CN203269811U - High-purity n-butane production device - Google Patents
High-purity n-butane production device Download PDFInfo
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- CN203269811U CN203269811U CN 201320251197 CN201320251197U CN203269811U CN 203269811 U CN203269811 U CN 203269811U CN 201320251197 CN201320251197 CN 201320251197 CN 201320251197 U CN201320251197 U CN 201320251197U CN 203269811 U CN203269811 U CN 203269811U
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Abstract
The utility model provides a high-purity n-butane production device. The high-purity n-butane production device comprises a C4 modification part and a saturation hydrogenation part, wherein a C4 modification raw material tank and a C4 modification reactor are connected, a modified product obtained through internal modification reaction enters a hydrogenated reactor through equipment such as a cutting tower and a stabilizing tower, and is separated through a high-separation tank and a low-separation tank and the like, to finally obtain the product n-butane. According to the high-purity n-butane production device, the utilization rate of the reaction product is high by taking C4 as a raw material, the production device is simple in structure, small in investment, easy to operate, and capable of recycling the heat of the reaction product and avoiding heat waste, as well as realizing the recycling of hydrogen and regenerative air.
Description
Technical field
The utility model relates to a kind of production equipment of high purity normal butane.
Background technology
Normal butane is colourless gas, and is water insoluble, easy molten alcohol, chloroform, and have inflammable and explosive property, be often used as solvent, cooling agent and organic synthesis raw material.All contain normal butane in oil field gas, wet natural gas and reacted gas, the topmost mode of production of normal butane is for to transform preparation by C-4-fraction, corresponding C-4-fraction also mainly is present in oil field gas, wet natural gas and reacted gas, for example: carbon four hydrocarbon of coproduction in petrochemical complex light oil cracking ethylene unit processed account for 40% of ethylene yield; Carbon four hydrocarbon that petroleum refinery's catalytic cracking unit is produced account for 6% of unit capacity; Separate from oil field gas and wet natural gas and the condensation of pressurizeing obtains the liquefied petroleum gas (LPG) of carbon three, carbon four, then separate with distillation method and obtain carbon four.Owing to containing more alkene in C-4-fraction, its polyreaction is more, and exothermic heat of reaction is violent, makes carbon four be converted into the transformation efficiency of normal butane very limited, and then make C-4-fraction directly enter liquid gas storage tank to use as low price fuel, reduced the economic worth of C-4-fraction.Therefore how the freshening C-4-fraction, rationally utilize carbon four and then produce highly purified normal butane, becomes the technical problem that those skilled in the art need to be resolved hurrily.
The utility model content
Technical problem to be solved in the utility model is to provide a kind of production equipment of high purity normal butane, has solved the technical problem of efficient purification normal butane in the prior art.
The utility model provides a kind of production equipment of high purity normal butane, comprise carbon four upgrading head tanks, described carbon four upgrading head tanks are connected with the opening for feed of carbon four reforming reactors by First Heat Exchanger, vapour producer, the first process furnace in turn, and the discharge port of carbon four reforming reactors connects Cutting Tap by First Heat Exchanger;
The regeneration gas import of described carbon four reforming reactors is connected with the second process furnace, the second interchanger in turn, and the regeneration tail gas outlet of carbon four reforming reactors is connected with the regeneration gas import of carbon four reforming reactors by the second interchanger, the first condenser, surge tank, the first compressor in turn;
The tower bottom outlet of described Cutting Tap is connected with the heavy hydrocarbon storage tank, the tower top outlet of described Cutting Tap connects knockout drum by the second condenser, the liquid-phase outlet of knockout drum is through boosting pump stable connection tower, the gaseous phase outlet of knockout drum is through the second compressor also stable connection tower, the tower top outlet of stabilizer tower connects carbon four raw material surge tanks, and the tower bottom outlet of stabilizer tower connects light hydrocarbon storage tank through the 3rd condenser;
Described carbon four raw material surge tanks are connected with the feeding mouth of hydrogenator by the 3rd interchanger, the reaction product spout of hydrogenator is connected with the high score tank by the 4th condenser, the first liquid-phase outlet of high score tank is connected with the feeding mouth of hydrogenator, and the second liquid phase outlet of high score tank is connected with the entrance of low minute tank; The top gaseous phase outlet of low minute tank is connected with the inlet mouth of hydrogenator by the 3rd compressor, and the liquid-phase outlet of low minute tank is connected with the normal butane holding tank.
Further, described hydrogenator also is connected with well heater.
Further, be connected with the 3rd interchanger between the reaction product spout of described hydrogenator and the 4th condenser.
The advantage that the utlity model has is:
The utility model problem that carbon four can't utilize, the alkane value is lower after for ether, a kind of production equipment of high purity normal butane is provided, utilize this production equipment can carbon four be converted into the low aromatic component of olefin(e) centent, the blending component that also can produce simultaneously motor liquified gas under the condition of non-hydrogen.Take carbon four as raw material, react with series of complexes such as dehydrocyclization, aromatization, dehydrocyclizations through C 4 olefin is superimposed in this production equipment, produce light aromatic hydrocarbons and heavy aromatics, its principle utilization ratio is high.This production equipment is simple in structure, invest little, processing ease, heat that can the recycle reaction product is avoided heat waste.
Description of drawings
Fig. 1 is the structural representation that the utility model provides a kind of production equipment of high purity normal butane.
In figure: 1-carbon four head tanks; The 2-First Heat Exchanger; The 3-vapour producer; 4-the first process furnace; 5--carbon four reforming reactors; The 6-Cutting Tap; 7-the second interchanger; 8-the second process furnace; 9-the first condenser; The 10-surge tank; 11-the first compressor; 12-normal butane holding tank; 13-the second condenser; The 14-knockout drum; The 15-boosting pump; The 16-stabilizer tower; 17 the 3rd condensers; 18-the second compressor; 19-heavy hydrocarbon storage tank; 20-carbon four raw material surge tanks; The 21-light hydrocarbon storage tank; 22-hydrogenation fresh feed pump; 23-the 3rd interchanger; The 24-hydrogenator; The 25-well heater; 26-the 4th condenser; 27-high score tank; The low minute tank of 28-; 29-the 3rd compressor.
Embodiment
The utility model is described in further detail below in conjunction with the drawings and specific embodiments, so that those skilled in the art can better understand the utility model and being implemented, but illustrated embodiment is not as to restriction of the present utility model.
The utility model provides a kind of production equipment of high purity normal butane, as shown in Figure 1, mainly comprises carbon four upgrading part and saturated hydrogenation parts, and wherein carbon four upgradings partly comprise upgrading reaction member, catalyst regeneration units and fractionation unit.The saturated hydrogenation part mainly comprises hydrogenation reaction unit and separating unit.
Described upgrading reaction member comprise realize feed vaporization, reactor turnover logistics heat exchange, charging heating, reactor, reaction product is cooling and the part such as catalyst regeneration.After raw material in carbon four upgrading head tanks 1 (carbon four after the ether removed of Trimethylmethane) carries out heat exchange by the reaction product that produces with the upgrading reaction by First Heat Exchanger 2, vaporize by vapour producer 3, gas-phase carbon four upgrading raw materials after vaporization can be more further with upgrading after reaction product carry out heat exchange after, be heated to 280 ℃～405 ℃ (raise initial stage to latter stage gradually) by the first process furnace 4, then the opening for feed by carbon four reforming reactors enters and carries out the upgrading reaction in carbon four reforming reactors 5.Approximately 40 ℃ of temperature rises, the working pressure 0.6MPaG of carbon four reforming reactors 5,280～430 ℃ of temperature.In the presence of catalyzer, carry out the upgrading reaction, after the upgrading reaction finishes, after the discharge port outflow of the reaction product that production obtains by carbon four reforming reactors, after carrying out heat exchange with the charging of carbon four by First Heat Exchanger 2, cool to certain temperature, carry out preliminary gas-liquid separation, liquid phase after initial gross separation enters Cutting Tap 6, has also obtained gas phase after initial gross separation, can pass through the cooling rear discharge of condenser.
In catalyst regeneration units, adopt nitrogen and air as regeneration gas, control the oxygen level in regeneration gas, in case beds temperature runaway when regeneration in blocking four reforming reactors, and destroy catalyzer.The heat of the tail gas that produces during for reclaiming, regeneration gas first carried out heat exchange by the second interchanger 7 with regeneration tail gas before entering carbon four reforming reactors 5, then be heated to regenerate by the second process furnace 8 temperature required, enter in carbon four reforming reactors 5 by the regeneration gas import and carry out catalyst regeneration.Regeneration pressure 0.7MPaG, 450 ℃ of temperature.And after regeneration tail gas and fresh regenerated gas carries out heat exchange by the second interchanger 7, by the first condenser 9(water-cooled) be cooled to 40 ℃, then pass through 10 unwaterings of flue gas surge tank, again after the first compressor 11 compression again after the surge tank buffering as regeneration gas, circulation enters in carbon four reforming reactors 5 regenerates.
Described dividing cell is Cutting Tap 6, in carbon four reforming reactors after reaction the liquid phase after the initial gross separation that obtains enter Cutting Tap 6, the working pressure 0.15MPaG of Cutting Tap 6, temperature 60 C～260 ℃.The tower bottom outlet flows out heavier hydrocarbon products, delivers to corresponding heavy hydrocarbon storage tank 19.Tower top outlet flows out light hydrocarbon product, through the second condenser 13(water-cooled) after enter knockout drum 14 and separate, liquid phase after separation flows out by liquid-phase outlet and enters stabilizer tower 16 after boosting by boosting pump 15, and the gas phase after separation also enters stabilizer tower 16 after gaseous phase outlet flows out by the second compressor 18 compressions.The working pressure 0.8MPaG of stabilizer tower 16, temperature 50 C～160 ℃.The overhead product of stabilizer tower 16 is collected carbon four raw material surge tanks 20, in order to carrying out next step reaction in the saturated hydrogenation part, can certainly use as the liquefied gas of high-quality.The above component of carbon five of tower bottom outlet output is delivered to light hydrocarbon storage tank 21 as light hydrocarbon product and is stored after the 3rd condenser 17 is cooled to 40 ℃.The return tank discharge outlet of stabilizer tower 16 non-condensable gas of the discharging gas that acts as a fuel is in addition delivered in the utility model in each process furnace, realizes that heat recycles.
in entering carbon four raw material surge tanks 20 from the high-quality liquefied gas of the overhead product of stabilizer tower 16 in carbon four upgradings parts under liquid level is controlled, sneak into again recycle hydrogen after boosting to 2.70MPaG and hydrogenation products cycle stock from high score tank 27 mixes by hydrogenation fresh feed pump 22, the 3rd interchanger 23 of new hydrogen and enter reactor from the low minute gas of low minute tank 27 and advance/discharging heat exchange, heat up rear to 41 ℃ (60 ℃ of latter stages) left and right with reaction effluent heat exchange in hydrogenator 24, feeding mouth by hydrogenator enters in hydrogenator 24, material carbon four in hydrogenator 24 carries out olefin saturation, temperature rises to 71 ℃ (83.58 ℃ of latter stages) left and right, reaction pressure is 2.48MPaG.During reaction, hydrogenator 24 is steam heated to 40 ℃ (60 ℃ of latter stages) left and right with 1.2MPaG under the effect of well heater 25.When well heater 25 can be simultaneously as reducing catalyst, the hydrogen well heater uses.
In hydrogenator 24, the reaction product that obtains of reaction exports outflow by reactant flow, this reaction product initial stage the 3rd interchanger 23 need not, approximately 71 ℃ of the reactant flow temperature outs of hydrogenator 24 directly enter the 3rd interchanger 23 through bypass; Latter stage, hydrogenator 24 reactant flow temperature out was approximately 83.6 ℃, be cooled to 71 ℃ of left and right through the 3rd interchanger 23 with the parallel feeding heat exchange, enter again reaction effluent cooling by the 4th condenser 26, can adopt to enter high score tank 27 after circulating water to 40 ℃ and carry out vapor-liquid separation, namely enter separating unit and separate.
The liquid phase of telling in high score tank 27 flows out by two outlets, the liquid phase that flows out in the first liquid-phase outlet is connected with the feeding mouth of hydrogenator 24, arriving hydrogenator 24 entrances as cycle stock by pump delivery mixes with fresh carbon four, to regulate the content of the alkene that hydrogenator 24 opening for feeds enter, the second liquid phase outlet enters the entrance of low minute tank 28 by Liquid level adjusting valve as product.Hydrogenated products oil in low minute tank 28 the step-down flash distillation to the 0.6MPaG left and right, low minute tank 28 a top gaseous phase outlets gas phase out enters in the 3rd compressor 29, be compressed to the feeding mouth that returns to hydrogenator 24 after 2.65MPaG, with come back in hydrogenator 24 after other charging mixes, its inlet mouth by hydrogenator enters.Low minute tank 28 liquid phase out flows out by the liquid-phase outlet of low minute tank, is stored to normal butane holding tank 12 as the finished product of whole production equipment by Liquid level adjusting valve and completes collection.
Be interrupted from high score tank 27 tops gas phase (recycle hydrogen) out and put sub-fraction to flare system, with controlled circulation hydrogen purity (CO, the CO2 etc. that accumulate in hydrogen are removed), rest part enters recycle compressor (the 4th compressor) entrance after a minute flow container is told micro-liquid phase, enter and enter in hydrogenator after circulating hydrogen compressor is compressed to 2.70MPaG and new hydrogen from battery limit (BL) 2.7MPaG mixes, realize the hydrogen recycle utilization.
The utility model provides a kind of production equipment of high purity normal butane, utilize this production equipment can C 4 olefin be converted into the cut of the amount of being rich in aromatic hydrocarbons under the condition of non-hydrogen, and the normal butane of having purified simultaneously, in this production equipment after the ether that does not contain Trimethylmethane carbon four as raw material, through the reaction of the series of complexes such as the superimposed and dehydrocyclization of C 4 olefin, aromatization, dehydrocyclization, C 4 olefin is converted into light aromatic hydrocarbons and heavy aromatics so that normal butane is purified.This production equipment is simple in structure, invest little, processing ease, heat that can the recycle reaction product is avoided heat waste, can also realize the recycle of hydrogen, the recycle of regeneration air simultaneously, really realizes green production.
The above embodiment is the preferred embodiment that proves absolutely that the utility model is lifted, and protection domain of the present utility model is not limited to this.Being equal to that those skilled in the art do on the utility model basis substitutes or conversion, all within protection domain of the present utility model.Protection domain of the present utility model is as the criterion with claims.
Claims (3)
1. the production equipment of a high purity normal butane, it is characterized in that, comprise carbon four upgrading head tanks, described carbon four upgrading head tanks are connected with the opening for feed of carbon four reforming reactors by First Heat Exchanger, vapour producer, the first process furnace in turn, and the discharge port of carbon four reforming reactors connects Cutting Tap by First Heat Exchanger;
The regeneration gas import of described carbon four reforming reactors is connected with the second process furnace, the second interchanger in turn, and the regeneration tail gas outlet of carbon four reforming reactors is connected with the regeneration gas import of carbon four reforming reactors by the second interchanger, the first condenser, surge tank, the first compressor in turn;
The tower bottom outlet of described Cutting Tap is connected with the heavy hydrocarbon storage tank, the tower top outlet of described Cutting Tap connects knockout drum by the second condenser, the liquid-phase outlet of knockout drum is through boosting pump stable connection tower, the gaseous phase outlet of knockout drum is through the second compressor also stable connection tower, the tower top outlet of stabilizer tower connects carbon four raw material surge tanks, and the tower bottom outlet of stabilizer tower connects light hydrocarbon storage tank through the 3rd condenser;
Described carbon four raw material surge tanks are connected with the feeding mouth of hydrogenator by the 3rd interchanger, the reaction product spout of hydrogenator is connected with the high score tank by the 4th condenser, the first liquid-phase outlet of high score tank is connected with the feeding mouth of hydrogenator, and the second liquid phase outlet of high score tank is connected with the entrance of low minute tank; The top gaseous phase outlet of low minute tank is connected with the inlet mouth of hydrogenator by the 3rd compressor, and the liquid-phase outlet of low minute tank is connected with the normal butane holding tank.
2. the production equipment of high purity normal butane according to claim 1, is characterized in that, described hydrogenator also is connected with well heater.
3. the production equipment of high purity normal butane according to claim 2, is characterized in that, is connected with the 3rd interchanger between the reaction product spout of described hydrogenator and the 4th condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320251197 CN203269811U (en) | 2013-05-10 | 2013-05-10 | High-purity n-butane production device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201320251197 CN203269811U (en) | 2013-05-10 | 2013-05-10 | High-purity n-butane production device |
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| CN203269811U true CN203269811U (en) | 2013-11-06 |
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| CN 201320251197 Expired - Fee Related CN203269811U (en) | 2013-05-10 | 2013-05-10 | High-purity n-butane production device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103773498A (en) * | 2013-11-28 | 2014-05-07 | 山东海成石化工程设计有限公司 | High-temperature hydrogenation and purification process for liquefied gas materials |
-
2013
- 2013-05-10 CN CN 201320251197 patent/CN203269811U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103773498A (en) * | 2013-11-28 | 2014-05-07 | 山东海成石化工程设计有限公司 | High-temperature hydrogenation and purification process for liquefied gas materials |
| CN103773498B (en) * | 2013-11-28 | 2015-09-02 | 山东海成石化工程设计有限公司 | The high temperature hydrogenation purification process of liquefied gas material |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20131106 Termination date: 20190510 |
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| CF01 | Termination of patent right due to non-payment of annual fee |