• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention discloses a method and apparatus for processing liquid nitrogen scrubbing exhaust gases and belongs to the field of energy sources and environmental protection. The method of the present invention divides air into upper air, middle air and lower air, respectively, the upper air, the middle air and the lower air each being mixed with a liquid nitrogen scrubbing exhaust gas and then performing heat exchange, then the upper air middle air and the lower air successively flow through an upper part, a middle part and a lower part of an incinerator to perform first partial combustion, second partial combustion and full combustion, respectively, and lower exhaust gas is discharged through a lower gas exhaust pipe and supplied to a coal dust dryer. The method of the present invention has the advantages of simple technology, low investment, operating costs and low energy consumption, simple and convenient operation, safety and high combustion efficiency.
    公开号:BE1026545B1
    申请号:E20195410
    申请日:2019-06-25
    公开日:2020-07-10
    发明作者:Ping Ning；Liangtao Yin；Qiulin Zhang；Lijuan Jia；Zaifei Yin
    申请人:Univ Kunming Science & Tech；
    IPC主号:
    专利说明:

    METHOD AND DEVICE FOR PROCESSING LIQUID NITROGEN WASHES
    FIELD OF THE INVENTION
    The present invention relates to a method and an apparatus for processing liquid nitrogen scrubbing exhaust gases and belongs to the field of energy sources and environmental protection.
    BACKGROUND OF THE INVENTION
    In modern coal chemistry production, coal is used as a raw material, mostly pure oxygen gasification is used, the oxygen content is improved by air separation, and at the same time liquid nitrogen can be made available for washing traces of CO in synthesis gas. At a lower temperature, the liquid nitrogen is used as the absorbent, and components of CO, Ar and CH4 contained in the raw synthesis gas, the boiling points of which are close to the boiling point of nitrogen, are absorbed by the liquid nitrogen and then the processed raw synthesis gas after performing cold recovery is discharged from a system in a gas state, the discharged gas being called liquid nitrogen scrubbing exhaust gas. The liquid nitrogen scrubbing exhaust gas contains CO, H 2 , CH 4 , Ar and N 2 , its gas components are clean and contain no components that easily poison the catalyst, and the components of the liquid nitrogen scrubbing exhaust gas are as shown in Table 1.
    Table 1: Components of the liquid nitrogen scrubbing exhaust gas
    H 2 content in% by volume N 2 content in% by volume CO in contentVol .-% Ar in contentVol .-% CH4 content inVol .-% 1.6 to 1.9 80 to 85 12 to 16 0.1 to 0.4 0 to 0.4 As in Tabel e 1 shown contains t the liquid nitrogen scrubbing exhaust gas with combustible gas
    a calorific value of 1,700 to 2,250 kJ / m 3 ; however, the liquid nitrogen scrubbing exhaust gas contains no oxygen, so that although the CO content is relatively high, air must be supplied in the direct combustion of the liquid nitrogen scrubbing exhaust gas in order to be very unstable. In addition, some companies cannot directly emit liquid nitrogen scrubbing waste gas, which wastes energy and pollutes the environment. There are some companies that use shelled coal gasification technology for gasification, where coal dust must be ground and inert dried before the coal is fed to a gasification furnace to be burned; when the original construction is operated normally, synthesis gas and liquid nitrogen scrubbing exhaust gas are fed into a hot blast furnace to be burned and used as a drying heat source; and to ensure the safety of the system, the synthesis gas (which contains 80% H 2 and N 2 ) must contain 3,000 to 4,000 Nm 3 / h as additional fuel
    BE2019 / 5410 can be added. The introduced shell carbon gasification technology does not take over the construction and devices used by the liquid nitrogen scrubbing exhaust gas and uses the synthesis gas for combustion, with synthetic ammonia being burned unnecessarily, and more than 1 ton of synthetic ammonia is burned every hour, so more annually than 7,000 tons of the synthetic ammonia are burned down, which is very wasteful.
    In order to meet environmental protection requirements, the liquid nitrogen scrubbing exhaust gas can currently only be supplied to a thermoelectric boiler for mixed combustion; however, after the liquid nitrogen scrubbing exhaust gas is supplied to the thermoelectric boiler, the energy consumption of the thermoelectric boiler increases, and the main problem is that large amounts of thermal energy are removed by an induced draft so that the thermal energy is not recovered, but the thermal efficiency of the boiler is reduced. Therefore, in most cases, most of the liquid nitrogen scrubbing exhaust gas can actually only be expanded by adding fuel and using an auxiliary fuel combustion process, thereby wasting the energy.
    SUMMARY
    An object of the present invention is to provide a liquid nitrogen scrubbing exhaust gas processing method in which the liquid nitrogen scrubbing exhaust gas is burned at a relatively low temperature by a special liquid nitrogen scrubbing exhaust gas catalyst in which the temperature requirements of the catalyst are satisfied , and in which the thermal energy is fully used and recycled to achieve the goal of saving energy and reducing emissions.
    The present invention is achieved by the following technical solutions.
    A processing method for liquid nitrogen scrubbing exhaust gas comprises in particular the following steps:
    (1) after air blown from an air blower 4 has passed a bag chamber, dust in the air is removed and the air is divided into upper air, middle air and lower air; Liquid nitrogen scrubbing exhaust gas and the upper air enter an intermediate pipe part of a heat exchanger 1, and fuel gas discharged through an upper gas outlet pipe of an incinerator 2 (the temperature of which is 490 to 500 ° C) enters a pipe section of the heat exchanger 1 for heat exchange with the upper one Air and the liquid nitrogen scrubbing exhaust gas, so that the temperature of the liquid nitrogen scrubbing exhaust gas and the temperature of the upper air are increased from room temperature to 250 to 260 ° C; and then the processed mixed gas enters a gas distributor 9 of an incinerator through an upper gas inlet pipe and then uniformly enters an upper catalyst layer to be a
    BE2019 / 5410 carry out first partial combustion, in which the temperature of the catalyst layer is controlled in a range from 520 to 530 ° C;
    2) Upper fuel gas, which is discharged after the completion of the first partial combustion, is discharged through an upper gas outlet pipe and then carries out heat exchange in the heat exchanger 1 so that the temperature of the upper fuel gas is reduced to 230 to 240 ° C, and the upper one Fuel gas is mixed with the middle air, enters the gas distributor 9 at a middle portion of the incinerator through a middle gas inlet pipe, and then smoothly enters a middle catalyst layer to carry out a second partial combustion in which the temperature of the middle catalyst layer is in a range controlled from 480 to 500 ° C; and (3) medium fuel gas, which is discharged after the completion of the second partial combustion, is discharged through a central gas outlet pipe and then flows through a waste heat boiler 3 to transfer the thermal energy to boiler water, to saturated steam of 0.4 MPa for discharge to the outside generate, wherein the temperature of the average fuel gas is reduced to 220 to 230 ° C after performing the heat exchange; the processed middle fuel gas is mixed with the lower air, enters the gas distributor 9 at a lower portion of the incinerator through a lower gas inlet pipe, and then smoothly enters a lower catalyst layer to be completely burned there, the temperature of the catalyst layer in is controlled in a range of 400 to 480 ° C; and lower exhaust gas is discharged through a lower gas outlet pipe and supplied to a coal dust dryer, the lower air being excessively added according to a ratio of liquid nitrogen scrubbing exhaust gas to air of 0.25 to 0.3.
    In the method of the present invention, the amount of added air, according to the contents of C co, Ch2 and C CH 4 and x the required conversion rate C o, xm and x CH 4 of CO, H2 and CH4 in the liquid nitrogen wash exhaust gas or be calculated on the fuel gas;
    The amount of dry air (L 0 ) m 3 required for the combustion of the liquid nitrogen scrubbing exhaust gas is per m 3 :
    r Û. 5 (X ® Ckrj) 4 0.5 (X ΤΤΊ ® C TT-.) 4 2 (X --TTJ ® C ƒ.ΓΤ j) 3. / 3 ...,. ,
    L = -----—---—--------—--- Si ------—--- t / LL m air / m liquid nitrogen wash exhaust gas in the present Invention is the amount of liquid nitrogen scrubbing exhaust gas 30,000 m 3 / h; and preferably the addition amount of the upper air is 4,000 to 4,300 m 3 / h, the addition amount of the middle air is 2,500 to 3,000 m 3 / h and the addition amount of the lower air is 7,800 to 8,500 m 3 / h.
    An apparatus used by the method of the present invention comprises a heat exchanger 1, an incinerator 2, a waste heat boiler 3 and an air blower 4; the
    BE2019 / 5410
    Liquid nitrogen scrubbing exhaust gas is connected to a lower intermediate pipe part of the heat exchanger 1, an upper section of an intermediate pipe part of the heat exchanger 1 is connected to an upper part of the incinerator 2, an upper gas outlet pipe of the incinerator 2 is connected to an upper section of an inner pipe part of the heat exchanger 1 Connection, a bottom of the inner tube part of the heat exchanger 1 is connected to a central inlet of the incinerator 2, a central outlet of the incinerator 2 is connected to an upper intermediate tube part of the waste heat boiler 3, a lower intermediate tube part of the waste heat boiler 3 is connected to a lower inlet of the incinerator 2 in connection, the upper intermediate pipe part of the waste heat boiler 3 is connected to the lower intermediate pipe part of the waste heat boiler 3 via a high-temperature control valve, and a lower outlet of the incinerator 2 is connected via a high-temperature shut-off valve a user dryer in connection; and a lower outlet of the incinerator 2 communicates with a user dryer through a high temperature butterfly valve; and the air blower 4 is connected to the lower intermediate pipe part of the heat exchanger 1 via a control valve, the air blower 4 is connected to the upper inner pipe part of the heat exchanger 1 via a control valve, and the air blower 4 is connected to the upper intermediate pipe part of the waste heat boiler 3 via a control valve in connection.
    The incinerator 2 comprises a cylindrical shell 5, an upper part 6, a middle part 7, a lower part 8, gas distributor 9, gas outlet pipes 10, temperature detection holes 11, supports 12, sieve plates 13, refractory balls 14, stainless steel wire mesh 15, catalysts 16 and catalyst charging and Unloading holes 17; the cylindrical shell 5 is successively divided from top to bottom into the upper part 6, the middle part 7 and the lower part 8, the upper part 6 and the middle part 7 are separated using an elliptical head 118, and the middle part 7 and the lower part 8 are below Using an elliptical head II19 separately; the upper part 6, the middle part 7 and the lower part 8 are each provided with a contact medium layer; the contact medium layer contains the sieve plate 13, the refractory balls 14, the stainless steel wire mesh 15 and the catalyst 16, the sieve plate 13 is fixed by the lower supports 12 located underneath, a layer of refractory balls 14 is paved onto the sieve plate, the stainless steel wire mesh 15 is on the refractory balls 14 placed, and the catalyst 16 is arranged on the stainless steel wire mesh 15; a side wall of the upper part 6, a side wall of the middle part 7 and a side wall of the lower part 8 are each provided with the catalyst loading holes 17 and two temperature detection holes 11, namely an upper temperature detection hole and a lower temperature detection hole, and the temperature detection holes 11 are on one side arranged the contact medium layer; and a sidewall above the contact medium layer is with an inlet tube 5
    BE2019 / 5410
    Gas distributor 9 provided, while a side wall below the contact medium layer is provided with a gas outlet pipe 10 and an outer wall of the incinerator is provided with a heat insulation layer in order to prevent the device from dissipating the thermal energy.
    Preferably, in the present invention, the values of the thickness of the catalyst 16 of the upper part 6 and the thickness of the catalyst 16 of the central part 7 are in a range of 450 to 550 mm and the values of the thickness of the catalyst 16 of the lower part 8 are in a range of 1,100 to 1,300 mm.
    In the present invention, the cylindrical shell 5 is preferably made of a heat-resistant stainless steel plate.
    In the present invention, the thickness of the refractory ball 14 is preferably 60 mm, and its diameter Φ is in a range of 20 to 30 mm.
    The method of the present invention can also be applied to drying coal dust or other waste heat recovery.
    The catalyst of the present invention is a catalyst made in accordance with Chinese Patent Application No. 201610705294.7 entitled SUPPORTED CATALYST APPLIED TO OXYGEN-DEFICIENT COMBUSTION OF LOW-CONCENTRATION COMBUSTIBLE COMPONENT IN LIQUID NITROGEN WASH EXHAUST GAS AS WELL AS ANDPPARATION METHOD APPLICATION METHOD , and all catalysts made by the process can be applied to the present invention.
    The present invention develops a catalytic liquid nitrogen scrubbing exhaust gas combustion technology according to the properties of a specific combustion catalyst for combustible substances having a low concentration contained in the liquid nitrogen scrubbing exhaust gas and fulfills the requirement to achieve full heat recovery by introducing the shell carbon gasification technology with an annual production of synthetic ammonia of 500,000 Tons for performing low temperature combustion of the liquid nitrogen scrubbing exhaust gas; and the present invention is also applied to drying coal dust or other waste heat recovery.
    The principle of the catalytic combustion technology of the present invention is as follows:
    in a combustion process, the catalyst does not change the original chemical equilibrium and only changes the chemical reaction rate, and the catalytic combustion is as follows: after a catalytic reaction starts on the surface of the catalyst, the fuel mixtures involved in the reaction react at a relatively low level
    BE2019 / 5410
    Temperature, the heat energy released during the reaction can increase the temperature of the combustion gas, so that heat recovery is achieved.
    Combustibles CO, H 2 , CH 4 and the like in the liquid nitrogen scrubbing off gas produce the following reactions with oxygen in the presence of the catalyst, and the heat is released:
    CO + 0.5 O 2 = CO 2 + A Hr (1) _ 0.6384 xi
    - where the conversion rate of CO is: (2) where xco = the combustion conversion rate of CO in the liquid nitrogen scrubbing exhaust gas, in%;
    where t = the temperature of a catalyst layer, in ° C; and where C co = the content of CO in the liquid nitrogen scrubbing exhaust gas before combustion, in%.
    H 2 + O 2 = H 2 O + Δ Hr (3)
    Û.2736xr + 22 JC TT - --------------------- where the conversion rate of H 2 is as follows: (4) where x h2 = the combustion conversion rate of H 2 in the liquid nitrogen scrubbing exhaust gas, in%;
    where t = the temperature of the catalyst layer, in ° C; and where C h2 = the H 2 content in the liquid nitrogen scrubbing exhaust gas before combustion, in%.
    CH 4 + O 2 = CO 2 + H 2 O + Δ Hr (5) _ 4.202 ^ -380 where the conversion rate of CH 4 is as follows: (6) where x C H4 = the combustion conversion rate of CH 4 in the liquid nitrogen scrubbing exhaust gas, in %;
    where t = the temperature of the catalyst layer, in ° C; and where Cch4 = the content of CH 4 in the liquid nitrogen scrubbing exhaust gas before combustion, in%.
    The advantageous effects of the present invention are as follows:
    the annual output of 500,000 tons of synthetic ammonia corresponds to the comparative standard.
    (1) remarkable improvement in energy recovery: 2.2172 * 10 6 m 3 liquid nitrogen scrubbing waste gas is recovered annually; annually, 317,946.48 million kJ
    BE2019 / 5410
    Heat energy recovered; and this recovered thermal energy is converted into 10,850 tons of standard coal a year;
    (2) Reduction of energy consumption of synthetic ammonia: 21.7 kg of coal consumption per ton of synthetic ammonia are reduced;
    (3) Reduction of the cost of ammonia synthesis: If the price of the liquid nitrogen scrubbing exhaust gas is calculated according to the calorific value, 7,750 tons of ammonia synthesis are generated, with the market price for ammonia synthesis being 2,500 yuan per ton, so the total price for the ammonia synthesis accordingly Is 19.375 million yuan and the price of the liquid nitrogen scrubbing exhaust gas is 87.37 yuan per 1,000 cubic meters.
    (4) Significant reduction in CO 2 emissions: 28,644 tons of CO 2 are saved annually; and (5) simple technology, low investment, operating costs and energy consumption, simple and convenient operation, safety and high combustion efficiency.
    BRIEF DESCRIPTION OF THE DRAWINGS
    FIG. 1 is a flow diagram of a technique of the present invention; and
    FIG. 2 is a schematic structural diagram of an incinerator of the present invention.
    In FIG. 1, 1 = heat exchanger, 2 = incinerator, 3 = waste heat boiler and 4 = air blower.
    In FIG. 2, 5 = cylindrical shell, 6 = upper part, 7 = middle part, 8 = lower part, 9 = gas distributor, 10 = gas outlet pipe, 11 = two temperature detection holes, namely an upper temperature detection hole and a lower temperature detection hole, 12 = support, 13 = sieve plate, 14 = fireproof ball, 15 = stainless steel wire mesh, 16 = catalyst, 17 = catalyst loading or unloading hole, 18 = elliptical head I and 19 = elliptical head II.
    DETAILED DESCRIPTION
    The present invention will be described in more detail with reference to the accompanying drawings and specific embodiments, but the scope of the present invention is not limited to the content described.
    Embodiment 1
    A processing method for liquid nitrogen scrubbing exhaust gas comprises in particular the following steps:
    (1) after air blown from an air blower 4 has passed a bag chamber, dust is removed from the air and the air is divided into upper air, middle air and lower air; Liquid nitrogen scrubbing exhaust gas is expelled from a liquid nitrogen scrubber manifold through a valve into a combustion system manifold and flows through one
    BE2019 / 5410
    Liquid nitrogen scrubbing exhaust gas flow meter (LOI) under the control of an electric butterfly valve, then the liquid nitrogen scrubbing exhaust gas with the upper air enters an intermediate pipe portion of a heat exchanger 1, and fuel gas (whose temperature is 490 to 500 ° C) is discharged through an upper gas outlet pipe of a combustion furnace 2 ) enters an inner tube part of the heat exchanger 1 for heat exchange with the upper air and the liquid nitrogen scrubbing exhaust gas, so that the temperature of the liquid nitrogen scrubbing exhaust gas and the temperature of the upper air is increased from room temperature to 250 to 260 ° C; and then the processed mixed gas enters a gas distributor of an incinerator through an upper gas inlet pipe and then uniformly enters an upper catalyst layer to perform a first partial combustion in which the temperature of the catalyst layer is controlled in a range of 520 to 530 ° C ( wherein the temperature of the upper catalyst layer can be controlled by controlling an opening degree of an upper air control valve to adjust the amount of air), and the first partial combustion burns about 20 to 25% of the CO and about 70 to 80% of the H 2 ;
    (2) Upper fuel gas, which is discharged after completion of the first partial combustion, is discharged through an upper gas outlet pipe and then performs heat exchange in the heat exchanger 1 so that the temperature of the upper fuel gas is reduced to 230 to 240 ° C, and that upper fuel gas is mixed with the middle air, enters the manifold at a middle portion of the incinerator through a middle gas inlet pipe, and then smoothly enters a middle catalyst layer to perform a second partial combustion in which the temperature of the middle catalyst layer is in a range is controlled from 480 to 500 ° C (wherein the temperature of the middle catalyst layer can be controlled by controlling an opening degree of a middle air control valve to adjust the amount of air), and the second partial combustion burns about 30 to 40% of the CO;
    (3) Fuel gas discharged after the completion of the second partial combustion is discharged through a central gas outlet pipe and then flows through a waste heat boiler 3 to transfer the thermal energy to boiler water to generate saturated steam of 0.4 MPa for discharge to the outside , wherein the temperature of the medium fuel gas is reduced to 220 to 230 ° C after performing the heat exchange; the processed medium fuel gas is mixed with the lower air, enters a lower manifold of the incinerator through a lower gas inlet pipe, and then evenly enters a lower catalyst layer to be completely burned there, the temperature of the catalyst layer being in a range of 400 controlled up to 480 ° C (wherein the temperature can be controlled by controlling an opening degree of a lower fuel gas high temperature damper to adjust the amount of the middle fuel gas); and lower exhaust gas is discharged through a lower gas outlet pipe and to one
    BE2019 / 5410
    Coal dust dryer supplied (which requires the amount of CO to be less than 200 ppm), with the lower air being excessively added according to a ratio of the liquid nitrogen scrubbing exhaust gas to the amount of air of 0.25 to 0.3 (it should be ensured that the content of O 2 is in a range of 3.0 to 5.0%).
    In the embodiment, the components of the liquid nitrogen scrubbing exhaust gas are as follows: 1.92% H 2 , 6.65% CO, 1.08% CH 4 and 90.35% N 2 ; if the processing amount of the liquid nitrogen scrubbing exhaust gas is 28,000 m 3 / h, the total air amount is 13,000 m 3 / h and the by-product vapor amount is 5 tons per hour. In the embodiment, the addition amount of the upper air is 3,080 m 3 / h, the addition amount of the middle air is 3,024 m 3 / h and the addition amount of the lower air is 6,896 m 3 / h.
    An apparatus used by the method in the embodiment (as shown in FIG. 1) includes a heat exchanger 1, an incinerator 2, a waste heat boiler 3, and an air blower 4; the liquid nitrogen scrubbing exhaust gas is connected to a lower intermediate pipe part of the heat exchanger 1, an upper section of an intermediate pipe part of the heat exchanger 1 is connected to an upper part of the incinerator 2, an upper gas outlet pipe of the incinerator 2 is connected to an upper section of an inner pipe part of the heat exchanger 1 in connection, a bottom of the inner tube part of the heat exchanger 1 is connected to a middle inlet of the incinerator 2, a middle outlet of the incinerator 2 is connected to an upper intermediate tube part of the waste heat boiler 3, a lower intermediate tube part of the waste heat boiler 3 is connected to a lower inlet of the Incinerator 2 in connection, the upper intermediate pipe part of the waste heat boiler 3 is connected to the lower intermediate pipe part of the waste heat boiler 3 via a high-temperature control valve, and a lower outlet of the incinerator 2 is connected via a high-temperature shut-off valve in connection with a user dryer; and the air blower 4 is connected to the lower intermediate pipe part of the heat exchanger 1 via a control valve, the air blower 4 is connected to the upper tubular pipe part of the heat exchanger 1 via a control valve, and the air blower 4 is connected to the upper intermediate pipe part of the waste heat boiler 3 via a control valve in connection.
    The structure of the incinerator 2 in the embodiment is as shown in FIG. 2 shown: the incinerator 2 comprises a cylindrical shell 5, an upper part 6, a middle part 7, a lower part 8, gas distributor 9, gas outlet pipes 10, temperature detection holes 11, supports 12, sieve plates 13, refractory balls 14, stainless steel wire mesh 15, catalysts 16 and catalyst drawer - or unloading holes 17; the cylindrical shell 5 is successively divided from top to bottom into the upper part 6, the middle part 7 and the lower part 8, the upper part 6 and the middle part 7 are separated using an elliptical head 118, and the middle part 7 and the lower part 8 are below Using an elliptical head II19 separately; the upper part 6, the middle part 7 and the
    BE2019 / 5410
    Lower part 8 are each provided with a contact medium layer; the contact medium layer contains the sieve plate 13, the refractory balls 14, the stainless steel wire mesh 15 and the catalyst 16, the sieve plate 13 is fixed by the supports 12 located underneath, a layer of refractory balls 14 is paved onto the sieve plate, the stainless steel wire mesh 15 is on the 5 refractory Balls 14 placed, and the catalyst 16 is arranged on the stainless steel wire mesh 15; a side wall of the upper part 6, a side wall of the middle part 7 and a side wall of the lower part 8 are each provided with the catalyst loading holes 17 and two temperature detection holes 11, namely an upper temperature detection hole and a lower temperature detection hole, and the temperature detection holes 11 are 10 in one Side of the contact medium layer arranged; a side wall above the
    Contact medium layer is provided with an inlet tube gas distributor 9, while a side wall below the contact medium layer is provided with a gas outlet tube 10 and an outer wall of the incinerator is provided with a heat insulation layer to prevent the device from dissipating the thermal energy; the cylindrical shell 5 is made of a 15 heat-resistant stainless steel plate; the thickness of the refractory ball 14 is 60 mm and its diameter Φ is in a range of 20 mm; and the thickness of the catalyst 16 of the upper part 6 and the thickness of the catalyst 16 of the middle part 7 are 500 mm, and the thickness of the catalyst 16 of the lower part 8 is 1200 mm.
    权利要求:
    Claims (7)
    [1]
    (1) after air blown from an air blower (4) has passed a bag chamber, dust is removed from the air and the air is divided into upper air, middle air and lower air; Liquid nitrogen scrubbing exhaust gas and the upper air enter an intermediate pipe part of a heat exchanger (1), and fuel gas discharged through an upper gas outlet pipe of an incinerator (2) enters an inner pipe part of the heat exchanger (1) for heat exchange with the upper air and the liquid nitrogen scrubber Exhaust gas, so that the temperature of the liquid nitrogen scrubbing exhaust gas and the temperature of the upper air is increased from room temperature to 250 to 260 ° C; and then the processed mixed gas enters a gas manifold (9) through an upper gas inlet pipe at an upper portion of an incinerator and then uniformly enters an upper catalyst layer to perform a first partial combustion, the temperature of the catalyst layer being in a range of 520 to 530 ° C is controlled;
    1. A method for processing liquid nitrogen scrubbing exhaust gas, which comprises in particular the following steps:
    [2]
    2. The method for processing liquid nitrogen scrubbing exhaust gas according to claim 1, wherein
    BE2019 / 5410 the amount of liquid nitrogen scrubbing exhaust gas is measured in a range from 28,000 to 30,000 m 3 / h; the addition amount of the upper air is 4,000 to 4,300 m 3 / h, the addition amount of the middle air is 2,500 to 3,000 m 3 / h, and the addition amount of the lower air is 7,800 to 8,500 m 3 / h.
    (2) upper fuel gas, which is discharged after completion of the first partial combustion, is discharged through an upper gas outlet pipe and then carries out heat exchange in the heat exchanger (1), so that the temperature of the upper fuel gas is reduced to 230 to 240 ° C, and the upper fuel gas is mixed with the middle air, enters the gas distributor (9) at a middle portion of the incinerator through a middle gas inlet pipe, and then smoothly enters a middle catalyst layer to perform a second partial combustion, the temperature of the middle Catalyst layer is controlled in a range of 480 to 500 ° C; and (3) medium fuel gas, which is discharged after the completion of the second partial combustion, is discharged through a medium gas outlet pipe and then flows through a waste heat boiler (3) to transfer the thermal energy to boiler water to produce saturated steam of 0.4 MPa for discharge to generate outside, the temperature of the average fuel gas is reduced to 220 to 230 ° C after performing the heat exchange; the processed middle fuel gas is mixed with the lower air, enters the gas manifold (9) at a lower portion of the incinerator through a lower gas inlet pipe, and then smoothly enters a lower catalyst layer to be completely burned there, and becomes lower exhaust gas ejected through a lower gas outlet pipe and supplied to a pulverized coal dryer with the temperature of the catalyst layer being controlled in a range of 400 to 480 ° C, and the lower air is extracted according to a quantitative ratio of liquid nitrogen scrubbing exhaust gas to air of 0.25 to 0.3 added excessively.
    [3]
    3. An apparatus used by the liquid nitrogen scrubbing exhaust gas processing method, comprising a heat exchanger (1), an incinerator (2), a waste heat boiler (3), and an air blower (4); wherein the liquid nitrogen scrubbing exhaust gas communicates with a lower intermediate pipe part of the heat exchanger (1), an upper section of an intermediate pipe part of the heat exchanger (1) communicates with an upper section of the incinerator (2), an upper gas outlet pipe of the incinerator (2) an upper section of an inner pipe part of the heat exchanger (1) communicates, a bottom of the inner pipe part of the heat exchanger (1) communicates with a central inlet of the incinerator (2), a central outlet of the incinerator (2) with an upper intermediate pipe part of the waste heat boiler (3) is connected, a lower intermediate pipe part of the waste heat boiler (3) is connected to a lower inlet of the incinerator (2), the upper intermediate pipe part of the waste heat boiler (3) is connected to the lower intermediate pipe part of the waste heat boiler (3) via a high-temperature control valve stands, and a lower outlet of the incinerator (2) over a high temperature butterfly valve communicates with a user dryer; and the air blower (4) is connected to the lower intermediate pipe part of the heat exchanger (1) via a control valve, the air blower (4) is connected to the upper inner pipe part of the heat exchanger (1) via a control valve, and the air blower (4) is connected to the upper intermediate pipe section of the waste heat boiler (3) via a control valve.
    [4]
    4. The device according to claim 3, wherein the incinerator (2) a cylindrical shell (5), an upper part (6), a middle part (7), a lower part (8), gas distributor (9), gas outlet pipes (10), temperature detection holes ( 11), supports (12), sieve plates (13), refractory balls (14), stainless steel wire mesh (15), catalysts (16) and catalyst loading or unloading holes (17); the cylindrical shell (5) being successively divided from top to bottom into the top (6), middle (7) and bottom (8), the top (6) and middle (7) using an elliptical head I (18) are separated, and the middle part (7) and the bottom part (8) are separated using an elliptical head II (19); wherein the upper part (6), the middle part (7) and the lower part (8) are each provided with a contact medium layer; wherein the contact medium layer contains the sieve plate (13), the refractory balls (14), the stainless steel wire mesh (15) and the catalyst (16), the sieve plate (13) being fixed by the lower supports (12) underneath, a layer of refractory Balls (14) is paved on the sieve plate, the stainless steel wire mesh (15) on the refractory balls (14)
    BE2019 / 5410 is placed, and the catalyst (16) is arranged on the stainless steel wire mesh (15); wherein a side wall of the upper part (6), a side wall of the middle part (7) and a side wall of the lower part (8) are each provided with the catalyst loading or unloading holes (17) and two temperature detection holes (11), namely an upper temperature detection hole
    [5]
    5. The device according to claim 4, wherein the thickness of the catalyst (16) of the upper part (6) and the thickness of the catalyst (16) of the central part (7) are in a range from 450 to 550 mm and the thickness of the catalyst (16) of the lower part (8) is in a range from 1,100 to 1,300 mm.
    15
    [6]
    6. The device according to claim 4, wherein the cylindrical sleeve (5) is preferably made of a heat-resistant stainless steel plate.
    5 and a lower temperature detection hole, and wherein the temperature detection holes (11) are arranged on one side of the contact medium layer; and wherein a side wall above the contact medium layer is provided with an inlet pipe gas distributor (9), while a side wall below the contact medium layer is provided with a gas outlet pipe (10) and an outer wall of the incinerator is provided with a heat insulation layer to
    10 prevent the device from dissipating the thermal energy.
    [7]
    7. The device according to claim 4, wherein the thickness of the refractory ball (14) is preferably 60 mm, and its diameter Φ is in a range of 20 to 30 mm.
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    同族专利:
    公开号 | 公开日
    CN109163338A|2019-01-08|
    BE1026545A1|2020-03-11|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    CN103486578B|2013-09-16|2015-12-09|云南天安化工有限公司|The device and method of the tail gas catalyzed burning of a kind of liquid nitrogen washing|
    CN106268740A|2016-08-23|2017-01-04|昆明新光能源环保科技有限公司|A kind of loaded catalyst of low concentration combustible component anoxycausis and its preparation method and application in liquid nitrogen washing tail gas|
    CN103769164B|2014-01-10|2016-01-20|浙江工业大学|A kind of stainless steel cloth load platinum catalyst and application thereof|
    CN107478732B|2016-06-07|2021-01-01|中国石油化工股份有限公司|Volatile organic compound catalytic combustion evaluation device and test method|
    CN107490012A|2017-07-28|2017-12-19|北京化工大学|A kind of System and method for of VOCs catalysis oxidations|CN110285435B|2019-05-29|2020-10-02|昆明理工大学|Liquid nitrogen wash tail gas high-temperature catalytic combustion device and method|
    法律状态:
    2020-08-26| FG| Patent granted|Effective date: 20200710 |
    优先权:
    申请号 | 申请日 | 专利标题
    CN201810666089.3A|CN109163338A|2018-06-26|2018-06-26|A kind of method and device handling liquid nitrogen washing tail-gas|
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