CN116603365A - A skid-mounted coalbed methane MDEA deep decarbonization absorption device and method - Google Patents
A skid-mounted coalbed methane MDEA deep decarbonization absorption device and method Download PDFInfo
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Abstract
Description
技术领域technical field
本发明涉及一种煤层气脱碳装置，尤其涉及一种撬装式煤层气MDEA深脱碳吸收装置及方法。The invention relates to a coal bed gas decarbonization device, in particular to a skid-mounted coal bed gas MDEA deep decarbonization absorption device and method.
背景技术Background technique
煤层气是一种优质洁净的能源，立方米纯煤层气的热值相当于汽油、标准煤，其热值与天然气相当，可以与天然气混输混用，而且燃烧后很洁净，几乎不产生任何废气，是上好的工业、化工、发电和居民生活燃料，在我国目前能源结构依然以煤为主的状况下，开发利用煤层气资源具有重要现实意义。煤层气是一种对生态环境破坏性极强的温室气体，其温室效应约为二氧化碳的21倍，若直接排放到大气中，将会对环境造成极大的破坏。煤层气的综合利用对于改善和优化我国日趋严峻的能源结构，改善矿井安全生产条件，保障煤矿安全生产、降低煤矿生产成本、减少大气污染具有重要的经济与社会效益。但是，在煤层气开采过程中会含有较多的CO2在后续的液化过程中引起固化。这对天然气的处理过程和天然气的质量造成影响。因此，必须对煤层气进行脱碳处理，使煤层气中CO2含量在50ppm以下。Coalbed methane is a high-quality and clean energy. The calorific value of a cubic meter of pure coalbed methane is equivalent to that of gasoline and standard coal, and its calorific value is equivalent to that of natural gas. , is a good fuel for industry, chemical industry, power generation and residential life. Under the condition that my country's current energy structure is still dominated by coal, the development and utilization of coalbed methane resources has important practical significance. Coal bed methane is a kind of greenhouse gas that is extremely destructive to the ecological environment. Its greenhouse effect is about 21 times that of carbon dioxide. If it is directly discharged into the atmosphere, it will cause great damage to the environment. The comprehensive utilization of coalbed methane has important economic and social benefits for improving and optimizing my country's increasingly severe energy structure, improving mine safety production conditions, ensuring coal mine safety production, reducing coal mine production costs, and reducing air pollution. However, during the mining process of coalbed methane, there will be more CO2 which will cause solidification in the subsequent liquefaction process. This affects the gas processing process and the quality of the gas. Therefore, the coalbed methane must be decarbonized so that the CO2 content in the coalbed methane is below 50ppm.
在众多煤层气脱碳技术中，化学吸收法以其吸收速率快，吸收容量大，脱除效率高等优点而被广泛釆用。事实上，化学吸收法不仅仅在脱碳工艺上有所使用，在一些工业脱除酸性气体上该技术也早已有所应用，其技术成熟度也相对较高。但是由于化学吸收法在解吸过程中能热损耗严重，因此提出一个完整的优化节能方案对于采用化学吸收法脱除煤层气中CO2至关重要。Among many coalbed methane decarbonization technologies, the chemical absorption method is widely used due to its fast absorption rate, large absorption capacity, and high removal efficiency. In fact, the chemical absorption method is not only used in the decarbonization process, but also has been applied in some industrial acid gas removal, and its technical maturity is relatively high. However, due to the serious energy and heat loss in the desorption process of chemical absorption, it is very important to propose a complete optimized energy-saving scheme for the removal of CO 2 in coalbed methane by chemical absorption.
传统的化学吸收法脱碳的工艺流程如图1所示，来自压缩工序的原料气先经分离器除去液滴，接着与出吸收塔净化气换热后从吸收塔下部进入，自下而上通过吸收塔；再生后的N—甲基二乙醇胺（MDEA）贫液从脱碳塔上部进入，自上而下通过吸收塔，逆向流动的复合胺溶液和天然气在吸收塔内充分接触，气体中的CO2及H2S等被吸收而进入液相，未被吸收的组份从吸收塔顶部引出，被吸收塔进气冷却至40℃以下，随后进入净化气分离器。分离的气体送往脱汞工序，冷凝液去脱碳冷凝液储罐。The process flow of the traditional chemical absorption decarbonization process is shown in Figure 1. The raw material gas from the compression process first passes through the separator to remove the liquid droplets, and then exchanges heat with the purified gas from the absorption tower, and then enters from the lower part of the absorption tower, from bottom to top Through the absorption tower; the regenerated N-methyldiethanolamine (MDEA) lean liquid enters from the upper part of the decarbonization tower, and passes through the absorption tower from top to bottom. The CO 2 and H 2 S are absorbed and enter the liquid phase, and the unabsorbed components are drawn from the top of the absorption tower, cooled by the intake air of the absorption tower to below 40°C, and then enter the purified gas separator. The separated gas is sent to the mercury removal process, and the condensate is sent to the decarbonization condensate storage tank.
吸收了酸气的复合胺溶液称为富液，降压后进入闪蒸罐，闪蒸气排出，然后与再生塔底部流出的高温贫液换热后，升温到80℃后进入再生塔上部，在再生塔内进行汽提再生，直至达到贫液的控制指标。出再生塔的贫液经过贫富液换热器和贫液冷却器，被冷却到40～55℃，之后经贫液泵，后从吸收塔上部进入，完成循环。The complex amine solution that has absorbed the acid gas is called rich liquid. After depressurization, it enters the flash tank, and the flash steam is discharged. After exchanging heat with the high-temperature lean liquid flowing out from the bottom of the regeneration tower, the temperature rises to 80°C and enters the upper part of the regeneration tower. Stripping regeneration is carried out in the regeneration tower until the control index of lean liquid is reached. The lean liquid coming out of the regeneration tower is cooled to 40-55°C through the lean-rich liquid heat exchanger and the lean liquid cooler, then passes through the lean liquid pump, and then enters from the upper part of the absorption tower to complete the cycle.
再生塔顶部的气体进入塔顶冷凝器后，分离的气体送往界区外，冷凝液由塔上部回到再生塔。After the gas at the top of the regeneration tower enters the top condenser, the separated gas is sent to the outside of the boundary area, and the condensate returns to the regeneration tower from the upper part of the tower.
随着化学吸收技术在煤层气脱碳领域的发展，化学吸收技术脱除煤层气中CO2已经得到广泛应用。但如何提高二氧化碳吸收率、降低脱碳系统能耗，一直是本领域一直渴望解决的技术难题；另外，如何简化缩小过大的运行设备，使化学吸收在煤层气脱碳领域适用于工程生产实践，也是本领域亟待解决的问题。With the development of chemical absorption technology in the field of coalbed methane decarbonization, chemical absorption technology has been widely used to remove CO2 from coalbed methane. However, how to improve the carbon dioxide absorption rate and reduce the energy consumption of the decarbonization system has always been a technical problem that this field has been eager to solve; in addition, how to simplify and reduce the oversized operating equipment so that chemical absorption is suitable for engineering production practice in the field of coalbed methane decarbonization , is also an urgent problem to be solved in this field.
发明内容Contents of the invention
本发明针对上述现有技术中存在的问题，对化学吸收法进行优化，提供了一种撬装式煤层气MDEA深脱碳吸收装置，采用主副塔双塔结构设计，提高二氧化碳吸收效率，降低脱碳系统能耗，大幅缩小设备尺寸。Aiming at the problems existing in the above-mentioned prior art, the present invention optimizes the chemical absorption method, and provides a skid-mounted coalbed methane MDEA deep decarbonization absorption device, which adopts a main and auxiliary tower double-tower structure design, improves the carbon dioxide absorption efficiency, reduces The energy consumption of the decarbonization system can greatly reduce the size of the equipment.
本发明的另一目的在于提供一种撬装式煤层气MDEA深脱碳吸收方法。Another object of the present invention is to provide a skid-mounted coalbed methane MDEA deep decarbonization absorption method.
本发明的技术方案如下：Technical scheme of the present invention is as follows:
一种撬装式煤层气MDEA深脱碳吸收装置，吸收塔副塔分别与吸收塔主塔和闪蒸罐连接，吸收塔副塔与闪蒸罐之间设置有富液泵I，吸收塔主塔与闪蒸罐之间设置有富液泵II，闪蒸罐与换热器入口a相连；换热器出口b连接解吸塔，解析塔通过贫液泵II与吸收塔主塔连接，解析塔通过贫液泵I与换热器入口c连接，换热器出口d与吸收塔副塔连接。A skid-mounted coalbed methane MDEA deep decarbonization absorption device, the auxiliary tower of the absorption tower is connected with the main tower of the absorption tower and the flash tank respectively, a rich liquid pump I is arranged between the auxiliary tower of the absorption tower and the flash tank, and the main tower of the absorption tower A rich liquid pump II is set between the tower and the flash tank, and the flash tank is connected to the inlet a of the heat exchanger; the outlet b of the heat exchanger is connected to the desorption tower, and the desorption tower is connected to the main tower of the absorption tower through the lean liquid pump II, and the desorption tower The lean liquid pump I is connected to the inlet c of the heat exchanger, and the outlet d of the heat exchanger is connected to the auxiliary tower of the absorption tower.
所述的吸收塔副塔和吸收塔主塔之间设置有风机，吸收塔副塔通过风机连接在吸收塔主塔的底部。A fan is arranged between the sub-tower of the absorption tower and the main tower of the absorption tower, and the sub-tower of the absorption tower is connected to the bottom of the main tower of the absorption tower through the fan.
所述的贫液泵II与吸收塔主塔之间设有冷却器。A cooler is provided between the lean liquid pump II and the main tower of the absorption tower.
所述的解析塔中段通过贫液泵I与换热器入口c连接，贫液泵I与换热器入口c之间设有除沫器。The middle section of the analytical tower is connected with the heat exchanger inlet c through the lean liquid pump I, and a demister is arranged between the lean liquid pump I and the heat exchanger inlet c.
所述的换热器出口d与吸收塔副塔的中段入口连接，换热器出口d与吸收塔副塔的中段入口之间设有循环泵。The outlet d of the heat exchanger is connected to the middle inlet of the sub-column of the absorption tower, and a circulation pump is arranged between the outlet d of the heat exchanger and the inlet of the sub-column of the absorption tower.
一种撬装式煤层气MDEA深脱碳吸收方法，包括下述步骤：A skid-mounted coalbed methane MDEA deep decarbonization absorption method comprises the following steps:
步骤1，原料气进入吸收塔副塔，与解吸塔中段抽取半贫液进行逆向接触反应吸收原料气中部分CO2，未发生反应的CO2由吸收塔副塔的塔顶经风机加压后进入吸收塔主塔底部，与吸收塔主塔底部产生的全贫液接触反应，未反应的气体作为产品气由吸收塔主塔塔顶排出，微量CH4溶于MDEA溶液；Step 1. The raw material gas enters the sub-tower of the absorption tower, and conducts a reverse contact reaction with the semi-lean liquid extracted from the middle section of the desorption tower to absorb part of the CO 2 in the raw gas, and the unreacted CO 2 is pressurized by the fan from the top of the sub-tower of the absorption tower Enter the bottom of the main tower of the absorption tower, contact and react with the whole lean liquid produced at the bottom of the main tower of the absorption tower, the unreacted gas is discharged from the top of the main tower of the absorption tower as product gas, and a small amount of CH 4 dissolves in the MDEA solution;
步骤2，吸收塔副塔反应产生的富含CO2液体的第一富液经富液泵I加压后与吸收塔主塔产生的第二富液经富液泵II加压混合后注入闪蒸罐；Step 2, the first rich liquid rich in CO2 liquid produced by the reaction of the auxiliary tower of the absorption tower is pressurized by the rich liquid pump I, and the second rich liquid produced by the main tower of the absorption tower is pressurized and mixed by the rich liquid pump II, and then injected into the flash steamer;
步骤3，闪蒸罐对富液中的CH4进行闪蒸，闪蒸后的富液进入换热器；Step 3, the flash tank flashes the CH in the rich liquid, and the rich liquid after flashing enters the heat exchanger;
步骤4，富液在换热器中与解吸塔产生半贫液进行换热；Step 4, the rich liquid exchanges heat with the semi-lean liquid produced in the desorption tower in the heat exchanger;
步骤5，换热后的富液进入解吸塔由解吸塔顶部喷淋，在再沸器加热的作用下，富液升温到130℃，CO2从MDEA吸收剂中解吸，解吸出的再生气经由再生气出口进入气液分离器。Step 5, the rich liquid after heat exchange enters the desorption tower and is sprayed from the top of the desorption tower. Under the action of the heating of the reboiler, the temperature of the rich liquid rises to 130°C, CO2 is desorbed from the MDEA absorbent, and the desorbed regeneration gas passes through The regeneration gas exits into the gas-liquid separator.
所述的步骤1中，原料气为来自煤矿采动区、采空区地面煤层气抽采井的CH4含量30%-50%的中低浓度煤层气提纯后的原料气；产品气中CO2含量低于50ppm；半贫液为20%wtMDEA溶液，全贫液为40%wt MDEA溶液；吸收的部分CO2为30%的CO2；风机加压到3bar。In the described step 1, the raw material gas is the raw material gas after the purification of medium and low concentration coalbed methane with CH4 content of 30%-50% from the ground coalbed methane extraction well in the coal mine mining area and goaf; the CO in the product gas 2 content is less than 50ppm; the semi-poor solution is 20%wt MDEA solution, and the total barren solution is 40%wt MDEA solution; part of the CO 2 absorbed is 30% CO 2 ; the fan is pressurized to 3bar.
所述的步骤3中，闪蒸后温度为85-95℃。In the step 3, the temperature after flash evaporation is 85-95°C.
所述的步骤4中，解吸塔产生半贫液温度为110-130℃，换热后的富液温度100℃。In step 4, the temperature of the semi-lean liquid produced by the desorption tower is 110-130°C, and the temperature of the rich liquid after heat exchange is 100°C.
所述的步骤5中，解吸塔中段半贫液经贫液泵I抽出后进入除沫器，除去半贫液中的气沫，再经过换热器换热，换热后温度60℃，换热后的半贫液进入吸收塔副塔完成循环；解吸塔塔底产生的全贫液经贫液泵II和冷却器冷却到40℃后进入吸收塔主塔，开始新一轮吸收。In the step 5, the semi-poor liquid in the middle section of the desorption tower is pumped out by the lean liquid pump 1 and enters the demister to remove the foam in the semi-poor liquid, and then heat exchange through a heat exchanger. After the heat exchange, the temperature is 60° C. The heated semi-lean liquid enters the auxiliary tower of the absorption tower to complete the cycle; the whole lean liquid produced at the bottom of the desorption tower is cooled to 40°C by the lean liquid pump II and cooler, and then enters the main tower of the absorption tower to start a new round of absorption.
本发明的优点效果如下：The advantages and effects of the present invention are as follows:
1、本发明对化学吸收法原流程进行优化，将原料气进入脱碳模块进行CO2脱除，使产品气中CO2含量低于50ppm。1. The present invention optimizes the original process of the chemical absorption method, and feeds the raw material gas into the decarbonization module for CO 2 removal, so that the CO 2 content in the product gas is lower than 50ppm.
2、本发明通过闪蒸罐对富液中的甲烷进行闪蒸，可防止溶液在管道中发泡，造成管线动荡，形成气堵。2. The present invention flashes the methane in the rich liquid through the flash tank, which can prevent the solution from foaming in the pipeline, causing the pipeline to be turbulent and forming gas blockage.
3、本发明采用主副塔双塔结构设计，提高二氧化碳吸收效率，降低脱碳系统能耗，大幅缩小原吸收塔尺寸，实现吸收装置撬装化和模块化；3. The present invention adopts the double-tower structure design of the main and auxiliary towers to improve the carbon dioxide absorption efficiency, reduce the energy consumption of the decarbonization system, greatly reduce the size of the original absorption tower, and realize skid-mounting and modularization of the absorption device;
4、解吸塔中贫液分为半贫液和全贫液，半贫液由解吸塔中部抽出，抽出的半贫液中夹带气沫，通过除沫器去除其中夹带气沫；全贫液由解吸塔底部抽出，半贫液注入吸收塔副塔，全贫液注入吸收塔主塔分别循环利用，提高MDEA化学吸收剂吸收二氧化碳效率，降低脱碳系统能耗。4. The poor liquid in the desorption tower is divided into semi-poor liquid and full-poor liquid. The semi-poor liquid is extracted from the middle of the desorption tower, and the extracted semi-poor liquid contains air foam, which is removed by a demister; The bottom of the desorption tower is drawn out, the semi-poor liquid is injected into the auxiliary tower of the absorption tower, and the whole lean liquid is injected into the main tower of the absorption tower for recycling respectively, so as to improve the efficiency of MDEA chemical absorbent to absorb carbon dioxide and reduce the energy consumption of the decarbonization system.
附图说明Description of drawings
图1为现有技术中化学吸收法MDEA脱碳工艺流程示意图。Fig. 1 is a schematic flow chart of the chemical absorption method MDEA decarburization process in the prior art.
图2为本发明一种撬装式煤层气MDEA深脱碳吸收装置结构示意图。Fig. 2 is a structural schematic diagram of a skid-mounted coalbed methane MDEA deep decarbonization absorption device of the present invention.
图3为本发明煤层气MDEA深脱碳吸收流程示意图。Fig. 3 is a schematic diagram of the deep decarburization absorption process of the coalbed methane MDEA of the present invention.
图中，101、吸收塔，102、贫富液换热器，103、再生塔，104、冷凝器，105、贫液泵，106、再沸器；In the figure, 101, absorption tower, 102, lean-rich liquid heat exchanger, 103, regeneration tower, 104, condenser, 105, lean liquid pump, 106, reboiler;
201、吸收塔副塔，202、风机，203、吸收塔主塔，204、循环泵，205、富液泵I，206、富液泵II，207、闪蒸罐，208、换热器，209、除沫器，210、解吸塔，211、气液分离器，212、再沸器，213、贫液泵I，214、贫液泵II，215、冷却器。201, auxiliary tower of absorption tower, 202, fan, 203, main tower of absorption tower, 204, circulation pump, 205, rich liquid pump I, 206, rich liquid pump II, 207, flash tank, 208, heat exchanger, 209 , demister, 210, desorption tower, 211, gas-liquid separator, 212, reboiler, 213, lean liquid pump I, 214, lean liquid pump II, 215, cooler.
实施方式Implementation
实施例Example
如图2所示，一种撬装式煤层气MDEA深脱碳吸收装置，吸收塔副塔201分别与吸收塔主塔203和闪蒸罐207连接，所述的吸收塔副塔201和吸收塔主塔203之间设置有风机202，吸收塔副塔201通过风机202连接在吸收塔主塔203的底部。吸收塔副塔201与闪蒸罐207之间设置有富液泵I，吸收塔主塔203与闪蒸罐207之间设置有富液泵II，闪蒸罐207与换热器入口a相连；换热器出口b连接解吸塔210上部，解析塔210底部依次通过贫液泵II、冷却器215与吸收塔主塔203的上部连接，所述的解析塔210中段通过贫液泵I、除沫器209与换热器入口3连接；所述的换热器出口4通过循环泵204与吸收塔副塔的中段入口连接。As shown in Figure 2, a skid-mounted coalbed methane MDEA deep decarbonization absorption device, the absorption tower sub-tower 201 is connected with the absorption tower main tower 203 and the flash tank 207 respectively, the absorption tower sub-tower 201 and the absorption tower A fan 202 is arranged between the main towers 203, and the auxiliary tower 201 of the absorption tower is connected to the bottom of the main tower 203 of the absorption tower through the fan 202. A rich liquid pump I is arranged between the sub-tower 201 of the absorption tower and the flash tank 207, and a rich liquid pump II is arranged between the main tower 203 of the absorption tower and the flash tank 207, and the flash tank 207 is connected to the inlet a of the heat exchanger; The outlet b of the heat exchanger is connected to the top of the desorption tower 210, and the bottom of the desorption tower 210 is connected to the top of the absorption tower main tower 203 through the lean liquid pump II and the cooler 215 successively. The device 209 is connected with the inlet 3 of the heat exchanger; the outlet 4 of the heat exchanger is connected with the inlet of the middle section of the sub-column of the absorption tower through the circulation pump 204 .
如图3所示，一种撬装式煤层气MDEA深脱碳吸收方法，包括下述步骤：As shown in Figure 3, a skid-mounted coalbed methane MDEA deep decarbonization absorption method includes the following steps:
步骤1，来自煤矿采动区、采空区地面煤层气抽采井的CH4含量40%的中低浓度煤层气提纯后的原料气进入吸收塔副塔，原料气气体组成为CH4 90.61%；N2 5.34%；O2 0.03%；CO2 4.02%，与解吸塔中段抽取20%wt MDEA溶液的半贫液进行逆向接触反应吸收原料气中30%的CO2，未发生反应的CO2由吸收塔副塔的塔顶经风机加压到3bar后进入吸收塔主塔底部，与吸收塔主塔底部产生的40%wt MDEA溶液的全贫液接触反应，未反应的气体作为产品气由吸收塔主塔塔顶排出，微量CH4溶于MDEA溶液；产品气中CO2含量低于50ppm。Step 1, the raw material gas from the medium and low concentration coalbed methane with CH 4 content of 40% purified from the ground coal bed methane drainage wells in coal mining areas and goafs enters the auxiliary tower of the absorption tower, and the gas composition of the raw gas is CH 4 90.61% ; N 2 5.34%; O 2 0.03%; CO 2 4.02%, reverse contact reaction with the semi-lean solution of 20%wt MDEA solution extracted from the middle section of the desorption tower to absorb 30% of CO 2 in the raw gas, and the unreacted CO 2 The top of the sub-tower of the absorption tower is pressurized to 3bar by a fan and then enters the bottom of the main tower of the absorption tower, and reacts with the whole lean liquid of 40%wt MDEA solution produced at the bottom of the main tower of the absorption tower, and the unreacted gas is produced as a product gas by The absorption tower is discharged from the top of the main tower, and a small amount of CH 4 is dissolved in the MDEA solution; the CO 2 content in the product gas is less than 50ppm.
步骤2，吸收塔副塔反应产生的富含CO2液体的第一富液经富液泵I加压后与吸收塔主塔产生的第二富液经富液泵II加压混合后注入闪蒸罐；Step 2, the first rich liquid rich in CO2 liquid produced by the reaction of the auxiliary tower of the absorption tower is pressurized by the rich liquid pump I, and the second rich liquid produced by the main tower of the absorption tower is pressurized and mixed by the rich liquid pump II, and then injected into the flash steamer;
步骤3，闪蒸罐对富液中的CH4进行闪蒸，闪蒸后的富液进入换热器，闪蒸后温度为90℃；Step 3, the flash tank flashes the CH 4 in the rich liquid, and the rich liquid after flashing enters the heat exchanger, and the temperature after flashing is 90°C;
步骤4，富液在换热器中与解吸塔产生半贫液进行换热；解吸塔产生半贫液温度为120℃，换热后的富液温度100℃；Step 4, the rich liquid is exchanged with the semi-lean liquid produced by the desorption tower in the heat exchanger; the temperature of the semi-lean liquid produced by the desorption tower is 120°C, and the temperature of the rich liquid after heat exchange is 100°C;
步骤5，换热后的富液进入解吸塔由解吸塔顶部喷淋，在再沸器加热的作用下，富液升温到130℃，CO2从MDEA吸收剂中解吸，解吸出的再生气经由再生气出口进入气液分离器；Step 5, the rich liquid after heat exchange enters the desorption tower and is sprayed from the top of the desorption tower. Under the action of the heating of the reboiler, the temperature of the rich liquid rises to 130°C, CO2 is desorbed from the MDEA absorbent, and the desorbed regeneration gas passes through The regeneration gas outlet enters the gas-liquid separator;
所述的步骤6，气液分离器将再生气分离掉部分水蒸汽后得到CO2。In step 6, the gas-liquid separator separates part of the water vapor from the regeneration gas to obtain CO 2 .
所述的步骤5中，解吸塔中段半贫液经贫液泵I抽出后进入除沫器，除去半贫液中的气沫，再经过换热器换热，换热后温度60℃，换热后的半贫液进入吸收塔副塔完成循环；解吸塔塔底产生的全贫液经贫液泵II和冷却器冷却到40℃后进入吸收塔主塔，开始新一轮吸收。In the step 5, the semi-poor liquid in the middle section of the desorption tower is pumped out by the lean liquid pump 1 and enters the demister to remove the foam in the semi-poor liquid, and then heat exchange through a heat exchanger. After the heat exchange, the temperature is 60° C. The heated semi-lean liquid enters the auxiliary tower of the absorption tower to complete the cycle; the whole lean liquid produced at the bottom of the desorption tower is cooled to 40°C by the lean liquid pump II and cooler, and then enters the main tower of the absorption tower to start a new round of absorption.
在本发明的描述中，需要说明的是，术语“中心”、“纵向”、“横向”、“上”、“下”、“前”、“后”、“左”、“右”、“竖直”、“水平”、“顶”、“底”“内”、“外”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作。因此不能理解为对本发明的限制，本发明的保护范围不受具体实施例所限制。In the description of the present invention, it should be noted that the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", " The orientations or positional relationships indicated by "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. are based on the orientation or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying describe, but do not indicate or imply that the referred device or element must have a particular orientation, be constructed in a particular orientation, and operate. Therefore, it should not be understood as a limitation of the present invention, and the protection scope of the present invention is not limited by specific embodiments.
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