CN221637366U - Negative pressure ammonia distillation device adopting residual heat of benzene removal tower top - Google Patents
Negative pressure ammonia distillation device adopting residual heat of benzene removal tower top Download PDFInfo
- Publication number
- CN221637366U CN221637366U CN202323406420.3U CN202323406420U CN221637366U CN 221637366 U CN221637366 U CN 221637366U CN 202323406420 U CN202323406420 U CN 202323406420U CN 221637366 U CN221637366 U CN 221637366U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- tower
- heat exchanger
- communicated
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 255
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 131
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 238000004821 distillation Methods 0.000 title claims abstract description 74
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 78
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 78
- 239000002918 waste heat Substances 0.000 claims abstract description 35
- 239000007789 gas Substances 0.000 claims abstract description 23
- 239000012808 vapor phase Substances 0.000 claims abstract description 18
- 239000002351 wastewater Substances 0.000 claims description 41
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 238000004939 coking Methods 0.000 abstract description 18
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000011027 product recovery Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 description 34
- 230000008020 evaporation Effects 0.000 description 34
- 238000000034 method Methods 0.000 description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 235000019198 oils Nutrition 0.000 description 7
- 230000002378 acidificating effect Effects 0.000 description 6
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 1
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 238000013475 authorization Methods 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 235000019476 oil-water mixture Nutrition 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
本实用新型属于炼焦化工产品回收技术领域，尤其涉及一种采用脱苯塔顶余热的负压蒸氨装置，其特征在于，包括脱酸塔、蒸氨塔、真空设备、脱苯塔和油汽余热换热器等；剩余氨水管道与氨水换热器相连通；氨水换热器剩余氨水出口与脱酸塔顶部相连通；氨水换热器的热氨水出口与蒸氨塔中部相连通；蒸氨塔顶部与氨分缩器直接相连；氨分缩器氨汽出口与真空设备相连通；油汽余热换热器壳程出口与蒸氨塔底部汽相空间相连通；脱苯塔顶部汽相出口与油汽余热换热器管程汽相入口相连通。与现有焦化焦化粗苯蒸馏与蒸氨技术相比，本实用新型有益之处是能够大幅降低焦化蒸氨和粗苯蒸馏的运行成本。
The utility model belongs to the technical field of coking chemical product recovery, and particularly relates to a negative pressure ammonia distillation device using waste heat from the top of a debenzene tower, characterized in that it includes a deacidification tower, an ammonia distillation tower, a vacuum device, a debenzene tower and an oil-gas waste heat exchanger, etc.; the residual ammonia water pipeline is connected to the ammonia water heat exchanger; the residual ammonia water outlet of the ammonia water heat exchanger is connected to the top of the deacidification tower; the hot ammonia water outlet of the ammonia water heat exchanger is connected to the middle of the ammonia distillation tower; the top of the ammonia distillation tower is directly connected to the ammonia decompressor; the ammonia vapor outlet of the ammonia decompressor is connected to the vacuum device; the shell side outlet of the oil-gas waste heat exchanger is connected to the vapor phase space at the bottom of the ammonia distillation tower; the vapor phase outlet at the top of the debenzene tower is connected to the vapor phase inlet of the oil-gas waste heat exchanger tube side. Compared with the existing coking coking crude benzene distillation and ammonia distillation technology, the utility model is beneficial in that it can greatly reduce the operating costs of coking ammonia distillation and crude benzene distillation.
Description
技术领域Technical Field
本实用新型属于炼焦化工产品回收技术领域，尤其涉及一种采用脱苯塔顶余热的负压蒸氨装置。The utility model belongs to the technical field of coking chemical product recovery, and particularly relates to a negative pressure ammonia distillation device using waste heat from the top of a debenzene tower.
背景技术Background Art
目前焦化企业的剩余氨水蒸氨普遍采用蒸汽汽提法常压下进行氨的分离与回收，以此来降低废水中的氨氮含量。但常压蒸氨工艺技术成熟，操作稳定，但此工艺消耗蒸汽量较大，每处理1吨剩余氨水约消耗170～200kg的低压蒸汽，耗能较大，运行成本较高。At present, the coking enterprises generally use steam stripping method to separate and recover ammonia under normal pressure to reduce the ammonia nitrogen content in the wastewater. However, the atmospheric pressure ammonia distillation process is mature and stable in operation, but this process consumes a large amount of steam. For every ton of residual ammonia water treated, about 170 to 200 kg of low-pressure steam is consumed, which consumes a lot of energy and has a high operating cost.
为解决蒸氨过程能耗较高的问题，热泵蒸氨工艺和负压蒸氨工艺等节能工艺被陆续创新实践应用。其中热泵蒸氨工艺采用第二类吸收式热泵将蒸氨塔顶氨汽的潜热回收用于加热塔底废水，提供部分热源，节省了蒸氨的能源消耗。此工艺能够降低34％的蒸氨运行成本，但此工艺增加了较多设备，固定设备投资较大，也使得蒸氨操作变得更加复杂。负压蒸氨工艺采用降低蒸氨塔的操作温度，能够利用其他工序的余热作为蒸氨的热源进行节能降耗；其他工序的余热可为荒煤气余热、循环氨水余热以及烟道气余热等；但现有负压蒸氨工艺均采用真空设备对冷凝后的不凝含氨酸汽进行抽吸产生负压，不凝含氨酸汽的介质特性对真空设备的材质要求较高，且较多负压蒸氨工艺不能获得浓度较高的浓氨水。In order to solve the problem of high energy consumption in the ammonia evaporation process, energy-saving processes such as heat pump ammonia evaporation process and negative pressure ammonia evaporation process have been innovatively applied. Among them, the heat pump ammonia evaporation process uses the second type of absorption heat pump to recover the latent heat of ammonia vapor at the top of the ammonia evaporation tower for heating the wastewater at the bottom of the tower, providing part of the heat source and saving the energy consumption of ammonia evaporation. This process can reduce the operating cost of ammonia evaporation by 34%, but this process adds a lot of equipment, the investment in fixed equipment is large, and the ammonia evaporation operation becomes more complicated. The negative pressure ammonia evaporation process uses the lowering of the operating temperature of the ammonia evaporation tower to use the waste heat of other processes as the heat source for ammonia evaporation to save energy and reduce consumption; the waste heat of other processes can be waste heat from waste gas, waste heat from circulating ammonia water, and waste heat from flue gas, etc.; but the existing negative pressure ammonia evaporation processes all use vacuum equipment to extract the condensed non-condensable ammonia-containing vapor to generate negative pressure. The medium characteristics of non-condensable ammonia-containing vapor have high requirements on the material of vacuum equipment, and many negative pressure ammonia evaporation processes cannot obtain high-concentration concentrated ammonia water.
授权公告号为CN 106673012 B的中国发明专利公开了“一种负压操作生产浓氨水的工艺及装置”，利用干式真空泵对蒸氨塔进行抽吸，能够获得高浓度浓氨水，但此氨水产品中存在有大量的硫化氢、氰化氢和二氧化碳等酸性气体，氨水产品中存在有大量的铵盐，容易产生盐结晶，产品的纯度也限制了产品氨水的用途。但此工艺仍不能克服含氨酸汽对真空泵的材质要求高的缺点。The Chinese invention patent with the authorization announcement number CN 106673012 B discloses "a process and device for producing concentrated ammonia water by negative pressure operation". By using a dry vacuum pump to pump the ammonia evaporation tower, high-concentration concentrated ammonia water can be obtained. However, the ammonia water product contains a large amount of acidic gases such as hydrogen sulfide, hydrogen cyanide and carbon dioxide. There is a large amount of ammonium salt in the ammonia water product, which is easy to produce salt crystals. The purity of the product also limits the use of the ammonia water product. However, this process still cannot overcome the disadvantage that ammonia-containing gas has high requirements for the material of the vacuum pump.
目前焦化行业的常见的粗苯蒸馏工艺一般分为常压过热蒸汽汽提法粗苯蒸馏工艺和负压过热蒸汽汽提法粗苯蒸馏工艺；负压过热蒸汽汽提法粗苯蒸馏是近10年发展的节能粗苯蒸馏工艺，相对于常压过热蒸汽汽提法粗苯蒸馏工艺，此工艺增加了真空设备等少量投资，但能够大幅降低过热蒸汽的消耗。除新建焦化厂，当前国内较多焦化老厂仍采用常压过热蒸汽汽提法粗苯蒸馏工艺，常压粗苯蒸馏工艺中脱苯塔顶出来的93℃左右油汽进入粗苯冷凝冷却器直接被循环水冷凝冷却，这些温度品质较高的含油蒸汽能源利用率较低。At present, the common crude benzene distillation processes in the coking industry are generally divided into atmospheric pressure superheated steam stripping crude benzene distillation process and negative pressure superheated steam stripping crude benzene distillation process; negative pressure superheated steam stripping crude benzene distillation is an energy-saving crude benzene distillation process developed in the past 10 years. Compared with the atmospheric pressure superheated steam stripping crude benzene distillation process, this process adds a small amount of investment such as vacuum equipment, but can greatly reduce the consumption of superheated steam. In addition to the newly built coking plants, many old coking plants in China still use the atmospheric pressure superheated steam stripping crude benzene distillation process. In the atmospheric pressure crude benzene distillation process, the oil vapor at about 93°C coming out of the top of the debenzene tower enters the crude benzene condenser cooler and is directly condensed and cooled by circulating water. The energy utilization rate of these high-quality oil-containing steam at high temperature is low.
实用新型内容Utility Model Content
本实用新型的目的是提供一种采用脱苯塔顶余热的负压蒸氨装置，克服现有技术的不足，通过事先去除剩余氨水中的H2S、CO2和HCN等酸性组份，降低负压蒸氨系统中氨汽的腐蚀能力，降低负压蒸氨系统中真空设备对材质的要求，降低设备投资，延长设备使用周期，可为常压过热蒸汽汽提法粗苯蒸馏工艺提供升级方案。The purpose of the utility model is to provide a negative pressure ammonia distillation device using the waste heat from the top of a debenzene tower, to overcome the shortcomings of the prior art, to reduce the corrosive ability of ammonia vapor in the negative pressure ammonia distillation system by removing acidic components such as H2S , CO2 and HCN in the residual ammonia water in advance, to reduce the material requirements of the vacuum equipment in the negative pressure ammonia distillation system, to reduce equipment investment, to extend the equipment life, and to provide an upgrade plan for the crude benzene distillation process by the atmospheric superheated steam stripping method.
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:
一种采用脱苯塔顶余热的负压蒸氨装置，其特征在于，包括脱酸塔、蒸氨塔、真空设备和和油汽余热换热器等；剩余氨水管道与氨水换热器剩余氨水入口相连通；氨水换热器剩余氨水出口与脱酸塔顶部相连通；脱酸塔底部与热氨水泵入口相连通；热氨水泵出口与氨水换热器热氨水入口相连通；氨水换热器的热氨水出口与蒸氨塔中部相连通；蒸氨塔底部与蒸氨废水泵入口相连通；蒸氨废水泵出口与废水冷却器废水入口相连通；废水冷却器废水出口与生化处理装置相连通；蒸氨塔顶部与氨分缩器直接相连；氨分缩器氨汽出口与真空设备相连通；真空设备出口与氨冷凝器氨汽入口相连通；氨冷凝器氨水出口与氨水用户相连通；蒸氨塔底部与废水循环泵相连通，废水循环泵与油汽余热换热器壳程入口相连通；油汽余热换热器壳程出口与蒸氨塔底部汽相空间相连通；脱苯塔顶部汽相出口与油汽余热换热器管程汽相入口相连通；油汽余热换热器管程汽相出口与粗苯冷凝冷却器汽相入口相连通；NaOH溶液供给管道与蒸氨塔中部管道相连通。A negative pressure ammonia distillation device using waste heat from the top of a debenzene tower, characterized in that it comprises a deacidification tower, an ammonia distillation tower, a vacuum device and an oil-gas waste heat exchanger, etc.; a residual ammonia water pipeline is connected to a residual ammonia water inlet of an ammonia water heat exchanger; a residual ammonia water outlet of an ammonia water heat exchanger is connected to the top of the deacidification tower; the bottom of the deacidification tower is connected to a hot ammonia water pump inlet; the hot ammonia water pump outlet is connected to a hot ammonia water inlet of an ammonia water heat exchanger; the hot ammonia water outlet of the ammonia water heat exchanger is connected to the middle of the ammonia distillation tower; the bottom of the ammonia distillation tower is connected to an ammonia distillation wastewater pump inlet; the ammonia distillation wastewater pump outlet is connected to a wastewater inlet of a wastewater cooler; and the wastewater outlet of the wastewater cooler is connected to a biochemical treatment device The top of the ammonia distillation tower is directly connected to the ammonia expander; the ammonia vapor outlet of the ammonia expander is connected to the vacuum equipment; the vacuum equipment outlet is connected to the ammonia vapor inlet of the ammonia condenser; the ammonia water outlet of the ammonia condenser is connected to the ammonia water user; the bottom of the ammonia distillation tower is connected to the wastewater circulation pump, and the wastewater circulation pump is connected to the shell side inlet of the oil-gas waste heat exchanger; the shell side outlet of the oil-gas waste heat exchanger is connected to the vapor phase space at the bottom of the ammonia distillation tower; the vapor phase outlet at the top of the debenzene tower is connected to the vapor phase inlet of the oil-gas waste heat exchanger tube side; the vapor phase outlet of the oil-gas waste heat exchanger tube side is connected to the vapor phase inlet of the crude benzene condenser cooler; the NaOH solution supply pipeline is connected to the middle pipeline of the ammonia distillation 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)本实用新型中负压蒸氨工艺采用先去除剩余氨水中的H2S、CO2和HCN等酸性组份，降低了负压蒸氨系统中氨汽的腐蚀能力，有效降低了负压蒸氨系统中真空设备对材质的要求，降低了设备投资，延长设备使用周期；1) The negative pressure ammonia distillation process of the utility model adopts the method of first removing acidic components such as H2S , CO2 and HCN in the remaining ammonia water, thereby reducing the corrosive ability of ammonia vapor in the negative pressure ammonia distillation system, effectively reducing the material requirements of the vacuum equipment in the negative pressure ammonia distillation system, reducing equipment investment, and extending the equipment service life;
2)本实用新型中负压蒸氨工艺能够获得不含酸性组份的洁净浓氨水，拓展了产品氨水的用途，提高经济效益；2) The negative pressure ammonia distillation process of the utility model can obtain clean concentrated ammonia water without acidic components, which expands the use of the product ammonia water and improves economic benefits;
3)本实用新型能够降低蒸氨工艺的蒸汽消耗量的同时，也降低了粗苯蒸馏工艺的循环水消耗量，大幅降低了焦化蒸氨和粗苯蒸馏的运行成本；3) The utility model can reduce the steam consumption of the ammonia distillation process, and also reduce the circulating water consumption of the crude benzene distillation process, thereby greatly reducing the operating costs of coking ammonia distillation and crude benzene distillation;
4)本实用新型适用于常压过热蒸汽汽提法粗苯蒸馏工艺，其在原有常压粗苯蒸馏工艺的基础上增加的设备较少，且设备材质要求降低，较少的固定投资和运行成本适合现有焦化厂进行改造升级。4) The utility model is applicable to the crude benzene distillation process of atmospheric superheated steam stripping method. It has less equipment added on the basis of the original atmospheric crude benzene distillation process, and the material requirements of the equipment are reduced. The lower fixed investment and operating cost are suitable for the transformation and upgrading of existing coking plants.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1是本实用新型实施例工艺流程结构示意图；FIG1 is a schematic diagram of the process structure of an embodiment of the utility model;
图中：1-脱苯塔、2-油汽余热换热器、3-粗苯冷凝冷却器、4-蒸氨塔、5-氨分缩器、6-真空设备、7-氨冷凝器、8-废水循环泵、9-蒸氨废水泵、10-废水冷却器、11-脱酸塔、12-热氨水泵、13-氨水换热器。In the figure: 1-benzene removal tower, 2-oil and gas waste heat exchanger, 3-crude benzene condenser cooler, 4-ammonia evaporation tower, 5-ammonia fractionator, 6-vacuum equipment, 7-ammonia condenser, 8-wastewater circulation pump, 9-ammonia evaporation wastewater pump, 10-wastewater cooler, 11-deacidification tower, 12-hot ammonia water pump, 13-ammonia water heat exchanger.
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，是本实用新型一种采用脱苯塔顶余热的负压蒸氨装置实施例结构示意图，包括脱苯塔1、油汽余热换热器2、粗苯冷凝冷却器3、蒸氨塔4、氨分缩器5、真空设备6、氨冷凝器7、废水循环泵8、蒸氨废水泵9、废水冷却器10、脱酸塔11、热氨水泵12、氨水换热器13及连接管道；剩余氨水管道与氨水换热器13剩余氨水入口管道相连；氨水换热器13剩余氨水出口与脱酸塔11顶部管道相连；脱酸塔11底部与热氨水泵12入口管道相连；热氨水泵12出口与氨水换热器13热氨水入口管道相连；氨水换热器13热氨水出口与蒸氨塔4中部管道相连；蒸氨塔4底部与蒸氨废水泵9入口管道相连；蒸氨废水泵9出口与废水冷却器10废水入口管道相连；废水冷却器10废水出口与生化处理装置管道相连；蒸氨塔4顶部与氨分缩器5直接相连；氨分缩器5氨汽出口与真空设备6管道相连；真空设备9出口与氨冷凝器7氨汽入口管道相连；氨冷凝器7氨水出口管道与氨水用户管道相连；蒸氨塔4底部与废水循环泵8相连，废水循环泵8与油汽余热换热器2壳程入口相连；油汽余热换热器2壳程出口与蒸氨塔4底部汽相空间相连；脱苯塔1顶部汽相出口与油汽余热换热器2管程汽相入口相连；油汽余热换热器2管程汽相出口与粗苯冷凝冷却器3汽相入口相连；NaOH溶液供给管道与蒸氨塔4中部管道相连。See Figure 1, which is a schematic structural diagram of an embodiment of a negative pressure ammonia distillation device using waste heat from the top of a debenzene tower of the utility model, comprising a debenzene tower 1, an oil-gas waste heat exchanger 2, a crude benzene condenser cooler 3, an ammonia distillation tower 4, an ammonia fractionator 5, a vacuum device 6, an ammonia condenser 7, a wastewater circulation pump 8, an ammonia distillation wastewater pump 9, a wastewater cooler 10, a deacidification tower 11, a hot ammonia water pump 12, an ammonia water heat exchanger 13 and connecting pipes; the residual ammonia water pipe is connected to the residual ammonia water inlet pipe of the ammonia water heat exchanger 13; the residual ammonia water outlet of the ammonia water heat exchanger 13 is connected to the top pipe of the deacidification tower 11; the bottom of the deacidification tower 11 is connected to the inlet pipe of the hot ammonia water pump 12; the outlet of the hot ammonia water pump 12 is connected to the hot ammonia water inlet pipe of the ammonia water heat exchanger 13; the hot ammonia water outlet of the ammonia water heat exchanger 13 is connected to the middle pipe of the ammonia distillation tower 4; the bottom of the ammonia distillation tower 4 is connected to the inlet pipe of the ammonia water distillation wastewater pump 9 The outlet of ammonia evaporation wastewater pump 9 is connected to the wastewater inlet pipeline of wastewater cooler 10; the wastewater outlet of wastewater cooler 10 is connected to the pipeline of biochemical treatment device; the top of ammonia evaporation tower 4 is directly connected to ammonia decompressor 5; the ammonia vapor outlet of ammonia decompressor 5 is connected to the pipeline of vacuum equipment 6; the outlet of vacuum equipment 9 is connected to the ammonia vapor inlet pipeline of ammonia condenser 7; the ammonia water outlet pipeline of ammonia condenser 7 is connected to the ammonia water user pipeline; the bottom of ammonia evaporation tower 4 is connected to wastewater circulation pump 8, and wastewater circulation pump 8 is connected to the shell side inlet of oil-gas waste heat exchanger 2; the shell side outlet of oil-gas waste heat exchanger 2 is connected to the vapor phase space at the bottom of ammonia evaporation tower 4; the vapor phase outlet at the top of debenzene tower 1 is connected to the vapor phase inlet of oil-gas waste heat exchanger 2 tube side; the vapor phase outlet of oil-gas waste heat exchanger 2 tube side is connected to the vapor phase inlet of crude benzene condenser cooler 3; the NaOH solution supply pipeline is connected to the middle pipeline of ammonia evaporation tower 4.
本实用新型一种采用脱苯塔顶余热的负压蒸氨方法，通过事先去除剩余氨水中的H2S、CO2和HCN等酸性组份，降低负压蒸氨系统中氨汽的腐蚀能力，包括脱酸、蒸氨、废水循环换热、粗苯油汽余热换热，具体步骤如下：The utility model discloses a negative pressure ammonia distillation method using waste heat from the top of a benzene removal tower, which reduces the corrosiveness of ammonia vapor in a negative pressure ammonia distillation system by removing acidic components such as H2S , CO2 and HCN in the residual ammonia water in advance, including deacidification, ammonia distillation, wastewater circulation heat exchange, and crude benzene oil vapor waste heat heat exchange. The specific steps are as follows:
1)脱酸，焦化剩余氨水经氨水换热器13与脱酸塔11底被热氨水泵12抽出的脱酸后剩余氨水进行换热后，进入脱酸塔11顶部进行脱酸操作；低压饱和蒸汽直接进入脱酸塔11底部为剩余氨水脱酸提供汽提蒸汽；脱酸塔11顶部排出的含少量氨酸汽排至脱硫前煤气管道或硫铵饱和器；与脱酸塔11底被热氨水泵12抽出的脱酸后剩余氨水换热后的剩余氨水温度控制为90℃～100℃；1) Deacidification: the residual ammonia water from coking is heat-exchanged with the residual ammonia water after deacidification pumped out by the hot ammonia water pump 12 at the bottom of the deacidification tower 11 through the ammonia water heat exchanger 13, and then enters the top of the deacidification tower 11 for deacidification operation; low-pressure saturated steam directly enters the bottom of the deacidification tower 11 to provide stripping steam for the deacidification of the residual ammonia water; the steam containing a small amount of ammonia discharged from the top of the deacidification tower 11 is discharged to the pre-desulfurization coal gas pipeline or ammonium sulfate saturator; the temperature of the residual ammonia water after heat-exchanging with the residual ammonia water after deacidification pumped out by the hot ammonia water pump 12 at the bottom of the deacidification tower 11 is controlled to be 90°C to 100°C;
2)蒸氨，与焦化剩余氨水换热13后的脱酸后剩余氨水送至蒸氨塔4中部进行蒸氨操作；NaOH溶液进入蒸氨塔4中部进行分解固定铵；蒸氨塔4顶氨汽经氨分缩器5部分冷凝后进入真空设备6进行抽吸，使得蒸氨4塔保持负压蒸氨操作；被抽吸后的氨汽进入氨冷凝器7中被循环水冷却为不含酸性组份的洁净浓氨水；脱酸塔11顶的操作压力为10kPag～30kPag；与焦化剩余氨水换热后的脱酸后剩余氨水温度控制为80～95℃；2) Ammonia distillation: the residual ammonia water after deacidification after heat exchange 13 with the residual ammonia water from coking is sent to the middle of the ammonia distillation tower 4 for ammonia distillation operation; the NaOH solution enters the middle of the ammonia distillation tower 4 to decompose and fix ammonium; the ammonia vapor at the top of the ammonia distillation tower 4 is partially condensed by the ammonia decompressor 5 and then enters the vacuum equipment 6 for suction, so that the ammonia distillation tower 4 maintains a negative pressure ammonia distillation operation; the ammonia vapor after suction enters the ammonia condenser 7 and is cooled by circulating water to become clean concentrated ammonia water without acidic components; the operating pressure at the top of the deacidification tower 11 is 10kPag-30kPag; the temperature of the residual ammonia water after deacidification after heat exchange with the residual ammonia water from coking is controlled to be 80-95°C;
3)废水循环换热，蒸氨塔4底部的蒸氨废水被废水循环泵8抽出送至油汽余热换热器2壳程与粗苯油汽进行换热；换热后的蒸氨废水送至蒸氨塔4底部进行部分闪蒸，为蒸氨操作提供上升汽提蒸汽；蒸氨塔4底部的蒸氨废水由蒸氨废水泵9抽出排至废水冷却器10，经循环水冷却后排至生化处理装置；蒸氨塔4顶的操作压力控制为-90kPag～-80kPag；氨分缩器5后的氨汽温度控制为50℃～60℃；3) Wastewater circulation heat exchange: the ammonia evaporation wastewater at the bottom of the ammonia evaporation tower 4 is pumped out by the wastewater circulation pump 8 and sent to the shell side of the oil-gas waste heat exchanger 2 for heat exchange with crude benzene oil and gas; the ammonia evaporation wastewater after heat exchange is sent to the bottom of the ammonia evaporation tower 4 for partial flash evaporation to provide ascending stripping steam for the ammonia evaporation operation; the ammonia evaporation wastewater at the bottom of the ammonia evaporation tower 4 is pumped out by the ammonia evaporation wastewater pump 9 and discharged to the wastewater cooler 10, and discharged to the biochemical treatment device after circulating water cooling; the operating pressure at the top of the ammonia evaporation tower 4 is controlled to be -90kPag to -80kPag; the ammonia vapor temperature after the ammonia fractionator 5 is controlled to be 50°C to 60°C;
4)粗苯油汽余热换热，脱苯塔1顶部的含油蒸汽进入油汽余热换热器2管程与蒸氨废水换热后，再进入粗苯冷凝冷却器3经循环水和低温水冷却为油水混合物进入后续油水分离操作。脱苯塔1顶部的含油蒸汽进入油汽余热换热器2管程与蒸氨废水换热后为70℃～75℃；脱苯塔1顶的操作压力控制为5kPag～15kPag。4) Heat exchange of crude benzene oil and steam waste heat. The oil-containing steam at the top of the debenzene tower 1 enters the oil-steam waste heat exchanger 2 tube side and exchanges heat with the ammonia waste water, then enters the crude benzene condenser cooler 3 and is cooled by circulating water and low-temperature water to an oil-water mixture to enter the subsequent oil-water separation operation. The oil-containing steam at the top of the debenzene tower 1 enters the oil-steam waste heat exchanger 2 tube side and exchanges heat with the ammonia waste water at 70℃～75℃; the operating pressure at the top of the debenzene tower 1 is controlled to be 5kPag～15kPag.
本实用新型最大优势在于较之以往的焦化粗苯蒸馏和蒸氨，既能够降低蒸氨工艺的蒸汽消耗量的同时，也降低了粗苯蒸馏工艺的循环水消耗量，大幅降低了焦化蒸氨和粗苯蒸馏的运行成本。The greatest advantage of the utility model is that, compared with the previous coking crude benzene distillation and ammonia evaporation, it can not only reduce the steam consumption of the ammonia evaporation process, but also reduce the circulating water consumption of the crude benzene distillation process, thereby greatly reducing the operating costs of coking ammonia evaporation and crude benzene distillation.
以焦化生产能力为250万吨/年焦炭，洗苯用洗油循环量为300m3/h，剩余氨水处理量为100m3/h为例，采用本实用新型采用脱苯塔顶余热的负压蒸氨工艺的蒸氨蒸汽耗量为35kg/吨剩余氨水，相比传统焦化蒸氨工艺的170kg/吨剩余氨水的低压蒸汽耗量，此工艺节省了79.4％的低压蒸汽；粗苯蒸馏循环水耗量为33t/吨粗苯，相比负压过热蒸汽汽提法粗苯蒸馏工艺的102t/吨粗苯的循环水耗量，此工艺节省了67.6％的循环水。Taking the coking production capacity of 2.5 million tons of coke per year, the circulation volume of washing oil for benzene washing of 300m3 /h, and the residual ammonia water treatment volume of 100m3 /h as an example, the ammonia steam consumption of the negative pressure ammonia distillation process using the waste heat from the top of the debenzene tower of the utility model is 35kg/ton of residual ammonia water, which saves 79.4% of low-pressure steam compared with the low-pressure steam consumption of 170kg/ton of residual ammonia water in the traditional coking ammonia distillation process; the circulating water consumption of crude benzene distillation is 33t/ton of crude benzene, which saves 67.6% of circulating water compared with the circulating water consumption of 102t/ton of crude benzene in the crude benzene distillation process using the negative pressure superheated steam stripping method.
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.
Claims (1)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323406420.3U CN221637366U (en) | 2023-12-13 | 2023-12-13 | Negative pressure ammonia distillation device adopting residual heat of benzene removal tower top |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202323406420.3U CN221637366U (en) | 2023-12-13 | 2023-12-13 | Negative pressure ammonia distillation device adopting residual heat of benzene removal tower top |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN221637366U true CN221637366U (en) | 2024-09-03 |
Family
ID=92507156
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202323406420.3U Active CN221637366U (en) | 2023-12-13 | 2023-12-13 | Negative pressure ammonia distillation device adopting residual heat of benzene removal tower top |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN221637366U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117865376A (en) * | 2023-12-13 | 2024-04-12 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure ammonia distillation method and device adopting residual heat of benzene removal tower top |
-
2023
- 2023-12-13 CN CN202323406420.3U patent/CN221637366U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117865376A (en) * | 2023-12-13 | 2024-04-12 | 中冶焦耐(大连)工程技术有限公司 | Negative pressure ammonia distillation method and device adopting residual heat of benzene removal tower top |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN106673014A (en) | Process of removing sulfur and ammonia from coke gas to prepare ammonia water | |
| CN202808402U (en) | Residual ammonia water heat pump distillation system | |
| CN116751613A (en) | An energy-saving negative pressure benzene removal process and system | |
| CN221637366U (en) | Negative pressure ammonia distillation device adopting residual heat of benzene removal tower top | |
| CN219449378U (en) | An energy-saving deacidification and ammonia distillation device | |
| CN116216830B (en) | Energy-saving deacidification and ammonia distillation process and device | |
| CN114212850B (en) | A highly efficient and energy-saving thermally coupled ammonia distillation process | |
| CN104056462B (en) | A kind of heat pump distillation energy saver | |
| CN111744328A (en) | Low-energy-consumption carbon dioxide capturing method and system for low-concentration carbon dioxide-containing tail gas | |
| CN221514023U (en) | A negative pressure deacidification and ammonia distillation treatment device | |
| CN222841531U (en) | A device for producing liquid ammonia by desorption of ammonium phosphate washing ammonia rich liquid | |
| CN221644638U (en) | Ammonia distillation device for double-effect energy-saving residual ammonia water | |
| CN221788177U (en) | Energy-saving negative pressure crude benzene distillation device | |
| CN221522480U (en) | Energy-saving desorption device for vacuum carbonate desulfurization rich liquid | |
| CN219709430U (en) | Energy-saving negative pressure benzene removal system | |
| CN117585746A (en) | Phenol-ammonia wastewater treatment method for saving high-temperature steam based on double-effect phenol tower | |
| CN104629818A (en) | Desulfurization liquid enrichment dual-effect desorption process and system by virtue of vacuum carbonate method | |
| CN111717948A (en) | A coking gas phase circulating ammonia distillation process and device | |
| CN117865376A (en) | Negative pressure ammonia distillation method and device adopting residual heat of benzene removal tower top | |
| CN206244421U (en) | A device for producing concentrated ammonia water by negative pressure operation | |
| CN103387271B (en) | A heat integrated device for ammonia distillation and desulfurization by using chemical products | |
| CN203461846U (en) | Heat integration device for ammonia distillation and desulfurization in chemical production | |
| CN216737642U (en) | High-efficiency energy-saving ammonia distillation system | |
| CN223112690U (en) | Drying oven waste gas recovery system in diaphragm industry |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |