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Naphtha hydrogenation method and decoking tank

A process method and naphtha technology, applied in the fields of hydrotreating process, petroleum industry, separation method, etc., can solve the problems of complex process, coking can not play an effective role, etc., and achieve large deposition amount, simple structure, and not easy to clog Effect

Active Publication Date: 2012-10-17
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

US4,113,603 reports the use of a two-stage hydrorefining method to treat dienes and sulfides in pyrolysis gasoline. The first stage uses a nickel-tungsten catalyst to remove mercaptans, and the second stage uses a precious metal palladium catalyst to remove dienes. It is more complicated and cannot effectively play a role in coking due to factors other than dienes

Method used

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  • Naphtha hydrogenation method and decoking tank
  • Naphtha hydrogenation method and decoking tank
  • Naphtha hydrogenation method and decoking tank

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1 and comparative example 1

[0034] Coking naphtha hydrorefining process. Coked naphtha is mixed with hydrogen and heated to 230°C in a heating furnace, and then enters the decoking tank and then enters the hydrogenation reactor. The hydrogenation catalyst FH-40A is a commercial hydrogenation refining catalyst developed and produced by Sinopec Fushun Petrochemical Research Institute. The properties of raw materials are shown in Table 1, and the operating conditions and results are shown in Table 2. The difference of the comparative example is that no decoking tank is provided.

[0035] Table 1 Raw oil properties.

[0036] raw material coker naphtha Distillation range, ℃ 36～192 Sulfur, μg / g 4960 Nitrogen, μg / g 126 Bromine value, gBr / (100mL) 48

[0037] Table 2 Operating conditions and product properties.

[0038] Example 1 Comparative example 1 Reaction hydrogen pressure, MPa 4.0 4.0 Hydrogen oil volume ratio 800:1 800:1 volumet...

Embodiment 2 and comparative example 2

[0041] Catalytic cracking heavy naphtha selective hydrodesulfurization process. Catalytic cracking naphtha adopts commercial AFS-12 catalyst (produced by Petroleum University), at a pressure of 0.5MPa, a temperature of 35℃~45℃, and a volume space velocity of 2.0h -1 , Deodorization is carried out under the condition of gas-oil volume ratio (air / gasoline) 4:1. The deodorized product is subjected to fractionation, and the fractionation point is 70°C to obtain catalytically cracked heavy naphtha. The catalytically cracked heavy naphtha is mixed with hydrogen and heated to 250°C in a heating furnace, and then enters the decoking tank for decoking and then enters the hydrogenation reactor. Hydrogenation catalyst FGH-11 is a commercial selective hydrodesulfurization catalyst developed and produced by Sinopec Fushun Petrochemical Research Institute. The properties of raw materials are shown in Table 3, and the operating conditions and results are shown in Table 4. The difference of...

Embodiment 3 and comparative example 3

[0047] Pre-hydrogenation of straight-run naphtha provides feedstock for catalytic reforming. Straight-run naphtha is mixed with hydrogen and heated to 300°C in a heating furnace, and then enters the decoking tank for decoking and then enters the hydrogenation reactor. Hydrogenation catalyst FH-40C is a commercial hydrogenation refining catalyst developed and produced by Sinopec Fushun Petrochemical Research Institute. The properties of raw materials are shown in Table 5, and the operating conditions and results are shown in Table 6. The difference of the comparative example is that no decoking tank is provided.

[0048] Table 5 Main properties of straight-run naphtha.

[0049] raw material straight run naphtha source Blended Straight Run Naphtha Density (20℃), g / cm 3 0.7348 Sulfur content, μg / g 800 Nitrogen content, μg / g 2.8

[0050] Table 6 Operating conditions and results.

[0051] Process conditions Example 3 Com...

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Abstract

The invention discloses a naphtha hydrogenation method and a decoking tank. The naphtha hydrogenation method comprises the following steps of heating a mixture of a naphtha feedstock and hydrogen in a heating surface to a temperature required by hydrofining, then carrying out decoking by the decoking tank, and then feeding the decoked mixture into a fixed bed hydrogenation reactor. The decoking tank comprises a cylindrical body, an upper head, a lower head and a separator. The separator comprises a box plate and multiple separation pipe assemblies fixed to the box plate. The decoking tank is divided into two parts by the box plate, wherein one part is a channel for outflow of filtered materials and the other part is a coke deposition zone. Compared with the prior art, the naphtha hydrogenation method and the decoking tank can effectively and economically prolong a naphtha hydrogenation device running period.

Description

technical field [0001] The invention relates to a naphtha hydrogenation method and a decoking tank, in particular to a hydrogenation method for prolonging the operation period of a naphtha hydrogenation device and a decoking tank used in the method. Background technique [0002] Naphtha (that is, gasoline fraction) is an important gasoline raw material and chemical raw material, mainly used to produce various grades of gasoline fuel, catalytic reforming to produce aromatics (or high-octane gasoline blending components) raw materials, steam cracking or catalytic Cracking to produce ethylene, propylene, butene and other chemical raw materials, as well as raw materials for hydrogen production. Naphtha is generally derived from straight-run naphtha obtained from petroleum distillation, and naphtha obtained from secondary processing, such as coking naphtha, catalytic cracking naphtha, cracking naphtha, etc. The various uses of naphtha from various sources require deep removal of...

Claims

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Application Information

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IPC IPC(8): C10G67/14C10G75/00B01D45/04B01D46/24
Inventor 彭德强王岩齐慧敏刘杰李欣王明星姜阳
Owner CHINA PETROLEUM & CHEM CORP
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