CN204111689U - Selective hydrogenation device - Google Patents
Selective hydrogenation device Download PDFInfo
- Publication number
- CN204111689U CN204111689U CN201420469312.2U CN201420469312U CN204111689U CN 204111689 U CN204111689 U CN 204111689U CN 201420469312 U CN201420469312 U CN 201420469312U CN 204111689 U CN204111689 U CN 204111689U
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- CN
- China
- Prior art keywords
- control valve
- selective hydrogenation
- pipeline
- interchanger
- flow control
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 23
- 239000001257 hydrogen Substances 0.000 claims abstract description 33
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 33
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 150000001336 alkenes Chemical class 0.000 claims abstract description 19
- 238000000605 extraction Methods 0.000 claims abstract description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 11
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims description 20
- 238000004519 manufacturing process Methods 0.000 claims description 9
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 8
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 8
- 239000004571 lime Substances 0.000 claims description 8
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 6
- 239000010962 carbon steel Substances 0.000 claims description 6
- 239000012809 cooling fluid Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 10
- 238000003912 environmental pollution Methods 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000002407 reforming Methods 0.000 abstract description 2
- 238000003795 desorption Methods 0.000 abstract 3
- 239000000047 product Substances 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 241000196324 Embryophyta Species 0.000 description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 6
- 240000006909 Tilia x europaea Species 0.000 description 6
- 150000002431 hydrogen Chemical class 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000004927 clay Substances 0.000 description 3
- 229910052763 palladium Inorganic materials 0.000 description 3
- 238000004061 bleaching Methods 0.000 description 2
- 238000001833 catalytic reforming Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 231100001010 corrosive Toxicity 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a selective hydrogenation device relates to petrochemical equipment field, selective hydrogenation device sets up between reforming unit and extraction device for the trace alkene that contains in the desorption arene, selective hydrogenation device includes: the system comprises a buffer tank, a first pressure control valve, a nitrogen delivery pipe, a second pressure control valve, a pump, a first flow control valve, a heat exchanger, a heater, a reactor, a second flow control valve, a liquid cooler, a product separation tank, a liquid level control valve, a third flow control valve, a fourth flow control valve, a hydrogen delivery pipe and a fifth flow control valve; through using the utility model discloses carry out selective hydrogenation technology, the alkene in the desorption C6C 7 component, owing to this technology need not to use carclazyte desorption alkene, so practiced thrift the resource, reduced useless carclazyte processing procedure, reduced environmental pollution, alleviateed operating personnel intensity of labour.
Description
Technical field
The utility model relates to field of petrochemical industrial, particularly a kind of selective hydrogenation device.
Background technology
Naphtha fraction is after catalytic reforming, and it generates in oil and is rich in aromatic hydrocarbons and spirit fraction, simultaneously also containing a small amount of alkene.The unstable chemcial property of alkene, its existence can cause the off quality of the aromatic hydrocarbon product produced, and therefore produces the problem being all faced with in the process of aromatic hydrocarbons and removing alkene.
Now generally adopt the exquisite technique of carclazyte to remove alkene, namely naphtha fraction enters Clay Refining Unit after reformer catalytic reforming, by entering extraction plant extracting after carclazyte delicate instruments adsorbs olefins.
Contriver is realizing in process of the present utility model, finds that prior art at least exists following problem:
Under existing processing condition, along with the expansion of reformer scale, carclazyte is changed more frequent, not only need to consume a large amount of carclazytes, and discarded carclazyte also can cause serious environmental pollution, also add the labour intensity of operator, in addition simultaneously, because carclazyte can not regenerate and reuse, also result in the waste of resource.
Utility model content
In order to solve the problem that prior art utilizes the exquisite technique of carclazyte to remove alkene to there is contaminate environment, increase labor intensity of operating staff and waste resource, the utility model embodiment provides a kind of selective hydrogenation device, and described technical scheme is as follows:
A kind of selective hydrogenation device, be arranged between reformer and extraction plant, for the trace amounts of olefin contained in Arene removal, described selective hydrogenation device comprises: surge tank, the first pressure controlled valve, nitrogen transfer lime, the second pressure controlled valve, pump, first flow control valve, interchanger, well heater, reactor, second control valve, liquid cooling appts, product separation tank, level control valve, the 3rd flowrate control valve, the 4th flowrate control valve, hydrogen delivery tube and the 5th flowrate control valve;
Described reformer is connected with described surge tank through pipeline, described surge tank is connected with described pump through pipeline, described pump is connected with described interchanger shell through described first flow control valve, described interchanger shell is connected with described well heater shell through pipeline, described well heater shell is connected with described reactor through described second control valve, described reactor is connected with described interchanger tube layer through pipeline, described interchanger tube layer is connected with described liquid cooling appts tube layer through pipeline, described liquid cooling appts tube layer is connected with described product separation tank through pipeline, the lower part outlet of described product separation tank is connected with described extraction plant through described level control valve and the 3rd flowrate control valve, the upper outlet of described product separation tank is connected with described hydrogen delivery tube through the 4th flowrate control valve,
Described hydrogen delivery tube is connected on the pipeline between described pump and described first flow control valve through described 5th flowrate control valve;
Described nitrogen transfer lime is connected to described surge tank upper outlet place through described first pressure controlled valve, and described second pressure controlled valve is arranged at described surge tank upper outlet place.
Particularly, the cooling fluid in described liquid cooling appts is water.
Particularly, described surge tank, described pump, described interchanger, described well heater, described reactor, described liquid cooling appts, described product separation tank, the described first to the 5th flowrate control valve, described first pressure controlled valve, described second pressure controlled valve, described level control valve all adopt carbon steel manufacture.
The beneficial effect that the technical scheme that the utility model embodiment provides is brought is:
By using the utility model to carry out selective hydrogenation technique, remove the alkene in C6/C7 component, because this technique removes alkene without the need to using carclazyte, so saved resource, decrease spent bleaching clay treatment scheme, reduce environmental pollution, alleviate labor intensity of operating staff.In addition, C6/C7 component before the utility model reaction and the mixture of hydrogen are by the shell of interchanger, resultant and excessive hydrogen are by the tube layer of interchanger, resultant and the mixture of excessive hydrogen to the C6/C7 component before reaction and hydrogen is utilized to heat, by the recycle of heat energy, reduce production cost.
Accompanying drawing explanation
In order to be illustrated more clearly in the technical scheme in the utility model embodiment, below the accompanying drawing used required in describing embodiment is briefly described, apparently, accompanying drawing in the following describes is only embodiments more of the present utility model, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
Fig. 1 is the structural representation of the selective hydrogenation device that the utility model embodiment provides.
Wherein: 1 reformer, 2 surge tanks, 3 pumps, 4 first flow control valves, 5 interchanger, 6 well heaters, 7 reactors, 8 second control valves, 9 liquid cooling appts, 10 product separation tanks, 11 level control valves, 12 the 3rd flowrate control valves, 13 extraction plants, 14 the 4th flowrate control valves, 15 hydrogen delivery tube, 16 the 5th flowrate control valves, 17 first pressure controlled valves, 18 second pressure controlled valves, 19 nitrogen transfer limes.
Embodiment
For making the purpose of this utility model, technical scheme and advantage clearly, below in conjunction with accompanying drawing, the utility model embodiment is described in further detail.
As shown in Figure 1, the utility model embodiment provides a kind of selective hydrogenation device, be arranged between reformer 1 and extraction plant 13, for the trace amounts of olefin contained in Arene removal, described selective hydrogenation device comprises: surge tank 2, first pressure controlled valve 17, nitrogen transfer lime 19, second pressure controlled valve 18, pump 3, first flow control valve 4, interchanger 5, well heater 6, reactor 7, second control valve 8, liquid cooling appts 9, product separation tank 10, level control valve 11, 3rd flowrate control valve 12, 4th flowrate control valve 14, hydrogen delivery tube 15 and the 5th flowrate control valve 16,
Described reformer 1 is connected with described surge tank 2 through pipeline, described surge tank 2 is connected with described pump 3 through pipeline, described pump 3 is connected with described interchanger 5 shell through described first flow control valve 4, described interchanger 5 shell is connected with described well heater 6 shell through pipeline, described well heater 6 shell is connected with described reactor 7 through described second control valve 8, described reactor 7 is connected with described interchanger 5 tube layer through pipeline, described interchanger 5 tube layer is connected with described liquid cooling appts 9 tube layer through pipeline, described liquid cooling appts 9 tube layer is connected with described product separation tank 10 through pipeline, the lower part outlet of described product separation tank 10 is connected with described extraction plant 13 through described level control valve 11 and described 3rd flowrate control valve 12, the upper outlet of described product separation tank 10 is connected with described hydrogen delivery tube 15 through described 4th flowrate control valve 14,
Described hydrogen delivery tube 15 is connected on the pipeline between described pump 3 and described first flow control valve 4 through described 5th flowrate control valve 16;
Described nitrogen transfer lime 19 is connected to described surge tank 2 upper outlet place through described first pressure controlled valve 17, and described second pressure controlled valve 18 is arranged at described surge tank 2 upper outlet place.
Principle of work of the present utility model is as follows:
The C6/C7 component of the reformed oil of reformer unit 1 enters surge tank 2 by pipeline, store in surge tank 2, when the pressure in surge tank 2 is less, the first pressure controlled valve 17 is opened, and nitrogen supplements nitrogen by nitrogen transfer lime 19 and increases pressure in surge tank 2, when the pressure in surge tank 2 is larger, second pressure controlled valve 18 is opened, the gas go out C6/C7 component volatilization in surge tank 2 and air are wherein discharged, ensure that in reaction process, C6/C7 composition flow rate is steady, C6/C7 component from surge tank 2 out after enter pump 3 through pipeline, boost to guarantee that the pressure of C6/C7 component meets the pressure conditions of selective hydrogenation by pump 3, first its flow is regulated through first flow control valve 4 by the C6/C7 component after pump 3 boosts, mix with the hydrogen of coming in hydrogen delivery tube 15 again, its flow is controlled by the 5th flowrate control valve 16 by the hydrogen come in hydrogen delivery tube 15, guarantee that the hydrogen entered in reactor 7 is excessive, enter well heater 6 shell after the mixture of C6/C7 component and hydrogen is tentatively heated by the shell of interchanger 5 to heat, the high temperature fluid of flowing is provided with in the tube layer of well heater 6, as water vapour etc., by heating, guarantee that the temperature of the mixture of C6/C7 component and hydrogen meets the temperature condition of selective hydrogenation, meet the C6/C7 component of the condition of selective hydrogenation and the mixture of hydrogen to be regulated after its flow through second control valve 8 again by well heater 6 shell and enter reactor 7, guarantee response capacity and the flows match of the alkene entered in the C6/C7 component in reactor 7, palladium system catalyst converter is placed with in reactor 7, palladium system catalyst converter can suppress the reaction of aromatic hydrocarbons and hydrogen but can promote the reaction of alkene and hydrogen, the resultant reacted and excessive hydrogen enter interchanger 5 tube layer through pipeline, tentatively heat through the C6/C7 component of interchanger 5 shell and the mixture of hydrogen, and reduce the temperature of self, liquid cooling appts 9 tube layer is entered through pipeline from interchanger 5 tube layer resultant out and excessive hydrogen, by entering product separation tank 10 through pipeline after the cooling of liquid cooling appts 9 tube layer, wherein excessive hydrogen gets back to hydrogen delivery tube 15 by the upper outlet of product separation tank 10 and the 4th flowrate control valve 14, extraction plant 13 is entered after entering level control valve 11 and the 3rd flowrate control valve 12 by the lower part outlet of product separation tank 10 in resultant, guarantee that the flow of the resultant entering extraction plant 13 meets production requirement.
Oily C6/C7 component inlet amount is generated for 107143kg/h to reform, reforming and generating oily C6/C7 component inlet amount is 107143kg/h, and wherein, the massfraction of C6/C7 alkane is 28.75%, the massfraction of C6/C7 alkene is 4.3%, the massfraction of benzene is 18.33%, and the massfraction of toluene is 48.62%, temperature of reaction 170 DEG C, reaction pressure 1.7MPa (g), air speed 4/h, hydrogen to oil volume ratio 300, selects the palladium system catalyst converter of bar shaped.After process for selective hydrogenation of the present utility model, product bromine index is far below 100mgBr/100g charging, and aromatic hydrocarbons loss is far below 0.5%.For 2,200,000 tons/year of continuous reformers 1, need granular carclazyte 400m3 every year, production cost about 7,000,000 yuan, selective hydrogenation technique is carried out by using the utility model, remove the alkene in C6/C7 component, because this technique removes alkene without the need to using carclazyte, so saved resource, decrease the treatment scheme of spent bleaching clay, reduce environmental pollution, alleviate labor intensity of operating staff, in addition, because the mixture of C6/C7 component of the present utility model and hydrogen is by the shell of interchanger 5, resultant and excessive hydrogen are through the tube layer of interchanger 5, resultant is utilized to heat reactant, reduce production cost.
Preferably, in the utility model embodiment, the cooling fluid in described liquid cooling appts 9 is water.Cooling liquid flowing, through liquid cooling appts 9, is lowered the temperature to the resultant of its internal flow, and selectively, in the utility model embodiment, cooling fluid also may be selected to be the larger liquid of other specific heat capacities.
Preferably, in the utility model embodiment, described surge tank 2, described pump 3, described interchanger 5, described well heater 6, described reactor 7, described liquid cooling appts 9, described product separation tank 10, the described first to the 5th flowrate control valve 16, described first pressure controlled valve 17, described second pressure controlled valve 18, described level control valve 11 all adopt carbon steel manufacture.Because temperature of reaction is below 200 DEG C, pressure lower than 1.8MPa, and does not contain any corrosives in reaction, therefore use carbon steel material manufacture to meet the demands, and carbon steel is easy to buying, manufactures, construction, cheap, adopting carbon steel, to manufacture the utility model cost lower, and the engineering construction cycle is short.
The foregoing is only preferred embodiment of the present utility model, not in order to limit the utility model, all within spirit of the present utility model and principle, any amendment done, equivalent replacement, improvement etc., all should be included within protection domain of the present utility model.
Claims (3)
1. a selective hydrogenation device, be arranged between reformer and extraction plant, for the trace amounts of olefin contained in Arene removal, it is characterized in that, described selective hydrogenation device comprises: surge tank, the first pressure controlled valve, nitrogen transfer lime, the second pressure controlled valve, pump, first flow control valve, interchanger, well heater, reactor, second control valve, liquid cooling appts, product separation tank, level control valve, the 3rd flowrate control valve, the 4th flowrate control valve, hydrogen delivery tube and the 5th flowrate control valve;
Described reformer is connected with described surge tank through pipeline, described surge tank is connected with described pump through pipeline, described pump is connected with described interchanger shell through described first flow control valve, described interchanger shell is connected with described well heater shell through pipeline, described well heater shell is connected with described reactor through described second control valve, described reactor is connected with described interchanger tube layer through pipeline, described interchanger tube layer is connected with described liquid cooling appts tube layer through pipeline, described liquid cooling appts tube layer is connected with described product separation tank through pipeline, the lower part outlet of described product separation tank is connected with described extraction plant through described level control valve and the 3rd flowrate control valve, the upper outlet of described product separation tank is connected with described hydrogen delivery tube through the 4th flowrate control valve,
Described hydrogen delivery tube is connected on the pipeline between described pump and described first flow control valve through described 5th flowrate control valve;
Described nitrogen transfer lime is connected to described surge tank upper outlet place through described first pressure controlled valve, and described second pressure controlled valve is arranged at described surge tank upper outlet place.
2. selective hydrogenation device according to claim 1, is characterized in that, the cooling fluid in described liquid cooling appts is water.
3. selective hydrogenation device according to claim 1 and 2, it is characterized in that, described surge tank, described pump, described interchanger, described well heater, described reactor, described liquid cooling appts, described product separation tank, the described first to the 5th flowrate control valve, described first pressure controlled valve, described second pressure controlled valve and described level control valve all adopt carbon steel manufacture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420469312.2U CN204111689U (en) | 2014-08-19 | 2014-08-19 | Selective hydrogenation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420469312.2U CN204111689U (en) | 2014-08-19 | 2014-08-19 | Selective hydrogenation device |
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| Publication Number | Publication Date |
|---|---|
| CN204111689U true CN204111689U (en) | 2015-01-21 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201420469312.2U Expired - Fee Related CN204111689U (en) | 2014-08-19 | 2014-08-19 | Selective hydrogenation device |
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| Country | Link |
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| CN (1) | CN204111689U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106566581A (en) * | 2016-10-27 | 2017-04-19 | 王延睿 | Simulation test device and method |
-
2014
- 2014-08-19 CN CN201420469312.2U patent/CN204111689U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106566581A (en) * | 2016-10-27 | 2017-04-19 | 王延睿 | Simulation test device and method |
| CN106566581B (en) * | 2016-10-27 | 2017-11-07 | 王延睿 | A kind of analogue experiment installation |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100007 Dongcheng District, Dongzhimen, China, North Street, No. 9 Oil Mansion, No. Patentee after: PetroChina Company Limited Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Address before: 100007 Dongcheng District, Dongzhimen, China, North Street, No. 9 Oil Mansion, No. Patentee before: PetroChina Company Limited Patentee before: China Petroleum Engineering & Construction Corp. |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20190531 Address after: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Co-patentee after: CNPC EAST CHINA DESIGN INSTITUTE CO.,LTD. Patentee after: PetroChina Company Limited Address before: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Co-patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee before: PetroChina Company Limited |
|
| TR01 | Transfer of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150121 |
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| CF01 | Termination of patent right due to non-payment of annual fee |