CN221522480U - Energy-saving desorption device for vacuum carbonate desulfurization rich liquid - Google Patents
Energy-saving desorption device for vacuum carbonate desulfurization rich liquid Download PDFInfo
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- 239000007788 liquid Substances 0.000 title claims abstract description 81
- 238000003795 desorption Methods 0.000 title claims abstract description 58
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 41
- 230000023556 desulfurization Effects 0.000 title claims abstract description 41
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 title claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 72
- 239000002253 acid Substances 0.000 claims abstract description 43
- 238000010992 reflux Methods 0.000 claims abstract description 16
- 239000012808 vapor phase Substances 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 230000005501 phase interface Effects 0.000 claims abstract description 7
- 239000007791 liquid phase Substances 0.000 claims abstract description 6
- 238000005086 pumping Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 abstract description 7
- 239000002918 waste heat Substances 0.000 abstract description 6
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 5
- 238000009833 condensation Methods 0.000 abstract description 5
- 230000005494 condensation Effects 0.000 abstract description 5
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 5
- 238000007255 decyanation reaction Methods 0.000 abstract description 3
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 239000003034 coal gas Substances 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 15
- 239000007789 gas Substances 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 6
- 239000000571 coke Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 1
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- WVULZDFWPQCPPJ-UHFFFAOYSA-N potassium;hydrochloride Chemical compound Cl.[K] WVULZDFWPQCPPJ-UHFFFAOYSA-N 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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Abstract
本实用新型属于煤气净化脱硫脱氰技术领域，尤其涉及一种真空碳酸盐脱硫富液节能解吸装置，包括酸汽部分冷凝换热、汽液分离、循环热水换热；解吸塔顶部酸汽出口与热泵机组酸汽入口相连；热泵机组汽液混合物出口与酸汽冷却器酸汽入口相连；液分离器液相接口端与回流液泵入口相连；热泵机组热水出口与热水再沸器热水入口相连；热水再沸器出口与解吸塔底部汽相空间相连。与现有技术相比，本实用新型的有益效果是：采用第一类吸收式热泵将解吸塔顶部的酸汽潜热在热泵机组内与高温位热源低压蒸汽驱动作用下提升温度品质后加热循环热水，用于加热塔底贫液给解吸塔碳酸盐脱硫富液解吸硫化氢提供全部热源，实现了塔顶酸汽余热回收利用，降低运行成本。
The utility model belongs to the technical field of coal gas purification, desulfurization and decyanation, and particularly relates to a vacuum carbonate desulfurization rich liquid energy-saving desorption device, including acid vapor partial condensation heat exchange, vapor-liquid separation, and circulating hot water heat exchange; the acid vapor outlet at the top of the desorption tower is connected to the acid vapor inlet of the heat pump unit; the vapor-liquid mixture outlet of the heat pump unit is connected to the acid vapor inlet of the acid vapor cooler; the liquid phase interface end of the liquid separator is connected to the reflux liquid pump inlet; the hot water outlet of the heat pump unit is connected to the hot water inlet of the hot water reboiler; the hot water reboiler outlet is connected to the vapor phase space at the bottom of the desorption tower. Compared with the prior art, the utility model has the beneficial effects of: using the first type of absorption heat pump to increase the temperature quality of the acid vapor latent heat at the top of the desorption tower under the driving action of the high-temperature heat source low-pressure steam in the heat pump unit and then heating the circulating hot water, which is used to heat the lean liquid at the bottom of the tower to provide all the heat sources for the carbonate desulfurization rich liquid of the desorption tower to desorb hydrogen sulfide, realizing the recovery and utilization of the waste heat of the acid vapor at the top of the tower, and reducing the operating cost.
Description
技术领域Technical Field
本实用新型属于煤气净化脱硫脱氰技术领域，尤其涉及一种真空碳酸盐脱硫富液节能解吸装置。The utility model belongs to the technical field of coal gas purification, desulfurization and decyanation, and particularly relates to a vacuum carbonate desulfurization rich liquid energy-saving desorption device.
背景技术Background Art
真空碳酸盐法脱硫一般设置在焦炉煤气除氨和洗苯后。真空碳酸盐法脱硫属于一种湿式吸收法脱硫脱氰方法，其是以碳酸钾碱性物质作吸收剂吸收H2S、HCN、CO2，再通过蒸汽汽提法和负压进行脱硫富液解吸，解吸浓缩后的浓酸汽可送至后续制酸装置或克劳斯硫回收装置，将酸性气体转化生成硫酸或优质硫磺产品。但采用蒸汽汽提法对脱硫富液进行解吸，需要的能耗较高，因此如何提高真空碳酸盐脱硫富液解吸过程的能源利用率，降低能源单耗，成为人们普遍关注的问题。Vacuum carbonate desulfurization is generally set up after the removal of ammonia and benzene from coke oven gas. Vacuum carbonate desulfurization is a wet absorption desulfurization and decyanation method, which uses potassium carbonate alkaline substances as absorbents to absorb H2S , HCN, and CO2 , and then desorbs the desulfurized rich liquid through steam stripping and negative pressure. The concentrated acid gas after desorption can be sent to the subsequent acid production unit or Claus sulfur recovery unit to convert the acid gas into sulfuric acid or high-quality sulfur products. However, the use of steam stripping to desorb the desulfurized rich liquid requires high energy consumption. Therefore, how to improve the energy utilization rate of the vacuum carbonate desulfurization rich liquid desorption process and reduce the energy consumption per unit has become a common concern.
第二类吸收式热泵可以有效地回收温度较低的余热，并将其转化为温度较高的热源，从而实现余热的回收和利用。其与压缩式热泵相比，吸收式热泵具有较高的效率和可靠性，目前工业应用较为成熟和广泛，但是在真空碳酸盐脱硫富液解吸生产环节还未见有应用。The second type of absorption heat pump can effectively recover the waste heat with lower temperature and convert it into a higher temperature heat source, thereby realizing the recovery and utilization of waste heat. Compared with the compression heat pump, the absorption heat pump has higher efficiency and reliability. At present, its industrial application is more mature and widespread, but it has not been applied in the production link of vacuum carbonate desulfurization rich liquid desorption.
实用新型内容Utility Model Content
本实用新型的目的是提供一种真空碳酸盐脱硫富液节能解吸装置，克服现有技术的不足，采用第一类吸收式热泵将解吸塔顶部的酸汽潜热在热泵机组内与高温位热源低压蒸汽驱动作用下提升温度品质后加热循环热水，用于加热塔底贫液给解吸塔碳酸盐脱硫富液解吸硫化氢提供全部热源，实现了塔顶酸汽余热回收利用，工艺流程简单，减少设备投资、降低操作费用。The utility model aims to provide a vacuum carbonate desulfurization rich liquid energy-saving desorption device, overcomes the shortcomings of the prior art, adopts the first type of absorption heat pump to heat the acid vapor latent heat at the top of the desorption tower to increase the temperature quality under the driving action of the high-temperature heat source low-pressure steam in the heat pump unit, and then heats the circulating hot water for heating the lean liquid at the bottom of the tower to provide all the heat sources for the carbonate desulfurization rich liquid of the desorption tower to desorb hydrogen sulfide, realizes the recovery and utilization of the waste heat of the acid vapor at the top of the tower, has a simple process flow, reduces equipment investment and reduces operating costs.
为实现上述目的，本实用新型通过以下技术方案实现：To achieve the above purpose, the utility model is implemented through the following technical solutions:
一种真空碳酸盐脱硫富液节能解吸装置，其特征在于，包括解吸塔、热泵机组、循环热水泵﹑热水再沸器﹑膨胀槽、酸汽冷却器、汽液分离器及回流液泵，解吸塔顶部酸汽出口与热泵机组酸汽入口相连；热泵机组汽液混合物出口与酸汽冷却器酸汽入口相连；酸汽冷却器酸汽出口与汽液分离器相连；液分离器液相接口端与回流液泵入口相连；回流液泵出口与解吸塔顶部回流液入口相连；汽液分离器汽相接口端与后续抽真空系统相连；热泵机组热水出口与热水再沸器热水入口相连；热水再沸器热水出口与循环热水泵入口相连；循环热水泵出口与热泵机组热水入口相连；膨胀槽底部水出口与循环热水管路高点处相连；解吸塔底部脱硫贫液出口与热水再沸器相连；热水再沸器出口与解吸塔底部汽相空间相连。A vacuum carbonate desulfurization rich liquid energy-saving desorption device is characterized in that it comprises a desorption tower, a heat pump unit, a circulating hot water pump, a hot water reboiler, an expansion tank, an acid vapor cooler, a vapor-liquid separator and a reflux liquid pump, wherein the acid vapor outlet at the top of the desorption tower is connected to the acid vapor inlet of the heat pump unit; the vapor-liquid mixture outlet of the heat pump unit is connected to the acid vapor inlet of the acid vapor cooler; the acid vapor outlet of the acid vapor cooler is connected to the vapor-liquid separator; the liquid phase interface end of the liquid separator is connected to the reflux liquid pump inlet; the reflux liquid pump outlet is connected to the reflux liquid inlet at the top of the desorption tower; the vapor phase interface end of the vapor-liquid separator is connected to a subsequent vacuum pumping system; the hot water outlet of the heat pump unit is connected to the hot water inlet of the hot water reboiler; the hot water outlet of the hot water reboiler is connected to the inlet of the circulating hot water pump; the circulating hot water pump outlet is connected to the hot water inlet of the heat pump unit; the water outlet at the bottom of the expansion tank is connected to the high point of the circulating hot water pipeline; the desulfurization lean liquid outlet at the bottom of the desorption tower is connected to the hot water reboiler; and the hot water reboiler outlet is connected to the vapor phase space at the bottom of the desorption tower.
与现有技术相比，本实用新型的有益效果是：Compared with the prior art, the beneficial effects of the utility model are:
1)采用第一类吸收式热泵将解吸塔顶部的酸汽潜热在热泵机组内与高温位热源低压蒸汽驱动作用下提升温度品质后加热循环热水，用于加热塔底贫液给解吸塔碳酸盐脱硫富液解吸硫化氢提供全部热源，实现了塔顶酸汽余热回收利用，采用本实用新型工艺进行真空碳酸盐脱硫富液解吸，在余热水消耗或蒸汽消耗方面，仅在开工时需加入临时蒸汽或余热水，在正常生产操作时消耗较少余热水或蒸汽。1) The first type of absorption heat pump is used to heat the acid vapor latent heat at the top of the desorption tower to increase the temperature quality under the driving action of the high-temperature heat source low-pressure steam in the heat pump unit, and then heat the circulating hot water to heat the lean liquid at the bottom of the tower to provide all the heat sources for the carbonate desulfurization rich liquid in the desorption tower to desorb hydrogen sulfide, thereby realizing the recovery and utilization of the waste heat of the acid vapor at the top of the tower. The process of the utility model is used for vacuum carbonate desulfurization rich liquid desorption. In terms of waste hot water consumption or steam consumption, only temporary steam or waste hot water needs to be added at the start of operation, and less waste hot water or steam is consumed during normal production operation.
2)在设备投资方面，相对于现有技术，仅增加了热泵机组、热水再沸器、循环热泵水、膨胀槽等设备，工艺流程简单，操作方便，可在减少设备投资的同时，降低操作费用，相比传统的真空碳酸盐脱硫富液解吸技术，节省了27.6％的能耗，提高了自身能源利用率，降低生产企业的运行成本。2) In terms of equipment investment, compared with the existing technology, only the heat pump unit, hot water reboiler, circulating heat pump water, expansion tank and other equipment are added. The process flow is simple and easy to operate. It can reduce equipment investment while reducing operating costs. Compared with the traditional vacuum carbonate desulfurization rich liquid desorption technology, it saves 27.6% of energy consumption, improves its own energy utilization rate, and reduces the operating costs of production enterprises.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1是本实用新型实施例工艺流程示意图；FIG1 is a schematic diagram of a process flow diagram of an embodiment of the utility model;
图中：1-解吸塔；2-热泵机组；3-循环热水泵；4-热水再沸器；5-膨胀槽；6-酸汽冷却器；7-汽液分离器；8-回流液泵。In the figure: 1-desorption tower; 2-heat pump unit; 3-circulating hot water pump; 4-hot water reboiler; 5-expansion tank; 6-acid vapor cooler; 7-vapor-liquid separator; 8-reflux liquid pump.
具体实施方式DETAILED DESCRIPTION
下面将结合具体实施例对本实用新型的技术方案进行清楚、完整地描述，显然，所描述的实施例是本实用新型一部分实施例，而不是全部的实施例。The technical solution of the present utility model will be clearly and completely described below in conjunction with specific embodiments. Obviously, the described embodiments are only part of the embodiments of the present utility model, rather than all of the embodiments.
为了更清楚地说明本实用新型具体实施方式或现有技术中的技术方案，下面将对具体实施方式或现有技术描述中所需要使用的具体实施例作简单地介绍，显而易见地，下面描述中的具体实施例是本实用新型的一些实施方式，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些具体实施例获得其他的具体实施例。In order to more clearly illustrate the specific implementation methods of the utility model or the technical solutions in the prior art, the specific embodiments required to be used in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the specific embodiments described below are some implementation methods of the utility model. For ordinary technicians in this field, other specific embodiments can be obtained based on these specific embodiments without paying creative work.
通常在此处具体实施例中描述和显示出的本实用新型实施例的组件可以以无数种不同的配置来布置和设计。因此，以下对在具体实施例中提供的本实用新型的实施例的详细描述并非旨在限制要求保护的本实用新型的范围，而是仅仅表示本实用新型的选定实施例。The components of the embodiments of the present invention generally described and shown in the specific embodiments herein can be arranged and designed in countless different configurations. Therefore, the following detailed description of the embodiments of the present invention provided in the specific embodiments is not intended to limit the scope of the utility model claimed, but only represents the selected embodiments of the utility model.
见图1，是本实用新型一种真空碳酸盐脱硫富液节能解吸装置实施例结构示意图，包括解吸塔1、热泵机组2、循环热水泵3﹑热水再沸器4﹑膨胀槽5、酸汽冷却器6、汽液分离器7及回流液泵8；解吸塔1顶部酸汽出口与热泵机组2酸汽入口相连；热泵机组2汽液混合物出口与酸汽冷却器6酸汽入口相连；酸汽冷却器6酸汽出口与汽液分离器7相连；汽液分离器7液相接口端与回流液泵8入口相连；回流液泵8出口与解吸塔1顶部回流液入口相连；汽液分离器7汽相接口端与后续抽真空系统相连；热泵机组2热水出口与热水再沸器4热水入口相连；热水再沸器4热水出口与循环热水泵3入口相连；循环热水泵3出口与热泵机组2热水入口相连；膨胀槽5底部水出口与循环热水管路高点处相连；解吸塔1底部脱硫贫液出口与热水再沸器4相连；热水再沸器4出口与解吸塔1底部汽相空间相连。See Figure 1, which is a schematic diagram of the structure of an embodiment of a vacuum carbonate desulfurization rich liquid energy-saving desorption device of the utility model, including a desorption tower 1, a heat pump unit 2, a circulating hot water pump 3, a hot water reboiler 4, an expansion tank 5, an acid vapor cooler 6, a vapor-liquid separator 7 and a reflux pump 8; the acid vapor outlet at the top of the desorption tower 1 is connected to the acid vapor inlet of the heat pump unit 2; the vapor-liquid mixture outlet of the heat pump unit 2 is connected to the acid vapor inlet of the acid vapor cooler 6; the acid vapor outlet of the acid vapor cooler 6 is connected to the vapor-liquid separator 7; the liquid phase interface end of the vapor-liquid separator 7 is connected to the inlet of the reflux pump 8 The outlet of the reflux liquid pump 8 is connected to the reflux liquid inlet at the top of the desorption tower 1; the vapor phase interface end of the vapor-liquid separator 7 is connected to the subsequent vacuum system; the hot water outlet of the heat pump unit 2 is connected to the hot water inlet of the hot water reboiler 4; the hot water outlet of the hot water reboiler 4 is connected to the inlet of the circulating hot water pump 3; the outlet of the circulating hot water pump 3 is connected to the hot water inlet of the heat pump unit 2; the water outlet at the bottom of the expansion tank 5 is connected to the high point of the circulating hot water pipeline; the desulfurization lean liquid outlet at the bottom of the desorption tower 1 is connected to the hot water reboiler 4; the outlet of the hot water reboiler 4 is connected to the vapor phase space at the bottom of the desorption tower 1.
本实用新型真空碳酸盐脱硫富液节能解吸方法，包括酸汽部分冷凝换热、汽液分离、循环热水换热，具体步骤如下：1)酸汽部分冷凝换热，热的碳酸盐脱硫富液进入解吸塔顶部进行富液解吸，解吸塔顶热解吸出的酸汽进入热泵机组换热冷凝后成为汽液混合物后进入酸汽冷却器与循环水换热冷却后进入汽液分离器进行汽液分离；2)汽液分离，汽液分离器分离出的液相部分经回流液泵进入解吸塔顶部，分离出的汽相部分进入后续抽真空系统；3)循环热水换热，经热水再沸器换热后的循环热水经循环热水泵送入热泵机组吸收热量提升温度后，循环送回至热水再沸器，为解吸塔底脱硫贫液间接换热为脱硫解吸提供全部热源；循环热水管路高点处设置膨胀槽，定期在膨胀槽补除盐水，以保证循环热水管路满水循环。The utility model discloses a vacuum carbonate desulfurization rich liquid energy-saving desorption method, comprising acid vapor partial condensation heat exchange, vapor-liquid separation, and circulating hot water heat exchange, and the specific steps are as follows: 1) acid vapor partial condensation heat exchange, hot carbonate desulfurization rich liquid enters the top of a desorption tower for rich liquid desorption, the acid vapor thermally desorbed from the top of the desorption tower enters a heat pump unit for heat exchange condensation to become a vapor-liquid mixture, then enters an acid vapor cooler for heat exchange cooling with circulating water, and then enters a vapor-liquid separator for vapor-liquid separation; 2) vapor-liquid separation, the liquid phase separated by the vapor-liquid separator enters the top of the desorption tower through a reflux liquid pump, and the separated vapor phase enters a subsequent vacuum pumping system; 3) circulating hot water heat exchange, the circulating hot water after heat exchange in a hot water reboiler is sent to the heat pump unit through a circulating hot water pump to absorb heat and increase the temperature, and then circulated back to the hot water reboiler, so as to provide all heat sources for desulfurization desorption by indirect heat exchange of the desulfurization lean liquid at the bottom of the desorption tower; an expansion tank is arranged at a high point of the circulating hot water pipeline, and desalted water is regularly added to the expansion tank to ensure that the circulating hot water pipeline is full of water circulation.
以处理128000Nm3/h焦炉煤气(干气)的真空碳酸盐脱硫中富液解吸为例，焦炉煤气杂质：H2S：7.5g/Nm3，真空碳酸盐脱硫净化至200mg/Nm3。Taking the desorption of rich liquid in vacuum carbonate desulfurization of 128000Nm 3 /h coke oven gas (dry gas) as an example, the impurity of coke oven gas is: H 2 S: 7.5g/Nm 3 , which is purified to 200mg/Nm 3 by vacuum carbonate desulfurization.
解吸塔顶部温度为58℃，压力为-82kPag；解吸塔底部温度为60℃；解吸顶部热解吸出的酸汽进入热泵机组冷凝换热成为54℃的汽液混合物，此汽液混合物进入酸汽冷却器冷却至33℃后进入汽液分离器进行汽液分离，分离出的液相部分经回流液泵进入脱硫富液解吸塔顶部，分离出的汽相部分进入后续抽真空系统；经热水再沸器换热后的65℃循环热水经循环热水泵送入热泵机组吸收热量提升温度至75℃后，循环送回至热水再沸器，为解吸塔底脱硫贫液间接换热为脱硫解吸提供全部热源；回收塔顶酸汽余热的热泵机组为第一类吸收式热泵，热泵驱动高温位热源为0.5MPag低压饱和蒸汽。The top temperature of the desorption tower is 58°C and the pressure is -82kPag; the bottom temperature of the desorption tower is 60°C; the acid vapor desorbed from the top of the desorption tower enters the heat pump unit for condensation and heat exchange to become a vapor-liquid mixture at 54°C. This vapor-liquid mixture enters the acid vapor cooler and is cooled to 33°C before entering the vapor-liquid separator for vapor-liquid separation. The separated liquid phase enters the top of the desulfurization rich liquid desorption tower through the reflux liquid pump, and the separated vapor phase enters the subsequent vacuum system; the 65°C circulating hot water after heat exchange in the hot water reboiler is sent to the heat pump unit through the circulating hot water pump to absorb heat and raise the temperature to 75°C, and then circulated back to the hot water reboiler to provide all the heat sources for desulfurization desorption by indirect heat exchange of the desulfurization lean liquid at the bottom of the desorption tower; the heat pump unit that recovers the waste heat of the acid vapor at the top of the tower is a first-class absorption heat pump, and the high-temperature heat source driven by the heat pump is 0.5MPag low-pressure saturated steam.
实施例中，脱硫富液解吸塔底部贫液中碳酸盐含量为80g/L左右；实施例的经济效益分析如下：以处理含H2S：7.5g/Nm3的128000Nm3/h焦炉煤气(干气)、真空碳酸盐脱硫净化至200mg/Nm3的脱硫富液解吸为例，两种真空盐酸盐脱硫富液解吸工艺的能耗对比详见表1。In the embodiment, the carbonate content in the lean liquid at the bottom of the desulfurization rich liquid desorption tower is about 80g/L; the economic benefit analysis of the embodiment is as follows: taking the treatment of 128000Nm3 /h coke oven gas (dry gas) containing H2S : 7.5g/ Nm3 and the desulfurization rich liquid desorption purified to 200mg/ Nm3 by vacuum carbonate desulfurization as an example, the energy consumption comparison of the two vacuum hydrochloride desulfurization rich liquid desorption processes is shown in Table 1.
表1Table 1
由上表可知：本实用新型真空碳酸盐脱硫富液节能解吸方法远低于常规真空盐酸盐脱硫富液解吸工艺。It can be seen from the above table that the energy-saving desorption method of the vacuum carbonate desulfurization rich liquid of the utility model is far lower than the conventional vacuum hydrochloride desulfurization rich liquid desorption process.
本实用新型真空碳酸盐脱硫富液节能解吸方法较目前应用普遍的常规真空盐酸盐脱硫富液解吸工艺总运行成本降低了27.6％，大幅降低了焦化等企业的真空盐酸钾脱硫富液解吸能耗，较好地解决了真空碳酸盐脱硫单元的能耗高问题。The utility model reduces the total operating cost of the vacuum carbonate desulfurization rich liquid energy-saving desorption method by 27.6% compared with the currently commonly used conventional vacuum hydrochloride desulfurization rich liquid desorption process, greatly reduces the energy consumption of vacuum potassium hydrochloride desulfurization rich liquid desorption in coking and other enterprises, and effectively solves the problem of high energy consumption of vacuum carbonate desulfurization units.
尽管已经示出和描述了本实用新型的实施例，对于本领域的普通技术人员而言，可以理解在不脱离本实用新型的原理和精神的情况下可以对这些实施例进行多种变化、修改、替换和变型，本实用新型的范围由所附权利要求及其等同物限定。Although the embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the appended claims and their equivalents.
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