CN108079611B - An intermediate reboiler cascade heating system based on absorption heat pump - Google Patents
An intermediate reboiler cascade heating system based on absorption heat pump Download PDFInfo
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- CN108079611B CN108079611B CN201810126772.8A CN201810126772A CN108079611B CN 108079611 B CN108079611 B CN 108079611B CN 201810126772 A CN201810126772 A CN 201810126772A CN 108079611 B CN108079611 B CN 108079611B
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 92
- 238000010438 heat treatment Methods 0.000 title claims abstract description 29
- 239000000463 material Substances 0.000 claims abstract description 84
- 230000000694 effects Effects 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 239000006096 absorbing agent Substances 0.000 claims description 23
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims 1
- 238000009833 condensation Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 19
- 239000002918 waste heat Substances 0.000 abstract description 7
- 238000001816 cooling Methods 0.000 abstract description 2
- 230000000630 rising effect Effects 0.000 abstract 1
- 238000005194 fractionation Methods 0.000 description 30
- 238000010992 reflux Methods 0.000 description 12
- 238000013475 authorization Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
- F25B30/04—Heat pumps of the sorption type
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- 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
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- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
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Abstract
Description
技术领域technical field
本发明涉及石油炼化技术领域，尤其涉及一种基于吸收式热泵的中间再沸器梯级加热系统。The invention relates to the technical field of petroleum refining, in particular to an intermediate reboiler cascade heating system based on an absorption heat pump.
背景技术Background technique
石油化工行业高耗能、高污染，精馏作为该行业中应用最广泛的分离技术，其能耗占石油化工总能耗的40％以上。常规分馏工艺缺点如下：塔顶物料余热通过塔顶冷凝器散失到环境中，造成大量低品位能源浪费；淳胺再生、脱丙烷、催化蒸馏等分馏塔塔底物料工作温度约110℃，通常采用压力为0.3MPa左右的工艺蒸汽加热，这种加热方式存在较大换热温差，加热环节的熵增较大，能源利用不合理。因此，如果能够利用工艺蒸汽回收塔顶物料低品位余热，制备热量用于系统本身，对于系统节能意义重大。The petrochemical industry has high energy consumption and high pollution. As the most widely used separation technology in this industry, rectification accounts for more than 40% of the total energy consumption of petrochemical industry. The disadvantages of the conventional fractionation process are as follows: the waste heat of the tower top material is lost to the environment through the tower top condenser, causing a lot of low-grade energy waste; Process steam with a pressure of about 0.3MPa is heated. This heating method has a large heat exchange temperature difference, and the entropy of the heating link increases greatly, and the energy utilization is unreasonable. Therefore, if the process steam can be used to recover the low-grade waste heat of the tower top material and prepare the heat for the system itself, it is of great significance for the energy saving of the system.
中国专利申请号为201310206921.9，授权公告日为2015年3月4日，专利名称为一种低温精馏装置，提出利用吸收式热泵回收塔顶物料余热用来加热塔底物料，但受热泵制热温度的限制，该方式仅能用于低温蒸馏，应用范围有限；中国专利申请号为201410483273.6，授权公告日为2016年6月15日，专利名称为一种对气体分馏塔进口物料预热的梯级加热方法及加热系统，提出利用吸收式热泵回收塔顶余热用来对进口物料进行预热处理，但进口物料温度升高影响塔底回流比，系统能效仅能提高15％。The Chinese patent application number is 201310206921.9, the authorization announcement date is March 4, 2015, and the patent name is a cryogenic rectification device. Due to the limitation of temperature, this method can only be used for low-temperature distillation, and the scope of application is limited; the Chinese patent application number is 201410483273.6, the authorization announcement date is June 15, 2016, and the patent name is a cascade for preheating the inlet material of the gas fractionation tower Heating method and heating system, it is proposed to use absorption heat pump to recover the waste heat at the top of the tower to preheat the imported materials, but the increase of the temperature of the imported materials affects the reflux ratio of the bottom of the tower, and the energy efficiency of the system can only be improved by 15%.
发明内容SUMMARY OF THE INVENTION
本发明的目的是提出一种基于吸收式热泵的中间再沸器梯级加热系统，解决现有工艺流程中由于低品位余热排放、换热不匹配导致的能源浪费问题。The purpose of the present invention is to propose an intermediate reboiler cascade heating system based on an absorption heat pump to solve the problem of energy waste caused by low-grade waste heat discharge and heat exchange mismatch in the existing process flow.
为解决上述技术问题，本发明采用如下技术方案：In order to solve the above-mentioned technical problems, the present invention adopts the following technical solutions:
本发明一种基于吸收式热泵的中间再沸器梯级加热系统,包括分馏塔、塔顶冷凝器、回流罐、双效吸收式热泵、单效吸收式热泵、双级大温升热泵、一号中间再沸器、二号中间再沸器、三号中间再沸器和塔底重沸器；The present invention is an intermediate reboiler cascade heating system based on an absorption heat pump, comprising a fractionation tower, a tower top condenser, a reflux tank, a double-effect absorption heat pump, a single-effect absorption heat pump, a double-stage large temperature rise heat pump, and a No. 1 heat pump. Intermediate reboiler, No. 2 intermediate reboiler, No. 3 intermediate reboiler and column bottom reboiler;
所述分馏塔的顶部连接有塔顶产品物料管道，塔顶产品物料管道经三通分为两输出管路，其中一个输出管路通过所述塔顶冷凝器与所述回流罐的入口相连；另一个输出管路与所述双级大温升热泵的蒸发器入口相连，所述双级大温升热泵的蒸发器出口通过塔顶产品物料管道与所述单效吸收式热泵的蒸发器入口相连，所述单效吸收式热泵的蒸发器出口通过塔顶产品物料管道与所述双效吸收式热泵的蒸发器入口相连，所述双效吸收式热泵的蒸发器出口通过塔顶产品物料管道与所述回流罐的入口相连；所述回流罐的出口通过塔顶产品物料管道分别与所述分馏塔、塔顶产品区相连通；The top of the fractionation tower is connected with a column top product material pipeline, and the column top product material pipeline is divided into two output pipelines through a tee, and one of the output pipelines is connected to the inlet of the reflux tank through the column top condenser; The other output pipeline is connected to the evaporator inlet of the two-stage large temperature rise heat pump, and the evaporator outlet of the two-stage large temperature rise heat pump is connected to the evaporator inlet of the single-effect absorption heat pump through the top product material pipeline. connected, the evaporator outlet of the single-effect absorption heat pump is connected with the evaporator inlet of the double-effect absorption heat pump through the tower top product material pipeline, and the evaporator outlet of the double-effect absorption heat pump is connected through the tower top product material pipeline be connected with the inlet of the reflux tank; the outlet of the reflux tank is respectively communicated with the fractionation tower and the top product area through the top product material pipeline;
所述分馏塔的底部通过塔底产品物料管道与所述塔底重沸器的入口相连，所述塔底重沸器的出口通过塔底产品物料管道与分馏塔相连通，所述分馏塔的底部通过塔底产品物料管道与塔底产品区相连通；The bottom of the fractionation column is connected with the inlet of the reboiler at the bottom of the column through the product material pipeline at the bottom of the column, and the outlet of the reboiler at the bottom of the column is communicated with the fractionation column through the product material pipeline at the bottom of the column. The bottom is connected with the bottom product area through the bottom product material pipeline;
所述一号中间再沸器的物料进出口通过一号中间物料管道与所述分馏塔连通，所述二号中间再沸器的物料进出口通二号中间物料管道与所述分馏塔连通，所述三号中间再沸器的物料进出口通过三号中间物料管道与所述分馏塔连通；The material inlet and outlet of the No. 1 intermediate reboiler is communicated with the fractionation tower through the No. 1 intermediate material pipeline, and the material inlet and outlet of the No. 2 intermediate reboiler is communicated with the fractionation tower through the No. 2 intermediate material pipeline, The material inlet and outlet of the No. 3 intermediate reboiler is communicated with the fractionating tower through the No. 3 intermediate material pipeline;
所述双级大温升热泵的吸收器与冷凝器出口通过循环水管道与所述三号中间再沸器的循环水进口相连，所述三号中间再沸器的循环水出口通过循环水管道与所述二号中间再沸器的循环水进口相连，所述二号中间再沸器的循环水出口通过循环水管道与所述一号中间再沸器的循环水进口相连，所述一号中间再沸器的循环水出口通过循环水管道与所述双效吸收式热泵的吸收器及冷凝器入口相连，所述双效吸收式热泵的吸收器及冷凝器出口通过循环水管道与所述单效吸收式热泵的吸收器及冷凝器入口相连，所述单效吸收式热泵的吸收器及冷凝器出口通过循环水管道与所述双级大温升热泵的吸收器与冷凝器入口相连；The absorber and condenser outlet of the two-stage large temperature rise heat pump are connected with the circulating water inlet of the No. 3 intermediate reboiler through a circulating water pipeline, and the circulating water outlet of the No. 3 intermediate reboiler is connected through a circulating water pipeline. It is connected to the circulating water inlet of the No. 2 intermediate reboiler, and the circulating water outlet of the No. 2 intermediate reboiler is connected to the circulating water inlet of the No. 1 intermediate reboiler through a circulating water pipeline. The circulating water outlet of the intermediate reboiler is connected to the absorber and the condenser inlet of the double-effect absorption heat pump through a circulating water pipeline, and the absorber and condenser outlet of the double-effect absorption heat pump are connected to the said double-effect absorption heat pump through a circulating water pipeline. The absorber and the inlet of the condenser of the single-effect absorption heat pump are connected, and the absorber and the outlet of the condenser of the single-effect absorption heat pump are connected with the absorber of the two-stage large temperature rise heat pump and the inlet of the condenser through a circulating water pipeline;
蒸汽通过蒸汽管道分别与所述塔底重沸器的蒸汽入口、所述双效吸收式热泵的发生器入口、所述单效吸收式热泵的发生器入口、所述双级大温升热泵的发生器入口相连通。The steam is respectively connected with the steam inlet of the bottom reboiler, the generator inlet of the double-effect absorption heat pump, the generator inlet of the single-effect absorption heat pump, and the two-stage large temperature rise heat pump through the steam pipeline. The generator inlet is connected.
进一步的，循环水管道上设置有循环泵。Further, a circulating pump is arranged on the circulating water pipeline.
再进一步的，所述双效吸收式热泵发生器、单效吸收式热泵发生器、双级大温升热泵发生器均设置有凝水管道。Still further, the double-effect absorption heat pump generator, the single-effect absorption heat pump generator and the double-stage high temperature rise heat pump generator are all provided with condensate pipes.
再进一步的，所述双效吸收式热泵、单效吸收式热泵、双级大温升热泵均采用蒸汽型溴化锂吸收式热泵。Still further, the double-effect absorption heat pump, the single-effect absorption heat pump, and the two-stage large temperature rise heat pump all use a steam-type lithium bromide absorption heat pump.
再进一步的，所述一号中间再沸器、二号中间再沸器和三号中间再沸器从上向下顺次排布，所述双效吸收式热泵、单效吸收式热泵和双级大温升热泵从上向下顺次排布，且所述一号中间再沸器、二号中间再沸器和三号中间再沸器分别与所述双效吸收式热泵、单效吸收式热泵和双级大温升热泵一一对应。Still further, the No. 1 intermediate reboiler, the No. 2 intermediate reboiler and the No. 3 intermediate reboiler are sequentially arranged from top to bottom, and the double-effect absorption heat pump, single-effect absorption heat pump and double-effect absorption heat pump are arranged in sequence from top to bottom. The high temperature rise heat pumps are arranged in order from top to bottom, and the No. 1 intermediate reboiler, No. 2 intermediate reboiler and No. 3 intermediate reboiler are respectively connected with the double-effect absorption heat pump and single-effect absorption heat pump. One-to-one correspondence between type heat pump and two-stage large temperature rise heat pump.
与现有技术相比，本发明的有益技术效果：Compared with the prior art, the beneficial technical effects of the present invention:
本发明一种基于吸收式热泵的中间再沸器梯级加热系统，利用工艺蒸汽做功能力驱动热泵循环回收塔顶物料低温余热，制备热量加热中间物料，同时采用由双效吸收式热泵、单效吸收式热泵、双级大温升热泵组成的三级热泵形式，实现中间物料梯级升温，塔顶物料梯级降温，进而实现系统能源的梯级利用，显著提高分馏塔能源利用效率，降低工艺蒸汽耗量25％以上。The invention is an intermediate reboiler cascade heating system based on an absorption heat pump, which utilizes the process steam as a power to drive the heat pump to circulate and recover the low temperature waste heat of the tower top material, and prepares the heat to heat the intermediate material. The three-stage heat pump composed of absorption heat pump and two-stage high temperature rise heat pump realizes the stepwise heating of intermediate materials and the stepwise cooling of tower top materials, thereby realizing the step-by-step utilization of system energy, significantly improving the energy utilization efficiency of the fractionation tower, and reducing the process steam consumption. 25% or more.
附图说明Description of drawings
下面结合附图说明对本发明作进一步说明。The present invention will be further described below with reference to the accompanying drawings.
图1为本发明基于吸收式热泵的中间再沸器梯级加热系统示意图；1 is a schematic diagram of an intermediate reboiler cascade heating system based on an absorption heat pump of the present invention;
附图标记说明：1、分馏塔；2、塔顶冷凝器；3、回流罐；4、双效吸收式热泵；5、单效吸收式热泵；6、双级大温升热泵；7、一号中间再沸器；8、二号中间再沸器；9、三号中间再沸器；10、塔底重沸器；11、循环泵；P1、塔顶产品物料管道；P2、塔底产品物料管道；P3、蒸汽管道；P4、循环水管道；P5、一号中间物料管道；P6、二号中间物料管道；P7、三号中间物料管道。Description of reference numerals: 1. Fractionation tower; 2. Tower top condenser; 3. Reflux tank; 4. Double-effect absorption heat pump; 5. Single-effect absorption heat pump; 6. Double-stage large temperature rise heat pump; No. 8 intermediate reboiler; 8, No. 2 intermediate reboiler; 9, No. 3 intermediate reboiler; 10, column bottom reboiler; 11, circulating pump; P1, column top product material pipeline; P2, column bottom product Material pipeline; P3, steam pipeline; P4, circulating water pipeline; P5, No. 1 intermediate material pipeline; P6, No. 2 intermediate material pipeline; P7, No. 3 intermediate material pipeline.
具体实施方式Detailed ways
如图1所示，一种基于吸收式热泵的中间再沸器梯级加热系统，分馏塔1、塔顶冷凝器2、回流罐3、双效吸收式热泵4、单效吸收式热泵5、双级大温升热泵6、一号中间再沸器7、二号中间再沸器8、三号中间再沸器9和塔底重沸器10；As shown in Figure 1, an intermediate reboiler cascade heating system based on an absorption heat pump includes a fractionation tower 1, a tower top condenser 2, a reflux tank 3, a double-effect absorption heat pump 4, a single-effect absorption heat pump 5, a double-effect absorption heat pump 5, Stage large temperature rise heat pump 6, No. 1 intermediate reboiler 7, No. 2 intermediate reboiler 8, No. 3 intermediate reboiler 9 and column bottom reboiler 10;
所述分馏塔1的顶部连接有塔顶产品物料管道P1，塔顶产品物料管道P1经三通分为两输出管路，其中一个输出管路通过所述塔顶冷凝器2与所述回流罐3的入口相连；另一个输出管路与所述双级大温升热泵6的蒸发器入口相连，所述双级大温升热泵6的蒸发器出口通过塔顶产品物料管道P1与所述单效吸收式热泵5的蒸发器入口相连，所述单效吸收式热泵5的蒸发器出口通过塔顶产品物料管道P1与所述双效吸收式热泵4的蒸发器入口相连，所述双效吸收式热泵4的蒸发器出口通过塔顶产品物料管道P1与所述回流罐3的入口相连；所述回流罐3的出口通过塔顶产品物料管道P1分别与所述分馏塔1、塔顶产品区相连通；The top of the fractionation tower 1 is connected with a tower top product material pipeline P1, and the tower top product material pipeline P1 is divided into two output pipelines through a tee, and one of the output pipelines passes through the tower top condenser 2 and the reflux tank. The inlet of 3 is connected; another output pipeline is connected with the evaporator inlet of the two-stage high temperature rise heat pump 6, and the evaporator outlet of the two-stage high temperature rise heat pump 6 is connected with the single-stage product material pipeline P1 through the top of the tower. The evaporator inlet of the single-effect absorption heat pump 5 is connected to the evaporator inlet of the single-effect absorption heat pump 5, and the evaporator outlet of the single-effect absorption heat pump 5 is connected to the evaporator inlet of the double-effect absorption heat pump 4 through the top product material pipeline P1. The evaporator outlet of the type heat pump 4 is connected with the inlet of the described reflux tank 3 through the overhead product material pipeline P1; connected;
所述分馏塔1的底部通过塔底产品物料管道P2与所述塔底重沸器10的入口相连，所述塔底重沸器10的出口通过塔底产品物料管道P2与分馏塔1相连通，所述分馏塔1的底部通过塔底产品物料管道P2与塔底产品区相连通；The bottom of the fractionation tower 1 is connected to the inlet of the reboiler 10 at the bottom of the column through the product material pipeline P2 at the bottom of the column, and the outlet of the reboiler 10 is connected to the fractionation tower 1 through the product material pipeline P2 at the bottom of the column. , the bottom of the fractionation tower 1 is communicated with the product area at the bottom of the tower through the product material pipeline P2 at the bottom of the tower;
所述一号中间再沸器7的物料进出口通过一号中间物料管道P5与所述分馏塔1连通，所述二号中间再沸器8的物料进出口通二号中间物料管道P6与所述分馏塔1连通，所述三号中间再沸器9的物料进出口通过三号中间物料管道P7与所述分馏塔1连通；The material inlet and outlet of the No. 1 intermediate reboiler 7 is communicated with the fractionation tower 1 through the No. 1 intermediate material pipeline P5, and the material inlet and outlet of the No. 2 intermediate reboiler 8 is connected to the No. 2 intermediate material pipeline P6. Described fractionation tower 1 is communicated, and the material inlet and outlet of described No. 3 intermediate reboiler 9 is communicated with described fractionation tower 1 through No. 3 intermediate material pipeline P7;
所述双级大温升热泵6的吸收器与冷凝器出口通过循环水管道P4与所述三号中间再沸器9的循环水进口相连，所述三号中间再沸器9的循环水出口通过循环水管道P4与所述二号中间再沸器8的循环水进口相连，所述二号中间再沸器8的循环水出口通过循环水管道P4与所述一号中间再沸器7的循环水进口相连，所述一号中间再沸器7的循环水出口通过循环水管道P4与所述双效吸收式热泵4的吸收器及冷凝器入口相连，所述双效吸收式热泵4的吸收器及冷凝器出口通过循环水管道P4与所述单效吸收式热泵5的吸收器及冷凝器入口相连，所述单效吸收式热泵5的吸收器及冷凝器出口通过循环水管道P4与所述双级大温升热泵6的吸收器与冷凝器入口相连；The absorber and condenser outlet of the two-stage large temperature rise heat pump 6 are connected to the circulating water inlet of the No. 3 intermediate reboiler 9 through the circulating water pipeline P4, and the circulating water outlet of the No. 3 intermediate reboiler 9 is connected. The circulating water pipe P4 is connected to the circulating water inlet of the No. 2 intermediate reboiler 8, and the circulating water outlet of the No. 2 intermediate reboiler 8 is connected to the circulating water pipe P4 of the No. 1 intermediate reboiler 7. The circulating water inlet is connected, and the circulating water outlet of the No. 1 intermediate reboiler 7 is connected with the absorber and the condenser inlet of the double-effect absorption heat pump 4 through the circulating water pipeline P4. The outlet of the absorber and the condenser is connected to the inlet of the absorber and the condenser of the single-effect absorption heat pump 5 through the circulating water pipeline P4, and the outlet of the absorber and the condenser of the single-effect absorption heat pump 5 is connected to the outlet of the single-effect absorption heat pump 5 through the circulating water pipeline P4. The absorber of the two-stage large temperature rise heat pump 6 is connected with the condenser inlet;
蒸汽通过蒸汽管道P3分别与所述塔底重沸器10的蒸汽入口、所述双效吸收式热泵4的发生器入口、所述单效吸收式热泵5的发生器入口、双级大温升热泵6的发生器入口相连通。The steam passes through the steam pipeline P3 and is respectively connected with the steam inlet of the bottom reboiler 10, the generator inlet of the double-effect absorption heat pump 4, the generator inlet of the single-effect absorption heat pump 5, and the double-stage large temperature rise. The generator inlets of the heat pump 6 are communicated.
具体来说，循环水管道P4上设置有循环泵11，循环泵的设置可以有效的保证水循环的动力。Specifically, the circulating water pipeline P4 is provided with a circulating pump 11, and the setting of the circulating pump can effectively ensure the power of the water circulation.
所述双效吸收式热泵4发生器、单效吸收式热泵5发生器、双级大温升热泵6发生器均设置有凝水管道，用于收集工艺蒸汽凝水。The generator of the double-effect absorption heat pump 4, the generator of the single-effect absorption heat pump 5, and the generator of the double-stage large temperature rise heat pump 6 are all provided with condensate pipes for collecting process steam condensate.
所述双效吸收式热泵4、单效吸收式热泵5、双级大温升热泵6均采用蒸汽型溴化锂吸收式热泵。The double-effect absorption heat pump 4, the single-effect absorption heat pump 5, and the two-stage large temperature rise heat pump 6 all adopt the steam-type lithium bromide absorption heat pump.
所述一号中间再沸器7、二号中间再沸器8和三号中间再沸器9从上向下顺次排布，所述双效吸收式热泵4、单效吸收式热泵5和双级大温升热泵6从上向下顺次排布，且所述一号中间再沸器7、二号中间再沸器8和三号中间再沸器9分别与所述双效吸收式热泵4、单效吸收式热泵5和双级大温升热泵6一一对应。The No. 1 intermediate reboiler 7, the No. 2 intermediate reboiler 8 and the No. 3 intermediate reboiler 9 are sequentially arranged from top to bottom, the double-effect absorption heat pump 4, the single-effect absorption heat pump 5 and The two-stage large temperature rise heat pumps 6 are arranged in sequence from top to bottom, and the No. 1 intermediate reboiler 7, No. 2 intermediate reboiler 8 and No. 3 intermediate reboiler 9 are respectively connected to the double-effect absorption type The heat pump 4, the single-effect absorption heat pump 5 and the two-stage large temperature rise heat pump 6 correspond one by one.
本发明的工作过程如下：The working process of the present invention is as follows:
分馏塔顶部的物料流通过程：所述分馏塔1的塔顶产品物料通过塔顶产品物料管道P1经三通分为两输出管路输出，其中一部分塔顶物料经过塔顶冷凝器2进入到回流罐3内；另一部分塔顶物料依次进入双级大温升热泵6的蒸发器、单效吸收式热泵5的蒸发器、双效吸收式热泵4的蒸发器梯级降温，再回流到回流罐3内，回流罐3内的塔顶物料通过塔顶产品物料管道P1分别输送至分馏塔1、塔顶产品区。The material circulation process at the top of the fractionation tower: the top product material of the fractionation tower 1 is divided into two output pipelines through the top product material pipeline P1 through the tee, and a part of the top material enters the reflux through the top condenser 2. In the tank 3; another part of the tower top material enters the evaporator of the double-stage large temperature rise heat pump 6, the evaporator of the single-effect absorption heat pump 5, and the evaporator of the double-effect absorption heat pump 4 in order to cool down, and then return to the reflux tank 3 Inside, the top material in the reflux tank 3 is respectively transported to the fractionation tower 1 and the top product area through the top product material pipeline P1.
分馏塔底部的物料流通过程：分馏塔1的塔底产品物料通过塔底产品物料管道P2经三通分流为两路，其中一部分塔底物料经塔底产品物料管道P2进入塔底产品区，另一部分进入塔底重沸器10加热，升温后的物料再通过塔底产品物料管道P2返回至分馏塔1进行分馏处理，工艺蒸汽通过蒸汽管道P3进入塔底重沸器10为其提供加热热源。The material circulation process at the bottom of the fractionation tower: the bottom product material of the fractionation tower 1 is divided into two paths through the bottom product material pipeline P2 through the three-way, and a part of the column bottom material enters the tower bottom product area through the column bottom product material pipeline P2, and the other A part enters the bottom reboiler 10 for heating, and the heated material is returned to the fractionation tower 1 through the bottom product material pipeline P2 for fractionation treatment, and the process steam enters the bottom reboiler 10 through the steam pipeline P3 to provide a heating source for it.
中间再沸器工作流程：循环水经过循环水管道P4依次通过双效吸收式热泵4吸收器及冷凝器、单效吸收式热泵5吸收器及冷凝器、双级大温升热泵6吸收器及冷凝器梯级升温，再依次通过三号中间再沸器9、二号中间再沸器8、一号中间再沸器7加热中间物料并梯级降温，降温后的循环水通过循环泵11返回至双级大温升热泵6吸收器及冷凝器，实现循环水闭式循环；三号中间物料经过三号中间物料管道P7进入三号中间再沸器9加热，升温后的物料再返回至分馏塔，二号中间物料经过二号中间物料管道P6进入二号中间再沸器8加热，升温后的物料再返回至分馏塔，一号中间物料经过一号中间物料管道P7进入一号中间再沸器7加热，升温后的物料再返回至分馏塔，工艺蒸汽通过蒸汽管道P3分别进入双级大温升热泵6发生器、单效吸收式热泵5发生器、双效吸收式热泵4发生器，为热泵循环提供驱动热源。The working process of the intermediate reboiler: the circulating water passes through the circulating water pipeline P4 through the double-effect absorption heat pump 4 absorber and condenser, the single-effect absorption heat pump 5 absorber and condenser, the double-stage large temperature rise heat pump 6 absorber and the condenser. The condenser heats up in steps, and then passes through the No. 3 intermediate reboiler 9, the No. 2 intermediate reboiler 8, and the No. 1 intermediate reboiler 7 to heat the intermediate material and step down the temperature. The high temperature rise heat pump 6 absorber and condenser realize the closed circulation of circulating water; the No. 3 intermediate material enters the No. 3 intermediate reboiler 9 through the No. 3 intermediate material pipeline P7 for heating, and the heated material is returned to the fractionation tower, The No. 2 intermediate material enters the No. 2 intermediate reboiler 8 through the No. 2 intermediate material pipeline P6 for heating, the heated material is returned to the fractionation tower, and the No. 1 intermediate material enters the No. 1 intermediate reboiler 7 through the No. 1 intermediate material pipeline P7 After heating, the heated material is returned to the fractionation tower, and the process steam enters the two-stage large temperature rise heat pump 6 generator, the single-effect absorption heat pump 5 generator, and the double-effect absorption heat pump 4 generator respectively through the steam pipeline P3, which are heat pumps. The cycle provides the driving heat source.
双效吸收式热泵适宜制热温度为40～60℃，单效吸收式热泵适宜制热温度为55～75℃，双级大温升热泵适宜制热温度为75～95℃，选择适宜的热泵设备对中间物料进行三级加热。The suitable heating temperature of the double-effect absorption heat pump is 40-60℃, the suitable heating temperature of the single-effect absorption heat pump is 55-75℃, and the suitable heating temperature of the double-stage large temperature rise heat pump is 75-95℃. The equipment conducts three-stage heating for the intermediate material.
由此可见，本发明利用工艺蒸汽驱动三级热泵循环回收塔顶物料余热，制备热量梯级加热中间物料，使得分馏塔能源利用效率提高25％。It can be seen that the present invention utilizes the process steam to drive the three-stage heat pump to circulate and recover the waste heat of the tower top material to prepare the heat cascade heating intermediate material, so that the energy utilization efficiency of the fractionation tower is increased by 25%.
以上所述的实施例仅是对本发明的优选方式进行描述，并非对本发明的范围进行限定，在不脱离本发明设计精神的前提下，本领域普通技术人员对本发明的技术方案做出的各种变形和改进，均应落入本发明权利要求书确定的保护范围内。The above-mentioned embodiments are only to describe the preferred modes of the present invention, but not to limit the scope of the present invention. Without departing from the design spirit of the present invention, those of ordinary skill in the art can make various modifications to the technical solutions of the present invention. Variations and improvements should fall within the protection scope determined by the claims of the present invention.
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