CN212431495U - Device for energy utilization in a demethanizer with a plurality of flow plate-fin reboilers - Google Patents

Device for energy utilization in a demethanizer with a plurality of flow plate-fin reboilers Download PDF

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Publication number
CN212431495U
CN212431495U CN202021322954.1U CN202021322954U CN212431495U CN 212431495 U CN212431495 U CN 212431495U CN 202021322954 U CN202021322954 U CN 202021322954U CN 212431495 U CN212431495 U CN 212431495U
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China
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demethanizer
fin
reboiler
pipeline
plate
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CN202021322954.1U
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Inventor
刘子兵
常志波
粱璇玑
邱鹏
范君来
张璞
薛政
张磊
韦玮
李京子
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China National Petroleum Corp
Xian Changqing Technology Engineering Co Ltd
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China National Petroleum Corp
Xian Changqing Technology Engineering Co Ltd
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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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/76—Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
    • 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
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Abstract

The utility model provides an equipment that can utilize in demethanizer with many streams of plate-fin reboilers, this equipment include raw materials natural gas, the poor natural gas of backward flow, the mixed cryogen of high-pressure normal atmospheric temperature, main cold box, low temperature separator, coaxial pressure boost expander, demethanizer and many streams of plate-fin reboilers at least, the utility model discloses a many streams of plate-fin reboilers are as demethanizer tower bottom reboiler to avoided conventional tubulation heat exchanger to set up in large quantity, area big and the inconvenient shortcoming of built on stilts installation, and reduced plate-fin heat exchanger's the biggest heat transfer difference in temperature through the measure of replenishing other commodity circulation, thereby overcome the little shortcoming of plate-fin heat exchanger heat transfer difference in temperature.

Description

Device for energy utilization in a demethanizer with a plurality of flow plate-fin reboilers
Technical Field
The utility model belongs to natural gas processing field, concretely relates to can utilize's equipment in demethanizer with multiple stream plate-fin reboiler.
Background
Ethane is a high-quality raw material of ethylene, the production cost of ethylene prepared by cracking ethane is two thirds of the molecular weight of naphtha, and the ethylene raw material C is internationally2-C4The proportion is about 48 percent, and China is restricted by raw materials, and naphtha is mainly used. The ethane product is recovered from the natural gas and is used as the raw material for preparing the ethylene by the steam thermal cracking, so that the method has positive significance for improving the yield of the ethylene product, reducing the energy consumption of an ethylene device, improving the quality and increasing the efficiency.
The natural gas produced by the Changqing oil field in the ancient world has large total gas amount, contains large-scale ethane and heavy hydrocarbon components, and the recovered ethane can be used for constructing a large-scale ethylene plant, thereby having important significance for reformation and innovation of the ethylene industry in China.
The demethanizer is one of key equipment in natural gas ethane recovery engineering, and its main function is to complete the separation of methane and ethane and above light hydrocarbon components, and the equipment is low in operation temperature, large in the number of inlet and outlet materials, large in the temperature change between tower top and tower bottom, and maximum in the number of tower trays, and the demethanizer determines the quality of key indexes of the whole natural gas ethane recovery engineering, such as ethane recovery rate, ethane product index, energy consumption index and engineering investment.
The methane and ethane and above light hydrocarbon components are separated by the demethanizer by adopting the principle of rectification separation, a reboiler is arranged at the bottom of the demethanizer, condensation reflux is arranged at the top of the demethanizer, the reboiler at the bottom of the demethanizer in the similar project at present completely adopts a tubular kettle reboiler, and the single set of device for the project has very large treatment scale (1500 multiplied by 10)4m3And d), the world ranks the first three, Asia is the largest, if a conventional tubular kettle type reboiler is adopted, 2-3 reboilers are arranged in parallel, the process is complex, the investment is high, the occupied area is large, the installation and maintenance are inconvenient, the phenomenon of uneven flow and heat distribution is easily caused, the stable operation of the device is influenced, and the quality index of the product is further influenced.
SUMMERY OF THE UTILITY MODEL
To the above-mentioned defect that prior art exists, the utility model provides an equipment that can utilize in the demethanizer tower of stranded stream plate-fin reboiler has carries out light hydrocarbons recovery technology's such as ethane supporting auxiliary system as ancient natural gas in the oil field of Changqing.
The utility model discloses the technical scheme who adopts as follows:
the device comprises at least raw natural gas, reflux lean natural gas, high-pressure normal-temperature mixed refrigerant, a main cooling box, a low-temperature separator, a coaxial booster expander, a demethanizer and a multi-stream plate-fin reboiler; the main cooling box and the multi-strand flow plate-fin reboiler are respectively provided with a plurality of feed inlets and discharge outlets, the demethanizer is provided with a plurality of material flow inlets, the last tray at the lower part of the demethanizer is provided with a reboiled condensate outlet and a reboiled condensate return outlet, and the bottom of the demethanizer is provided with C2 +The mixed hydrocarbon is discharged from the outlet of the mixing tank,
the raw material natural gas is connected with a fourth feed inlet of the main cooling box through a pipeline, a fourth discharge outlet of the main cooling box is connected with a feed inlet of a low-temperature separator through a pipeline, the low-temperature separator is provided with a first gas phase discharge outlet, a second gas phase discharge outlet and a liquid phase discharge outlet, and the first gas phase discharge outlet of the low-temperature separator is sequentially connected with a coaxial booster expander and a third material flow inlet of the demethanizer through pipelines; the second gas phase discharge hole of the low-temperature separator is connected with the fifth feed inlet of the main cooling box through a pipeline, and the fifth discharge hole of the main cooling box is connected with the second material flow inlet of the demethanizer through a pipeline; the liquid phase discharge port of the low-temperature separator is connected with the fourth material flow inlet of the demethanizer through a pipeline;
the high-pressure normal-temperature mixed refrigerant is connected with a first feed inlet of the multi-stream plate-fin reboiler through a pipeline, a first discharge outlet of the multi-stream plate-fin reboiler is connected with a third feed inlet of the main cooling box through a pipeline, and a third discharge outlet of the main cooling box externally conveys the low-pressure normal-temperature mixed refrigerant through a pipeline;
the returned lean natural gas is connected with a second feed inlet of the multi-stream plate-fin reboiler through a pipeline, a second discharge outlet of the multi-stream plate-fin reboiler is connected with a first feed inlet of the main cooling box through a pipeline, and a first discharge outlet of the main cooling box is connected with a first stream inlet of the demethanizer through a pipeline;
the outlet of the reboiled condensate is connected with a third feed inlet of the multi-stream plate-fin reboiler through a pipeline, and a third discharge outlet of the multi-stream plate-fin reboiler is connected with the outlet of the reboiled condensate return tower through a pipeline;
c at the bottom of the demethanizer2 +The mixed hydrocarbon outlet is connected with a fourth feed inlet of the multi-flow plate-fin reboiler through a pipeline, and a third discharge outlet of the multi-flow plate-fin reboiler is used for outputting C through the pipeline2 +And (3) mixing hydrocarbons.
The top of the demethanizer is provided with a low-temperature lean natural gas outlet, the low-temperature lean natural gas outlet is connected with a second feed inlet of the main cooling box through a pipeline, a second discharge outlet of the main cooling box is connected with an inlet of the coaxial booster expander through a pipeline, and an outlet of the coaxial booster expander is connected with the inlet of the coaxial booster expander through a pipeline2 +And a mixed hydrocarbon lean natural gas recovery tank.
And a tower outlet side boiling condensate outlet and a tower return side boiling condensate inlet are formed in the side wall of the middle upper part of the demethanizing tower, and the tower outlet side boiling condensate outlet and the tower return side boiling condensate inlet form a circulating loop with a sixth feeding hole and a sixth discharging hole of the main cooling box.
And a bypass flow regulating valve is connected in parallel between the first feeding hole and the first discharging hole of the multi-stream plate-fin reboiler.
And a mixed refrigerant J-T valve is arranged between the third feeding port and the third discharging port of the main cooling box.
C at the bottom of the demethanizer2 +Mixed hydrocarbon is led out through C2 +The hydrocarbon-mixed booster pump is connected with a fourth feed inlet of the multi-stream plate-fin reboiler, and the pipeline C2 +A C is arranged on a connecting pipeline between the hydrocarbon mixture booster pump and the fourth feed inlet of the multi-stream plate-fin reboiler2 +Mixed hydrocarbon liquid level detector and C2 +A hydrocarbon mixing liquid level regulating valve.
A first flow regulating valve is connected on a connecting pipeline between a first discharge hole of the main cooling box and a first stock flow inlet of the demethanizer;
a second flow regulating valve is arranged on a connecting pipeline between a second gas phase discharge hole of the low-temperature separator and a second stream inlet connected with the demethanizer; and a liquid level detector and a liquid level regulating valve are arranged on a connecting pipeline between a liquid phase discharge port of the low-temperature separator and a fourth material flow inlet connected with the demethanizer.
The utility model has the advantages as follows:
(1) the utility model discloses utilize the characteristics that plate-fin heat exchanger heat exchange efficiency is high, small and the commodity circulation number is many, adopted plate-fin heat exchanger (the multiple stream plate-fin reboiler promptly) as demethanization tower bottom of the tower reboiler to avoided conventional tubulation heat exchanger to set up in large quantity, area is big and built on stilts inconvenient shortcoming of installation, and reduced plate-fin heat exchanger's the biggest heat transfer difference in temperature through the measure of replenishing other commodity circulation, thereby overcome the shortcoming that plate-fin heat exchanger heat transfer difference in temperature is little.
(2) Equipment and method can realize going out demethanizer tower bottom reboiler from original 2 ~ 3 parallelly connected large-scale tubulation reboiler that set up for 1 the very little multiple stream plate-fin reboiler of specification, cold volume integration utilizes the optimization, reduces the loss that utilizes the process cold volume, very big simplification the flow, the investment is synthesized, improve the stability of device operation and the quality of product simultaneously, recovery system cold volume that can be more and reduce the energy consumption, improve natural gas ethane recovery engineering economic benefits.
The above description is only an overview of the technical solution of the present invention, and in order to clearly understand the technical means of the present invention and to implement the technical solution according to the content of the description, the following detailed description is made with reference to the preferred embodiments of the present invention and accompanying drawings.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic view of the process of the present invention.
Description of reference numerals:
1、C2 +a mixed hydrocarbon lean natural gas recovery tank; 2. mixing refrigerant at low pressure and normal temperature; 3. raw material natural gas; 4. c2 +Mixing hydrocarbons; 5. refluxing the lean natural gas; 6. cold mixing agent under high pressure and normal temperature; 7. a raw natural gas battery limit valve; 8. a main cooling box; 9. a cryogenic separator; 10. a liquid level regulating valve; 11. a liquid level detector; 12. a coaxial booster expander; 13. a second flow regulating valve; 14. a first flow regulating valve; 15. a demethanizer; 16. the reboiled condensate is discharged from the tower outlet; 17. returning the reboiled condensate to the tower mouth; 18. a temperature detector; 19. c2 +A mixed hydrocarbon liquid level detector; 20. c2 +A hydrocarbon mixture booster pump; 21. c2 +A hydrocarbon mixture level regulating valve; 22. multi-flow plate-fin typeA reboiler; 23. a bypass flow regulating valve; 24. a mixed refrigerant J-T valve; 25. a check valve; 26. a lean natural gas boundary region valve; 27. c2 +A hydrocarbon mixture outlet; 28. a side boiling condensate outlet; 29. a side boiling condensate inlet returning to the tower; 30. and (5) a low-temperature lean natural gas outlet.
Detailed Description
The following description is provided for illustrative embodiments of the present invention, and other advantages and effects of the present invention will be readily apparent to those skilled in the art from the disclosure herein.
The exemplary embodiments of the present invention will now be described with reference to the accompanying drawings, which, however, may be embodied in many different forms and are not limited to the embodiments described herein, which are provided for complete and complete disclosure of the present invention and to fully convey the scope of the invention to those skilled in the art. The terminology used in the exemplary embodiments presented in the accompanying drawings is not intended to be limiting of the invention. In the drawings, the same units/elements are denoted by the same reference numerals.
Unless otherwise defined, terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. Further, it will be understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense.
The first embodiment:
the present embodiment relates to an apparatus capable of being utilized in a demethanizer having a plurality of flow plate-fin reboilers, as shown in fig. 1, the apparatus at least includes a raw natural gas 3, a reflux lean natural gas 5, a high-pressure normal-temperature mixed refrigerant 6, a main cooling box 8, a low-temperature separator 9, a coaxial booster expander 12, a demethanizer 15, and a plurality of flow plate-fin reboilers 22; the main cooling box 8 and the multi-stream plate-fin reboiler 22 are respectively provided with a plurality of feed inlets and discharge outlets, the demethanizer 15 is provided with a plurality of stream inlets, and the last layer of tray at the lower part of the demethanizer 15 is provided with a reboiled condensate outlet 16 and a reboiled condensate outletThe liquid returns to the tower opening 17, and the tower bottom of the demethanizer 15 is provided with C2 +The outlet 27 for the mixed hydrocarbon is provided,
the raw material natural gas 3 is connected with a fourth feed inlet of the main cooling box 8 through a pipeline, a fourth discharge outlet of the main cooling box 8 is connected with a feed inlet of the low-temperature separator 9 through a pipeline, the low-temperature separator 9 is provided with a first gas phase discharge outlet, a second gas phase discharge outlet and a liquid phase discharge outlet, and the first gas phase discharge outlet of the low-temperature separator 9 is sequentially connected with the coaxial booster expander 12 and a third stream inlet of the demethanizer 15 through pipelines; a second gas phase discharge hole of the low-temperature separator 9 is connected with a fifth feed hole of the main cooling box 8 through a pipeline, and a fifth discharge hole of the main cooling box 8 is connected with a second stream inlet of the demethanizer 15 through a pipeline; the liquid phase discharge port of the low temperature separator 9 is connected with the fourth material flow inlet of the demethanizer 15 through a pipeline;
the high-pressure normal-temperature mixed refrigerant 6 is connected with a first feeding hole of the multi-flow plate-fin reboiler 22 through a pipeline, a first discharging hole of the multi-flow plate-fin reboiler 22 is connected with a third feeding hole of the main cooling box 8 through a pipeline, and a third discharging hole of the main cooling box 8 conveys the low-pressure normal-temperature mixed refrigerant 2 outside through a pipeline;
the returned lean natural gas 5 is connected with a second feed inlet of the multi-stream plate-fin reboiler 22 through a pipeline, a second discharge outlet of the multi-stream plate-fin reboiler 22 is connected with a first feed inlet of the main cooling box 8 through a pipeline, and a first discharge outlet of the main cooling box 8 is connected with a first stream inlet of the demethanizer 15 through a pipeline;
the outlet 16 of the reboiled condensate is connected with a third inlet of the multi-stream plate-fin reboiler 22 through a pipeline, and a third outlet of the multi-stream plate-fin reboiler 22 is connected with the reboiled condensate return tower outlet 17 through a pipeline;
c at the bottom of the demethanizer 152 +The mixed hydrocarbon outlet 27 is connected with the fourth feed inlet of the multi-flow plate-fin reboiler 22 through a pipeline, and the third discharge outlet of the multi-flow plate-fin reboiler 22 outputs C through a pipeline2 +And (4) mixed hydrocarbon.
The utility model discloses a plate fin heat exchanger utilizes the characteristics that plate fin heat exchanger heat exchange efficiency is high, small and the commodity circulation number is many as demethanization tower bottom reboiler, has adopted the plate fin heat exchanger of 4 strands of commodity circulation as demethanization tower bottom reboiler to avoided conventional tubulation heat exchanger to set up in large quantity, area is big and built on stilts inconvenient shortcoming of installation.
Second embodiment:
a first embodiment of the present invention relates to a method for a device for energy utilization in a demethanizer having a plurality of flow plate-fin reboilers, comprising the following steps, with reference to fig. 1:
s1, taking the high-pressure normal-temperature mixed refrigerant 6 from the outside as a main heat source at the bottom of the demethanizer 15, and entering the multi-stream plate-fin reboiler 22 for precooling;
s2, the backflow lean natural gas 5 is used as a secondary heat source at the bottom of the demethanizer 15 and enters the multi-stream plate-fin reboiler 22 for precooling;
s3, introducing the mixed refrigerant precooled in the step S1 into the main cooling box 8 for cooling and supercooling; then the mixed refrigerant is throttled, depressurized and cooled by a mixed refrigerant J-T valve 24 and returns to the main cold box 8 to give cold energy, and the mixed refrigerant flows out of the main cold box 8 after being reheated to become a low-pressure normal-temperature mixed refrigerant 2;
s4, introducing the backflow lean natural gas 5 precooled in the step S2 into a main cold box 8 for cooling and supercooling; then sending the first stream to the upper half part of the demethanizer 15 as a first stream;
s5, introducing the raw material natural gas 3 into a main cooling box 8 for precooling;
s6, sending the raw material natural gas 3 precooled in the step S1 to a low-temperature separator 9 for gas-liquid separation, wherein the gas phase is divided into two streams, and one stream enters a coaxial booster expander 12 for expansion and enters the upper half part of a demethanizer 15 as a third stream; the other gas phase enters the main cooling box 8 for cooling and then enters the upper half part of the demethanizer 15 through the control of the regulating valve to be used as a second stream; the liquid phase enters the middle part of the demethanizer 15 through liquid level control to be used as a fourth material flow;
s7, after cold energy recovery is carried out on the low-temperature lean natural gas from the top of the demethanizer 15 in the main cold box 8, the low-temperature lean natural gas is introduced into the coaxial booster expander 12 for boosting and then is conveyed to the outside;
s8, mixingBottom C of demethanizer 152 +Pressurizing the mixed hydrocarbon by using a booster pump;
s9, C after pressurization in the step S82 +The mixed hydrocarbon 27 is reheated and sent to the multi-stream plate-fin reboiler 22 to control the minimum pinch point temperature difference and the maximum section temperature difference of the multi-stream plate-fin reboiler 22;
s10, leading out the low-temperature condensate of the last tray at the lower part of the demethanizer 15 into the multi-stream plate-fin reboiler 22 for heat exchange, forming a thermosiphon circulation and returning to the gas phase space of the last tray at the lower part of the demethanizer 15 again to distill out the dissolved light hydrocarbon component so as to discharge C from the bottom of the demethanizer2 +The methane content index in the mixed hydrocarbon 27 is qualified.
Equipment and method can realize going out demethanizer tower bottom reboiler from original 2 ~ 3 parallelly connected large-scale tubulation reboiler that set up for 1 the very little multiple stream plate-fin reboiler of specification, cold volume integration utilizes the optimization, reduces the loss that utilizes the process cold volume, very big simplification the flow, the investment is synthesized, improve the stability of device operation and the quality of product simultaneously, recovery system cold volume that can be more and reduce the energy consumption, improve natural gas ethane recovery engineering economic benefits.
The third embodiment:
on the basis of the first embodiment, further, a low-temperature lean natural gas outlet 30 is arranged at the top of the demethanizer 15, the low-temperature lean natural gas outlet 30 is connected with the second feed inlet of the main cooling box 8 through a pipeline, the second discharge outlet of the main cooling box 8 is connected with the inlet of the coaxial booster expander 12 through a pipeline, and the outlet of the coaxial booster expander 12 is connected with the inlet of the coaxial booster expander 12 through a pipeline C2 +A mixed hydrocarbon lean natural gas recovery tank 1.
Furthermore, a tower outlet side boiling condensate outlet 28 and a tower return side boiling condensate inlet 29 are arranged on the side wall of the middle upper part of the demethanizer 15, and the tower outlet side boiling condensate outlet 28 and the tower return side boiling condensate inlet 29, and a sixth feeding hole and a sixth discharging hole of the main cooling box 8 form a circulation loop.
Further, a raw material natural gas boundary area valve 7 is arranged on a connecting pipeline between the raw material natural gas 3 and a fourth feed inlet of the main cooling box 8; specifically, the raw natural gas 3, the raw natural gas battery limit valve, the main cooling box 8, the cryogenic separator 9, the coaxial booster expander 12 and the demethanizer 15 are connected end to end through pipelines.
Further, a coaxial booster expander 12 and C2 +A check valve and a lean natural gas boundary valve 26 are arranged on a connecting pipeline between the mixed hydrocarbon lean natural gas recovery tanks.
Further, C of the bottom of the demethanizer 152 +Mixed hydrocarbon outlet 27 through C2 +The hydrocarbon mixture booster pump 20 is connected with the fourth feed inlet of the multi-flow plate-fin reboiler 22, and the pipeline C2 +A C is arranged on a connecting pipeline between the hydrocarbon mixture booster pump 20 and the fourth feed inlet of the multi-stream plate-fin reboiler 222 +Mixed hydrocarbon liquid level detector 19 and C2 +A hydrocarbon mixture level adjusting valve 21.
Further, a first flow regulating valve 14 is connected on a connecting pipeline between a first discharge hole of the main cooling box 8 and a first stream inlet of the demethanizer 15;
further, a second flow regulating valve 13 is arranged on a connecting pipeline between a second gas phase discharge hole of the low-temperature separator 9 and a second stream inlet connected with the demethanizer 15; a liquid level detector 11 and a liquid level regulating valve 10 are arranged on a connecting pipeline between a liquid phase discharge port of the low-temperature separator 9 and a fourth material flow inlet connected with the demethanizer 15.
Further, a bypass flow regulating valve 23 is connected in parallel between the first feed inlet and the first discharge outlet of the multi-stream plate-fin reboiler 22, and the bypass flow regulating valve 23 is used for controlling the precooling flow of the normal-temperature mixed refrigerant, so that the heat source load is controlled; and the bypass flow regulating valve 23 and the methane tower bottom temperature detector 18 form a temperature regulating loop so as to control the temperature of the bottom of the demethanizer. Further, a mixed refrigerant J-T valve 24 is arranged between the third feed port and the third discharge port of the main cooling box 8.
The utility model discloses borrow for reference LNG refrigeration process's multiple stream heat transfer theory, adopted plate fin heat exchanger as removing the methane tower bottom reboiler, utilize plate fin heat exchanger heat exchange efficiency high, small and the many characteristics of commodity circulation number, adopted plate fin heat exchanger as removing the methane tower bottom reboiler, thereby avoided conventional tubulation heat exchanger to set up in large quantity, area is big and built on stilts inconvenient shortcoming of installation, and reduce plate fin heat exchanger's the biggest heat transfer difference in temperature through the measure of supplementing other commodity circulation, thereby overcome the little shortcoming of plate fin heat exchanger heat transfer difference in temperature.
Fourth embodiment:
the embodiment relates to a method for utilizing energy in a demethanizer with a plurality of flow plate-fin reboilers, which comprises the following steps:
s1, taking a high-pressure normal-temperature mixed refrigerant 6 from the outside as a main heat source at the bottom of the demethanizer 15, and entering a multi-stream plate-fin reboiler 22 for precooling, wherein the temperature is precooled from 40 ℃ to-1.5 ℃;
s2, enabling the backflow lean natural gas 5 to serve as a secondary heat source at the bottom of the demethanizer 15, entering a multi-stream plate-fin reboiler 22 for precooling, and precooling the temperature from 40 ℃ to-1.5 ℃;
s3, introducing the mixed refrigerant precooled in the step S1 into a main cooling box 8 for cooling and supercooling, and cooling the mixed refrigerant from-1.5 ℃ to-93 ℃; then the mixed refrigerant is throttled, depressurized and cooled by a mixed refrigerant J-T valve 24 and returns to the main cold box 8 to give cold energy, and the mixed refrigerant flows out of the main cold box 8 after being reheated to become a low-pressure normal-temperature mixed refrigerant 2;
s4, introducing the backflow lean natural gas 5 precooled in the step S2 into a main cooling box 8 for cooling and supercooling, and cooling the backflow lean natural gas from-1.5 ℃ to-93 ℃; then sending the first stream to the upper half part of the demethanizer 15 as a first stream;
s5, introducing the raw material natural gas 3 into a main cooling box 8 for precooling, wherein the temperature is precooled from 28 ℃ to-70 ℃;
s6, sending the raw material natural gas 3 precooled in the step S1 to a low-temperature separator 9 for gas-liquid separation, wherein the gas phase is divided into two streams, one stream enters a coaxial booster expander 12 for expansion and enters the upper half part of a demethanizer 15 to be used as a third stream, the pressure of the third stream is expanded from 3.8MPa to 2.65MPa, and the temperature is reduced from-70 ℃ to-83 ℃; the other gas phase enters a main cooling box 8 for cooling, the temperature is pre-cooled to-93 ℃ from-70 ℃, and the gas phase is controlled by a regulating valve to enter the upper half part of a demethanizer 15 to be used as a second stream; the liquid phase enters the middle part of the demethanizer 15 through liquid level control to be used as a fourth material flow;
s7, after cold energy recovery is carried out on the low-temperature lean natural gas from the top of the demethanizer 15 in the main cooling box 8, the temperature is precooled from-98 ℃ to 25 ℃; introducing a coaxial booster expansion machine 12 for boosting, and conveying the pressure to the outside after boosting from 2.6MPa to 2.8 MPa;
s8, C of the bottom of the demethanizer 152 +The pressure of the mixed hydrocarbon is increased from 2.65MPa to 3.05MPa by using a booster pump;
s9, C after pressurization in the step S82 +The mixed hydrocarbon 27 is reheated and sent to the multi-stream plate-fin reboiler 22, and the temperature is reheated from 3 ℃ to 26 ℃ so as to control the minimum pinch point temperature difference and the maximum section temperature difference of the multi-stream plate-fin reboiler 22.
S10, leading out the low-temperature condensate of the last tray at the lower part of the demethanizer 15, entering the multi-stream plate-fin reboiler 22 for heat exchange, raising the temperature of the low-temperature condensate from-7 ℃ to 3 ℃, ensuring that the gasification rate reaches 58%, forming thermosiphon circulation, and returning the thermosiphon circulation to the gas phase space of the last tray at the lower part of the demethanizer 15 again to distill out the dissolved light hydrocarbon component so as to ensure that C discharged from the bottom of the demethanizer2 +The methane content index in the mixed hydrocarbon 27 is qualified.
The mixed refrigerant consists of methane, ethylene, propane and isobutane, the pressure is 3.2MPa, and the flow rate is 233 x 104m3/d。
The main component of the returned lean natural gas is methane, the volume content of the methane reaches 98.57 percent, the pressure is 4.4MPa, and the flow rate is 188 multiplied by 104m3/d。
C2 +The mixed hydrocarbon is formed from methane, ethane, propane and C4 +And CO2The pressure is 2.65MPa, and the liquid flow is 34.4m3/h。
To sum up, the utility model provides a device that can utilize in this kind of demethanizer with strand flow plate-fin reboiler can regard as demethanizer auxiliary device of ancient natural gas ethane recovery technique on the oil field of Changqing, provides high-quality raw materials for national ethane schizolysis system ethylene, is favorable to improving the present comparatively laggard naphtha schizolysis system ethylene technique of china.
The utility model discloses a multiple stream plate-fin is as removing methane tower reboiler in the natural gas ethane recovery technique, can realize removing methane tower bottom reboiler from the less plate-fin reboiler of 1 platform specification of the optimization of the parallelly connected large-scale shell and tube reboiler of original 2 ~ 3 platforms, very big simplification the flow, only equipment investment has saved 1 hundred million yuan for this project, save the combined investment and can reach more than 3 hundred million yuan, the steady operation to this project device simultaneously, product quality index has brought very big benefit, also the possibility of bringing to the maximization of similar project rectification equipment.
It will be understood by those skilled in the art that the foregoing embodiments are specific examples of the invention, and that various changes in form and details may be made therein without departing from the spirit and scope of the invention in its practical application.

Claims (10)

1. Apparatus for energy utilization in a demethanizer having a plurality of flow plate fin reboilers, characterized by: the equipment at least comprises raw material natural gas (3), reflux lean natural gas (5), high-pressure normal-temperature mixed refrigerant (6), a main cooling box (8), a low-temperature separator (9), a coaxial booster expander (12), a demethanizer (15) and a multi-stream plate-fin reboiler (22); the main cooling box (8) and the multi-strand flow plate-fin reboiler (22) are respectively provided with a plurality of feed inlets and discharge outlets, the demethanizer (15) is provided with a plurality of material flow inlets, the last layer tray at the lower part of the demethanizer (15) is provided with a reboiled condensate outlet (16) and a reboiled condensate return (17), and the bottom of the demethanizer (15) is provided with C2 +A hydrocarbon mixture outlet (27),
the raw material natural gas (3) is connected with a fourth feeding hole of the main cooling box (8) through a pipeline, a fourth discharging hole of the main cooling box (8) is connected with a feeding hole of the low-temperature separator (9) through a pipeline, the low-temperature separator (9) is provided with a first gas phase discharging hole, a second gas phase discharging hole and a liquid phase discharging hole, and the first gas phase discharging hole of the low-temperature separator (9) is sequentially connected with the coaxial booster expander (12) and a third material flow inlet of the demethanizer (15) through pipelines; a second gas phase discharge hole of the low-temperature separator (9) is connected with a fifth feed hole of the main cooling box (8) through a pipeline, and a fifth discharge hole of the main cooling box (8) is connected with a second stream inlet of the demethanizer (15) through a pipeline; the liquid phase discharge port of the low-temperature separator (9) is connected with the fourth stream inlet of the demethanizer (15) through a pipeline;
the high-pressure normal-temperature mixed refrigerant (6) is connected with a first feeding hole of the multi-flow plate-fin reboiler (22) through a pipeline, a first discharging hole of the multi-flow plate-fin reboiler (22) is connected with a third feeding hole of the main cooling box (8) through a pipeline, and a third discharging hole of the main cooling box (8) is used for conveying the low-pressure normal-temperature mixed refrigerant (2) through the pipeline;
the backflow lean natural gas (5) is connected with a second feed inlet of the multi-stream plate-fin reboiler (22) through a pipeline, a second discharge outlet of the multi-stream plate-fin reboiler (22) is connected with a first feed inlet of the main cooling box (8) through a pipeline, and a first discharge outlet of the main cooling box (8) is connected with a first stream inlet of the demethanizer (15) through a pipeline;
the reboiled condensate outlet (16) is connected with a third feed inlet of the multi-stream plate-fin reboiler (22) through a pipeline, and a third discharge outlet of the multi-stream plate-fin reboiler (22) is connected with the reboiled condensate return outlet (17) through a pipeline;
c at the bottom of the demethanizer (15)2 +The mixed hydrocarbon outlet (27) is connected with a fourth feed inlet of the multi-flow plate-fin reboiler (22) through a pipeline, and a third discharge outlet of the multi-flow plate-fin reboiler (22) outputs C through the pipeline2 +And (4) a mixed hydrocarbon.
2. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: the top of the demethanizer (15) is provided withA low-temperature lean natural gas outlet (30) is arranged, the low-temperature lean natural gas outlet (30) is connected with a second feeding hole of the main cooling box (8) through a pipeline, a second discharging hole of the main cooling box (8) is connected with an inlet of the coaxial booster expansion machine (12) through a pipeline, and an outlet of the coaxial booster expansion machine (12) is connected with the inlet of the coaxial booster expansion machine (12) through a pipeline2 +A mixed hydrocarbon lean natural gas recovery tank (1).
3. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: and a tower outlet side boiling condensate outlet (28) and a tower return side boiling condensate inlet (29) are formed in the side wall of the middle upper part of the demethanizer (15), and the tower outlet side boiling condensate outlet (28), the tower return side boiling condensate inlet (29) and a sixth feeding hole and a sixth discharging hole of the main cooling box (8) form a circulation loop.
4. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: and a bypass flow regulating valve (23) is connected in parallel between the first feeding hole and the first discharging hole of the multi-stream plate-fin reboiler (22).
5. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: and a mixed refrigerant J-T valve (24) is arranged between the third feeding port and the third discharging port of the main cooling box (8).
6. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: c at the bottom of the demethanizer (15)2 +The mixed hydrocarbon outlet (27) is passed through C2 +The hydrocarbon mixture booster pump (20) is connected with a fourth feed inlet of the multi-stream plate-fin reboiler (22), and C2 +C is arranged on a connecting pipeline between the hydrocarbon mixture booster pump (20) and the fourth feed inlet of the multi-stream plate-fin reboiler (22)2 +Liquid level of mixed hydrocarbonDetectors (19) and C2 +A hydrocarbon mixture liquid level regulating valve (21).
7. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: and a first flow regulating valve (14) is connected on a connecting pipeline between a first discharge hole of the main cooling box (8) and a first stock flow inlet of the demethanizer (15).
8. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: a second flow regulating valve (13) is arranged on a connecting pipeline between a second gas phase discharge hole of the low-temperature separator (9) and a second stream inlet connected with the demethanizer (15); a liquid level detector (11) and a liquid level regulating valve (10) are arranged on a connecting pipeline between a liquid phase discharge port of the low-temperature separator (9) and a fourth material flow inlet connected with the demethanizer (15).
9. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: the coaxial booster expander (12) and C2 +A check valve (25) and a lean natural gas boundary valve (26) are arranged on a connecting line between the mixed hydrocarbon lean natural gas recovery tanks (1).
10. The apparatus for energy utilization in a demethanizer having a multi-stream plate-fin reboiler as set forth in claim 1, wherein: and a raw material natural gas boundary valve (7) is arranged on a connecting pipeline between the raw material natural gas and the fourth feed inlet of the main cooling box (8).
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111750613A (en) * 2020-07-08 2020-10-09 西安长庆科技工程有限责任公司 Apparatus and method for energy utilization in a demethanizer having a plurality of flow plate-fin reboilers

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111750613A (en) * 2020-07-08 2020-10-09 西安长庆科技工程有限责任公司 Apparatus and method for energy utilization in a demethanizer having a plurality of flow plate-fin reboilers

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