footprint, negative pressure calcination, safe and stable operation.
  • the technical features of this furnace type also include a boundary zone between the calcining section and the cooling section with a negative pressure operating zone and a positive pressure operating zone. Wherein, the co-current flue gas is extracted from the kiln body in this boundary zone, part of the waste flue gas enters the heat exchanger through the inner sleeve, and the other part is preheated from the mineral material and is taken out from the upper part of the kiln body.
  • a negative pressure operating zone is formed above the boundary zone.
  • the cooling air taken in from the bottom of the kiln is extracted from the upper portion of the cooling section, so that a positive pressure operating zone is formed in the lower portion of the boundary zone.
  • the CO 2 generated by calcination in the kiln is discharged through the exhaust system 4, and since the air is mixed therein, the cost of recovering CO 2 is high; the heat of the pre-tropical zone 1-1 and the calcination zone 1-2 are both derived from the gaseous fuel.
  • the high-temperature flue gas formed by the combustion of the combustion air in the combustor 5 is mixed, and all the burners are arranged on the kiln body 1 in two belts, and the raw materials are heated by direct combustion, so that the heat cannot be evenly distributed.
  • the entire calcination reaction time is long, which increases the size of the kiln while greatly limiting the productivity.
  • the parallel flow regenerative kiln (Mertz kiln) is also one of the most widely used kiln types.
  • lime shaft kiln There are currently two forms of lime shaft kiln, namely single-dump counter-flow and multi-column co-current lime kiln (generally double kiln).
  • the standard cocurrent regenerative lime kiln is a double-dip lime kiln that is switched between the combustion kiln and the non-combustion kiln. It adopts the structure of a ring-shaped double cymbal, which is connected by a channel at regular intervals. Rotate once for calcination.
  • the combustion gas flows from the combustion kiln through the passage into the non-combustion kiln, preheating the raw limestone, and the preheating zone functions as a heat exchanger.
  • the co-current regenerative kiln has the advantages of high thermal efficiency, low energy consumption, high quality of lime products, etc., but because of a set of reversing systems, the equipment is complicated and the investment is large. Similarly, the productivity of the co-current regenerative kiln technology has not increased significantly, and the cost of recovering CO 2 is high.
  • the working principle of the double-flow lime shaft kiln of the parallel flow regenerative kiln is shown in Figure 2. These include: 7-combustion crucible, 7-1-combustion wind, 7-2-calcination zone, 7-3 cooling zone, 8-exhaust crucible, 8-1-pre-tropical zone, 8-2 exhaust gas, 9-channel , 8-3 cooling belt, 10-cooling wind.
  • a beam type heat storage lime kiln (CN 203007146 U), as shown in Figure 3, which includes:
  • 1c-feed system 2c-upper suction beam, 3c-pre-tropical, 6c-kiln body, 7c-lower suction beam, 8c-cooling belt, 9c-outlet, 10c- cyclone, 11c- Bag filter, 12c-leader, 13c- 2nd valve, 14c-2 regenerator, 15c-burner, 16c- 4th valve, 17c-first valve, 18c-three-way valve, 19c-1 Heat accumulator, 20c - 3rd valve, 21c - combustion air, 22c - fuel, 23c - exhaust system.
  • the technology is to remove and purify the hot exhaust gas extracted from the upper part of the cooling section of the kiln body, and then enter the preheater as combustion air.
  • the combustion air preheater is composed of two regenerative heat exchangers, and two regenerative heat exchangers are used.
  • the heaters alternately heat the combustion air to continuously provide hot combustion air to the kiln burner, which is placed on the combustion beam of the kiln.
  • the regenerative heat exchanger uses low calorific value gas as fuel, and the main structure includes a burner and a regenerator; the kiln burner can also use low calorific value gas due to the use of preheated combustion air.
  • This technology is characterized by the use of a regenerative heat exchanger to preheat the combustion-supporting gas, which increases the temperature of the combustion air, so that the kiln burner can use a low calorific value gas.
  • this technology only solves the problem of using low calorific value gas to reduce operating costs, it does not involve other common technical problems of gas-fired lime kiln, so the application is limited.
  • an air heat storage lime kiln (CN 203144298 U)
  • a “regenerative burner” is designed on the kiln burner to utilize this The burner of the hot material preheats the combustion air for the purpose of utilizing low calorific value gas during combustion.
  • this technology does not address the common technical problems of other gas-fired lime kilns.
  • a lime kiln technology close to the present invention is "a CO 2 enriched cocurrent regenerative lime kiln production process" (CN 105000811 A), as shown in Figure 4.
  • the main feature of this technology is that it uses a parallel-flow regenerative double kiln form with 95% oxygen as a combustion-supporting gas and a solid pulverized coal injected into the calcined kiln.
  • the solid coal powder is transported by CO 2 gas.
  • the cooling section in the lower part of the kiln is cooled by CO 2 gas, and the calcined flue gas is mixed with the high-temperature cooling gas in the upper part of the cooling section, and then enters the regenerative kiln through the passage of the double kiln for the mineral material.
  • Preheating according to a certain time, the calcining kiln and the preheating kiln are rotated through the reversing device.
  • This technology uses solid fuel-pulverized coal as fuel. Although 95% oxygen is used as the combustion-supporting gas and the excess coefficient is 1.1-1.4, a certain amount of fuel dust will still be mixed in the lime product, which will contaminate the finished product. The quality of the finished product is lowered. Further, according to the technical description, "the high temperature CaO having a temperature of 1000 ° C to 1150 ° C is cooled to 80 ° C to 100 ° C using CO 2 as a cooling gas.” Although the technology lists three examples of 450 tons, 500 tons, and 550 tons per day in the technical description, the inventors still question the feasibility of using CO 2 as a cooling gas.
  • the present invention provides a lime kiln apparatus for fully recovering CO 2 and a process for producing industrial lime using the apparatus.
  • a fully recovered CO 2 lime kiln device comprises a kiln body and a heating furnace group, characterized in that: the kiln body does not have a burner, and the heating furnace group heats the CO 2 to a set temperature to form a CO 2 hot air and sends it to the kiln body.
  • the preheated mineral aggregate of calcined, hot CO 2 and CO 2 produced when mixing the calcined mineral aggregate, up to the upper portion of the mineral aggregate kiln is preheated and is withdrawn at the upper kiln body portion was collected after treatment
  • the CO 2 enters the heating furnace group again, and is heated to the set temperature and then returned to the kiln body.
  • the calcined limestone product is cooled by air and discharged from the bottom of the kiln body.
  • the kiln body comprises a feeding mechanism and a discharging mechanism.
  • the working area of the kiln body comprises a preheating section, a calcining section and a cooling section from top to bottom, and an inner sleeve is arranged in the kiln body, and the inner wall of the kiln and the outer wall of the inner sleeve A material passage is formed between the materials, the total width of the material passage section is a diameter, and the diameters of the material passages in the preheating section, the calcining section and the cooling section are different, and the mineral material enters the kiln body from the loading mechanism, along the material The passage passes from the preheating section to the calcination section, the finished product passes through the cooling section along the material passage, and finally the kiln body is discharged from the discharge mechanism.
  • the side wall of the kiln calcination section is provided with a CO 2 hot air inlet, and the inner sleeve is disposed at the upper part of the cooling section.
  • the cooling air enters the material passage between the kiln body and the inner sleeve from the lower part of the kiln body, and after the limestone product is cooled, it enters the inner sleeve from the air inlet and is extracted from the top.
  • the material passage has a transition section between the calcination section and the cooling section, the passage diameter of the transition section is reduced, and the moving speed of the material along the material passage in the transition section is faster, forming a material seal layer.
  • the material passage in which the material inside the kiln body moves is preferably in the lower part of the preheating section, the middle diameter of the calcining section is larger, and the diameter of the lower part of the calcining section is decreased. After the transition section, the diameter of the cooling section is larger and larger. .
  • the preferred range of the ratio of the maximum diameter of the material passage of the kiln body to the minimum diameter of the lower portion of the calcination section is 2 to 3.5, and the maximum passage diameter and transition section of the material passage of the kiln body in the cooling section
  • the preferred range of the ratio of the diameters is from 2 to 3.5.
  • the inner sleeve is provided with a dust-reducing device, and a dust collecting device is arranged at a lower portion thereof, and an upper portion thereof is connected with the air guiding pipe, and the air guiding tube is used for extracting high-temperature cooling air from the upper part of the kiln body, and the extracted high-temperature cooling air is used for heating and supporting combustion. gas.
  • the heating furnace group includes a regenerative heating furnace, a regenerative preheating furnace and a mixing chamber.
  • the low calorific value gaseous fuel and the combustion air from the mixing chamber enter the burner for combustion.
  • the generated hot flue gas heats the heat storage material of the regenerator; in the air supply cycle of the regenerative heating furnace, the CO 2 gas enters the heating furnace from the lower portion of the regenerator of the heating furnace, and is heated by the heat storage material.
  • the hot air outlet at the upper part of the chamber exits the furnace and is sent to the kiln body.
  • the high-temperature cooling air extracted from the top of the kiln body is used to heat the heat storage material inside the regenerative preheating furnace, and the heated heat storage material is used to heat the combustion air, and the heated combustion air is discharged from the upper portion of the heat storage material.
  • the air mixing chamber adjusts the combustion air to a set temperature and sends the combustion air to the regenerative heating furnace.
  • the set temperature value of the CO 2 hot air is in the range of 800 ° C to 1200 ° C, preferably 850 ° C to 1150 ° C.
  • the lime kiln uses a non-flame, constant temperature and adjustable CO 2 hot air to calcine the mineral material; by precisely controlling the hot air temperature of the CO 2 gas to improve the calcination effect, there is no over-burning phenomenon. It is beneficial to improve the activity of the product; the thermal energy using CO 2 gas as the carrier is used for the calcination of the mineral material, which substantially shortens the calcination time, and can greatly increase the production capacity without increasing the volume of the kiln body.
  • the inventors have carried out experimental verification to prove that the thermal energy using CO 2 gas as a carrier is used for calcination of mineral materials, which not only greatly reduces the calcination time, but also has high quality and high activity of lime finished products.
  • the kiln burner is eliminated, the kiln structure is substantially simplified, the system is more stable, reliable, easy to maintain, and reduces system maintenance costs;
  • the invention eliminates the kiln burner, thus simplifying The kiln structure, the present invention greatly reduces the operating cost of the lime kiln compared to various lime kiln technologies.
  • FIG. 2 is a schematic structural view of a second prior art described in the background art
  • FIG. 3 is a schematic structural view of a third structure of the prior art described in the background art.
  • FIG. 4 is a schematic structural view of a fourth structure of the prior art described in the background art.
  • Figure 5 is a composition diagram of a lime kiln apparatus in Embodiment 1 of the present invention.
  • Figure 6 is a schematic view showing the working principle of the lime kiln in the first embodiment of the present invention.
  • Figure 7 is a schematic view showing the working principle of the regenerative heating furnace in the first embodiment of the present invention.
  • Figure 5 shows the composition and working principle of the fully achievable CO 2 lime kiln system according to the present invention, including: 100-kiln body, 20-heating furnace group, 21-blast furnace gas, 22-combustion air, 23-combustion Fan, 30-loading device, 40-discharge mechanism, 50-cooling air, 60-CO 2 recovery mechanism, 70-CO 2 cooked air.
  • the kiln body 100 comprises: 110-preheating section, 120-calcining section, 130-cooling section
  • the meaning of the present invention is firstly to use CO 2 hot air as a thermal energy carrier to calcine the mineral material, CO 2 hot air has no flame, and the temperature is constant. The effect is to accelerate the cracking of the mineral material, not only to obtain a high-grade lime product, but also to greatly shorten the calcination time;
  • the mineral material enters the kiln body 100 from the loading mechanism 30, passes through the preheating section 110, the calcining section 120, and the cooling section 130, and the cooled lime product is discharged from the lower discharging mechanism 40 of the kiln body 100; wherein the mineral material is used
  • the CO 2 hot air is preheated and calcined, and the calcined lime product is cooled by air;
  • the CO 2 hot air 70 entering the kiln from the calcination section is calcined by the preheated ore, and then merged with the CO 2 produced by the cracking of the ore material, and enters the preheating section 110 of the upper part of the kiln body 100, and is cooled from the kiln.
  • the upper part of the body 100 is taken out, enters the CO 2 gas recovery mechanism 60, after the dust removal process, a part is recycled, and the other part enters the regenerative heating furnace group, and is heated and then returned to the calcination section 120 of the kiln body 100;
  • the preferred arrangement of the heating furnace group 20 is composed of three regenerative heating furnaces and two regenerative combustion air preheating furnaces.
  • the heating furnace group 20 uses the blast furnace gas 21 as a fuel to supply CO 2 gas from the kiln body. Heating to the temperature required for the process, the temperature is generally in the range of 800 ° C ⁇ 1200 ° C, preferably in the range of 850 ° C ⁇ 1150 ° C;
  • the calcined lime product enters the cooling section 130, and the cooling air 50 enters the cooling section 130 of the kiln body 100 from the lower portion of the kiln body 100, cools the lime product, and is extracted from the upper portion of the cooling section 130 of the kiln body 100.
  • the residual heat generated by the cooling air 50 during the cooling of the lime product is used to heat the combustion air 22 in the furnace group 20.
  • auxiliary devices and devices not shown in FIG. 5 that do not relate to the present invention are not meant to be essential to the practice of the present invention.
  • the inventors propose to adopt mature as much as possible. The technology configures these necessary ancillary facilities and equipment.
  • FIG. 6 is a schematic view showing the working principle of the lime kiln involved in the embodiment, illustrating the method for recovering CO 2 gas from the lime kiln and calcining the mineral material by using CO 2 hot air
  • FIG. 7 is an embodiment of the present invention.
  • a schematic diagram of the working principle of the regenerative heating furnace group illustrates a method in which the regenerative fuel group uses a low calorific value fuel to heat CO 2 and a residual heat of the cooling air to heat the combustion air.
  • one of the keys to the realization of the present invention for the kiln body of the lime kiln system is the isolation technology of the CO 2 gas in the upper part of the kiln body and the cooling air in the lower part of the kiln body, and the dust removal and waste heat utilization technology of the cooling air.
  • Figure 6 is a typical example of a relatively simple and efficient implementation of CO 2 reduction.
  • the kiln body 100 is provided with an inner sleeve AB, and a material passage for material movement is formed between the inner wall of the kiln body 100 and the outer wall of the inner sleeve AB, and the material passage is in the preheating section, the calcining section and the cooling section.
  • the mineral material enters the kiln body 100 from the top by the feeding system 30, and goes down along the material passage between the inner wall of the kiln and the outer wall of the inner sleeve AB, passes through the preheating section 110, the calcining section 120, and the finished product enters. Cooling section 130, and finally, the cooled lime product is discharged through the discharging system 40;
  • the CO 2 hot air 70 enters the kiln body 100 through three rows of air inlet nozzles arranged on the kiln body 100. Below the calcining section 120, the diameter of the material passage is reduced, and the calcining section 120 and the cooling section 130 are Forming a transition between the calcining section and the cooling section to establish a "seal" layer of material, a so-called “seal seal", the main function of which is to block the cooling air 50 enters the calcination section 120.
  • the kiln body 100 is in the form of a circular shaft kiln, preferably in the form of a drum-shaped shaft kiln having a larger inner diameter in the lower portion of the preheating section 110, a middle portion of the calcining section 120, and a smaller inner diameter in the lower portion of the calcining section 120;
  • the kiln body 100 is internally provided with an inner sleeve AB.
  • the inner sleeve AB is usually in the form of a circular cylinder, and can also be designed as a shaped cylinder.
  • the material moving between the inner wall of the kiln body 100 and the outer wall of the inner sleeve AB forms a material moving material.
  • the passage, the total width of the material passage section is a diameter, the passage diameter of the material passage in the preheating section, the calcination section and the cooling section is different, and the material passage has a larger diameter in the middle of the calcination section 120, such as a1, the material passage is There is a transition section between the calcination section and the cooling section, and the passage diameter of the transition section is small, such as a; the ratio of the maximum diameter of the material passage in the middle of the calcination section 120 to the minimum diameter of the lower part of the calcination section is 1 to 4, The preferred range is 2 to 3.5;
  • the material moves faster in the transition section having a smaller diameter, thereby forming a so-called transition section "seal seal layer"; It can hinder the entry of cooling air into the calcination section 120, and also contributes to the activity of the lime product.
  • the cooling solution is used to cool the calcined lime product.
  • the typical solution provided by the present invention is as follows:
  • the kiln body 100 is internally provided with an inner sleeve AB, and the inner sleeve AB is internally provided with a dust reducing device, and a dust collecting device is arranged at a lower portion thereof, and an upper portion thereof is connected with the air guiding pipe, and the air guiding tube is used for the high temperature cooling air 50
  • the upper portion of the kiln body 100 is withdrawn, and the inner sleeve AB has an air inlet at a position above the cooling section 130; the cooling air 50 enters the material passage at the lower portion of the cooling section 130, that is, the lower portion of the kiln body 100, and then the inner sleeve
  • the air inlet of the AB located at the upper part of the cooling section 130 is drawn into the inner sleeve AB;
  • the lime product moves downward along the material passage, and the cooling air 50 and the lime product flow upwards to cool the finished lime product;
  • the material passage has a larger diameter in the middle and lower portions of the cooling section, such as a2, the material
  • the ratio of the maximum diameter a2 of the passage in the cooling section to the minimum diameter a of the transition section in the upper part of the cooling section is 1 to 4, preferably in the range of 2 to 3.5; after the lime product is cooled, it enters the discharge mechanism 40; Under suction, a negative pressure is formed inside the inner sleeve AB, and the cooling air 50 is drawn into the inner sleeve AB from the air inlet located at the upper portion of the cooling section 130, and is removed by the inner sleeve AB, and then extracted out of the kiln through the air guiding duct.
  • Body 100 is a negative pressure is formed inside the inner sleeve AB, and the cooling air 50 is drawn into the inner sleeve AB from the air inlet
  • Fig. 7 is a schematic view showing the operation of the regenerative heating furnace group 20 according to the present invention. These include: 201-regenerative heating furnace, 202-regenerative preheating furnace, 21-blast furnace gas, 22-combustion air, 23-combustion fan, 24-mixing chamber, 25-regenerative preheating furnace To the mechanism, 26-regenerative furnace flue gas.
  • the other two heating furnaces can also maintain production.
  • the three regenerative heating furnaces adopt a "two-burn-and-one-feed" operation mode
  • the regenerative heating furnace 201 uses the blast furnace gas 21 and the combustion-supporting air 22 in the furnace; the cold air is collected from the lime kiln system.
  • the dust-removed CO 2 gas is heated by the heating furnace 201 to 800 ° C to 1200 ° C, and then sent back to the lime kiln 100 through a ring-shaped hot air nozzle.
  • the working principle of the heating furnace 201 is: in the furnace cycle: the blast furnace gas 21 and the combustion air 22 enter the burner of the regenerative heating furnace 201 for combustion, and generate high temperature flue gas of 1100 ° C to 1300 ° C for heating
  • the heat storage material in the furnace in the air supply cycle: the burner is closed, and the cold CO 2 gas is introduced, and the cold CO 2 gas is collected from the lime kiln 100, and a part of the CO 2 is removed after the dust is removed, and the CO 2 gas is heated by the furnace.
  • the heat storage material of 201 is heated and returned to the lime kiln 100 through a ring-shaped hot air nozzle at a constant temperature in the range of 800 ° C to 1200 ° C.
  • the heating furnace group has two working modes of "two firings and one delivery", that is, two heating furnaces and one heating furnace are simultaneously supplied with air.
  • the lower portion of the heating furnace 201 has a dust collector for collecting dust and cleaning out the heating furnace during routine maintenance.
  • the waste flue gas of the heating furnace 201 generally needs to continue to be cooled and discharged after dust removal.
  • the preferred technical solution of the present invention is to connect the waste flue gas of the heating furnace 201 to the air mixing chamber 24 to adjust the combustion air from the preheating furnace 202. temperature.
  • the outer casing of the two regenerative preheating furnaces 202 is made of metal structural steel, and is provided with a heat insulating lining, the upper part has an arch structure, the lower part is a regenerator, the regenerator has a heat storage material, and the heat storage material is preferably a lattice brick form.
  • the lower part of the checker brick has a heat-resistant cast iron support device.
  • the lower part of the regenerative preheating furnace 202 has an exhaust gas outlet and a combustion air inlet.
  • the upper part of the checker brick has a combustion air outlet.
  • the bottom of the preheating furnace is provided with a dust collecting structure, and the upper part of the arched shape is provided with high temperature cooling.
  • the high-temperature cooling air 50 from the kiln body 100 enters the preheating furnace 202 from the arched upper portion of the regenerative preheating furnace 202 via the air guiding duct.
  • the high-temperature cooling air 50 from the kiln body 100 enters the preheating furnace through the pipeline from the arched top of the first regenerative preheating furnace 202, heats the heat storage material of the regenerator, and is discharged from the exhaust gas outlet after being cooled. emission;
  • the high temperature cooling air 50 passes through the pipeline and enters the second regenerative preheating furnace 202 through the switching valve to heat the second seat.
  • the heat storage material of the preheating furnace regenerator at the same time, the cold combustion air 22 enters the first regenerative preheating furnace 202 from the lower portion, is heated by the heat storage material of the regenerator, and is discharged from the upper portion of the heat storage material to enter
  • the air mixing chamber 24; the air mixing chamber is also connected to the cold combustion air and the waste flue gas from the heating furnace 201 for adjusting the temperature of the combustion air 22, and the combustion air 22 enters the heat storage from the air mixing chamber 24 at a fixed temperature. Furnace 201.
  • a small amount of dust carried by the high-temperature cooling air 50 is collected by the collecting mechanism at the lower portion of the preheating furnace 202, and the preheating furnace is cleaned up during maintenance of the daily equipment.

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Abstract

一种全回收CO2石灰窑装置及其石灰制备方法，包括窑体（100）和加热炉组（20），加热炉组（20）将CO2加热至设定温度后形成CO2热风送入到窑体（100）中对预热后的矿料进行煅烧，矿料煅烧时产生的CO2与CO2热风混合，向上对窑体（100）上部的矿料进行预热并在窑体（100）上部被抽出，经收集处理后的部分CO2再次进入加热炉组（20），加热至设定温度后返回窑体（100），煅烧后的石灰成品经空气冷却后从窑体（100）底部排出。

Description

一种全回收CO 2的石灰窑装置 技术领域
本发明涉及一种利用气体为燃料的石灰窑及利用该石灰窑生产石灰的工艺方法。
背景技术
石灰即氧化钙(CaO)，广泛应用于钢铁工业、电石工业、氧化铝工业、耐火材料等工业，也是这些大规模工业领域所必需的生产原料之一，例如在冶金工业中，每生产1吨的钢就需要70公斤的石灰。制取石灰的主要原料是石灰石，石灰石主要成分是碳酸钙(CaCO 3)，烧制石灰的基本原理就是借助高温，把石灰石中碳酸钙分解成氧化钙和二氧化碳。
基本反应式：CaCO 3+42.5Kcal＝CaO+CO 2
石灰制取工艺过程主要分为预热、煅烧、冷却和卸灰。基于现有的石灰制取技术的工艺方法是：将石灰石和固体燃料装入石灰窑，或者在石灰石装入石灰窑的同时，将气体燃料经管道和燃烧器送入窑体；石灰石被预热到800℃～850℃开始分解，到1200℃完成煅烧；生成的石灰经过冷却后，卸出窑外，即完成生石灰产品的生产。在现有的石灰生产工艺中，每生产1吨的石灰就会产生超过1吨的CO 2排放。虽然CO 2在食品、卫生、石油化工、核工业、消防领域等国民经济的各部门中有着十分重要的用途，在冶金行业也应用广泛，但在现有的石灰生产工艺中，由于燃料在燃烧时需要鼓入助燃空气，烟气中CO 2的体积浓度约为10-15％，回收CO 2的成本很高，企业一般将含有大量CO 2的烟气直接排入大气，造成环境污染。
现有的石灰窑按燃料分：有混烧窑(即以烧固体燃料为主，包括焦炭、焦粉、煤等)和气烧窑(即以燃烧气体燃料为主，如高炉煤气、焦炉煤气、转炉 煤气、电石尾气、发生炉煤气、天然气等)，其中气烧窑应用更为广泛；按窑形分：有竖窑、回转窑、套筒窑、并流蓄热式双膛竖窑(麦尔兹窑，也称迈尔兹窑)、弗卡斯窑(意大利)等，其中应用比较广泛的是环形套筒竖窑、麦尔兹窑：按操作方式分：有负压操作窑(如环形套筒竖窑)和正压操作窑(如并流蓄热式双膛竖窑)。
无论哪一种形式的石灰窑，均是由窑体、上料装置、布料装置、燃烧装置、卸灰装置、电器、仪表控制装置、除尘装置等部件组成。现有的石灰窑技术、尤其是各种气烧窑共有的特点是都需要配置燃烧器系统，气烧窑的燃烧器系统一般由多排、多组燃烧器分布组成，配置有气体燃料管道和助燃空气管道、喷嘴等。
为了更清楚地说明各种形式的气烧窑技术的普遍特点，下面以应用比较普遍的环形套筒竖窑、并流蓄热式窑(麦尔兹窑)为例进行阐述。
如附图1，环形套筒竖窑系统包括：1-炉体、1a-冷却空气、2-上料系统、3-1-上内套筒、3-2-换热器、3-3下内套筒、4-废气排出系统、4a-全部废气、5-燃烧器、5a-燃气+烧嘴空气、6-出料系统；炉体1内有：1-1-预热带、1-2-煅烧带、1-3-冷却带。
在预热带1-1内，石灰石被加热至其煅烧温度。预热带1-1的热量来自于煅烧带1-2的废烟气，煅烧带1-2产生的一部分废烟气向上进入预热带1-1，再从预热带1-1上部进入废气系统4；另一部分废气(带有多余的热量)通过上内套筒3-1进入换热器3-2，用于加热助燃空气，加热后的助燃空气通过管道送到燃烧器5，换热后的废气再经废气系统4排出。
煅烧过程在煅烧带1-2进行，燃气和助燃空气在燃烧器5内混合、燃烧，在煅烧带1-2内对石灰石煅烧，煅烧后的一部分废烟气4a向上在预热带1-1中 对矿料进行预热，石灰成品在煅烧带1-2底部即进入冷却带1-3。
在冷却带1-3内，热的石灰与窑底吸入的冷空气1a进行热交换，温度降低后通过出料系统6排出窑体。冷却空气1a从冷却带1-3下部进入窑内，在下内套筒3-3内与燃烧器5的一部分废烟气混合成为高温废空气，从下内套筒3-3上部排出进入燃烧器5参与燃烧。
套筒窑的主要技术优势包括：热效率高、原料入窑粒度范围大、占地面积小、负压煅烧、运行安全稳定等。这种炉型的技术特点还包括在煅烧段与冷却段之间具有一个负压操作区和正压操作区的分界带。其中，并流烟气在此分界带被抽出窑体，全部废烟气的一部分通过内套筒进入换热器，另一部分对矿料进行预热后从窑体上部被抽出，因此，自所述分界带以上形成了负压操作区。在冷却段，从窑体底部吸入的冷却空气从冷却段上部被抽出，因此在所述分界带的下部形成正压操作区。
在上述系统里，窑内煅烧生成的CO 2经废气系统4排放，由于其中混合了空气，因此回收CO 2成本很高；预热带1-1和煅烧带1-2的热量均来自气体燃料和助燃空气在燃烧器5内混合燃烧形成的高温烟气，所有的燃烧器分两带布置在窑体1上，采用直接燃烧的方式对原料进行加热，因此，热量不能均衡分布。在这种情况下，为了获得高品质的石灰，整个煅烧反应时间较长，这既增大了窑体尺寸，同时又极大地限制了生产率。
并流蓄热式窑(麦尔兹窑)也是目前应用比较广泛的窑型之一。目前有两种形式的石灰竖窑，即单膛逆流式和多膛并流式石灰窑(一般是双窑膛)。标准的并流蓄热式石灰窑是由燃烧窑膛和非燃烧窑膛相互切换运行的双膛式石灰窑，其采用的是环形双膛的结构形式，中间由通道连接，每隔一定时间即轮换煅烧一次。在完成煅烧后，燃烧气体从燃烧窑膛内通过所述通道流入到非燃烧 窑膛，对原料石灰石进行预热，预热区起到了一个换热器的作用。这种并流蓄热式窑具有热效率高、能耗低、石灰产品的品质较高等优点，但因为多了一套换向系统，设备比较复杂并且投资较大。同样地，并流蓄热式窑技术的生产率并没有明显提高，回收CO 2成本很高。
并流蓄热式窑(麦尔兹窑)双膛石灰竖窑工作原理示意图如附图2。其中包括：7-燃烧膛，7-1-燃烧风，7-2-煅烧带，7-3冷却带，8-排气膛，8-1-预热带，8-2废气，9-通道，8-3冷却带，10-冷却风。
如上所述，对于应用比较广泛的不同形式的气烧式石灰窑来说，其结构形式和煅烧形式虽然有所区别，但工艺流程、主要设备构成基本类似，共性的问题都是采用了安装在窑体上的燃烧器对矿料进行加热煅烧，煅烧时间较长，设备投资大、运行费用高、维护费用高，生产率较低，CO 2排放污染严重。工程技术人员虽然进行了许多重大改进，但上述共性问题依然没有得到彻底解决。
与本发明接近的几项石灰窑的研究成果包括：
一种梁式蓄热石灰窑(CN 203007146 U)，如附图3，其中包括：
1c-进料系统、2c-上抽吸梁、3c-预热带、6c-窑体、7c-下抽吸梁、8c-冷却带、9c-出料口、10c-旋风除尘器、11c-布袋除尘器、12c-引风机、13c-第2阀门、14c-2号蓄热器、15c-烧嘴、16c-第4阀门、17c-第1阀门、18c-三通阀、19c-1号蓄热器、20c-第3阀门、21c-助燃空气、22c-燃料、23c-排放系统。
该技术是将从窑体冷却段上部抽出的热废气进行除尘净化处理，然后作为助燃空气进入预热器，助燃空气预热器由2台蓄热式换热器组成，2台蓄热式换热器轮流对助燃空气进行加热，持续地为窑体燃烧器提供热的助燃空气，窑体燃烧器被布置在窑体的燃烧梁上。蓄热式换热器采用低热值煤气为燃料，主要 结构包括燃烧器和蓄热室；由于使用了预热后的助燃空气，窑体燃烧器也可以采用低热值煤气。这种技术的特征是利用蓄热式换热器对助燃气体进行预热，提高了助燃空气温度，窑体燃烧器因此可以采用低热值煤气。但因为这种技术只解决了采用低热值煤气降低运行成本的问题，并未涉及其它的气烧式石灰窑共性技术问题，因此应用受到局限。
与上述技术类似的，还有“一种空气蓄热石灰窑(CN 203144298 U)”，其技术特点是在窑体燃烧器上设计了一种“蓄热式烧嘴”，利用这种带蓄热材料的烧嘴对助燃空气进行预热，目的是在燃烧时利用低热值煤气。同样地，这项技术也没有涉及其它的气烧式石灰窑共性技术问题。
与本发明接近的一项石灰窑技术是“一种基于CO 2富集的并流蓄热式石灰窑生产工艺方法”(CN 105000811 A)，如附图4。
其中包括：1d-窑膛1、2d-窑膛2、3d-富氧、4d-CO 2与煤粉混合、5d-CO 2为载气输送煤粉、6d-CO 2换热、净化装置、7d-CO 2循环气、8d-预热带、9d-煅烧带、10d-冷却带、11d-冷却后的石灰成品、12d-回收储存的CO 2、13d-换向机构。
这项技术的主要特征是：采用并流蓄热式双窑膛形式，以95％的氧气作为助燃气体与喷入煅烧窑膛的固体煤粉混合燃烧，固体煤粉以CO 2气体输送，在窑膛下部的冷却段，采用CO 2气体对石灰成品进行冷却，煅烧后的烟气与冷却段上部的高温冷却气体混合后，通过双窑膛的通道进入蓄热窑膛，用于对矿料的预热，按一定时间，煅烧窑膛与预热窑膛通过换向装置轮换操作。按照该项技术的说明，最终可以回收浓度达95％以上的CO 2气体，这些CO 2气体的约10％用于输送固体燃料，约55％用于冷却石灰成品，约35％则回收利用，例如用于制作干冰。
这项技术采用固体燃料-煤粉作为燃料，虽然采用了浓度95％的氧作为助燃 气体且过量系数1.1～1.4，但是在石灰成品里仍然将会混合一定的燃料粉尘，这些粉尘会污染成品、降低成品的品质；另外，根据该项技术说明，“采用CO 2作为冷却气体将温度为1000℃～1150℃的高温CaO冷却至80℃～100℃”。虽然该项技术在技术说明资料中列举了日产450吨、500吨、550吨三个实施例，但是发明人仍然对其采用CO 2作为冷却气体的技术措施的可行性存在质疑。根据发明人的研究成果，以及公开的研究资料都证明：如果采用CO 2气体冷却高温石灰成品，部分石灰成品将会与CO 2反应重新生成碳酸钙，导致石灰成品的品质严重下降。
如上所述，对于上述与本发明相近的研究，或者因为其并未解决各种气烧窑的共性技术问题，或者因为其采用固体燃料，或者因为使用CO 2作为冷却气体等问题，使得这些研究都无法广泛应用。
发明内容
针对现有技术中存在的问题，本发明提供了一种全回收CO 2的石灰窑装置，以及采用该装置制取工业用石灰的工艺方法。
本发明采用如下的技术方案：
一种全回收CO 2石灰窑装置，包括窑体和加热炉组，其特征在于：窑体内不带燃烧器，加热炉组将CO 2加热至设定温度后形成CO 2热风送入到窑体中对预热后的矿料进行煅烧，矿料煅烧时产生的CO 2与CO 2热风混合，向上对窑体上部的矿料进行预热并在窑体上部被抽出，经收集处理后的部分CO 2再次进入加热炉组，加热至设定温度后返回窑体，煅烧后的石灰石成品经空气冷却后从窑体底部排出。
所述窑体包括上料机构和出料机构，窑体的工作区域自上而下包括预热段、 煅烧段、冷却段，窑体内设置有内套筒，在窑体内壁和内套筒外壁之间形成物料移动的物料通道，所述物料通道截面的总宽度为通径，物料通道在预热段、煅烧段和冷却段的通径不同，矿料从上料机构进入窑体，沿物料通道从预热段到煅烧段，成品沿物料通道经过冷却段，最后从出料机构排出窑体，窑体煅烧段侧壁上设置有CO 2热风进口，内套筒位于冷却段的上部设置有进风口，冷却空气从窑体的下部进入到窑体与内套筒之间的物料通道，对石灰石成品冷却后从进风口进入到内套筒内并从顶部被抽出窑体。
物料通道在煅烧段和冷却段之间具有过渡段，过渡段通径减小，物料沿物料通道在过渡段的移动速度较快，形成料封层。
所述窑体内部物料移动的物料通道优选在预热段下部、煅烧段中部的通径较大、在煅烧段下部通径减小，经过过渡段后，在冷却段的通径较大变大。
所述窑体的物料通道在煅烧段中部的最大通径与煅烧段下部的最小通径的比值的优选范围是2～3.5，所述窑体的物料通道在冷却段的最大通径与过渡段通径的比值的优选范围是2～3.5。
内套筒内部设置有降尘装置，其下部有粉尘收集装置，其上部与引风管连接，引风管用于将高温的冷却空气从窑体上部抽出，被抽出的高温冷却空气用于加热助燃气体。
加热炉组包括蓄热式加热炉、蓄热式预热炉和混风室，在蓄热式加热炉的烧炉周期里，低热值的气体燃料和来自混风室的助燃空气进入燃烧器燃烧，生成的热烟气加热蓄热室的蓄热材料；在蓄热式加热炉的送风周期里，CO 2气体从加热炉蓄热室下部进入加热炉，经蓄热材料加热后从蓄热室上部的热风出口排出加热炉并送入窑体中。
从窑体顶部被抽出的高温冷却空气用于加热蓄热式预热炉内部的蓄热材 料，加热后的蓄热材料再用于加热助燃空气，被加热的助燃空气从蓄热材料上部排出进入所述混风室，混风室将所述助燃空气调整到设定的温度，再将其送至所述蓄热式加热炉。
CO 2热风的设定温度值的范围是800℃～1200℃，优选是850℃～1150℃。
将CO 2加热至设定温度后形成CO 2热风送入到窑体中对预热后的矿料进行煅烧，矿料煅烧时产生的CO 2与CO 2热风混合，向上对窑体上部的矿料进行预热并在窑体上部被抽出，经收集处理后的部分CO 2再次进入加热炉组，加热至设定温度后返回窑体，煅烧后的石灰石成品经空气冷却后从窑体底部排出。
本发明具有的技术效果：
1、所述石灰窑使用没有火焰的、温度恒定且可调的CO 2热风对矿料进行煅烧；通过精准地控制CO 2气体的热风风温来提高煅烧效果，因此不存在过烧现象，这有利于提高产品活性；以CO 2气体作为载体的热能用于矿料煅烧，实质性地大幅度缩短了煅烧时间，在不增加窑体容积的情况下就可以大幅度提高产能。发明人对此进行了试验验证，证明以CO 2气体作为载体的热能用于矿料煅烧，不仅大幅度缩减了煅烧时间，而且石灰成品质量高、活性高。
2、取消了窑体燃烧器，实质性地简化了窑体结构，系统更加稳定、可靠，便于维护，降低了系统维护成本；
3、一方面实现了CO 2减排，另一方面相当于为石灰窑系统提供了高附加值的副产品，提高了本发明的经济效益；
4、使用较低热值的高炉煤气作为燃料、持续为石灰窑提供热能，实质性地取代了价格昂贵的焦炉煤气或其它的高热值燃料；本发明取消了窑体燃烧器，因此简化了窑体结构，相比现在各种石灰窑技术，本发明大幅度地降低了石灰窑运行成本。
附图说明
下面结合附图对本发明进一步说明：
图1为背景技术中描述的现有技术之一结构示意图；
图2为背景技术中描述的现有技术之二结构示意图；
图3为背景技术中描述的现有技术之三结构示意图；
图4为背景技术中描述的现有技术之四结构示意图；
图5为本发明实施例1中的石灰窑装置组成图；
图6为本发明实施例1中的石灰窑工作原理示意图；
图7为本发明实施例1中的蓄热式加热炉工作原理示意图；
具体实施方式
下面结合附图说明和具体实施方式对本发明作进一步描述：
实施例1
图5展示的是本发明涉及的可全回收CO 2的石灰窑系统组成和工作原理图，包括：100-窑体、20-加热炉组，21-高炉煤气，22-助燃空气，23-助燃风机，30-上料装置，40-出料机构，50-冷却空气，60-CO 2回收机构，70-CO 2熟风。其中，窑体100包括：110-预热段，120-煅烧段，130-冷却段
如附图5所示，相对于现有的所有形式的气烧石灰窑技术来说，本发明的意义首先在于采用CO 2热风作为热能载体对矿料进行煅烧，CO 2热风没有火焰、温度恒定，其效果是加速了矿料裂解，不仅可以获得高品位的石灰成品，而且大幅度缩短了煅烧时间；
其中，矿料从上料机构30进入窑体100，经过预热段110、煅烧段120、冷 却段130，降温后的石灰成品从窑体100的下部出料机构40排出；其中，矿料采用CO 2热风进行预热和煅烧，煅烧后的石灰成品采用空气进行冷却；
其中，从煅烧段进入窑体的CO 2热风70对预热后的矿料进行煅烧，再与矿料裂解产生的CO 2汇合，向上进入窑体100上部的预热段110，降温后从窑体100的上部被抽出，进入CO 2气体回收机构60，经过除尘处理后，一部分回收利用，另一部分进入蓄热式加热炉组，被加热后再返回窑体100的煅烧段120；
其中，加热炉组20优选的方案是由三座蓄热式加热炉和二座蓄热式助燃空气预热炉组成，加热炉组20使用高炉煤气21为燃料，将来自窑体的CO 2气体加热到工艺所需温度，该温度一般在800℃～1200℃范围内，优选范围是850℃～1150℃；
其中，煅烧后的石灰成品进入冷却段130，冷却空气50从窑体100的下部进入窑体100的冷却段130，对石灰成品进行冷却，再从窑体100的冷却段130上部被抽出，送入加热炉组20，冷却空气50在冷却石灰成品过程中产生的余热，用于在加热炉组20中加热助燃空气22。
对于附图5并没有显示的那些不涉及本发明的一些辅助设施和设备，并不意味这些附属设施和设备对于实现本发明没有必要的，为实现本发明目的，发明人建议尽可能采用成熟的技术配置这些必要的附属设施和设备。
为更清晰地说明本发明的实施方法，发明人利用附图6、附图7对石灰窑和蓄热式加热炉组的工作原理做进一步的技术说明。附图6是所述实施案例涉及的石灰窑工作原理示意图，说明了所述石灰窑回收CO 2气体、以及利用CO 2热风对矿料进行煅烧的方法；附图7为本发明实施案例涉及的蓄热式加热炉组的工作原理示意图，说明了所述蓄热式燃料组使用低热值燃料加热CO 2、以及利用冷却空气的余热加热助燃空气的方法。
根据附图5，对于石灰窑系统的窑体来说，实现本发明的关键之一是涉及窑体上部CO 2气体与窑体下部冷却空气的隔离技术，以及冷却空气的除尘和余热利用技术。
附图6是结构相对简单、有效地实现CO 2减排的一个典型实施案例。
其中包括：100-石灰窑窑体，AB-内套筒、110-预热段，120-煅烧段，130冷却段，30-上料装置，40-出料装置，50-冷却空气，60-CO 2回收装置，70-CO 2热风；
根据附图6，所述窑体100设置有内套筒AB，窑体100内壁与内套筒AB外壁之间形成物料移动的物料通道，物料通道在预热段、煅烧段和冷却段的通径不同，矿料由上料系统30从顶部进入窑体100，向下且沿着窑体内壁与内套筒AB的外壁之间的物料通道，经过预热段110、煅烧段120，成品进入冷却段130，最后，冷却后的石灰成品经出料系统40排出；
所述CO 2热风70经窑体100上布置的三排进风喷嘴进入窑体100，在所述煅烧段120下方，采用减小物料通道通径的方式，在煅烧段120和冷却段130之间形成过渡段，所述过渡段在煅烧段和冷却段之间建立起物料“密封”层，即所谓的“料封层”，所述过渡段“料封层”的主要作用是阻碍冷却空气50进入到煅烧段120。
为实现上述目的，本发明提供的典型解决方案如下：
所述窑体100的形式为圆形竖窑，优选形式是一种在预热段110下部、煅烧段120中部的内径较大、在煅烧段120下部内径减小的鼓腰形竖窑；所述窑体100内部设置有内套筒AB，内套筒AB的形式通常为圆形筒体，也可以设计为异形筒体，窑体100内壁与内套筒AB外壁之间形成物料移动的物料通道，所述物料通道截面的总宽度为通径，物料通道在预热段、煅烧段和冷却段的通径不 同，物料通道在煅烧段120中部的通径较大，如a1，物料通道在煅烧段和冷却段之间有过渡段，过渡段的通径较小，如a；所述物料通道在煅烧段120中部的最大通径与煅烧段下部的最小通径的比值为1～4，优选范围是2～3.5；
由于所述物料通道位于煅烧段120的下部的过渡段的通径较小，物料在通径较小的过渡段移动速度较快，因此形成所谓的过渡段“料封层”；这种结构不仅可以阻碍冷却空气进入到煅烧段120，也有利于石灰成品提高活性。
采用冷却空气对煅烧后的石灰成品进行冷却，本发明提供的典型解决方案如下：
所述窑体100内部设置有内套筒AB，内套筒AB内部设置有降尘装置，其下部有粉尘收集装置，其上部与引风管连接，引风管用于将高温的冷却空气50从窑体100上部抽出，内套筒AB在位于冷却段130的上部的位置有进风口；冷却空气50在所述冷却段130下部，也就是窑体100的下部进入物料通道，再从内套筒AB位于冷却段130上部的进风口被抽进内套筒AB；
在冷却段130，石灰成品沿物料通道向下移动，而冷却空气50与石灰成品逆流向上，对石灰成品进行冷却；物料通道在冷却段中部和下部的通径较大，如a2，所述物料通道在冷却段的最大通径a2与冷却段上部的过渡段的最小通径a的比值为1～4，优选范围是2～3.5；石灰成品冷却后进入出料机构40；在引风管的吸抽作用下，内套筒AB内部形成负压，冷却空气50从位于冷却段130上部的进风口被抽进内套筒AB，经过内套筒AB除尘后，再通过引风管被抽出窑体100。
为实现上述目的，可以采取与上述典型方案不同的其它的解决方案，但无论哪种解决方案，都应努力实现：1)冷却空气不会进入煅烧段，2)高温的冷却空气经初步降尘后再被抽出窑体。
附图7是本发明所涉及的蓄热式加热炉组20工作原理图。其中包括：201-蓄热式加热炉，202-蓄热式预热炉，21-高炉煤气，22-助燃空气，23-助燃风机，24-混风室，25-蓄热式预热炉换向机构，26-蓄热式加热炉烟气。
其中，优选采用三座蓄热式加热炉201，可以保证为石灰窑系统连续提供热风，当一座加热炉维护时，其余2座加热炉也可以维持生产。
其中，三座蓄热式加热炉采用“两烧一送”工作模式，所述蓄热式加热炉201在烧炉时使用高炉煤气21和助燃空气22；冷风则为来自石灰窑系统收集的、经过除尘的CO 2气体，被加热炉201加热至800℃～1200℃，再经环形布置的热风喷嘴送回到石灰窑100。
所述加热炉201的工作原理是：在烧炉周期里：高炉煤气21与助燃空气22进入蓄热式加热炉201的燃烧器进行燃烧，生成1100℃～1300℃的高温烟气，用于加热炉内蓄热材料；在送风周期里：燃烧器关闭，通入冷的CO 2气体，冷的CO 2气体来自石灰窑100收集、除尘后的一部分CO 2，所述CO 2气体被加热炉201的蓄热材料加热，在800℃～1200℃范围内，以一个恒定的温度经环形布置的热风喷嘴送回到石灰窑100。所述加热炉组“两烧一送”工作模式，即同时有2座加热炉烧炉、1座加热炉送风。
所述加热炉201下部有粉尘收集器，便于将粉尘收集，在日常性维修时清理出加热炉。
所述加热炉201的废烟气一般需继续降温、除尘后排放。有多种可选择的技术方案对加热炉201废烟气进行降温，本发明优选的技术方案是：将加热炉201的废烟气接入混风室24，调节来自预热炉202的助燃空气温度。
所述两座蓄热式预热炉202的外壳为金属结构钢，设置保温内衬，上部有拱形结构，下部是蓄热室，蓄热室有蓄热材料，蓄热材料优选格子砖形式，格 子砖下部有耐热铸铁支撑装置，蓄热式预热炉202下部有废气出口和助燃空气进口，格子砖上部有助燃空气出口，预热炉底部设置粉尘收集结构，拱形上部设置高温冷却空气50的进风口，来自窑体100的高温冷却空气50经引风管道从蓄热式预热炉202的拱形上部进入预热炉202。
来自窑体100的高温冷却空气50经过管道从第1座蓄热式预热炉202的拱形顶部进入预热炉，加热蓄热室的蓄热材料，降温后从废气出口排出，经除尘后排放；
在第1座预热器蓄热材料加温到设计温度、完成一轮“加热”后，经过切换阀门，高温冷却空气50通过管道进入第2座蓄热式预热炉202，加热第2座预热炉蓄热室的蓄热材料；同时，冷的助燃空气22从下部进入第1座蓄热式预热炉202，经蓄热室的蓄热材料加热后从蓄热材料上部排出，进入混风室24；混风室还接入冷的助燃空气和来自加热炉201的废烟气，用于调节助燃空气22的温度，助燃空气22以一个固定的温度从混风室24进入蓄热式加热炉201。
高温冷却空气50携带的少量的粉尘被预热炉202下部的收集机构收集起来，在日常设备维护时清理出预热炉。
对于所属技术领域的技术人员而言，随着技术的发展，本发明构思可以不同方式实现。本发明的实施方式并不仅限于以上描述的实施例，而且可在权利要求的范围内进行变化。

Claims (10)

  1. 一种全回收CO 2石灰窑装置，包括窑体和加热炉组，其特征在于：窑体内不带燃烧器，加热炉组将CO 2加热至设定温度后形成CO 2热风送入到窑体中对预热后的矿料进行煅烧，矿料煅烧时产生的CO 2与CO 2热风混合，向上对窑体上部的矿料进行预热并在窑体上部被抽出，经收集处理后的部分CO 2再次进入加热炉组，加热至设定温度后返回窑体，煅烧后的石灰成品经空气冷却后从窑体底部排出。
  2. 如权利要求1所述的一种全回收CO 2石灰窑装置，其特征在于，所述窑体包括上料机构和出料机构，窑体的工作区域自上而下包括预热段、煅烧段、冷却段，窑体内设置有内套筒，在窑体内壁和内套筒外壁之间形成物料移动的物料通道，所述物料通道截面的总宽度为通径，矿料从上料机构进入窑体，沿物料通道从预热段到煅烧段，成品沿物料通道经过冷却段，最后从出料机构排出窑体，窑体煅烧段侧壁上设置有CO 2热风进口，内套筒位于冷却段的上部设置有进风口，冷却空气从窑体的下部进入到窑体与内套筒之间的物料通道，对石灰石成品冷却后从进风口进入到内套筒内并从顶部被抽出窑体。
  3. 如权利要求2所述的一种全回收CO 2石灰窑装置，其特征在于，所述物料通道在煅烧段和冷却段之间具有过渡段，过渡段通径减小，物料沿物料通道在过渡段的移动速度较快，形成料封层。
  4. 如权利要求3所述的一种全回收CO 2石灰窑装置，其特征在于，所述窑体的物料通道优选在预热段下部、煅烧段中部的通径较大、在煅烧段下部通径减小，经过过渡段后，在冷却段的通径变大。
  5. 如权利要求4所述的一种全回收CO 2石灰窑装置，其特征在于，所述窑体的物料通道在煅烧段中部的最大通径与煅烧段下部的最小通径的比值优选范围是2～3.5，所述窑体的物料通道在冷却段的最大通径与过渡段通径的比值优 选范围是2～3.5。
  6. 如权利要求3所述的一种全回收CO 2石灰窑装置，其特征在于，内套筒内部设置有降尘装置，其下部有粉尘收集装置，其上部与引风管连接，引风管用于将高温的冷却空气从窑体上部抽出，被抽出的高温冷却空气用于加热助燃气体。
  7. 如权利要求1所述的一种全回收CO 2石灰窑装置，其特征在于，加热炉组包括蓄热式加热炉、蓄热式预热炉和混风室，在蓄热式加热炉的烧炉周期里，低热值的气体燃料和来自混风室的助燃空气进入燃烧器燃烧，生成的热烟气加热蓄热室的蓄热材料；在蓄热式加热炉的送风周期里，CO 2气体从加热炉蓄热室下部进入加热炉，经蓄热材料加热后从蓄热室上部的热风出口排出加热炉并送入窑体中。
  8. 如权利要求7所述的一种全回收CO 2石灰窑装置，其特征在于，从窑体顶部被抽出的高温冷却空气用于加热蓄热式预热炉内部的蓄热材料，加热后的蓄热材料再用于加热助燃空气，被加热的助燃空气从蓄热材料上部排出进入所述混风室，混风室将所述助燃空气调整到设定的温度，再将其送至所述蓄热式加热炉。
  9. 如权利要求1所述的一种全回收CO 2石灰窑装置，其特征在于，CO 2热风的设定温度值的范围是800℃～1200℃，优选是850℃～1150℃。
  10. 一种全回收CO 2制备工业用石灰的工艺方法，其特征在于，将CO 2加热至设定温度后形成CO 2热风送入到窑体中对预热后的矿料进行煅烧，矿料煅烧时产生的CO 2与CO 2热风混合，向上对窑体上部的矿料进行预热并在窑体上部被抽出，经收集处理后的部分CO 2再次进入加热炉组，加热至设定温度后返回窑体，煅烧后的石灰石成品经空气冷却后从窑体底部排出。
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