Method for heterogeneous synthesis

专利摘要:
Improved process for heterogeneous synthesis and related reactors according to which the synthesis catalyst is distributed in three catalytic beds (C1, C22, C3) either axial-radial or radial, control of the temperature between beds being effected by means of fresh quench gas (4) between the first and the second bed and by means of indirect cooling with an exchanger (S2) between the second and the third bed of the gas leaving the second bed, using fresh gas which is heated inside the tubes of said exchanger.
公开号:SU1671148A3
申请号:SU884356145
申请日:1988-07-01
公开日:1991-08-15
发明作者:Зарди Умберто；Пагани Джорджо
申请人:Аммониа Казале С.А.(Фирма)；Умберто Зарди (Фирма)；
IPC主号:

专利说明:

The invention relates to the field of chemical technology and can be used for the production of ammonia, methanol and other products.
The purpose of the invention is to increase productivity and reduce energy consumption.
The drawing shows a cartridge of a synthesis reactor with three catalytic beds and an axial radial flow of gas.
Most of the feed gas stream 1 from the bottom of the reactor shell 2 passes from the bottom to the top along the air space between the shell 2 and the cartridge 3 and then goes to the outside of the heat exchanger 4 for preheating with hot gas leaving the reactor head ( stream 5).
The gas stream 6 thus preheated, whose temperature is controlled by part of the gas stream 7, is mixed with stream 8 preheated in the heat exchanger 9 and reaches the first catalytic layer, through which it passes through the axial-radial flow from the inside to the outside, the air space between the cartridge 3 and the outer wall 10 of the first catalytic layer, where it mixes with the fresh cooling gas flow 11 Gas mixed with the flow 12, which has a lower rate ture reaches the second catalytic bed through which it passes, to undergo a reaction and heating Referring axial-radial flow from the outside towards the inside of the bed is then hot gas
ABOUT
Vj
-N 00
I
I

with
is collected in the air space formed by the inner wall of the catalytic layer and the outer shell of the heat exchanger 9 located in the central part of the second catalytic layer, and is cooled, the passage from the upper part to the bottom outside the tubes of the heat exchanger 9, ultimately collecting at the outlet of the heat exchanger 9 to reach the entrance to the third catalytic layer (stream 13).
A stream of fresh gas is supplied to the bottom of the heat exchanger 9, through which it passes from inside the pipes, eventually connected to stream 6 and preheating it. Flow 13 flows through the axial-radial flow from the outside to the inside through the third catalytic base 14, collecting in the central manifold 15, from where it reaches the inside of the tubes of the heat exchanger 4 through the central displacement tube 16, where it is cooled, preheating the flow before finally leaves the converter, stream 5.
PRI me R. In the synthesis reactor for the production of 1000 Mt of ammonia, the pressure at the inlet of the reactor is 140 bar.
Flow
1 7 11
eight
c
Mark 11.8, pier

%
66.68
22.22
4.7
4.30
2.1
The composition of the stream 5, mol. %;
54.68 18.22 5.38 4.92
H2 N2
CH4
A nh3
16.80
five
0
five
0
five

权利要求:
Claims (2)
[1]
1. A method of heterogeneous synthesis in a reactor with three catalyst beds, which predominantly involves radial transmission of gas streams through catalyst beds with cooling gas leaving the catalyst bed, fresh gas, while cooling the gas leaving the first layer is carried out with a fresh gas flow, that, in order to increase productivity and reduce energy consumption, gas is passed through one catalyst bed in the direction from the inner side of the layer to its outer side, and through two x layer - in the direction from the outside layer to the inside thereof, wherein the cooling gas leaving the second catalyst layer is carried out by indirect cooling heat exchanger, the tube space which is fed a fresh gas.
[2]
2. A method according to claim 1, characterized in that the amount of fresh gas supplied to the cooling is at least 20% of the total amount of gas supplied, and the amount of gas supplied to the tube space of the heat exchanger is at least 20% total feed gas flow.

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同族专利:

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CA1306846C|1992-09-01|

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CN1030878A|1989-02-08|

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DE3869677D1|1992-05-07|

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ES2030467T3|1992-11-01|

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US4963338A|1990-10-16|

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EP0297474B1|1992-04-01|

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EP0297474A2|1989-01-04|

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法律状态:

优先权:

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申请号 | 申请日 | 专利标题

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CH252987|1987-07-03|

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