CN210163383U - Light hydrocarbon humidifying and steam distributing system - Google Patents
Light hydrocarbon humidifying and steam distributing system Download PDFInfo
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- CN210163383U CN210163383U CN201920883207.6U CN201920883207U CN210163383U CN 210163383 U CN210163383 U CN 210163383U CN 201920883207 U CN201920883207 U CN 201920883207U CN 210163383 U CN210163383 U CN 210163383U
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- raw material
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- light hydrocarbon
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 32
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 32
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 31
- 239000002994 raw material Substances 0.000 claims abstract description 71
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 238000000034 method Methods 0.000 claims abstract description 42
- 238000005336 cracking Methods 0.000 claims abstract description 37
- 238000010992 reflux Methods 0.000 claims abstract description 14
- 239000007788 liquid Substances 0.000 claims abstract description 4
- 238000005507 spraying Methods 0.000 claims abstract description 3
- 239000010865 sewage Substances 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 abstract description 4
- 229920006395 saturated elastomer Polymers 0.000 abstract description 3
- 238000010790 dilution Methods 0.000 description 30
- 239000012895 dilution Substances 0.000 description 30
- 239000007921 spray Substances 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000010791 quenching Methods 0.000 description 3
- 230000000171 quenching effect Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000009738 saturating Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a light hydrocarbon humidifying and steam distributing system, which uses a raw material humidifying tower, a process water stripping tower and a cracking furnace, wherein the light hydrocarbon raw material enters the lower part of the raw material humidifying tower after being preheated by the cracking furnace; the process water after steam stripping in the process water stripping tower enters the lower part of the raw material humidifying tower after being pressurized; the liquid phase in the raw material humidifying tower returns to the upper part of the raw material humidifying tower from the bottom of the tower through a reflux pump and a reflux heater to be used as spraying liquid, and is in countercurrent contact with the light hydrocarbon raw material entering the lower part of the raw material humidifying tower for heat exchange to form saturated mixed light hydrocarbon raw material; the saturated mixed light hydrocarbon raw material passes through a raw material superheater through a pipeline on the top of the raw material humidifying tower and finally enters a cracking section of a cracking furnace to generate cracked gas.
Description
Technical Field
The utility model relates to a light hydrocarbon humidifying steam distribution system in the ethylene cracking technology.
Background
At present, the ethylene cracking technology mainly utilizes the combination of short retention time, high temperature and low hydrocarbon partial pressure (i.e. optimum dilution steam to hydrocarbon feeding ratio) to promote the reaction equilibrium to improve the diene yield and inhibit the movement of coking direction. The flexible adjustment of the proportion of the dilution steam and the raw material is a key technology of the cracking furnace.
A traditional feed gas proportioning dilution steam system is shown in figure 1 and comprises a process water stripping tower 11, a dilution steam generator 12 and a cracking furnace 13, process water enters the process water stripping tower 11 through a process water feeding heater 14, the pressure of the process water is increased through a dilution steam feeding pump 15 at the bottom of the tower, the process water is heated through a dilution steam heater 16 and enters the dilution steam generator 12, generated dilution steam flows through a dilution steam superheater 17 and then enters a convection section of the cracking furnace 13 to complete heat exchange, the dilution steam is mixed with raw materials which complete heat exchange through convection sections of various coil pipes and the cracking furnace, and finally the raw materials enter the cracking section of the cracking furnace 13 to form cracking gas.
Wherein, the dilution steam generator generally adopts two reboiling heat sources, one is quenching oil, and the other is steam. If the light feedstock is cracked, only steam heating is used. The operating pressure of the dilution steam is 0.6-0.9 MPaA so as to meet the pressure requirement of the dilution steam mixed into the raw material, and the mass ratio (such as 0.3) of the dilution steam and the raw material is controlled through the flow ratio so as to achieve the purpose of steam distribution. The operation pressure of the dilution steam is limited, if steam heating is adopted, medium-pressure steam is generally adopted, and the pressure range is 0.9-1.6 MPaA.
The traditional process adopts a pipeline mixing method, steam is directly heated, supplemented and vaporized to generate diluted steam so as to achieve the pressure required by mixing, the pressure grade of the steam is high, a low-grade heat source cannot be used, and the energy consumption is high.
In addition, patent CN90108341.0 discloses a method for saturating feed gas by steam cracking, which utilizes the thermosiphon principle of a tubular heat exchanger, wherein feed gas and water enter a tube from bottom to top, and the outlet water phase is partially gasified and mixed with the feed gas to realize the saturation of the feed gas. The method heats a two-phase mixture of water and feed gas by adjusting the flow rate of steam, the water is partially vaporized, and the heat exchange is complex and difficult to meet the heat exchange requirement due to the heat exchange of the two phases and the strict control of the outlet temperature.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a light hydrocarbon humidification steam distribution system, on the one hand reduce the pressure level of steam, reduce the energy consumption, on the other hand make the system unlikely too complicated, strengthen the practicality.
In order to achieve the above object, the utility model adopts the following technical scheme:
a light hydrocarbon humidifying steam distribution system, which is characterized in that: comprises a raw material humidifying tower, a process water stripping tower and a cracking furnace, wherein:
the light hydrocarbon raw material is preheated by the cracking furnace and communicated to the lower part of the raw material humidifying tower;
the process water after steam stripping in the process water stripping tower is pressurized and then communicated to the lower part of the raw material humidifying tower;
the bottom of the raw material humidifying tower returns to the upper part of the raw material humidifying tower as spraying liquid through a reflux pump and a reflux heater to form a circulation loop;
the top of the raw material humidifying tower is finally communicated to the cracking section of the cracking furnace through a raw material superheater by a pipeline.
The light hydrocarbon humidifying steam distribution system comprises: the pipeline is firstly communicated to the convection section of the cracking furnace, exchanges heat through the first heat exchange coil and the second heat exchange coil and then is communicated to the cracking section of the cracking furnace.
The light hydrocarbon humidifying steam distribution system comprises: the raw material humidifying tower is provided with a continuous sewage discharge pipeline which is communicated to the battery compartment through a sewage discharge cooler.
The utility model provides a system, raw materials humidifying tower is equipped with circulation circuit, and circulation circuit adopts steam or the indirect heat transfer input heat of other heat sources, realizes that hot water and light hydrocarbon gas reverse spray mix to reach certain raw materials dilution steam ratio. The system has simple operation principle, is easy to control the proportion of dilution steam, the proportion (dilution ratio) of water and feed gas in the mixed gas at the outlet of the tower is a function of the operation pressure and temperature of the raw material humidifying tower, and the required dilution ratio can be achieved by controlling the operation temperature of the raw material humidifying tower when the pressure (back pressure of the cracking furnace) is constant.
In the system provided by the utility model, the temperature of the water returning to the raw material humidifying tower after heat exchange through the reflux heater in the circulation loop is within the range of 120-165 ℃, so that the reflux heater can use a lower-grade heat source to replace a traditional dilution steam generator system; the low-grade low-pressure steam is used for replacing medium-pressure steam in the traditional process, and 10-20 kg of standard oil/ton of ethylene can be saved, so that the purpose of energy conservation is achieved.
Drawings
FIG. 1 is a schematic diagram of a conventional feed gas proportioning dilution steam system;
fig. 2 is a schematic structural diagram of a light hydrocarbon humidifying steam distribution system provided by the utility model.
Description of reference numerals: a process water stripper 11; a dilution steam generator 12; a cracking furnace 13; a process water feed heater 14; a dilution steam feed pump 15; a dilution steam heater 16; a dilution steam superheater 17; a raw material humidifying tower 21; a process water stripper 22; a cracking furnace 23; a preheating coil 231; a first heat exchange coil 232; a second heat exchange coil 233; a process water feed heater 24; a raw material feed pump 25; a process water stripper reboiler 26; a reflux pump 27; a reflux heater 28; a blowdown cooler 29; a feedstock superheater 30.
Detailed Description
Some specific embodiments of the invention will be described in detail below, by way of example and not by way of limitation, with reference to the accompanying drawings. The same reference numbers in the drawings identify the same or similar elements or components. Those skilled in the art will appreciate that the drawings are not necessarily drawn to scale.
The present invention provides a light hydrocarbon humidifying and steam distributing system, which comprises a raw material humidifying tower 21, a process water stripping tower 22 and a cracking furnace 23, as shown in fig. 2, wherein:
the light hydrocarbon raw material becomes a superheated raw material after being preheated by the preheating coil 231 of the cracking furnace 23, and enters the lower part of the raw material humidifying tower 21;
removing trace solids and hydrocarbons from process water from a quenching water tower, heating the process water by a process water feeding heater 24, feeding the process water into a process water stripping tower 22, stripping volatile components in the process stripping tower 22, returning the stripped process water (the temperature is 118 ℃, the operating pressure is 0.15MPaA, and the flow rate is 66t/h) to the quenching water tower, boosting the pressure of the stripped process water by a raw material feeding pump 25, feeding the process water into a raw material humidifying tower 21 (the tower top temperature is 131 ℃, the tower bottom temperature is 106 ℃, and the operating pressure is 0.82MPaA), boosting a liquid phase at the tower bottom of the raw material humidifying tower 21 by a reflux pump 27 (the flow rate is 900t/h), heating the liquid phase by a reflux heater 28 (the outlet temperature is 140 ℃), returning the liquid phase to the raw material humidifying tower 21 as a spray liquid (forming a circulation loop), and carrying out countercurrent contact with a superheated raw material (the temperature is 150 ℃, and the flow rate; the saturated mixed light hydrocarbon raw material (with the temperature of 131 ℃ and the flow rate of 260t/h) in the raw material humidifying tower 21 is superheated (with the temperature of 140 ℃) by the raw material superheater 30 from the top of the raw material humidifying tower 21 and then returns to the convection section of the cracking furnace 23; the subsequent processing path and the processing method of the superheated mixed light hydrocarbon raw material are the same as those of the prior art, that is, the superheated mixed light hydrocarbon raw material enters the cracking section of the cracking furnace 23 to form cracked gas after passing through the heat exchange of the first heat exchange coil 232 and the second heat exchange coil 233 in the convection section of the cracking furnace 23.
Wherein, the mass ratio of the reflux spray amount of the raw material humidifying tower 21 to the raw material gas is 4.5, and the mass ratio of water to hydrocarbon is 0.3 after humidifying, saturating and distributing steam for the mixed light hydrocarbon raw material;
moreover, the raw material humidifying tower 21 is provided with a continuous sewage drainage pipeline, and sewage is cooled to 40 ℃ by a sewage cooler 29 and then is sent to a battery compartment.
The utility model provides a system and method, raw materials humidification tower is equipped with circulation circuit, and circulation circuit adopts steam or the indirect heat transfer of other heat sources input heat, realizes that hot water and light hydrocarbon gas reverse spray mix to reach certain raw materials dilution steam ratio. The system and the method have simple operation principle, the proportion of dilution steam is easy to control, the proportion (dilution ratio) of water and feed gas in the mixed gas at the outlet of the tower is a function of the operation pressure and the temperature of the raw material humidifying tower, and the required dilution ratio can be achieved by controlling the operation temperature of the raw material humidifying tower when the pressure (the backpressure of the cracking furnace) is constant.
The utility model provides a system and method can realize lower grade heat source utilization, and the fungible traditional dilution steam generator system uses the low pressure steam of low grade to replace the middling pressure steam in the traditional handicraft, can save 10 ~ 20 kg standard oil/ton ethylene to reach energy-conserving mesh.
The system and the method provided by the utility model, the light hydrocarbon raw material is the mixture or pure substance of ethane, propane, carbon four, carbon five, etc.
The utility model provides a system and method, the operating pressure of raw materials humidification tower is at 0.4-1.0MPaA within range, and when operating pressure was constant, through adjusting circulation loop's flow and/or temperature, can control the operating temperature of raw materials humidification tower to set for the mass ratio of steam and feed gas, this mass ratio is in 0 ~ 1 within range.
The utility model provides a system and method, reflux heater can use low-grade steam or other low-grade heat sources, and the temperature that satisfies the water that circulation circuit returned raw materials humidification tower is at 120 ~ 165 ℃ within ranges, and circulation circuit's water does not take place the phase transition after the heat transfer promptly.
The system and method provided by the utility model, circulation circuit's the quality that sprays volume and get into the light hydrocarbon raw materials of raw materials humidification tower lower part sprays than in the within range of 1-10.
The foregoing description is intended to be illustrative rather than limiting, and it will be appreciated by those skilled in the art that many modifications, variations or equivalents may be made without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (3)
1. A light hydrocarbon humidifying steam distribution system, which is characterized in that: comprises a raw material humidifying tower, a process water stripping tower and a cracking furnace, wherein:
the light hydrocarbon raw material is preheated by the cracking furnace and communicated to the lower part of the raw material humidifying tower;
the process water after steam stripping in the process water stripping tower is pressurized and then communicated to the lower part of the raw material humidifying tower;
the bottom of the raw material humidifying tower returns to the upper part of the raw material humidifying tower as spraying liquid through a reflux pump and a reflux heater to form a circulation loop;
the top of the raw material humidifying tower is finally communicated to the cracking section of the cracking furnace through a raw material superheater by a pipeline.
2. The light hydrocarbon moisturization steam distribution system of claim 1 wherein: the pipeline is firstly communicated to the convection section of the cracking furnace, exchanges heat through the first heat exchange coil and the second heat exchange coil and then is communicated to the cracking section of the cracking furnace.
3. The light hydrocarbon moisturization steam distribution system of claim 1 wherein: the raw material humidifying tower is provided with a continuous sewage discharge pipeline which is communicated to the battery compartment through a sewage discharge cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920883207.6U CN210163383U (en) | 2019-06-12 | 2019-06-12 | Light hydrocarbon humidifying and steam distributing system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920883207.6U CN210163383U (en) | 2019-06-12 | 2019-06-12 | Light hydrocarbon humidifying and steam distributing system |
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| Publication Number | Publication Date |
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| CN210163383U true CN210163383U (en) | 2020-03-20 |
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| CN201920883207.6U Active CN210163383U (en) | 2019-06-12 | 2019-06-12 | Light hydrocarbon humidifying and steam distributing system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110257100A (en) * | 2019-06-12 | 2019-09-20 | 中国寰球工程有限公司 | Light hydrocarbons humidification steam distribution system and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110257100A (en) * | 2019-06-12 | 2019-09-20 | 中国寰球工程有限公司 | Light hydrocarbons humidification steam distribution system and method |
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| TR01 | Transfer of patent right |
Effective date of registration: 20210224 Address after: 100120 Xicheng District six paw Kang in Beijing City Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. Address before: No.1, Chuangda 2nd Road, Laiguangying hi tech Industrial Park, Chaoyang District, Beijing, 100012 Patentee before: CHINA HUANQIU CONTRACTING & ENGINEERING Co.,Ltd. |
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