CN216712018U - A vacuum carbonate desulfurization rich liquid desorption system - Google Patents
A vacuum carbonate desulfurization rich liquid desorption system Download PDFInfo
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- 239000007788 liquid Substances 0.000 title claims abstract description 296
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 166
- 230000023556 desulfurization Effects 0.000 title claims abstract description 165
- 238000003795 desorption Methods 0.000 title claims abstract description 93
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 title claims abstract description 37
- 239000002253 acid Substances 0.000 claims abstract description 47
- 238000010992 reflux Methods 0.000 claims abstract description 15
- 239000007791 liquid phase Substances 0.000 claims description 23
- 239000000203 mixture Substances 0.000 claims description 19
- 239000012808 vapor phase Substances 0.000 claims description 19
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 8
- 239000011593 sulfur Substances 0.000 claims description 8
- 229910052717 sulfur Inorganic materials 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 238000011084 recovery Methods 0.000 claims description 7
- 238000000034 method Methods 0.000 abstract description 30
- 230000008569 process Effects 0.000 abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 19
- 230000006872 improvement Effects 0.000 abstract description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 28
- 239000007789 gas Substances 0.000 description 20
- 229910000027 potassium carbonate Inorganic materials 0.000 description 14
- 238000005265 energy consumption Methods 0.000 description 11
- 239000002918 waste heat Substances 0.000 description 9
- 239000000571 coke Substances 0.000 description 7
- 230000009471 action Effects 0.000 description 6
- 230000005484 gravity Effects 0.000 description 6
- 238000004939 coking Methods 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000002912 waste gas Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000013475 authorization Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- WVULZDFWPQCPPJ-UHFFFAOYSA-N potassium;hydrochloride Chemical compound Cl.[K] WVULZDFWPQCPPJ-UHFFFAOYSA-N 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
Description
技术领域technical field
本实用新型涉及煤气净化脱硫技术领域，尤其涉及一种高效节能的真空碳酸盐脱硫富液解吸系统。The utility model relates to the technical field of gas purification and desulfurization, in particular to a high-efficiency and energy-saving vacuum carbonate desulfurization and rich liquid desorption system.
背景技术Background technique
真空碳酸钾法脱硫工序一般设于焦炉煤气净化流程的末端。真空碳酸钾法脱硫技术是使用碳酸钾溶液直接吸收煤气中的H2S和HCN。含硫煤气通过碳酸盐脱硫塔与贫液(碳酸钾溶液)逆流接触，吸收煤气中的酸性气体H2S、HCN，脱硫富液再送至解吸塔进行脱硫解吸再生。解吸塔在负压下运行，脱硫富液与解吸塔底上升的解吸蒸汽逆流接触，使酸性气体从脱硫富液中解析出来，解吸后的贫液再送至脱硫塔循环使用。真空碳酸钾法脱硫工艺的产品为含H2S和HCN浓度较高的酸汽，可进一步送至硫磺回收单元或制酸单元进行回收利用。The vacuum potassium carbonate desulfurization process is generally located at the end of the coke oven gas purification process. Vacuum potassium carbonate desulfurization technology uses potassium carbonate solution to directly absorb H 2 S and HCN in coal gas. The sulfur-containing gas is in countercurrent contact with the lean liquid (potassium carbonate solution) through the carbonate desulfurization tower to absorb the acid gas H 2 S and HCN in the gas, and the desulfurized rich liquid is sent to the desorption tower for desulfurization, desorption and regeneration. The desorption tower operates under negative pressure, and the desulfurization rich liquid is in countercurrent contact with the desorption steam rising at the bottom of the desorption tower, so that the acid gas is desorbed from the desulfurized rich liquid, and the desorbed lean liquid is sent to the desulfurization tower for recycling. The product of the vacuum potassium carbonate desulfurization process is acid vapor with high concentration of H 2 S and HCN, which can be further sent to the sulfur recovery unit or the acid production unit for recycling.
目前，焦化行业中真空碳酸盐脱硫工艺多采用汽提法配合较大的真空度进行脱硫富液解吸，以此增加H2S和HCN的脱除率。但采用汽提法对脱硫富液进行再生需要的能耗较高，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，成为行业内技术人员普遍关注的问题。At present, the vacuum carbonate desulfurization process in the coking industry mostly adopts the stripping method with a larger vacuum degree for desulfurization and rich liquid desorption, so as to increase the removal rate of H 2 S and HCN. However, the use of stripping method to regenerate the desulfurized rich liquid requires high energy consumption. Therefore, how to improve the energy utilization rate of the vacuum carbonate desulfurization and rich liquid desorption process and reduce the energy consumption per unit has become a common concern of technicians in the industry.
授权公告号为CN 100560698C的中国实用新型专利公开了一种“直接利用荒煤气余热为解吸热源的真空碳酸盐法煤气脱硫工艺及其设备”，采用荒煤气余热为真空碳酸盐脱硫富液解吸提供热源，具体方式为在初冷器上段设置换热段，利用80℃左右的焦炉煤气在初冷器上段换热段为碳酸盐脱硫解吸塔底贫液进行强制循环换热，为碳酸盐脱硫富液汽提再生过程提供绝大部分热源或所全部热源；该方法整合了焦化厂大部分的低品位余热，较大地节省了真空碳酸盐脱硫富液解吸过程的能源消耗。但是，该工艺虽然将荒煤气的余热利用在真空碳酸盐脱硫解吸过程中，却并没有提高碳酸盐脱硫富液解吸工艺中自身的能耗效率，且循环水耗量仍然较大。当焦化厂采用真空碳酸盐脱硫工艺时，荒煤气的余热大部分用于脱硫富液解吸过程，而这部分余热本可用于厂内制冷系统等可以利用低品质余热地方，因而该工艺并不能真正降低工厂自身的能耗。The Chinese utility model patent with the authorization announcement number CN 100560698C discloses a "vacuum carbonate gas desulfurization process and its equipment which directly utilizes the waste heat of the waste gas as a heat source for desorption", and uses the waste heat of the waste gas as the vacuum carbonate desulfurization rich liquid Desorption provides heat source. The specific method is to set up a heat exchange section in the upper section of the primary cooler, and use coke oven gas at about 80°C in the upper section of the primary cooler to perform forced circulation heat exchange for the lean liquid at the bottom of the carbonate desulfurization desorption tower, which is as follows: The carbonate desulfurization and rich liquid stripping regeneration process provides most or all of the heat sources; this method integrates most of the low-grade waste heat in the coking plant, and greatly saves the energy consumption of the vacuum carbonate desulfurization and rich liquid desorption process. However, although this process utilizes the waste heat of waste gas in the vacuum carbonate desulfurization and desorption process, it does not improve its own energy consumption efficiency in the carbonate desulfurization and rich liquid desorption process, and the consumption of circulating water is still large. When the coking plant adopts the vacuum carbonate desulfurization process, most of the waste heat of the waste gas is used in the desulfurization and rich liquid desorption process, and this part of the waste heat can be used in the refrigeration system in the plant and other places where low-quality waste heat can be used, so this process cannot Really reduce the energy consumption of the factory itself.
授权公告号为CN 104629818 B的中国实用新型专利公开了一种“真空碳酸盐法脱硫富液双效解吸工艺及系统”，采用蒸氨过程中塔顶氨汽的潜热作为真空碳酸盐脱硫富液解吸的部分热源，其整合了焦化厂的部分低品位余热，提高了工厂自身的能源利用率。但此工艺方法能够利用的余热量只占真空碳酸盐脱硫富液解吸塔底用热量的19％左右，真空碳酸盐脱硫富液解吸工艺的能耗仍然较高。The Chinese utility model patent with the authorization announcement number CN 104629818 B discloses a "vacuum carbonate desulfurization and rich liquid double-effect desorption process and system", using the latent heat of the ammonia vapor at the top of the tower during the ammonia distillation process as the vacuum carbonate desulfurization Part of the heat source of the rich liquid desorption integrates part of the low-grade waste heat of the coking plant and improves the energy utilization rate of the plant itself. However, the waste heat that can be utilized by this process method only accounts for about 19% of the heat used at the bottom of the vacuum carbonate desulfurization and rich liquid desorption tower, and the energy consumption of the vacuum carbonate desulfurization and rich liquid desorption process is still high.
发明内容SUMMARY OF THE INVENTION
本实用新型提供了一种真空碳酸盐脱硫富液解吸系统，采用增压机将脱硫富液解吸塔顶部的酸汽增压以提升酸汽的温度，再将增压提温后的酸汽作为脱硫富液解吸塔的热源，充分利用了塔顶酸汽中水蒸汽的潜热；设备投资少、运行费用低、工艺流程简单，实现了真空碳酸盐脱硫富液解吸工艺的高效节能改进。The utility model provides a vacuum carbonate desulfurization and rich liquid desorption system, which adopts a supercharger to pressurize the acid vapor at the top of a desulfurization and rich liquid desorption tower to increase the temperature of the acid vapor, and then pressurizes the acid vapor after the temperature increase. As the heat source of the desulfurization and rich liquid desorption tower, the latent heat of water vapor in the acid vapor at the top of the tower is fully utilized; the equipment investment is low, the operation cost is low, and the process flow is simple, which realizes the high-efficiency and energy-saving improvement of the vacuum carbonate desulfurization and rich liquid desorption process.
为了达到上述目的，本实用新型采用以下技术方案实现：In order to achieve the above object, the utility model adopts the following technical solutions to realize:
一种真空碳酸盐脱硫富液解吸系统，包括脱硫富液解吸塔﹑1#汽液分离器、增压机﹑ 1#再沸器﹑2#汽液分离器、酸汽冷却器﹑3#汽液分离器、真空泵、回流液泵、贫液泵、贫富液换热器、贫液冷却器及2#再沸器；1#再沸器、2#再沸器设于脱硫富液解吸塔的底部两侧，分别通过对应的脱硫贫液循环管道与脱硫富液解吸塔相连；A vacuum carbonate desulfurization and rich liquid desorption system, including a desulfurization and rich liquid desorption tower, a 1# vapor-liquid separator, a booster, a 1# reboiler, a 2# vapor-liquid separator, an acid vapor cooler, a 3# Vapor-liquid separator, vacuum pump, reflux liquid pump, lean liquid pump, lean-rich liquid heat exchanger, lean liquid cooler and 2# reboiler; 1# reboiler and 2# reboiler are located in desulfurization and rich liquid desorption Both sides of the bottom of the tower are respectively connected with the desulfurization rich liquid desorption tower through the corresponding desulfurization lean liquid circulation pipeline;
脱硫富液解吸塔的上部设脱硫富液入口连接脱硫富液管道，脱硫富液管道上设贫富液换热器；贫富液换热器的脱硫贫液入口通过贫液入口管连接脱硫富液解吸塔底部的脱硫贫液出口，贫液入口管上设贫液泵；贫富液换热器的脱硫贫液出口通过贫液出口管连接脱硫塔上的脱硫贫液入口，贫液出口管上设贫液冷却器；The desulfurization and rich liquid inlet is connected to the desulfurization and rich liquid pipeline on the upper part of the desulfurization and rich liquid stripping tower, and the lean and rich liquid heat exchanger is arranged on the desulfurization and rich liquid pipeline; The desulfurization lean liquid outlet at the bottom of the liquid desorption tower, and the lean liquid inlet pipe is provided with a lean liquid pump; the desulfurization and lean liquid outlet of the lean rich liquid heat exchanger is connected to the desulfurization lean liquid inlet on the desulfurization tower through the lean liquid outlet pipe, and the lean liquid outlet pipe A lean liquid cooler is installed on it;
脱硫富液解吸塔的顶部设酸汽出口管连接1#汽液分离器的汽液混合物入口，1#汽液分离器的液相出口通过管道连接脱硫富液解吸塔上部的液相入口；1#汽液分离器的汽相出口通过管道连接1#再沸器的热源入口，对应管道上设增压机；1#再沸器的热源出口通过管道连接2#汽液分离器的汽液混合物入口；The top of the desulfurization and rich liquid desorption tower is provided with an acid vapor outlet pipe connected to the vapor-liquid mixture inlet of the 1# vapor-liquid separator, and the liquid phase outlet of the 1# vapor-liquid separator is connected to the liquid phase inlet of the upper part of the desulfurization and rich liquid desorption tower through a pipeline; 1 #The vapor-phase outlet of the vapor-liquid separator is connected to the heat source inlet of the 1# reboiler through a pipeline, and a booster is installed on the corresponding pipeline; the heat source outlet of the 1# reboiler is connected to the vapor-liquid mixture of the 2# vapor-liquid separator through a pipeline. Entrance;
2#汽液分离器的液相出口通过管道连接脱硫富液解吸塔上部的回流液入口，对应管道上设回流液泵；2#汽液分离器的汽相出口通过管道连接3#汽液分离器的汽液混合物入口，对应管道上设酸汽冷却器；The liquid phase outlet of the 2# vapor-liquid separator is connected to the reflux liquid inlet of the upper part of the desulfurization and rich liquid desorption tower through a pipeline, and a reflux liquid pump is installed on the corresponding pipeline; the vapor phase outlet of the 2# vapor-liquid separator is connected to the 3# vapor-liquid separation through pipeline The inlet of the vapor-liquid mixture of the device, and an acid vapor cooler is installed on the corresponding pipeline;
3#汽液分离器的液相出口通过管道连接2#汽液分离器的液相入口；3#汽液分离器的汽相出口通过管道连接外部的硫磺回收单元或制酸单元，对应管道上设真空泵；The liquid phase outlet of the 3# vapor-liquid separator is connected to the liquid phase inlet of the 2# vapor-liquid separator through a pipeline; the vapor phase outlet of the 3# vapor-liquid separator is connected to the external sulfur recovery unit or acid production unit through a pipeline, and the corresponding pipeline Set up a vacuum pump;
2#再沸器的热源入口连接外部热源管道。The heat source inlet of the 2# reboiler is connected to the external heat source pipeline.
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 present utility model are:
(1)能源消耗大大降低：(1) Energy consumption is greatly reduced:
相比传统的真空碳酸盐脱硫富液解吸技术，采用本实用新型所述工艺进行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，在正常生产操作时仅消耗较少的余热水或蒸汽，节省了75％左右的余热水消耗或蒸汽消耗；在循环水消耗方面，节省了81.5％左右的循环水消耗；在电能消耗方面，新增耗电仅为0.009度/Nm3煤气；总运行成本可降低68％～81％。Compared with the traditional vacuum carbonate desulfurization and rich liquid desorption technology, the process of the present utility model is used to carry out carbonate desulfurization and rich liquid desorption. In terms of waste hot water consumption or steam consumption, it is only necessary to add temporary steam or surplus liquid at the start of construction. Hot water, only consumes less residual hot water or steam during normal production operations, saving about 75% of residual hot water consumption or steam consumption; in terms of circulating water consumption, it saves about 81.5% of circulating water consumption; In terms of power consumption, the newly added power consumption is only 0.009 kWh/Nm 3 gas; the total operating cost can be reduced by 68% to 81%.
(2)设备投资小：(2) Small investment in equipment:
相对于现有技术，仅增加了增压机、再沸器、汽液分离器以及回流液泵等设备，但却节省了传统真空碳酸盐脱硫富液解吸系统中的酸汽冷凝冷却器；Compared with the prior art, only equipment such as a booster, a reboiler, a vapor-liquid separator and a reflux liquid pump are added, but the acid vapor condensation cooler in the traditional vacuum carbonate desulfurization and rich liquid desorption system is saved;
(3)工艺流程较为简单，操作方便，运行费用低。(3) The technological process is relatively simple, the operation is convenient, and the operating cost is low.
附图说明Description of drawings
图1是本实用新型所述一种真空碳酸盐脱硫富液解吸系统的结构示意图。FIG. 1 is a schematic structural diagram of a vacuum carbonate desulfurization rich liquid desorption system according to the present invention.
图中：1.脱硫富液解吸塔 2.1#汽液分离器 3.增压机 4.1#再沸器 5.2#汽液分离器 6.酸汽冷却器 7.3#汽液分离器 8.真空泵 9.回流液泵 10.贫液泵 11.贫富液换热器12.贫液冷却器 13.2#再沸器In the picture: 1. Desulfurization rich liquid desorption tower 2.1# vapor-liquid separator 3. Booster 4.1# reboiler 5.2# vapor-liquid separator 6. Acid vapor cooler 7.3# vapor-
具体实施方式Detailed ways
下面结合附图对本实用新型的具体实施方式作进一步说明：The specific embodiments of the present utility model will be further described below in conjunction with the accompanying drawings:
如图1所示，本实用新型所述一种真空碳酸盐脱硫富液解吸系统，包括脱硫富液解吸塔1﹑1#汽液分离器2、增压机3﹑1#再沸器4﹑2#汽液分离器5、酸汽冷却器6﹑3#汽液分离器7、真空泵8、回流液泵9、贫液泵10、贫富液换热器11、贫液冷却器12及2#再沸器13；1#再沸器4、2#再沸器13设于脱硫富液解吸塔1的底部两侧，分别通过对应的脱硫贫液循环管道与脱硫富液解吸塔1相连；As shown in Figure 1, a vacuum carbonate desulfurization and rich liquid desorption system according to the present utility model comprises a desulfurization and rich liquid desorption tower 1, a 1# vapor-liquid separator 2, a booster 3, a 1# reboiler 4 ﹑2# vapor-
脱硫富液解吸塔1的上部设脱硫富液入口连接脱硫富液管道，脱硫富液管道上设贫富液换热器11；贫富液换热器11的脱硫贫液入口通过贫液入口管连接脱硫富液解吸塔1底部的脱硫贫液出口，贫液入口管上设贫液泵10；贫富液换热器11的脱硫贫液出口通过贫液出口管连接脱硫塔上的脱硫贫液入口，贫液出口管上设贫液冷却器12；The upper part of the desulfurization and rich liquid stripping tower 1 is provided with a desulfurization and rich liquid inlet connected to a desulfurization and rich liquid pipeline, and a lean and rich
脱硫富液解吸塔1的顶部设酸汽出口管连接1#汽液分离器2的汽液混合物入口，1#汽液分离器2的液相出口通过管道连接脱硫富液解吸塔1上部的液相入口；1#汽液分离器2的汽相出口通过管道连接1#再沸器4的热源入口，对应管道上设增压机3；1#再沸器4 的热源出口通过管道连接2#汽液分离器5的汽液混合物入口；The top of the desulfurization and rich liquid desorption tower 1 is provided with an acid vapor outlet pipe to connect the vapor-liquid mixture inlet of the 1# vapor-liquid separator 2, and the liquid phase outlet of the 1# vapor-liquid separator 2 is connected to the upper part of the desulfurization and rich liquid desorption tower 1 through a pipeline. Phase inlet; the vapor phase outlet of 1# vapor-liquid separator 2 is connected to the heat source inlet of 1# reboiler 4 through a pipeline, and a booster 3 is installed on the corresponding pipeline; the heat source outlet of 1# reboiler 4 is connected to 2# through a pipeline The vapor-liquid mixture inlet of vapor-
2#汽液分离器5的液相出口通过管道连接脱硫富液解吸塔1上部的回流液入口，对应管道上设回流液泵9；2#汽液分离器5的汽相出口通过管道连接3#汽液分离器7的汽液混合物入口，对应管道上设酸汽冷却器6；The liquid phase outlet of the 2# vapor-
3#汽液分离器7的液相出口通过管道连接2#汽液分离器5的液相入口；3#汽液分离器7的汽相出口通过管道连接外部的硫磺回收单元或制酸单元，对应管道上设真空泵8；The liquid-phase outlet of the 3# vapor-liquid separator 7 is connected to the liquid-phase inlet of the 2# vapor-
2#再沸器13的热源入口连接外部热源管道。The heat source inlet of the 2
本实用新型所述一种真空碳酸盐脱硫富液解吸系统是一种高效节能型的系统，其工作原理是：脱硫富液经贫富液换热器11升温后进入脱硫富液解吸塔1顶部进行解吸，塔顶酸汽经脱除夹带液滴后再经增压机8加压升温，然后进入塔底再沸器与脱硫贫液进行换热，为脱硫富液解吸提供所需的大部分热量；脱硫富液解吸操作所需的其余少量热量由外部热源(如余热水、低压蒸汽等)提供。The vacuum carbonate desulfurization and rich liquid desorption system described in the utility model is a high-efficiency and energy-saving system. The top is desorbed, and the acid vapor at the top of the column is removed from the entrained liquid droplets, and then pressurized and heated by the
本实用新型所述一种真空碳酸盐脱硫富液解吸系统的工艺过程如下：The technical process of the vacuum carbonate desulfurization rich liquid desorption system described in the utility model is as follows:
(1)脱硫后的碳酸盐脱硫富液经贫富液换热器11与脱硫富液解吸塔1底部抽出的脱硫贫液换热后，进入脱硫富液解吸塔1顶部进行解吸操作；(1) after the carbonate desulfurization rich liquid after desulfurization exchanges heat with the desulfurization lean liquid drawn from the bottom of the desulfurization and rich liquid stripping tower 1 through the lean and rich
(2)脱硫富液解吸塔1顶部的酸汽进入1#汽液分离器2脱除汽相气流夹带的液滴，分离出的液相在重力作用下进入脱硫富液解吸塔1顶部，分离出的汽相经增压机3进行加压升温；(2) The acid vapor at the top of the desulfurization-rich liquid stripping tower 1 enters the 1# vapor-liquid separator 2 to remove the droplets entrained by the vapor-phase gas flow, and the separated liquid phase enters the top of the desulfurization-rich liquid stripping tower 1 under the action of gravity, and separates The outgoing vapor phase is pressurized and heated by the supercharger 3;
(3)酸汽经加压升温后进入脱硫富液解吸塔1底部的1#再沸器4，与脱硫富液解吸塔1底部的脱硫贫液进行换热成为汽液混合物一，为脱硫富液解吸提供大部分热量，其余小部分热量由外部热源提供；(3) The acid vapor enters the 1# reboiler 4 at the bottom of the desulfurization and rich liquid stripping tower 1 after being pressurized and heated, and exchanges heat with the desulfurized lean liquid at the bottom of the desulfurization and rich liquid stripping tower 1 to become a vapor-liquid mixture 1, which is a desulfurization rich liquid. Liquid desorption provides most of the heat, and a small part of the heat is provided by external heat sources;
(4)从1#再沸器4出来的汽液混合物一进入2#汽液分离器5进行汽液分离，分离出的液相经回流液泵9进入脱硫富液解吸塔1顶部，分离出的汽相进入酸汽冷却器6被循环水冷却为汽液混合物二；(4) As soon as the vapor-liquid mixture coming out from the 1# reboiler 4 enters the 2# vapor-
(5)从酸汽冷却器6出来的汽液混合物二进入3#汽液分离器7再次进行汽液分离，分离出的液相在重力作用下进入2#汽液分离器5，分离出的汽相酸汽进入真空泵8，被抽吸送至硫磺回收单元或制酸单元；(5) The second vapor-liquid mixture from the acid vapor cooler 6 enters the 3# vapor-liquid separator 7 for vapor-liquid separation again, and the separated liquid phase enters the 2# vapor-
(6)脱硫富液解吸塔1底部的脱硫贫液经贫液泵10抽取，经贫富液换热器11与进脱硫富液解吸塔1前的脱硫富液换热，再经贫液冷却器12被低温水冷却后，送至脱硫塔进行脱硫；(6) The desulfurization lean liquid at the bottom of the desulfurization and rich liquid stripping tower 1 is extracted by the lean
(7)外部热源经2#再沸器13与脱硫富液解吸塔1底部的脱硫贫液进行换热，为脱硫富液解吸提供步骤(3)中的其余小部分热量。(7) The external heat source exchanges heat with the desulfurization lean liquid at the bottom of the desulfurization rich liquid desorption tower 1 through the 2
所述步骤(1)中，与脱硫贫液换热后的碳酸盐脱硫富液温度为45℃～55℃；脱硫富液解吸塔1的顶部压力为-88kPag～-75kPag，塔顶温度为50℃～65℃。In the step (1), the temperature of the carbonate desulfurization rich liquid after heat exchange with the desulfurized lean liquid is 45° C. to 55° C.; 50℃～65℃.
所述步骤(2)中，增压机3出口的酸汽排出压力为-68kPag～-55kPag。In the step (2), the discharge pressure of the acid vapor at the outlet of the supercharger 3 is -68kPag～-55kPag.
所述步骤(3)中，汽液混合物一的温度为62℃～72℃。In the step (3), the temperature of the first vapor-liquid mixture is 62°C to 72°C.
所述步骤(4)中，汽液混合物二的温度为33℃～40℃。In the step (4), the temperature of the second vapor-liquid mixture is 33°C to 40°C.
所述步骤(5)中，真空泵入口的酸汽抽取压力为-74kPag～-54kPag；真空泵出口的酸汽排出压力为15kPag～40kPag。In the step (5), the extraction pressure of the acid vapor at the inlet of the vacuum pump is -74kPag～-54kPag; the discharge pressure of the acid vapor at the outlet of the vacuum pump is 15kPag～40kPag.
所述步骤(6)中，被低温水冷却后的脱硫贫液温度为25℃～35℃。In the step (6), the temperature of the desulfurization lean liquid cooled by the low temperature water is 25°C to 35°C.
所述外部热源为低压蒸汽或初冷器余热水。The external heat source is low-pressure steam or residual hot water from the primary cooler.
以下实施例在以本实用新型技术方案为前提下进行实施，给出了详细的实施方式和具体的操作过程，但本实用新型的保护范围不限于下述的实施例。The following examples are implemented on the premise of the technical solutions of the present utility model, and provide detailed implementation manners and specific operation processes, but the protection scope of the present utility model is not limited to the following examples.
【实施例1】[Example 1]
本实施例中，以处理100000Nm3/h焦炉煤气(干气)的真空碳酸钾脱硫中富液解吸为例，焦炉煤气杂质含量：H2S 7.5g/Nm3，真空碳酸钾脱硫净化至200mg/Nm3。In this example, taking the desorption of rich liquid in the vacuum potassium carbonate desulfurization for the treatment of 100000Nm 3 /h coke oven gas (dry gas) as an example, the impurity content of the coke oven gas: H 2 S 7.5g/Nm 3 , and the vacuum potassium carbonate desulfurization and purification to 200mg/ Nm3 .
真空碳酸钾脱硫后的碳酸盐脱硫富液经贫富液换热器与脱硫富液解吸塔底部抽出的脱硫贫液换热到50℃后，进入脱硫富液解吸塔顶部进行解吸操作；脱硫富液解吸塔顶部温度为58℃，压力为-84kPag；脱硫富液解吸塔底部温度为61℃，压力为-82kPag。The carbonate desulfurization rich liquid after vacuum potassium carbonate desulfurization passes through the lean rich liquid heat exchanger and the desulfurized rich liquid extracted from the bottom of the desulfurization and rich liquid desorption tower. The temperature at the top of the rich liquid desorption tower is 58°C and the pressure is -84kPag; the temperature at the bottom of the desulfurization rich liquid desorption tower is 61°C and the pressure is -82kPag.
脱硫富液解吸塔顶部的酸汽进入1#汽液分离器，脱除汽相气流夹带的液滴，分离出的液相在重力作用下进入脱硫富液解吸塔顶部，分离出的汽相经增压机加压升温至 -64kPag、75℃后，进入脱硫富液解吸塔底部的1#再沸器中，与自脱硫富液解吸塔底部的脱硫贫液进行换热，成为温度为69℃的汽液混合物一，为脱硫富液解吸提供大部分热量。The acid vapor at the top of the desulfurization and rich liquid desorption tower enters the 1# vapor-liquid separator to remove the liquid droplets entrained by the vapor phase gas flow. The separated liquid phase enters the top of the desulfurization and rich liquid desorption tower under the action of gravity. After the booster is pressurized and heated to -64kPag and 75°C, it enters into the 1# reboiler at the bottom of the desulfurization and rich liquid stripping tower, and exchanges heat with the desulfurization lean liquid at the bottom of the self-desulfurization and rich liquid stripping tower. The temperature becomes 69°C The vapor-liquid mixture 1 provides most of the heat for the desulfurization rich liquid desorption.
温度为69℃的汽液混合物一进入2#汽液分离器进行汽液分离，分离出的液相经回流液泵进入脱硫富液解吸塔顶部，分离出的汽相进入酸汽冷却器，被循环水冷却至40℃后进入3#汽液分离器再次进行汽液分离；分离出的液相在重力作用下进入2#汽液分离器，分离出的汽相(酸汽)进入真空泵，真空泵抽吸产生-65kPag的负压，被抽吸的酸汽经真空泵加压升温至30kPag、40℃后，送至硫磺回收单元或制酸单元。As soon as the vapor-liquid mixture with a temperature of 69°C enters the 2# vapor-liquid separator for vapor-liquid separation, the separated liquid phase enters the top of the desulfurization and rich liquid desorption tower through the reflux liquid pump, and the separated vapor phase enters the acid vapor cooler and is After the circulating water is cooled to 40°C, it enters the 3# vapor-liquid separator for vapor-liquid separation again; the separated liquid phase enters the 2# vapor-liquid separator under the action of gravity, and the separated vapor phase (acid vapor) enters the vacuum pump. The suction generates a negative pressure of -65kPag, and the sucked acid vapor is pressurized and heated to 30kPag and 40°C by a vacuum pump, and then sent to the sulfur recovery unit or the acid production unit.
脱硫富液解吸塔底部的脱硫贫液经贫液泵抽出，与脱硫富液换热为37℃，再进入贫液冷却器被低温水冷却至28℃后，送至碳酸钾脱硫塔进行脱硫。The desulfurization lean liquid at the bottom of the desulfurization and rich liquid stripping tower is pumped out by the lean liquid pump, and the heat exchange with the desulfurization rich liquid is 37 °C, and then enters the lean liquid cooler and is cooled to 28 °C by low-temperature water, and then sent to the potassium carbonate desulfurization tower for desulfurization.
脱硫富液解吸塔操作所需的其余少量热量由低压蒸汽提供，低压蒸汽经2#再沸器与脱硫富液解吸塔底部的脱硫贫液进行换热，从而为脱硫富液解吸提供少量热量。The remaining small amount of heat required for the operation of the desulfurization and rich liquid desorption tower is provided by the low-pressure steam, and the low-pressure steam exchanges heat with the desulfurized and depleted liquid at the bottom of the desulfurized and rich liquid desorption tower through the 2# reboiler, thereby providing a small amount of heat for the desulfurization and rich liquid desorption.
实施例1中，脱硫富液解吸塔底部脱硫贫液中碳酸钾含量为80g/L左右。In Example 1, the potassium carbonate content in the desulfurization lean liquid at the bottom of the desulfurization rich liquid stripping tower is about 80 g/L.
【实施例2】[Example 2]
本实施例中，以处理100000Nm3/h焦炉煤气(干气)的真空碳酸钾脱硫中富液解吸为例，焦炉煤气杂质含量：H2S 7.5g/Nm3，真空碳酸钾脱硫净化至200mg/Nm3。In this example, taking the desorption of rich liquid in the vacuum potassium carbonate desulfurization for the treatment of 100000Nm 3 /h coke oven gas (dry gas) as an example, the impurity content of the coke oven gas: H 2 S 7.5g/Nm 3 , and the vacuum potassium carbonate desulfurization and purification to 200mg/ Nm3 .
真空碳酸钾脱硫后的碳酸盐脱硫富液经贫富液换热器与脱硫富液解吸塔底部抽出的脱硫贫液换热到50℃后，进入脱硫富液解吸塔顶部进行解吸操作；脱硫富液解吸塔顶部温度为58℃，压力为-84kPag；脱硫富液解吸塔底部温度为61℃，压力为-82kPag。The carbonate desulfurization rich liquid after vacuum potassium carbonate desulfurization passes through the lean rich liquid heat exchanger and the desulfurized rich liquid extracted from the bottom of the desulfurization and rich liquid desorption tower. The temperature at the top of the rich liquid desorption tower is 58°C and the pressure is -84kPag; the temperature at the bottom of the desulfurization rich liquid desorption tower is 61°C and the pressure is -82kPag.
脱硫富液解吸塔顶部的酸汽进入1#汽液分离器，脱除汽相气流夹带的液滴，分离出的液相在重力作用下进入脱硫富液解吸塔顶部，分离出的汽相经增压机加压升温至 -64kPag、75℃后，进入脱硫富液解吸塔底部的1#再沸器中，与脱硫富液解吸塔底部的脱硫贫液进行换热，成为温度为69℃的汽液混合物一，为脱硫富液解吸提供大部分热量。The acid vapor at the top of the desulfurization and rich liquid desorption tower enters the 1# vapor-liquid separator to remove the liquid droplets entrained by the vapor phase gas flow. The separated liquid phase enters the top of the desulfurization and rich liquid desorption tower under the action of gravity. After the booster is pressurized and heated to -64kPag and 75°C, it enters into the 1# reboiler at the bottom of the desulfurization and rich liquid desorption tower, and exchanges heat with the desulfurization lean liquid at the bottom of the desulfurization and rich liquid desorption tower. The temperature becomes 69°C. The vapor-liquid mixture 1 provides most of the heat for the desulfurization and rich liquid desorption.
温度为69℃汽液混合物一进入2#汽液分离器进行汽液分离，分离出的液相经回流液泵进入脱硫富液解吸塔顶部，分离出的汽相进入酸汽冷却器，被循环水冷却至40℃后进入3#汽液分离器再次进行汽液分离；分离出的液相在重力作用下进入2#汽液分离器，分离出的汽相(酸汽)进入真空泵，真空泵抽吸产生-65kPag的负压，被抽吸的酸汽经真空泵加压升温至30kPag、40℃后，送至硫磺回收单元或制酸单元。When the temperature is 69℃, the vapor-liquid mixture enters the 2# vapor-liquid separator for vapor-liquid separation. The separated liquid phase enters the top of the desulfurization and rich liquid desorption tower through the reflux liquid pump, and the separated vapor phase enters the acid vapor cooler and is circulated After the water is cooled to 40°C, it enters the 3# vapor-liquid separator for vapor-liquid separation again; the separated liquid phase enters the 2# vapor-liquid separator under the action of gravity, and the separated vapor phase (acid vapor) enters the vacuum pump, which is pumped by the vacuum pump. A negative pressure of -65kPag is generated by suction, and the suctioned acid vapor is pressurized and heated to 30kPag and 40°C by a vacuum pump, and then sent to the sulfur recovery unit or the acid production unit.
脱硫富液解吸塔底部的脱硫贫液经贫液泵抽出，与脱硫富液换热为37℃，再进入贫液冷却器被低温水冷却至28℃后，送至碳酸钾脱硫塔进行脱硫。The desulfurization lean liquid at the bottom of the desulfurization and rich liquid stripping tower is pumped out by the lean liquid pump, and the heat exchange with the desulfurization rich liquid is 37 °C, and then enters the lean liquid cooler and is cooled to 28 °C by low-temperature water, and then sent to the potassium carbonate desulfurization tower for desulfurization.
脱硫富液解吸塔操作所需的其余少量热量由初冷器余热水(温度为73℃～63℃)提供，初冷器余热水经2#再沸器与脱硫富液解吸塔底部的脱硫贫液进行换热，从而为脱硫富液解吸提供少量热量。The remaining small amount of heat required for the operation of the desulfurization and rich liquid desorption tower is provided by the residual hot water of the primary cooler (temperature is 73℃～63℃). The desulfurization lean liquid conducts heat exchange, thereby providing a small amount of heat for the desorption of the desulfurization rich liquid.
实施例2中，脱硫富液解吸塔底部脱硫贫液中碳酸钾含量为80g/L左右。In Example 2, the potassium carbonate content in the desulfurization lean liquid at the bottom of the desulfurization rich liquid stripping tower is about 80 g/L.
本实用新型所述一种真空碳酸盐脱硫富液解吸系统的经济效益分析：Economic benefit analysis of a vacuum carbonate desulfurization rich liquid desorption system described in the utility model:
以处理H2S含量为7.5g/Nm3的100000Nm3/h焦炉煤气(干气)、真空碳酸钾脱硫净化至 200mg/Nm3的脱硫富液解吸为例，三种真空盐酸盐脱硫富液解吸系统的能耗对比详见表1。Taking the treatment of 100,000Nm 3 /h coke oven gas (dry gas) with H 2 S content of 7.5g/Nm 3 and the desulfurization and rich liquid desorption of vacuum potassium carbonate desulfurization and purification to 200mg/Nm 3 as examples, three kinds of vacuum hydrochloride desulfurization The energy consumption comparison of the rich liquid desorption system is shown in Table 1.
表1 三种真空盐酸钾脱硫富液解吸系统的能耗效益比较Table 1 Comparison of energy consumption and benefits of three vacuum potassium hydrochloride desulfurization and rich liquid desorption systems
由表1可知：本实用新型所述真空碳酸盐脱硫富液解吸系统较目前应用普遍的常规真空盐酸盐脱硫富液解吸系统，总运行成本降低了68％～81％，大幅降低了焦化等企业真空盐酸盐脱硫富液解吸系统的能耗，从根本上解决了现有真空碳酸盐脱硫单元存在的高能耗问题。As can be seen from Table 1: the vacuum carbonate desulfurization and rich liquid desorption system of the present utility model reduces the total operating cost by 68% to 81% compared with the commonly used conventional vacuum hydrochloride desulfurization and rich liquid desorption system, and greatly reduces the coking rate. The energy consumption of the vacuum hydrochloride desulfurization rich liquid desorption system of other enterprises has fundamentally solved the high energy consumption problem of the existing vacuum carbonate desulfurization unit.
以上所述，仅为本实用新型较佳的具体实施方式，但本实用新型的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本实用新型揭露的技术范围内，根据本实用新型的技术方案及其实用新型构思加以等同替换或改变，都应涵盖在本实用新型的保护范围之内。The above description is only a preferred embodiment of the present invention, but the protection scope of the present invention is not limited to this. Equivalent replacement or modification of the new technical solution and its utility model concept shall be included within the protection scope of the present utility model.
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