CN203474726U - Device for separating catalytic cracking dry gas - Google Patents
Device for separating catalytic cracking dry gas Download PDFInfo
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- CN203474726U CN203474726U CN201320360852.2U CN201320360852U CN203474726U CN 203474726 U CN203474726 U CN 203474726U CN 201320360852 U CN201320360852 U CN 201320360852U CN 203474726 U CN203474726 U CN 203474726U
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- Hydrogen, Water And Hydrids (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a device for separating catalytic cracking dry gas, relates to the technical field of petroleum and chemical engineering, and particularly relates to a method and a device for simultaneously recycling the catalytic cracking dry gas in a multi-target manner by using a membrane separation and cryogenic separation coupling technology. The device comprises a buffering tank, a compressor, a gas-liquid separator, a filter, a heater I, a heater II, a heater III, a heater IV, a hydrogen membrane system, a refrigeration compressor, a cold box, an organic steam membrane, a demethanizer, a dethanizer and a fuel gas pipe net. The device is used for replacing a pure cryogenic separation technology and is small in occupied area, low in investment and simple in structure; the recycling rate of hydrogen and light hydrocarbon can be up to be more than 99%; the device has good economic benefits, social benefits and environmental benefits and can be applied to petroleum and chemical engineering industries.
Description
Technical field
The utility model relates to petroleum and chemical industry technical field, is a kind of membrane sepn and low temperature separation process coupling technique of utilizing specifically, and multiple goal reclaims the device of catalytic cracked dry gas simultaneously.
background technology
Oil has become the weapon of great powers in the world's economy, military affairs, political struggle, and the reserves that it is limited and growing demand have become the problem that everybody is concerned about most.In petroleum refining process, can produce the refinery exhaust that the lighter hydrocarbons such as a large amount of hydrogen and methane, ethane, propane form, in tail gas, contain a large amount of high added value materials.How fully utilizing refinery gas resource, is the necessary means that improves oil refining working depth and economic benefit.
Domestic refinery mostly is extensive production, and refinery gas tripping device generally adopts monotechnics, but exist, raw material subject range is narrow, recovery target is single, the shortcomings such as the rate of recovery is low, per unit area yield energy consumption height.
utility model content
Technical problem to be solved in the utility model is that a kind of device for separating of catalytic cracked dry gas will be provided, the rate of recovery of this device hydrogen and lighter hydrocarbons reaches more than 99%, there is good economic benefit, social benefit and environmental benefit, can be in petroleum and chemical industry sector application.
The purpose of this utility model is achieved through the following technical solutions:
Device for separating of catalytic cracked dry gas, it is characterized in that: surge tank, compressor, gas-liquid separator, strainer, well heater I, well heater II, well heater III, well heater IV, hydrogen membrane system, refrigeration compressor, ice chest, organic steam film, demethanizing tower, deethanizing column and fuel gas pipe network, consist of, the right-hand member outlet of surge tank is connected with the entrance that is positioned at the compressor on its right side; The outlet of compressor is connected with the upper end import that is positioned at the gas-liquid separator on its right side; The upper end outlet of gas-liquid separator is connected with the import that is positioned at the strainer on its right side, and the lower end outlet of gas-liquid separator is connected with the well heater I import that is positioned at its below; The outlet of strainer is connected with the well heater II import that is positioned at its right side, and well heater II outlet is connected with the hydrogen membrane import that is positioned at its right side; The upper end outlet of hydrogen membrane is connected with the ice chest upper end import that is positioned at its below; The right-hand member of ice chest is connected with refrigeration compressor left end; The lower end outlet of ice chest is connected with the well heater III import that is positioned at its below; The left upper end outlet of ice chest is connected with the well heater IV import that is positioned at its left side, and well heater IV outlet is connected with the organic steam film import that is positioned at its left side, and the outlet of organic steam film upper end is connected with the filter outlet being located thereon; The outlet of organic steam film left side is connected with the demethanizing tower upper right side import that is positioned at its left side, and the lower end outlet of demethanizing tower is connected with the right-hand member import that is positioned at the deethanizing column in its left side.Wherein demethanizing tower upper end outlet, the outlet of deethanizing column upper end, the outlet of well heater III left side, the outlet of well heater I lower end are connected with fuel gas pipe network, and described fuel gas pipe network is positioned at the upper end of demethanizing tower and deethanizing column.The described pipeline that is connected to is fixedly connected with.
For separating of the combination process of catalytic cracked dry gas, it adopts the combination process that comprises membrane sepn and low temperature separation process operation, is mainly that novel organic steam film is applied in catalytic cracked dry gas sepn process.Comprise: (1) catalytic cracked dry gas is introduced into after surge tank voltage stabilizing, de-liquid, enter compressor and carry out supercharging, gas after supercharging enters gas-liquid separator and carries out gas-liquid separation, after liquid hydrocarbon heater via I heating, entering fuel gas pipe net reclaims, mixed gas enters strainer and removes solia particle and the heavy hydrocarbon in gas, and heater via II is heated to than the high 10-20 ℃ of dew point, obtain not only clean but also warm gas, then enter hydrogen membrane system and carry out separation, because the relative infiltration rate of hydrogen is the fastest, Hydrogen Separation can be purified and recycled; (2) be enriched in hydrogen membrane system and hold back the lighter hydrocarbons of side and enter ice chest and compress coolingly, not only remove the moisture content of a great deal of, and C5+ cut and C1-C4 cut are carried out to separation, wherein C5+ cut enters fuel gas pipe net after well heater III heating; (3) C1-C4 cut enters organic steam film through after well heater IV heating, be enriched in the hydrogen of holding back side by pipeline with from filter outlet gas mixture out mixes, enter well heater II, reenter hydrogen membrane system and recycle; (4) mixed gas in organic steam membrane permeation side enters demethanizing tower, realize the fine separation of C1 and C2-C4 cut, tower top is sloughed C1 cut, liquid at the bottom of tower is C2-C4 cut, enter deethanizing column, tower top separates C2 cut and LPG (liquefied petroleum gas (LPG) is mainly C3, C 4 fraction); (5) C1 reclaiming, C2, C5+ cut are used as fuel gas through fuel gas pipe network.
The utility model has the advantages that: (1) hydrogen membrane system recoveries most of hydrogen in catalytic cracked dry gas, significantly reduced the dry gas amount that low temperature separation process is processed, obviously reduced cooling load and investment operation expense; (2) through organic steam film system, dry gas pressure drop is little, and suitably pressurization is applicable to the operation of demethanizing tower in low temperature separation process, has reduced operation easier; (3) this combination process has substituted simple deep cooling process for separating, and the rate of recovery of hydrogen and lighter hydrocarbons is reached more than 99%, has good economic benefit and environmental benefit.
Accompanying drawing explanation
Fig. 1 is that the utility model is for separating of the apparatus structure schematic block diagram of catalytic cracked dry gas
Embodiment
For separating of the apparatus structure schematic block diagram of catalytic cracked dry gas, comprise surge tank 1, compressor 2, gas-liquid separator 3, strainer 4, well heater I5, well heater II6, well heater III7, well heater IV8, hydrogen membrane system 9, refrigeration compressor 10, ice chest 11, organic steam film 12, demethanizing tower 13, deethanizing column 14, fuel gas pipe network 15 as shown in Figure 1.
The catalytic cracked dry gas of having collected is introduced into surge tank 1 voltage stabilizing, after de-liquid, enter compressor 2 and carry out supercharging, gas after supercharging enters gas-liquid separator 3 and carries out gas-liquid separation, after liquid hydrocarbon heater via I5 heating, entering fuel gas pipe net 15 reclaims, mixed gas enters strainer 4 and removes solia particle and the heavy hydrocarbon in gas, and heater via II6 is heated to than the high 10-20 ℃ of dew point, obtain not only clean but also warm gas, then enter hydrogen membrane system 9 and carry out separation, because the relative infiltration rate of hydrogen is the fastest, Hydrogen Separation can be purified and recycled, (2) being enriched in hydrogen membrane system 9 holds back the lighter hydrocarbons of side and enters ice chest 11, and cooling through refrigeration compressor 10 compressions, not only remove the moisture content of a great deal of, and C5+ cut and C1-C4 cut are carried out to separation, wherein C5+ cut enters fuel gas pipe net 15 after well heater III heating, (3) C1-C4 cut enters organic steam film 12 through after well heater IV8 heating, be enriched in the hydrogen of holding back side by pipeline with from filter outlet gas mixture out mixes, enter well heater II6, reenter hydrogen membrane system 9 and recycle, (4) mixed gas in organic steam film 12 per-meate side enters demethanizing tower 13, realize the fine separation of C1 and C2-C4 cut, tower top is sloughed C1 cut, liquid at the bottom of tower is C2-C4 cut, enter deethanizing column 14, tower top separates C2 cut and LPG (liquefied petroleum gas (LPG) is mainly C3, C 4 fraction), (5) C1 reclaiming, C2, C5+ cut are used as fuel gas through fuel gas pipe network 15.
The utility model has substituted simple deep cooling process for separating, and floor space is little, and less investment is simple in structure, and the rate of recovery of hydrogen and lighter hydrocarbons reaches more than 99%, has obvious economic benefit and social benefit, has reduced environmental pollution.
Claims (1)
1. for separating of a device for catalytic cracked dry gas, it is characterized in that:
Comprise surge tank, compressor, gas-liquid separator, strainer, well heater I, well heater II, well heater III, well heater IV, hydrogen membrane system, refrigeration compressor, ice chest, organic steam film, demethanizing tower, deethanizing column and fuel gas pipe network;
The right-hand member outlet of surge tank is connected with the entrance that is positioned at the compressor on its right side; The outlet of compressor is connected with the upper end import that is positioned at the gas-liquid separator on its right side; The upper end outlet of gas-liquid separator is connected with the import that is positioned at the strainer on its right side, and the lower end outlet of gas-liquid separator is connected with the well heater I import that is positioned at its below; The outlet of strainer is connected with the well heater II import that is positioned at its right side, and well heater II outlet is connected with the hydrogen membrane import that is positioned at its right side; The upper end outlet of hydrogen membrane is connected with the ice chest upper end import that is positioned at its below; The right-hand member of ice chest is connected with refrigeration compressor left end; The lower end outlet of ice chest is connected with the well heater III import that is positioned at its below; The left upper end outlet of ice chest is connected with the well heater IV import that is positioned at its left side, and well heater IV outlet is connected with the organic steam film import that is positioned at its left side, and the outlet of organic steam film upper end is connected with the filter outlet being located thereon; The left side outlet of organic steam film is connected with the demethanizing tower upper right side import that is positioned at its left side, and the lower end outlet of demethanizing tower is connected with the right-hand member import of deethanizing column on the left of being positioned at it, described in be connected to pipeline and be fixedly connected with; The outlet of demethanizing tower upper end, the outlet of deethanizing column upper end, the outlet of well heater III left side, the outlet of well heater I lower end are connected with fuel gas pipe network, and described fuel gas pipe network is positioned at the upper end of demethanizing tower and deethanizing column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320360852.2U CN203474726U (en) | 2013-06-24 | 2013-06-24 | Device for separating catalytic cracking dry gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320360852.2U CN203474726U (en) | 2013-06-24 | 2013-06-24 | Device for separating catalytic cracking dry gas |
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| Publication Number | Publication Date |
|---|---|
| CN203474726U true CN203474726U (en) | 2014-03-12 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201320360852.2U Expired - Fee Related CN203474726U (en) | 2013-06-24 | 2013-06-24 | Device for separating catalytic cracking dry gas |
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| CN (1) | CN203474726U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111467913A (en) * | 2020-03-27 | 2020-07-31 | 大连海奥膜技术有限公司 | Comprehensive recycling process and equipment for refinery tail gas |
| CN112023605A (en) * | 2019-06-03 | 2020-12-04 | 中石化南京化工研究院有限公司 | Organic steam retrieves experimental apparatus |
-
2013
- 2013-06-24 CN CN201320360852.2U patent/CN203474726U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112023605A (en) * | 2019-06-03 | 2020-12-04 | 中石化南京化工研究院有限公司 | Organic steam retrieves experimental apparatus |
| CN111467913A (en) * | 2020-03-27 | 2020-07-31 | 大连海奥膜技术有限公司 | Comprehensive recycling process and equipment for refinery tail gas |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140312 Termination date: 20210624 |
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| CF01 | Termination of patent right due to non-payment of annual fee |