CN104830371A - Device and method of recycling C2 from refinery dry gas - Google Patents
Device and method of recycling C2 from refinery dry gas Download PDFInfo
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- CN104830371A CN104830371A CN201510013305.0A CN201510013305A CN104830371A CN 104830371 A CN104830371 A CN 104830371A CN 201510013305 A CN201510013305 A CN 201510013305A CN 104830371 A CN104830371 A CN 104830371A
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Abstract
The invention discloses a device of recycling C2 from refinery dry gas, which includes a PSA unit, a compression unit and an oil absorption unit. The PSA unit includes a first-section PSA device. The compression unit includes a compressor and a liquid separation pot. An inlet of the first-section PSA device is communicated with the raw material dry gas and an outlet of the first-section PSA device is communicated with the inlet of the compressor. The outlet of the compressor is communicated with the inlet of the liquid separation pot. The invention is advantaged in that firstly the raw material dry gas is subjected to primary concentration in the first-section PSA device being low in energy consumption, and then the PSA concentrated gas is further concentrated through an adsorption/desorption method being high in recycle rate and product purity, wherein the temperature of fed gas material, an absorbent and top reflux are all 40 DEG C in the absorption unit. By means of circulated cooling water, the cooling condensation temperature can be achieved without any refrigerating device. By means of the compressed condensate as the absorbent, it is unnecessary to feed a C4 absorbent from other apparatus. The invention also discloses a method of recycling C2 from the refinery dry gas.
Description
Technical field
What the present invention relates to is a kind of apparatus and method reclaiming C2 in oil refinery dry gas, specifically, about to C2 and the C2+ component in oil refinery dry gas, after utilizing PSA technique to carry out preliminary concentrate, recycling normal temperature oil absorption process to remove in concentrate gas the light constituents such as methane, hydrogen, nitrogen, oxygen further, the product of final acquisition, as a kind of method of ethylene production raw material, belongs to petroleum refinery's tail gas recycle technical field.
Background technology
The method that current oil refinery dry gas reclaims C2 mainly contains two sections of PSA methods and shallow cold oil method.
Two sections of PSA methods are provided with two sections of PSA, first paragraph PSA is main absorbing unit, and it is adsorbent bed to adopt PSA concentrate gas to replace after adsorption step further as displacement gas, to reduce the concentration of the undesirable components such as methane residual in bed, reaches the object improving concentrate purity of product gas.The effect of second segment PSA reclaims C2 and C2+ component in displacement waste gas, to improve total yield.
Shallow cold oil method take refining plant C 4 as absorption agent, at 10 ~ 15 DEG C of shallow cold temperature, absorbs C2, C3 component in dry gas, reach the object removing the component such as methane, hydrogen in absorption tower after original dry gas compression is boosted to about 4.0MPa.And then in desorption tower, desorb is carried out to the C4 absorption agent absorbing C2, C3 component, thus obtain rich C2 gas product.Absorb in the methane rich hydrogen fuel gas of tower top and carry C3, C4 component, then absorb C3, C4 component in fuel gas with gasoline or petroleum naphtha.Shallow cold oil method needs to provide cold by BrLi chiller, and dry gas and absorption agent are cooled to 10 ~ 15 DEG C.
Two sections of PSA methods have the advantage that energy consumption is low, working pressure is low, but simultaneously also have the shortcoming that the rate of recovery is lower, purity of product gas is lower, and its C2 rate of recovery is about 84% ~ 88%, methane content is about 10% (V) left and right in gas product.
Shallow cold oil method has the advantage of the rate of recovery high (90% ~ 93%), purity of product gas high (in gas product, methane content is less than 5% (V)), but has that energy consumption is high, working pressure is high simultaneously, needs to arrange BrLi chiller, needs to introduce C4 absorption agent and the shortcoming large with other device relational degree from outer device.
Summary of the invention
The object of this invention is to provide a kind of apparatus and method reclaiming C2 in oil refinery dry gas, while guaranteeing high-recovery and high product purities, reduce energy consumption level greatly.
For achieving the above object, the present invention carrys out specific implementation by the following technical programs:
Reclaim a device of C2 in oil refinery dry gas, comprise PSA unit, compressed element and oily absorptive unit;
Described PSA unit comprises one section of PSA device;
Described compressed element comprises compressor, point flow container, and the entrance of wherein said one section of PSA device is communicated with raw material dry gas, and the described outlet of one section of PSA device is communicated with the entrance of compressor, and the outlet of compressor is communicated with the entrance of point flow container;
Described oily absorptive unit comprises deoxidation demethanizing tower, desorption tower, absorption tower, naphtha scrubber, the entrance of described deoxidation demethanizing tower is by the bottom compressed condensate outlet of pipeline and described point of flow container, the liquid-phase outlet of described deoxidation demethanizer bottom is communicated with by the entrance of pipeline with described desorption tower, the pneumatic outlet of described deoxidation demethanizer overhead, the pneumatic outlet of described separatory tank top is connected to the gas inlet on described absorption tower respectively by pipeline, liquid-phase outlet bottom described desorption tower is connected to the liquid inlet on absorption tower by pump tubing length, the pneumatic outlet at top, described absorption tower is communicated with the entrance of naphtha scrubber by pipeline, liquid-phase outlet bottom described absorption tower is communicated with by the entrance of pump tubing length with described deoxidation demethanizing tower.
The fuel gas of the top exit of described naphtha scrubber goes pipe network to be communicated with, and the rich petroleum naphtha of the outlet at bottom of described naphtha scrubber removes cracking of ethylene.
Pump tubing length bottom described desorption tower is drawn a branch road and remove cracking of ethylene for C4 product.
The top exit of described desorption tower is connected with return tank by pipeline, and desorption tower is returned by trim the top of column pump delivery in the bottom of return tank, and the top of return tank is provided with pipeline makes ethylene-rich gas remove cracking of ethylene.
Also comprise lime set pump, described lime set pump is located on the pipeline of described separatory pot bottom outlet.
Group PSA adsorber comprises 10 PSA adsorbers, the working process of each PSA adsorber comprises absorption, all pressure drop, inverse put by process sequence, finds time, all voltage rises, fill eventually, 10 PSA adsorbers alternately enter absorbing process, and the time in office has 4 PSA adsorbers to be in absorbing process, other 6 PSA adsorbers are then in equal pressure drop, inverse put respectively, find time, all voltage rises, fill technique eventually.
Reclaim a method of C2 in oil refinery dry gas, comprise the following steps:
1st step, raw material dry gas is through one section of PSA concentrate, by adsorber, C2 and the C2+ component in raw material dry gas is adsorbed, and the components such as the hydrogen not easily adsorbed, methane, nitrogen are discharged from adsorber top, then by inverse put, vacuumize C2 and the C2+ component desorb made by adsorbing, obtain concentrate stripping gas;
2nd step, the concentrate stripping gas 1st step obtained is through the laggard row cooling of overdraft and separatory, the pressure of compression process is 2-5MPa, and compressed gas enters separatory tank and carries out separatory after being cooled to 40 DEG C, is the fuel non-condensable gas collected from separatory tank top and the compressed condensate collected from pot bottom respectively;
3rd step, the pneumatic outlet of deoxidation demethanizer overhead, the bottom that the pneumatic outlet of described separatory tank top is connected to described absorption tower respectively by pipeline absorb, C4 absorption agent is utilized to absorb the components such as C2, C3 in gas in absorption tower, obtain the absorption agent of rich C4, the fuel gas such as non-absorbent methane, hydrogen flow out from the tower top on absorption tower;
4th step, the compressed condensate that the absorption agent of the rich C4 the 3rd step obtained and the 2nd step obtain is sent into deoxidation demethanizing tower and is carried out air lift, oxygen contained by making in rich C4 absorption agent and compressed condensate, methane are removed, afterwards the absorption agent at the bottom of tower is sent into desorption tower, the gas stripping gas containing C2, C3 of tower top is repeated the 3rd step;
5th step, absorption agent at the bottom of 4th step tower is sent into desorption tower, heated by low-pressure steam at the bottom of the tower of desorption tower, C2, C3 component in absorption agent is resolved, the overhead product of desorption tower enters return tank and carries out separatory after being cooled to 40 DEG C, the discharging of return tank gas phase is rich C2 gas product, and return tank liquid phase returns desorption tower tower top through trim the top of column pump delivery;
6th step, 3rd step is obtained the fuel gas such as non-absorbent methane, hydrogen flowed out from the tower top on absorption tower, enter naphtha scrubber bottom, contact with the petroleum naphtha entered from tower top is reverse, make the lighter hydrocarbons such as C3, the C4 carried in fuel gas absorb by petroleum naphtha.Tower top fuel gas removes fuel gas pipe network, and at the bottom of tower, rich petroleum naphtha goes ethylene unit to do cracking material.
In 5th step, C4 absorption agent at the bottom of the tower of desorption tower through pump boosting, heat exchange, be cooled to 40 DEG C after be divided into two strands, one is the C4 product carrying device that flow is less, and another strand is that absorption agent is made on the top, absorption tower that the 3rd step delivered to by circulation C4 absorption agent that flow is larger.
The invention has the beneficial effects as follows: first utilize one of less energy-consumption section of PSA to carry out preliminary concentrate to raw material dry gas, the absorption and desorption method of recycling high-recovery, high product purities is purified further to PSA concentrate gas, the gas feed of absorptive unit, absorption agent and trim the top of column temperature are 40 DEG C, adopt recirculated cooling water can reach this cooling condensation temperature, do not need refrigeration equipment.Adopt compressed condensate as absorption agent, do not need to introduce C4 absorption agent from other device.
The present invention is under the prerequisite ensureing high-recovery, high product purities (the C2 rate of recovery 93%, gas product methane content 3% ~ 5% (V)), and energy consumption index is lower than shallow cold oil method by 20 ~ 30%.
Accompanying drawing explanation
According to drawings and embodiments the present invention is described in further detail below.
Fig. 1 is structure iron of the present invention.
Fig. 2 is the structure iron of one section of PSA device.
In figure:
1, one section of PSA device; 2, compressor; 3, flow container is divided; 4, deoxidation demethanizing tower; 5, desorption tower; 6, absorption tower; 7, naphtha scrubber; 8, return tank; 9, trim the top of column pump; 10, lime set pump; 11, unstripped gas surge tank; 12, cooling driers; 13, PSA adsorber; 14, vacuum pump; 15, inverse put gas surge tank; 16, concentrate gas surge tank.
Embodiment
As shown in Figure 1-2, in the present embodiment, a kind of device reclaiming C2 in oil refinery dry gas, comprises PSA unit, compressed element and oily absorptive unit;
Described PSA unit comprises one section of PSA device 1, comprise unstripped gas surge tank 11, cooling driers 12, one group of PSA adsorber 13, vacuum pump 14, inverse put gas surge tank 15, concentrate gas surge tank 16, unstripped gas surge tank 11 is connected by the entrance of pipeline with cooling driers 12, the outlet of cooling driers 12 is connected with PSA adsorber 13, the outlet of described PSA adsorber 13 is connected with concentrate gas surge tank 16 by vacuum pump 14, the inverse put gas branch road of described PSA adsorber 13 is connected with inverse put gas surge tank 15 and concentrate gas surge tank 16 respectively, the outlet of described inverse put gas surge tank 15 is connected with concentrate gas surge tank 16, the outlet of concentrate gas surge tank 16 is connected with compressor,
Described compressed element comprises compressor 2, point flow container 3, and the entrance of wherein said one section of PSA device 1 is communicated with raw material dry gas, and the outlet of described one section of PSA device 1 is communicated with the entrance of compressor 2, and the outlet of compressor 2 is communicated with the entrance of point flow container 3;
Described oily absorptive unit comprises deoxidation demethanizing tower 4, desorption tower 5, absorption tower 6, naphtha scrubber 7, the entrance of described deoxidation demethanizing tower 4 is communicated with by the outlet at bottom of pipeline with described point of flow container 3, liquid-phase outlet bottom described deoxidation demethanizing tower 4 is communicated with by the entrance of pipeline with described desorption tower 5, the pneumatic outlet at described deoxidation demethanizing tower 4 top, the pneumatic outlet at described point of flow container 3 top is connected to the gas inlet on described absorption tower 6 respectively by pipeline, liquid-phase outlet bottom described desorption tower 5 is connected to the liquid inlet on absorption tower 6 by pump tubing length, the pneumatic outlet at top, described absorption tower 6 is communicated with by the entrance of pipeline with naphtha scrubber 7, liquid-phase outlet bottom described absorption tower 6 is communicated with by the entrance of pump tubing length with described deoxidation demethanizing tower 4.
The fuel gas of the top exit of described naphtha scrubber 7 goes pipe network to be communicated with, and the rich petroleum naphtha of the outlet at bottom of described naphtha scrubber 7 removes cracking of ethylene.
Pump tubing length bottom described desorption tower 5 is drawn a branch road and remove cracking of ethylene for C4 product.
The top exit of described desorption tower 5 is connected with return tank 8 by pipeline, and the bottom of return tank 8 is transmitted back to desorption tower 5 by trim the top of column pump 9, and the top of return tank is provided with pipeline makes ethylene-rich gas remove cracking of ethylene.
Also comprise lime set pump 10, described lime set pump is located on the pipeline of described separatory pot bottom outlet.
One group of PSA adsorber comprises 10 PSA adsorbers, the working process of each PSA adsorber comprises absorption, all pressure drop, inverse put by process sequence, finds time, all voltage rises, fill eventually, 10 PSA adsorbers alternately enter absorbing process, and the time in office has 4 PSA adsorbers to be in absorbing process, other 6 PSA adsorbers are then in equal pressure drop, inverse put respectively, find time, all voltage rises, fill technique eventually.
From raw material dry gas out-of-bounds, carry out cushioning and after separatory, entering cooling driers and remove the saturation water and a small amount of heavy hydrocarbon that contain in raw material dry gas through unstripped gas surge tank.Cold dry after unstripped gas enter the PSA absorber bottoms that 4 are in adsorbed state, in gas, most more than C2 active princlple is by sorbent material selective adsorption, and weakly stable component H2, N2, CH4 etc. are then sent out-of-bounds from adsorber top as absorption waste gas by adsorber bed.All the other 6 towers carry out the operation of other step (equal pressure drop, inverse put, find time, all voltage rises, to fill eventually) respectively, and 10 towers replace blocked operation, and the switching of each step of adsorber has been automatically switched by sequencing valve.Absorption more than C2 active principle (i.e. concentrate gas) on the sorbent discharges adsorber in inverse put and evacuation step.Inverse put gas (concentrate gas) part that pressure is high that inverse put step is discharged is introduced into inverse put gas surge tank, concentrate gas surge tank is sent into after buffering decompression, the part that pressure is low directly enters concentrate gas surge tank, and concentrate gas delivers to the compressor of compressed element after buffering voltage stabilizing.The finding time of PSA device is completed by vacuum pump, and the draws air (concentrate gas) of extraction, after vacuum pump aftercooler is cooled to normal temperature, also enters concentrate gas surge tank.
Reclaim a method of C2 in oil refinery dry gas, comprise the following steps:
1st step, raw material dry gas is through one section of PSA concentrate, by adsorber, C2 and the C2+ component in raw material dry gas is adsorbed, and the components such as the hydrogen not easily adsorbed, methane, nitrogen are discharged from adsorber top, then by inverse put, vacuumize C2 and the C2+ component desorb made by adsorbing, obtain concentrate stripping gas;
2nd step, the concentrate stripping gas 1st step obtained is through the laggard row cooling of overdraft and separatory, the pressure of compression process is 2-5MPa, and compressed gas enters separatory tank and carries out separatory after being cooled to 40 DEG C, is the fuel non-condensable gas collected from separatory tank top and the compressed condensate collected from pot bottom respectively;
3rd step, the pneumatic outlet of deoxidation demethanizer overhead, the bottom that the pneumatic outlet of described separatory tank top is connected to described absorption tower respectively by pipeline absorb, C4 absorption agent is utilized to absorb the components such as C2, C3 in gas in absorption tower, obtain the absorption agent of rich C4, the fuel gas such as non-absorbent methane, hydrogen flow out from the tower top on absorption tower;
4th step, the compressed condensate that the absorption agent of the rich C4 the 3rd step obtained and the 2nd step obtain is sent into deoxidation demethanizing tower and is carried out air lift, oxygen contained by making in rich C4 absorption agent and compressed condensate, methane are removed, afterwards the absorption agent at the bottom of tower is sent into desorption tower, the gas stripping gas containing C2, C3 of tower top is repeated the 3rd step;
5th step, absorption agent at the bottom of 4th step tower is sent into desorption tower, heated by low-pressure steam at the bottom of the tower of desorption tower, C2, C3 component in absorption agent is resolved, the overhead product of desorption tower enters return tank and carries out separatory after being cooled to 40 DEG C, the discharging of return tank gas phase is rich C2 gas product, and return tank liquid phase returns desorption tower tower top through trim the top of column pump delivery.
6th step, 3rd step is obtained the fuel gas such as non-absorbent methane, hydrogen flowed out from the tower top on absorption tower, enter naphtha scrubber bottom, contact with the petroleum naphtha entered from tower top is reverse, make the lighter hydrocarbons such as C3, the C4 carried in fuel gas absorb by petroleum naphtha.Tower top fuel gas removes fuel gas pipe network, and at the bottom of tower, rich petroleum naphtha goes ethylene unit to do cracking material.
In 5th step, C4 absorption agent at the bottom of the tower of desorption tower through pump boosting, heat exchange, be cooled to 40 DEG C after be divided into two strands, one is the C4 product carrying device that flow is less, and another strand is that absorption agent is made on the top, absorption tower that the 3rd step delivered to by circulation C4 absorption agent that flow is larger.
Claims (8)
1. reclaim a device of C2 in oil refinery dry gas, comprise PSA unit, compressed element and oily absorptive unit; It is characterized in that,
Described PSA unit comprises one section of PSA device, comprise unstripped gas surge tank, cooling driers, one group of PSA adsorber, vacuum pump, inverse put gas surge tank, concentrate gas surge tank, unstripped gas surge tank is connected with the entrance of cooling driers by pipeline, the outlet of cooling driers is connected with PSA adsorber, the outlet of described PSA adsorber is connected with concentrate gas surge tank by vacuum pump, the inverse put gas branch road of described PSA adsorber is connected with inverse put gas surge tank and concentrate gas surge tank respectively, the outlet of described inverse put gas surge tank is connected with concentrate gas surge tank, the outlet of concentrate gas surge tank is connected with compressor,
Described compressed element comprises compressor, point flow container, and the entrance of wherein said one section of PSA device is communicated with raw material dry gas, and the described outlet of one section of PSA device is communicated with the entrance of compressor, and the outlet of compressor is communicated with the entrance of point flow container;
Described oily absorptive unit comprises deoxidation demethanizing tower, desorption tower, absorption tower, naphtha scrubber, the entrance of described deoxidation demethanizing tower is by the bottom compressed condensate outlet of pipeline and described point of flow container, the liquid-phase outlet of described deoxidation demethanizer bottom is communicated with by the entrance of pipeline with described desorption tower, the pneumatic outlet of described deoxidation demethanizer overhead, the pneumatic outlet of described separatory tank top is connected to the gas inlet on described absorption tower respectively by pipeline, liquid-phase outlet bottom described desorption tower is connected to the liquid inlet on absorption tower by pump tubing length, the pneumatic outlet at top, described absorption tower is communicated with the entrance of naphtha scrubber by pipeline, liquid-phase outlet bottom described absorption tower is communicated with by the entrance of pump tubing length with described deoxidation demethanizing tower.
2. a kind of device reclaiming C2 in oil refinery dry gas as claimed in claim 1, is characterized in that, the fuel gas of the top exit of described naphtha scrubber goes pipe network to be communicated with, and the rich petroleum naphtha of the outlet at bottom of described naphtha scrubber removes cracking of ethylene.
3. a kind of device reclaiming C2 in oil refinery dry gas as claimed in claim 1, is characterized in that, the pump tubing length bottom described desorption tower is drawn a branch road and removes cracking of ethylene for C4 product.
4. a kind of device reclaiming C2 in oil refinery dry gas as claimed in claim 1, it is characterized in that, the top exit of described desorption tower is connected with return tank by pipeline, and desorption tower is returned by trim the top of column pump delivery in the bottom of return tank, and the top of return tank is provided with pipeline makes ethylene-rich gas remove cracking of ethylene.
5. a kind of device reclaiming C2 in oil refinery dry gas as claimed in claim 1, is characterized in that, also comprise lime set pump, and described lime set pump is located on the pipeline of described separatory pot bottom outlet.
6. a kind of device reclaiming C2 in oil refinery dry gas as claimed in claim 1, it is characterized in that, one group of PSA adsorber comprises 10 PSA adsorbers, the working process of each PSA adsorber comprises absorption, all pressure drop, inverse put by process sequence, finds time, all voltage rises, fill eventually, 10 PSA adsorbers alternately enter absorbing process, and the time in office has 4 PSA adsorbers to be in absorbing process, other 6 PSA adsorbers are then in equal pressure drop, inverse put respectively, find time, all voltage rises, fill technique eventually.
7. reclaim a method of C2 in oil refinery dry gas, comprise the following steps:
1st step, raw material dry gas is through one section of PSA concentrate, by adsorber, C2 and the C2+ component in raw material dry gas is adsorbed, and the components such as the hydrogen not easily adsorbed, methane, nitrogen are discharged from adsorber top, then by inverse put, vacuumize C2 and the C2+ component desorb made by adsorbing, obtain concentrate stripping gas;
2nd step, the concentrate stripping gas 1st step obtained is through the laggard row cooling of overdraft and separatory, the pressure of compression process is 2-5MPa, and compressed gas enters separatory tank and carries out separatory after being cooled to 40 DEG C, is the fuel non-condensable gas collected from separatory tank top and the compressed condensate collected from pot bottom respectively;
3rd step, the pneumatic outlet of deoxidation demethanizer overhead, the bottom that the pneumatic outlet of described separatory tank top is connected to described absorption tower respectively by pipeline absorb, C4 absorption agent is utilized to absorb the components such as C2, C3 in gas in absorption tower, obtain the absorption agent of rich C4, the fuel gas such as non-absorbent methane, hydrogen flow out from the tower top on absorption tower;
4th step, the compressed condensate that the absorption agent of the rich C4 the 3rd step obtained and the 2nd step obtain is sent into deoxidation demethanizing tower and is carried out air lift, oxygen contained by making in rich C4 absorption agent and compressed condensate, methane are removed, afterwards the absorption agent at the bottom of tower is sent into desorption tower, the gas stripping gas containing C2, C3 of tower top is repeated the 3rd step;
5th step, absorption agent at the bottom of 4th step tower is sent into desorption tower, heated by low-pressure steam at the bottom of the tower of desorption tower, C2, C3 component in absorption agent is resolved, the overhead product of desorption tower enters return tank and carries out separatory after being cooled to 40 DEG C, the discharging of return tank gas phase is rich C2 gas product, and return tank liquid phase returns desorption tower tower top through trim the top of column pump delivery;
6th step, 3rd step is obtained the fuel gas such as non-absorbent methane, hydrogen flowed out from the tower top on absorption tower, enter naphtha scrubber bottom, contact with the petroleum naphtha entered from tower top is reverse, make the lighter hydrocarbons such as C3, the C4 carried in fuel gas absorb by petroleum naphtha.Tower top fuel gas removes fuel gas pipe network, and at the bottom of tower, rich petroleum naphtha goes ethylene unit to do cracking material.
8. a kind of method reclaiming C2 in oil refinery dry gas as claimed in claim 7, it is characterized in that, in 5th step, C4 absorption agent at the bottom of the tower of desorption tower through pump boosting, heat exchange, be cooled to 40 DEG C after be divided into two strands, one is the C4 product carrying device that flow is less, and another strand is that absorption agent is made on the top, absorption tower that the 3rd step delivered to by circulation C4 absorption agent that flow is larger.
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| CN107961644A (en) * | 2016-10-20 | 2018-04-27 | 中国石油化工股份有限公司 | A kind of system and method for harmless treatment broken coal low-temperature methanol washing tail-gas |
| CN109248535A (en) * | 2018-09-04 | 2019-01-22 | 海南凯美特气体有限公司 | A kind of device for reducing the fuel gas compressor gas-liquid separator condensed oil and being formed |
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| CN103588604A (en) * | 2012-08-15 | 2014-02-19 | 中国石油化工集团公司 | Recovering system and method of C2 in refinery dry gas by compound adsorption method |
| CN104031682A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for separating hydrogen and ethylene from refinery dry gas by shallow condensing adsorption-absorption |
| CN204607933U (en) * | 2015-01-09 | 2015-09-02 | 北京燕山玉龙石化工程有限公司 | A kind of device reclaiming C2 in oil refinery dry gas |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103588604A (en) * | 2012-08-15 | 2014-02-19 | 中国石油化工集团公司 | Recovering system and method of C2 in refinery dry gas by compound adsorption method |
| CN104031682A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for separating hydrogen and ethylene from refinery dry gas by shallow condensing adsorption-absorption |
| CN204607933U (en) * | 2015-01-09 | 2015-09-02 | 北京燕山玉龙石化工程有限公司 | A kind of device reclaiming C2 in oil refinery dry gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107961644A (en) * | 2016-10-20 | 2018-04-27 | 中国石油化工股份有限公司 | A kind of system and method for harmless treatment broken coal low-temperature methanol washing tail-gas |
| CN109248535A (en) * | 2018-09-04 | 2019-01-22 | 海南凯美特气体有限公司 | A kind of device for reducing the fuel gas compressor gas-liquid separator condensed oil and being formed |
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| CN104830371B (en) | 2017-04-05 |
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