CN204973834U - Device of high concentration acetylene hydrogenation system ethylene - Google Patents
Device of high concentration acetylene hydrogenation system ethylene Download PDFInfo
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- CN204973834U CN204973834U CN201520595612.XU CN201520595612U CN204973834U CN 204973834 U CN204973834 U CN 204973834U CN 201520595612 U CN201520595612 U CN 201520595612U CN 204973834 U CN204973834 U CN 204973834U
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Abstract
The utility model relates to a device of acetylene hydrogenation system ethylene, the device includes the reactor urceolus and is located an inside reactor section of thick bamboo and the annular distributor of reactor urceolus, the top and the bottom of a reactor section of thick bamboo are open structure, evenly distributed trompil on its lateral wall, the annular distributor is located under the reactor section of thick bamboo, the annular is the evenly distributed hole of upwards exhausting on the distributor, reactor urceolus top is equipped with hydrogen import, acetylene gas import and the export of product gas, the hydrogen import is connected to through gas pipeline the annular distributor, the acetylene gas import lets in in the reactor section of thick bamboo. The device provided by the utility model can realize that acetylene and hydrogen part the feeding and the self -loopa is carried out to the liquid phase under the effect of density contrast to the efficiency of acetylene hydrogenation system ethylene has been improved.
Description
Technical field
The utility model belongs to gas treatment processing method technical field, particularly a kind of device of high concentration producing ethylene with acetylene hydrogenation.
Background technology
Along with petroleum resources are day by day exhausted, Development of Coal chemical industry is the significant process that the chemical process of raw material becomes petroleum replacing chemical industry route, obtains extensive concern, and obtains fast development.
In coal chemical technology, be that raw material produces acetylene by calcium carbide technique, extensive use with coal, take acetylene as raw material, under selective hydrocatalyst effect, by Hydrogenation for ethylene product, Coal Chemical Industry Route can be expanded further.And the downstream product polyvinyl chloride (PVC) that acetylene was main in the last few years supply exceed demand, PVC industrial profit is not high, is badly in need of expanding acetylene downstream product industrial chain; Ethene is most important basic material in petrochemical industry, is called as " mother of petrochemical industry ".Be widely used in plastics, lubricating oil, polymer and some intermediates, pass through cracking primarily of oil or low-carbon alkanes at present.Ethene downstream product is as ethylene glycol, and butanediol, acrylic acid, polyvinyl alcohol etc. also have good economic worth.Therefore, the novel technique of exploitation producing ethylene with acetylene hydrogenation can provide a kind of new raw material to originate for ethylene industry, and reduces ethene to the degree of dependence of petroleum resources and production cost of ethylene, has broad application prospects.
Prior art discloses and adopt fixed-bed catalytic hydrogenation technique, because alkynes is hydrogenated to strong exothermal reaction, fixed bed device moves heat difficulty, and a large amount of reaction heat can make palladium catalyst carbon distribution inactivation.Again because its activity is very high, when reacting, acetylene polymerization generates green oil, covers catalyst surface and causes rapid catalyst deactivation.
Although acetylene selective hydrogenation is the current focus of attention, but its research contents is mainly used in the acetylene (0.01-5 volume %) that removing cracking petroleum hydrocarbon prepares trace in ethylene process process, for the special catalysis selective hydrogenation ethene then rare exploration being raw material with high concentration acetylene, corresponding industrialization large-scale application has no report especially.
Utility model content
The purpose of this utility model is the defect overcoming prior art, provides the device being applicable to " solution-air " haptoreaction, being specially adapted to preparing ethylene by selective hydrogenation of acetylene.
The device that the utility model provides comprises reactor urceolus and is positioned at reactor inner core and the circle distributor of described reactor outer barrel.
Top and the bottom of described reactor inner core are Open architecture, and its sidewall is uniformly distributed perforate;
Described circle distributor is positioned at immediately below described reactor inner core, it is uniformly distributed to upper air-vent;
Described reactor urceolus top is provided with hydrogen inlet, acetylene gas import and product gas outlet; Described hydrogen inlet is connected to circle distributor by gas pipeline; Described acetylene gas import passes in described reactor inner core.
Preferably, described reactor urceolus, reactor inner core and circle distributor are coaxially arranged; Described reactor urceolus and reactor inner core are cylindric.
The utility model fully can mix with rational ratio with acetylene in order to ensure hydrogen, thus realizes highly effective reaction, is optimized the dimension scale of described reactor inner core, reactor inner core and circle distributor.
Concrete, the horizontal cross-section diameter ratio of described reactor inner core and reactor urceolus is 0.4 ~ 0.8:1, is preferably 0.6:1.The outer annular diameter of described circle distributor and the horizontal cross-section diameter ratio of reactor urceolus are 0.7 ~ 0.9:1, are preferably 0.7:1.In order to realize the liquid flow that density based difference is formed, guarantee that the high density liquid phase absorbing acetylene can enter reactor urceolus from reactor inner core, the distance of described circle distributor and reactor inner core is 10 ~ 50mm, is preferably 15mm.Distance bottom described circle distributor and reactor urceolus is 50 ~ 400mm, is preferably 80mm.
The utility model is in order to ensure the reasonable layout of acetylene gas in reactor inner core region, and the distance bottom the bottom of preferred described acetylene gas import and reactor inner core is 5 ~ 20mm, more preferably 5mm.
The utility model, the sidewall of described reactor inner core is provided with the perforate that aperture is 5 ~ 10mm, is preferably the opening of aperture 6mm.The described perforate gross area account for reactor inner cylindrical surface long-pending 0.1 ~ 10%.Described perforate is uniformly distributed in 1/3rd and 2/3rds places of reactor inner core height, is more conducive to ethene desorption and carries out product-collecting.
The utility model is in order to realize hydrogen gas to distribute with the specific ratio uniform of acetylene, described circle distributor is preferably one pipe circuit, which is provided with to upper air-vent, the described diameter to upper air-vent is 0.002 ~ 0.1 with the ratio of the bore of described one pipe circuit, and this ratio is preferably 0.08.The even upper surface that must be distributed in described one pipe circuit of described upwards vent port openings, to ensure from the hydrogen gas stream direction of wherein discharging upwards, to make hydrogen react with acetylene fast and efficiently.The described diameter to upper air-vent specifically can be 0.02 ~ 3mm.Discharge from circle distributor with rational ratio and speed to realize hydrogen gas, preferably adjacent two is 0.03 ~ 1 to the distance between upper air-vent and the ratio of the bore with described one pipe circuit, be preferably 0.15, described adjacent two is distance between finger-hole center to the distance between upper air-vent.
The utility model is based on above structure, acetylene and hydrogen separately can be entered reactor, acetylene gas enters reactor inner core district through acetylene air inlet bottom inner core district, hydrogen enters reactor urceolus district through hydrogen inlet from circle distributor, after reaction, product gas outlet is by gas product ejector.
The utility model, by carrying out preferably to the proportionate relationship of parts each in device and relative position, can realize gas phase and the reasonable layout of liquid phase in device, thus reaction more fully, is efficiently carried out.
Described device can also comprise the heating jacket being positioned at the outer drum outer wall of reactor.Described heating jacket can as the thermal source of producing ethylene with acetylene hydrogenation reaction.
The device adopting the utility model to provide efficiently can carry out " gas-liquid phase " two phase reaction of producing ethylene with acetylene hydrogenation.In practical operation, hydrogen and acetylene are respectively from hydrogen inlet and acetylene air inlet access equipment.Liquid phase liquid level is in a device higher than the top of reactor inner core, and it is 4 ~ 6:1 that described liquid level is preferably with the horizontal cross-section diameter ratio of reactor urceolus, is preferably 5:1.
The device adopting the utility model to provide carries out producing ethylene with acetylene hydrogenation reflection, can specifically comprise the following steps:
Get hydrogen and acetylene respectively; Described hydrogen is from hydrogen inlet, the bottom entering reactor urceolus through circle distributor; Described acetylene passes in reactor inner core by acetylene air inlet; Within the unit interval, the charge volume of hydrogen and acetylene is than being 4:1;
The liquid phase of having dissolved acetylene in reactor inner core enters reactor urceolus from the hole reactor inner core sidewall and its open bottom due to fluid density difference, simultaneously, liquid phase in reactor urceolus enters reactor inner core due to liquid level difference from open top, forms the self-loopa of liquid phase in device inside;
Under described self-loopa state, be dissolved in hydrogen in liquid phase and acetylene 150 DEG C, fully react under the effect of liquid-phase catalyst, the product of generation is discharged by product gas outlet.
The device adopting the utility model to provide is implemented to carry out producing ethylene with acetylene hydrogenation reflection, acetylene can be realized and hydrogen separates charging, acetylene enters reactor by acetylene air inlet, hydrogen enters reactor by hydrogen inlet, and hydrogen inlet is connected with the circle distributor being in bottom of device reactor urceolus, acetylene air inlet is in reactor inner core district, make to cause certain density contrast at the bottom reactor inner core of reactor and urceolus district like this, the density of inner core district solution is greater than the density of urceolus district solution, the solution having dissolved acetylene in inner core enters urceolus district from the hole inner tube wall and reactor lower part and contacts with hydrogen, under the effect of liquid-phase catalyst, carry out reaction generate ethene, ethene and unreacted hydrogen are discharged by product gas outlet.On reactor top, because solution page height has exceeded inner core height, therefore the solution on top is circulated to inner core district by urceolus district, reach the self-loopa of solution in reactor, thus make the Contact of hydrogen, acetylene and liquid-phase catalyst more fully, react more abundant, the efficiency of raising producing ethylene with acetylene hydrogenation.
The utility model can realize following beneficial effect: the device that the utility model provides can make traditional " gas-solid " two " gas-liquid-solid " three haptoreactions become " solution-air " haptoreaction; Traditional solid catalyst is become liquid-phase catalyst, avoids generating green oil to the covering of catalyst active center; Improve the selective of producing ethylene with acetylene hydrogenation, add the yield of ethene in gas product; Acetylene and hydrogen is adopted to separate charging, acetylene enters inner core district, hydrogen enters urceolus district, thus avoid hydrogen and acetylene mixes in advance, in this reactor selective hydrogenation of acetylene liquid solution system under the effect of density contrast by urceolus to inner core self-loopa, thus improve the efficiency of producing ethylene with acetylene hydrogenation.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of device described in the utility model; In figure: 1, heating jacket, 2, reactor urceolus, 3, reactor inner core, 4, circle distributor, 5, hydrogen inlet, 6, acetylene gas import, 7, product gas outlet.
Detailed description of the invention
Following examples for illustration of the utility model, but are not used for limiting scope of the present utility model.
Embodiment 1
The device (as shown in Figure 1) of producing ethylene with acetylene hydrogenation, described device comprises reactor urceolus 2 and is positioned at reactor inner core 3 and the circle distributor 4 of described reactor urceolus 2 inside; Also comprise the heating jacket 1 covering described reactor urceolus 2 outer wall;
Described reactor urceolus 2 is cylindric with reactor inner core 3; Top and the bottom of described reactor inner core 3 are Open architecture; Described reactor urceolus 2, reactor inner core 3 and circle distributor 4 are coaxially arranged;
The horizontal cross-section diameter of described reactor inner core 3 is 138mm, and the horizontal cross-section diameter of described reactor urceolus 2 is 200mm, and the outer annular diameter of described circle distributor 4 is 150mm;
Described circle distributor 4 is 15mm with the distance of reactor inner core 3;
Described circle distributor 4 is 80mm with the distance bottom reactor urceolus 2;
The sidewall of described reactor inner core 3 there is aperture be the perforate of 6mm; The gross area of described perforate account for inner cylindrical surface long-pending 2%; Described perforate is uniformly distributed in 1/3rd and 2/3rds places of reactor inner core 2 height;
Described circle distributor 4 is positioned at immediately below reactor inner core 3; Described circle distributor be provided with diameter 1mm to upper air-vent; The described diameter to upper air-vent is 0.08 with the ratio of the bore of described one pipe circuit, and adjacent two is 0.15 to the distance between upper air-vent and the ratio of the bore of described one pipe circuit;
Described reactor urceolus 2 top is provided with hydrogen inlet 5, acetylene gas import 6 and product gas outlet 7; Described hydrogen inlet 5 is connected to circle distributor 4 by gas pipeline; Described acetylene gas import 6 passes in described reactor inner core 3, and the distance bottom its bottom and reactor inner core 3 is 5mm; Described product gas outlet 7 is by gas product ejector.
Embodiment 2
The device adopting embodiment 1 to provide, carries out high concentration selective hydrogenation of acetylene " solution-air " two-phase haptoreaction;
Described method adopts high-purity acetylene and hydrogen as reaction raw materials, acetylene and hydrogen separate charging, acetylene enters reactor by acetylene air inlet 6, hydrogen enters reactor by hydrogen inlet 5, the ratio of the hydrogen and acetylene that enter reactor is 4:1, certain density contrast is caused like this at the bottom reactor inner core of reactor and urceolus district, the density of inner core district solution is greater than the density of urceolus district solution, therefore the solution having dissolved acetylene in inner core enters urceolus district from the hole inner tube wall and reactor lower part and contacts with hydrogen, under the effect of liquid-phase catalyst, carry out reaction generate ethene, ethene and unreacted hydrogen are discharged by 7 product gas outlet, on reactor top, liquid level is higher than reactor inner core, and liquid level and reactor outer barrel diameter are than being 5:1, and therefore the solution on top is circulated to inner core district by urceolus district, reaches the self-loopa of solution in reactor, by heating jacket, the temperature controlling reactor is 150 DEG C.
Although above with general explanation, detailed description of the invention and test, done detailed description to the utility model, on the utility model basis, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements on the basis of not departing from the utility model spirit, all belong to the scope that the utility model is claimed.
Claims (10)
1. a device for producing ethylene with acetylene hydrogenation, is characterized in that, described device comprises reactor urceolus and is positioned at reactor inner core and the circle distributor of described reactor outer barrel;
Top and the bottom of described reactor inner core are Open architecture, and its sidewall is uniformly distributed perforate;
Described circle distributor is positioned at immediately below described reactor inner core, described circle distributor is uniformly distributed to upper air-vent;
Described reactor urceolus top is provided with hydrogen inlet, acetylene gas import and product gas outlet; Described hydrogen inlet is connected to described circle distributor by gas pipeline; Described acetylene gas import passes in described reactor inner core.
2. device according to claim 1, is characterized in that, described reactor urceolus, reactor inner core and circle distributor are coaxially arranged; Described reactor urceolus and reactor inner core are cylindric.
3. device according to claim 2, is characterized in that, the diameter ratio of described reactor inner core and reactor urceolus is 0.4 ~ 0.8:1;
The outer annular diameter of described circle distributor and the horizontal cross-section diameter ratio of reactor urceolus are 0.7 ~ 0.9:1.
4. device according to claim 1, is characterized in that, the distance bottom described circle distributor and reactor inner core is 10 ~ 50mm, is 50 ~ 400mm with the distance bottom reactor urceolus;
Distance bottom the bottom of described acetylene gas import and reactor inner core is 5 ~ 20mm.
5. the device according to Claims 1 to 4 any one, is characterized in that, the open pore size on the sidewall of described reactor inner core is 5 ~ 10mm; The gross area of described perforate account for reactor inner cylindrical surface long-pending 0.1 ~ 10%.
6. device according to claim 5, is characterized in that, described perforate is uniformly distributed in 1/3rd and 2/3rds places of reactor inner core height.
7. the device according to Claims 1 to 4 any one, is characterized in that, described circle distributor is one pipe circuit, and the described diameter to upper air-vent is 0.002 ~ 0.1 with the ratio of the bore of described one pipe circuit.
8. device according to claim 7, is characterized in that, the described diameter to upper air-vent is 0.02 ~ 3mm.
9. device according to claim 7, is characterized in that, adjacent two is 0.03 ~ 1 to the distance between upper air-vent and the ratio of the bore of described one pipe circuit.
10. device according to claim 1, is characterized in that, the outer wall of described reactor urceolus covers heating jacket.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520595612.XU CN204973834U (en) | 2015-08-07 | 2015-08-07 | Device of high concentration acetylene hydrogenation system ethylene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520595612.XU CN204973834U (en) | 2015-08-07 | 2015-08-07 | Device of high concentration acetylene hydrogenation system ethylene |
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| CN204973834U true CN204973834U (en) | 2016-01-20 |
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| CN201520595612.XU Active CN204973834U (en) | 2015-08-07 | 2015-08-07 | Device of high concentration acetylene hydrogenation system ethylene |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105061131A (en) * | 2015-08-07 | 2015-11-18 | 北京神雾环境能源科技集团股份有限公司 | Method and device for high-concentration acetylene hydrogenated ethylene production |
| CN108018070A (en) * | 2016-10-28 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of heavy oil feedstock fixed bed hydrogenation system |
-
2015
- 2015-08-07 CN CN201520595612.XU patent/CN204973834U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105061131A (en) * | 2015-08-07 | 2015-11-18 | 北京神雾环境能源科技集团股份有限公司 | Method and device for high-concentration acetylene hydrogenated ethylene production |
| CN105061131B (en) * | 2015-08-07 | 2017-06-09 | 北京华福工程有限公司 | A kind of method and device of high concentration producing ethylene with acetylene hydrogenation |
| CN108018070A (en) * | 2016-10-28 | 2018-05-11 | 中国石油化工股份有限公司 | A kind of heavy oil feedstock fixed bed hydrogenation system |
| CN108018070B (en) * | 2016-10-28 | 2020-07-28 | 中国石油化工股份有限公司 | Heavy oil raw materials fixed bed hydrogenation system |
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| C14 | Grant of patent or utility model | ||
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| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20160930 Address after: 102200 Beijing City, Changping District science and Technology Park Fukang Road No. 18 Patentee after: Beijing Huafu Engineering Co., Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Patentee before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200526 Address after: 100121 1105, floor 1, building 1, yard 18, Shuangqiao East Road, Chaoyang District, Beijing Patentee after: Beijing Jintai Chengrui Technology Development Co., Ltd Address before: 102200 No. 18 Fukang Road, Changping District science and Technology Park, Beijing Patentee before: BEIJING HUAFU ENGINEERING Co.,Ltd. |