CN204676038U - A kind of C5 the refining system of C6 isomerate feeds - Google Patents
A kind of C5 the refining system of C6 isomerate feeds Download PDFInfo
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- CN204676038U CN204676038U CN201520349287.9U CN201520349287U CN204676038U CN 204676038 U CN204676038 U CN 204676038U CN 201520349287 U CN201520349287 U CN 201520349287U CN 204676038 U CN204676038 U CN 204676038U
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Abstract
The utility model be a kind of C5 the refining system of C6 isomerate feeds, comprise separation column, dehydration facility and fixed-bed reactor ABC.First raw material enters the cutting that separation column carries out isomerate feeds component, tower top obtains suitable isomerization reaction feed composition and introduces dehydration facility, water-content in raw material is taken off to≤10ppm, then introduce fixed-bed reactor A/B/C, the sulphur in raw material and nitrogen content are removed to≤0.1ppm.The utility model can by C5 sulphur in C6 isomerization reaction raw material and nitrogen content is reduced to≤0.1ppm, water-content is reduced to≤10ppm, solve the problem lost efficacy when sweetening agent is different with denitrfying agent in common process simultaneously, extend catalyst change time and on-stream time, raw material that is slightly high for sulphur nitrogen content and height fluctuation can both process up to standard simultaneously, given full play to sweetening agent and denitrfying agent activity separately in addition, economy is better.
Description
Technical field
The utility model relates to a kind of refining system of isomerate feeds, be particularly useful for C5 the treating process of C6 isomerization reaction raw material.
Background technology
Carry out the light naphthar after refining primarily of C5, C6 component composition from continuous reformer, wherein straight-chain paraffin account for major part, and octane value is low, is generally between 60 ~ 68, changes straight-chain paraffin into isoparaffin by isomerization, can improve octane value.The isomerization reaction of C5, C6 normal paraffin is under hydro condition, contacts occurred Structural Isomerismization react with the strongly acidic catalyst of platiniferous (palladium), and the octane value of light naphthar can improve more than 10 units, meets full factory gasoline and to dispatch from the factory requirement.
Catalyzer due to isomerization unit is noble metal catalyst, therefore require harsh to the sulphur in its charging, nitrogen, water-content, namely organosulfur nitrogen and inorganic sulfur nitrogen all require to be less than 0.1wppm, water-content is lower than 10ppm, inorganic sulfur nitrogen in light naphthar at present after reformed pre-hydrogenated (C5 C6) cannot meet the requirement being less than 0.1wppm, water-content also cannot meet, therefore need to enter isomerized raw material refine (fine de-sulfur, smart denitrogenation and essence dehydration) process after, reaching requirement can carry out isomerization reaction device.
CN101972638A discloses a kind of oil fuel deep denitrification method, previously prepared good denitrification adsorbent joins by the method to be needed in the oil fuel of denitrogenation, react 0.5 ~ 6 hour under 20 ~ 90 DEG C of conditions, filtration is gone out denitrification adsorbent and is obtained advanced nitrogen oil fuel, and denitrification adsorbent in atmosphere thermal regeneration Posterior circle uses.This denitrification adsorbent and denitrogenation method can realize advanced nitrogen, and reaction conditions also compares mitigation, but need due to sorbent material and oil fuel carries out Forced Mixing and reaction, there is sorbent material and remain in problem in oil fuel, filtering system also more complicated in addition.
CN202962436U proposes adsorpting desulfurization device always, for adopting the S-Zorb adsorption desulfurize technology of sorbent material, sorbent material wherein mainly plays the reaction of sulphur and the function of storage, by reaction, the sulphur in hydrocarbon stream is stored on the sorbent, then deviate from by regenerative response the sulphur one that sorbent material stores and reply the desulphurizing activated of sorbent material, this adsorpting desulfurization device comprises adsorption desulfurize reactive system, sampling system and testing and analysis system.The method is mainly used in the degree of depth and deviates from sulfide in hydrocarbon oil, whole absorption and regenerative response system process more complicated, sorbent material is also special, is suitable for the situation that sulfide content is higher, and seems that economy is poor for low-down for sulphur content level being reduced to lower level.
Summary of the invention
For the deficiencies in the prior art, the utility model provide a kind of C5 the refining system of C6 isomerization reaction raw material, this system can by C5 sulphur in C6 isomerization reaction raw material and nitrogen content is reduced to≤0.1ppm, water-content is reduced to≤10ppm.
C5 of the present utility model the refining system of C6 isomerization reaction raw material, comprise separation column, dehydration facility and fixed-bed reactor A B C, fractionation tower top arranges feedstream outlet, be connected with dehydration facility feed(raw material)inlet by pipeline, dehydration facility material outlet through pipeline and fixed-bed reactor A B the feed(raw material)inlet of C be connected, fixed-bed reactor A exports the entrance through pipeline and fixed-bed reactor B, the total discharge port of raw material is connected respectively, fixed-bed reactor B exports the entrance through pipeline and fixed-bed reactor C, the total discharge port of raw material is connected respectively, fixed-bed reactor C outlet is connected respectively through the total discharge port of pipeline and raw material.
The working process of the utility model system is as follows: first raw material enters the cutting that separation column carries out isomerate feeds component, tower top obtain suitable C5 C6 isomerization reaction feed composition, dehydration facility introduced by fractionation tower top raw material, by C5 water-content in C6 isomerization reaction raw material take off to≤10ppm, the material being stripped of moisture enters fixed-bed reactor A/B/C, by C5 sulphur in C6 isomerization reaction raw material and nitrogen content be removed to≤0.1ppm.
In the fixed-bed reactor A/B/C of native system, A is main denitrification reactor, B is main desulphurization reactor, C is supplementary treatment reactor, the operating method of three row reactors and technical process can be selected flexibly according to sulphur, nitrogen height and the situation that removes in raw material, working method is as follows: (1) goes into operation the initial stage: if the nitrogen content in raw material is higher than sulphur content, isomerate feeds enters reactor A; If the sulphur content in raw material is higher than nitrogen content, isomerate feeds enters reactor B; If the nitrogen content in raw material is suitable with sulphur content, isomerate feeds enters reactor C; (2) go into operation mid-term: if the nitrogen content in raw material is higher than sulphur content, adopt reactor A+C series system to carry out; If the sulphur content in raw material is higher than nitrogen content, reactor B+C series system is adopted to carry out; If the nitrogen content in raw material is suitable with sulphur content, the mode of reactor A+C or B+C is adopted to carry out; (3) go into operation latter stage: adopt the mode of reactor A+B+C series connection to carry out.
In the utility model, separation column is a common fillers tower structure, tower top be C5 C6 component, feed component is light naphthar, ratio≤10% of below C4 (containing C4) component concentration in total overhead product in the tower top isomerization reaction raw material that separation column obtains, ratio≤10% of more than C7 (containing C7) component concentration in total overhead product.
In the utility model, the container that isomerization reaction raw material dehydration facility can adopt electrical dehydrator, oily water separation filler is equipped with in inside and coalescer structure etc.
In the utility model, fixed-bed reactor A is main denitrification reactor, inner filling denitrification adsorbent and desulfuration adsorbent, and wherein denitrification adsorbent loadings is 2 ~ 10 times of desulfuration adsorbent; Fixed-bed reactor B is main desulphurization reactor, inner filling denitrification adsorbent and desulfuration adsorbent, and wherein desulfuration adsorbent loadings is 2 ~ 10 times of denitrification adsorbent; Fixed-bed reactor C is for supplementing treatment reactor, and composite desulfate denitrification adsorbent is loaded in inside.
In the utility model, described adsorption desulfurizing agent can adopt conventional absorbtion sweetening agent in the art, as being Zinc oxide desulfurizer.
In the utility model, described adsorption denitrifier comprises always or multiple porous acid material usually, as molecular sieve component or unformed acidic components.Described molecular sieve generally comprise X-type, Y type, β, SAPO series, MCM-41, ZSM-5, L-type, ZSM-22, ZSM-23 and EU-1 equimolecular sieve one or more.Described unformed acidic components are generally one or more in amorphous silicon aluminium, unformed silicon magnesium and clay.
In the utility model, the making method of described composite desulfate denitrfying agent is as follows: sweetening agent is made up of alkaline agent 3 ~ 20%, complexing agent 2 ~ 20%, support powder 60 ~ 90%, water 5 ~ 20%, denitrfying agent has acidizer 3 ~ 20%, complexing agent 2 ~ 20%, support powder 60 ~ 90%, water 5 ~ 20% to form, and obtains the agent of solid absorption desulfurization removing nitric after above-mentioned each component mixing moulding.
In the utility model, fixed-bed reactor A/B/C includes reactor, feed-pipe, inlet control valve, discharge nozzle and discharging control valve; By inlet control valve and discharging control valve, the array mode to reactor adjusts.
In the utility model, fixed bed A B the operational condition of C be: temperature of reaction is 10 ~ 230 DEG C, and volume space velocity is 0.5h
-1~ 1.0h
-1, working pressure is 0 ~ 10MPa.
The refining system of C5 C6 isomerization reaction raw material of the present utility model, tool has the following advantages:
(1) C5 that can process in C6 isomerate feeds sulphur and nitrogen content scope wide, raw material that is slightly high for sulphur nitrogen content and height fluctuation can both process up to standard;
(2) solve the problem lost efficacy when sweetening agent is different with denitrfying agent in common process, extend catalyst change time and on-stream time;
(3) by adjusting the operation of native system, with petroleum naphtha production fractionating system and the synchronous start-stop of isomerization reaction device below synchronous, and adapt to go into operation in earlier stage, the difference in mid-term and latter stage goes into operation demands;
(4) given full play to sweetening agent and denitrfying agent activity separately, economy is better.
Accompanying drawing explanation
Fig. 1 be C5 of the present utility model the refining system structural representation of C6 isomerization reaction raw material.
Wherein: 1-petroleum naphtha source pipeline, 2-separation column, discharging pipeline at the bottom of 3-separation column tower, 4-fractionator overhead discharging pipeline, 5-dewaters facility, the main denitrification reactor of 6-fixed-bed reactor A(), the main desulphurization reactor of 7-fixed-bed reactor B(), 8-fixed-bed reactor C(supplements treatment reactor), 9-dehydration facility exit material pipeline, 10-fixed-bed reactor A feeding pipe, 11-fixed-bed reactor B feeding pipe, 12-fixed-bed reactor C feeding pipe, 13-sweetening agent, 14-denitrfying agent, 15-sweetening agent, 16-denitrfying agent, 17-Composite denitrification sweetening agent, 18-fixed-bed reactor A discharging pipeline, 19-fixed-bed reactor B discharging pipeline, 20-fixed-bed reactor C discharging pipeline, the total discharging pipeline of 21-.
Embodiment
Structure and the using method of the utility model device is further illustrated below in conjunction with accompanying drawing.
A kind of C5 of the utility model the refining system of C6 isomerization reaction raw material, for dewatering to the raw material of isomerization unit, denitrogenation and desulfurization process, carry out in the following manner: cerebrol enters the middle part of separation column 2 through raw material sources pipeline 1, tower top heavy constituent 3 is discharged by the road, tower top C5 C6 light constituent and isomerate feeds enter dehydration facility 5 via pipeline 4; C5 C6 isomerate feeds through dewater qualified after, product enters fixed-bed reactor by the facility discharging pipeline that dewaters, and the moisture removed is discharged by pipeline 22; The isomerate feeds of autospasy hydration lattice, enters the top of fixed-bed reactor A 6 via feed-pipe 10, successively through sweetening agent bed 13 and denitrfying agent bed 14, draw from bottom discharge pipe 18; Material through fixed-bed reactor A extraction can enter the top of fixed-bed reactor B 7, also can enter the top of fixed-bed reactor C8, can also directly draw through total discharge nozzle 21; Material through fixed-bed reactor B extraction can enter the top of fixed-bed reactor C8, also can directly draw through total discharge nozzle 21; The material of drawing through fixed-bed reactor C is directly drawn via total discharge nozzle 21.
In the utility model, the denitrfying agent that fixed-bed reactor A loads is 2 times of sweetening agent, and the sweetening agent that fixed-bed reactor B loads is 2 times of denitrfying agent, and the Composite denitrification sweetening agent that fixed-bed reactor C loads is the summation of sweetening agent and denitrfying agent in reactor A.
Below in conjunction with embodiment for C5 described in the utility model the result of use of refining system of C6 isomerization reaction raw material further illustrate, but not by the restriction of following embodiment.
Comparative example 1
Petroleum naphtha is after separation column fractionation, tower top obtains C5/C6 isomerate feeds, nitrogen content in this raw material is 0.45wppm, and sulphur content is 0.15wppm, and this raw material is introduced common fixed bed denitrification reactor and desulphurization reactor, specification is φ 100 × 450mm, denitrfying agent is loaded in denitrification reactor inside, and sweetening agent is loaded in desulphurization reactor inside, and temperature of reaction is 40 DEG C, reaction pressure is 1.0MPa, and volume space velocity is 0.8h
-1.After this method reaction, within 720 hours, in nitrogen and desulfurization reactor outlet material, sulphur and nitrogen content are all less than 0.1wppm; Nitrogen content after reaction in 720 hours in nitrogen and desulfurization reactor outlet material starts higher than 0.1wppm, and sulphur content is qualified; Again after 250 hours, the nitrogen in nitrogen and desulfurization reactor outlet material and sulphur content all start higher than 0.1wppm, and namely aforesaid method can only be maintain certain desulfurization and denitrification percent in the short period of time.
Embodiment 1
Embodiment adopts the technical scheme of native system: petroleum naphtha is after separation column fractionation, tower top obtains C5/C6 isomerate feeds, nitrogen content in this raw material is 0.4wppm, sulphur content is 0.2wppm, this raw material is introduced fixed-bed reactor ABC, and specification is φ 80 × 400mm, and the denitrfying agent that fixed-bed reactor A loads inside is 2 times of sweetening agent, the sweetening agent that fixed-bed reactor B loads inside is 2 times of denitrfying agent, loads Composite denitrification sweetening agent in fixed-bed reactor C.Temperature of reaction is 40 DEG C, and reaction pressure is 1.0MPa, and volume space velocity is 0.8h
-1.After the fixed bed A of this method reacts, within 1000 hours, in reactor outlet material, sulphur and nitrogen content are all less than 0.1wppm; Nitrogen content again after fixed bed A+C reacts again after reaction in 1500 hours in fixed-bed reactor outlet material starts higher than 0.1wppm.
Embodiment 2
Embodiment adopts the technical scheme of native system: petroleum naphtha is after separation column fractionation, tower top obtains C5/C6 isomerate feeds, nitrogen content in this raw material is 0.3wppm, sulphur content is 0.3wppm, this raw material is introduced fixed-bed reactor ABC, and specification is φ 80 × 400mm, and the denitrfying agent that fixed-bed reactor A loads inside is 2 times of sweetening agent, the sweetening agent that fixed-bed reactor B loads inside is 2 times of denitrfying agent, loads Composite denitrification sweetening agent in fixed-bed reactor C.Temperature of reaction is 40 DEG C, and reaction pressure is 1.0MPa, and volume space velocity is 0.8h
-1.After the fixed bed A of this method reacts, within 1450 hours, in reactor outlet material, sulphur and nitrogen content are all less than 0.1 wppm; Again after fixed bed A+C reacts, the nitrogen content within 1200 hours in fixed-bed reactor outlet material is all less than 0.1 wppm; Again after fixed bed B+C reacts, the nitrogen content within 1200 hours in fixed-bed reactor outlet material is all less than 0.1wppm; Again after fixed bed A+B+C reacts, the nitrogen content within 1600 hours in fixed-bed reactor outlet material is all less than 0.1 wppm.
Claims (9)
1. the refining system of a C5 C6 isomerization reaction raw material, it is characterized in that: comprise separation column, dehydration facility and fixed-bed reactor A B C, fractionation tower top arranges feedstream outlet, be connected with dehydration facility feed(raw material)inlet by pipeline, dehydration facility material outlet through pipeline and fixed-bed reactor A B the feed(raw material)inlet of C be connected, fixed-bed reactor A exports the entrance through pipeline and fixed-bed reactor B, the total discharge port of raw material is connected respectively, fixed-bed reactor B exports the entrance through pipeline and fixed-bed reactor C, the total discharge port of raw material is connected respectively, fixed-bed reactor C outlet is connected respectively through the total discharge port of pipeline and raw material.
2. according to refining system according to claim 1, it is characterized in that the working process of this system is as follows: first raw material enters the cutting that separation column carries out isomerate feeds component, tower top obtain suitable C5 C6 isomerization reaction feed composition, dehydration facility introduced by fractionation tower top raw material, by C5 water-content in C6 isomerization reaction raw material take off to≤10ppm, the material being stripped of moisture enters fixed-bed reactor A/B/C, by C5 sulphur in C6 isomerization reaction raw material and nitrogen content be removed to≤0.1ppm.
3. according to refining system according to claim 1, it is characterized in that: in fixed-bed reactor A/B/C, A is main denitrification reactor, B is main desulphurization reactor, C is supplementary treatment reactor.
4. according to the refining system described in claim 1 or 3, it is characterized in that: the working method of three row reactors is as follows: (1) goes into operation the initial stage: if the nitrogen content in raw material is higher than sulphur content, isomerate feeds enters reactor A; If the sulphur content in raw material is higher than nitrogen content, isomerate feeds enters reactor B; If the nitrogen content in raw material is suitable with sulphur content, isomerate feeds enters reactor C; (2) go into operation mid-term: if the nitrogen content in raw material is higher than sulphur content, adopt reactor A+C series system to carry out; If the sulphur content in raw material is higher than nitrogen content, reactor B+C series system is adopted to carry out; If the nitrogen content in raw material is suitable with sulphur content, the mode of reactor A+C or B+C is adopted to carry out; (3) go into operation latter stage: adopt the mode of reactor A+B+C series connection to carry out.
5. according to refining system according to claim 1, it is characterized in that: separation column is a common fillers tower structure, C4 and ratio≤10% of following component concentration in total overhead product in the tower top isomerization reaction raw material that separation column obtains, C7 and ratio≤10% of above component concentration in total overhead product.
6. according to refining system according to claim 1, it is characterized in that: isomerization reaction raw material dehydration facility adopts electrical dehydrator, wherein inner container and the coalescer structure that oily water separation filler is housed.
7. according to refining system according to claim 1, it is characterized in that: fixed-bed reactor A is main denitrification reactor, inner filling denitrification adsorbent and desulfuration adsorbent, wherein denitrification adsorbent loadings is 2 ~ 10 times of desulfuration adsorbent; Fixed-bed reactor B is main desulphurization reactor, inner filling denitrification adsorbent and desulfuration adsorbent, and wherein desulfuration adsorbent loadings is 2 ~ 10 times of denitrification adsorbent; Fixed-bed reactor C is for supplementing treatment reactor, and composite desulfate denitrification adsorbent is loaded in inside.
8. according to refining system according to claim 1, it is characterized in that: fixed-bed reactor A/B/C comprises reactor, feed-pipe, inlet control valve, discharge nozzle and discharging control valve; By inlet control valve and discharging control valve, the array mode to reactor adjusts.
9., according to refining system according to claim 1, it is characterized in that: fixed bed A B the operational condition of C be: temperature of reaction is 10 ~ 230 DEG C, and volume space velocity is 0.5h
-1~ 1.0h
-1, working pressure is 0 ~ 10MPa.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106675618A (en) * | 2015-11-11 | 2017-05-17 | 中国石油化工股份有限公司 | Sulfur and nitrogen homogenization system and treatment method of isomerization raw material |
| CN113956900A (en) * | 2021-11-04 | 2022-01-21 | 辽宁北方华锦五洲化工工程设计有限公司 | Based on C5C6Naphtha deep processing method and device for isomerization device |
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2015
- 2015-05-27 CN CN201520349287.9U patent/CN204676038U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106675618A (en) * | 2015-11-11 | 2017-05-17 | 中国石油化工股份有限公司 | Sulfur and nitrogen homogenization system and treatment method of isomerization raw material |
| CN106675618B (en) * | 2015-11-11 | 2018-04-10 | 中国石油化工股份有限公司 | A kind of processing method of sulphur nitrogen homogenization system and isomerate feeds |
| CN113956900A (en) * | 2021-11-04 | 2022-01-21 | 辽宁北方华锦五洲化工工程设计有限公司 | Based on C5C6Naphtha deep processing method and device for isomerization device |
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